Title of Invention	"A PROCESS FOR PREPARING 4 AMINODIPHENYLAMINE"
Abstract	A process for preparing 4-aminodiphenylamine using nitrobenzene and aniline as raw materials, a complex base catalyst as the condensation catalyst, and a powdery composite catalyst as the hydrogenation catalyst. The process has 5 process stages including condensation, hydrogenation, separation I, separation II, and refining. The diagrammatical representation of the process is as in fig 1.

Full Text

Technical field The present invention relates to a process for preparing 4-aminodiphenylamine. In particular, the present invention relates to a continuous process for preparing 4-aminodiphenylamine, which process uses nitrobenzene and aniline as raw materials, a complex base catalyst as condensation catalyst and a powdery composite catalyst as hydrogenation catalyst, and comprises five process stages: condensation; hydrogenation; separating, recovering and reusing the complex base catalyst and separating, recovering and reusing the powdery composite catalyst which is optionally at least partially regenerated; separating, recovering and reusing aniline and optionally separating, recovering and reusing hydrogenation solvent; and refining. Background of the Invention 4-Aminodiphenylamine is an important intermediate of antioxidant and stabilizer, and is an important chemical product for rubber industry and polymer industry. Depending on starting materials, current methods for preparing 4-aminodiphenylamine include: (1) aniline method, wherein p-nitro-chlorobenzene and aniline as raw materials react in the presence of a catalyst to produce 4-nitrodiphenylamine, then 4-nitrodiphenylamine is reduced by sodium sulfide to form 4-aminodiphenylamine; (2) formanilide method, wherein formic acid and aniline are used as starting materials to prepare formanilide, which in turn reacts with p-nitro-chlorobenzene in the presence of an acid-binding agent such as potassium carbonate, to produce 4-nitrodiphenylamine, and then 4-nitrodiphenylamine is reduced by sodium sulfide to form 4-aminodiphenylamine; (3) diphenylamine method, wherein diphenylamine as raw material is nitrosated using a nitrite in an organic solvent to produce N-nitrosodiphenyamine, which rearranged to 4-nitrosodiphenyamine hydrochloride under the action of anhydrous hydrogen chloride, then 4-nitrosodiphenyamine hydrochloride is neutralized with a base to give 4-nitrosodiphenyamine, and said 4-nitrosodiphenyamine is finally reduced to 4-aminodiphenylamine by sodium sulfide. Although these methods use different starting materials, traditional sodium sulfide is used as reducing agent to prepare 4-aminodiphenylamine. These reactions suffers from severe reaction conditions, complex operation, higher energy consumption, lower yield, higher cost and environment pollution caused by concomitant waste water, waste gas and waste residue. Among the preparation methods of 4-aminodiphenylamine, another method utilizes nitrobenzene or nitrobenzene and aniline or nitrosobenzene as raw materials to carry out condensation reaction, and then utilizes hydrogen gas to perform hydrogenation to produce 4-aminodiphenylamine. In fact, it was reported in 1901 (Wohl, Chemische Berichte, 34, p. 2442 (1901)) and in 1903 (Wohl, Chemische Berichte, 36, p. 4135 (1903)) that nitrobenzene reacted with aniline under the action of a base to form 4-nitrosodiphenylamine and 4-nitrodiphenylamine. However, said method is neither attached importance to nor developed because of its relatively low yield until 1990s when it is researched and developed again and achieved some progresses (See DEI 9734055.5, DE19810929.6, and DEI9709124.5). The disclosed methods share the following disadvantages: 1) catalysts used are expensive so as to result in relatively high production cost when said catalysts are used in industrial scale production, so that said methods have no advantage in comparison with the current production techniques. For example, tetraalkyl ammonium hydroxide and fluoride used in condensation reaction and noble metal, such as palladium, platinum, rhodium, and the like, used in hydrogenation reaction are expensive. The instability of tetraalkyl ammonium hydroxide imparts some difficulty to recovery and reuse of tetraalkyl ammonium hydroxide. The use of noble metal hydrogenation catalysts applies higher requirements to raw materials and equipment; 2) the yield is relatively low, and only suitable for laboratory research. This is an important reason why said methods are very difficult to be industrialized; 3) operation is complexed, and this isn't in favor of continuous operation and limits the production scale; 4) separation is difficult and purity of product is not high. US 6,395,933 discloses a process for synthesizing 4-aminodiphenylamine by reacting nitrobenzene and a substituted aniline at a certain temperature in the presence of a strong base and a phase-transfer catalyst. The process is not satisfactory in yield and there are many side reactions. In the mixture of 4-nitrodiphenylamine and 4-nitrosodiphenylamine produced, the proportion of 4-nitrodiphenylamine is too high so that too much hydrogen is consumed during hydrogenation reaction and the production cost is thereby increased. Furthermore, said process needs an oxidizing agent so that it is not suitable for industrial production. EP 0566783 describes an example that demonstrates a reaction of a base, tetrabutyl bisulfate, nitrobenzene and aniline, but the reaction has the same drawbacks of low yield and being difficult to be industrialized. WO9300324 discloses a process for preparing 4-aminodiphenylamine by reacting nitrobenzene and aniline at a proper temperature in a proper solvent in the presence of a base with the content of proton materials in solution being controlled. Said process requires a solvent and has to control the content of proton materials in solution. The introduction of the solvent results in the increment of energy consumption and separation difficulty. Controlling the content of proton materials gives rise to difficulty of operating and controlling the reaction. In particular, at the later stage of condensation reaction, controlling the content of proton materials, which mainly means dehydrating to lower water content, will prolong reaction time and partial aniline will be entrained out. The later stage, the more difficult removing the proton materials. Controlling the proton materials at a certain range is difficult, and goes against industrial production. The expensive tetraalkyl quaternary amine base catalyst will quickly decompose in the course of controlling the content of proton materials to a range of from 0.5 to 4 percent, resulting in the increment of the production cost. US 5,453,541 and US 5,739,403 also mentions the control of the content of proton solvent, but it is necessary to increase temperature and to prolong reaction time to lower the content of proton solvent, and this is very unfavorable for tetraalkylammonium hydroxide catalyst that is relatively costly and easy to decompose. Among hydrogenation catalysts, powdery nickel catalyst is commonly used in industry and can be conventionally prepared, as described in US 6,395,934. However, in a continuous completely back mixing reactor, the powdery catalyst as hydrogenation catalyst will inevitably entrained by an effluent during the reaction, resulting in increased consumption of the hydrogenation catalyst, while this portion of the catalyst is actually not deactivated and can be further utilized. In industry, the catalyst is generally recycled by settlement, but desired effect is difficult to be achieved in a system that is well back mixed by stirring. Filtering operation also suffers from some inconveniences in a hydrogenation system under pressure. Therefore, it is a key of the preparation of hydrogenation catalyst to increase magnetism of the catalyst by adding appropriate component during the preparation of the hydrogenation catalyst so as to fulfill the purpose of enabling the recycle of the catalyst in the reaction system. Summary of the Invention The invention aims at the selection of inexpensive catalysts with good performance used in condensation and hydrogenation reactions and at the selection of a process suitable for industrial scale production, to continuously produce 4-aminodiphenylamine. The present invention uses a complex base catalyst as condensation catalyst and a powdery composite catalyst as hydrogenation catalyst, to prepare 4-aminodiphenylamine in a continuous process comprising five process stages of condensation; hydrogenation; separation I (separating, recovering and reusing the complex base catalyst and separating, recovering and reusing the powdery composite catalyst which is optionally at least partially regenerated); separation II (separating, recovering and reusing aniline and optionally separating, recovering and reusing hydrogenation solvent); and refining. Brief description of the figures Figure 1 is a flowchart showing an embodiment of the process for preparing 4-aminodiphenylamine according to the present invention. Figure 2 is a schematic diagram illustrating a gas-aid falling film evaporator used in an embodiment of the present invention. Detailed description of the invention In the process according to the present invention, "separation I" means separating, recovering and reusing complex base catalyst and separating, recovering and reusing powdery composite catalyst which is optionally at least partially regenerated; and "separation II" means separating, recovering and reusing aniline and optionally separating, recovering and reusing hydrogenation solvent. The expression "optionally separating, recovering and reusing hydrogenation solvent" as used herein intends to means that, when water is used as hydrogenation solvent, the water is optionally recovered and reused, and when an alcohol solvent, which will be described herein below, is used as hydrogenation solvent, the alcohol hydrogenation solvent is separated, recovered and reused. With reference to the Figure 1, the process for preparing 4-aminodiphenylamine according to the present invention comprises the steps of: continuously feeding nitrobenzene, aniline and a complex base catalyst, at desired proportion, to condensation process stage via metering pumps, and allowing them to react to form a condensation liquid (7) containing 4-nitrodiphenylamine, 4-nitrosodiphenylamine and/or salts thereof; continuously feeding the condensation liquid (7) and hydrogenation solvent, including supplementary hydrogenation solvent (2) and optionally recovered hydrogenation solvent (5), at desired proportion to hydrogenation process stage, and allowing them to react with hydrogen gas under the catalytic action of a powdery composite catalyst, including supplementary powdery composite catalyst (1) and reused, optionally regenerated, powdery composite catalyst (4), to form a hydrogenation liquid (8) containing 4-aminodiphenylamine; feeding the hydrogenation liquid (8) to separation I process stage, where (a) powdery composite catalyst (4), which is to be recycled back to the hydrogenation process stage directly or after being at least partially regenerated, (b) complex base catalyst (3), which is to be recycled back to the condensation process stage, and (c) aqueous phase obtained by evaporation during concentration and organic phase obtained by extraction (9) are obtained; feeding separately the aqueous phase and the organic phase (9) obtained in separation I process stage to separation II process stage, where (a) aniline (6), which is to be recycled back to the condensation process stage, (b) crude 4-aminodiphenylamine from which most aniline has been separated, and (c) optionally, hydrogenation solvent (5), which is to be recycled back to the hydrogenation process stage, are obtained; and feeding crude 4-aminodiphenylamine (10) to refining process stage, where (a) partial aniline (6), which is to be recycled back to the condensation process stage, and (b) finished 4-aminodiphenylamine are obtained. The whole process is conducted continuously. In the condensation reaction, molar ratio of nitrobenzene to aniline is in a range of from 1:1 to 1:15; reaction temperature may be in a range of from 20 to 150°C, preferably from 50 to 90°C, and controlling the reaction temperature not higher than 90°C can result in a decomposition ratio of the complex base catalyst of less than 0.5 percent during the condensation; reaction pressure may vary from 0.005 to 0.1 MPa (absolute pressure); and residence time of the feedstock in the whole condensation reactor is in a range of from 3.5 to 6h. The complex base catalyst used in condensation reaction comprises tetraalkyl ammonium hydroxide, alkali metal hydroxide, tetraalkyl ammonium salt and optional water, wherein the concentration sum of tetraalkyl ammonium hydroxide, alkali metal hydroxide and tetraalkyl ammonium salt is in a range of from 10 to 100 percent by weight, preferably from 25 to 38 percent by weight, and wherein the molar ratio of tetraalkyl ammonium hydroxide to alkali metal hydroxide to tetraalkyl ammonium salt is (0-9):(0.5-3):(0.5-3). The combination of part tetraalkyl ammonium hydroxide and inexpensive alkali metal hydroxide or oxide and tetraalkyl ammonium salt can achieve the same goal as obtained in the prior art where highly pure tetraalkyl ammonium hydroxide is used as catalyst. In the condensation reaction mixture, the molar ratio of hydroxide ion in complex base catalyst to nitrobenzene is in a range of from 1:4 to 4:1. The complex base catalyst used in the condensation reaction is prepared as follows: tetraalkyl ammonium hydroxide, alkali metal hydroxide or oxide and tetraalkyl ammonium salt, at desired molar ratio, are stirred in water at a temperature of from 0 to 90°C until being homogeneous, to form an aqueous form of the complex base catalysts. Then water can be completely removed by adding benzene through azeotropic process, to form an anhydrous form of the complex base catalysts. Said tetraalkyl ammonium hydroxide, alkali metal hydroxide or oxide and tetraalkyl ammonium salt as raw materials can be in solid form or in aqueous solution form. In the course of industrial production, the reaction mixture unavoidably contacts with carbon dioxide and carbon monoxide in ambient air and hydrogen, so that the tetraalkyl ammonium hydroxide will decrease in amount by converting to tetraalkyl ammonium carbonate. In the case where only tetraalkyl ammonium hydroxide is used as catalyst, the transformation of tetraalkyl ammonium hydroxide into ammonium salt will decrease the quantity of the catalyst, so that there need supply catalyst and get rid of ammonium salt. In contrast, with the complex base catalyst according to the present invention, there needs not any complex technology other than increasing the content of alkali metal hydroxide or oxide in the complex base catalyst. According to the present invention, nitrobenzene and aniline are condensed to form 4-nitrodiphenylamine and 4-nitrosodiphenylamine and/or their salts using the complex base catalyst at certain conditions. Anhydrous complex base catalyst may be used to convert nitrobenzene and aniline to 4-nitrodiphenylamine and 4-nitrosodiphenylamine and/or their salts in the condensation reaction according to the present invention. The selectivity and conversion of the reaction attain to the desired level at an anhydrous condition. In the case of using the complex base catalyst, it is possible not to severely control proton materials such as water, methanol and the like, thereby avoiding as much as possible the loss of the complex base catalyst and operation complexity caused by the control of proton materials. Without limited to any specific theory, it is believed that the integrated action of tetraalkyl ammonium hydroxide, alkali hydroxide and tetraalkyl ammonium salt in the complex base catalyst gives such a result, thereby reducing the difficulty of operating and controlling the reaction. It is believed that the use of the complex base catalyst comprising tetraalkyl ammonium hydroxide, alkali hydroxide and tetraalkyl ammonium salt makes the control of proton materials, for example, water in reaction system unimportant. That is to say, condensation reaction can be carried out and the conversion and selectivity are not affected no matter whether there are no proton materials such as water in the solution or there is high content of proton materials such as water in the solution. Thus, the difficulty of operating and controlling the reaction can be reduced and the quantity of aniline entrained out by azeotropic dehydration can be decreased, so that the process is more suitable for industrial scale production. In the process according to the present invention, the proton materials such as water no longer construct a restricting factor of the reaction, and the selectivity and conversion can attain the desired level whether or not there are proton materials such as water. Furthermore, it has been found that the decomposition ratio of the complex base catalyst is lower than that of the single tetraalkyl ammonium hydroxide. In a preferred embodiment of the present invention, condensation reaction can be carried out as follows: nitrobenzene, aniline and complex base catalyst in desired proportion are continuously fed to a falling film reactor via a metering pump to be heated and allowed to condense; the condensation liquid in the falling film reactor is discharged from the bottom of the reactor into a first reactor to continue condensation reaction; a part of condensation liquid from the bottom of the first reactor is conveyed back to the falling film reactor via a circulating pump, to establish a local circulating system of the condensation reaction according to the present invention. The circulating system is mainly consisted of the falling film reactor and the first reactor, and reactants continuously circulate via the condensation circulating pump. The circulating process maintains an amount of condensation liquid sufficient to form a uniform film in the falling film reactor. The falling film reactor may utilize ethanol vapor, hot water, steam or methanol vapor, preferably ethanol vapor as heat medium, to make the temperature of the system very homogeneous and avoid local overheating. That there is hardly back-mixing of reaction liquid in a falling film reactor significantly decreases the contact chance of product and raw materials and minimizes the side reaction. The local circulating system including the falling film reactor enhances the condensation reaction rate and reduces the reaction time, which is shortened from more than ten hours to 3.5-6 hours. It has also been found that continuous film reaction is higher than complete mixing reaction in both selectivity and yield. During this reaction, nitrobenzene reacts with aniline to form 4-nitrosodiphenylamine, nitrobenzene can also react with 4-nitrosodiphenylamine to form 4-nitrodiphenylamine, and nitrobenzene itself is reduced to nitrosobenzene, which in turn can react with aniline to form azobenzene. The latter reaction goes against main reaction and reduces the selectivity of the reaction. At the beginning of reaction, the quantity of nitrobenzene is relatively bigger. Nitrobenzene is gradually converted to 4-nitrosodiphenylamine and the quantity of nitrobenzene becomes smaller along with the reaction. The use of the continuous film reactor reduces the contact and reaction between nitrobenzene added and 4-nitrosodiphenylamine which is later formed (when the reactants enter the reactor to react, the concentration of nitrobenzene is relatively higher yet the concentration of 4-nitrosodiphenylamine is relatively lower, while at the end of the reaction, the concentration of 4-nitrosodiphenylamine is relatively higher yet the concentration of nitrobenzene is relatively lower), as well as the opportunity that nitrobenzene is reduced to nitrosobenzene by 4- nitrosodiphenylamine, thereby reducing reaction between nitrobenzene and aniline to form azobenzene. In the condensation reaction of nitrobenzene and aniline in the presence of the complex base catalyst, the main side reaction is to form by-products, azobenzene and phenazine. It is found that the bigger the quantity of aniline, the less the side reaction to convert nitrobenzene to phenazine. Another by-product in the reaction is azobenzene. Azobenzene can be easily transformed into aniline at the hydrogenation process stage, so that it can be reused in the production. Therefore, the molar ratio of nitrobenzene to aniline used in the invention is selected as from 1:1 to 1:15. Furthermore, in the process according to the present invention, condensation reaction can be performed under proper ratio of nitrobenzene and aniline without the introduction of any solvent into the system and a good yield can be achieved. The invention improves the yield of the condensation reaction and makes the reaction moving towards desired direction utilizing the above method. Those skilled in the art can contemplate that the condensation reaction according to the present process might employ more stages of reactors in series. In the condensation process stage, it is unavoidable to lose part of complex base catalyst used in condensation process along with the reaction. It is possible to supply only alkali metal hydroxide component and tetraalkyl ammonium salt component of the complex base catalyst when replenishing the catalyst, and their molar ratio is in a range of from 4:1 to 1:4. Alkali metal oxide can be used to replace alkali metal hydroxide, and its amount can be gotten by conversion of corresponding hydroxide. The tetraalkyl ammonium salts useful in the present invention can be represented by a general formula of [(Rl)(R2)(R3)(R4)N]+nXn- wherein Rl, R2, R3 and R4, which may be identical or different, can be alkyl having from 1 to 4 carbon atoms, said alkyl can carry a hydrophilic substituent selected from the group consisting of hydroxy, methoxy, polyether, cationic polyamide, polyester, polyethylene polyamine, highly water-soluble quaternary ammonium salt-containing radical, etc., XTH is selected from the group consisting of halide ion, sulfate radical, carbonate radical, phosphate radical, bicarbonate radical, bisulfate radical, Ci-Cz-alkyl carbonate radical, C1-C2-alkyl sulfate radical, etc., and n is a value of from 1 to 2. Examples of the tetraalkyl ammonium salts include, but not limited to, poly-methylated triethylene tetraamine sulfate, poly-methylated diethylene triamine carbonate, N,N-dimethyl-N,N-bis(methoxyethyl)ammoniumcarbonate, N-methyl-N,N,N-tri(methoxyethyl)ammoniumcarbonate, N,N,N-trimethyl-N-hydroxyethyl ammonium carbonate, trimethyl hydroxyethyl ammonium chloride, N,N,N-trimethyl-N-ethoxylated (1-4 moles of ethylene oxide) ethyl ammonium carbonate, N,N,N-trimethyl-N-ethoxylated (1-4 moles of ethylene oxide) propyl ammonium carbonate, N,N,N-trimethyl-N-ethoxylated (1-4 moles of ethylene oxide) propyl ammonium chloride, N,N-dimethyl-N,N-bis(ethoxylated (1-4 moles of ethylene oxide) propyl) ammonium carbonate, tetramethyl ammonium carbonate, tetramethyl ammonium methyl-carbonate, tetraethyl ammonium carbonate, tetraethyl ammonium ethyl-carbonate, tetramethyl ammonium sulfate, tetramethyl ammonium methyl-sulfate, tetraethyl ammonium sulfate, and tetraethyl ammonium ethyl-sulfate. The tetraalkyl ammonium hydroxide used in the complex base catalyst can be represented by a formula of R'4N+OH~, wherein R' is independently an alkyl having one or two carbon atoms. The tetraalkyl ammonium hydroxide may be prepared from corresponding tetraalkyl ammonium salt and base in polar solvent according to a process known per se. The alkali metal hydroxides or oxides include hydroxides and oxides of lithium, sodium, potassium and rubidium, such as sodium hydroxide, potassium hydroxide, lithium hydroxide, sodium oxide or potassium oxide. The tetraalkyl ammonium alkyl-carbonates or tetraalkyl ammonium alkyl-sulfates useful in the present invention can be prepared by the reaction of trialkyl amine and dialkyl (C1-C2) carbonate or dialkyl(C1-C2) sulfate in polar solvent. According to the present invention, the reaction temperature for the preparation of tetraalkyl ammonium alkyl-carbonate or tetraalkyl ammonium alkyl-sulfate varies from 50 to 200°C, preferably from 60 to 150°C, and reaction pressure varies from 0.1 to 3MPa (gauge pressure). In general, the pressure depends on the selected temperature, type and amount of the solvent, namely, the less the amount of solvent, the higher the system pressure; and the higher the temperature, the higher the pressure. In the invention, the reaction pressure is preferably controlled in a range of from 0.4 to 2MPa to obtain higher product yield. In the reaction for the preparation of tetraalkyl ammonium alkyl-carbonate or tetraalkyl ammonium alkyl-sulfate according to the present invention, the molar ratio of trialkyl amine to dialkyl(C1-C2) carbonate or dialkyl(C1-C2) sulfate is selected as from 2:1 to 1:2. If the proportion of trialkyl amine is too high, then trialkyl amine will be superabundant in the reaction system and thus impose operational difficulty to subsequent processes and pollutes the environment. If the proportion of trialkyl amine is too low, then dialkyl(C1-C2) carbonate or dialky(C1-C2) sulfate will be superabundant, and thus cause the loss of dialkyl(C1-C2) carbonate or dialkyl(C1-C2) sulfate in the subsequent reaction, thereby increasing the production cost. In the process for the preparation of tetraalkyl ammonium alkyl-carbonate or tetraalkyl ammonium alkyl-sulfate according to the present invention, reaction time of trialkyl amine and dialkyl(C1-C2) carbonate or dialkyl(C1-C2) sulfate is in a range of from 1.5 to 6h. At the initial stage of the reaction, the reaction rate is high, and exothermic phenomenon is obvious. With consumption of raw materials, the reaction slows down and heat release is gradually reduced. During the reaction, the amount of cooling water is continuously adjusted to keep reaction temperature and pressure in a certain range. The polar solvents useful in the condensation reaction according to the present invention include methanol, ethanol or isopropyl alcohol. The amount of solvents used varies from 1 to 10 times of weight of trialkyl amine. In the hydrogenation reaction according to the present invention, hydrogen gas can be used as reducing agent. The reaction temperature is in a range of from 50 to 100°C, the pressure is in a range of from 0.2 to S.OMPa (absolute pressure), and the reaction time varies from 2 to 7h. Volume ratio of gas to liquid is in a range of from 10:1 to 1500:1, weight ratio of solid to liquid is in a range of from 0.5:100 to 16:100, with the gas meaning hydrogen gas, the liquid meaning hydrogenation solvent and condensation liquid, and the solid meaning powdery composite catalyst. In the practice of the invention, alcohols and/or water can be used as hydrogenation solvent. As alcohols, methanol, ethanol and isopropyl alcohol are preferred. The hydrogenation solvent can be used in such an amount that weight ratio of hydrogenation solvent to condensation liquid is in a range of from 1:10 to 5:10. When an alcohol is used as hydrogenation solvent, the alcohol need be separated, recovered and recycled. When water is used as hydrogenation solvent, the aqueous phase after extraction, which will be described herein below, is concentrated to give the complex base catalyst of the present invention and the condensed water obtained during the concentration is optionally recycled back to hydrogenation process stage. The powdery composite catalyst useful in the hydrogenation reaction according to the present invention comprises nickel, aluminum and component A which is at least one selected from the group consisting of Fe, Cu, Co, Mn, Cr, Mo, B and P, wherein the content of nickel is in a range of from 25 to 99.9 wt.-%, and the total content of aluminum and component A is in a range of from 0.1 to 75 wt.-%. The particle size of the catalysts may vary from 40 to 300 mesh. The modifying agent A, which is at least one of Fe, Cu, Co, Mn, Cr, Mo, B and P, can modify the crystalline state of nickel-aluminum alloy so as to achieve the purpose of improving the selectivity of hydrogenation reaction and enhancing the activity of catalyst. The powdery composite catalyst according to the present invention can be prepared by mixing powdery nickel, powdery aluminum and component A in desired proportion, then melting them at high temperature, followed by pulverizing them into powder of from 40 to 300 mesh after discharging and quenching, and finally, treating the powder with hydroxide aqueous solution. The concentration of hydroxide can be in a range of from 5 to 50 weight percent. The reaction temperature is 50-90°C. In order to improve the recovering effect of hydrogenation catalysts by magnetic separator in the subsequent process, it is preferred to use at least iron as modifying agent to increase the ferromagnetism of the powdery composite catalysts. Therefore, in a preferred embodiment of the present invention, the powdery composite catalyst according to the present invention can be prepared by taking powdery nickel, powdery aluminum, powdery iron, and optional other modifying agent A, which is selected from the group consisting of Cu, Cr, Co, Mn, Mo, B and P, in desired proportion; melting them into alloy in an induction furnace; ejecting the molten alloy using gas pressure through a nozzle to a copper drum rotating at high speed to quench quickly the alloy with cooling speed being as high as 105-106K/sec; pulverizing the cooled alloy using a ball mill into powder of from 40 to 300 mesh, preferably from 100 to 200 mesh; and finally, treating the powder with 5 to 50 wt.-% hydroxide aqueous solution at a temperature of 50 to 90°C. According to a preferred embodiment of the invention, hydrogenation reaction can be carried out as follows: condensation liquid, hydrogenation solvent, powdery composite catalyst recovered and, if necessary, complementary fresh powdery composite catalyst are fed to first-stage, second-stage and optional high-stage hydrogenation reactors by a solid-liquid conveyer, and hydrogen gas is bubbled into the reactors from bottom of the reactors via a hydrogen gas circulator, to carry out the hydrogenation reaction under the above hydrogenation reaction conditions to form crude hydrogenation liquid containing 4-aminodiphenylamine. The powdery composite catalyst entrained out by crude hydrogenation liquid is separated by a settling vessel and a magnetic separator. Solid-liquid phase, which separates from hydrogenation liquid and contains high concentration of the powdery composite catalyst, enters into the first reactor to be reused through a mixed solid-liquid conveying device. At the same time, hydrogenation liquid containing 4-aminodiphenylamine is obtained. The powdery composite catalyst according to the present invention is a solid-state material during the hydrogenation. In industry, a hydrogenation catalyst is typically circulated via a pump, however, when a pump is used to convey a catalyst containing a high concentration of powdery metal, pump cavity is easily damaged and the transportation effect is also not good. The inventors design a Venturi-like solid-liquid conveying device, and circulation of the powdery composite catalyst in hydrogenation system is achieved through a pump-free circulation performed by skillfully employing the power of the pump for feeding condensation solution, so that the loss of catalyst is significantly reduced, the concentration of catalyst in condensation solution is significantly enhanced. According to a preferred embodiment, in continuous hydrogenation process, the powdery composite catalyst in crude hydrogenation liquid is recovered through sedimentation and magnetic separator and recycled via Venturi type solid-liquid conveying device, and circulating hydrogen gas is bubbled into the reactors. The whole hydrogenation step is conducted in a complete mixing flow mode by continuously feeding stock into multistage reactors in series. The hydrogenation solvents can be the recovered and reused. The hydrogenation liquid having part of the powdery composite catalyst recovered through sedimentation and magnetic separator enters into separation I process stage, where the residual powdery composite catalyst in the hydrogenation liquid is recovered from hydrogenation liquid by filtration, and circulated back to the hydrogenation process stage directly or after being at least partially regenerated. In the hydrogenation reaction according to the present invention, with optionally continuously renewing a minor amount of hydrogenation catalyst, the catalyst concentration in the reaction system can always maintain at high level. Such a method of recycling catalyst can always and stably maintain the total activity of catalyst in the system at a higher level and avoid the problem that catalyst activity gradually decreases suffered by the processes employing fixed bed catalyst. The use of magnetic separator facilitates the recovery of the catalyst, and the designing and application of mixed solid-liquid conveying device makes powdery composite catalyst circulating in the hydrogenation system. In the present invention, deactivation of catalyst usually attributes to that inorganic matter or organic carbon deposition clog pores of the catalyst, so that the active sites of the catalyst are covered, and thereby the activity of the catalyst decreases. Therefore, the present invention employs washing with a high concentration base solution, for example, 5-50 wt.-% aqueous solution of alkali metal hydroxide in combination with ultrasonic oscillation to regenerate the catalyst. Ultrasonic oscillation facilitates to get rid of the inorganic or organic carbon deposition, while the high concentration base solution can dissolve the aluminum, which isn't dissolved in the first base dissolution, in the catalyst to form new loose pore structures, thereby increasing the activity of the catalyst. The inventors utilize sedimentation and magnetic separator to recover magnetic hydrogenation catalyst, and design a Venturi type mixed solid-liquid conveying device to convey the catalyst back to hydrogenation reactor using the force of feeding the stocks, thereby achieving the circulation of powdery composite catalyst. The inventors also take out the catalyst after filtration to regenerate it to restore its initial activity. By the two measures, the consumption of catalyst is significantly reduced, and the activity and life time of catalyst are improved. The filtrate is extracted with extracting agent and co-extracting agent to obtain an organic phase and an aqueous phase. The organic phase is conveyed to separation II process. The aqueous phase is subjected to one-stage or multistage concentration to give the complex base catalyst of the present invention, which is recycled back to the condensation process. Specifically, in the practice of the present invention, water is used as extracting agent and the volume ratio of water to hydrogenation liquid can vary from 0.5:1 to 5:1, preferably from 0.8:1 to 1.2:1. Organic polyethers is used as co-extracting agent, and examples includes, but not limited to, polyethylene glycol ethers, such as polyethylene glycol dimethyl ether having a molecular weight of from 200 to 1000, polyethylene glycol diethyl ether having a molecular weight of from 200 to 1000, and polyethylene glycol methyl ethyl ether having a molecular weight of from 200 to 1000; polypropylene glycol ethers, such as polypropylene glycol dimethyl ether having a molecular weight of from 200 to 1000, polypropylene glycol diethyl ether having a molecular weight of from 200 to 1000, and polypropylene glycol methyl ethyl ether having a molecular weight of from 200 to 1000; fatty alcohol polyoxyethylene ethers, such as those wherein the fatty alcohol has 12 to 18 carbon atoms and polymerization degree of polyoxyethylene is from 3 to 15. The volume ratio of the co-extracting agent to water is in a range of from 0.0001:1 to 0.005:1. Pressure during extraction can be in a range of from 0.005 to 0.1 MPa, extraction temperature can be in a range of from 0 to 80°C, and extraction time can vary from 2 to 5h. Supernatant aqueous phase containing hydrogenation solvent and complex base catalyst and organic phase mainly containing aniline, 4-aminodiphenylamine and a minor amount of organic impurities are obtained after separation. Concentration of aqueous phase can be conducted using one-stage or multistage gas-aid falling film evaporator. In general, heat medium used in the concentration can be water, steam or secondary steam from the preceding stage evaporator. In the gas-aid falling film evaporator of the present invention, shell pass is heated by steam, and another part of steam enters into the tube pass from steam inlet on the top of one-stage falling film evaporator, namely flow-aiding inlet. Aqueous phase enters into the tube pass from lower concentration aqueous phase inlet of the gas-aid falling film evaporators. The direction of steam motion is the same as the direction of aqueous phase motion, and the steam is of an assistant power. Specifically, the gas-aid falling film evaporators include shell pass (2'), tube pass (3'), steam inlet (8') installed on the top of shell pass (2'), condensed water outlet (!') installed at the bottom of shell pass (2'), lower concentration aqueous phase inlet (6') installed on the top of tube pass (3'), higher concentration aqueous phase outlet (9') installed at the bottom of tube pass (3'), flow-aiding steam inlet (5' and 7') installed on the top of tube pass (3') and distributing tray (4') installed at a position below the lower concentration aqueous phase inlet (6')- In the falling film evaporators, the aqueous phase, carried by the steam, passes through distributing tray and flows in film form from top to bottom in the tubes. The residence time of the aqueous phase is controlled in a range of from 2 to 60 seconds and the temperature of the aqueous phase can be in a range of from 30 to 105°C. The pressure of shell pass steam used in the concentration is in a range of from 0.005 to 0.1 MPa (absolute pressure). With the use of a gas-aid falling film evaporator and utilizing the steam to carry the aqueous phase flowing from the top to the bottom, the liquid flow rate is quickened and the residence time is controlled, at the meantime, low-boiling substances in the aqueous phase is largely evaporated at the higher temperature. Thus the decomposition of complex base catalyst containing tetraalkyl ammonium hydroxide can be minimized. If the hydrogenation solvent is an alcohol, the condensate from the condensation of evaporated substances which is a mixture of water and the alcohol can be conveyed to separation II process to recover the hydrogenation solvent. If the hydrogenation solvent is a mixture of water and an alcohol, the condensate from the condensation of evaporated substances which is a mixture of water and the alcohol can be recycled back to the hydrogenation process or conveyed to separation II process to recover the alcohol. If the hydrogenation solvent is water, the condensate from the condensation of evaporated substances which is water can be recycled back to the hydrogenation process. In the separation II process stage of the present invention, aniline is obtained by evaporation from the extracted organic phase conveyed from separation I process stage, and the aniline is recycled back to the condensation process. The column bottoms from which most aniline is separated are conveyed to refining process. The operating pressure of the evaporator can vary from 0.005 to 0.1 MPa (absolute pressure), column bottom temperature is in a range of from 120 to 320°C, and the temperature of gas phase is in a range of from 60 to 190°C. In the cases where the hydrogenation solvent is an alcohol or a mixture of an alcohol and water, the evaporator condensate which is obtained from the condensation of aqueous phase in separation I process is subjected to rectification to give the alcohol as hydrogenation solvent, and the alcohol is recycled back to the hydrogenation process. The organic phase having most aniline separated in separation II process stage contains 4-aminodiphenylamine, aniline, azobenzene and phenazine, etc. In an embodiment of the present invention, the refining process is conducted through three-column continuous rectification and batch rectification, wherein the organic phase to be refined is conveyed via a pump into rectification column 1, where aniline, azobenzene and phenazine are taken out from the column top, and crude 4-aminodiphenylamine is discharged from the column bottom. The effluent from the top of rectification column 1 enters into rectification column 3, where aniline with a purity of about 99% is distilled from the top of rectification column 3 and can be directly recycled back to condensation process, and azobenzene and phenazine are left in the column bottom. Column bottoms of rectification column 1 are conveyed via a pump to rectification column 2, where the finished 4-aminodiphenylamine is distilled from the top of rectification column 2, and column bottoms of rectification column 2, after accumulating to a certain amount, are conveyed to batch still, where a minor amount of 4-aminodiphenylamine left in the bottoms is distilled off and conveyed back to rectification column 2, and the other residues are discharged from the still bottom. In the above refining process according to the present invention, the rectification column 1 is operated at a vacuum degree of from 0.09 to 0.098MPa, a reflux ratio of from 2:1 to 10:1, a column top temperature of from 80 to 130°C, a still temperature of from 260 to 290°C; the rectification column 2 is operated at a vacuum degree of from 0.09 to 0.098MPa, a reflux ratio of from 1:0.5 to 1:4, a column top temperature of from 140 to 190°C, a still temperature of from 260 to 300°C; the rectification column 3 is operated at a vacuum degree of from 0.09 to 0.098MPa, a reflux ratio of from 1:0.5 to 1:2, a column top temperature of from 80 to 120°C, a still temperature of from 120 to 170°C; and the batch rectification column is operated at a vacuum degree of from 0.09 to 0.098MPa, a column top temperature of from 235-250°C, and a still temperature of from 280 to 330°C. The still temperature of the rectification column 2 is relatively lower, thus coking of 4-aminodiphenylamine can be reduced, and 96% or more of 4-aminodiphenylamine can be distilled off at the top of rectification column 2 operated at a relatively lower still temperature, so that the amount of 4-aminodiphenylamine in the bottoms to be subjected to batch evaporation is significantly reduced. In the process for preparing 4-aminodiphenylamine according to the present invention, the complex base catalyst and powdery composite catalyst used have lower production cost and higher catalytic activity; the whole process can be continuously carried out and is suitable for industrial scale production; the use of the complex base catalysts in condensation process significantly decreases the difficulty of operating and controlling the reaction and renders the water in the reaction system being no longer a reaction-confining factor; the decomposition of complex base catalyst is much less than that of the single tetraalkyl ammonium hydroxide catalyst; the selection of a falling film reactor and raw material proportion improves selectivity of the reaction; there needs no solvent; the hydrogenation reaction can be carried out at a lower temperature and mild reaction conditions, and the hydrogenation catalyst is good at antitoxic performance, by-product is little, and conversion and selectivity is high; a magnetic separator is used to recover magnetic powdery composite catalyst during hydrogenation process; the hydrogenation catalyst is conveyed back to hydrogenation reactor via a Venturi type mixed solid-liquid conveying device using the force of feeding stocks; catalyst can be regenerated by chemical and/or physical methods, and thus the consumption of catalyst is reduced; the complex base catalyst is recovered after hydrogenation, and water containing co-extracting agent is used as extracting agent to separate the complex base catalyst; the aqueous phase is concentrated by one-effect or multi-effect gas-aid falling film evaporator to recover the complex base catalyst; the whole process is continuous and the operational strength is low; no corrosive liquid is produced, and environment pollution is almost eliminated. The purity of 4-aminodiphenylamine can exceed 99%, and the yield in the whole industrial production process can be over 95%. Examples The following examples further describe the invention, but do not make limitation to the invention in any way. Example 1 Preparation of a complex base catalyst To a 1000ml three-necked flask equipped with a condenser and a stirrer were added 227.5g of 20wt.-% aqueous solution of tetramethyl ammonium hydroxide (O.Smol), lOg (0.25mol) of sodium hydroxide and 346g of 30wt.-% aqueous solution of tetramethyl ammonium carbonate (0.5mol). The mixture was homogeneously stirred at 72-77 °C to give a complex base catalyst having a concentration of 27.3 wt.-%. Example 2 Preparation of a powdery composite catalyst 46g of powdery nickel, 51g of powdery aluminum, and 3g of powdery iron were taken and mixed, then molten into alloy state in an induction furnace. The molten alloy was ejected using gas pressure through a nozzle to a copper drum rotating at high speed to be quenched quickly with cooling speed being as high as 105-106K/sec. The cooled alloy was pulverized using a ball mill, and 99.7g of powder of from 40 to 300 mesh were obtained by sieving. 375g of 20 wt.-% sodium hydroxide aqueous solution was charged into a 500ml three-necked flask equipped with a thermometer and a stirrer, and the above powder is slowly added thereto. The mixture was stirred at 60°C for 4h, then the solid was washed with deionized water until neutral to give a powdery composite catalyst. Example 3 Under vacuum condition, feeding pumps of the above complex base catalyst, aniline and nitrobenzene were simultaneously switched on and adjusted to such flow rate as aniline 150kg/h, nitrobenzene 30kg/h and the complex base catalyst 200kg/h. The aniline, nitrobenzene and complex base catalyst were continuously fed into a falling film reactor to be heated and allowed to condense. Condensation liquid in the falling film reactor was discharged from the bottom into a first reactor to proceed with condensing. Part of condensation liquid from the bottom of the first reactor was conveyed back to the falling film reactor via a circulating pump, forming a local circulating system. Ethanol vapor at 78-90°C was used as the heat medium of the falling film reactor. Reaction temperature was controlled as 75°C, pressure was controlled as OOOSMPa (absolute pressure) and flow rate of the circulating liquid was controlled as Im3/h. The reactants overflowed from the first reactor into a second-stage reactor. The process conditions of the second-stage reactor, such as operational temperature and pressure, were identical with that of the first reactor. The total residence time of the reactants in the falling film reactor, first reactor and second-stage reactor was controlled as 5h. Once the condensation reaction became stable, the complex base catalyst recovered according to the procedure as described in the following examples could be used, with only a minor amount of fresh complex base catalyst prepared according to example 1 being replenished, so that the molar ratio of hydroxide ion to nitrobenzene was controlled not less than 1:1. The effluent of the second-stage reactor was found to contain not larger than 0.1wt.-% of nitrobenzene, 24.9 wt.-% of water and 16.1 wt.-% of 4-nitrosodiphenylamine and 4-nitrodiphenylamine. Example 4 Under vacuum condition, feeding pumps of the complex base catalyst, aniline and nitrobenzene were simultaneously switched on and adjusted to such flow rate as aniline 150kg/h, nitrobenzene 30kg/h and the complex base catalyst 200kg/h. The aniline, nitrobenzene and complex base catalyst were continuously fed into a falling film reactor to be heated and allowed to condense. Condensation liquid in the falling film reactor was discharged from the bottom into a first reactor to proceed with condensing. Part of condensation liquid from the bottom of the first reactor was conveyed back to the falling film reactor via a circulating pump, forming a local circulating system. Ethanol vapor at 78-90°C was used as the heat medium of the falling film reactor. Reaction temperature was controlled as 75°C, pressure was controlled as O.OOSMPa (absolute pressure) and flow rate of the circulating liquid was controlled as Im3/h. The reactants overflowed from the first reactor into a second-stage reactor. The process conditions of the second-stage reactor, such as operational temperature and pressure, were identical with that of the first reactor. The total residence time of the reactants in the falling film reactor, first reactor and second-stage reactor was controlled as 5h. Once the condensation reaction became stable, the complex base catalyst recovered was used, with sodium hydroxide and tetraalkyl ammonium salt (i.e. tetramethylammnium carbonate according to Example 1) in a molar ratio of 1:1 being replenished, so that the molar ratio of hydroxide ion to nitrobenzene was controlled not less than 1:1. The effluent of the second-stage reactor was found to contain not larger than 0.1wt.-% of nitrobenzene, 15.6 wt.-% of water and 17.6 wt.-% of 4-nitrosodiphenylamine and 4-nitrodiphenylamine. Example 5 Hydrogenation The condensation liquid as prepared in Example 3 was conveyed to hydrogenation reactor after filtration. Hydrogen gas was used to replace the atmosphere of the system and pressurize to 1.3MPa. A hydrogen gas circulator was switched on and flow rate of circulating hydrogen gas was maintained at INmVh. The circulating hydrogen gas was bubbled into the hydrogenation reactor to improve the gas-liquid mass transfer effect during reaction. The flow rate of condensation liquid of nitrobenzene and aniline was controlled as 306kg/h, and the flow rate of methanol was controlled as 601/h (48kg/h). The hydrogenation feedstock was fed into a first-stage hydrogenation reactor equipped with a sealed magnetic stirrer and a cooling and heating system, and powdery composite catalyst above prepared was added simultaneously so that the solid-liquid ratio by weight was 6:100. Hydrogenation-reduced liquid overflowed from the first reactor into a second-stage reactor, then into a third-stage reactor, finally into a settler. The reaction temperature was 75-80°C, pressure was IJMPa and total residence time was 5h. The powdery composite catalyst was recovered as much as possible under the action of a magnetic separator. Solid-liquid mixture containing higher concentration of solid catalyst at the bottom of the settler was returned to the first-stage hydrogenation reactor via a Venturi type solid-liquid conveying device using the force of feeding stocks. The activity of the catalyst in the hydrogenation reaction was judged by monitoring the endpoint of reducing reaction, and thus it could be determined whether powdery composite catalyst for hydrogenation reaction was replenished. The hydrogenation-reducing liquid was measured by high performance liquid chromatograph (HPLC) and was found not containing 4-nitrodiphenylamine and 4-nitrosodiphenylamine. Example 6 Separation I The hydrogenation liquid as prepared in Example 5, after settling and magnetic separating the powdery composite catalyst, was subjected to filtration to recover extremely fine powdery composite catalyst which was not recovered by magnetic separation. The powdery composite catalyst recovered by filtration was recycled back to the hydrogenation process after regeneration. Hydrogenation-reduced liquid containing no solid catalyst was continuously fed at a flow rate of 3601/h to top of an extraction column via a metering pump, and extracting agent water having the same flow rate of 3601/h and co-extracting agent polyethylene glycol dimethyl ether with a molecular weight of 400-800 having a flow rate of 0.41/h were continuously fed to the bottom of the extraction column. After extraction, aqueous phase was discharged from the column top and organic phase was discharged from the column bottom. The extraction time was 3h and extraction pressure was atmospheric pressure. Methanol and the complex base catalyst in the hydrogenation-reduced liquid were extracted by water to aqueous phase. An aqueous phase was obtained at an amount of 5401/h and organic phase was obtained at an amount of 1801/h. The aqueous phase, after preheated to 80°C, was fed at a flow rate of 5401/h via a metering pump to top of a gas-aid falling film evaporator whose shell pass was heated with 120°C steam. The residence time of the stuff in the evaporator was 10 sec. The primary concentrated liquid was conveyed to a second-stage shell-and-tube falling film evaporator under 0.1 MPa (absolute pressure) and the residence time of the stuff in this evaporator was 10 sec. The temperature of gas-liquid mixture discharged from second-stage falling film evaporator was 80-95°C. After separating via secondary gas-liquid separator, recovery ratio of the complex base catalyst in the whole concentrating process might be as high as 99.7%. The complex base catalyst was recycled back to the condensation process. Example 7 Separation II The gas phase evaporated from the falling film evaporators condensed to give a methanol-water solution containing about 28wt.% of methanol. The methanol-water solution was continuously pumped to a rectification column to conduct separation, thus methanol having a purity of more than 99wt.% was obtained from column top and could be reused in the hydrogenation process, and water was in the column bottom. The water in the column bottom was measured by gas chromatography (GC) and it was found that the content of methanol therein was less than 0.3 wt.% The organic phase from extraction operation was fed to a shell-and-tube rising film evaporator to separate most aniline. Operational pressure of the rising film evaporator was O.OlMPa (absolute pressure), and 180°C steam was used to heat in the shell pass. A gas phase at 75-105°C and a liquid phase at 160°C were gained from a gas-liquid separator located on the top of the rising film evaporator. The gas phase material after condensation was measured by chromatography and the content of aniline was found as high as 99 wt. %. Most of aniline was distilled during the process, and the distilled aniline could be recycled back to the condensation process as the raw material of condensation reaction. Liquid phase material was the crude product of 4-aminodiphenylamine, containing 78.1 percent of 4-aminodiphenylamine, 21.75 percent of aniline and the balance amount of other organic impurities. Example 8 Refining The crude product of 4-aminodiphenylamine (containing 78.1 percent of 4-aminodiphenylamine, 21.75 percent of aniline, 0.05 percent of azobenzene and 0.1 percent of phenazine) was continuously fed to rectification column 1 at a flow rate of 120kg/h via a gear pump. The temperature of still was controlled as 270°C, the temperature of column top was controlled as 110°C, vacuum degree was controlled as 0.094MPa and reflux ratio was controlled as 5:1. Light components, i.e. aniline, azobenzene and phenazine, were taken out from the column top at a flow rate of about 26.2kg/h, and conveyed to rectification column 3. The rectification column 3 was operated at conditions of still temperature of 150°C, column top temperature of 90°C, vacuum degree of 0.094MPa and reflux ratio of 1:1. Aniline was distilled off from column top at a flow rate of 24kg/h, and azobenzene and phenazine were left in column bottom. Column bottoms of the rectification column 1 were conveyed to rectification column 2. The rectification column 2 was operated at conditions of still temperature of 280°C, column top temperature of 170°C, vacuum degree of 0.097MPa and reflux ratio of 1:1. The finished 4-aminodiphenylamine was obtained at the column top of the rectification column 2. Column bottoms of the rectification column 2 were conveyed to batch still. The batch still was operated at conditions of kettle temperature of 285-320°C, vacuum degree of 0.094MPa and top temperature of 235-250°C, to distill off the residual 4-aminodiphenylamine, which was recycled back to the rectification column 2 to be further distilled. The whole refining process of 4-aminodiphenylamine was continuously carried out. The finished 4-aminodiphenylamine product obtained had a purity of 99.1%, a melting point of 72°C and a solidifying point of 72.4°C. The yield of the process step in industrial production was 95.1%. Example 9 Process for Regenerating Catalyst 20g of powdery composite catalyst, which was recovered by filtration of the hydrogenation liquid, was charged into a 100ml three-necked flask equipped with a stirrer and a thermometer. 20 ml of 40% aqueous solution of sodium hydroxide was added thereto. While stirring, the mixture was heated to 90°C and maintained at that temperature for Ih. At the end of the reaction, the catalyst was subjected to ultrasonic washing for 30min in a washing tank, followed by washing with water for multiple times until the pH of the washing water was 7-8. The gained solid was regenerated powdery composite catalyst. Example 10 Preparation of a complex base catalyst To a 500ml three-necked flask equipped with a condenser and a stirrer were added 230g of water, followed by adding 91 g of pentahydrated tetramethyl ammonium hydroxide (containing O.Smol of tetramethyl ammonium hydroxide), 20g (O.Smol) of sodium hydroxide and 70g of trimethylhydroxyethyl ammonium chloride (0.5mol). The mixture was homogeneously stirred at 75±2 °C to give a complex base catalyst having a concentration of 32.85 wt.-%. Example 11 Preparation of a complex base catalyst To a 500ml three-necked flask equipped with a condenser and a stirrer were added 230g of water, followed by adding 91g of pentahydrated tetramethyl ammonium hydroxide (containing 0.5mol of tetramethyl ammonium hydroxide), 20g (O.Smol) of sodium hydroxide and 74.5g of tetramethyl ammonium methylcarbonate ([(CH3)4N]+[C03CH3]" )(0.5mol). The mixture was homogeneously stirred at 75±2 °C to give a complex base catalyst having a concentration of 33.7 wt.-%. Example 12 To a 500ml four-necked flask equipped with a stirrer and a water segregator and a condenser were added 150g of water, followed by adding 91g of pentahydrated tetramethyl ammonium hydroxide (containing O.Smol of tetramethyl ammonium hydroxide), 20g (O.Smol) of sodium hydroxide and 74.5g of tetramethyl ammonium methylcarbonate ([(CH3)4N]+[CC>3CH3]~X0.5rnol). Then 25g of benzene were added thereto, and the mixture was heated to reflux. There were water layer and oil layer in the water segregator. Oil layer was returned to the four-necked flask and water layer was separated out until there was no water in distilled liquid. An anhydrous form of complex base catalyst was obtained. Example 13 Preparation of tetramethylammonium methyl-carbonate ([(CH3)4N]+[CO3CH3J~) To a 1.5 L autoclave equipped with a stirrer and a heating means were added 90g (l.Omol) of dimethyl carbonate, 59g (l.Omol) of trimethyl amine and 510g (15mol) of methanol. Stirring was initiated after the autoclave was sealed. The autoclave was heat to 140°C, and pressure was l.SMPa. The reaction was kept at 140°C for 4h. Then the reaction mixture was cooled to 50°C and discharged into a 1L three-necked flask. Part of methanol was removed from the solution of tetramethylammonium methyl-carbonate in methanol thus obtained under vacuum, and then the solution was cooled to ambient temperature. White crystal precipitated out. The crystal was filtrated, oven dried and recrystallized from methanol, to give 119.5g of tetramethylammonium methyl-carbonate having a purity of 99.2% as measured by chromatography. The yield was 80.2%. Example 14 92.5g (Imol) of l-chloro-2,3-epoxy propane, 3g (Imol) of N-methyl diethanolamine, 2g of sodium hydroxide and 700g of water were charged into an autoclave with a stirrer, a heating means and a thermometric means. With stirring, the mixture was gradually heated to 120°C, then gaseous ethylene oxide was continuously passed into the autoclave to maintain a reactor pressure of 0.3MPa until the quantity of ethylene oxide passed into reached 150g. The reaction continued for further 2h at that temperature, to give ClCH2[CH2CH2OJ2-5-H. 60g of gaseous trimethylamine were passed thereto. The autoclave was heat to 140°C, and pressure was l.SMPa. The reaction was maintained at that temperature for 4h. Then the mixture was cooled to room temperature. After conventionally dehydrating and drying, 105g of N,N,N-trimethyl-N-ethoxylated (1-4 moles of ethylene oxide) propyl ammonium chloride was obtained. Example 15 Preparation of tetramethyl ammonium hydroxide To a 1.5 L autoclave equipped with a stirrer and a heating means were added 90g (l.Omol) of dimethyl carbonate, 59g (l.Omol) of trimethyl amine and 510g (15mol) of methanol. Stirring was initiated after the autoclave was sealed. The autoclave was heated to 140°C, and pressure was 1.5MPa. The reaction was kept at 140°C for 4h. Then the reaction mixture was cooled to room temperature and discharged into a 1L three-necked flask. A slurry consisting of 148g (2.0mol) of calcium hydroxide and 350g of water was added thereto. Methanol was distilled off by heating over 8h while stirring. 355g of tetramethyl ammonium hydroxide solution was obtained after filtration. The content of tetramethyl ammonium hydroxide was found as 24.4% and the total reaction yield was 95.2%. Example 16 Preparation of tetraethyl ammonium hydroxide To a 1.5 L autoclave equipped with a stirrer and a heating means were added 154g (l.Omol) of diethyl sulfate, lOlg (l.Omol) of triethyl amine and 690g (15mol) of ethanol. Stirring was initiated after the autoclave was sealed. The autoclave was heat to 140°C, and pressure was l.OMPa. The reaction was kept at 140°C for 4h. Then the reaction mixture was cooled to room temperature and discharged into a 1L three-necked flask. 80g (2.0mol) of sodium hydroxide was added thereto. The reaction mixture was heated to 45°C for 4h while stirring. After filtration, part of ethanol was distilled off from the filtrate. Then 500g of water was added while ethanol was distilled off (part of water was entrained out), to give 604g of tetraethyl ammonium hydroxide solution. The content of tetraethyl ammonium hydroxide was found as 23.3wt.-% and the total reaction yield was 95.7%. Example 17 Effect on reaction imposed by the quantity of aniline and nitrobenzene A local circulating system having a total volume of 1L was comprised of a miniature reactor equipped with a vacuum system and a temperature control system, a film reactor and a circulating pump. The system was firstly filled with aniline, and the flow of the circulating pump was set at 2 1/h. A mixture, containing nitrobenzene, aniline and the complex base catalyst prepared according to example 1 at a molar ratio of nitrobenzene to aniline to OH" in the complex base catalyst of 1:1:1.8, was fed to the reactor at a flow rate of 200ml/h. The residence time was 5h. The system temperature was maintained as 75°C and the system pressure was maintained as O.OOSMPa (absolute pressure). After the aniline was replaced by reaction liquid and reaction liquid was stable in composition, a sample was taken and analyzed. Nitrobenzene was substantially not detectable. The reaction selectivity was calculated according to the total mole number of 4-nitrosodiphenylamine and 4-nitrodiphenylamine generated. The results obtained under the same conditions except that the ratio of nitrobenzene to aniline was changed were showed in table 1. (Table Removed)It can be seen from the data showed in table 1 that increasing the molar ratio of aniline to nitrobenzene will enhance the reaction selectivity, increase target products and reduce the by-products. However, in the practice, if the quantity of aniline is too large, the loss of aniline and the energy consumption during separation will increase. Example 18 Effect on condensation reaction imposed by water A continuous reactor was connected to a vacuum system and equipped with a temperature control system, and formed a local circulating system with a falling film evaporator and a circulating pump. Total volume of the reaction system was 1L. The system was firstly filled with aniline, and the flow of the circulating pump was set at 21/h. A mixing liquid containing nitrobenzene, aniline and the complex base catalyst at a molar ratio of nitrobenzene to aniline to OH" in the complex base catalyst of 1:7:1.15 was fed to the reactor at a certain flow. The system temperature was maintained as 75°C and the system pressure was maintained as O.OOSMPa (absolute). After the aniline was replaced by reaction liquid and reaction liquid was stable in composition, the feeding flow rate of the reaction mixture was varied to adjust the residence time. The water contents of reaction effluent, measured when the measured content of nitrobenzene was equal to or less than 0.1% and calculated yield based on 4-nitrosodiphenylamine and 4-nitrodiphenylamine generated was 97%, were listed below. (Table Removed)It can be seen that water content at the end of the reaction increases as the proportion of N,N-dimethyl-N,N-bis(ethoxylated (1-4 moles of ethylene oxide) propyl) ammonium carbonate in the complex catalyst increases. Namely, with the use of a complex base catalyst according to the present invention, the range of permitted water content in the reaction mixture at the end of reaction is greatly enlarged, that is, the yield is good enough even when there is a higher content of water in the reaction system. The less the water content is in the later phase of the reaction, the lower the dehydration efficiency is, thus reaction difficulty is reduced in the process according to the present invention. If only the tetramethyl ammonium hydroxide is used as catalyst, the yield is not 97% until the water content of reaction mixture is reduced to 1.2% by dehydration, which imposes difficulty to the reaction control and increases the power consumption. Example 19 Anhydrous complex catalyst prepared in example 12 and 65 Ig of aniline were charged into a four-necked flask with stirring device and thermometer. With stirring, the temperature was elevated to 75°C and pressure was reduced to O.OOSMPa (absolute pressure). Aniline was returned to the four-necked flask after demixing of the water-aniline azeotrope distilled until the water content in the system is less than 0.5%. 123g of nitrobenzene was dropwise added over 2h, then the dehydrating was continued for 4h. It was found via chromatographic analysis that the yield of 4-nitrosodiphenylamine and 4-nitrodiphenylamine was 97.4% and the water content in the system was less than 0.5%. Example 20 The comparison of continuous film reaction and complete mixing reaction Continuous film reactions and complete mixing reactions were conducted under the following conditions: molar ratio of aniline to nitrobenzene to OH" in complex base catalyst was controlled as 7.5:1:1, reaction temperature was 75°C, reaction time was 5h, and reaction pressure was O.OOSMPa (absolute pressure). Results were listed in Table 2 and Table 3. Table 2 Results of complete mixing reactions(Table Removed) Example 21 Batch hydrogenating example 500g of condensation liquid containing 17.5 weight percent of 4-nitrosodiphenylamine and 3.0 weight percent of 4-nitrodiphenylamine was charged into a 1L autoclave with stirring device and temperature control device. 150g of ethanol and 5g of the powdery composite catalyst prepared in example 1 were added thereto. The system atmosphere was replaced with hydrogen gas for three times, and then the system was pressurized to O.SMPa. While stirring, the reaction mixture was heated to 100°C and maintained at this temperature for 4h. At the end of the reaction, the mixture was cooled, and then discharged after pressure release. The reaction liquid was analyzed via HPLC, and was found containing no 4-nitrosodiphenylamine and 4-nitrodiphenylamine but 14.6% of 4-aminodiphylamine (chromatograph content). Comparison of powdery composite catalyst and noble metal catalyst Pd/C catalyst with 5 wt.% of palladium was compared with the powdery composite catalyst according to the present invention. Experiments were carried out under the same conditions as described in above batch hydrogenating example. The quantity of catalysts used was the same, and both Pd/C catalyst and powdery composite catalyst were recovered and reused after the reaction. Within 21 times of reuse, 4-nitrosodiphenylamine was undetectable in both reaction liquids. However, at the twenty-first time of reuse, the reaction liquid obtained by using Pd/C catalyst was found containing 0.1 wt.% of 4-nitrodiphylamine while the reaction liquid obtained by using the powdery composite catalyst according to the present invention was found containing no 4-nitrodiphylamine. The results showed that the antitoxic performance of the powdery composite catalyst according to the present invention was better than that of the noble metal catalyst. We claim: 1. A process for preparing 4-aminodiphenylamine from nitrobenzene and aniline as raw materials, a complex base catalyst as condensation catalyst and a powdery composite catalyst as hydrogenation catalyst, said process comprising five process stages: condensation; hydrogenation; separation I, i.e. separating, recovering and reusing complex base catalyst and separating, recovering and reusing powdery composite catalyst which is optionally at least partially regenerated; separation II, i.e. separating, recovering and reusing aniline and optionally separating, recovering and reusing hydrogenation solvent; and refining, , wherein the complex base catalyst used in the condensation reaction comprises a tetraalkyl ammonium hydroxide, an alkali metal hydroxide, and a tetraalkyl ammonium salt, and the powdery composite catalyst used in the hydrogenation reaction comprises nickel, aluminum and component A, said component A being at least one selected from the group consisting of Fe, Cu, Co, Mn, Cr, Mo, B and P, and wherein the content of nickel ranges from 25 to 99.9 wt.-%, and the total content of aluminum and component A ranges from 0.1 to 75 wt.-%. 2. The process for preparing 4-aminodiphenylamine as claimed in claim 1, wherein the condensation reaction is carried out under conditions of a molar ratio of nitrobenzene to aniline of from 1:1 to 1:15, a reaction temperature of from 20 to 150°C, a reaction pressure of from 0.005 to 0.1 MPa (absolute pressure) and a reaction time of from 3.5 to 6h. 3. The process for preparing 4-aminodiphenylamine as claimed in claim 1 or 2, wherein molar ratio of hydroxide ion in the complex base catalyst to nitrobenzene is in a range of from 1:4 to 4:1. 4. The process for preparing 4-aminodiphenylamine as claimed in claim 1, wherein molar ratio of tetraalkyl ammonium hydroxide to alkali metal hydroxide to tetraalkyl ammonium salt in the complex base catalyst equals (0-9):(0.5-3):(0.5-3), and the sum of concentration of tetraalkyl ammonium hydroxide, alkali metal hydroxide and tetraalkyl ammonium salt ranges from 10 to 100 percent by weight. 5. The process for preparing 4-aminodiphenylamine as claimed in any one ot claims 1 to 4, wherein the used complex base catalyst is prepared as follows: tetraalkyl ammonium hydroxide, alkali metal hydroxide or oxide and tetraalkyl ammonium salt, at desired molar ratio, are stirred in water at a temperature of from 0 to 90°C until being homogeneous, to form an aqueous form of the complex base catalysts, said tetraalkyl ammonium hydroxide, alkali metal hydroxide or oxide and tetraalkyl ammonium salt as raw materials being in solid form or in aqueous solution form. 6. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 4, wherein the used complex base catalyst is prepared as follows: tetraalkyl ammonium hydroxide, alkali metal hydroxide or oxide and tetraalkyl ammonium salt, at desired molar ratio, are stirred in water at a temperature of from 0 to 90°C until being homogeneous, then water is completely removed through azeotropic process by adding benzene, to form an anhydrous form of the complex base catalysts, said tetraalkyl ammonium hydroxide, alkali metal hydroxide or oxide and tetraalkyl ammonium salt as raw materials being in solid form or in aqueous solution form. 7. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 6, wherein the tetraalkyl ammonium salt is represented by a general formula of [(Rl)(R2)(R3)(R4)N]+nXn- wherein Rl, R2, R3 and R4, which may be identical or different, can be alkyl having from 1 to 4 carbon atoms, said alkyl being optionally substituted by a hydrophilic substituent; Xn- is selected from the group consisting of halide ion, sulfate radical, carbonate radical, phosphate radical, bicarbonate radical, bisulfate radical, Cl-C2-alkyl carbonate radical, Cl-C2-alkyl sulfate radical,; and n is a value of from 1 to 2. 8. The process for preparing 4-aminodiphenylamine as claimed in claim 7, wherein in said general formula of the tetraalkyl ammonium salt, at least one of Rl, R2, R3 and R4 is substituted by a hydrophilic substituent selected from the group consisting of hydroxy, methoxy, polyether, cationic polyamide, polyester, polyethylene polyamine and highly water-soluble quaternary ammonium salt-containing radical. 9. The process for preparing 4-aminodiphenylamine as claimed in claim 8, wherein the tetraalkyl ammonium salt is a hydrophilic substituent-carrying tetraalkyl ammonium salt selected from the group consisting of poly-methylated triethylene tetraamine sulfate, poly-methylated diethylene triamine carbonate, N,N-dimethyl-N,N-bis(methoxyethyl) ammonium carbonate, N-methyl-N,N,N-tri(methoxyethyl) ammonium carbonate, N,N,N-trimethyl-N-hydroxyethyl ammonium carbonate, trimethyl hydroxyethyl ammonium chloride, N,N,N-trimethyl-N-ethoxylated (1-4 moles of ethylene oxide) ethyl ammonium carbonate, N,N,N-trimethyl-N-ethoxylated (1-4 moles of ethylene oxide) propyl ammonium carbonate, N,N,N-trimethyl-N-ethoxylated (1-4 moles of ethylene oxide) propyl ammonium chloride, N,N-dimethyl-N,N-bis(ethoxylated (1-4 moles of ethylene oxide) propyl) ammonium carbonate. 10. The process for preparing 4-aminodiphenylamine as claimed in claim 7, wherein the tetraalkyl ammonium salt is selected from the group consisting of tetramethyl ammonium carbonate, tetramethyl ammonium methyl-carbonate, tetraethyl ammonium carbonate, tetraethyl ammonium ethyl-carbonate, tetramethyl ammonium sulfate, tetramethyl ammonium methyl-sulfate, tetraethyl ammonium sulfate, and tetraethyl ammonium ethyl-sulfate. 11. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 7 to 10, wherein the tetraalkyl ammonium salt is those prepared by reacting trialkyl amine with di(Cl-C2)alkyl carbonate or di(Cl-C2)alkyl sulfate in polar solvent,, 12. The process for preparing 4-aminodiphenylamine as claimed in claim 11, wherein the reaction for the preparation of the tetraalkyl ammonium salt is carried out under the following conditions: reaction pressure ranges from 0.1 to 3.0MPa, reaction temperature ranges from 50-200°C, reaction time ranges from 1.5 to 6h, molar ratio of trialkyl amine to di(Cl-C2)alkyl carbonate or di(Cl-C2)alkyl sulfate ranges from 2:1 to 1:2, the polar solvent used is methanol, ethanol or isopropanol, and the polar solvent is used in an amount of from 1 to 10 times of weight of the trialkyl amine. 13. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 12, wherein the condensation reaction is carried out in the absence ofoxygen. 14. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 13, wherein the condensation reaction is without additional or controlled proton material. 15. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 14, wherein the condensation reaction is carried out without any additional solvent. 16. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 15, wherein an amount of complex base catalyst is added during initial stage of the condensation reaction and only tetraalkyl ammonium salt and alkali metal hydroxide or oxide components of the complex base catalyst are replenished in the course of the reaction in the ratio of 4:1 tol :4. 17. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 16, wherein the condensation process stage is conducted in a circulating system consisting of a condensing circulating pump, a falling film reactor and a first reactor, and optional subsequent reactor(s). 18. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 17, wherein a falling film reactor is used in the condensation process stage and the falling film reactor utilizes ethanol vapor, hot water, steam or methanol vapor as heat medium. 19. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 18, wherein the hydrogenation reaction is carried out under the following conditions: hydrogen gas is used as reducing agent; volume ratio of gas to liquid is in a range of from 10:1 to 1500:1, weight ratio of solid to liquid is in a range of from 0.5:100 to 16:100, and weight ratio of solvent to condensation liquid is in a range of from 1:10 to 5:10, with the gas representing hydrogen gas, the liquid including solvent and condensation liquid, and the solid representing powdery composite catalyst; the temperature of hydrogenation reaction ranges from 50 to 100°C, the pressure of the reactor ranges from 0.2 to 3.0MPa (absolute pressure), and the reaction time ranges from 2 to 7h. 20. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 19, wherein the powdery composite catalyst used in the hydrogenation reaction is prepared by mixing powdery nickel, powdery aluminum and component A in desired proportion, then melting them at high temperature, followed by pulverizing them into powder after discharging and quenching, and then treating the powder with aqueous solution of a hydroxide. 21. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 20, wherein a magnetic separator is used to recover magnetic powdery composite catalyst after the hydrogenation reaction. 22. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to21, wherein recovered powdery composite catalyst is conveyed back to the hydrogenation reactor via a Venturi type mixed solid-liquid conveying equipment utilizing feeding power. 23. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 22, wherein deactivated powdery composite catalyst is regenerated either by treating with ultrasonic vibration or strong base, or the combination thereof. 24. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 23, wherein the solvent used in the hydrogenation reaction is either alcohol or water or its mixture thereof. 25. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 24, wherein separation I comprises of extraction of hydrogenation liquid from the hydrogenation reaction with extracting agent water, containing a polyether as co-extracting agent, and wherein volume ratio of the extracting agent to the hydrogenation liquid ranges from 0.5:1 to 5:1, preferably from 0.8:1 to 1.2:1, and extracting time ranges from 2 to 5h. 26. The process for preparing 4-aminodiphenylamine as claimed in claim 25, wherein the polyether co-extracting agent is selected from the group consisting of polyethylene glycol ether, polypropylene glycol ether, fatty alcohol polyethenoxy ether and mixture thereof, and volume ratio of the polyether co-extracting agent to water extracting agent ranges from 0.0001:1 to 0.005:1. 27. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 26, wherein the aqueous phase obtained by extracting hydrogenation liquid is concentrated by one-stage or multi-stage gas-aid falling film evaporators to recover the complex base catalyst. 28. The process for preparing 4-aminodiphenylamine as claimed in claim 27. wherein said gas-aid falling film evaporator includes shell pass (2'), tube pass (3'), steam inlet (8') installed on the top of shell pass (2'), condensed water outlet (1') installed at the bottom of shell pass (2'), lower concentration aqueous phase inlet (6') installed on the top of tube pass (3'), higher concentration aqueous phase outlet (9') installed at the bottom of tube pass (3'), flow-aiding steam inlet (5' and 7') installed on the top of tube pass (3') and distributing tray (4') installed at a position below the lower concentration aqueous phase inlet (6'). 29. The process for preparing 4-aminodiphenylamine as claimed in claim 27 or 28, wherein system pressure ranges from 0.005 to O.lMPa (absolute pressure), residence time ranges from 2 to 60s and pressure of flow-aiding steam is maintained in a range of from 0.01 to 0.5MPa during the concentration of the aqueous phase. 30. The process for preparing 4-aminodiphenylamine as claimed in any one of claims 1 to 29, wherein the refining is performed through three-column continuous rectification and batch rectification, and wherein rectification column 1, rectification column 2 and rectification column 3 are operated at a vacuum degree ranging independently from 0.09 to 0.098MPa; a still temperature of from 260 to 290°C, from 260 to 300°C and from 120 to 170°C, respectively; a reflux ratio of from 2:1 to 10:1, from 1:0.5 to 1:4 and from 1:0.5 to 1:2, respectively; and the batch rectification column is operated at a vacuum degree of from 0.09 to 0.098MPa, and a still temperature of from 280 to 330°C. 31. A process for preparing 4-aminodiphenylamine, comprising the steps of: i. continuously feeding nitrobenzene, aniline and a complex base catalyst, at flow rate ratio 3:15:20, to condensation process stage via metering pumps, and allowing them to react to form a condensation liquid (7) containing 4-nitrodiphenylamine, 4-nitrosodiphenylamine, and their salts thereof, or the mixtures thereof; ii. continuously feeding the condensation liquid (7) and a hydrogenation solvent, or mixture of one or more hydrogenation solvents (2) and optionally recovered hydrogenation solvent (5), 6.375:1 proportion of flow rate to hydrogenation process stage, and allowing them to react with hydrogen gas under the catalytic action of a powdery composite catalyst, or mixture of powdery composite catalysts (1) and reused, optionally regenerated, powdery composite catalyst (4), to form a hydrogenation liquid (8) containing 4-aminodiphenylamine; iii. feeding the hydrogenation liquid (8) to separation I process stage, where (a) powdery composite catalyst (4), which is to be recycled back to the hydrogenation process stage directly or after being at least partially regenerated, (b) complex base catalyst (3), which is to be recycled back to the condensation process stage, and (c) aqueous phase obtained by evaporation during concentration and organic phase obtained by extraction (9) are obtained; iv. feeding separately aqueous phase and organic phase (9) obtained in separation I process stage to separation II process stage, where (a) aniline (6), which is to be recycled back to the condensation process stage, (b) crude 4-aminodiphenylamine from which most aniline has been separated, and (c) optionally, hydrogenation solvent (5), which is to be recycled back to the hydrogenation process stage, are obtained; and v. feeding crude 4-aminodiphenylamine (10) to refining process stage, where (a) partial aniline (6), which is to be recycled back to the condensation process stage, and (b) the finished 4-aminodiphenylamine are obtained. Dated this 17th day of August 2005

Documents:

3623-DEL-1998-Abstract-03-03-2008.pdf

3623-DEL-1998-Claims-03-03-2008.pdf

3623-DEL-1998-Description (Complete)-03-03-2008.pdf

3623-DELNP-2005-Abstract-(08-08-2008).pdf

3623-DELNP-2005-Abstract-(08-09-2008).pdf

3623-DELNP-2005-Abstract-(26-12-2008).pdf

3623-delnp-2005-abstract.pdf

3623-DELNP-2005-Abstract17-04-2008-1.pdf

3623-DELNP-2005-Abstract17-04-2008-2.pdf

3623-DELNP-2005-Abstract17-04-2008-3.pdf

3623-DELNP-2005-Abstract17-04-2008-4.pdf

3623-DELNP-2005-Abstract17-04-2008-6.pdf

3623-DELNP-2005-Abstract17-04-2008-7.pdf

3623-DELNP-2005-Abstract17-04-2008-8.pdf

3623-DELNP-2005-Abstract17-04-2008-9.pdf

3623-DELNP-2005-Claims-(08-08-2008).pdf

3623-DELNP-2005-Claims-(08-09-2008).pdf

3623-DELNP-2005-Claims-(26-12-2008).pdf

3623-DELNP-2005-Claims-17-04-2008-1.pdf

3623-DELNP-2005-Claims-17-04-2008-2.pdf

3623-DELNP-2005-Claims-17-04-2008-3.pdf

3623-DELNP-2005-Claims-17-04-2008-4.pdf

3623-DELNP-2005-Claims-17-04-2008-6.pdf

3623-DELNP-2005-Claims-17-04-2008-7.pdf

3623-DELNP-2005-Claims-17-04-2008-8.pdf

3623-DELNP-2005-Claims-17-04-2008-9.pdf

3623-delnp-2005-claims.pdf

3623-DELNP-2005-Correspondence-Others -17-04-2008.pdf

3623-DELNP-2005-Correspondence-Others-(08-09-2008).pdf

3623-DELNP-2005-Correspondence-Others-(17-03-2011).pdf

3623-DELNP-2005-Correspondence-Others-(26-12-2008).pdf

3623-DELNP-2005-Correspondence-Others-27-05-2008.pdf

3623-delnp-2005-correspondence-others.pdf

3623-DELNP-2005-Description (Complete)-08-09-2008.pdf

3623-DELNP-2005-Description (Complete)-17-04-2008-1.pdf

3623-DELNP-2005-Description (Complete)-17-04-2008-2.pdf

3623-DELNP-2005-Description (Complete)-17-04-2008-3.pdf

3623-DELNP-2005-Description (Complete)-17-04-2008-4.pdf

3623-DELNP-2005-Description (Complete)-17-04-2008-6.pdf

3623-DELNP-2005-Description (Complete)-17-04-2008-7.pdf

3623-DELNP-2005-Description (Complete)-17-04-2008-8.pdf

3623-DELNP-2005-Description (Complete)-17-04-2008-9.pdf

3623-delnp-2005-description (complete).pdf

3623-DELNP-2005-Drawings-(08-09-2008).pdf

3623-DELNP-2005-Drawings-17-04-2008-2.pdf

3623-DELNP-2005-Drawings-17-04-2008-3.pdf

3623-DELNP-2005-Drawings-17-04-2008-4.pdf

3623-DELNP-2005-Drawings-17-04-2008-8.pdf

3623-DELNP-2005-Drawings-17-04-2008-9.pdf

3623-delnp-2005-drawings.pdf

3623-delnp-2005-form-1.pdf

3623-delnp-2005-form-13-(20-03-2009).pdf

3623-delnp-2005-form-13-(25-04-2008).pdf

3623-delnp-2005-form-18.pdf

3623-delnp-2005-form-2.pdf

3623-DELNP-2005-Form-26-27-05-2008.pdf

3623-DELNP-2005-Form-3-(08-08-2008).pdf

3623-DELNP-2005-Form-3-(08-09-2008).pdf

3623-DELNP-2005-Form-3-(26-12-2008).pdf

3623-delnp-2005-form-3.pdf

3623-DELNP-2005-Form-5-(08-08-2008).pdf

3623-DELNP-2005-Form-5-(08-09-2008).pdf

3623-delnp-2005-form-5.pdf

3623-delnp-2005-form-6-(20-03-2009).pdf

3623-delnp-2005-form-6-(25-04-2008).pdf

3623-DELNP-2005-Others Docoment-17-04-2008-2.pdf

3623-DELNP-2005-Others Docoment-17-04-2008-3.pdf

3623-DELNP-2005-Others Docoment-17-04-2008-4.pdf

3623-DELNP-2005-Others Docoment-17-04-2008-6.pdf

3623-DELNP-2005-Others Docoment-17-04-2008-8.pdf

3623-DELNP-2005-Others Docoment-17-04-2008-9.pdf

3623-DELNP-2005-Others-Docoment-17-04-2008-1.pdf

3623-DELNP-2005-Others-Docoment-17-04-2008-7.pdf

3623-DELNP-2005-Others-Document-(08-09-2008).pdf

3623-delnp-2005-pct-210.pdf

3623-delnp-2005-pct-237.pdf

3623-delnp-2005-pct-308.pdf

3623-delnp-2005-pct-332.pdf