Title of Invention	A RECOVERY AND PURIFICATION SYSTEM AND A PROCESS FOR RECYCLING A LIQUID MEDIUM
Abstract	A recycling and recovery system and process comprising a flash gas separator that receives a slurry comprising liquid medium and solid polymer particles. The flash gas separator separates the diluent from the solid polymer particles as a vapor stream comprising at least diluent and heavies. A line receives the vapor stream from the flash gas separator. The line leads to a heavies removal system that yields a liquid that is relatively concentrated in heavies and a diluent vapor that is relatively free of heavies. The liquid is passed to a heavies column, while the diluent vapor is passed to a diluent recycle chamber and then recycled to a slurry polymerization reactor without additional treatment to remove heavies. 617/CHENP/2005 ABSTRACT A RECOVERY AND PURIFICATION\|. SYSTEM AND A PRCOESS FOR RECYCLING A LIQUID MEDIUM A recycling and recovery system and process comprising a flash gas separator that receives a slurry comprising liquid medium and solid polymer particles. The flash gas separator separates the diluent from the solid polymer particles as a vapor stream comprising at least diluent and heavies. A line receives the vapor stream from the flash gas separator. The line leads to a heavies removal system that yields a liquid that is relatively concentrated in heavies and a diluent vapor that is relatively free of heavies. The Hquid is passed to a heavies column, while the diluent vapor is passed to a diluent recycle chamber and then recycled to a slurry polymerization reactor without additional treatment to remove heavies.

Title of Invention

A RECOVERY AND PURIFICATION SYSTEM AND A PROCESS FOR RECYCLING A LIQUID MEDIUM

Abstract

A recycling and recovery system and process comprising a flash gas separator that receives a slurry comprising liquid medium and solid polymer particles. The flash gas separator separates the diluent from the solid polymer particles as a vapor stream comprising at least diluent and heavies. A line receives the vapor stream from the flash gas separator. The line leads to a heavies removal system that yields a liquid that is relatively concentrated in heavies and a diluent vapor that is relatively free of heavies. The liquid is passed to a heavies column, while the diluent vapor is passed to a diluent recycle chamber and then recycled to a slurry polymerization reactor without additional treatment to remove heavies. 617/CHENP/2005 ABSTRACT A RECOVERY AND PURIFICATION|. SYSTEM AND A PRCOESS FOR RECYCLING A LIQUID MEDIUM A recycling and recovery system and process comprising a flash gas separator that receives a slurry comprising liquid medium and solid polymer particles. The flash gas separator separates the diluent from the solid polymer particles as a vapor stream comprising at least diluent and heavies. A line receives the vapor stream from the flash gas separator. The line leads to a heavies removal system that yields a liquid that is relatively concentrated in heavies and a diluent vapor that is relatively free of heavies. The Hquid is passed to a heavies column, while the diluent vapor is passed to a diluent recycle chamber and then recycled to a slurry polymerization reactor without additional treatment to remove heavies.

Full Text	FIELD OF THE INVENTION The present invention relates to a recovery and purification system for a liquid medium from a slurry polmerization. More particularly, the present invention relates to an olefin polymerization system and process that include an improved way of removing heavies from diluent and/or unreacted monomer withdrawn from and recycled to the polymerization reactor. The invention also relates to a process for recycling a liquid medium. BACKGROUND OF THE INVENTION Olefin polymerization processes may be conducted under slurry conditions. Such polymerization processes may be carried out in a loop reactor in which monomers are polymerized to form a slurry of solid polymer particles in a liquid medium. Portions of the slurry axe withdrawn from the loop reactor through take-offs devices such as settling legs and continuous take-offs. The slurry is then processed to separate the liquid medium (for example, a liquid diluent) from the solid polymer particles. Flashline heaters and flash chambers have been used to vaporize the liquid diluent though a combination of temperature and pressure adjustments, thereby separating the diluent from the solid polymer particles. Additionally, other types of equipment, such as purge columns, separating drums and cyclones, have been used for separation and other downstream treatment. Efficient slurry polymerization processes typically recycle as much diluent as they reasonably can. That is, as the diluent is vaporized, diluent is processed for recycling back to the loop reactor. As the liquid diluent is vaporized at various stages of the polymerization process after the slurry is withdrawn from the loop reactor, various compounds and contaminants may also be vaporized along with the diluent. "Heavies" are liquid components heavier than the diluent, and are often vaporized along with the diluent. During the recycling process, a vapor stream containing the diluent and heavies may be condensed and returned to the loop reactor as a recycle stream of the diluent and heavies. Heavies may concentrate or accumulate within the loop reactor and decrease reactor efficiency and/or cause damage within the loop reactor. For example, heavies buildup within the reactor may degrade product quality and/or distort reactor control making reactor problems and blockage more likely. Another recycling technique separates a slip stream comprising diluent and minor amounts of monomer from the bulk of the flashed fluid conqjonents. The slip stream is subjected to olefin removal to give an essentially olefin-free stream for recycle to a catalyst preparation area. The slip stream may be taken off before and/or after a diluent recycle cooler. The slip stream(s) is then passed to a heavies removal column. The heavies removal column removes heavies from the slip stream, which can then be used to prepare a catalyst mud or slurry. The bulk of monomer-containing recycle diluent is passed to a diluent recycle surge (storage) vessel, and a recycle stream is passed back to the reactor. If desired, other purification steps such as water removal can be carried out on this recycle stream. An efficient system and process of recycling diluent in a slurry polymerization process are desired. Furttier, an improved heavies removal system and process, which remove heavies from the diluent to be recycled to the reactor, are desired. BRIEF SUMMARY OF THE INVENTION As one aspect of the present invention, a process for recycling a liquid medium withdrawn from a slurry polymerization reactor is provided. The method comprises separating a first vapor stream from a slurry comprising a liquid medium and solid polymer particles, wherein the vapor stream comprises at least the medium and heavies. A first portion of the first vapor stream is passed to a first condensing zone, and a first portion of the first vapor stream is condensed to form a first liquid. A second portion of the first vtepor stream is passed to a collection zone without substantial condensation. A second liquid and a second vapor stream are separated in the collection zone. The second liquid is passed to a heavies purification zone, and the medium is recycled fi:om the second vapor stream without firactionating to remove heavies. As another aspect of the present invention, a recovery and purification system for a liquid medium fmm a slurry polymerization is provided. The system comprises a first fluid passage connected at one end to a slurry polymerization reactor and connected at an opposite end to a flash gas separator, for separating a vapor stream comprising the medium firom solid polymer particles. The system also comprises a vapor removal line coimected at a top portion of the flash gas separator, for transporting the vapor stream firom the flash gas separator. The vapor removal line is connected to a first condenser and also to a vapor bypass line that provides a bypass around the condenser. A bypass valve controls the flow of vapor through the vapor bypass line. The output of the condenser and the opposite end of the bypass line are both fluidly connected to a liquid collection tank. A liquid delivery line is at a bottom portion of the liquid collection tank, and a vapor recycle line is at a top portion of the liquid collection tank. A second condenser is fluidly connected to the vapor recycle line, and a second fluid passage connects the output of the second condenser to the slurry polymerization reactor. The present invention may include control apparatus or steps associated with the bypass valve. For example, the bypass valve can be in informational communication with at least one of a temperature controller downstream of the liquid collection tank and a level controller positioned within the liquid collection tank. The bypass line is advantageous because it is difBcult to operate a condenser to produce only a small amount of liquids. The present invention is able to produce a relatively small amount of liquids because the first vapor stream (which is the flash gas fi-om the first flash chamber) is spUt, with a first portion passing through a condenser and a second portion bypassing the condenser. The flash gas passing through the condenser may be entirely or nearly entirely condensed into liquid, or a small part (for example, about 1-10%) maybe condensed, or some other proportions. Downstream of the condenser, the hot flash gas is combined with the cold liquid and mixed and allowed to come to an equilibrium (at least with respect to temperature). After this mixing, the liquid that remains is more concentrated m the heavier components. The desired amount of liquid is set by the flow controller on the liquid line. The level in the tank is controlled by adjusting the temperature controller, which in turn adjusts the bypass valve so that a sufficient amount of vapor bypasses the condenser to generate enough liquid to satisfy the flow controller. To accomplish the desired amount of heavies removal, from about 0.1 to about 20% of the flash gas alternatively from about 0.5% to about 10%, alternatively from about 1% to about 5%, will be converted into liquids by the condenser. At times it may be desirable to collect no liquids. At other times (for example, during resin transitions), it may be desirable to maximize liquids generation and collect more than usual. The present invention may also include a heavies colunm or other heavies removal treatment at an opposite end of the heavies delivery line. A flow controller and/or a pump can be disposed along the heavies delivery line. A static mixer can be fluidly connected to and downstream from the first condenser, and the static mixer is upstream from and fluidly connected to the liquid collection tank. The static mixer is employed to quicken the formation of an equilibrium mixture after the hot flash gas and cold liquid are combined. It is desirable to have equilibrium conditions before entering the collection tank, at least a temperature equilibrium. A recycle tank may be disposed along the diluent recycle line dowmtream of the flash gas condenser. BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a r^resentation of a slurry polymerization system which includes a novel heavies removal system, FIG, 2 is a representation of the heavies condenser, static mixer, and liquid collection tank from the system of FIG. 1, as well as a novel control scheme. FIG. 3 is another representation of a slurry polymerization system which includes a novel heavies removal system. DETAILED DESCRIPTION OF THE INVENTION The present invention provides a diluent recovery and purification system and process for a slurry polymerization reactor, especially for a loop polymerization reactor. The system and process comprise a flash chamher or flash gas separator, a vapor removal line, a condenser, and a liquid collection tank. The flash chamber or flash gas separator receives a slurry withdrawn from a loop reactor. Diluent, unreacted monomer, and various heavies are separated from the solid polymer particles as a first vapor stream. The vapor removal line receives the first vapor stream and transfers a first portion to a condenser that condenses at least some of the first portion to form a first liquid. It may be a relatively small amount portion, for example, about 2% of the first vapor stream that is condensed. The second portion of the first vapor stream bypasses the condenser but is thereafter combined and mixed with the first liquid to form a combined stream. The combined stream is sent to a liquid collection tank. As the vapor and liquid mix in the mixing device and/or in the line to the liquid collection tank, some of the Uquid will be vaporized again, and the mixture may come to an equilibrium temperature. The combined stream will be cooled enough such that some liquid will be present. The liquid that collects in the Uquid coUection tank wiU have a higher concentration of the heavier compounds than the vapor leaving the collection tank. The liquid phase of an eqxiilibrium mixture will be richer in the heavier components than the vwpoT phase because the heavier components are less volatile. The Uquid containmg a higher concentration of the heavier components is passed from the Uquid collection tank to a heavies deUvery Une, and the vapor is passed to a diluait recycle line. The vapor may be passed to a second condenser and a recycle surge tank. The vapor from the Uquid collection tank can be condensed and recycled to the slurry polymerization reactor without further treatment to remove heavies. During the separating step, vapor comprising diluent, unreacted monomers/comonomers and various inerts, both heavier and lighter than the primary diluent (for example, isobutane), are separated. Various other compounds associated with the feedstocks and diluent feed, such as other compounds with 4 carbons (for example, n-butane) and compounds with six carbons (for example, n-hexane), are inerts, which do not polymerize and function as a diluent along with isobutane. Heavies include additional compounds with six carbons along with any heavier corapoxmds that may be produced in the reactor (such as oligomers). A portion of the v^or stream is then passed to a condenser in a heavies removal zone. The condenser may only condense a small portion of the stream or it may condense most or essentially all of the first portion. The liquid and vapor are then combined, which allows them to form a combined stream. The combined stream is passed to a liquid collection zone, and liquid and vapor are separated in the collection zone, after which the diluent vapor is passed to a diluent recycle line and the liquid is passed into a heavies delivery line. The diluent vapor separated from the liquid (that is, diluent vapor exiting from a top portion of the liquid collection tank) is suitable for recycling to the polymerization reactor. The diluent vapor is passed from the diluent recycle line to a diluent recycle tank. The diluent vapor is condensed by heat exchange. The diluent can then be recycled to the polymerization zone without having to remove additional heavies. Further, the liquid is passed from the heavies delivery line to a heavies column. The present invention is applicable to any olefin polymerization in a loop reactor utilizing a liquid medium so as to produce a fluid slurry of polymer solids in the liquid medium. Suitable olefin monomers include 1-olefins having up to 8 carbon atoms per molecule and no branching nearer the double bond than the 4-position. The present invention is particularly suitable for the homopolymerization of ethylene and copolymerization of ethylene and a higher 1-olefin such as butene, 1-pentene, 1-hexene, 1-octene or 1-decene. Suitable dihients for use as the liquid medium are well known in the art and include hydrocarbons, which are inert and liquid under reaction conditions. Suitable hydrocarbons include isobutane, propane, n-pentane, i-pentane, neopentane and n-hexane, with isobutane being especially preferred. Additional details regarding loop reactor apparatus and polymerization processes may be found in U.S. Patent Nos. 4.674,290; 5,183,866; 5,455,314; 5,565,174; 5,624,877; 6,005,061; 6,045,661; 6,051,631; 6,114,501; 6,262,191; and 6,420,497, which are incorporated by reference herein. Additionally, the present techniques for controlling heavies may be employed where the monomer is the liquid medium for the polymerization. For example, the present techniques may be used for the polymerization of propylene where propylene is the liquid medium and an inert diluent is not present in any substantial amount. A diluent may still be used for the catalyst. For illustration, but not as a limitation, the present invention will be described in connection with a polyethylene process using an inert diluent as the liquid medium, but it is to be understood that the present invention may also be employed where the monomer is used as the liquid medium and would take the place of the diluent in the following descriptions, FIG. 1 is a representation of a slurry polymerization system 10 according to the present invention. The slurry polymerization system 10 includes a catalyst feed tank 12 (such as a catalyst mudpot or an agitated tank) containing a mixture of catalyst and diluent. Catalyst and diluent from the catalyst tank 12 are pumped into a loop reactor 14. FIG. 1 also shows flashline heaters 16, a flash gas separator (also described as an intermediate pressure flash chamber) 18, a heavies removal system 20, a fluff chamber 22, a purge column 24, a recycle treater 26, an isobutane/nitrogen recovery unit (INRU) 28, a recycle tank 30, a heavies column 32, a lights column 34, an olefin free surge unit 36, and a series of conduits, pumps and condensers. For the sake of simplicity, some components unrelated to the claimed systems and processes and/or that are related to production or routine details, such as mtervening valves and connecting lines/conduits of the slurry polymerization system 10, are not shown. Catalyst or catalyst and diluent from the catalyst feed tank 12 passes through conduit 40 and is piunped into the loop reactor 14 by pump 42. Suitable catalysts are well known in the art. For example, chromium oxide on a support such as silica may be used, as disclosed in United States Patent No. 2,825,721, issued to Hogan and Banlcs, which is hereia incorporated by reference m its entirety. Additionally, other catalysts well known in the art (for example, Ziegler catalysts, metallocene catalysts) may also be used for olefin polymerization. The slurry polymerization system 10 also includes a monomer feed 38. A monomer such as ethylene, for example, is introduced into the loop reactor 14. Additional conduits and lines may supply monomer and/or diluent into the loop reactor 14 or join in a line 46 for introducing a combined stream of fiesh e&ylene and diluent recycle as shown. Monomer, diluent, catalyst and any other feed materials may be introduced into the loop reactor 14 at one or several points. As shown m FIG. 1, the loop reactor 14 may comprise a plurality of vertical members 48 formed integrally with horizontal members 50 (or curved connecting members), hi order to maximize heat transfer within the reactor 14, the distance between vertical members 48 is preferably minimized. Thus, the horizontal members 50 may be of minimal length. Alternatively, the horizontal members 50 may be eliminated such that the vertical members 48 are connected through curved connecting members. Altematively, the loop reactor may be substantially horizontal and not have any vertical members. The longer members 48 preferably have heat exchange jackets 49. The vertical members 48 and horizontal members 50 (or curved connecting members) define a loop reaction zone. The loop reaction zone may include more or fewer vertical members 48 and correspondmg horizontal members 50 as that shown m FIG. 1. Further, the loop reactor may be oriented vertically or horizontally (for example, by rotating reactor 14 in FIG. 1 by 90 degrees) or may be entirely horizontal, with no vertical members. The connecting members 50 may be any sh^e or form that connects the vertical segments 48 and allows fluid to flow therebetween. An unpeller is located in the loop reactor 14 to circulate the slurry. The unpeller is driven by a motor 47. The raipeller is located in the interior of the loop reaction zone defined by the vertical members 48 and the horizontal members 50. The impeller 47 is operable to circulate fluid slurry, comprising liquid diluent and solid olefin polymer particles, through the loop reactor 14. An intennediate product slurry, comprising the liquid medium and solid polymer particles, is withdrawn, or taken off, from the loop reactor 14 by way of the continuous take-off devices 52. A continuous take-off device 52 is disclosed in U.S. Patent No. 6,239,235, which is incorporated by reference herein. The slurry polymerization system 10 may include more or fewer than the continuous take-off devices 52 (and correspondit^ conduits and flashline heaters 16) shown in FIG. 1. For example, one, two, three or more continuous take-off devices 52 may be used. Further, the continuous take-off devices 52 may be tangentially positioned on curved members. The continuous take-oflf devices 52 may be positioned anywhere on the loop reactor 14. Alternatively, settling legs may be used in conjunction with, or instead of, the continuous take-off devices 52. As flxiid slurry is withdrawn from the loop reactor 14 as uitermediate product slurry, the intennediate product slurry is passed from the continuous take off-device 52 to a flashline 54, which forms a first fluid passage for the withdrawn portion of the slurry to downstream processing apparatus. The flashline 54 may be provided with a flashline heater 16 surrounding at least a portion of the flashline 54. The flashline heater 16 contains a heated fluid (for example, steam) that provides indirect heating to the contents of the flashline 54, such that intennediate product slurry that passes flirough the flashline 54 is heated. Preferably, the intermediate product slurry is heated such that at least a majority of the liquid diluent is vaporized, thereby yielding diluent vapor and a post-flashline slurry. The post-flashline slurry comprises the solid polymer particles and a reduced amount of liquid diluent (as compared to the intermediate product slurry). Alternatively, the post-flashline slurry may be heated such that less than a majority of the liquid diluent is vaporized. Preferably, the intennediate product slurry is heated in the flashline 54 such that, as it enters the flash gas separator 18, essentially all of the liquid diluent has been vaporized ("flashed") within the flashline 54. The "flashing" tends to occur as the intennediate product slurry passes across the continuous take-off device 52 and the flashUne 54. Preferably, the intermediate product sluny is heated in the flashline 54 to fully vaporize the diluent liquids so that the solids and vapors that discharge into the flash gas separator 18 are free of Uquids. la some systems utilizing a flashline heater 16, some or all of fee diluent (or other liquid medium) will flash in flashline 54 prior to introduction to the flash gas separator 18, which may be termed a "flash chamber" or an "intermediate pressure flash chamber." These terms still are frequently used for the tank that follows the flashline, where vaporized diluent separates from polymer solids. "Flash tank" or "flash chamber" are still used even though there may be little or no flashing in the flash tank if all or substantially all of the diluent is vaporized in the flashline. In current designs that have the flashlines discharging at higher pressures and without downstream drying devices, it is intended to design the flashlines so there is little or no pressure drop on entering the flash tank, with essentially all of the liquids vaporized prior to entering the vessel. After the intermediate product slurry passes through the flashline 54, the resulting post-flashline fluff and vaorized diluent is passed into the flash gas separator' tank or chamber 18, The flash gas separator 18 preferably is at an intermediate pressure, lower than the pressure in the reactor but higher than the pressure of downstream apparatus. Preferably the flash gas separator 18 is at a pressure whereby the separated flash gas (or a majority or other large portion) may be condensed by heat exchange without compression. In the flash gas separator 18, most of the diluent, unreacted monomer, and heavies form a vapor stream (flash gas) that rises toward a top portion of the flash gas separator 18, while "fluff falls to a bottom portion of the flash gas separator 18. The fluff comprises solid polyma:, which may have trace or other small amounts of diluent entrained therein. The fluff may pass to a second flash gas separator (for example, a low pressure flash chamber). A two-stage flash system is disclosed in U.S. Patent No. 4,424,341, which is incorporated by reference herein. Alternatively, the fluff may pass from a bottom portion of the first flash chamber to the purge column 24. (The purge column 24 may follow the second flash chamber instead). Alternatively, the fluff may be passed through a conveyor dryer and then to a purge column as described in U.S. Patent No. 4,501,885, which is incorporated by reference herein. Entrained diluent within the polymer particles is separated from the fluff in the purge column 24 by passing nitrogen gas through the solid polymer particles (the fluff). The nitrogen extracts entrained diluent and/or liquid diluent, thereby leaving solid polymer essentially ftoe of entrained diluent. The solid polymer is then d^osited, collected, ejected or otherwise withdrawn from a bottom portion of the purge column 24. The nitrogen and extracted diluent are then passed out a top portion of the purge column 24 to an isobutane/nitrogen recovery unit (INRU) 28. The INRU processes the vapors removed from the fluff in the purge column. The INRU separates the nitrogen from the diluent vt^jors by condensing the diluent vapors into liquids, hi one sense the INRU functions somewhat like the heavies removal system by condensing a relatively small amount of the flash gas and sending a liquid to the heavies column. The INRU 28 separates nitrogen from diluent and other hydrocarbons. The nitrogen is then passed back to the purge column 24 through a nitrogen return line 60. The separated diluent and other hydrocarbons may be returned to the recycle taiik 30 and ultimately returned to the loop reactor 14. Alternatively, some or all of the liquids from the INRU 28 may be sent to the heavies column 32, The INRU is designed to produce a liquid product which contains substantially all the hydrocarbons (but not the solid polymer particles) removed in the purge colunm. The vapor stream which has been vaporized either in the flashline 54 and/or in the flash gas separator 18, which is also referred to herein as the first vapor stream, is passed to the heavies removal system 20 by way of va^or ranoval line 56. The v^or removal line 56 may include a series of filters and components, such as bag filters, for filtering fine polymer particles torn the vapor stream in order to prevent the fines fix)m altering tiie heavies removal system 20. For example, for a suitable polyethylene process, the vapor stream is primarily isobutane diluent, but the vapor stream diluent also contains heavies, such as 1-hexene co-monomers and other hydrocarbons having six or more carbon atoms. The vapor stream may also contain lighter hydrocarbons such as efriane and ethylene. FIG. 2 is a representation of an exemplary heavies removal system 20. The heavies removal system 20 is fluidly connected to, and communicates with, a top portion of the flash gas separator 18 through the v^or removal line 56. In the equipment shown in FIG. 2, the heavies removal system 20 includes a first condenser 62, a bypass line 63, a bypass valve 64, a static mixer 66, a liquid collection talk 68, a temperature controller 70, a level controller 72, a pump 74, a flow controller 76 and a flow control valve 78. The heavies removal system 20 is designed and/or set so as to condense a small amount of liquid fom the first vapor stream. A fraction of flash gas (in other words, a first portion of the first vapor stream) is passed through the condenser 62, which condenses some of that fraction into a liquid. When the liquid fix>m condenser 62 contacts the relatively hot flash gas that has bypassed the condenser 62 (in other words, a second portion of the first vapor stream), some of the liquid again vaporizes, leaving a residual amount of liquid and a larger amount of flash gas. The liquid and flash gas are passed to the liquid collection tank 68. A static mixer 66 can be used to assure proper contact, rapid revaporization and equilibrium conditions in the liquid collection tank 68. The rate of flow may be set on flow controller 76. The level in the liquid collection tank 68 is determined by the amount of liquid generated by the condenser 62. If the liquid level in the collection tank 68 rises, the temperature controller 70 adjusts to a higher temperature to decrease the amount of liquids generated by the condenser 62. Conversely, if the level within the liquid collection tank 68 decreases, the level controller 72 acts to decrease the temperature set point on the temperature controller 70, thereby directing more flow througji the condenser 62 to generate more liquids. Consequently, the level controller adjusts the temperature controller to generate an amount of liquids that matches flie desired amount of liquids as set by the flow controller. This provides an efficient and relatively easy way to control the amount of liquid condensed firom the first vapor stream. As seen in FIG. I, the condenser 62 of the heavies removal system 20 is in addition to flash gas condenser 84. The heavies removal system 20 will generally be used to condense a relatively small amount of the total vapor fi-om vapor removal line (in other words, of the first vapor stream). For example, the heavies removal system 20 may condense (in other words, form a liquid from) as little as about 1% or less of the total vapor stream firom the first flash chamber. One may desire to set a maximum for the amount of the first vapor stream condensed by the first condenser. For example, the heavies removal system 20 may be set to condense at most about 10%, alternatively at most about 5%, alternatively at most about 4%, alternatively at most about 3% of the first vapor stream. Condenser 62 may condense from about 0.1 to about 15% of the flash gas. The amount of liquid condensed by cond^ser 62 may be up to 5 times greater than the liquid generated by the heavies removal system 20. i The heavies removal system 20 produces liquid with a higher percentage of the heavier components than is found in the vapor stream. For example, the liquid in the collection tank 68 may contain at least about 1%, alternatively at least about 5%, alternatively at least about 10%, of the heavies in the vapor stream. In particular, the heavies removal system is expected to be particularly effective in removing most oligomers, for example, at least about 2%, alternatively at least about 10%, alternatively about 20% of the oligomers in the vapor stream. Even if the heavies removal system does not remove all the heavies from the liquid medium to be recycled to the polymerization reactor, it still provides an important benefit by preventing an excessive buildup of heavies hi the recycled medium. The liquid concentrated in heavies may be referred to as a heavies liquid. The heavies liquid is routed to a heavies column where the heavier components can be removed from the process. Thus the concentration of heavier components in the flash gas is decreased from levels that would otherwise exist. The present process and system result in the generation of a recycle diluent stream having fewer heavies than would otherwise build up in the recycle diluent stream. This system can work in conjunction with a direct recycle process, allowing most of the diluent to be condensed and recycled directly back to the reactor without passing through fractionation columns that remove heavier and lighter components, hi the direct recycle process it is desirable that only a fraction of the total recycle diluent is sent to fiiactionation where heavier components can be rejected and lights can be removed and olefin-free diluent generated. With only a fraction of the recycle diluent feeding fractionation, the fractionation columns can be relatively small. As shown in FIG. 2, the condenser 62 is in fluid coimection with the vapour removal line 56 and is upstream from the static mixer 66. The bypass valve 64 is interposed within the bypass line 63 such that the bypass valve 64 may selectively open and close the bypass line 63, thereby controlling the flow of vapor through the bypass line 63. The liquid collection talk 68 is downstream from the static mixer 66. A diluent recycle line 80 is in fluid communication with the liquid collection tank 68 and connects the liquid collection tank 68 to a recycle tank 30. The bypass valve 64 may be in informational communication with the temperature controller 70, which is interposed within the diluent recycle line 70. Additionally, or alternatively, the bypass valve may be in informational communication with the level controller 72, which is positioned within the liquid collection tank 68. The temperature controller 70 and the level controller 72 may be assisted by or used in conjunction wifli a central processing unit or other logic unit or main controller. The temperature controller 70 and the level controller 72 relay signals to the bypass valve 64 to close or open the bypass line 63, depending on temperature and level conditions wthiin the heavies removal Systran 20. This control scheme permits automatic control to obtain the desired amount of liquid in the liquid collection tank 68, The bottom portion of the liquid collection tank 68 is in fluid communication with a heavies delivery line 82, which receives a hquid concentrated in heavies from the liquid collection tank 68. A pump 74 may be positioned in the heavies delivery Ime 82, which provides sufBcient force to move the liquid concentrated in heavies through the heavies delivery line 82 to the heavies column 32. A flow controller 76, which may be assisted by or used in conjunction with a central processing unit or logic unit or a main controller, is positioned downstream from the pump 74 and is in informational communication with the flow control valve 78, which may selectively open and close the heavies delivery Ime 82. The flow control valve 78 may be operated in conjunction with the flow controller 76. Depending on the rate of flow of heavies through the heavies delivery line 82, the flow controller 76 may send a command signal to the flow control valve 78 to open or close the heavies delivery line 82. The heavies removal system 20 is used to produce a liquids stream relatively rich in heavier components. Once the heavies or a portion of heavies are removed, the diluent may be recycled and returned to the loop reactor 14. The heavies removal system 20 does not necessarily remove all heavies. Rather, the heavies removal system 20 may only remove a small portion of the heavies in order to limit potential build-up of heavies to relatively low levels. In particular, the heavies removal system can limit the build-up of oligomers. The heavies removal system 20 is configured to produce liquids relatively concentrated ui heavies that were contained within the first vapor stream. It is contemplated that at least some of the heavies from the first vapor stream, or a major portion thereof, will be passed to the heavies delivery line 82. For example, about 98% of the first vapor stream may remain as a vapor as a result of bypassing the first condenser, in other words only a small amount of liquids are generated. A portion of the first vapor stream is sent to the condenser where all or most of that portion is converted to liquid. This colder liquid is combmed with the hotter gases that bypassed the condenser and this liquid and vapor mixture is sent to the static mixer 66. The static mixer ensures good mixing of the liquids and vapors so that substantially equilibrium conditions can quickly be generated. Substantially equilibrium conditions means that the liquid and vapor in the liquid collection tank come to substantially the same temperature with some of the liquids vaporizing to accomplish this. The gas may then be passed to collection tank where the liquids and vapors initially intermingle but also are separated. As fiash gas condenses and re-evaporates, heavies are left behind in the liquid at the bottom of the collection tank. The amount of the first vqjor stream that is diverted into the condenser 62 is controlled to generate a desired amount of liquids in the liquid collection tank 68. The bypassed hot vapor and condenser-cooled liquid from the condenser 62 are then mixed by the static mixer 66. The temperature controller 70 may signal the bypass valve 64 to open or close to a desired extent, depending on the temperature of the diluent vapor in the diluent recycle line 80. After the flash gas vapor and condensed liquid are mixed together to form a mixture, the mixture is passed into the liquid collection tank 68. The liquid collection tank 68 separates the liquids containing a higher concentration of the heavier components from the diluent vapor. It is desirable to reduce or avoid pressure or temperature gradients in the liquid collection tank. The temperature controller 70 can be periodically or occasionally reset by the level controller on the collection tank. If the level in the collection tank drops below the level setpoint, the controller sends a signal to lower the setpoint of the temperature controller which in turn sends a signal to close the bypass valve to a desired extent and force more flow through the condenser to generate more liquids. Conversely, if the level in the tank is above the desired setpoint, the level controller sends a signal to raise the setpoint of the temperature controller which in turns sends a signal to open the bypass valves to a desired extent which decreases the flow through the condenser which reduces the amount of liquids formed. When the setoint of the flow controller is changed, the flow control valve opens or closes to produce the desired flow, and this change of flow is reflected as a change in level in the tank, and the level controller reacts to change the amount of liquids condensed. The liquid concentrated in heavies is passed from the liquid collection tank 68 througih the heavies delivery line 82 and pumped towards the heavies column 32 by ' the pimip 74. The flow controller 76 monitors and controls the flow of the liquid through the heavies delivery line 82 by signaling the flow control valve 78 to open or close the flow control valve 78, depending on the desired amount of liquids to be generated. For example, if the operators want to create 1500 kg/hr liquids, it is desirable that that number can be entered as a setpoint to the flow controller. The liquids are ultimately delivered to the heavies column 32. Referring again to FIG. 1, the heavies column 32 separates the Uquid medium and lighter components from the heavies. The diluent (in other words, the liquid mediimi) extracted in the heavies column 32 is then passed to a lights column 34, where lights are removed, thereby yielding essentially or substantially pure diluent, which is then passed through the olefln-free surge 36 and pumped to the catalyst feed tank 12 or to the recycle tank 30, and it is then pumped to the loop reactor 14. The diluent vapor within the diluent recycle line 80 is passed through a flash gas condenser 84, which may condense, or liquefy, the diluent. Some diluent with a relatively high concentration of lighter components may remain as vapor. The stream is passed to the recycle tank 30, which serves as a vapor-Uquid separation drum and the liquids are passed direcfly back to the loop reactor 14 through the recycle treater 26. The vapor which has a higher relative concentration of the lighter components is passed to fractionation where the light components are rejected, and 1-hexene and hexanes are recovered or rejected, octane and heavier compounds are rejected, and diluent (usually isobutane) is recovered free of olefins i FIG. 3 is a sdiematic representation of another slurry polymerization system 11, which includes a novel heavies removal system. As shown in FIG. 3, the lights removal line 86 may be a vapor line that enters through the side of the heavies colmnn 32. Since vapor line 86 will contain small amounts of hexane, it is desirable to have it enter the heavies column because all hexanes must be excluded from the lights column. Also, there is a liquid product line 90 extending from the JNBJJ 28. The INRU is designed to recover both nitrogen and hydrocarbons (diluent) as liquid. The liquid product line 90 may be split with one branch connecting to the heavies column 32 and another branch connecting to the recycle tank 30. In this way, liquids may be directed to the heavies column 32 and/or to the recycle tank 30. Also, the olefin-free product that is passed from the olefin-fiee surge unit 36 may be pxmiped back to the recycle tank 30 in addition to the catalyst mix tank 12. Thus, the present invention provides a more efficient system and process of recycling the liquid medium in a slurry polymerization process. The present invention provides an improved heavies removal system and process, which removes a greater amount of heavies, as compared to prior systems, from the liquid medium that is to be recycled to the reactor. A direct recycle system is provided where most or all of the liquid in the reactor effluait (diluent and other hydrocarbons) is separated from the fluff, condaised and recycled back to the reactor without passing through purification (fractionation) steps. Other systems pass substantially all of the diluent v^or (reactor effluent) through fractionation (purification steps) where all of the heavier compounds can be separated. In a direct recycle system there is a desire to reject heavier components as well as lighter components so they do not concentrate in the process and harm the reactor or product. So in the direct recycle process some recycle diluent (in other words, reactor effluent hydrocarbons) are still processed in a small purification (fractionation) section to generate some pure (olefin-free) diluent for use as catalyst diluent, and to reject some heavy and light components to prevent abnormal build up or concentration. By fractionating only a small portion of the diluent recycle, the fractionators can be smaller. The direct recycle fractionators can be fed from a recycle liquid slip stream or by INRU liquid product but by creating liquids with the present heavies removal system, heavies concentration is controlled better, in other words for the same fractionation feed rate, heavies concentration in the recycle is lower. The present system and process described may also feed fractionation (heavies and lights columns) when the INRU is not operational so that olefin-free diluent may be generated to slurry the catalyst. While the invention has been described with reference to certain embodiments, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted without departing from the scope of the invention, in addition, many modifications may be made to adapt a particular situation or material to the teachings of the invention without departing from its scope. Therefore, it is intended that the invention not be limited to the particular embodiment disclosed, but that the invention will include allembodiments falling within the scope of the appended claims. WE CLAIM : 1. A recovery and purification system for a liquid medium from a slurry polymerization, the system comprising: a flashline (16) configured to pass an intermediate product slurry from a slurry polymerization reactor (14) to a flash gas separator (18); the flash gas separator (18) configured to separate a vapor stream (56); a first condenser (62) disposed downstream of the flash gas separator and configured to partially condense a first portion of the vapor stream; a vapor bypass line(63) configured to pass a second portion of the vapor stream around the first condenser; a bypass valve (64) configured to facilitate control of the flow rate of the second portion of the vapor stream through the vapor bypass line; a collection tank (68) disposed downstream of the first condenser and configured to receive the partially-condensed first portion of the vapor stream from the first condenser and to receive the second portion of the vapor stream bypassed around the first condenser; a second condenser (84) configured to condense a second vapor stream (80) discharged from a top portion of the collection tank; a recycle tank (30) configured to receive the condensed second vapor stream from the second condenser; a diluent recycle line (starting at bottom of 30) configured to facilitate recycle of diluent fi"om the recycle tank to the slurry polymerization reactor; a liquid delivery line (82) coupled to a bottom portion of the collection tank and configured to pass a liquid stream from the collection tank to a fractionation system (32, 34). 2. The recovery and purification system as claimed in claim 1, wherein the bypass valve is in informational communication with a temperature controller configured to indicate temperature of the second vapor stream discharged from the top portion of the collection tanic, or wherein the bypass valve is in informational communication with a level controller configured to indicate a level of liquid in-the collection tank, or a combination thereof 3. The recovery and purification system as claimed in claim 2, wherein the level controller is in informational communication with the temperature controller, and the temperature controller is in informational communication with the bypass valve. 4. The recovery and purification system as claimed in claim 1, wherein the fractionation system comprises a heavies column coupled to the liquid delivery line. 5. The recovery and purification system as claimed in claim 4 comprising a flow controller disposed along the liquid delivery line. 6. The recovery and purification system as claimed in claim 4 comprising a pump disposed along the liquid delivery line for propelling the liquid into the heavies column. 7. The recovery and purification system as claimed in claim 1 comprising a static mixer disposed downstream of the first condenser and upstream of^ the collection tank, wherein the static mixer is configured to mix the partially-condensed first portion of the vapor stream and the second portion of the vapor stream. 8. The recovery and purification system as claimed in claim 1 comprising a purge column configured-to receive solid polymer particles from the flash gas separator. 9. A process for recycling a liquid medium withdrawn from a slurry polymerization reactor, the method comprising: discharging a slurry from a slurry polymerization reactor, wherein the slurry comprises a liquid medium and solid polymer particles, the liquid medium comprising a diluent; passing the slurry thought a flashline to flash at least a portion of the liquid medium; separating a first vapor stream from the slurry, wherein the first vapor stream comprises diluent, light components lighter than the diluent, and heavy components heavier than the diluent at least partially condensing a first portion of the first vapor stream in a first condensing zone to form a first liquid; passing a second portion of the first vapor stream to a collection zone without passing the second portion through the first condensing zone; separating a second liquid and a second vapor stream in the liquid collection zone; passing the second liquid to a purification zone configured to remove at least heavy components heavier than the diluent firom the second liquid; and at least partially condensing the second vapor stream to form a third liquid; recycling the third liquid to the slurry polymerization reactor without fractionating the third liquid to remove heavies. 10. The recycling process as claimed in claim 9 comprising the step of mixing together the first liquid and the second portion of the first vapor stream before passing the first liquid and the second portion to the collection zone. 11. The recycling process as claimed in claim 9, wherein the separating a first vapor stream from the slurry yields solid polymer fluff having entrained diluent and the method comprisesf passing the solid polymer fluff from the flashing step to a purge zone wherein the purge zone extracts entrained diluent from the solid polymer fluff. 12. The recycling process as claimed in claim 9 wherein at least about 1% of the heavy components in the first vapor stream are condensed into the second liquid. 13. The recycling process as claimed in claim 9 wherein at least about 5% of the heavy components in the first vapor stream are condensed into the second liquid. 14. The recycling process as claimed in claim 9 wherein at least about 10% of the heavy components in the first vapor stream are condensed into the second liquid. 15. The recycling process as claimed in claim 9 wherein at least about 2% of the oligomers in the first vapor stream are condensed into the second liquid. 16. The recycling process as claimed in claim 9 wherein at least about 10% of the oligomers in the first vapor stream are condensed into the second liquid. 17. The recycling process as claimed in claim 9 wherein at least about 20% of the oligomers in the first vapor stream are condensed into the second liquid. 18. The recycling process as claimed in claim 9 comprising measuring the level of liquid in the liquid collection zone; and controlling the condensing of the vapor stream based on the measured liquid level. 19. A process for operating a slurry polymerization system, the process comprising the steps of: forming a slurry comprising solid polyolefin particles in a liquid mediimi in a polymerization reaction zone, wherein the liquid medium comprises at least diluent, monomer, and heavies; withdrawing a portion of the slurry from the polymerization reaction zone; vaporizing the liquid medium to form a first vapor stream comprising at least diluent and heavies, wherein the heavies are components heavier than the diluent; separating the first vapor stream from the solid polyolefin particles; passing a first portion of the first vapor stream to a condensation zone whereby a first liquid stream is formed; passing a second portion of the vapor stream to a collection zone without passing the second portion through the condensation zone; collecting the first liquid stream and the second portion in the liquid collection zone; separating a second vapor stream-and a second liquid stream in the liquid collection zone; condensing and recycling the second vapor stream back into the polymerization reaction zone without heavies removal treatment; and passing the second liquid stream to heavies removal treatment. 20. The operating process as claimed in claim 19 wherein the diluent comprises isobutane, the monomer comprises ethylene, and the solid polyolefin particles comprise polyethylene. 21. The operating process as claimed in claim 19 wherein the diluent and monomer comprise propylene, and the solid polyolefin particles- comprise polypropylene. 22. The operating process as claimed in claim 19 comprising passing the solid polyolefin particles to a purging step, where entrained diluent is extracted from the solid polyolefin particles. 23. The operating process as claimed in claim 19 comprising measuring the level of liquid in the liquid collection zone and controlling the condensing of the first vapor stream based on the measured liquid level. 24. The operating process as claimed in claim 19 passing, wherein passing the second liquid stream to heavies removal treatment comprises passing the second liquid stream from the collection zone to a heavies fractionation column. 25. The operating process as claimed in claim 19 comprising the steps of: measuring the temperature of the vapor in the liquid collection zone; and adjusting the amount of the first vapor sfream being passed to the condensation zone in response to the measured temperature. 26. The operating process as claimed in claim 19 wherein the liquid removed from the collection zone contains at least about 1% of the heavies in the first vapor stream. 27. The operating process as claimed in claim 19 wherein the liquid removed from the collection zone contains at least about 5% of the heavies in the first vapor stream. 28. The operating process as claimed in claim 19 wherein the liquid removed from the collection zone contains at least about 10% of the heavies in the first vapor stream. 29. The operating process as claimed in claim 19 wherein the liquid removed from the collection zone contains at least about 2% of the oligomers in the first vapor stream. 30. The operating process as claimed in claim 19 wherein the liquid removed from the collection zone contains at least about 10% of the heavies in the first vapor stream. 31. The operating process as claimed in claim 19 wherein the liquid removed from the collection zone contains at least about 20% of the heavies in the first vapor stream. 32. The operating process as claimed in claim 19 wherein essentially all the heavies removed from the liquid collection zone are removed in liquid form. 33. The operating process as claimed in claim 19 wherein the second liquid stream is held in the liquid collection zone for a time sufficient to allow heavies from the vapor to transfer to the liquid.

Full Text

FIELD OF THE INVENTION
The present invention relates to a recovery and purification system for a liquid medium from a slurry polmerization. More particularly, the present invention relates to an olefin polymerization system and process that include an improved way of removing heavies from diluent and/or unreacted monomer withdrawn from and recycled to the polymerization reactor. The invention also relates to a process for recycling a liquid medium.
BACKGROUND OF THE INVENTION
Olefin polymerization processes may be conducted under slurry conditions. Such polymerization processes may be carried out in a loop reactor in which monomers are polymerized to form a slurry of solid polymer particles in a liquid medium. Portions of the slurry axe withdrawn from the loop reactor through take-offs devices such as settling legs and continuous take-offs.
The slurry is then processed to separate the liquid medium (for example, a liquid diluent) from the solid polymer particles. Flashline heaters and flash chambers have been used to vaporize the liquid diluent though a combination of temperature and pressure adjustments, thereby separating the diluent from the solid polymer particles. Additionally, other types of equipment, such as purge columns, separating drums and cyclones, have been used for separation and other downstream treatment.
Efficient slurry polymerization processes typically recycle as much diluent as they reasonably can. That is, as the diluent is vaporized, diluent is processed for

recycling back to the loop reactor. As the liquid diluent is vaporized at various stages of the polymerization process after the slurry is withdrawn from the loop reactor, various compounds and contaminants may also be vaporized along with the diluent.
"Heavies" are liquid components heavier than the diluent, and are often vaporized along with the diluent. During the recycling process, a vapor stream containing the diluent and heavies may be condensed and returned to the loop reactor as a recycle stream of the diluent and heavies. Heavies may concentrate or accumulate within the loop reactor and decrease reactor efficiency and/or cause damage within the loop reactor. For example, heavies buildup within the reactor may degrade product quality and/or distort reactor control making reactor problems and blockage more likely.
Another recycling technique separates a slip stream comprising diluent and minor amounts of monomer from the bulk of the flashed fluid conqjonents. The slip stream is subjected to olefin removal to give an essentially olefin-free stream for recycle to a catalyst preparation area. The slip stream may be taken off before and/or after a diluent recycle cooler. The slip stream(s) is then passed to a heavies removal column. The heavies removal column removes heavies from the slip stream, which can then be used to prepare a catalyst mud or slurry. The bulk of monomer-containing recycle diluent is passed to a diluent recycle surge (storage) vessel, and a recycle stream is passed back to the reactor. If desired, other purification steps such as water removal can be carried out on this recycle stream.
An efficient system and process of recycling diluent in a slurry polymerization process are desired. Furttier, an improved heavies removal system and process, which remove heavies from the diluent to be recycled to the reactor, are desired.
BRIEF SUMMARY OF THE INVENTION
As one aspect of the present invention, a process for recycling a liquid medium withdrawn from a slurry polymerization reactor is provided. The method comprises separating a first vapor stream from a slurry comprising a liquid medium and solid polymer particles, wherein the vapor stream comprises at least the medium and heavies. A first portion of the first vapor stream is passed to a first condensing

zone, and a first portion of the first vapor stream is condensed to form a first liquid. A second portion of the first vtepor stream is passed to a collection zone without substantial condensation. A second liquid and a second vapor stream are separated in the collection zone. The second liquid is passed to a heavies purification zone, and the medium is recycled fi:om the second vapor stream without firactionating to remove heavies.
As another aspect of the present invention, a recovery and purification system for a liquid medium fmm a slurry polymerization is provided. The system comprises a first fluid passage connected at one end to a slurry polymerization reactor and connected at an opposite end to a flash gas separator, for separating a vapor stream comprising the medium firom solid polymer particles. The system also comprises a vapor removal line coimected at a top portion of the flash gas separator, for transporting the vapor stream firom the flash gas separator. The vapor removal line is connected to a first condenser and also to a vapor bypass line that provides a bypass around the condenser. A bypass valve controls the flow of vapor through the vapor bypass line. The output of the condenser and the opposite end of the bypass line are both fluidly connected to a liquid collection tank. A liquid delivery line is at a bottom portion of the liquid collection tank, and a vapor recycle line is at a top portion of the liquid collection tank. A second condenser is fluidly connected to the vapor recycle line, and a second fluid passage connects the output of the second condenser to the slurry polymerization reactor.
The present invention may include control apparatus or steps associated with the bypass valve. For example, the bypass valve can be in informational communication with at least one of a temperature controller downstream of the liquid collection tank and a level controller positioned within the liquid collection tank. The bypass line is advantageous because it is difBcult to operate a condenser to produce only a small amount of liquids. The present invention is able to produce a relatively small amount of liquids because the first vapor stream (which is the flash gas fi-om the first flash chamber) is spUt, with a first portion passing through a condenser and a second portion bypassing the condenser. The flash gas passing through the condenser

may be entirely or nearly entirely condensed into liquid, or a small part (for example, about 1-10%) maybe condensed, or some other proportions.
Downstream of the condenser, the hot flash gas is combined with the cold liquid and mixed and allowed to come to an equilibrium (at least with respect to temperature). After this mixing, the liquid that remains is more concentrated m the heavier components. The desired amount of liquid is set by the flow controller on the liquid line. The level in the tank is controlled by adjusting the temperature controller, which in turn adjusts the bypass valve so that a sufficient amount of vapor bypasses the condenser to generate enough liquid to satisfy the flow controller. To accomplish the desired amount of heavies removal, from about 0.1 to about 20% of the flash gas alternatively from about 0.5% to about 10%, alternatively from about 1% to about 5%, will be converted into liquids by the condenser. At times it may be desirable to collect no liquids. At other times (for example, during resin transitions), it may be desirable to maximize liquids generation and collect more than usual.
The present invention may also include a heavies colunm or other heavies removal treatment at an opposite end of the heavies delivery line. A flow controller and/or a pump can be disposed along the heavies delivery line.
A static mixer can be fluidly connected to and downstream from the first condenser, and the static mixer is upstream from and fluidly connected to the liquid collection tank. The static mixer is employed to quicken the formation of an equilibrium mixture after the hot flash gas and cold liquid are combined. It is desirable to have equilibrium conditions before entering the collection tank, at least a temperature equilibrium. A recycle tank may be disposed along the diluent recycle line dowmtream of the flash gas condenser.
BRIEF DESCRIPTION OF THE DRAWINGS
FIG. 1 is a r^resentation of a slurry polymerization system which includes a novel heavies removal system,
FIG, 2 is a representation of the heavies condenser, static mixer, and liquid collection tank from the system of FIG. 1, as well as a novel control scheme.

FIG. 3 is another representation of a slurry polymerization system which includes a novel heavies removal system.
DETAILED DESCRIPTION OF THE INVENTION
The present invention provides a diluent recovery and purification system and process for a slurry polymerization reactor, especially for a loop polymerization reactor. The system and process comprise a flash chamher or flash gas separator, a vapor removal line, a condenser, and a liquid collection tank. The flash chamber or flash gas separator receives a slurry withdrawn from a loop reactor. Diluent, unreacted monomer, and various heavies are separated from the solid polymer particles as a first vapor stream. The vapor removal line receives the first vapor stream and transfers a first portion to a condenser that condenses at least some of the first portion to form a first liquid. It may be a relatively small amount portion, for example, about 2% of the first vapor stream that is condensed. The second portion of the first vapor stream bypasses the condenser but is thereafter combined and mixed with the first liquid to form a combined stream. The combined stream is sent to a liquid collection tank. As the vapor and liquid mix in the mixing device and/or in the line to the liquid collection tank, some of the Uquid will be vaporized again, and the mixture may come to an equilibrium temperature. The combined stream will be cooled enough such that some liquid will be present. The liquid that collects in the Uquid coUection tank wiU have a higher concentration of the heavier compounds than the vapor leaving the collection tank. The liquid phase of an eqxiilibrium mixture will be richer in the heavier components than the vwpoT phase because the heavier components are less volatile.
The Uquid containmg a higher concentration of the heavier components is passed from the Uquid collection tank to a heavies deUvery Une, and the vapor is passed to a diluait recycle line. The vapor may be passed to a second condenser and a recycle surge tank. The vapor from the Uquid collection tank can be condensed and recycled to the slurry polymerization reactor without further treatment to remove heavies.

During the separating step, vapor comprising diluent, unreacted monomers/comonomers and various inerts, both heavier and lighter than the primary diluent (for example, isobutane), are separated. Various other compounds associated with the feedstocks and diluent feed, such as other compounds with 4 carbons (for example, n-butane) and compounds with six carbons (for example, n-hexane), are inerts, which do not polymerize and function as a diluent along with isobutane. Heavies include additional compounds with six carbons along with any heavier corapoxmds that may be produced in the reactor (such as oligomers). A portion of the v^or stream is then passed to a condenser in a heavies removal zone. The condenser may only condense a small portion of the stream or it may condense most or essentially all of the first portion. The liquid and vapor are then combined, which allows them to form a combined stream. The combined stream is passed to a liquid collection zone, and liquid and vapor are separated in the collection zone, after which the diluent vapor is passed to a diluent recycle line and the liquid is passed into a heavies delivery line.
The diluent vapor separated from the liquid (that is, diluent vapor exiting from a top portion of the liquid collection tank) is suitable for recycling to the polymerization reactor. The diluent vapor is passed from the diluent recycle line to a diluent recycle tank. The diluent vapor is condensed by heat exchange. The diluent can then be recycled to the polymerization zone without having to remove additional heavies. Further, the liquid is passed from the heavies delivery line to a heavies column.
The present invention is applicable to any olefin polymerization in a loop reactor utilizing a liquid medium so as to produce a fluid slurry of polymer solids in the liquid medium. Suitable olefin monomers include 1-olefins having up to 8 carbon atoms per molecule and no branching nearer the double bond than the 4-position. The present invention is particularly suitable for the homopolymerization of ethylene and copolymerization of ethylene and a higher 1-olefin such as butene, 1-pentene, 1-hexene, 1-octene or 1-decene.
Suitable dihients for use as the liquid medium are well known in the art and include hydrocarbons, which are inert and liquid under reaction conditions. Suitable

hydrocarbons include isobutane, propane, n-pentane, i-pentane, neopentane and n-hexane, with isobutane being especially preferred. Additional details regarding loop reactor apparatus and polymerization processes may be found in U.S. Patent Nos. 4.674,290; 5,183,866; 5,455,314; 5,565,174; 5,624,877; 6,005,061; 6,045,661; 6,051,631; 6,114,501; 6,262,191; and 6,420,497, which are incorporated by reference herein.
Additionally, the present techniques for controlling heavies may be employed where the monomer is the liquid medium for the polymerization. For example, the present techniques may be used for the polymerization of propylene where propylene is the liquid medium and an inert diluent is not present in any substantial amount. A diluent may still be used for the catalyst. For illustration, but not as a limitation, the present invention will be described in connection with a polyethylene process using an inert diluent as the liquid medium, but it is to be understood that the present invention may also be employed where the monomer is used as the liquid medium and would take the place of the diluent in the following descriptions,
FIG. 1 is a representation of a slurry polymerization system 10 according to the present invention. The slurry polymerization system 10 includes a catalyst feed tank 12 (such as a catalyst mudpot or an agitated tank) containing a mixture of catalyst and diluent. Catalyst and diluent from the catalyst tank 12 are pumped into a loop reactor 14. FIG. 1 also shows flashline heaters 16, a flash gas separator (also described as an intermediate pressure flash chamber) 18, a heavies removal system 20, a fluff chamber 22, a purge column 24, a recycle treater 26, an isobutane/nitrogen recovery unit (INRU) 28, a recycle tank 30, a heavies column 32, a lights column 34, an olefin free surge unit 36, and a series of conduits, pumps and condensers. For the sake of simplicity, some components unrelated to the claimed systems and processes and/or that are related to production or routine details, such as mtervening valves and connecting lines/conduits of the slurry polymerization system 10, are not shown.
Catalyst or catalyst and diluent from the catalyst feed tank 12 passes through conduit 40 and is piunped into the loop reactor 14 by pump 42. Suitable catalysts are well known in the art. For example, chromium oxide on a support such as silica may be used, as disclosed in United States Patent No. 2,825,721, issued to Hogan and

Banlcs, which is hereia incorporated by reference m its entirety. Additionally, other catalysts well known in the art (for example, Ziegler catalysts, metallocene catalysts) may also be used for olefin polymerization.
The slurry polymerization system 10 also includes a monomer feed 38. A monomer such as ethylene, for example, is introduced into the loop reactor 14. Additional conduits and lines may supply monomer and/or diluent into the loop reactor 14 or join in a line 46 for introducing a combined stream of fiesh e&ylene and diluent recycle as shown. Monomer, diluent, catalyst and any other feed materials may be introduced into the loop reactor 14 at one or several points.
As shown m FIG. 1, the loop reactor 14 may comprise a plurality of vertical members 48 formed integrally with horizontal members 50 (or curved connecting members), hi order to maximize heat transfer within the reactor 14, the distance between vertical members 48 is preferably minimized. Thus, the horizontal members 50 may be of minimal length. Alternatively, the horizontal members 50 may be eliminated such that the vertical members 48 are connected through curved connecting members. Altematively, the loop reactor may be substantially horizontal and not have any vertical members. The longer members 48 preferably have heat exchange jackets 49. The vertical members 48 and horizontal members 50 (or curved connecting members) define a loop reaction zone. The loop reaction zone may include more or fewer vertical members 48 and correspondmg horizontal members 50 as that shown m FIG. 1. Further, the loop reactor may be oriented vertically or horizontally (for example, by rotating reactor 14 in FIG. 1 by 90 degrees) or may be entirely horizontal, with no vertical members. The connecting members 50 may be any sh^e or form that connects the vertical segments 48 and allows fluid to flow therebetween.
An unpeller is located in the loop reactor 14 to circulate the slurry. The unpeller is driven by a motor 47. The raipeller is located in the interior of the loop reaction zone defined by the vertical members 48 and the horizontal members 50. The impeller 47 is operable to circulate fluid slurry, comprising liquid diluent and solid olefin polymer particles, through the loop reactor 14.

An intennediate product slurry, comprising the liquid medium and solid polymer particles, is withdrawn, or taken off, from the loop reactor 14 by way of the continuous take-off devices 52. A continuous take-off device 52 is disclosed in U.S. Patent No. 6,239,235, which is incorporated by reference herein. The slurry polymerization system 10 may include more or fewer than the continuous take-off devices 52 (and correspondit^ conduits and flashline heaters 16) shown in FIG. 1. For example, one, two, three or more continuous take-off devices 52 may be used. Further, the continuous take-off devices 52 may be tangentially positioned on curved members. The continuous take-oflf devices 52 may be positioned anywhere on the loop reactor 14. Alternatively, settling legs may be used in conjunction with, or instead of, the continuous take-off devices 52.
As flxiid slurry is withdrawn from the loop reactor 14 as uitermediate product slurry, the intennediate product slurry is passed from the continuous take off-device 52 to a flashline 54, which forms a first fluid passage for the withdrawn portion of the slurry to downstream processing apparatus. The flashline 54 may be provided with a flashline heater 16 surrounding at least a portion of the flashline 54. The flashline heater 16 contains a heated fluid (for example, steam) that provides indirect heating to the contents of the flashline 54, such that intennediate product slurry that passes flirough the flashline 54 is heated. Preferably, the intermediate product slurry is heated such that at least a majority of the liquid diluent is vaporized, thereby yielding diluent vapor and a post-flashline slurry. The post-flashline slurry comprises the solid polymer particles and a reduced amount of liquid diluent (as compared to the intermediate product slurry). Alternatively, the post-flashline slurry may be heated such that less than a majority of the liquid diluent is vaporized. Preferably, the intennediate product slurry is heated in the flashline 54 such that, as it enters the flash gas separator 18, essentially all of the liquid diluent has been vaporized ("flashed") within the flashline 54. The "flashing" tends to occur as the intennediate product slurry passes across the continuous take-off device 52 and the flashUne 54. Preferably, the intermediate product sluny is heated in the flashline 54 to fully vaporize the diluent liquids so that the solids and vapors that discharge into the flash gas separator 18 are free of Uquids.

la some systems utilizing a flashline heater 16, some or all of fee diluent (or other liquid medium) will flash in flashline 54 prior to introduction to the flash gas separator 18, which may be termed a "flash chamber" or an "intermediate pressure flash chamber." These terms still are frequently used for the tank that follows the flashline, where vaporized diluent separates from polymer solids. "Flash tank" or "flash chamber" are still used even though there may be little or no flashing in the flash tank if all or substantially all of the diluent is vaporized in the flashline. In current designs that have the flashlines discharging at higher pressures and without downstream drying devices, it is intended to design the flashlines so there is little or no pressure drop on entering the flash tank, with essentially all of the liquids vaporized prior to entering the vessel.
After the intermediate product slurry passes through the flashline 54, the resulting post-flashline fluff and vaorized diluent is passed into the flash gas separator' tank or chamber 18, The flash gas separator 18 preferably is at an intermediate pressure, lower than the pressure in the reactor but higher than the pressure of downstream apparatus. Preferably the flash gas separator 18 is at a pressure whereby the separated flash gas (or a majority or other large portion) may be condensed by heat exchange without compression. In the flash gas separator 18, most of the diluent, unreacted monomer, and heavies form a vapor stream (flash gas) that rises toward a top portion of the flash gas separator 18, while "fluff falls to a bottom portion of the flash gas separator 18. The fluff comprises solid polyma:, which may have trace or other small amounts of diluent entrained therein.
The fluff may pass to a second flash gas separator (for example, a low pressure flash chamber). A two-stage flash system is disclosed in U.S. Patent No. 4,424,341, which is incorporated by reference herein. Alternatively, the fluff may pass from a bottom portion of the first flash chamber to the purge column 24. (The purge column 24 may follow the second flash chamber instead). Alternatively, the fluff may be passed through a conveyor dryer and then to a purge column as described in U.S. Patent No. 4,501,885, which is incorporated by reference herein. Entrained diluent within the polymer particles is separated from the fluff in the purge column 24 by passing nitrogen gas through the solid polymer particles (the fluff). The nitrogen

extracts entrained diluent and/or liquid diluent, thereby leaving solid polymer essentially ftoe of entrained diluent. The solid polymer is then d^osited, collected, ejected or otherwise withdrawn from a bottom portion of the purge column 24.
The nitrogen and extracted diluent are then passed out a top portion of the purge column 24 to an isobutane/nitrogen recovery unit (INRU) 28. The INRU processes the vapors removed from the fluff in the purge column. The INRU separates the nitrogen from the diluent vt^jors by condensing the diluent vapors into liquids, hi one sense the INRU functions somewhat like the heavies removal system by condensing a relatively small amount of the flash gas and sending a liquid to the heavies column. The INRU 28 separates nitrogen from diluent and other hydrocarbons. The nitrogen is then passed back to the purge column 24 through a nitrogen return line 60. The separated diluent and other hydrocarbons may be returned to the recycle taiik 30 and ultimately returned to the loop reactor 14. Alternatively, some or all of the liquids from the INRU 28 may be sent to the heavies column 32, The INRU is designed to produce a liquid product which contains substantially all the hydrocarbons (but not the solid polymer particles) removed in the purge colunm.
The vapor stream which has been vaporized either in the flashline 54 and/or in the flash gas separator 18, which is also referred to herein as the first vapor stream, is passed to the heavies removal system 20 by way of va^or ranoval line 56. The v^or removal line 56 may include a series of filters and components, such as bag filters, for filtering fine polymer particles torn the vapor stream in order to prevent the fines fix)m altering tiie heavies removal system 20. For example, for a suitable polyethylene process, the vapor stream is primarily isobutane diluent, but the vapor stream diluent also contains heavies, such as 1-hexene co-monomers and other hydrocarbons having six or more carbon atoms. The vapor stream may also contain lighter hydrocarbons such as efriane and ethylene.
FIG. 2 is a representation of an exemplary heavies removal system 20. The heavies removal system 20 is fluidly connected to, and communicates with, a top portion of the flash gas separator 18 through the v^or removal line 56. In the equipment shown in FIG. 2, the heavies removal system 20 includes a first condenser

62, a bypass line 63, a bypass valve 64, a static mixer 66, a liquid collection talk 68, a temperature controller 70, a level controller 72, a pump 74, a flow controller 76 and a flow control valve 78.
The heavies removal system 20 is designed and/or set so as to condense a small amount of liquid fom the first vapor stream. A fraction of flash gas (in other words, a first portion of the first vapor stream) is passed through the condenser 62, which condenses some of that fraction into a liquid. When the liquid fix>m condenser 62 contacts the relatively hot flash gas that has bypassed the condenser 62 (in other words, a second portion of the first vapor stream), some of the liquid again vaporizes, leaving a residual amount of liquid and a larger amount of flash gas. The liquid and flash gas are passed to the liquid collection tank 68. A static mixer 66 can be used to assure proper contact, rapid revaporization and equilibrium conditions in the liquid collection tank 68. The rate of flow may be set on flow controller 76. The level in the liquid collection tank 68 is determined by the amount of liquid generated by the condenser 62. If the liquid level in the collection tank 68 rises, the temperature controller 70 adjusts to a higher temperature to decrease the amount of liquids generated by the condenser 62. Conversely, if the level within the liquid collection tank 68 decreases, the level controller 72 acts to decrease the temperature set point on the temperature controller 70, thereby directing more flow througji the condenser 62 to generate more liquids. Consequently, the level controller adjusts the temperature controller to generate an amount of liquids that matches flie desired amount of liquids as set by the flow controller. This provides an efficient and relatively easy way to control the amount of liquid condensed firom the first vapor stream.
As seen in FIG. I, the condenser 62 of the heavies removal system 20 is in addition to flash gas condenser 84. The heavies removal system 20 will generally be used to condense a relatively small amount of the total vapor fi-om vapor removal line (in other words, of the first vapor stream). For example, the heavies removal system 20 may condense (in other words, form a liquid from) as little as about 1% or less of the total vapor stream firom the first flash chamber. One may desire to set a maximum for the amount of the first vapor stream condensed by the first condenser. For example, the heavies removal system 20 may be set to condense at most about 10%,

alternatively at most about 5%, alternatively at most about 4%, alternatively at most about 3% of the first vapor stream. Condenser 62 may condense from about 0.1 to about 15% of the flash gas. The amount of liquid condensed by cond^ser 62 may be up to 5 times greater than the liquid generated by the heavies removal system 20.
i The heavies removal system 20 produces liquid with a higher percentage of
the heavier components than is found in the vapor stream. For example, the liquid in the collection tank 68 may contain at least about 1%, alternatively at least about 5%, alternatively at least about 10%, of the heavies in the vapor stream. In particular, the heavies removal system is expected to be particularly effective in removing most oligomers, for example, at least about 2%, alternatively at least about 10%, alternatively about 20% of the oligomers in the vapor stream. Even if the heavies removal system does not remove all the heavies from the liquid medium to be recycled to the polymerization reactor, it still provides an important benefit by preventing an excessive buildup of heavies hi the recycled medium.
The liquid concentrated in heavies may be referred to as a heavies liquid. The heavies liquid is routed to a heavies column where the heavier components can be removed from the process. Thus the concentration of heavier components in the flash gas is decreased from levels that would otherwise exist.
The present process and system result in the generation of a recycle diluent stream having fewer heavies than would otherwise build up in the recycle diluent stream. This system can work in conjunction with a direct recycle process, allowing most of the diluent to be condensed and recycled directly back to the reactor without passing through fractionation columns that remove heavier and lighter components, hi the direct recycle process it is desirable that only a fraction of the total recycle diluent is sent to fiiactionation where heavier components can be rejected and lights can be removed and olefin-free diluent generated. With only a fraction of the recycle diluent feeding fractionation, the fractionation columns can be relatively small.
As shown in FIG. 2, the condenser 62 is in fluid coimection with the vapour removal line 56 and is upstream from the static mixer 66. The bypass valve 64 is interposed within the bypass line 63 such that the bypass valve 64 may selectively open and close the bypass line 63, thereby controlling the flow of vapor through the

bypass line 63. The liquid collection talk 68 is downstream from the static mixer 66. A diluent recycle line 80 is in fluid communication with the liquid collection tank 68 and connects the liquid collection tank 68 to a recycle tank 30. The bypass valve 64 may be in informational communication with the temperature controller 70, which is interposed within the diluent recycle line 70. Additionally, or alternatively, the bypass valve may be in informational communication with the level controller 72, which is positioned within the liquid collection tank 68. The temperature controller 70 and the level controller 72 may be assisted by or used in conjunction wifli a central processing unit or other logic unit or main controller. The temperature controller 70 and the level controller 72 relay signals to the bypass valve 64 to close or open the bypass line 63, depending on temperature and level conditions wthiin the heavies removal Systran 20. This control scheme permits automatic control to obtain the desired amount of liquid in the liquid collection tank 68,
The bottom portion of the liquid collection tank 68 is in fluid communication with a heavies delivery line 82, which receives a hquid concentrated in heavies from the liquid collection tank 68. A pump 74 may be positioned in the heavies delivery Ime 82, which provides sufBcient force to move the liquid concentrated in heavies through the heavies delivery line 82 to the heavies column 32. A flow controller 76, which may be assisted by or used in conjunction with a central processing unit or logic unit or a main controller, is positioned downstream from the pump 74 and is in informational communication with the flow control valve 78, which may selectively open and close the heavies delivery Ime 82. The flow control valve 78 may be operated in conjunction with the flow controller 76. Depending on the rate of flow of heavies through the heavies delivery line 82, the flow controller 76 may send a command signal to the flow control valve 78 to open or close the heavies delivery line 82.
The heavies removal system 20 is used to produce a liquids stream relatively rich in heavier components. Once the heavies or a portion of heavies are removed, the diluent may be recycled and returned to the loop reactor 14. The heavies removal system 20 does not necessarily remove all heavies. Rather, the heavies removal system 20 may only remove a small portion of the heavies in order to limit potential

build-up of heavies to relatively low levels. In particular, the heavies removal system can limit the build-up of oligomers.
The heavies removal system 20 is configured to produce liquids relatively concentrated ui heavies that were contained within the first vapor stream. It is contemplated that at least some of the heavies from the first vapor stream, or a major portion thereof, will be passed to the heavies delivery line 82. For example, about 98% of the first vapor stream may remain as a vapor as a result of bypassing the first condenser, in other words only a small amount of liquids are generated. A portion of the first vapor stream is sent to the condenser where all or most of that portion is converted to liquid. This colder liquid is combmed with the hotter gases that bypassed the condenser and this liquid and vapor mixture is sent to the static mixer 66. The static mixer ensures good mixing of the liquids and vapors so that substantially equilibrium conditions can quickly be generated.
Substantially equilibrium conditions means that the liquid and vapor in the liquid collection tank come to substantially the same temperature with some of the liquids vaporizing to accomplish this. The gas may then be passed to collection tank where the liquids and vapors initially intermingle but also are separated. As fiash gas condenses and re-evaporates, heavies are left behind in the liquid at the bottom of the collection tank.
The amount of the first vqjor stream that is diverted into the condenser 62 is controlled to generate a desired amount of liquids in the liquid collection tank 68. The bypassed hot vapor and condenser-cooled liquid from the condenser 62 are then mixed by the static mixer 66. The temperature controller 70 may signal the bypass valve 64 to open or close to a desired extent, depending on the temperature of the diluent vapor in the diluent recycle line 80.
After the flash gas vapor and condensed liquid are mixed together to form a mixture, the mixture is passed into the liquid collection tank 68. The liquid collection tank 68 separates the liquids containing a higher concentration of the heavier components from the diluent vapor. It is desirable to reduce or avoid pressure or temperature gradients in the liquid collection tank.

The temperature controller 70 can be periodically or occasionally reset by the level controller on the collection tank. If the level in the collection tank drops below the level setpoint, the controller sends a signal to lower the setpoint of the temperature controller which in turn sends a signal to close the bypass valve to a desired extent and force more flow through the condenser to generate more liquids. Conversely, if the level in the tank is above the desired setpoint, the level controller sends a signal to raise the setpoint of the temperature controller which in turns sends a signal to open the bypass valves to a desired extent which decreases the flow through the condenser which reduces the amount of liquids formed. When the setoint of the flow controller is changed, the flow control valve opens or closes to produce the desired flow, and this change of flow is reflected as a change in level in the tank, and the level controller reacts to change the amount of liquids condensed.
The liquid concentrated in heavies is passed from the liquid collection tank 68 througih the heavies delivery line 82 and pumped towards the heavies column 32 by ' the pimip 74. The flow controller 76 monitors and controls the flow of the liquid through the heavies delivery line 82 by signaling the flow control valve 78 to open or close the flow control valve 78, depending on the desired amount of liquids to be generated. For example, if the operators want to create 1500 kg/hr liquids, it is desirable that that number can be entered as a setpoint to the flow controller. The liquids are ultimately delivered to the heavies column 32.
Referring again to FIG. 1, the heavies column 32 separates the Uquid medium and lighter components from the heavies. The diluent (in other words, the liquid mediimi) extracted in the heavies column 32 is then passed to a lights column 34, where lights are removed, thereby yielding essentially or substantially pure diluent, which is then passed through the olefln-free surge 36 and pumped to the catalyst feed tank 12 or to the recycle tank 30, and it is then pumped to the loop reactor 14.
The diluent vapor within the diluent recycle line 80 is passed through a flash gas condenser 84, which may condense, or liquefy, the diluent. Some diluent with a relatively high concentration of lighter components may remain as vapor. The stream is passed to the recycle tank 30, which serves as a vapor-Uquid separation drum and the liquids are passed direcfly back to the loop reactor 14 through the recycle treater

26. The vapor which has a higher relative concentration of the lighter components is passed to fractionation where the light components are rejected, and 1-hexene and hexanes are recovered or rejected, octane and heavier compounds are rejected, and diluent (usually isobutane) is recovered free of olefins
i FIG. 3 is a sdiematic representation of another slurry polymerization system
11, which includes a novel heavies removal system. As shown in FIG. 3, the lights removal line 86 may be a vapor line that enters through the side of the heavies colmnn 32. Since vapor line 86 will contain small amounts of hexane, it is desirable to have it enter the heavies column because all hexanes must be excluded from the lights column. Also, there is a liquid product line 90 extending from the JNBJJ 28. The INRU is designed to recover both nitrogen and hydrocarbons (diluent) as liquid. The liquid product line 90 may be split with one branch connecting to the heavies column 32 and another branch connecting to the recycle tank 30. In this way, liquids may be directed to the heavies column 32 and/or to the recycle tank 30. Also, the olefin-free product that is passed from the olefin-fiee surge unit 36 may be pxmiped back to the recycle tank 30 in addition to the catalyst mix tank 12.
Thus, the present invention provides a more efficient system and process of recycling the liquid medium in a slurry polymerization process. The present invention provides an improved heavies removal system and process, which removes a greater amount of heavies, as compared to prior systems, from the liquid medium that is to be recycled to the reactor. A direct recycle system is provided where most or all of the liquid in the reactor effluait (diluent and other hydrocarbons) is separated from the fluff, condaised and recycled back to the reactor without passing through purification (fractionation) steps. Other systems pass substantially all of the diluent v^or (reactor effluent) through fractionation (purification steps) where all of the heavier compounds can be separated. In a direct recycle system there is a desire to reject heavier components as well as lighter components so they do not concentrate in the process and harm the reactor or product. So in the direct recycle process some recycle diluent (in other words, reactor effluent hydrocarbons) are still processed in a small purification (fractionation) section to generate some pure (olefin-free) diluent for use as catalyst diluent, and to reject some heavy and light components to prevent

abnormal build up or concentration. By fractionating only a small portion of the diluent recycle, the fractionators can be smaller. The direct recycle fractionators can be fed from a recycle liquid slip stream or by INRU liquid product but by creating liquids with the present heavies removal system, heavies concentration is controlled better, in other words for the same fractionation feed rate, heavies concentration in the recycle is lower.
The present system and process described may also feed fractionation (heavies and lights columns) when the INRU is not operational so that olefin-free diluent may be generated to slurry the catalyst.
While the invention has been described with reference to certain embodiments, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted without departing from the scope of the invention, in addition, many modifications may be made to adapt a particular situation or material to the teachings of the invention without departing from its scope. Therefore, it is intended that the invention not be limited to the particular embodiment disclosed, but that the invention will include allembodiments falling within the scope of the appended claims.

WE CLAIM :
1. A recovery and purification system for a liquid medium from a slurry polymerization, the
system comprising:
a flashline (16) configured to pass an intermediate product slurry from a slurry polymerization reactor (14) to a flash gas separator (18);
the flash gas separator (18) configured to separate a vapor stream (56);
a first condenser (62) disposed downstream of the flash gas separator and configured to partially condense a first portion of the vapor stream;
a vapor bypass line(63) configured to pass a second portion of the vapor stream around the first condenser;
a bypass valve (64) configured to facilitate control of the flow rate of the second portion of the vapor stream through the vapor bypass line;
a collection tank (68) disposed downstream of the first condenser and configured to receive the partially-condensed first portion of the vapor stream from the first condenser and to receive the second portion of the vapor stream bypassed around the first condenser;
a second condenser (84) configured to condense a second vapor stream (80) discharged from a top portion of the collection tank;
a recycle tank (30) configured to receive the condensed second vapor stream from the second condenser;
a diluent recycle line (starting at bottom of 30) configured to facilitate recycle of diluent fi"om the recycle tank to the slurry polymerization reactor;
a liquid delivery line (82) coupled to a bottom portion of the collection tank and configured to pass a liquid stream from the collection tank to a fractionation system (32, 34).
2. The recovery and purification system as claimed in claim 1, wherein the bypass valve is
in informational communication with a temperature controller configured to indicate

temperature of the second vapor stream discharged from the top portion of the collection tanic, or wherein the bypass valve is in informational communication with a level controller configured to indicate a level of liquid in-the collection tank, or a combination thereof
3. The recovery and purification system as claimed in claim 2, wherein the level controller is in informational communication with the temperature controller, and the temperature controller is in informational communication with the bypass valve.
4. The recovery and purification system as claimed in claim 1, wherein the fractionation system comprises a heavies column coupled to the liquid delivery line.
5. The recovery and purification system as claimed in claim 4 comprising a flow controller disposed along the liquid delivery line.
6. The recovery and purification system as claimed in claim 4 comprising a pump disposed along the liquid delivery line for propelling the liquid into the heavies column.
7. The recovery and purification system as claimed in claim 1 comprising a static mixer disposed downstream of the first condenser and upstream of^ the collection tank, wherein the static mixer is configured to mix the partially-condensed first portion of the vapor stream and the second portion of the vapor stream.
8. The recovery and purification system as claimed in claim 1 comprising a purge column configured-to receive solid polymer particles from the flash gas separator.
9. A process for recycling a liquid medium withdrawn from a slurry polymerization reactor,

the method comprising:
discharging a slurry from a slurry polymerization reactor, wherein the slurry comprises a liquid medium and solid polymer particles, the liquid medium comprising a diluent;
passing the slurry thought a flashline to flash at least a portion of the liquid medium;
separating a first vapor stream from the slurry, wherein the first vapor stream comprises diluent, light components lighter than the diluent, and heavy components heavier than the diluent
at least partially condensing a first portion of the first vapor stream in a first condensing zone to form a first liquid;
passing a second portion of the first vapor stream to a collection zone without passing the second portion through the first condensing zone;
separating a second liquid and a second vapor stream in the liquid collection zone; passing the second liquid to a purification zone configured to remove at least heavy components heavier than the diluent firom the second liquid; and
at least partially condensing the second vapor stream to form a third liquid;
recycling the third liquid to the slurry polymerization reactor without fractionating the third liquid to remove heavies.
10. The recycling process as claimed in claim 9 comprising the step of mixing together the first liquid and the second portion of the first vapor stream before passing the first liquid and the second portion to the collection zone.
11. The recycling process as claimed in claim 9, wherein the separating a first vapor stream from the slurry yields solid polymer fluff having entrained diluent and the method comprisesf passing the solid polymer fluff from the flashing step to a purge zone wherein the purge zone extracts entrained diluent from the solid polymer fluff.

12. The recycling process as claimed in claim 9 wherein at least about 1% of the heavy components in the first vapor stream are condensed into the second liquid.
13. The recycling process as claimed in claim 9 wherein at least about 5% of the heavy components in the first vapor stream are condensed into the second liquid.
14. The recycling process as claimed in claim 9 wherein at least about 10% of the heavy components in the first vapor stream are condensed into the second liquid.
15. The recycling process as claimed in claim 9 wherein at least about 2% of the oligomers in the first vapor stream are condensed into the second liquid.
16. The recycling process as claimed in claim 9 wherein at least about 10% of the oligomers in the first vapor stream are condensed into the second liquid.
17. The recycling process as claimed in claim 9 wherein at least about 20% of the oligomers in the first vapor stream are condensed into the second liquid.
18. The recycling process as claimed in claim 9 comprising
measuring the level of liquid in the liquid collection zone; and
controlling the condensing of the vapor stream based on the measured liquid level.
19. A process for operating a slurry polymerization system, the process comprising the steps
of:
forming a slurry comprising solid polyolefin particles in a liquid mediimi in a polymerization reaction zone, wherein the liquid medium comprises at least diluent, monomer, and heavies;

withdrawing a portion of the slurry from the polymerization reaction zone;
vaporizing the liquid medium to form a first vapor stream comprising at least diluent and heavies, wherein the heavies are components heavier than the diluent;
separating the first vapor stream from the solid polyolefin particles;
passing a first portion of the first vapor stream to a condensation zone whereby a first liquid stream is formed;
passing a second portion of the vapor stream to a collection zone without passing the second portion through the condensation zone;
collecting the first liquid stream and the second portion in the liquid collection zone;
separating a second vapor stream-and a second liquid stream in the liquid collection zone;
condensing and recycling the second vapor stream back into the polymerization reaction zone without heavies removal treatment; and
passing the second liquid stream to heavies removal treatment.
20. The operating process as claimed in claim 19 wherein the diluent comprises isobutane, the monomer comprises ethylene, and the solid polyolefin particles comprise polyethylene.
21. The operating process as claimed in claim 19 wherein the diluent and monomer comprise propylene, and the solid polyolefin particles- comprise polypropylene.
22. The operating process as claimed in claim 19 comprising passing the solid polyolefin particles to a purging step, where entrained diluent is extracted from the solid polyolefin particles.
23. The operating process as claimed in claim 19 comprising measuring the level of liquid in the liquid collection zone and controlling the condensing of the first vapor stream based on the measured liquid level.

24. The operating process as claimed in claim 19 passing, wherein passing the second liquid
stream to heavies removal treatment comprises passing the second liquid stream from the
collection zone to a heavies fractionation column.
25. The operating process as claimed in claim 19 comprising the steps of:
measuring the temperature of the vapor in the liquid collection zone; and
adjusting the amount of the first vapor sfream being passed to the condensation zone in response to the measured temperature.
26. The operating process as claimed in claim 19 wherein the liquid removed from the collection zone contains at least about 1% of the heavies in the first vapor stream.
27. The operating process as claimed in claim 19 wherein the liquid removed from the collection zone contains at least about 5% of the heavies in the first vapor stream.
28. The operating process as claimed in claim 19 wherein the liquid removed from the collection zone contains at least about 10% of the heavies in the first vapor stream.
29. The operating process as claimed in claim 19 wherein the liquid removed from the collection zone contains at least about 2% of the oligomers in the first vapor stream.
30. The operating process as claimed in claim 19 wherein the liquid removed from the collection zone contains at least about 10% of the heavies in the first vapor stream.
31. The operating process as claimed in claim 19 wherein the liquid removed from the collection zone contains at least about 20% of the heavies in the first vapor stream.

32. The operating process as claimed in claim 19 wherein essentially all the heavies removed
from the liquid collection zone are removed in liquid form.
33. The operating process as claimed in claim 19 wherein the second liquid stream is held in
the liquid collection zone for a time sufficient to allow heavies from the vapor to transfer to the
liquid.

Documents:

0617-chenp-2005 abstract.jpg

0617-chenp-2005 abstract.pdf

0617-chenp-2005 claims.pdf

0617-chenp-2005 correspondence-others.pdf

0617-chenp-2005 correspondence-po.pdf

0617-chenp-2005 description (complete).pdf

0617-chenp-2005 drawings-duplicate.pdf

0617-chenp-2005 form-1.pdf

0617-chenp-2005 form-18.pdf

0617-chenp-2005 form-26.pdf

0617-chenp-2005 form-3.pdf

0617-chenp-2005 form-5.pdf

0617-chenp-2005 others.pdf

0617-chenp-2005 abstract-duplicate.pdf

0617-chenp-2005 claims-duplicate.pdf

0617-chenp-2005 description (complete)-duplicate.pdf

0617-chenp-2005 drawings.pdf

0617-chenp-2005 pct.pdf

« Previous Patent

Next Patent »

Patent Number

219777

Indian Patent Application Number

617/CHENP/2005

PG Journal Number

27/2008

Publication Date

04-Jul-2008

Grant Date

13-May-2008

Date of Filing

12-Apr-2005

Name of Patentee

CHEVRON PHILLIPS CHEMICAL COMPANY LP

Applicant Address

Inventors:

#	Inventor's Name	Inventor's Address
1	VERSER, Donald, W
2	BURNS, David, H

PCT International Classification Number

B01J 8/00

PCT International Application Number

PCT/US2003/029334

PCT International Filing date

2003-09-15

PCT Conventions:

#	PCT Application Number	Date of Convention	Priority Country
1	60/411,254	2002-09-16	U.S.A.
2	10/662,249	2003-09-15	U.S.A.