US20010027257A1 - Continuous Ni/low A1 catalyzed hydrogenation of aromatic nitro compounds - Google Patents
Continuous Ni/low A1 catalyzed hydrogenation of aromatic nitro compounds Download PDFInfo
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- US20010027257A1 US20010027257A1 US09/818,507 US81850701A US2001027257A1 US 20010027257 A1 US20010027257 A1 US 20010027257A1 US 81850701 A US81850701 A US 81850701A US 2001027257 A1 US2001027257 A1 US 2001027257A1
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- catalyst
- nickel
- aluminum
- carried out
- aromatic compound
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 25
- -1 aromatic nitro compounds Chemical class 0.000 title claims abstract description 21
- 239000003054 catalyst Substances 0.000 claims abstract description 118
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims abstract description 92
- 229910052782 aluminium Inorganic materials 0.000 claims abstract description 70
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims abstract description 70
- 229910052759 nickel Inorganic materials 0.000 claims abstract description 45
- 150000001491 aromatic compounds Chemical class 0.000 claims abstract description 15
- 238000000034 method Methods 0.000 claims description 47
- 230000008569 process Effects 0.000 claims description 47
- 238000006243 chemical reaction Methods 0.000 claims description 31
- 239000001257 hydrogen Substances 0.000 claims description 26
- 229910052739 hydrogen Inorganic materials 0.000 claims description 26
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 24
- 239000002904 solvent Substances 0.000 claims description 16
- 125000003118 aryl group Chemical group 0.000 claims description 13
- 239000002019 doping agent Substances 0.000 claims description 13
- 239000000203 mixture Substances 0.000 claims description 12
- 229910052751 metal Inorganic materials 0.000 claims description 9
- 239000002184 metal Substances 0.000 claims description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 8
- 239000000047 product Substances 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 7
- 239000000758 substrate Substances 0.000 claims description 7
- 238000009903 catalytic hydrogenation reaction Methods 0.000 claims description 6
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 claims description 4
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 4
- 229910052804 chromium Inorganic materials 0.000 claims description 4
- 239000011651 chromium Substances 0.000 claims description 4
- 229910052742 iron Inorganic materials 0.000 claims description 4
- 239000010936 titanium Substances 0.000 claims description 4
- 229910052719 titanium Inorganic materials 0.000 claims description 4
- 239000004215 Carbon black (E152) Substances 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 3
- 150000004292 cyclic ethers Chemical class 0.000 claims description 3
- 229930195733 hydrocarbon Natural products 0.000 claims description 3
- 230000000737 periodic effect Effects 0.000 claims description 3
- 125000004122 cyclic group Chemical group 0.000 claims description 2
- 229920006395 saturated elastomer Polymers 0.000 claims description 2
- DNIAPMSPPWPWGF-GSVOUGTGSA-N (R)-(-)-Propylene glycol Chemical compound C[C@@H](O)CO DNIAPMSPPWPWGF-GSVOUGTGSA-N 0.000 claims 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims 1
- 239000007795 chemical reaction product Substances 0.000 claims 1
- 125000000449 nitro group Chemical group [O-][N+](*)=O 0.000 claims 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims 1
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 claims 1
- 229910052814 silicon oxide Inorganic materials 0.000 claims 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 claims 1
- 229910001928 zirconium oxide Inorganic materials 0.000 claims 1
- 230000015572 biosynthetic process Effects 0.000 abstract description 6
- 150000004982 aromatic amines Chemical class 0.000 abstract description 2
- 238000011282 treatment Methods 0.000 description 44
- 150000001875 compounds Chemical class 0.000 description 36
- 229910045601 alloy Inorganic materials 0.000 description 23
- 239000000956 alloy Substances 0.000 description 23
- 238000012360 testing method Methods 0.000 description 15
- 238000005406 washing Methods 0.000 description 8
- 230000002093 peripheral effect Effects 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 239000007868 Raney catalyst Substances 0.000 description 6
- 239000011541 reaction mixture Substances 0.000 description 6
- DYSXLQBUUOPLBB-UHFFFAOYSA-N 2,3-dinitrotoluene Chemical compound CC1=CC=CC([N+]([O-])=O)=C1[N+]([O-])=O DYSXLQBUUOPLBB-UHFFFAOYSA-N 0.000 description 5
- 229910000564 Raney nickel Inorganic materials 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 125000000524 functional group Chemical group 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000002441 X-ray diffraction Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 3
- 150000002739 metals Chemical class 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 2
- 229910000624 NiAl3 Inorganic materials 0.000 description 2
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical compound [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 150000002826 nitrites Chemical class 0.000 description 2
- 150000002894 organic compounds Chemical class 0.000 description 2
- 230000003071 parasitic effect Effects 0.000 description 2
- 239000002243 precursor Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000011877 solvent mixture Substances 0.000 description 2
- WDCYWAQPCXBPJA-UHFFFAOYSA-N 1,3-dinitrobenzene Chemical compound [O-][N+](=O)C1=CC=CC([N+]([O-])=O)=C1 WDCYWAQPCXBPJA-UHFFFAOYSA-N 0.000 description 1
- RYHBNJHYFVUHQT-UHFFFAOYSA-N 1,4-Dioxane Chemical compound C1COCCO1 RYHBNJHYFVUHQT-UHFFFAOYSA-N 0.000 description 1
- VOZKAJLKRJDJLL-UHFFFAOYSA-N 2,4-diaminotoluene Chemical compound CC1=CC=C(N)C=C1N VOZKAJLKRJDJLL-UHFFFAOYSA-N 0.000 description 1
- IQUPABOKLQSFBK-UHFFFAOYSA-N 2-nitrophenol Chemical compound OC1=CC=CC=C1[N+]([O-])=O IQUPABOKLQSFBK-UHFFFAOYSA-N 0.000 description 1
- ZPTVNYMJQHSSEA-UHFFFAOYSA-N 4-nitrotoluene Chemical compound CC1=CC=C([N+]([O-])=O)C=C1 ZPTVNYMJQHSSEA-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- MXRIRQGCELJRSN-UHFFFAOYSA-N O.O.O.[Al] Chemical compound O.O.O.[Al] MXRIRQGCELJRSN-UHFFFAOYSA-N 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 125000002877 alkyl aryl group Chemical group 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 150000004645 aluminates Chemical class 0.000 description 1
- 238000000137 annealing Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 125000000484 butyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 229910052792 caesium Inorganic materials 0.000 description 1
- TVFDJXOCXUVLDH-UHFFFAOYSA-N caesium atom Chemical compound [Cs] TVFDJXOCXUVLDH-UHFFFAOYSA-N 0.000 description 1
- 239000012018 catalyst precursor Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000003292 diminished effect Effects 0.000 description 1
- VMMLSJNPNVTYMN-UHFFFAOYSA-N dinitromethylbenzene Chemical class [O-][N+](=O)C([N+]([O-])=O)C1=CC=CC=C1 VMMLSJNPNVTYMN-UHFFFAOYSA-N 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 125000001495 ethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 description 1
- 230000005496 eutectics Effects 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000000543 intermediate Substances 0.000 description 1
- 239000012948 isocyanate Substances 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 125000001624 naphthyl group Chemical group 0.000 description 1
- 150000002815 nickel Chemical class 0.000 description 1
- BFDHFSHZJLFAMC-UHFFFAOYSA-L nickel(ii) hydroxide Chemical compound [OH-].[OH-].[Ni+2] BFDHFSHZJLFAMC-UHFFFAOYSA-L 0.000 description 1
- 150000002825 nitriles Chemical class 0.000 description 1
- LQNUZADURLCDLV-UHFFFAOYSA-N nitrobenzene Chemical compound [O-][N+](=O)C1=CC=CC=C1 LQNUZADURLCDLV-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 125000001147 pentyl group Chemical group C(CCCC)* 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 229920002635 polyurethane Polymers 0.000 description 1
- 239000004814 polyurethane Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 description 1
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 1
- 125000001436 propyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000012429 reaction media Substances 0.000 description 1
- 229910052701 rubidium Inorganic materials 0.000 description 1
- IGLNJRXAVVLDKE-UHFFFAOYSA-N rubidium atom Chemical compound [Rb] IGLNJRXAVVLDKE-UHFFFAOYSA-N 0.000 description 1
- 238000007790 scraping Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 1
- 150000004998 toluenediamines Chemical class 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 229910052726 zirconium Inorganic materials 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
- C07C209/30—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of nitrogen-to-oxygen or nitrogen-to-nitrogen bonds
- C07C209/32—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of nitrogen-to-oxygen or nitrogen-to-nitrogen bonds by reduction of nitro groups
- C07C209/36—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of nitrogen-to-oxygen or nitrogen-to-nitrogen bonds by reduction of nitro groups by reduction of nitro groups bound to carbon atoms of six-membered aromatic rings in presence of hydrogen-containing gases and a catalyst
Definitions
- the present invention relates to the continuous nickel catalyzed hydrogenation of nitrated aromatic compounds, the nickel catalysts of which optionally comprising low/trace amounts of aluminum values, namely, a content of up to at most 5.5% by weight of aluminum.
- This invention more especially relates to such continuous nickel/low aluminum catalyzed hydrogenation of aromatic nitro compounds, which can be carried out for at least three days without any necessity or requirement for replenishing and/or reactivating the catalyst substrate.
- the nitrated compounds, fresh solvent, if indeed used, fresh catalyst and a catalyst suspension, emanating from the reaction zone and then the separation zone are typically admixed in this preparation zone. It is not necessary for the reaction and separation zones to be separate; this because they may exist in the same apparatus, as for example when a reactor/settling tank is employed.
- the hydrogenation reaction is a very rapid reaction and highly exothermic. It is typically carried out in a stirred reactor, or in a loop reactor.
- the process of separating the catalyst from the hydrogenate may be carried out in various ways, such as tangential filtration, transverse filtration and settling.
- the hydrogenation processes for aromatic nitrated compounds are carried out in the presence of catalysts comprising at least nickel and aluminum values.
- the catalyst is of the Raney nickel type.
- This catalyst may optionally be doped with various metals, such as iron and/or chromium, for example.
- Such catalysts are obtained via a basic treatment on an alloy comprising the catalyst metal, in this instance nickel, aluminum and possibly dopant metal or metals.
- Such deposit creates a screen on the walls of the reactor, the settling tank and the peripherals, thereby reducing the productivity of the process whereas the goal was to in fact increase same.
- a major object of the present invention is the provision of an improved process for the continuous Ni/low Al catalyzed hydrogenation of aromatic nitro compounds, but which conspicuously avoids or markedly diminishes those disadvantages and drawbacks to date characterizing the state of this art.
- the present invention features a process for the catalytic hydrogenation of nitrated aromatic compounds, carried out in a reaction zone, a separation zone and peripherals therefor, in which process the hydrogenation is conducted continuously, in the presence of a catalyst which includes at least nickel and possibly/optionally aluminum; the total aluminum content, if aluminum is present, in the catalyst being at most 5.5% by weight of the catalyst.
- the residence time of the same unchanged catalyst in the reaction zone, separation zone and peripherals can be at least three days without adversely affecting the efficacy and/or productivity of the reaction.
- total aluminum is intended the sum of aluminum (0) values plus aluminum (+III) values.
- the present invention therefore also features the use of a catalyst comprising at least nickel and optionally aluminum, the total aluminum content, if aluminum is indeed present, being at most 5.5% by weight, for the purpose of limiting the formation of nickel aluminates while carrying out the catalytic hydrogenation reaction of aromatic nitrated compounds continuously.
- the reduction (or limitation) in the formation of nickel aluminate may especially be observed by the increase by a factor of at least 1.5, preferably at least 2, in the operating time of the process between two shutdowns. It should be appreciated that these shutdowns are necessary since the nickel aluminate deposit then prevents the plant from being operated properly (significant reduction in productivity, blockage of the pipes, especially). Though, when the amount of initial aluminum in the catalyst is low, or when there exists no aluminum whatsoever, it is possible that no shutdown is required between two predetermined stoppages or shutdowns.
- the process employed under the conditions of the invention makes it possible to achieve a yield of hydrogenated compound (and therefore of aromatic amine) of at least 99.5% by weight.
- the catalyst employed in the subject process is particularly suitable for achieving productivities as high as 2 mol of hydrogen converted per hour and per gram of catalyst, or indeed up to 3 mol of hydrogen converted per hour and per gram of catalyst. More particularly, the productivities attained by the process according to the invention range from 0.1 to 3 mol of hydrogen converted per hour per gram of catalyst, preferably from 0.2 to 2 mol of hydrogen converted per hour per gram of catalyst.
- the process according to the invention makes it possible to employ, in this reaction, catalysts comprising nickel emanating from other hydrogenation processes such as, for example, those employed for hydrogenating compounds comprising nitrated functional groups or nitrites, or even emanating from the regeneration of catalysts employed in the same process.
- the process according to the invention particularly relates to the hydrogenation of aromatic nitrated compounds in the presence of a catalyst comprising nickel and aluminum.
- the catalyst has a total aluminum content of at most 5.5% by weight of the catalyst. It should be noted that the catalyst has this maximum aluminum content initially, namely, before it is actually used in the hydrogenation reaction.
- the total aluminum content is greater than or equal to 1% by weight with respect to the total weight of the catalyst.
- the total aluminum content ranges from 1% to 5.5% by weight with respect to the total weight of catalyst. Even more advantageously, the total aluminum content in the catalyst ranges from 2% to 5% by weight with respect to the total weight of the catalyst.
- the catalyst is obtained from an alloy based on nickel, aluminum and optionally at least one dopant (Raney alloy).
- the dopant is selected from among titanium, iron and chromium, or a mixture thereof.
- Catalysts of this type are available from various sources.
- a catalyst is used which is from the alkaline treatment of an alloy comprising aluminum, nickel and optionally at least one dopant, the nature of the alloy and/or the conditions under which the alloy is manufactured and/or the conditions under which the alkaline treatment is carried out having the consequence that the total aluminum content thereof does not exceed 5.5% by weight of the catalyst.
- the alkaline treatment may, advantageously, be carried out as follows:
- the alkaline compound is, in general, a hydroxide of an alkali metal, such as lithium, sodium, potassium, cesium and/or rubidium.
- This treatment may, for example, be carried out using an excess of alkaline compound with respect to aluminum.
- said alkaline compound may be employed in an amount such that the molar ratio of alkaline compound to the number of mol of aluminum present ranges from 1.5 to 10. Preferably, said ratio is from 1.5 to 3.
- the alkaline compound in the form of an aqueous solution. More particularly, the concentration of the alkaline compound at the beginning of the treatment ranges from 10% to 50% by weight. Preferably, said concentration is from 15% to 30% by weight.
- the alkaline treatment is carried out under conditions such that the hydrogen content in the gas phase remains below the lower explosivity limit of the air/hydrogen mixture.
- Such conditions may be obtained, for example, by carrying out this treatment under a stream of air or an inert gas such as, inter alia, nitrogen.
- the pressure at which the alkaline treatment is carried out is more particularly greater than or equal to the saturation vapor pressure of the liquid medium at the temperature of the alkaline treatment.
- this liquid medium comprises, inter alia, water, dissolved aluminum salts and the alkaline compound.
- saturation vapor pressure is intended the partial pressure of the liquid medium at the temperature in question.
- the temperature at which the alkaline treatment is carried out preferably ranges from 50° to 130° C.
- the treatment is carried out at a temperature of from 60° to 90° C.
- the treatment temperature may change during the alkaline treatment. More particularly, it may be advantageous to increase the temperature at the end of the treatment.
- duration of the alkaline treatment this more particularly ranges from 1 to 12 hours. Usually this duration is from 1 to 3 hours.
- the aforementioned conditions are selected such that the aluminum remains in a soluble state, especially as an aluminate, during the alkaline treatment to permit same to be separated from the remaining solids after the treatment.
- a catalyst precursor alloy is used having a high aluminum content.
- alloys having an aluminum content greater than 50% by weight of the alloy are suitable according to the invention.
- such alloys have an aluminum content of less than or equal to 70% by weight of the alloy, preferably from 55% to 70% by weight of the alloy. Nonetheless, it is also within the scope of the present invention to use alloys whose aluminum content is greater than 70%. Simply, though, the use of this type of alloy may incur unnecessary additional costs during its treatment (cost of the raw material (alkaline compound) and effluent treatment cost).
- a second option entails carrying out the alkaline treatment of the precursor alloy under conditions of a higher level than those indicated with respect to the alkaline treatment described above.
- all that is required is for at least one of the conditions to be at a greater level in order for the treatment to be regarded as being carried out at a higher level.
- these conditions may include a higher alkaline compound/Al molar ratio, and/or a higher initial concentration of the alkaline compound, and/or a higher temperature maintained during the treatment or temperature at the end of the treatment, and/or a longer duration.
- an additional alkaline treatment can be carried out, i.e., at least one other alkaline treatment is carried out on the product resulting from the first alkaline treatment of an alloy, to further reduce the residual aluminum content.
- a first alkaline treatment may be carried out under conventional conditions and a second treatment under conditions at a higher level, as indicated above.
- the second treatment may be carried out under conditions similar to those of the first treatment
- a third option entails employing a catalyst from an alloy that has undergone a particular treatment during its manufacture. Thus, it is possible to employ catalysts obtained from an alloy that has been subjected to an annealing step.
- the alloy ingot is subjected to a heat treatment at a temperature remaining below the peritectic temperature which results in the formation of NiAl 3 . More particularly, the temperature used in this heat treatment ranges from 650° to 850° C.
- this treatment is carried out under an inert atmosphere.
- This treatment rearranges the structure of the alloy and promotes the formation of phases rich in aluminum, such as NiAl 3 or the eutectic phase, for example.
- the aluminum can be easily removed from such phases during the alkaline treatment for obtaining the actual catalyst.
- Another source of catalyst is from the recycling of catalysts that have been used in hydrogenation processes, which may or may not be different from that in which the catalyst is employed.
- the catalysts of the Raney nickel type, doped or undoped, employed in the hydrogenation of compounds comprising nitrated functional groups or nitrites may be suitable for this embodiment.
- the consumption of the catalysts during such hydrogenation reactions results, among other things, in a significant decrease in the residual aluminum content.
- the catalyst Before it is used in the process according to the invention, the catalyst is advantageously subjected to a first washing operation with water to remove any trace of organic compounds present during the previous operation.
- the resulting catalyst then is subjected to a regeneration step entailing conducting at least one alkaline washing operation.
- the purpose of this operation is to remove all or some of the oxidized aluminum values present in the catalyst.
- the alkaline washing is carried out at a temperature of less than or equal to 150° C., although higher temperatures may be employed depending on the type of apparatus used and the energy sources available. More particularly, the temperature is advantageously greater than or equal to 50° C., preferably ranging from 80° to 140° C.
- the alkaline washing may be carried out at atmospheric or higher pressure, depending on the characteristics of the apparatus utilized. It should be appreciated that there is no significant advantage in carrying out the treatment at total pressures greater than 30 ⁇ 10 5 Pa.
- alkaline compound this is advantageously employed at a concentration of less than or equal to 35% by weight in water.
- This regeneration step may also be carried out advantageously under a hydrogen pressure to possibly further reduce a fraction of the oxidized nickel.
- the treatment is carried out more particularly with a hydrogen partial pressure of at least 10 5 Pa (1 bar).
- the hydrogen partial pressure may be as high as possible, depending on the equipment employed. However, this hydrogen partial pressure is advantageously less than or equal to 30 ⁇ 10 5 Pa (30 bar).
- the total pressure in the case of a treatment in hydrogen advantageously ranges from 6 to 30 ⁇ 10 5 Pa (6-30 bar).
- Another embodiment of this invention entails the use of catalysts comprising nickel and aluminum, deposited onto a support therefor.
- the nickel may optionally be combined with at least one dopant metal such as those belonging to Groups IVA, VA, VIA, VII of the Periodic Table of Elements, preferably titanium, iron or chromium, or a mixture thereof.
- dopant metal such as those belonging to Groups IVA, VA, VIA, VII of the Periodic Table of Elements, preferably titanium, iron or chromium, or a mixture thereof.
- Said support is more particularly selected such as to be stable under the reaction conditions.
- the support advantageously comprises aluminum (more especially in the form of alumina) combined with at least one oxide as zirconium, titanium or silicon, whether by themselves or as mixtures.
- the catalyst is such that the total aluminum content thereof, whatever its degree of oxidation, satisfies the conditions indicated above, namely, it does not exceed 5.5% of the total weight of the catalyst.
- the amount of support more particularly ranges from 25% to 80% by weight of catalyst, preferably from 30% to 65% by weight of catalyst.
- This type of catalyst is usually obtained by precipitating onto the support a nickel salt and optionally at least one salt of a dopant metal.
- the catalyst is then separated, for example by filtration, then dried and calcined at a high enough temperature to convert the nickel hydroxide, and perhaps the salt or hydroxide of the dopant metal, into oxides.
- the catalyst is subjected to a treatment during which some of the nickel is reduced. This reduction is generally carried out at high temperature in a reducing atmosphere, such as hydrogen.
- the catalyst comprises nickel but not aluminum.
- the catalyst employed comprises a support which contains no aluminum.
- the description indicated above with regard to supported catalysts comprising aluminum (preparation; origin (fresh or recycled), treatment of the recycled catalyst before it is introduced into the hydrogenation process according to the invention) remains valid for this embodiment given that aluminum is not present therein.
- the catalyst indicated immediately above is therefore employed in a reaction involving the catalytic hydrogenation of nitrated aromatic compounds, carried out continuously.
- the residence time of use of the catalyst is at least 3 days.
- nitrated aromatic compounds are intended, in particular, compounds comprising at least one nitrated functional group, and preferably at least two nitrated functional groups, and at least one C 6 -C 14 , preferably C 6 -C 10 aromatic basic nucleus, which may or may not be substituted with one or more C 1 -C 10 linear, cyclic or branched, saturated or unsaturated, hydrocarbon radicals and/or one or more hydroxyl radicals.
- the aforesaid optional hydrocarbon radical substituents borne by said aromatic basic nuclei may be selected from C 1 -C 10 , preferably C 1 -C 6 , alkyl, aryl, alkylaryl and arylalkyl radicals.
- Exemplary aromatic basic nuclei include, especially, benzene rings and naphthalene rings, which may or may not be substituted with one or more methyl, ethyl, propyl, butyl, pentyl or hexyl radicals and/or isomers thereof.
- the process according to the invention may be carried out in a reaction medium comprising at least one compound selected from among mononitrobenzene, dinitrobenzene, mononitrotoluene, dinitrotoluene, paranitrocumene or orthonitrophenol.
- the aromatic nitrated compounds may be employed in the presence of a solvent for said compounds.
- the solvent employed is selected from among aliphatic alcohols or cyclic ethers, whether alone or in admixture.
- methanol, ethanol, propanol or isopropanol are exemplary aliphatic alcohols.
- exemplary cyclic ethers include dioxane and tetrahydrofuran, also either alone or in admixture.
- the concentration of nitrated compounds in the solvent or solvent mixture may vary over a wide range. However, single-phase mixtures, namely, mixtures for which the solubility limit of the nitrated compound or compounds is not reached for the solvent or mixture in question, are used. Without intending to be limited thereby, the concentration range is advantageously less than or equal to 25% by weight.
- the solvent employed is the hydrogenated compound.
- the aromatic nitro compounds are introduced in the liquid or molten state.
- This embodiment is advantageous in that it does not dilute the reactant, as is the case when a solvent or solvent mixture is employed. This helps, in particular, to maintain a high process productivity. Moreover, this embodiment obviates any additional step of separating the products from the solvent(s) used during the reaction, which step runs the risk of loss of hydrogenated products.
- the instantaneous content of nitrated compounds in the reaction zone is maintained as low as possible. Usually, measures are taken to ensure that it does not exceed 1,000 ppm.
- This content of nitrated compounds in the reactor is maintained by adjusting the feed rate of nitrated starting compounds such that they are essentially instantly reduced by the catalyst as soon as they are introduced into the reactor.
- the process according to the invention is very suitable for operating at very high productivity levels, i.e., the aromatic nitrated compound is introduced almost at the maximum rate at which it can be accommodated by the reactor/catalyst pair.
- the hydrogen employed is more particularly pure hydrogen.
- pure hydrogen is intended a gas containing at least 99% hydrogen and more especially at least 99.9% hydrogen. It should be appreciated that it would not be outside the scope of the present invention to carry out the hydrogenation reaction with diluted hydrogen, although this provides no particular advantage.
- the hydrogen is introduced in the stoichiometric amount.
- it is also intended to carry out the hydrogenation with hydrogen in an excess amount compared with stoichiometry.
- Such conditions may be advantageous for meeting hydrodynamic criteria, more particularly for optimizing gas/liquid transfer parameters of certain technologies.
- the hydrogen pressure in the reactor advantageously ranges from 5 to 70 ⁇ 10 5 Pa (5 and 70 bar), preferably from 10 to 50 ⁇ 10 5 Pa (10 and 50 bar).
- This gas is charged by any means known to this art for enabling the gas to be distributed homogeneously within the reactor.
- the reaction is carried out in a stirred reactor, or in a loop reactor.
- the temperature of reaction more particularly ranges from 50° to 200° C.
- reaction mixture is separated from the catalyst by settling or filtration, using conventional techniques.
- the amount of reaction mixture separated corresponds to the amount of nitrated compound, optionally in the presence of the solvent, introduced into the reaction zone, such as to maintain stable operating conditions.
- reaction mixture separated from the catalyst is then treated according to its composition and its subsequent intended use.
- the hydrogenated amino product obtained is separated, for example, by distillation. It will be appreciated that, depending on the choice of solvent and the subsequent step to which the hydrogenated products will be subjected, this separation step may be unnecessary.
- the aromatic hydrogenated product can be employed in a phosgenation reaction, after being dehydrated, to obtain aromatic isocyanates, which are intermediates in the production of polyurethanes, or else, if necessary, distilled in order to separate the various isomers obtained.
- the hydrogen feed was determined by the progress of the reaction in order to remain at constant pressure in the reactor.
- a sample of the initial catalyst (not having been subjected to the hydrogenation) was introduced with a mixture of toluenediamine (TDA) isomers and water into a glass tube termed a Carius tube, which was sealed and then maintained for 1 month at 150° C. under autogenous pressure.
- TDA toluenediamine
- the structure of the catalyst was determined by X-ray diffraction to be that of a nickel aluminate (takovite). This structure was the same as that of the deposit (screen) observed on the walls of apparatus utilized on an industrial scale.
- the catalyst employed was a Raney nickel recovered from a nitrile hydrogenation unit containing 3.5% total aluminum by weight. The catalyst was first washed with water and then dilute (1N) sodium hydroxide and then again with water. The catalyst was then evaluated employing the same tests as those described in Example 1.
- the structure of the catalyst was basically that of nickel. It contained a small proportion of nickel aluminate (at least half the amount as that in the catalyst of Example 1).
- the catalyst employed in this example was an undoped nickel-based supported catalyst containing about 2% total aluminum by weight, in the form of alumina, 2 to 6% ZrO 2 , silica and nickel with a total nickel content of 55% by weight.
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Abstract
Description
- This application claims priority under 35 U.S.C. § 119 of FR-00/03903, filed Mar. 28, 2000, hereby expressly incorporated by reference.
- 1. Technical Field of the Invention
- The present invention relates to the continuous nickel catalyzed hydrogenation of nitrated aromatic compounds, the nickel catalysts of which optionally comprising low/trace amounts of aluminum values, namely, a content of up to at most 5.5% by weight of aluminum.
- This invention more especially relates to such continuous nickel/low aluminum catalyzed hydrogenation of aromatic nitro compounds, which can be carried out for at least three days without any necessity or requirement for replenishing and/or reactivating the catalyst substrate.
- 2. Description of the Prior Art
- Processes for catalytically hydrogenating aromatic nitrated compounds have long been known. In general, these prior art processes are carried out in apparatus usually comprising two zones and peripherals therefor. The first zone is that in which the actual hydrogenation reaction is carried out; the second zone is that in which the catalyst is separated from the reaction mixture and by “peripherals” are intended the pipes, conduits and other apparatus components (storage tanks, recycling tanks, pumps, etc.), by means of which the reaction mixture and/or the reactants are conveyed, and the zone or zones for preparing the reaction mixture. It should be appreciated that the nitrated compounds, fresh solvent, if indeed used, fresh catalyst and a catalyst suspension, emanating from the reaction zone and then the separation zone, are typically admixed in this preparation zone. It is not necessary for the reaction and separation zones to be separate; this because they may exist in the same apparatus, as for example when a reactor/settling tank is employed. The hydrogenation reaction is a very rapid reaction and highly exothermic. It is typically carried out in a stirred reactor, or in a loop reactor. The process of separating the catalyst from the hydrogenate may be carried out in various ways, such as tangential filtration, transverse filtration and settling.
- Usually, the hydrogenation processes for aromatic nitrated compounds are carried out in the presence of catalysts comprising at least nickel and aluminum values. Very often the catalyst is of the Raney nickel type. This catalyst may optionally be doped with various metals, such as iron and/or chromium, for example. Such catalysts are obtained via a basic treatment on an alloy comprising the catalyst metal, in this instance nickel, aluminum and possibly dopant metal or metals.
- Conventionally, the industrial processes that have been developed employ Raney catalysts whose residual aluminum content is relatively high, on the order of about 7% to 15% by weight of the catalyst.
- The advantages of these catalysts are well recognized and deserved, but they present a few drawbacks when employed under conditions such that the reaction is carried out continuously, with long residence times of the catalyst. The same limitations apply if these catalysts are employed under high productivity conditions.
- This is because, under such conditions, the parasitic oxidation of the nickel present in the catalyst becomes great. A very hard deposit is then formed over time on the walls of the reactor, of the settling tank and/or of the peripherals. This deposit, which has been identified as having a nickel aluminate structure, for example a lamellar double hydroxide of the takovite type, is due to this significant parasitic oxidation of nickel and to the concomitant presence of hydrated aluminum oxide.
- Such deposit creates a screen on the walls of the reactor, the settling tank and the peripherals, thereby reducing the productivity of the process whereas the goal was to in fact increase same.
- It is therefore necessary, at quite closely spaced regular intervals, to shut down the plant or the reaction zone in question, and to clean it. However, this operation is very burdensome as it requires the use of relatively powerful means to remove this deposit, such as, for example, high-pressure lances or scraping devices.
- Accordingly, a major object of the present invention is the provision of an improved process for the continuous Ni/low Al catalyzed hydrogenation of aromatic nitro compounds, but which conspicuously avoids or markedly diminishes those disadvantages and drawbacks to date characterizing the state of this art.
- Briefly, the present invention features a process for the catalytic hydrogenation of nitrated aromatic compounds, carried out in a reaction zone, a separation zone and peripherals therefor, in which process the hydrogenation is conducted continuously, in the presence of a catalyst which includes at least nickel and possibly/optionally aluminum; the total aluminum content, if aluminum is present, in the catalyst being at most 5.5% by weight of the catalyst. The residence time of the same unchanged catalyst in the reaction zone, separation zone and peripherals can be at least three days without adversely affecting the efficacy and/or productivity of the reaction.
- More particularly according to the present invention, by the expression “total aluminum” is intended the sum of aluminum (0) values plus aluminum (+III) values.
- Thus, it has now been found that by carrying out the hydrogenation under such conditions and by employing a catalyst having, immediately from the beginning of the hydrogenation reaction, a total aluminum content much lower than that present in the catalysts today employed on an industrial scale, or even containing no aluminum in certain cases, the formation of nickel aluminate is greatly diminished, or even eliminated.
- The present invention therefore also features the use of a catalyst comprising at least nickel and optionally aluminum, the total aluminum content, if aluminum is indeed present, being at most 5.5% by weight, for the purpose of limiting the formation of nickel aluminates while carrying out the catalytic hydrogenation reaction of aromatic nitrated compounds continuously.
- The reduction (or limitation) in the formation of nickel aluminate may especially be observed by the increase by a factor of at least 1.5, preferably at least 2, in the operating time of the process between two shutdowns. It should be appreciated that these shutdowns are necessary since the nickel aluminate deposit then prevents the plant from being operated properly (significant reduction in productivity, blockage of the pipes, especially). Though, when the amount of initial aluminum in the catalyst is low, or when there exists no aluminum whatsoever, it is possible that no shutdown is required between two predetermined stoppages or shutdowns.
- In addition, surprisingly, the use of such a catalyst does not significantly degrade the performance of the reaction, especially the yield and the consumption of catalyst. It is even more remarkable to note that the use of this type of catalyst may even help to increase the performance of the reaction.
- As one illustration, the process employed under the conditions of the invention makes it possible to achieve a yield of hydrogenated compound (and therefore of aromatic amine) of at least 99.5% by weight.
- The catalyst employed in the subject process is particularly suitable for achieving productivities as high as 2 mol of hydrogen converted per hour and per gram of catalyst, or indeed up to 3 mol of hydrogen converted per hour and per gram of catalyst. More particularly, the productivities attained by the process according to the invention range from 0.1 to 3 mol of hydrogen converted per hour per gram of catalyst, preferably from 0.2 to 2 mol of hydrogen converted per hour per gram of catalyst.
- Too, the process according to the invention makes it possible to employ, in this reaction, catalysts comprising nickel emanating from other hydrogenation processes such as, for example, those employed for hydrogenating compounds comprising nitrated functional groups or nitrites, or even emanating from the regeneration of catalysts employed in the same process.
- Lastly, it has also been found that the catalysts employed in the process according to the invention, even under high productivity conditions, were deactivated less rapidly than the conventional catalysts employed under the same conditions. This is because the pores of the catalysts having a lower aluminum content become blocked less rapidly.
- As indicated above, the process according to the invention particularly relates to the hydrogenation of aromatic nitrated compounds in the presence of a catalyst comprising nickel and aluminum.
- In one embodiment of the invention, the catalyst has a total aluminum content of at most 5.5% by weight of the catalyst. It should be noted that the catalyst has this maximum aluminum content initially, namely, before it is actually used in the hydrogenation reaction.
- In a preferred embodiment of the invention, the total aluminum content is greater than or equal to 1% by weight with respect to the total weight of the catalyst.
- Preferably, the total aluminum content ranges from 1% to 5.5% by weight with respect to the total weight of catalyst. Even more advantageously, the total aluminum content in the catalyst ranges from 2% to 5% by weight with respect to the total weight of the catalyst.
- In another embodiment of the invention, the catalyst is obtained from an alloy based on nickel, aluminum and optionally at least one dopant (Raney alloy).
- Among the conventional dopants in this field, exemplary are the metals of Groups IVA, VA, VIA, VIII of the Periodic Table of Elements (Supplement to the Chemical Society of France Bulletin No. 1, January 1966). Preferably, the dopant is selected from among titanium, iron and chromium, or a mixture thereof.
- Catalysts of this type are available from various sources.
- From one source, a catalyst is used which is from the alkaline treatment of an alloy comprising aluminum, nickel and optionally at least one dopant, the nature of the alloy and/or the conditions under which the alloy is manufactured and/or the conditions under which the alkaline treatment is carried out having the consequence that the total aluminum content thereof does not exceed 5.5% by weight of the catalyst.
- The alkaline treatment may, advantageously, be carried out as follows:
- First, the alkaline compound is, in general, a hydroxide of an alkali metal, such as lithium, sodium, potassium, cesium and/or rubidium.
- This treatment may, for example, be carried out using an excess of alkaline compound with respect to aluminum. More particularly, said alkaline compound may be employed in an amount such that the molar ratio of alkaline compound to the number of mol of aluminum present ranges from 1.5 to 10. Preferably, said ratio is from 1.5 to 3.
- Moreover, it is conventional to employ the alkaline compound in the form of an aqueous solution. More particularly, the concentration of the alkaline compound at the beginning of the treatment ranges from 10% to 50% by weight. Preferably, said concentration is from 15% to 30% by weight.
- Advantageously, and for safety reasons, the alkaline treatment is carried out under conditions such that the hydrogen content in the gas phase remains below the lower explosivity limit of the air/hydrogen mixture.
- Such conditions may be obtained, for example, by carrying out this treatment under a stream of air or an inert gas such as, inter alia, nitrogen.
- It should also be noted that the pressure at which the alkaline treatment is carried out is more particularly greater than or equal to the saturation vapor pressure of the liquid medium at the temperature of the alkaline treatment.
- It will be appreciated that this liquid medium comprises, inter alia, water, dissolved aluminum salts and the alkaline compound.
- In addition, by the term “saturation vapor pressure” is intended the partial pressure of the liquid medium at the temperature in question.
- Furthermore, the temperature at which the alkaline treatment is carried out preferably ranges from 50° to 130° C. Advantageously, the treatment is carried out at a temperature of from 60° to 90° C.
- Too, the treatment temperature may change during the alkaline treatment. More particularly, it may be advantageous to increase the temperature at the end of the treatment.
- As regards the duration of the alkaline treatment, this more particularly ranges from 1 to 12 hours. Usually this duration is from 1 to 3 hours.
- Finally, it should be noted that the aforementioned conditions are selected such that the aluminum remains in a soluble state, especially as an aluminate, during the alkaline treatment to permit same to be separated from the remaining solids after the treatment.
- In one embodiment, a catalyst precursor alloy is used having a high aluminum content. For example, alloys having an aluminum content greater than 50% by weight of the alloy are suitable according to the invention.
- More particularly, such alloys have an aluminum content of less than or equal to 70% by weight of the alloy, preferably from 55% to 70% by weight of the alloy. Nonetheless, it is also within the scope of the present invention to use alloys whose aluminum content is greater than 70%. Simply, though, the use of this type of alloy may incur unnecessary additional costs during its treatment (cost of the raw material (alkaline compound) and effluent treatment cost).
- According to one advantageous embodiment of this first possible route, and if a dopant is present in the precursor alloy, it is preferred to carry out the treatment on an alloy whose dopant content does not exceed 5% by weight of the alloy and preferably does not exceed 3% by weight of the alloy,
- A second option entails carrying out the alkaline treatment of the precursor alloy under conditions of a higher level than those indicated with respect to the alkaline treatment described above. Thus, among the conditions indicated above, all that is required is for at least one of the conditions to be at a greater level in order for the treatment to be regarded as being carried out at a higher level. For example, these conditions may include a higher alkaline compound/Al molar ratio, and/or a higher initial concentration of the alkaline compound, and/or a higher temperature maintained during the treatment or temperature at the end of the treatment, and/or a longer duration.
- In one embodiment of this second option, an additional alkaline treatment can be carried out, i.e., at least one other alkaline treatment is carried out on the product resulting from the first alkaline treatment of an alloy, to further reduce the residual aluminum content.
- Thus, a first alkaline treatment may be carried out under conventional conditions and a second treatment under conditions at a higher level, as indicated above.
- Likewise, the second treatment may be carried out under conditions similar to those of the first treatment
- A third option entails employing a catalyst from an alloy that has undergone a particular treatment during its manufacture. Thus, it is possible to employ catalysts obtained from an alloy that has been subjected to an annealing step.
- More particularly according to this third option, the alloy ingot is subjected to a heat treatment at a temperature remaining below the peritectic temperature which results in the formation of NiAl3. More particularly, the temperature used in this heat treatment ranges from 650° to 850° C.
- Advantageously, this treatment is carried out under an inert atmosphere.
- This treatment rearranges the structure of the alloy and promotes the formation of phases rich in aluminum, such as NiAl3 or the eutectic phase, for example. However, the aluminum can be easily removed from such phases during the alkaline treatment for obtaining the actual catalyst.
- Of course, it is also within the scope of the present invention to employ a combination of the three aforementioned options.
- Another source of catalyst is from the recycling of catalysts that have been used in hydrogenation processes, which may or may not be different from that in which the catalyst is employed.
- By way of illustration, the catalysts of the Raney nickel type, doped or undoped, employed in the hydrogenation of compounds comprising nitrated functional groups or nitrites may be suitable for this embodiment. The consumption of the catalysts during such hydrogenation reactions results, among other things, in a significant decrease in the residual aluminum content.
- Before it is used in the process according to the invention, the catalyst is advantageously subjected to a first washing operation with water to remove any trace of organic compounds present during the previous operation. The resulting catalyst then is subjected to a regeneration step entailing conducting at least one alkaline washing operation. The purpose of this operation is to remove all or some of the oxidized aluminum values present in the catalyst.
- The conditions detailed above for the alkaline treatments may be employed in this type of washing.
- However, in another embodiment of this invention, the alkaline washing is carried out at a temperature of less than or equal to 150° C., although higher temperatures may be employed depending on the type of apparatus used and the energy sources available. More particularly, the temperature is advantageously greater than or equal to 50° C., preferably ranging from 80° to 140° C.
- The alkaline washing may be carried out at atmospheric or higher pressure, depending on the characteristics of the apparatus utilized. It should be appreciated that there is no significant advantage in carrying out the treatment at total pressures greater than 30×105 Pa.
- With regard to the alkaline compound, this is advantageously employed at a concentration of less than or equal to 35% by weight in water.
- This regeneration step may also be carried out advantageously under a hydrogen pressure to possibly further reduce a fraction of the oxidized nickel.
- In such instance, the treatment is carried out more particularly with a hydrogen partial pressure of at least 105 Pa (1 bar). The hydrogen partial pressure may be as high as possible, depending on the equipment employed. However, this hydrogen partial pressure is advantageously less than or equal to 30×105 Pa (30 bar). The total pressure in the case of a treatment in hydrogen advantageously ranges from 6 to 30×105 Pa (6-30 bar).
- Another embodiment of this invention entails the use of catalysts comprising nickel and aluminum, deposited onto a support therefor.
- The nickel may optionally be combined with at least one dopant metal such as those belonging to Groups IVA, VA, VIA, VII of the Periodic Table of Elements, preferably titanium, iron or chromium, or a mixture thereof.
- Said support is more particularly selected such as to be stable under the reaction conditions.
- More particularly, the support advantageously comprises aluminum (more especially in the form of alumina) combined with at least one oxide as zirconium, titanium or silicon, whether by themselves or as mixtures.
- Nonetheless, the catalyst is such that the total aluminum content thereof, whatever its degree of oxidation, satisfies the conditions indicated above, namely, it does not exceed 5.5% of the total weight of the catalyst.
- The amount of support more particularly ranges from 25% to 80% by weight of catalyst, preferably from 30% to 65% by weight of catalyst.
- This type of catalyst is usually obtained by precipitating onto the support a nickel salt and optionally at least one salt of a dopant metal. The catalyst is then separated, for example by filtration, then dried and calcined at a high enough temperature to convert the nickel hydroxide, and perhaps the salt or hydroxide of the dopant metal, into oxides. Once this step has been carried out, the catalyst is subjected to a treatment during which some of the nickel is reduced. This reduction is generally carried out at high temperature in a reducing atmosphere, such as hydrogen.
- It would be possible to employ, in the reaction according to the invention, a supported catalyst, i.e., that just described, which had been utilized beforehand in another hydrogenation process. In such event, it is preferable, before the spent catalyst is used at all in the process according to the invention, to conduct a water washing step, or even an alkaline washing step, to remove any trace of organic compounds emanating from the previous process. After this washing step, it is recommended to carry out a reduction treatment, preferably at high temperature in a reducing atmosphere such as hydrogen.
- In another embodiment of the invention, the catalyst comprises nickel but not aluminum.
- According to this embodiment, the catalyst employed comprises a support which contains no aluminum. The description indicated above with regard to supported catalysts comprising aluminum (preparation; origin (fresh or recycled), treatment of the recycled catalyst before it is introduced into the hydrogenation process according to the invention) remains valid for this embodiment given that aluminum is not present therein.
- The catalyst indicated immediately above is therefore employed in a reaction involving the catalytic hydrogenation of nitrated aromatic compounds, carried out continuously.
- According to an important feature of the process according to the invention, the residence time of use of the catalyst is at least 3 days.
- Consistent with the present invention, the residence time (Tres) is defined as follows:
Catalyst employed: Amount of catalyst in the reaction zone, separation zone and peripherals, expressed in kg; Catalyst consumed: Amount of catalyst consumed in the process (amount of catalyst which is purged and not subsequently reinjected into the process); expressed in kg of purged catalyst per metric ton of aminated compound produced; Aminated compound Amount of aminated compound produced, expressed in production: metric tons per day. - Very often, the residence time of the catalyst in these zones is on the order of several weeks.
- By the term “nitrated aromatic compounds” are intended, in particular, compounds comprising at least one nitrated functional group, and preferably at least two nitrated functional groups, and at least one C6-C14, preferably C6-C10 aromatic basic nucleus, which may or may not be substituted with one or more C1-C10 linear, cyclic or branched, saturated or unsaturated, hydrocarbon radicals and/or one or more hydroxyl radicals.
- More specifically, the aforesaid optional hydrocarbon radical substituents borne by said aromatic basic nuclei may be selected from C1-C10, preferably C1-C6, alkyl, aryl, alkylaryl and arylalkyl radicals.
- Exemplary aromatic basic nuclei include, especially, benzene rings and naphthalene rings, which may or may not be substituted with one or more methyl, ethyl, propyl, butyl, pentyl or hexyl radicals and/or isomers thereof.
- The process according to the invention may be carried out in a reaction medium comprising at least one compound selected from among mononitrobenzene, dinitrobenzene, mononitrotoluene, dinitrotoluene, paranitrocumene or orthonitrophenol.
- The process according to the invention is highly advantageously carried out in a mixture of dinitrotoluene isomers.
- The aromatic nitrated compounds may be employed in the presence of a solvent for said compounds.
- In a first embodiment, the solvent employed is selected from among aliphatic alcohols or cyclic ethers, whether alone or in admixture.
- More particularly, methanol, ethanol, propanol or isopropanol, either alone or in admixture are exemplary aliphatic alcohols.
- And exemplary cyclic ethers include dioxane and tetrahydrofuran, also either alone or in admixture.
- In this embodiment of the invention, before the aromatic nitrated compounds are introduced into the reaction zone they are dissolved in the above solvents or solvent admixtures.
- The concentration of nitrated compounds in the solvent or solvent mixture may vary over a wide range. However, single-phase mixtures, namely, mixtures for which the solubility limit of the nitrated compound or compounds is not reached for the solvent or mixture in question, are used. Without intending to be limited thereby, the concentration range is advantageously less than or equal to 25% by weight.
- According to yet another preferred embodiment of the invention, the solvent employed is the hydrogenated compound. In this embodiment, the aromatic nitro compounds are introduced in the liquid or molten state.
- This embodiment is advantageous in that it does not dilute the reactant, as is the case when a solvent or solvent mixture is employed. This helps, in particular, to maintain a high process productivity. Moreover, this embodiment obviates any additional step of separating the products from the solvent(s) used during the reaction, which step runs the risk of loss of hydrogenated products.
- The instantaneous content of nitrated compounds in the reaction zone is maintained as low as possible. Usually, measures are taken to ensure that it does not exceed 1,000 ppm. This content of nitrated compounds in the reactor is maintained by adjusting the feed rate of nitrated starting compounds such that they are essentially instantly reduced by the catalyst as soon as they are introduced into the reactor. The process according to the invention is very suitable for operating at very high productivity levels, i.e., the aromatic nitrated compound is introduced almost at the maximum rate at which it can be accommodated by the reactor/catalyst pair.
- The hydrogen employed is more particularly pure hydrogen. By the expression “pure hydrogen” is intended a gas containing at least 99% hydrogen and more especially at least 99.9% hydrogen. It should be appreciated that it would not be outside the scope of the present invention to carry out the hydrogenation reaction with diluted hydrogen, although this provides no particular advantage.
- Preferably, the hydrogen is introduced in the stoichiometric amount. However, it is also intended to carry out the hydrogenation with hydrogen in an excess amount compared with stoichiometry. Such conditions may be advantageous for meeting hydrodynamic criteria, more particularly for optimizing gas/liquid transfer parameters of certain technologies.
- The hydrogen pressure in the reactor advantageously ranges from 5 to 70·105 Pa (5 and 70 bar), preferably from 10 to 50·105 Pa (10 and 50 bar).
- This gas is charged by any means known to this art for enabling the gas to be distributed homogeneously within the reactor.
- Preferably, the reaction is carried out in a stirred reactor, or in a loop reactor.
- The temperature of reaction more particularly ranges from 50° to 200° C.
- After the hydrogenation reaction is complete, the reaction mixture is separated from the catalyst by settling or filtration, using conventional techniques.
- Of course, the amount of reaction mixture separated corresponds to the amount of nitrated compound, optionally in the presence of the solvent, introduced into the reaction zone, such as to maintain stable operating conditions.
- The reaction mixture separated from the catalyst is then treated according to its composition and its subsequent intended use.
- Thus, if the reaction is carried out using a solvent, the hydrogenated amino product obtained is separated, for example, by distillation. It will be appreciated that, depending on the choice of solvent and the subsequent step to which the hydrogenated products will be subjected, this separation step may be unnecessary.
- Next, the aromatic hydrogenated product can be employed in a phosgenation reaction, after being dehydrated, to obtain aromatic isocyanates, which are intermediates in the production of polyurethanes, or else, if necessary, distilled in order to separate the various isomers obtained.
- In order to further illustrate the present invention and the advantages thereof, the following specific examples are given, it being understood that same are intended only as illustrative and in nowise limitative.
- A standard undoped Raney nickel containing 8% total aluminum by weight was evaluated using two tests (Test 1 and Test 2).
- (a) Test 1:
- 50 g/h of a mixture of dinitrotoluene (DNT) isomers were introduced continuously into a reactor containing 0.7 g of Raney nickel at 150° C. under a hydrogen pressure of 20 bar.
- The DNT feed was continued until the DNT content in the reactor exceeded 1,000 ppm.
- The hydrogen feed was determined by the progress of the reaction in order to remain at constant pressure in the reactor.
- The reaction was terminated after 6 hours (h). [00109] The yield of the reaction at t=4 hours was about 99%.
- (b) Test 2:
- A sample of the initial catalyst (not having been subjected to the hydrogenation) was introduced with a mixture of toluenediamine (TDA) isomers and water into a glass tube termed a Carius tube, which was sealed and then maintained for 1 month at 150° C. under autogenous pressure.
- After one month, the tube was opened; the catalyst was irrecoverable and extremely hard.
- The structure of the catalyst was determined by X-ray diffraction to be that of a nickel aluminate (takovite). This structure was the same as that of the deposit (screen) observed on the walls of apparatus utilized on an industrial scale.
- The catalyst employed was a Raney nickel recovered from a nitrile hydrogenation unit containing 3.5% total aluminum by weight. The catalyst was first washed with water and then dilute (1N) sodium hydroxide and then again with water. The catalyst was then evaluated employing the same tests as those described in Example 1.
- (a) Test 1:
- Test 1 of Example 1 was repeated.
- The results were as follows:
- (i) the reaction was terminated after 8 hours;
- (ii) the reaction yield at t=4 h was 99.2%.
- (b) Test 2:
- Test 2 of Example 1 was repeated.
- The results were as follows:
- (iii) the tube was opened after 1 month; the catalyst was recoverable and only slightly hard.
- Using X-ray diffraction, the structure of the catalyst was basically that of nickel. It contained a small proportion of nickel aluminate (at least half the amount as that in the catalyst of Example 1).
- The catalyst employed in this example was an undoped nickel-based supported catalyst containing about 2% total aluminum by weight, in the form of alumina, 2 to 6% ZrO2, silica and nickel with a total nickel content of 55% by weight.
- The catalyst was evaluated using the same tests as those described in Example 1.
- (a) Test 1:
- Test 1 of Example 1 was repeated.
- The results were as follows:
- (i) the reaction was terminated after 9 hours;
- (ii) the reaction yield at t=4 h was close to 99.2%.
- (b) Test 2:
- Test 2 of Example 1 was repeated.
- The results were as follows:
- (iii) when the tube was opened, after 1 month, the catalyst was recoverable and not hard.
- Using X-ray diffraction, the structure of the catalyst was found to be basically the same as that observed in the fresh catalyst.
- While the invention has been described in terms of various specific and preferred embodiments, the skilled artisan will appreciate that various modifications, substitutions, omissions, and changes may be made without departing from the spirit thereof. Accordingly, it is intended that the scope of the present invention be limited solely by the scope of the following claims, including equivalents thereof.
Claims (22)
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FR0003903 | 2000-03-28 | ||
FR0003903A FR2807036B1 (en) | 2000-03-28 | 2000-03-28 | CONTINUOUS HYDROGENATION OF AROMATIC NITER COMPOUNDS USING A LOW ALUMINUM CATALYST |
FR00/03903 | 2000-03-28 |
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US20010027257A1 true US20010027257A1 (en) | 2001-10-04 |
US6423872B2 US6423872B2 (en) | 2002-07-23 |
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US09/818,507 Expired - Lifetime US6423872B2 (en) | 2000-03-28 | 2001-03-28 | Continuous Ni/low A1 catalyzed hydrogenation of aromatic nitro compounds |
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US (1) | US6423872B2 (en) |
EP (1) | EP1138665B1 (en) |
JP (1) | JP2001316337A (en) |
KR (1) | KR100784741B1 (en) |
CN (1) | CN1198787C (en) |
AT (1) | ATE249416T1 (en) |
BR (1) | BR0101169B1 (en) |
CA (1) | CA2342257C (en) |
DE (1) | DE60100719T2 (en) |
ES (1) | ES2202263T3 (en) |
FR (1) | FR2807036B1 (en) |
HU (1) | HU230415B1 (en) |
ID (1) | ID29715A (en) |
MX (1) | MXPA01003213A (en) |
PL (1) | PL200746B1 (en) |
PT (1) | PT1138665E (en) |
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Cited By (9)
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US20070020508A1 (en) * | 2004-07-13 | 2007-01-25 | Hae Weon Lee | Anode of solid oxide fuel cell with networking structure and a method of its preparation |
WO2008145179A1 (en) * | 2007-05-29 | 2008-12-04 | Evonik Degussa Gmbh | Activated base metal catalysts |
US20100174116A1 (en) * | 2007-05-29 | 2010-07-08 | Evonik Degussa Gmbh | Activated Base Metal Catalysts |
US20100185026A1 (en) * | 2007-05-29 | 2010-07-22 | Evonik Degussa Gmbh | Activated Base Metal Catalysts |
US20100249460A1 (en) * | 2007-10-15 | 2010-09-30 | Evonik Degussa Gmbh | Fast Filtering Powder Catalytic Mixtures |
WO2012123469A1 (en) | 2011-03-16 | 2012-09-20 | Basf Se | Optimized metering of reactants for a process for preparing aromatic amines by hydrogenation of nitroaromatics |
WO2012177419A1 (en) * | 2011-06-24 | 2012-12-27 | Angus Chemical Company | Process and apparatus for production and filtration of aminoalcohols using a continuous stirred tank slurry reactor |
US8835688B2 (en) | 2011-03-16 | 2014-09-16 | Basf Se | Optimized introduction of the starting materials for a process for preparing aromatic amines by hydrogenation of nitroaromatics |
CN112076745A (en) * | 2020-09-21 | 2020-12-15 | 中北大学 | High-efficiency palladium-carbon catalyst and preparation method thereof |
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CA2515238C (en) * | 2003-07-04 | 2011-06-28 | Nongyue Wang | Process for preparing 4-aminodiphenylamine |
US8486223B2 (en) * | 2003-07-04 | 2013-07-16 | Jiangsu Sinorgchem Technology Co., Ltd. | Falling film evaporator |
US8686188B2 (en) | 2003-07-04 | 2014-04-01 | Jiangsu Sinorgchem Technology Co., Ltd. | Process for preparing 4-aminodiphenylamine |
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DE102005008613A1 (en) | 2005-02-23 | 2006-08-31 | Basf Ag | Preparation of e.g. aromatic amines comprises hydrogenating nitro-aromatic compounds in presence of catalyst, separating catalyst and measuring absorption of UV/visible radiation to determine concentrations of nitro and nitroso compounds |
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US8981155B2 (en) | 2010-12-06 | 2015-03-17 | Basf Se | Process for preparing aromatic amines |
BR112013012865A2 (en) | 2010-12-06 | 2016-09-06 | Basf Se | process for preparing aromatic amines, method of regulating the concentration of nitro compounds and nitro compounds, and apparatus |
CN110652985B (en) * | 2019-10-09 | 2022-05-10 | 南京科技职业学院 | Preparation method and application of catalyst for hydrogenation of dimer acid |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB821220A (en) * | 1957-06-27 | 1959-10-07 | Bayer Ag | A process for the production of toluylene diamines |
FR1290268A (en) * | 1961-03-01 | 1962-04-13 | Derives De L Acetylene Soc Ind | Manufacturing process of toluylenediamines 2-4 and 2-6 |
DE3537247A1 (en) * | 1985-10-19 | 1987-04-23 | Bayer Ag | USE OF MODIFIED RANEY CATALYSTS FOR PRODUCING AROMATIC DIAMINO COMPOUNDS |
-
2000
- 2000-03-28 FR FR0003903A patent/FR2807036B1/en not_active Expired - Lifetime
-
2001
- 2001-03-27 DE DE60100719T patent/DE60100719T2/en not_active Expired - Lifetime
- 2001-03-27 HU HU0101198A patent/HU230415B1/en unknown
- 2001-03-27 BR BRPI0101169-3A patent/BR0101169B1/en not_active IP Right Cessation
- 2001-03-27 KR KR1020010016066A patent/KR100784741B1/en not_active IP Right Cessation
- 2001-03-27 AT AT01400779T patent/ATE249416T1/en not_active IP Right Cessation
- 2001-03-27 EP EP01400779A patent/EP1138665B1/en not_active Expired - Lifetime
- 2001-03-27 CA CA002342257A patent/CA2342257C/en not_active Expired - Fee Related
- 2001-03-27 PL PL346686A patent/PL200746B1/en unknown
- 2001-03-27 ES ES01400779T patent/ES2202263T3/en not_active Expired - Lifetime
- 2001-03-27 PT PT01400779T patent/PT1138665E/en unknown
- 2001-03-28 TW TW90107222A patent/TW572872B/en not_active IP Right Cessation
- 2001-03-28 ID IDP20010260D patent/ID29715A/en unknown
- 2001-03-28 MX MXPA01003213A patent/MXPA01003213A/en active IP Right Grant
- 2001-03-28 US US09/818,507 patent/US6423872B2/en not_active Expired - Lifetime
- 2001-03-28 SG SG200101947A patent/SG91353A1/en unknown
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Also Published As
Publication number | Publication date |
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HUP0101198A3 (en) | 2002-12-28 |
US6423872B2 (en) | 2002-07-23 |
PL346686A1 (en) | 2001-10-08 |
EP1138665B1 (en) | 2003-09-10 |
BR0101169A (en) | 2001-10-30 |
ID29715A (en) | 2001-10-04 |
ES2202263T3 (en) | 2004-04-01 |
JP2001316337A (en) | 2001-11-13 |
PL200746B1 (en) | 2009-02-27 |
FR2807036B1 (en) | 2002-05-10 |
ATE249416T1 (en) | 2003-09-15 |
DE60100719D1 (en) | 2003-10-16 |
EP1138665A1 (en) | 2001-10-04 |
CN1332148A (en) | 2002-01-23 |
CA2342257C (en) | 2006-06-13 |
KR20010093726A (en) | 2001-10-29 |
CN1198787C (en) | 2005-04-27 |
BR0101169B1 (en) | 2011-05-03 |
KR100784741B1 (en) | 2007-12-13 |
HUP0101198A2 (en) | 2002-08-28 |
TW572872B (en) | 2004-01-21 |
CA2342257A1 (en) | 2001-09-28 |
MXPA01003213A (en) | 2004-07-30 |
HU230415B1 (en) | 2016-05-30 |
PT1138665E (en) | 2003-12-31 |
DE60100719T2 (en) | 2004-07-22 |
FR2807036A1 (en) | 2001-10-05 |
SG91353A1 (en) | 2002-09-17 |
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