CN1187316C - Method for preparing 4-amino diphenylamine - Google Patents
Method for preparing 4-amino diphenylamine Download PDFInfo
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- CN1187316C CN1187316C CNB031481914A CN03148191A CN1187316C CN 1187316 C CN1187316 C CN 1187316C CN B031481914 A CNB031481914 A CN B031481914A CN 03148191 A CN03148191 A CN 03148191A CN 1187316 C CN1187316 C CN 1187316C
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- China
- Prior art keywords
- aniline
- aminodiphenylamine
- hydrogenation
- mirbane
- oil
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- ATGUVEKSASEFFO-UHFFFAOYSA-N p-aminodiphenylamine Chemical compound C1=CC(N)=CC=C1NC1=CC=CC=C1 ATGUVEKSASEFFO-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title claims abstract description 48
- PAYRUJLWNCNPSJ-UHFFFAOYSA-N Aniline Chemical compound NC1=CC=CC=C1 PAYRUJLWNCNPSJ-UHFFFAOYSA-N 0.000 claims abstract description 88
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 61
- 239000003054 catalyst Substances 0.000 claims abstract description 47
- 239000007788 liquid Substances 0.000 claims abstract description 41
- 239000002131 composite material Substances 0.000 claims abstract description 35
- 238000006243 chemical reaction Methods 0.000 claims abstract description 31
- LQNUZADURLCDLV-UHFFFAOYSA-N nitrobenzene Chemical compound [O-][N+](=O)C1=CC=CC=C1 LQNUZADURLCDLV-UHFFFAOYSA-N 0.000 claims abstract description 26
- 238000004519 manufacturing process Methods 0.000 claims abstract description 20
- 239000002904 solvent Substances 0.000 claims abstract description 19
- 238000009833 condensation Methods 0.000 claims abstract description 14
- 230000005494 condensation Effects 0.000 claims abstract description 14
- 238000006482 condensation reaction Methods 0.000 claims abstract description 13
- 238000007670 refining Methods 0.000 claims abstract description 11
- 238000000926 separation method Methods 0.000 claims abstract description 8
- 239000000843 powder Substances 0.000 claims description 57
- 150000001875 compounds Chemical class 0.000 claims description 34
- 238000011084 recovery Methods 0.000 claims description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical group [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 13
- 229910052739 hydrogen Inorganic materials 0.000 claims description 13
- 239000001257 hydrogen Substances 0.000 claims description 13
- 229910052751 metal Inorganic materials 0.000 claims description 9
- 239000002184 metal Substances 0.000 claims description 9
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 8
- 150000005622 tetraalkylammonium hydroxides Chemical group 0.000 claims description 8
- 150000008044 alkali metal hydroxides Chemical class 0.000 claims description 7
- 239000004411 aluminium Substances 0.000 claims description 7
- 229910052782 aluminium Inorganic materials 0.000 claims description 7
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 7
- 239000012043 crude product Substances 0.000 claims description 7
- 229910052755 nonmetal Inorganic materials 0.000 claims description 7
- 238000002360 preparation method Methods 0.000 claims description 7
- 238000010992 reflux Methods 0.000 claims description 7
- 239000000126 substance Substances 0.000 claims description 7
- 150000005621 tetraalkylammonium salts Chemical class 0.000 claims description 7
- 230000002378 acidificating effect Effects 0.000 claims description 6
- 239000003513 alkali Substances 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 claims description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 4
- 239000002253 acid Substances 0.000 claims description 4
- 229910000272 alkali metal oxide Inorganic materials 0.000 claims description 4
- 239000007864 aqueous solution Substances 0.000 claims description 4
- -1 inorganic acid salt Chemical class 0.000 claims description 4
- 229910052759 nickel Inorganic materials 0.000 claims description 4
- 230000008929 regeneration Effects 0.000 claims description 4
- 238000011069 regeneration method Methods 0.000 claims description 4
- 238000003756 stirring Methods 0.000 claims description 4
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 claims description 4
- 229910052804 chromium Inorganic materials 0.000 claims description 3
- 229910052802 copper Inorganic materials 0.000 claims description 3
- 239000010949 copper Substances 0.000 claims description 3
- 230000004927 fusion Effects 0.000 claims description 3
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 3
- 239000011707 mineral Substances 0.000 claims description 3
- 235000010755 mineral Nutrition 0.000 claims description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 2
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 claims description 2
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims description 2
- 150000001342 alkaline earth metals Chemical class 0.000 claims description 2
- 229910052728 basic metal Inorganic materials 0.000 claims description 2
- 150000003818 basic metals Chemical class 0.000 claims description 2
- 229910052796 boron Inorganic materials 0.000 claims description 2
- 235000011089 carbon dioxide Nutrition 0.000 claims description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 claims description 2
- JYYOBHFYCIDXHH-UHFFFAOYSA-N carbonic acid;hydrate Chemical compound O.OC(O)=O JYYOBHFYCIDXHH-UHFFFAOYSA-N 0.000 claims description 2
- 239000007789 gas Substances 0.000 claims description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims description 2
- 229910052742 iron Inorganic materials 0.000 claims description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 2
- 229910052748 manganese Inorganic materials 0.000 claims description 2
- 229910052750 molybdenum Inorganic materials 0.000 claims description 2
- 230000007935 neutral effect Effects 0.000 claims description 2
- 229910017604 nitric acid Inorganic materials 0.000 claims description 2
- 230000035484 reaction time Effects 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- 230000007062 hydrolysis Effects 0.000 claims 1
- 238000006460 hydrolysis reaction Methods 0.000 claims 1
- 238000011112 process operation Methods 0.000 claims 1
- 238000000746 purification Methods 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 17
- 239000002994 raw material Substances 0.000 abstract description 12
- 230000002829 reductive effect Effects 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 2
- 239000006227 byproduct Substances 0.000 abstract description 2
- 230000003197 catalytic effect Effects 0.000 abstract 1
- 238000003912 environmental pollution Methods 0.000 abstract 1
- 239000000463 material Substances 0.000 description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 241000282326 Felis catus Species 0.000 description 12
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 12
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- XXYMSQQCBUKFHE-UHFFFAOYSA-N 4-nitro-n-phenylaniline Chemical compound C1=CC([N+](=O)[O-])=CC=C1NC1=CC=CC=C1 XXYMSQQCBUKFHE-UHFFFAOYSA-N 0.000 description 8
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 8
- OIJHFHYPXWSVPF-UHFFFAOYSA-N para-Nitrosodiphenylamine Chemical compound C1=CC(N=O)=CC=C1NC1=CC=CC=C1 OIJHFHYPXWSVPF-UHFFFAOYSA-N 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 7
- 150000004678 hydrides Chemical class 0.000 description 7
- 238000001914 filtration Methods 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 150000003839 salts Chemical class 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000012074 organic phase Substances 0.000 description 4
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 3
- 150000001298 alcohols Chemical class 0.000 description 3
- 238000000998 batch distillation Methods 0.000 description 3
- 230000005587 bubbling Effects 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 3
- 229910052979 sodium sulfide Inorganic materials 0.000 description 3
- CZGCEKJOLUNIFY-UHFFFAOYSA-N 4-Chloronitrobenzene Chemical compound [O-][N+](=O)C1=CC=C(Cl)C=C1 CZGCEKJOLUNIFY-UHFFFAOYSA-N 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- 239000011651 chromium Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- DYDNPESBYVVLBO-UHFFFAOYSA-N formanilide Chemical compound O=CNC1=CC=CC=C1 DYDNPESBYVVLBO-UHFFFAOYSA-N 0.000 description 2
- 238000004845 hydriding Methods 0.000 description 2
- 239000006148 magnetic separator Substances 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- NQPDZGIKBAWPEJ-UHFFFAOYSA-N pentanoic acid group Chemical group C(CCCC)(=O)O NQPDZGIKBAWPEJ-UHFFFAOYSA-N 0.000 description 2
- 239000010948 rhodium Substances 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- WGTYBPLFGIVFAS-UHFFFAOYSA-M tetramethylammonium hydroxide Chemical compound [OH-].C[N+](C)(C)C WGTYBPLFGIVFAS-UHFFFAOYSA-M 0.000 description 2
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 1
- OKIZCWYLBDKLSU-UHFFFAOYSA-M N,N,N-Trimethylmethanaminium chloride Chemical compound [Cl-].C[N+](C)(C)C OKIZCWYLBDKLSU-UHFFFAOYSA-M 0.000 description 1
- UBUCNCOMADRQHX-UHFFFAOYSA-N N-Nitrosodiphenylamine Chemical compound C=1C=CC=CC=1N(N=O)C1=CC=CC=C1 UBUCNCOMADRQHX-UHFFFAOYSA-N 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000003963 antioxidant agent Substances 0.000 description 1
- 239000008346 aqueous phase Substances 0.000 description 1
- 230000003190 augmentative effect Effects 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 238000010523 cascade reaction Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- 229910021472 group 8 element Inorganic materials 0.000 description 1
- 238000004128 high performance liquid chromatography Methods 0.000 description 1
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 1
- 230000006698 induction Effects 0.000 description 1
- 239000000543 intermediate Substances 0.000 description 1
- 238000007885 magnetic separation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 229910001092 metal group alloy Inorganic materials 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- NLRKCXQQSUWLCH-UHFFFAOYSA-N nitrosobenzene Chemical compound O=NC1=CC=CC=C1 NLRKCXQQSUWLCH-UHFFFAOYSA-N 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 238000010129 solution processing Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The present invention discloses a method for preparing 4-amino diphenylamine from nitrobenzene and aniline as raw materials of production. A composite base catalyst and a composite powdery catalyst corresponding to condensation reaction and hydrogenation reaction are selected respectively, and a circulation process is composed of the sequential working procedures of condensation, separation of the composite base catalysts, hydrogenation, separation of hydrogenation solvent, the composite powdery catalysts and aniline, refining, etc. The preparing method is continuous. The two selected composite catalysts have the advantages of low price, high catalytic activity, mild reaction condition, few byproducts, high conversion rate and high selectivity. The labor intensity of technical operation is low, and no corrosive liquid is generated, so that environmental pollution is reduced. The content of 4-amino diphenylamine reaches 99 wt%, and the yield of industrial scale production is higher than 92%.
Description
Technical field
The present invention relates to prepare the method for 4-aminodiphenylamine, being specifically related to oil of mirbane, aniline is raw material, adopts two kinds of composite catalysts and cyclical operation technical process, prepares the method for 4-aminodiphenylamine continuously.
Background technology
The 4-aminodiphenylamine is the intermediates of important antioxidants and stablizer, it is important chemical product in rubber industry and the polymer industry, according to the difference of using raw material, at present, the method of producing the 4-aminodiphenylamine has, and (1) aniline process is a raw material with p-Nitrophenyl chloride and aniline, reaction generates 4 nitrodiphenyl amine under catalyst action, is the 4-aminodiphenylamine with sodium sulfide reducing then.(2) formylaniline method is that the raw material condensation generates formylaniline with formic acid and aniline, reacts in the presence of acid binding agent with p-Nitrophenyl chloride to generate 4 nitrodiphenyl amine again, prepares the 4-aminodiphenylamine with sodium sulfide reducing then.(3) pentanoic method, it promptly is raw material with the pentanoic, in organic solvent, carry out nitrosification with nitrite, obtain N nitrosodiphenyl amine, again with anhydrous hydrogen chloride reset 4-nitrosodiphenylamine hydrochloride, with in the alkali and generate the 4-nitrosodiphenylamine, get the 4-aminodiphenylamine with sodium sulfide reducing at last.Although these method raw material differences are all made reductive agent with Sodium Sulphide and produced the 4-aminodiphenylamine, the shortcoming of these reactions is severe reaction conditions, complicated operation, and the energy consumption height, yield is low, and cost is high and produce contaminate environment etc. with " three wastes ".
In recent years, produce the raw material that the 4-aminodiphenylamine adopts and mostly be oil of mirbane or oil of mirbane and aniline or nitrosobenzene, carry out condensation reaction, then with hydrogen hydrogenation make (referring to publication number CN1209430A, CN1235153A, CN1193010A, CN1307556A).Above-mentioned the whole bag of tricks is that the mixture with hydrogen hydrogenation such as above raw material prepares the 4-aminodiphenylamine in the presence of catalyzer, but all there are some common shortcomings: the one,, selected catalyzer costs an arm and a leg, applicable industry scale production meeting causes production cost too high, and comparing with present production technique does not have advantage.For example, contract and react noble dilute metal palladium (Pd) that the tetraalkylammonium hydroxide used and hydrogenation adopt, platinum (Pt), rhodium (Rh) etc., raw material sources are few, and price is extremely expensive.The 2nd,, operate more loaded down with trivial detailsly, be unfavorable for serialization production, so industrial scale is restricted.The 3rd,, product purity is not high.
Summary of the invention
The technical issues that need to address of the present invention are to select to be used for catalyzer and technical process that is suitable for industrial-scale production of condensation, hydrogenation, inexpensive and superior performance, prepare the 4-aminodiphenylamine continuously.
The present invention is by adopt compound alkaline catalysts and composite powder powder catalyzer respectively in condensation and hydriding process, and carry out condensation successively, separate I, the cyclical operation flow process of hydrogenation, separation II and five operations such as refining, prepare the 4-aminodiphenylamine continuously.
Detailed content of the present invention is as follows:
In the technical process of the present invention, " separate I " is meant and is meant " separate, reclaim and apply mechanically compound alkaline catalysts ", " separating II " " separate, reclaim and apply mechanically hydrogenation solvent and aniline, separate, reclaim and apply mechanically composite powder powder catalyzer ".
Technical process of the present invention is, with oil of mirbane, compound alkaline catalysts, aniline by a certain percentage, enter the condensation operation continuously by volume pump, reaction generation 4 nitrodiphenyl amine and 4-nitrosodiphenylamine are or/and behind the condensated liquid of their salt, enter and separate the I operation, promptly separate compound alkaline catalysts, and compound alkaline catalysts is applied mechanically retraction close operation, the condensated liquid and the hydrogenation solvent that have separated compound alkaline catalysts enter hydrogenation process according to certain proportioning, under the effect of composite powder powder catalyzer, generate the hydride that contains the 4-aminodiphenylamine with hydrogen reaction, enter then and separate the II operation, return hydrogenation process behind a small amount of composite powder powder catalyst regeneration of carrying secretly in the hydrogenation process that filtration is obtained and apply mechanically.The Separation and Recovery hydrogenation solvent is applied mechanically back hydrogenation process in the hydride.Separate, reclaimed most aniline, apply mechanically retraction and close operation.The crude product that will contain the 4-aminodiphenylamine then enters refining step, and cutting out partial aniline is applied mechanically retraction and closed operation, and the finished product of gained is the 4-aminodiphenylamine, whole technological cycle operation, and preparation is continuously.
The operating process of each procedure technology is as follows:
Condensation reaction is by volume pump oil of mirbane, aniline and compound alkaline catalysts to be entered the forced heat-exchanging device in proportion continuously to dewater, reaction, and water vapour is through being condensed into water; Condensated liquid in the forced heat-exchanging device is squeezed into A reactor from its top, continues dehydration, reaction, then, by the condensation recycle pump of reactor bottom, condensated liquid is returned the forced heat-exchanging device again, and material constitutes the local circulation system of condensation reaction of the present invention through circulation constantly like this.Material constantly dewaters, and reaction is along with increasing of condensated liquid in the A reactor, upflow tube by this reactor side enters second reactor and staged reactor, dewater, reaction generates at last and contains 4 nitrodiphenyl amine and 4-nitrosodiphenylamine or/and the condensated liquid of their salt.
The ratio of oil of mirbane that condensation reaction is adopted and aniline is 1: 1-1: 15 (moles), preferably than being 1: 4-1: 10 (moles), the reaction temperature be 20-150 (℃), preferred 50-90 (℃), reaction pressure (absolute pressure) is 0.005-0.1 (MPa), material residence time in whole reactor be 3.5-6 (hour).
The aqueous solution that the compound alkaline catalysts that condensation reaction is adopted is made up of tetraalkylammonium hydroxide, alkali metal hydroxide or its oxide compound and tetraalkylammonium salt, wherein tetraalkylammonium hydroxide, alkali metal hydroxide and tetra-allkylammonium salt concn summation are 15-50 (weight %), be preferably 25-38 (weight %), three's ratio is (2-9): (0.5-3): (0.5-3) (mole).If adopt alkalimetal oxide, then the consumption in its catalyzer can convert by corresponding oxyhydroxide and get.The ratio of hydroxide ion and oil of mirbane is 1 in the compound alkaline catalysts: 4-4: 1 (mole).
The preparation method of the compound alkaline catalysts that condensation reaction is adopted is, with tetraalkylammonium hydroxide, alkali metal hydroxide, tetraalkylammonium salt is (2-9) in molar ratio: (0.5-3): (0.5-3), be added in certain water gaging, three's concentration summation is 15-50 (weight %), be preferably 25-38 (weight %) controlled temperature, stir, promptly get this compound alkaline catalysts.If adopt alkalimetal oxide, then its consumption in catalyzer can convert by corresponding oxyhydroxide and get.
Separating the I operation is, contains 4 nitrodiphenyl amine and 4-nitrosodiphenylamine or/and after their the salt condensated liquid filtration, add acidic substance the pH value of solution value is remained on about 8.After the solution layering, organic phase is the mixture of 4 nitrodiphenyl amine and 4-nitrosodiphenylamine.Then, add alkaline matter to water layer, the hydrogen ion mol ratio in the hydroxide ion in the alkaline matter and the original acidic substance that add is 1: 1-3: 1, obtain compound alkaline catalysts, and recovery set is used.
Separating the acidic substance that adopt in the I operation can be mineral acid, its oxide compound and water and other inorganic acid salt, example hydrochloric acid, sulfuric acid, nitric acid, carbonic acid, sodium bicarbonate, carbonic acid gas and water, sulphur trioxide and water etc., the alkali that adopts can be the oxyhydroxide of basic metal and alkaline-earth metal, need select corresponding acidic substance, alkali according to tetraalkylammonium salt and alkali in the compound alkaline catalysts.
Hydrogenation process is, condensated liquid and hydrogenation solvent and the composite powder powder catalyzer after sedimentation and magnetic Separation and Recovery are successively entered one-level by the solid-liquid e Foerderanlage, secondary or multistage hydrogenation reactor, hydrogen enters from reactor bottom by the form of hydrogen recycle machine with bubbling, the control certain condition carries out hydrogenation, generation contains the hydride of 4-aminodiphenylamine, separate with magnetic separator through settling vessel being hydrogenated the composite powder powder catalyzer that liquid carries secretly, make catalyzer pass through the solid-liquid e Foerderanlage, reenter the A reactor recycled, obtain containing the hydride of 4-aminodiphenylamine simultaneously.For hydrogenation is normally carried out continuously, in the reaction process, need to replenish the fresh composite powder powder catalyzer of interpolation.
In the hydrogenation, by selecting composite powder powder catalyzer for use, by hydrogen recycle and catalyst recirculation, and the control associated process conditions, hydrogenation is carried out continuously.
Alcohols selected by hydrogenation solvent or/and water, wherein alcohols particular methanol or ethanol or Virahol, and hydrogenation solvent can be a recycled.
In the continuous hydrogenation process, the circulation of hydrogen adopts the form of bubbling to enter reactor, and whole hydriding process takes continuously feeding, the placed in-line complete mixing flow mode of multi-stage reacting kettle to carry out.
In the hydrogenation, vapour-liquid ratio is 10: 1-1500: 1 (volume), solid-to-liquid ratio is 0.5: 100-6: 100 (weight), gas promptly refers to hydrogen, and liquid comprises solvent and condensated liquid, and solid promptly refers to composite powder powder catalyzer, solvent: condensated liquid=1: 10-5: 10 (weight), the hydrogenation temperature be 50-140 (℃), pressure is 0.2-3.0 (MPa), the residence time of reaction is 2-7 hour.
The composite powder powder catalyzer that hydrogenation adopted, its composition be nickel (Ni), aluminium (Al) and " other metal or nonmetal " (A), wherein A is a kind of among Fe, Cu, Cr, Co, Mn, Mo, B, the P, consisting of of catalyzer, nickel (Ni) content is 25-99.9 (weight %), aluminium (Al) and " other metal or nonmetal " (A) content are 0.1-75 (weight %), and the order number of catalyzer is the 40-300 order.
The composite powder powder Preparation of catalysts method of hydrogenation is, gets a certain amount of nickel powder, and aluminium powder and " other metal or nonmetal " are (A), fusion under the condition of high temperature, pulverize powdered after the discharging, order is counted the 40-300 order, makes with the hydroxide aqueous solution processing under certain temperature and concentration.
The circulation of composite powder powder catalyzer is to carry out Separation and Recovery by sedimentation, magnetic separating device, promptly is hydrogenated the composite powder powder catalyzer that liquid is carried secretly, and the solid-liquid e Foerderanlage by a kind of Venturi-type turns back to catalyzer in the hydrogenation reactor recycled.
Because after the condensation reaction, compound alkaline catalysts is separated before hydrogenation, so hydrogenation is selected the range extension of catalyzer for use, can for group VIII element or copper on the periodic table of elements, chromium as load etc. the common hydrogenation catalyst of industry, temperature of reaction can from 50-140 (℃), also can be granular catalyzer, hydrogenation reactor can be a thermopnore, also can be one or more levels fixed bed cascade reaction.
Separating the II operation is, by volume pump with the gained hydride with carry the minute quantity composite powder powder catalyzer of not separated recovery wherein secretly, filtration obtains composite powder powder catalyzer, returns hydrogenation process after the regeneration, and the gained hydride enters rectifying tower continuously, cat head is isolated hydrogenation solvent, apply mechanically back hydrogenation process, tower still feed liquid enters the aniline tower, and cat head obtains aniline, apply mechanically retraction and close operation, the tower still contains the crude product of 4-aminodiphenylamine; But hydrogenation solvent can enter the aniline tower after selecting the water layering for use; Hydrogenation solvent is selected alcohols and water for use, and behind the then first standing demix, rectifying obtains solvent and aniline and recovery set usefulness respectively again.
Refining step is with the crude product of above-mentioned 4-aminodiphenylamine, to adopt three tower continuous rectifications and batch fractionating to make with extra care and reclaim aniline.Feed liquid is gone in No. 1 rectifying tower by pump delivery, cat head discharging aniline, azophenlyene and nitrogen benzide, the discharging of tower still is a crude product 4-aminodiphenylamine, the cat head discharging of No. 1 rectifying tower enters in No. 3 rectifying tower, No. 3 the rectifying tower cat head steams aniline, its content is 99%, operation before can directly applying mechanically back, remaining azophenlyene of tower still and nitrogen benzide.No. 1 rectifying tower tower bottoms is by pump delivery to 2 tower, No. 2 the rectifying tower cat head distills out finished product 4-aminodiphenylamine, tower still feed liquid runs up to a certain amount of, enter the batch still distillation, distill out remaining a spot of 4-aminodiphenylamine in the feed liquid, eject material from still and return rectifying tower No. 2, other material slag is emitted at the bottom of by still.
Process for refining of the present invention, the vacuum tightness of its No. 1 rectifying tower are 0.09-0.098 (MPa), and reflux ratio is 2: 1-10: 1, tower top temperature be 80-130 (℃), tower still temperature be 260-290 (℃); The vacuum tightness of No. 2 rectifying tower is 0.09-0.098 (MPa), and reflux ratio is 1: 0.5-1: 4, tower top temperature be 140-190 (℃), tower still temperature be 260-300 (℃); The vacuum tightness of No. 3 rectifying tower is 0.09-0.098 (MPa), and reflux ratio is 1: 0.5-1: 2, tower top temperature be 80-120 (℃), tower still temperature be 120-170 (℃).The tower still temperature of No. 2 rectifying tower is relatively low, reduced the coking degree of 4-aminodiphenylamine, account for total amount 96% the 4-aminodiphenylamine oneself separate at the cat head of No. 2 rectifying tower of relatively low tower still temperature and make, thereby the amount of carrying out 4-aminodiphenylamine in the feed liquid of batch distillation significantly reduces.The batch still temperature be 280-330 (℃), batch distillation top temperature be 235-250 (℃), vacuum tightness is 0.09-0.098 (MPa).
In the above-mentioned refining step of the present invention, No. 1 rectifying tower and No. 2 rectifying tower adopt shallow liquid layer formula vaporizer heating, and heating agent adopts high-temperature molten salt, and No. 3 rectifying tower adopts steam heating, and batch distillation adopts the chuck heating, and heating agent adopts high-temperature molten salt.
The method for preparing the 4-aminodiphenylamine of the present invention, with oil of mirbane and aniline is raw material, successively through condensation, separate compound alkaline catalysts, hydrogenation, separate hydrogenation solvent and powder catalyst and aniline, operation such as refining, by selecting compound alkaline catalysts catalyzing and condensing reaction for use and before hydrogenation, it being separated and recovery set usefulness, avoided the thermo-sensitivity resolution problem of compound alkaline catalysts in the hydrogenation operation, increased the range of choice of hydrogenation catalyst greatly, thereby can select more cheap hydrogenation catalyst, reduced cost, increased the hydrogenation temperature range, can select fixed-bed reactor, reduce the industrialization technology difficulty of hydrogenation, in the whole process of preparation with loaded particles shape catalyzer, the reaction conditions gentleness, by product is few, transformation efficiency and selectivity height, and labour intensity is low, do not produce corrosive liquid, alleviated the pollution to environment, the content of 4-aminodiphenylamine is higher than 99 (weight %), and the industrial-scale production yield of this technological process is greater than 92%.
Description of drawings
Accompanying drawing is the process flow sheet for preparing the method for 4-aminodiphenylamine
Reference numeral
1---the compound alkaline catalysts of recovery set
2---composite powder powder catalyzer
3---hydrogenation solvent
4---the composite powder powder catalyzer of recovery set after the regeneration
5---the recovery set hydrogenation solvent
6---recovery set aniline
Embodiment
Open composite catalyst simultaneously, aniline and oil of mirbane transferpump, regulate flow to 150 kilograms/hour of aniline, 30 kilograms/hour in oil of mirbane, compound alkaline catalysts double centner/hour, enter continuously in the forced heat-exchanging device, the heating agent of forced heat-exchanging device adopts alcohol steam, condensated liquid in the forced heat-exchanging device is squeezed into A reactor from its top, continue dehydration, reaction, open A reactor bottom valve and condensation recycle pump then, regulate condensation circulating-pump outlet valve, material is turned back in the forced heat-exchanging device, form the local circulation system, material constantly circulates like this, dehydration, reaction.75 ℃ of control reaction temperature, pressure (absolute pressure) 0.008MPa, the Control Circulation flow quantity is at 2 meters
3/ hour.Along with raw material constantly enters, material in the A reactor constantly increases, when treating that material in the A reactor rises to A reactor to the pipe connecting of second reactor, the material overflow is to second reactor, in second reactor dewater more fully, condensation reaction.The total residence time of control material in reactor 5 hours, reaction finish material and detect less than oil of mirbane by analysis.
The gained condensated liquid enters continuously and separates I operation, the compound alkaline catalysts of recovery set.Filtering back continuous adding concentration of hydrochloric acid is 36 (weight %), flow is 25.8 kilograms/hour remains on about 8 the pH value of solution value, behind the system layering, the speed of 10.2 kilograms/hour in sodium hydroxide is added aqueous phase, filtration makes the compound alkaline catalysts that obtains turn back to condensation operation recycled, and organic phase obtains the mixed solution of 4 nitrodiphenyl amine and 4-nitrosodiphenylamine.
The organic phase of separating the I gained enters hydrogenation process, completes bed material, uses hydrogen exchange nitrogen, and pressurising is started circulator and kept the flow of recycle hydrogen at 6 meters to 1.3MPa
3(mark side)/hour, hydrogen enters hydrogenation reactor by circulator with the form of bubbling, the mass transfer effect of gas-liquid during with augmenting response, regulating its organic phase flow is 180 kilograms/hour, the flow of methyl alcohol is 60 kilograms/hour (weight %), enter the one-level hydrogenation reactor, reactor has magnetic seal and stirs, and the cooling heating system is added composite powder powder catalyzer simultaneously, the temperature 75-80 of maintenance reaction (℃), pressure 1.3MPa, the residence time is 5 hours, solid-to-liquid ratio 3: 100, the reduced liquid of system overflows to the second order reaction still from the first order reaction still, the third order reaction still overflows to subsider, under the effect of magnetic separator, the maximum possible recovery catalyzer, subsider bottom contain the bigger solidliquid mixture of solid catalyst concentration, through the solid-liquid e Foerderanlage, come back to reactor, realized applying mechanically circulation the circulation of hydrogen like this at the continuous production catalyzer.Reduced liquid detects through high performance liquid chromatography, does not contain 4 nitrodiphenyl amine, the 4-nitrosodiphenylamine.
Enter and separate the II preface, wherein the minute quantity composite powder powder catalyzer of separated recovery is not after filtration, apply mechanically back hydrogenation process after composite powder powder catalyzer regenerated again, the gained hydride with 240 kilograms/, the time enter methanol column, cat head is isolated methyl alcohol, applies mechanically back hydrogenation process, tower still feed liquid enters the aniline tower, cat head obtains aniline, applies mechanically retraction and closes operation, and the tower still contains the crude product of 4-aminodiphenylamine.
The crude product that contains the 4-aminodiphenylamine (containing the 4-aminodiphenylamine, aniline, nitrogen benzide, azophenlyene) that will merge the back gained after several covers after the above-mentioned same treatment separate the II operations enters rectifying tower with 120 kilograms/hour of flows No. 1 continuously by toothed gear pump.270 ℃ of control tower still temperature, 110 ℃ of control tower top temperatures, vacuum tightness is at 0.094Mpa, reflux ratio 5: 1, light constituent aniline, nitrogen benzide, three kinds of materials of azophenlyene are from the cat head extraction, and flow is about 26.2 kilograms/hour, enter rectifying tower No. 3,150 ℃ of No. 3 rectifying Tata still temperature, 90 ℃ of tower top temperatures, vacuum tightness 0.094MPa, reflux ratio 1: 1, cat head distills out aniline for 24 kilograms/hour with flow, what the tower still was remaining is nitrogen benzide, azophenlyene, No. 1 the rectifying tower tower bottoms enters rectifying tower No. 2, keeps 280 ℃ of tower still temperature, tower top temperature is controlled at 170 ℃, reflux ratio 1: 1, it is finished product 4-aminodiphenylamine that vacuum tightness 0.097MPa, the cat head of No. 2 rectifying tower obtain, No. 2 the rectifying tower bottoms enters batch still, the still temperature from 285-320 (℃), vacuum tightness 0.094MPa, the top temperature remain on 235-250 (℃), boil off remaining 4-aminodiphenylamine, apply mechanically back No. 2 rectifying tower rectifying again.It is continuous that the method for refining 4-amino pentanoic of the present invention has technological process, 4-aminodiphenylamine yield height, and quality is good, and aniline obtains reclaiming simultaneously.It is 99.1% that above-mentioned technology obtains finished product 4-ADP amine content, 72 ℃ of fusing points, and 72.4 ℃ at zero pour, the industrial-scale production yield of this technological process is 92.1%.
Be furnished with in 500 milliliters of three-necked flasks of condenser and agitator, add entry 230 grams, be not sequentially added into tetramethyl ammonium hydroxide 91 grams and (contain pure cerium hydroxide tetramethyl-ammonium 50%, 0.50 mole, all the other are water), sodium hydroxide 20 gram (0.5 mole), tetramethyl ammonium chloride 55 grams (0.5 mole), control mixing temperature 73-77 (℃), stir, make compound alkaline catalysts, concentration 30.4 (weight %).
Get nickel powder 46 grams, aluminium powder 51 grams, copper powder 3 grams, fusion in electric induction furnace is rolled into Powderedly after discharging, the cooling, handle, sieve, the order number remains on the 40-300 order, in capacity is 500 milliliters there-necked flask, thermometer and agitator are housed, and the 375 gram concentration of packing into are 20% aqueous sodium hydroxide solution, slowly add the metal alloy powder, temperature of reaction remains on 60 ℃, reaction times is 4 hours, and the after washing catalyzer promptly gets metal powder powder catalyzer to neutral.
Claims (11)
1. one kind is the method for feedstock production 4-aminodiphenylamine with oil of mirbane and aniline, it is characterized in that selecting for use respectively and condensation, the corresponding two kinds of composite catalysts of hydrogenation, carry out condensation successively, Separation and Recovery is applied mechanically compound alkaline catalysts, hydrogenation, Separation and Recovery and apply mechanically hydrogenation solvent and aniline and regeneration after composite powder powder catalyzer, the technical process operation that refining five operations are formed, the preparation method carries out continuously, wherein the composite catalyst of condensation reaction is compound alkaline catalysts, its component is a tetraalkylammonium hydroxide, the aqueous solution that alkali metal hydroxide or its oxide compound and tetraalkylammonium salt are formed, the composite catalyst of hydrogenation is a composite powder powder catalyzer, its component is a nickel, aluminium and " other metal or nonmetal " A, wherein " other metal or nonmetal " A is Fe, Cu, Co, Mn, Cr, Mo, B, a kind of among the P, refining step promptly is the method purification 4-aminodiphenylamine crude product that adopts three tower continuous rectifications to combine with batch fractionating.
2, according to claim 1 is the method for feedstock production 4-aminodiphenylamine with oil of mirbane and aniline, the mol ratio that it is characterized in that tetraalkylammonium hydroxide, alkali metal hydroxide or its oxide compound and tetraalkylammonium salt three in the compound alkaline catalysts that condensation reaction selects for use is (2-9): (0.5-3): (0.5-3), if adopt alkalimetal oxide, then its ratio in catalyzer converts by corresponding oxyhydroxide and gets.
3. according to claim 1 and 2 is the method for feedstock production 4-aminodiphenylamine with oil of mirbane and aniline, the preparation method who it is characterized in that the compound alkaline catalysts of condensation reaction is, with tetraalkylammonium hydroxide, alkali metal hydroxide, tetraalkylammonium salt is (2-9) in molar ratio: (0.5-3): (0.5-3) be added in certain water gaging, controlled temperature and stirring makes, tetraalkylammonium hydroxide, alkali metal hydroxide and tetraalkylammonium salt concentration expressed in percentage by weight summation are 15%-50%, if adopt alkalimetal oxide, then its ratio or consumption in catalyzer gets by corresponding oxyhydroxide conversion.
4, according to claim 1 is the method for feedstock production 4-aminodiphenylamine with oil of mirbane and aniline, it is characterized in that compound alkaline catalysts Separation and Recovery adopts the hydrolysis of interpolation acidic substance, use alkali neutral method again, acidic substance are selected from mineral acid, its oxide compound and water and other inorganic acid salt, and the alkali of employing is selected from the oxyhydroxide of basic metal and alkaline-earth metal.
5, according to claim 4 is the method for feedstock production 4-aminodiphenylamine with oil of mirbane and aniline, it is characterized in that described mineral acid, its oxide compound and water and other inorganic acid salt are hydrochloric acid, sulfuric acid, nitric acid, carbonic acid, sodium bicarbonate, carbonic acid gas and water, sulphur trioxide and water.
6, according to claim 1 is the method for feedstock production 4-aminodiphenylamine with oil of mirbane and aniline, the condition that it is characterized in that condensation reaction is, oil of mirbane and aniline mol ratio are 1: 1-1: 15, temperature of reaction is 20-150 ℃, reaction pressure is absolute pressure 0.005-0.1MPa, reaction times is 3.5-6 hour, and the mol ratio of hydroxide ion and oil of mirbane is 1 in the compound alkaline catalysts: 4-4: 1.
7, according to claim 1 is the method for feedstock production 4-aminodiphenylamine with oil of mirbane and aniline, the weight percentage that it is characterized in that nickel in the composite powder powder catalyzer is 25%-99.9%, the weight percentage of aluminium and " other metal or nonmetal " A is 0.1%-75%, and the order number is the 40-300 order.
8, according to claim 1 or 7 described be the method for feedstock production 4-aminodiphenylamine with oil of mirbane and aniline, it is characterized in that composite powder powder Preparation of catalysts method is: get nickel powder, aluminium powder and ' other metal or nonmetal " A; fusion under the condition of high temperature; pulverize powdered after the discharging, handle to obtain with hydroxide aqueous solution.
9, according to claim 1 is the method for feedstock production 4-aminodiphenylamine with oil of mirbane and aniline, the gas-liquid volume ratio that it is characterized in that hydrogenation is 10: 1-1500: 1, the solid-liquid weight ratio is 0.5: 100-6: 100, gas promptly refers to hydrogen, liquid comprises solvent and condensated liquid, solid promptly is meant composite powder powder catalyzer, condensated liquid is a condensation operation reaction gained feed liquid, solvent and condensated liquid weight ratio are 1: 10-5: 10, the temperature of hydrogenation is 50-140 ℃, the pressure of the reactor of hydro-reduction is 0.2-3.0MPa, and the residence time of hydrogenation is 2-7 hour.
10, according to claim 1 is the method for feedstock production 4-aminodiphenylamine with oil of mirbane and aniline, it is characterized in that the refining vacuum tightness of 1,2, No. 3 rectifying tower of three tower continuous rectifications that adopts is respectively 0.09-0.098MPa, 0.09-0.098MPa, 0.09-0.098MPa, tower still temperature is respectively 260-290 ℃, 260-300 ℃ and 120-170 ℃, and reflux ratio is respectively 2: 1-10: 1,1: 0.5-1: 4 and 1: 0.5-1: 2.
11, according to claim 1 is the method for feedstock production 4-aminodiphenylamine with oil of mirbane and aniline, it is characterized in that the tower still vacuum tightness of batch fractionating is 0.09-0.098MPa, and tower still temperature is 280-330 ℃.
Priority Applications (12)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB031481914A CN1187316C (en) | 2003-07-04 | 2003-07-04 | Method for preparing 4-amino diphenylamine |
| PL04738332T PL1645555T3 (en) | 2003-07-04 | 2004-07-02 | A method for producing 4-aminodiphenylamine |
| EA200600052A EA009396B1 (en) | 2003-07-04 | 2004-07-02 | A method for producing 4-aminodiphenylamine |
| CA2531074A CA2531074C (en) | 2003-07-04 | 2004-07-02 | Process for preparing 4-aminodiphenylamine |
| US10/882,677 US7176333B2 (en) | 2003-07-04 | 2004-07-02 | Process for preparing 4-aminodiphenylamine |
| PCT/CN2004/000734 WO2005003079A1 (en) | 2003-07-04 | 2004-07-02 | A method for producing 4-aminodiphenylamine |
| AT04738332T ATE526305T1 (en) | 2003-07-04 | 2004-07-02 | METHOD FOR PRODUCING 4-AMINODIPHENYLAMINE |
| ES04738332T ES2373720T3 (en) | 2003-07-04 | 2004-07-02 | METHOD FOR THE PRODUCTION OF 4-AMINODYPHENYLAMINE. |
| PT04738332T PT1645555E (en) | 2003-07-04 | 2004-07-02 | A method for producing 4-aminodiphenylamine |
| EP04738332A EP1645555B1 (en) | 2003-07-04 | 2004-07-02 | A method for producing 4-aminodiphenylamine |
| JP2006517937A JP4546958B2 (en) | 2003-07-04 | 2004-07-02 | Method for producing 4-aminodiphenylamine |
| KR1020040051932A KR100612923B1 (en) | 2003-07-04 | 2004-07-05 | A process for preparing 4-aminodiphenylamine |
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| CNB031481914A CN1187316C (en) | 2003-07-04 | 2003-07-04 | Method for preparing 4-amino diphenylamine |
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| CN102372639A (en) * | 2010-08-20 | 2012-03-14 | 中国石油化工集团公司 | Method for preparing 4-aminodiphenyamine |
| CN104741148B (en) * | 2013-12-25 | 2017-02-08 | 浙江衢州万能达科技有限公司 | Method for preparing 3-chlorine-4 fluoronitrobenzene hydrogenation catalyst |
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