EP3860969A1 - Procédé d'hydroformylation d'oléfines à chaîne courte en phase gazeuse - Google Patents
Procédé d'hydroformylation d'oléfines à chaîne courte en phase gazeuseInfo
- Publication number
- EP3860969A1 EP3860969A1 EP19773873.5A EP19773873A EP3860969A1 EP 3860969 A1 EP3860969 A1 EP 3860969A1 EP 19773873 A EP19773873 A EP 19773873A EP 3860969 A1 EP3860969 A1 EP 3860969A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- support
- catalyst system
- hydroformylation
- reactor
- catalyst
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 33
- 238000004519 manufacturing process Methods 0.000 title description 7
- 239000003054 catalyst Substances 0.000 claims abstract description 92
- 238000007037 hydroformylation reaction Methods 0.000 claims abstract description 37
- 238000000034 method Methods 0.000 claims abstract description 37
- 229910010293 ceramic material Inorganic materials 0.000 claims abstract description 16
- 230000008569 process Effects 0.000 claims abstract description 13
- 239000000203 mixture Substances 0.000 claims description 44
- 238000006243 chemical reaction Methods 0.000 claims description 24
- 239000002608 ionic liquid Substances 0.000 claims description 23
- 230000015572 biosynthetic process Effects 0.000 claims description 22
- 239000007789 gas Substances 0.000 claims description 19
- -1 amine compound Chemical class 0.000 claims description 18
- 239000000919 ceramic Substances 0.000 claims description 16
- 239000000463 material Substances 0.000 claims description 15
- 239000003381 stabilizer Substances 0.000 claims description 15
- 239000003446 ligand Substances 0.000 claims description 13
- 239000008187 granular material Substances 0.000 claims description 12
- 238000003786 synthesis reaction Methods 0.000 claims description 12
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 8
- 229910052698 phosphorus Inorganic materials 0.000 claims description 8
- 239000011574 phosphorus Substances 0.000 claims description 8
- 239000002245 particle Substances 0.000 claims description 7
- 239000000843 powder Substances 0.000 claims description 7
- 239000008188 pellet Substances 0.000 claims description 6
- 229910052751 metal Inorganic materials 0.000 claims description 5
- 239000002184 metal Substances 0.000 claims description 5
- 229910010271 silicon carbide Inorganic materials 0.000 claims description 5
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 claims description 5
- 229910021332 silicide Inorganic materials 0.000 claims description 4
- FVBUAEGBCNSCDD-UHFFFAOYSA-N silicide(4-) Chemical compound [Si-4] FVBUAEGBCNSCDD-UHFFFAOYSA-N 0.000 claims description 4
- 239000002638 heterogeneous catalyst Substances 0.000 claims description 3
- 230000000737 periodic effect Effects 0.000 claims description 3
- RKMGAJGJIURJSJ-UHFFFAOYSA-N 2,2,6,6-tetramethylpiperidine Chemical group CC1(C)CCCC(C)(C)N1 RKMGAJGJIURJSJ-UHFFFAOYSA-N 0.000 claims description 2
- 229910052580 B4C Inorganic materials 0.000 claims description 2
- 229910052582 BN Inorganic materials 0.000 claims description 2
- PZNSFCLAULLKQX-UHFFFAOYSA-N Boron nitride Chemical compound N#B PZNSFCLAULLKQX-UHFFFAOYSA-N 0.000 claims description 2
- 229910052581 Si3N4 Inorganic materials 0.000 claims description 2
- YXTPWUNVHCYOSP-UHFFFAOYSA-N bis($l^{2}-silanylidene)molybdenum Chemical compound [Si]=[Mo]=[Si] YXTPWUNVHCYOSP-UHFFFAOYSA-N 0.000 claims description 2
- INAHAJYZKVIDIZ-UHFFFAOYSA-N boron carbide Chemical compound B12B3B4C32B41 INAHAJYZKVIDIZ-UHFFFAOYSA-N 0.000 claims description 2
- PMHQVHHXPFUNSP-UHFFFAOYSA-M copper(1+);methylsulfanylmethane;bromide Chemical compound Br[Cu].CSC PMHQVHHXPFUNSP-UHFFFAOYSA-M 0.000 claims description 2
- 125000004430 oxygen atom Chemical group O* 0.000 claims description 2
- HQVNEWCFYHHQES-UHFFFAOYSA-N silicon nitride Chemical compound N12[Si]34N5[Si]62N3[Si]51N64 HQVNEWCFYHHQES-UHFFFAOYSA-N 0.000 claims description 2
- UONOETXJSWQNOL-UHFFFAOYSA-N tungsten carbide Chemical compound [W+]#[C-] UONOETXJSWQNOL-UHFFFAOYSA-N 0.000 claims description 2
- 229910021344 molybdenum silicide Inorganic materials 0.000 claims 1
- 239000002904 solvent Substances 0.000 description 25
- 239000000243 solution Substances 0.000 description 23
- 239000000047 product Substances 0.000 description 22
- 238000000926 separation method Methods 0.000 description 17
- 150000001299 aldehydes Chemical class 0.000 description 16
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- 230000000694 effects Effects 0.000 description 11
- 239000011261 inert gas Substances 0.000 description 11
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- 238000011065 in-situ storage Methods 0.000 description 9
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 9
- 238000005470 impregnation Methods 0.000 description 7
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- 239000007787 solid Substances 0.000 description 7
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 description 6
- 239000006227 byproduct Substances 0.000 description 6
- 229910017052 cobalt Inorganic materials 0.000 description 6
- 239000010941 cobalt Substances 0.000 description 6
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 6
- 229910052703 rhodium Inorganic materials 0.000 description 6
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 125000004209 (C1-C8) alkyl group Chemical group 0.000 description 5
- 150000001335 aliphatic alkanes Chemical class 0.000 description 5
- 235000013844 butane Nutrition 0.000 description 5
- 238000011049 filling Methods 0.000 description 5
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 125000004191 (C1-C6) alkoxy group Chemical group 0.000 description 4
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 4
- 125000004103 aminoalkyl group Chemical group 0.000 description 4
- IAQRGUVFOMOMEM-UHFFFAOYSA-N but-2-ene Chemical compound CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 4
- 238000009833 condensation Methods 0.000 description 4
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- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 4
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- 229910052723 transition metal Inorganic materials 0.000 description 4
- 150000003624 transition metals Chemical class 0.000 description 4
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- WEVYAHXRMPXWCK-UHFFFAOYSA-N Acetonitrile Chemical compound CC#N WEVYAHXRMPXWCK-UHFFFAOYSA-N 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 3
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000001273 butane Substances 0.000 description 3
- 239000012876 carrier material Substances 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- 230000009849 deactivation Effects 0.000 description 3
- ZUOUZKKEUPVFJK-UHFFFAOYSA-N diphenyl Chemical group C1=CC=CC=C1C1=CC=CC=C1 ZUOUZKKEUPVFJK-UHFFFAOYSA-N 0.000 description 3
- 238000004817 gas chromatography Methods 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 3
- 150000004767 nitrides Chemical class 0.000 description 3
- 239000002243 precursor Substances 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 239000007858 starting material Substances 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- ZXMGHDIOOHOAAE-UHFFFAOYSA-N 1,1,1-trifluoro-n-(trifluoromethylsulfonyl)methanesulfonamide Chemical compound FC(F)(F)S(=O)(=O)NS(=O)(=O)C(F)(F)F ZXMGHDIOOHOAAE-UHFFFAOYSA-N 0.000 description 2
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N Propene Chemical compound CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 2
- 230000004913 activation Effects 0.000 description 2
- 125000000217 alkyl group Chemical group 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 150000001768 cations Chemical class 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- XNMQEEKYCVKGBD-UHFFFAOYSA-N dimethylacetylene Natural products CC#CC XNMQEEKYCVKGBD-UHFFFAOYSA-N 0.000 description 2
- 238000003618 dip coating Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- ZMZDMBWJUHKJPS-UHFFFAOYSA-N hydrogen thiocyanate Natural products SC#N ZMZDMBWJUHKJPS-UHFFFAOYSA-N 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000011835 investigation Methods 0.000 description 2
- 229910052741 iridium Inorganic materials 0.000 description 2
- GKOZUEZYRPOHIO-UHFFFAOYSA-N iridium atom Chemical compound [Ir] GKOZUEZYRPOHIO-UHFFFAOYSA-N 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000012544 monitoring process Methods 0.000 description 2
- YWAKXRMUMFPDSH-UHFFFAOYSA-N pentene Chemical compound CCCC=C YWAKXRMUMFPDSH-UHFFFAOYSA-N 0.000 description 2
- QMMOXUPEWRXHJS-UHFFFAOYSA-N pentene-2 Natural products CCC=CC QMMOXUPEWRXHJS-UHFFFAOYSA-N 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 125000004178 (C1-C4) alkyl group Chemical group 0.000 description 1
- KIDIBVPFLKLKAH-UHFFFAOYSA-M 1-butyl-3-methylimidazol-3-ium;octyl sulfate Chemical compound CCCCN1C=C[N+](C)=C1.CCCCCCCCOS([O-])(=O)=O KIDIBVPFLKLKAH-UHFFFAOYSA-M 0.000 description 1
- VRFOKYHDLYBVAL-UHFFFAOYSA-M 1-ethyl-3-methylimidazol-3-ium;ethyl sulfate Chemical compound CCOS([O-])(=O)=O.CCN1C=C[N+](C)=C1 VRFOKYHDLYBVAL-UHFFFAOYSA-M 0.000 description 1
- ZDZHCHYQNPQSGG-UHFFFAOYSA-N 1-naphthalen-1-ylnaphthalene Chemical group C1=CC=C2C(C=3C4=CC=CC=C4C=CC=3)=CC=CC2=C1 ZDZHCHYQNPQSGG-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- RAXXELZNTBOGNW-UHFFFAOYSA-O Imidazolium Chemical compound C1=C[NH+]=CN1 RAXXELZNTBOGNW-UHFFFAOYSA-O 0.000 description 1
- 238000001069 Raman spectroscopy Methods 0.000 description 1
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 1
- ZMZDMBWJUHKJPS-UHFFFAOYSA-M Thiocyanate anion Chemical compound [S-]C#N ZMZDMBWJUHKJPS-UHFFFAOYSA-M 0.000 description 1
- 239000007983 Tris buffer Substances 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000002318 adhesion promoter Substances 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 238000005882 aldol condensation reaction Methods 0.000 description 1
- 125000002723 alicyclic group Chemical group 0.000 description 1
- 125000001931 aliphatic group Chemical group 0.000 description 1
- 125000003545 alkoxy group Chemical group 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 125000004429 atom Chemical group 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000011324 bead Substances 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- XITRBUPOXXBIJN-UHFFFAOYSA-N bis(2,2,6,6-tetramethylpiperidin-4-yl) decanedioate Chemical compound C1C(C)(C)NC(C)(C)CC1OC(=O)CCCCCCCCC(=O)OC1CC(C)(C)NC(C)(C)C1 XITRBUPOXXBIJN-UHFFFAOYSA-N 0.000 description 1
- INDFXCHYORWHLQ-UHFFFAOYSA-N bis(trifluoromethylsulfonyl)azanide;1-butyl-3-methylimidazol-3-ium Chemical compound CCCCN1C=C[N+](C)=C1.FC(F)(F)S(=O)(=O)[N-]S(=O)(=O)C(F)(F)F INDFXCHYORWHLQ-UHFFFAOYSA-N 0.000 description 1
- LRESCJAINPKJTO-UHFFFAOYSA-N bis(trifluoromethylsulfonyl)azanide;1-ethyl-3-methylimidazol-3-ium Chemical compound CCN1C=C[N+](C)=C1.FC(F)(F)S(=O)(=O)[N-]S(=O)(=O)C(F)(F)F LRESCJAINPKJTO-UHFFFAOYSA-N 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 229910052794 bromium Inorganic materials 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- GGRQQHADVSXBQN-FGSKAQBVSA-N carbon monoxide;(z)-4-hydroxypent-3-en-2-one;rhodium Chemical compound [Rh].[O+]#[C-].[O+]#[C-].C\C(O)=C\C(C)=O GGRQQHADVSXBQN-FGSKAQBVSA-N 0.000 description 1
- 150000007942 carboxylates Chemical class 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 150000008280 chlorinated hydrocarbons Chemical class 0.000 description 1
- 150000001805 chlorine compounds Chemical class 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000007598 dipping method Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 150000004820 halides Chemical class 0.000 description 1
- 125000005843 halogen group Chemical group 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 238000007172 homogeneous catalysis Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000003384 imaging method Methods 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 239000000543 intermediate Substances 0.000 description 1
- 229910052740 iodine Inorganic materials 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 238000010327 methods by industry Methods 0.000 description 1
- 125000000956 methoxy group Chemical group [H]C([H])([H])O* 0.000 description 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 229910021343 molybdenum disilicide Inorganic materials 0.000 description 1
- 238000001728 nano-filtration Methods 0.000 description 1
- 229910052756 noble gas Inorganic materials 0.000 description 1
- 150000002835 noble gases Chemical class 0.000 description 1
- 125000002347 octyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 125000006340 pentafluoro ethyl group Chemical group FC(F)(F)C(F)(F)* 0.000 description 1
- 125000005010 perfluoroalkyl group Chemical group 0.000 description 1
- 150000003003 phosphines Chemical class 0.000 description 1
- AQSJGOWTSHOLKH-UHFFFAOYSA-N phosphite(3-) Chemical class [O-]P([O-])[O-] AQSJGOWTSHOLKH-UHFFFAOYSA-N 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 238000002459 porosimetry Methods 0.000 description 1
- 229910021426 porous silicon Inorganic materials 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 229910052814 silicon oxide Inorganic materials 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 125000000999 tert-butyl group Chemical group [H]C([H])([H])C(*)(C([H])([H])[H])C([H])([H])[H] 0.000 description 1
- JOXIMZWYDAKGHI-UHFFFAOYSA-N toluene-4-sulfonic acid Chemical compound CC1=CC=C(S(O)(=O)=O)C=C1 JOXIMZWYDAKGHI-UHFFFAOYSA-N 0.000 description 1
- ITMCEJHCFYSIIV-UHFFFAOYSA-M triflate Chemical compound [O-]S(=O)(=O)C(F)(F)F ITMCEJHCFYSIIV-UHFFFAOYSA-M 0.000 description 1
- JFZKOODUSFUFIZ-UHFFFAOYSA-N trifluoro phosphate Chemical compound FOP(=O)(OF)OF JFZKOODUSFUFIZ-UHFFFAOYSA-N 0.000 description 1
- LAGQNGWYNLUQRI-UHFFFAOYSA-N trioctylmethylammonium bis(trifluoromethylsulfonyl)imide Chemical compound FC(F)(F)S(=O)(=O)[N-]S(=O)(=O)C(F)(F)F.CCCCCCCC[N+](C)(CCCCCCCC)CCCCCCCC LAGQNGWYNLUQRI-UHFFFAOYSA-N 0.000 description 1
- LENZDBCJOHFCAS-UHFFFAOYSA-N tris Chemical compound OCC(N)(CO)CO LENZDBCJOHFCAS-UHFFFAOYSA-N 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/49—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide
- C07C45/50—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide by oxo-reactions
- C07C45/505—Asymmetric hydroformylation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/49—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide
- C07C45/50—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide by oxo-reactions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
- B01J21/08—Silica
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/46—Ruthenium, rhodium, osmium or iridium
- B01J23/464—Rhodium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/20—Carbon compounds
- B01J27/22—Carbides
- B01J27/224—Silicon carbide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
- B01J31/0234—Nitrogen-, phosphorus-, arsenic- or antimony-containing compounds
- B01J31/0235—Nitrogen containing compounds
- B01J31/0237—Amines
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J31/24—Phosphines, i.e. phosphorus bonded to only carbon atoms, or to both carbon and hydrogen atoms, including e.g. sp2-hybridised phosphorus compounds such as phosphabenzene, phosphole or anionic phospholide ligands
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- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
- C07C2521/08—Silica
Definitions
- the present invention relates to a process for the hydroformylation of short-chain olefins, in particular C2 to C5 olefins, in which the catalyst system is present heterogeneously on a support made of a porous ceramic material, and to plants for carrying out this process.
- Alkenes olefins
- carbon monoxide and hydrogen also:
- Synthesis gas or syngas converted to aldehydes using a catalyst, which are important and valuable intermediates in the manufacture of chemical bulk products such as alcohols, esters or plasticizers.
- the hydroformylation is carried out on an industrial scale exclusively under homogeneous catalysis.
- the soluble transition metal catalyst systems are usually based on cobalt or rhodium, which is often used with phosphorus-containing ligands, for example phosphines or phosphites, for the hydroformylation of rather short-chain olefins.
- Immobilization should therefore be understood to mean that the catalyst is formed on the surface and / or in the surface by forming a thin liquid film using an ionic liquid Pores of a solid support material is immobilized and there is no reaction solution in the classic sense in which the catalyst is homogeneously dissolved.
- SILP systems Supported Lonic Liquid Phase
- the catalyst system with rhodium, iridium or cobalt as the central atom is immobilized, in particular on a porous silicon dioxide carrier, using an ionic liquid.
- the object of the present invention was therefore to provide a method for
- a catalyst system is used in the hydroformylation, the catalyst system being heterogenized on a support which is in the form of a powder, in the form of granules or in the form of pellets and is made of a porous ceramic material.
- the present invention thus relates to a process for the hydroformylation of C2 to C5 olefins in a reaction zone using a heterogenized one
- Catalyst system the method being characterized in that a gaseous feed mixture containing the C2 to C8 olefins together with
- Catalyst system which is a metal from the 8th or 9th group of the Periodic Table of the Elements, at least one organic phosphorus-containing ligand, a stabilizer and optionally an ionic liquid, is present in heterogeneous form; and the support, which is in the form of a powder, in the form of a granulate or in the form of pellets and consists of a carbide, nitride, silicide material or mixtures thereof, to which a washcoat, based on the ceramic material of the support, is the same or another ceramic material is applied.
- All mixtures which comprise C2 to C5 olefins, in particular ethene, propene, 1-butene, 2-butene, 1-pentene or 2-pentene, as starting materials can be used as the first feed mixture.
- the amount of olefins in the feed mixtures should understandably be high enough to be sufficient To operate hydroformylation reaction economically.
- These include in particular technical mixtures from the petrochemical industry, such as raffinate streams (raffinate I, II or III) or raw butane.
- raw butane comprises 5 to 40% by weight of butenes, preferably 20 to 40% by weight of butenes (the butenes are composed of 1 to 20% by weight of 1-butene and 80 to 99% by weight of 2 -Butene) and 60 to 95% by weight of butanes, preferably 60 to 80% by weight of butanes.
- the reaction zone comprises at least one reactor in which the inventive
- the reaction zone comprises a plurality of reactors which can be connected in parallel or in series.
- the reactors are preferably connected in parallel and are used alternately.
- At least one reactor (a) is used for the hydroformylation, so the reactor is in operation.
- At least one further reactor (b) is on hold, with no hydroformylation being carried out there. This should be understood to mean that as soon as the reactor (a) in operation is no longer sufficient
- Catalyst activity is determined, the flow of the feed mixture is switched from this reactor (a) to the next reactor (b) on hold and this reactor (b) is thus put into operation.
- Reactor (a) is then transferred to a regeneration mode, where the catalyst system is regenerated as described below or the support is re-impregnated, and then transferred to the waiting position until the reactor is started up again.
- This principle can also be applied to 3 or more reactors, where at least one reactor is in operation, one or more reactors are on hold at the same time and one or more reactors are in regeneration mode at the same time.
- the hydroformylation is preferably carried out under the following conditions:
- the temperature during the hydroformylation should be in the range from 65 to 200 ° C., preferably 75 to 175 ° C. and particularly preferably 85 to 150 ° C.
- the pressure should not exceed 35 bar, preferably 30 bar, particularly preferably 25 bar during the hydroformylation.
- the molar ratio between synthesis gas and the feed mixture should be between 6: 1 and 1: 1, preferably between 5: 1 and 3: 1.
- the feed mixture can optionally be diluted with inert gas, for example with the alkanes present in technical hydrocarbon streams.
- the catalyst system used in the hydroformylation process according to the invention preferably comprises a transition metal from the 8th or 9th group of the Periodic Table of the Elements, in particular iron, ruthenium, iridium, cobalt or rhodium, particularly preferably cobalt and rhodium, at least one organic phosphorus-containing ligand Stabilizer and optionally an ionic liquid.
- the stabilizer is preferably an organic amine compound, particularly preferably an organic amine compound which contains at least one 2,2,6,6-tetramethylpiperidine unit of the formula (I):
- the stabilizer is selected from the group consisting of the compounds of the following formulas (1.1), (I.2), (I.3), (I.4), (I.5) , (I.6), (I.7) and (I.8).
- n is an integer from 1 to 20;
- w Mob «eai n corresponds to an integer from 1 to 12;
- n is an integer from 1 to 17;
- R corresponds to a C6 to C20 alkyl group.
- the optionally present ionic liquid in the sense of the present invention is an almost water-free (water content ⁇ 1.5% by weight based on the total ionic liquid) liquid, which is liquid at normal pressure (1,01325 bar) and preferably at 25 ° C.
- the ionic liquid preferably consists of more than 98% by weight of ions.
- the anion of the ionic liquid is selected from the group consisting of tetrafluoroborate [BF4] -; Hexafluorophosphate [PF6] -; Dicyanamide
- the cation of the ionic liquid is preferably selected from the group consisting of quaternary ammonium cations of the general formula [NR 1 R 2 R 3 R 4 ] + where R 1 , R 2 , R 3 , R 4 are each independently a C1- Represent C8 alkyl group; Phosphonium cations of the general formula [PR 1 R 2 R 3 R 4 ] + where R 1 , R 2 , R 3 , R 4 each independently represent a C1-C8-alkyl group; Imidazolium cations of the general formula (II)
- R 1 , R 2 , R 3 and R 4 each independently represent H or a C1 to C8 alkyl group, a C1 to C6 alkoxy group, an optionally substituted C1 to C6 aminoalkyl group or an optionally substituted C5 to C12 aryl group;
- R 1 and R 2 each independently represent H or a C1 to C8 alkyl group, a C1 to C6 alkoxy group, an optionally substituted C1 to C6 aminoalkyl group or an optionally substituted C5 to C12 aryl group;
- R 1 and R 2 each independently represent H or a C1 to C8 alkyl group, a C1 to C6 alkoxy group, an optionally substituted C1 to C6 aminoalkyl group or an optionally substituted C5 to C12 aryl group;
- R 1 and R 2 and / or R 3 each independently represent H or a C1 to C8 alkyl group, a C1 to C6 alkoxy group, an optionally substituted C1 to C6 aminoalkyl group or an optionally substituted C5 to C12 aryl group.
- the cation of the ionic liquid is an imidazolium cation according to the aforementioned general formula (II) with a corresponding definition of the radicals R 1 to R 4 .
- the ionic liquid is selected from the group consisting of 1-ethyl-3-methylimidazolium bis (trifluoromethylsulfonyl) imide, 1-butyl-3-methylimidazolium hexafluorophosphate, 1-butyl-3-methylimidazolium tetrafluoroborate, 1-butyl -3-methylimidazolium bis (trifluoromethylsulfonyl) imide, 1-ethyl-3-methylimidazolium ethyl sulfate, trioctyl-methylammonium bis (trifluoromethylsulfonyl) imide and 1-butyl-3-methylimidazolium octyl sulfate.
- the optionally present ionic liquid serves in the catalyst system according to the invention as a carrier solution for the transition metal catalyst with ligands and the stabilizer. It is important that the ionic liquid absorb the reactants (feed olefins and synthesis gas) to a sufficient extent, i. H. solve, and a comparatively low
- Liquid reservoir is present.
- the stabilizer can also form a stable liquid film in the pores of the support and is therefore able to replace the ionic liquid partially or completely.
- the catalyst system contains no ionic liquid.
- the gas solubility for the reactants should be better than the gas solubility of the Products. Partial separation of the starting material olefins used and the product aldehydes formed can be achieved in this way alone. In principle, other film-forming substances would also be conceivable for this, but care must be taken to ensure that there is no increased formation of high boilers and / or that the feed of the educt olefins is restricted.
- the organic phosphorus-containing ligand for the catalyst system according to the invention preferably has the general formula (VI)
- R '- A - R "- A - R"' (VI) where R ', R “and R”' are each organic radicals and both A are each a bridging -0-P (-0) 2 group, where two of the three oxygen atoms -O- are each bound to radical R 'and the radical R "', with the proviso that R 'and R"' are not identical.
- the organic radicals R ', R “and R”' preferably do not contain a terminal trialkoxysilane group.
- the substituted 1, 1 ' biphenyl groups in the 3,3 ' and / or 5.5 ' position of the 1, 1 ' biphenyl main body particularly preferably have an alkyl group and / or an alkoxy group, in particular a C1-C4-alkyl group, particularly preferably a tert-butyl and / or methyl group and / or preferably a C1-C5 alkox group, particularly preferably a methoxy group.
- the aforementioned catalyst system is present heterogenized on a support made of a porous ceramic material.
- the expression “heterogenized on a support” is to be understood in such a way that the catalyst system passes through
- Carrier material is immobilized.
- the film can also be solid at room temperature and at
- the inner surface of the solid carrier material comprises in particular the inner surface of the pores.
- immobilization encompasses both the case that the catalyst system and / or the catalytically active species are present in solution in the solid or liquid film, and the cases that the stabilizer acts as an adhesion promoter or that the catalyst system is adsorbed on the surface, but not chemically or is covalently bound on the surface.
- the porous support material is preferably selected from the group consisting of a nitridic ceramic, a carbidic ceramic, a silicidic ceramic and mixtures thereof, for example carbonitridic materials.
- the nitridic ceramic is preferably selected from silicon nitride, boron nitride, aluminum nitride and mixtures thereof.
- the carbidic ceramic is preferably selected from silicon carbide, boron carbide, tungsten carbide or mixtures thereof. Mixtures of carbide and nitride ceramics, the so-called carbonitrides, are also conceivable.
- the silicide ceramic is preferably molybdenum disilicide.
- the support according to the present invention, to which the catalyst system is applied preferably consists of a carbide ceramic, particularly preferably of silicon carbide.
- the support is preferably in the form of a powder, in the form of granules or in the form of pellets.
- the average particle diameter (d50) of the support can be from 0.1 mm to 7 mm, preferably 0.3 to 6 mm, particularly preferably from 0.5 mm to 5 mm.
- the mean particle diameter can be determined by means of imaging methods, in particular by means of the methods mentioned in the standards ISO 13322-1 (status: 2004-12-01) and ISO 13322-2 (status: 2006-11-01).
- the support can be produced in the form of a powder, in the form of granules or in the form of pellets by methods known to the person skilled in the art. For example, it could be done by mechanically comminuting a monolith made of the carbide, nitride, silicide material or mixtures thereof, for example with a jaw crusher, and the particle size of the obtained one
- Fracture granulate is adjusted by means of sieving.
- the support are the particles of the powder, the granulate or the
- Pellet particles made of porous ceramic material, so the support has pores.
- the catalyst system according to the invention is in particular also in the solid or liquid film in these pores.
- the pore diameter is preferably in the range from 0.9 nm to 30 ⁇ m, preferably in the range from 10 nm to 25 ⁇ m and particularly preferably in the range from 70 nm to 20 ⁇ m.
- the pore diameter can be determined by means of nitrogen adsorption or mercury porosimetry according to DIN 66133 (status: 1993-06).
- the support has at least partially continuous pores that extend from one surface to another surface. It is also possible for a number of pores to be connected to one another and thus to form a single continuous pore.
- the catalyst system is heterogenized, as described below:
- a so-called washcoat is applied to the powder, granulate or pellet-shaped support made of the ceramic material, which, based on the ceramic material of the support, is preferably made of the same or a different ceramic material Silicon oxide.
- the washcoat itself can be porous or non-porous, preferably the washcoat is non-porous.
- the particle size of the washcoat is preferably 5 nm to 3 nm, preferably 7 nm to 700 nm.
- the washcoat is used to introduce or generate the desired pore size and / or to increase the surface of the support.
- the washcoat can be applied, in particular, by dipping (dipcoating) into a washcoat solution, which
- Ceramic material of the washcoat possibly also as a precursor, contains.
- the amount of washcoat on the support is ⁇ 20% by weight, preferably ⁇ 15% by weight, particularly preferably ⁇ 10% by weight, based on the total amount of support.
- a catalyst solution is first prepared by mixing, in particular at room temperature and ambient pressure, the catalyst solution comprising at least one organic phosphorus-containing ligand, at least one metal precursor, for example chlorides, oxides, carboxylates of the respective metal, at least one stabilizer and at least one solvent includes.
- An ionic liquid can optionally be used in the production of the catalyst system, but the catalyst solution can also be prepared explicitly without an ionic liquid.
- the catalyst solution should in particular be prepared in an inert environment, for example in a glove box. In this case, an inert environment means an atmosphere that is as free of water and oxygen as possible.
- the solvent can be selected from all solvent classes (protic, aprotic, polar or non-polar).
- a prerequisite for the solvent is the solubility of the catalyst system (ligand, metal precursor, stabilizer and optionally the ionic liquid) and preferably also the high boilers formed during the hydroformylation.
- the solubility can be within the
- Immobilization step can be increased by heating.
- the solvent is preferably aprotic, polar, such as. B. acetonitrile and ethyl acetate or else aprotic, non-polar such as. B. THF and diethyl ether.
- Chlorinated hydrocarbons such as B. dichloromethane can be used as a solvent.
- the catalyst solution prepared in this way is then brought into contact with the support (optionally including washcoat), for example by immersion (dip coating) or by filling a pressure vessel, for example directly in the reactor (in-situ impregnation). If the catalyst solution is applied outside the reactor, the support must be removed after the
- Solvent are of course reinstalled in the reactor. The is preferred
- the reactor is flushed with an inert gas, for example noble gases, alkanes or nitrogen, before filling.
- the flushing can be carried out at 1 to 25 bar, preferably under a slight excess pressure of 20 to 90 mbar, particularly preferably 30 to 60 mbar above normal pressure.
- the reactor can be cooled with inert gas before purging to prevent the solvent of the catalyst solution to be filled from evaporating immediately. However, if the solvent has a boiling temperature that is higher than the temperature of the reactor, cooling of the reactor can be omitted.
- the existing pressure can be, for example, via the
- Pressure control be drained, preferably until the reactor is depressurized, that is
- Ambient pressure approximately 1 bar
- a vacuum can also be generated in the reactor, for example with a vacuum pump.
- the reactor can be flushed again with an inert gas, as described above, after the pressure has been released or after the vacuum has been drawn. This process of releasing pressure / drawing vacuum and rinsing again can be repeated as often as required.
- the catalyst solution is placed in a pressure vessel for filling the reactor and is preferably subjected to an inert gas pressure of 1 to 25 bar, particularly preferably a slight inert gas pressure of 20 to 90 mbar, preferably 30 to 60 mbar above the reactor pressure.
- the inert gas can be an inert gas, an alkane, for example butane, or nitrogen.
- the catalyst solution is then filled into the reactor, in particular pressure-driven, with the above-mentioned pressure which is applied to the pressure vessel.
- the pressure vessel should be higher when filling than in the reactor. Temperatures in the range from 20 to 150 ° C. and a pressure from 1 to 25 bar can be present. Another possibility for filling is that the reactor is kept in a vacuum after flushing with inert gas and the catalyst solution is drawn into the reactor by the suppressor. For the preparation of the catalyst solution, a solvent should be used which boils under the prevailing vacuum or negative pressure and the prevailing temperatures.
- the reactor solution can be filled with the catalyst solution via the normal inputs and outputs. Liquid distributors or nozzles within the reactor can ensure a uniform distribution of the catalyst liquid, as can optionally present ones
- the solvent is separated off.
- the remaining catalyst solution is first drained through the outlet of the reactor.
- solvent residues remaining in the reactor are evaporated by adjusting the pressure or increasing the temperature.
- the pressure can also be set by simultaneously increasing the temperature.
- the temperature can be 20 to 150 ° C depending on the solvent.
- the pressure can be set to a high vacuum (10 3 to 10 7 mbar), but depending on the solvent and temperature, overpressures from a few mbar to several bar are also conceivable.
- the stabilizer and the optional ionic liquid remain heterogenized on the support with the catalyst made of the transition metal, in particular cobalt or rhodium, and the organic phosphorus-containing ligand.
- the catalyst system can be applied to the support either directly in the reactor (in situ) or outside the reactor. Another problem is that the support must always be transported with the air sealed off, which is difficult to implement when installing and removing. In a preferred embodiment of the present invention, the application of the catalyst system is therefore applied directly in the reactor, that is to say in situ. After removing the
- the reactor can be used immediately and charged with the feed mixture. This has the advantage that no time-consuming installation and removal steps are necessary, which would result in a longer failure of the reactor.
- the size of the support is no longer limited by the fact that there are suitable rooms with inert environments of a certain size. The size of the support can be freely selected depending on the reactor design.
- the aim of the start-up procedure is a gentle activation of the catalyst system and a cushioning of the maximum starting activity of the catalyst to extend the life of the catalyst system.
- the start-up procedure is intended to prevent the formation of a liquid phase, since this can lead to deactivation, blocking and or washing out of the catalyst system. Especially when starting up a freshly made one
- Catalyst system (on the support) with concentrated educt can namely
- the activation of the catalyst system is preferably carried out according to the invention with a sales increase that is prolonged over time. So for any combination of pressure,
- Aldehyde concentration can be determined, ie the start-up procedure depends on the maximum conversion of the olefins used. With known long-term operating conditions of the reactor, which allow a reliable degree of conversion of the feed olefins from 20 to 95%, preferably from 80% to 95%, the
- Start-up procedure can be implemented in such a way that the composition of the feed mixture which is fed into the reactor is changed in stages without the maximum conversion of the feed olefins being exceeded.
- composition of the feed mixture which ensures reliable conversion of the olefins under long-term operating conditions, can be varied so that it remains constant
- volume flow of the olefin and / or the synthesis gas portion in at least two, preferably more than three stages, in particular four or more stages, is raised without the maximum conversion of the feed olefins being exceeded.
- Synthesis gas mixtures can do this in the first stage (s) inert gases such as N2, argon, helium or the like is supplied.
- inert gases such as N2, argon, helium or the like is supplied.
- the activity of the catalyst can decrease, for example due to the accumulation of high boilers and / or the occupation or deactivation of active centers.
- the high boilers can lead to increased condensation in the pores, so that the pores are no longer accessible or more slowly for the educt olefins.
- some by-products can lead to decomposition of the catalyst system, which also reduces the activity of the catalyst.
- a decrease in the catalyst activity can be determined, for example, on the basis of a drop in sales or selectivities, in particular by means of appropriate analysis using Raman spectroscopy, gas chromatography or mass flow meter (MDM). Model-based monitoring of the catalyst activity would also be possible. This would be a method of monitoring the
- the catalyst system which is heterogenized on the porous ceramic support can be replaced.
- the reactor or the support in the reactor can be rinsed once or several times with a solvent.
- the catalyst system can be demobilized and removed by rinsing.
- the solvent can be one of the solvents mentioned for the preparation of the catalyst solution.
- the temperature when rinsing with solvent can be 20 to 150 ° C.
- the pressure can also be 1 to 25 bar when flushing with solvent.
- the support After rinsing, the support is impregnated once or several times, in particular with the previously described in-situ impregnation of the support.
- the in-situ impregnation is thus renewed and the heterogeneous catalyst system is freshly applied.
- the re-in-situ impregnation can be carried out under exactly the same conditions as described for the first in-situ impregnation Due to the fact that the catalyst system is completely replaced by rinsing and reapplying, these steps can be repeated as soon as the activity of the catalyst drops again.
- Another advantage is that high boilers and product aldehydes as well as decomposition products of the catalyst system can be removed. However, care should be taken to ensure that the properties of the support by
- Catalyst system is heterogenized, is exchanged.
- the catalyst system which is heterogenized on the support (removed from the reactor), can then be exchanged outside the reactor as described above and stored in the reactor until the next installation and use.
- an inert environment is required when applying the catalyst system, which is why the handling and storage of the above
- a gaseous effluent is preferably withdrawn continuously, which contains at least part of the product aldehydes formed and at least part of the unreacted olefins.
- the gaseous discharge can be subjected to one or more material separation step (s) in which the gaseous discharge is separated into at least one phase which is unreacted in olefins and at least one phase which is rich in product aldehyde.
- the material separation can be carried out using known material separation processes, such as condensation, distillation, centrifugation, nanofiltration or a combination of several thereof, preferably condensation or distillation.
- material separation processes such as condensation, distillation, centrifugation, nanofiltration or a combination of several thereof, preferably condensation or distillation.
- the one formed during the first separation can be carried out using known material separation processes, such as condensation, distillation, centrifugation, nanofiltration or a combination of several thereof, preferably condensation or distillation.
- Product aldehyde-rich phase are fed to a second material separation, in particular a subsequent aldehyde separation, in which the product aldehyde is separated from the other substances in this phase, often alkanes and educt olefins.
- the unreacted olefin-rich phase can be returned to the hydroformylation step or, in the case of a multi-stage configuration, to one of the hydroformylation steps in order to hydroformylate the olefins contained therein to the product aldehyde.
- a purge gas stream which has a composition which is at least similar or identical to that of the unreacted olefin phase can also be removed during the material separation.
- the purge gas stream can also be passed to the second material separation or aldehyde separation in order to separate the product aldehydes contained therein and to remove impurities (e.g. nitrogen in the synthesis gas) or inert substances (e.g. alkanes in the feed mixture) from the system.
- impurities or inert substances can usually be removed in the second separation as volatile substances, for example at the top of a column.
- Another object of the present invention is also a plant with which the present method can be carried out and which in particular comprises a reactor in which the hydroformylation step according to the invention is carried out.
- the system can comprise a material separation unit with which the gaseous discharge of the
- Hydroformylation step is separated into at least one phase unreacted olefin and at least one phase rich in product aldehyde, this separation unit being arranged after the hydroformylation according to the invention.
- a second material separation unit in particular one, can be located downstream of the first material separation
- Aldehyde separation unit with which the product aldehyde is separated.
- Experiment 1 Production and Investigation of a Catalyst System According to the Invention
- a monolith made of silicon carbide with a length of approximately 20 cm and a diameter of approximately 25 mm was used as the starting material for the support.
- This monolith was crushed with a jaw crusher with a roller gap of 2 mm.
- the crushed support was then pretreated to a target grain of 2 to 3.15 mm with a washcoat (S1O2).
- S1O2 washcoat
- the granules produced in this way were then introduced into a 20 cm long round reactor sleeve with a diameter of one inch (approx. 2.54 cm), glass beads of a similar size being introduced above and below the granules.
- the granulate was then with a
- Catalyst solution containing Rh (acac) (CO) 2, bisphephos (ligand), bis (2,2,6,6-tetramethyl-4-piperidyl) sebacate (stabilizer) and dichloromethane as solvent and prepared by mixing in an inert environment ( Glovebox).
- Rh (acac) (CO) 2 bisphephos (ligand), bis (2,2,6,6-tetramethyl-4-piperidyl) sebacate (stabilizer) and dichloromethane
- Glovebox inert environment
- a hydrocarbon stream with the following composition was used as the feed mixture:
- the hydroformylation was carried out at a temperature of 120 ° C. and a pressure of 10 bar.
- the total conversion of butenes (ie the conversion of all butenes in the feed mixture) and the n / iso selectivity (ratio of linear to branched products) was determined by gas chromatography using the product composition.
- the catalyst system was prepared analogously to the preparation of the catalytically active composition Rh (II) in WO 2015/028284 A1.
- a hydrocarbon stream with the following composition was used as the feed mixture:
- the hydroformylation was carried out at a temperature of 120 ° C. and a pressure of 10 bar.
- the total conversion of butenes i.e. the conversion of all butenes in the feed mixture
- the n / iso selectivity ratio of linear to branched products
- the heterogeneous catalyst systems according to the invention have the advantage over the known SILP systems that higher conversions and higher linearity of the products (n / iso selectivity) can be achieved.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
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- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
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Abstract
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EP18198794 | 2018-10-05 | ||
PCT/EP2019/076413 WO2020070052A1 (fr) | 2018-10-05 | 2019-09-30 | Procédé d'hydroformylation d'oléfines à chaîne courte en phase gazeuse |
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EP19773873.5A Pending EP3860969A1 (fr) | 2018-10-05 | 2019-09-30 | Procédé d'hydroformylation d'oléfines à chaîne courte en phase gazeuse |
EP19200448.9A Active EP3632887B1 (fr) | 2018-10-05 | 2019-09-30 | Procédé de démarrage d'un réacteur d'hydroformylation |
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US (1) | US11384042B2 (fr) |
EP (2) | EP3860969A1 (fr) |
KR (1) | KR20210071041A (fr) |
CN (1) | CN112888671B (fr) |
SG (1) | SG11202103356UA (fr) |
WO (1) | WO2020070052A1 (fr) |
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EP4091712B1 (fr) | 2021-05-18 | 2024-05-15 | Evonik Oxeno GmbH & Co. KG | Procédé de régénération d'un catalyseur pour l'hydroformylation d'oléfines en phase gazeuse |
WO2024017514A1 (fr) | 2022-07-19 | 2024-01-25 | Evonik Oxeno Gmbh & Co. Kg | Procédé de préparation par hydroformylation d'oléfines à chaîne courte en phase gazeuse |
WO2024017513A1 (fr) | 2022-07-19 | 2024-01-25 | Evonik Oxeno Gmbh & Co. Kg | Procédé de préparation par hydroformylation d'oléfines à chaîne courte en phase gazeuse |
EP4389731A1 (fr) | 2022-12-19 | 2024-06-26 | Evonik Oxeno GmbH & Co. KG | Procede de conservation de l'activite lors de la suppression de l'hydroformylation |
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BE758802A (fr) * | 1969-11-14 | 1971-04-16 | Johnson Matthey & Cy Ltd | |
DE102013217166A1 (de) * | 2013-08-28 | 2015-03-05 | Evonik Industries Ag | Verfahren zur Hydroformylierung von ungesättigten Verbindungen durch SILP-Katalyse |
ES2934872T3 (es) | 2018-10-05 | 2023-02-27 | Evonik Operations Gmbh | Procedimiento para la hidroformilación de olefinas C2 a C5 sin separación de sustancias intermedia |
US10647650B2 (en) | 2018-10-05 | 2020-05-12 | Evonik Operations Gmbh | Process for hydroformylating short-chain olefins using a heterogenized catalyst system without ionic liquid |
US10654784B2 (en) | 2018-10-05 | 2020-05-19 | Evonik Operations Gmbh | Process for hydroformylating short-chain olefins in the gas phase |
EP3736258B8 (fr) | 2018-10-05 | 2023-12-06 | Evonik Oxeno GmbH & Co. KG | Procédé d'hydroformylation d'oléfines à chaîne courte dans les flux de gaz d'échappement riches en alcanes |
EP3744707B1 (fr) | 2018-10-05 | 2024-01-10 | Evonik Oxeno GmbH & Co. KG | Procédé d'hydroformylation d'oléfines à chaîne courte dans le flux de recyclage d'une phase liquide de l'hydroformylation |
EP3632888B1 (fr) | 2018-10-05 | 2021-04-14 | Evonik Operations GmbH | Procédé de fabrication sur place d'un système de catalyseur d'hydroformylation se trouvant hétérogénisé sur un support |
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- 2019-09-30 SG SG11202103356UA patent/SG11202103356UA/en unknown
- 2019-09-30 KR KR1020217013344A patent/KR20210071041A/ko unknown
- 2019-09-30 EP EP19773873.5A patent/EP3860969A1/fr active Pending
- 2019-09-30 WO PCT/EP2019/076413 patent/WO2020070052A1/fr active Application Filing
- 2019-09-30 US US17/282,393 patent/US11384042B2/en active Active
- 2019-09-30 CN CN201980065380.8A patent/CN112888671B/zh active Active
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WO2020070052A1 (fr) | 2020-04-09 |
EP3632887B1 (fr) | 2021-04-14 |
US11384042B2 (en) | 2022-07-12 |
CN112888671B (zh) | 2023-12-12 |
EP3632887A1 (fr) | 2020-04-08 |
US20210340091A1 (en) | 2021-11-04 |
KR20210071041A (ko) | 2021-06-15 |
SG11202103356UA (en) | 2021-05-28 |
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