TW202345967A - 反應器 - Google Patents
反應器 Download PDFInfo
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- TW202345967A TW202345967A TW112106208A TW112106208A TW202345967A TW 202345967 A TW202345967 A TW 202345967A TW 112106208 A TW112106208 A TW 112106208A TW 112106208 A TW112106208 A TW 112106208A TW 202345967 A TW202345967 A TW 202345967A
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- Prior art keywords
- catalyst bed
- primary
- reactor
- inlet end
- stream
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- 239000003054 catalyst Substances 0.000 claims abstract description 251
- 238000006243 chemical reaction Methods 0.000 claims abstract description 58
- 239000007788 liquid Substances 0.000 claims abstract description 51
- 239000012263 liquid product Substances 0.000 claims abstract description 29
- 238000000034 method Methods 0.000 claims abstract description 16
- 238000004064 recycling Methods 0.000 claims abstract description 6
- 239000000047 product Substances 0.000 claims description 41
- 238000005984 hydrogenation reaction Methods 0.000 claims description 23
- 238000011084 recovery Methods 0.000 claims description 19
- 238000000926 separation method Methods 0.000 claims description 13
- 239000012084 conversion product Substances 0.000 claims description 8
- 150000001298 alcohols Chemical class 0.000 claims description 7
- 150000001299 aldehydes Chemical class 0.000 claims description 7
- 230000001276 controlling effect Effects 0.000 claims description 7
- 150000001993 dienes Chemical class 0.000 claims description 6
- 150000001336 alkenes Chemical class 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 5
- 150000001345 alkine derivatives Chemical class 0.000 claims description 4
- 150000001491 aromatic compounds Chemical class 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 125000003118 aryl group Chemical group 0.000 claims description 2
- 239000011810 insulating material Substances 0.000 claims description 2
- 230000001105 regulatory effect Effects 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 55
- 239000002245 particle Substances 0.000 description 17
- 239000000376 reactant Substances 0.000 description 14
- 230000000052 comparative effect Effects 0.000 description 12
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 10
- 230000000694 effects Effects 0.000 description 10
- 229910052739 hydrogen Inorganic materials 0.000 description 10
- 239000001257 hydrogen Substances 0.000 description 10
- 239000011800 void material Substances 0.000 description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- ZTQSAGDEMFDKMZ-UHFFFAOYSA-N Butyraldehyde Chemical compound CCCC=O ZTQSAGDEMFDKMZ-UHFFFAOYSA-N 0.000 description 6
- 239000010949 copper Substances 0.000 description 5
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 4
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 4
- 229910052802 copper Inorganic materials 0.000 description 4
- 239000012467 final product Substances 0.000 description 4
- NUJGJRNETVAIRJ-UHFFFAOYSA-N octanal Chemical compound CCCCCCCC=O NUJGJRNETVAIRJ-UHFFFAOYSA-N 0.000 description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 229910052804 chromium Inorganic materials 0.000 description 3
- 239000011651 chromium Substances 0.000 description 3
- HGBOYTHUEUWSSQ-UHFFFAOYSA-N valeric aldehyde Natural products CCCCC=O HGBOYTHUEUWSSQ-UHFFFAOYSA-N 0.000 description 3
- KBPLFHHGFOOTCA-UHFFFAOYSA-N 1-Octanol Chemical compound CCCCCCCCO KBPLFHHGFOOTCA-UHFFFAOYSA-N 0.000 description 2
- YIWUKEYIRIRTPP-UHFFFAOYSA-N 2-ethylhexan-1-ol Chemical compound CCCCC(CC)CO YIWUKEYIRIRTPP-UHFFFAOYSA-N 0.000 description 2
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 125000001931 aliphatic group Chemical group 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
- 230000015572 biosynthetic process Effects 0.000 description 2
- WERYXYBDKMZEQL-UHFFFAOYSA-N butane-1,4-diol Chemical compound OCCCCO WERYXYBDKMZEQL-UHFFFAOYSA-N 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 229910052763 palladium Inorganic materials 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000011949 solid catalyst Substances 0.000 description 2
- UEUXEKPTXMALOB-UHFFFAOYSA-J tetrasodium;2-[2-[bis(carboxylatomethyl)amino]ethyl-(carboxylatomethyl)amino]acetate Chemical compound [Na+].[Na+].[Na+].[Na+].[O-]C(=O)CN(CC([O-])=O)CCN(CC([O-])=O)CC([O-])=O UEUXEKPTXMALOB-UHFFFAOYSA-J 0.000 description 2
- 238000009736 wetting Methods 0.000 description 2
- PYLMCYQHBRSDND-VURMDHGXSA-N (Z)-2-ethyl-2-hexenal Chemical compound CCC\C=C(\CC)C=O PYLMCYQHBRSDND-VURMDHGXSA-N 0.000 description 1
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 1
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 1
- MUXOBHXGJLMRAB-UHFFFAOYSA-N Dimethyl succinate Chemical compound COC(=O)CCC(=O)OC MUXOBHXGJLMRAB-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 238000006424 Flood reaction Methods 0.000 description 1
- XHCLAFWTIXFWPH-UHFFFAOYSA-N [O-2].[O-2].[O-2].[O-2].[O-2].[V+5].[V+5] Chemical compound [O-2].[O-2].[O-2].[O-2].[O-2].[V+5].[V+5] XHCLAFWTIXFWPH-UHFFFAOYSA-N 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000005056 compaction Methods 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- -1 extrudates Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000005498 polishing Methods 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 229910001935 vanadium oxide Inorganic materials 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 229910001928 zirconium oxide Inorganic materials 0.000 description 1
Classifications
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- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0461—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds
- B01J8/0465—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds the beds being concentric
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0053—Details of the reactor
- B01J19/006—Baffles
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/02—Feed or outlet devices; Feed or outlet control devices for feeding measured, i.e. prescribed quantities of reagents
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- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0492—Feeding reactive fluids
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- C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
- C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
- C07C29/14—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group
- C07C29/141—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group with hydrogen or hydrogen-containing gases
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
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- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
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- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
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- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/50—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids in the presence of hydrogen, hydrogen donors or hydrogen generating compounds
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- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/44—Hydrogenation of the aromatic hydrocarbons
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
- C10G49/002—Apparatus for fixed bed hydrotreatment processes
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- C—CHEMISTRY; METALLURGY
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- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
- C10G65/06—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a selective hydrogenation of the diolefins
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- C—CHEMISTRY; METALLURGY
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- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
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- C10G65/08—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a hydrogenation of the aromatic hydrocarbons
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- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
- B01J2208/023—Details
- B01J2208/024—Particulate material
- B01J2208/025—Two or more types of catalyst
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J2219/00049—Controlling or regulating processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00761—Details of the reactor
- B01J2219/00763—Baffles
- B01J2219/00765—Baffles attached to the reactor wall
- B01J2219/00768—Baffles attached to the reactor wall vertical
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- Engineering & Computer Science (AREA)
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- Water Supply & Treatment (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
本發明揭示一種液體/氣體反應器。該反應器包括:初級觸媒床,其具有入口端及出口端;用於向該初級觸媒床之該入口端供應初級進料流之構件,該初級進料流包括新鮮進料及回收之至少部分轉化液體產物;次級觸媒床,其具有入口端及出口端,該次級觸媒床實質上垂直延伸通過該初級觸媒床;用於向該次級觸媒床之該入口端供應次級進料流之構件,該次級進料流包括回收之至少部分轉化液體產物;用於自該初級觸媒床之該出口端收集至少部分轉化液體產物且將該至少部分轉化液體產物之至少一部分回收至該初級觸媒床及次級觸媒床之該入口端之構件;分離壁,其位於該初級觸媒床與次級觸媒床之間;用於僅向該初級觸媒床之該入口端供應初級氣流之構件;及用於僅向該次級觸媒床之該入口端供應次級氣流之構件。本發明亦揭示一種使用該反應器進行氣體/液體反應之程序。
Description
本發明係關於一種液體/氣體反應器及一種使用該反應器進行氣體/液體反應之程序。特定而言,本發明係關於一種用於進行液體回收程序之液體/氣體反應器,包括初級及次級觸媒床。
液體與氣體之間的化學反應通常在固體觸媒床上進行。反應可為放熱的(即,產生熱),或其可為吸熱的(即,利用熱且引起周圍大氣冷卻)。在一些反應中,反應之熱效應係溫和的;然而,即使在此等中,若不控制溫度,則可導致選擇性損失。針對劇烈放熱或吸熱反應,需要更嚴格控制熱效應。在極端情況中,由強放熱反應產生之熱可導致熱失控。類似地,強吸熱反應之冷卻效應可導致反應淬火。
控制其中發生放熱或吸熱反應之液體/氣體反應器中之溫度之常用方法係將經加熱或冷卻產物回收至反應器中。此回收藉由稀釋反應物且允許轉化率每通過一次就降低來產生限制升溫之效應。此等所謂之「液體回收」反應器已廣泛商用,例如在苯之氫化、用於移除炔及/或二烯之烯烴之選擇性氫化及醛至醇之氫化中。
圖1中繪示用於選擇性氫化C
2及C
3流中之烯烴及二烯之典型反應器示意圖。氫化單元包括主反應器1及精加工反應器2。C
3原料用管線3供應至主反應器1,其中C
3原料與已用管線4供應之氫氣通過觸媒反應。產物在用管線7傳遞至液體/氣體分離器8之前用管線5提取且在冷卻器6中冷卻。一定比例之液體用管線9移除且回收至主反應器1。在所繪示之配置中,回收流9在供應至主反應器1之前與原料流3組合。來自分離器之多餘氣體用管線10移除。
來自氣體/液體分離器之剩餘液體用管線11移除且進給至精加工反應器2。此反應器係塞流反應器。產物用管線12移除。應理解,液體回收反應器係部分返混的,因為進料用回收之產物流稀釋。
在將100%烯烴氫化為烷烴或將醛氫化為醇之情況中,需要10倍至20倍進給率之典型回收率來避免跨反應器之升溫超過20°C。回收產物顯著稀釋反應物且因此反應速率降低且反應熱至少部分由回收產物吸收,兩者有助於減少跨反應器升溫。
需要精加工反應器2 (其亦可稱為拋光反應器)來製造具有低含量之未反應進料組分之高品質產物。為使液體速度適合於良好分佈,精加工級之橫截面積必須比液體回收反應器小得多且因此為達到足夠觸媒體積,必須使用長精加工反應器。
圖2中繪示由本發明之發明者開發且在EP2516050B1中揭示之另一類型之液體回收反應器。EP2516050B1中所揭示之反應器係填充床液體/氣體反應器21之修改,其藉由提供延伸通過主體(或初級)觸媒床22之次要(或次級)觸媒床23來提高觸媒之效力且無需精加工反應器。單獨進料流24、25經提供至初級及次級觸媒床22、23,且新鮮進料26及回收產物27之混合物經供應至初級床22,同時僅回收產物27經供應至次級床23,從而允許達成提高總轉化率。氣流28透過反應器頂部處之共用蒸汽空間供應至初級及次級觸媒床兩者。
隨著液體及氣體反應物通過觸媒床,壓力將自觸媒床之入口端(反應物在其中進入)處之最大壓力下降至出口端(產物及多餘反應物在其中離開)處之最小壓力。本發明之發明者驚訝地發現,使用EP2516050B1反應器之初級/次級觸媒床配置,通過初級及次級觸媒床之壓力降理論上需要相等以達成最佳總轉化率。壓力降可藉由厄貢(Ergun)方程式計算且取決於諸如各觸媒床之粒徑、床空隙率及液體流量之因數。吾人發現,透過兩個觸媒床一直達成相等壓力降實際上出奇地難。例如,各床中觸媒之粒徑可在自不同批次裝載時不同,或各床中之空隙率可歸因於觸媒裝載或觸媒在裝載之後沉降之差異而不同。
因此,本發明旨在解決與先前技術之液體/氣體反應器相關聯之一或多個問題且提供能夠達成一致及提高轉化率之液體/氣體反應器。
根據本發明之第一態樣,提供一種氣體/液體反應器,其包括:
(a)初級觸媒床,其具有入口端及出口端;
(b)用於向初級觸媒床之入口端供應初級進料流之構件,初級進料流包括新鮮進料及回收之至少部分轉化液體產物;
(c)次級觸媒床,其具有入口端及出口端,次級觸媒床實質上垂直延伸通過初級觸媒床;
(d)用於向次級觸媒床之入口端供應次級進料流之構件,次級進料流包括回收之至少部分轉化液體產物;
(e)用於自初級觸媒床之出口端收集至少部分轉化液體產物且將至少部分轉化液體產物之至少一部分回收至初級觸媒床及次級觸媒床之入口端之構件;
(f)分離壁,其位於初級觸媒床與次級觸媒床之間;
(g)用於僅向初級觸媒床之入口端供應初級氣流之構件;及
(h)用於僅向次級觸媒床之入口端供應次級氣流之構件。
藉由提供用於向初級及次級觸媒床供應單獨氣流,至初級及次級觸媒床之氣流動彼此獨立且可視情況經個別控制。發明者驚訝地發現,此允許減輕跨觸媒床之不相等壓力降效應以導致更一致且提高之總轉化率。
因此,在一些實施例中,反應器包括用於個別控制初級氣流之流速及次級氣流之流速之構件。氣流之流速可由諸如流量控制閥之任何適合構件控制。在一個配置中,初級及次級氣流可以經個別控制流速自單獨源供應至反應器。替代地,初級及次級氣流可透過經分支以提供單獨初級及次級氣流之導管自單一源供應。在此等實施例中,流量控制閥可設置於各分支上以個別控制初級及次級氣流之流速。
氣體流速應足以跨兩個觸媒床之整個區域使液體進料保持充滿氣體反應物。例如,飽和度可藉由形成過量氣體反應物之氣泡來判定。替代地或另外,可分析排氣流中之氫氣含量;若氫氣含量足夠高,則可推斷液體進料充滿氣體反應物。若判定任一床未充滿氣體反應物,則可提高氣體至床之流速。
次級觸媒床僅被供應已經受反應且因此至少部分轉化之進料。因此,離開次級觸媒床之產物流將提供比不具有次級觸媒床之反應器更完全轉化之最終產物。
次級觸媒床可安置於初級觸媒床中之任何適合位置中,但應理解,次級觸媒床垂直延伸通過初級觸媒床,使得次級觸媒床之入口及出口端不被初級觸媒床阻擋。在一些實施例中,次級觸媒床位於初級觸媒床之中心,使得初級觸媒床圍繞次級觸媒床形成環形。替代地,次級觸媒床可偏移至初級觸媒床之側或緊靠反應器之壁定位。
反應器係液體/氣體反應器,因為通過反應器之流體呈液相及氣相兩者。流體通過反應器中之固體(即,多相)觸媒。
反應器及其組件可由任何適合材料構造。在一些實施例中,分離壁由絕緣材料形成。此可在初級及次級觸媒床以不同溫度操作時特別有用。
分離壁可具有任何適合結構。例如,分離壁可由次級觸媒床定位於其中之內管形成。分離壁可具有任何適合橫截面形狀,諸如圓形。替代地,例如,分離壁可由緊固至反應器之壁之半管形成。
在一些實施例中,次級觸媒床包括用於將次級觸媒床之入口端與初級觸媒床之入口端隔離之蓋,且次級氣體及進料流供應至蓋內之次級觸媒床之入口端。應理解,蓋界定次級觸媒床之入口端上方之封閉腔,次級氣體及進料流供應至封閉腔中。因而,蓋可呈凸曲板或圓頂之形式或可包括側壁及頂部或單一連續側壁及頂部。在一些實施例中,蓋至少部分包括初級及次級觸媒床上方之分離壁之延伸部,使得分離壁之延伸部形成蓋之(若干)側壁。
在一些實施例中,蓋包括可移除帽。提供可移除帽允許根據需要方便地接取次級觸媒床,例如更換觸媒。在一些實施例中,蓋進一步包括用於與可移除帽形成氣密密封之墊片。
反應器可包括用於自次級觸媒床之出口端收集產物流之構件。在一些實施例中,用於自次級觸媒床之出口端收集產物流之構件包含用於將產物流自次級觸媒床轉移至反應器之接收部分之導管,接收部分至少在液體流方面與初級觸媒床之出口端隔離。接收部分可為容器或反應器之部分,其適合於接收自次級觸媒床離開之產物流且使其與自初級觸媒床離開之產物流保持分離。例如,接收部分可包括偏移至反應器之底部之一側之擋板,其充當被來自次級觸媒床之產物淹沒之堰。替代地,擋板可與導管通過之頂部組合以產生用於自該次級觸媒床接收產物之封閉容器;在此情況中,可平衡擋板之兩側之間的蒸汽壓力且使產物自次級觸媒床溢出至初級觸媒床之出口端。
在一些實施例中,回收來自初級觸媒床之出口端之所有至少部分轉化產物,其中一部分回收至初級觸媒床之入口端且一部分回收至次級觸媒床之入口端。
在一些實施例中,反應器包括用於調節回收產物流之溫度之構件,例如加熱器及/或冷卻器。
在一些實施例中,反應器包括用於個別控制初級進料流之流速及次級進料流之流速之構件。例如,初級進料流及次級進料流可各由其各自管線上之流量控制閥控制。供應至次級觸媒床之次級進料流之流速可等於最終產物速率。然而,為方便控制,較佳地供應高達100%之餘物。例如,餘物可與來自初級觸媒床之回收流組合。在尤佳實施例中,餘物淹沒堰且因此與來自初級反應器床之輸出組合。較佳地,接著控制最終產物速率以藉由使餘物溢過堰來維持堰之初級觸媒床側上之所要液位。
進料流比可界定為次級進料流流速與初級進料流流速之比率。類似地,床橫截面積比可界定為次級觸媒床橫截面積與初級觸媒床橫截面積之比率。
一般而言,床橫截面積比將經選擇以保持所需蒸汽/液體混合且達成觸媒之所需潤濕。床橫截面積比可為進料流比之0.1倍至5倍、0.2倍至3倍或0.5倍至2倍。在一些實施例中,床橫截面積比係1:1。此可允許次級觸媒床維持液體速度,其給出良好蒸汽/液體混合及良好潤濕,一般將具有與在初級觸媒床中達成之位準相同之位準。
回收率可經控制以旨在使跨初級觸媒床之升溫不超過10°C至15°C。達成此所需之準確回收率將取決於由反應產生之熱,其繼而取決於所使用之反應物。例如,較輕醇可比較重醇產生更多反應熱且因此需要更高回收率來提高稀釋率。一般而言,供應至初級觸媒床之回收流與新鮮進料之比率可為自1至100、自5至50、自10至40、自15至35或自20至30。例如,針對諸如丁醛氫化之反應,自20至30之比率可為尤佳的。針對辛醛氫化,可使用較低比率,此既是因為反應熱較低,又是因為較重醇對溫度更不敏感且因此可容忍較高升溫。例如,可使用自1至10之比率。供應至次級觸媒床之回收產物與供應至初級觸媒床之新鮮進料之比率可為自1至2。供應至次級觸媒床之回收產物與最終產物速率之比率較佳地大於1,例如自1至2。
任何適合觸媒可用於初級及次級觸媒床中。一般而言,觸媒之選擇將取決於待進行之反應,但可包含鎳、銅、鉻、鈀或其等之任何混合物。例如,觸媒亦可具有任何適合形式,諸如顆粒、擠出物、樹脂或浸漬填料。例如,適合觸媒載體可包含氧化鋁、二氧化矽、氧化釩、氧化鋯或碳。用於初級及次級觸媒床中之觸媒可相同或不同。
反應器可適用於可在固體觸媒床上進行之任何放熱或吸熱反應。放熱反應之實例包含醛、酮、炔、二烯或芳香族化合物之氫化及氧化反應。吸熱反應之實例包含脫氫反應。特定而言,本發明之反應器可適合於液相氫化反應(即,液體反應物與氫氣之氫化),例如丁二烯選擇性氫化為丁烯、由苯產生環己烷、丁醛氫化為丁醇或辛醛氫化為辛醇、丁二酸二甲酯氫化為1,4-丁二醇或由2-乙基-2-己烯醛產生2-乙基己醇。
根據本發明之第二實施例,提供一種使用第一態樣之反應器進行氣體/液體反應之程序。程序包括以下步驟:
(a)向反應器之初級觸媒床之入口端供應初級進料流,初級進料流包括新鮮進料及回收之至少部分轉化液體產物;
(b)向初級觸媒床之入口端供應初級氣流;
(c)允許在初級觸媒床中發生反應;
(d)自初級觸媒床之出口端收集至少部分轉化液體產物流;
(e)將至少部分轉化液體產物流之至少一部分回收至初級觸媒床之入口端;
(f)將至少部分轉化液體產物流之至少一部分回收至反應器之次級觸媒床之入口端;
(g)向次級觸媒床之入口端供應次級氣流;
(h)允許在次級觸媒床中發生反應;及
(i)自次級觸媒床收集產物流,與來自初級觸媒床之出口端之至少部分轉化液體產物流分離。
應理解,初級觸媒床中之反應發生於初級氣流與初級進料流之間,而次級觸媒床中之反應發生於次級氣流與次級進料流之間。
在一些實施例中,回收來自初級觸媒床之所有至少部分轉化液體產物。替代地,可自反應器收集及收回至少部分轉化液體產物之一部分。
在一些實施例中,程序包括使至少部分轉化液體產物流在回收至初級及/或次級觸媒床之前加熱或冷卻之額外步驟。應理解,加熱或冷卻至少部分轉化液體產物流之步驟發生於程序之步驟(d)與(e)/(f)之間。
在一些實施例中,程序涉及個別控制初級氣流及次級氣流之流速。初級及次級氣流之流速可由任何適合構件(例如各自管線上之單獨流量控制閥)控制。
程序可用於進行任何適合反應。在一些實施例中,反應係將醛氫化為醇。替代地,反應可為將二烯或炔選擇性氫化為烯烴。在其他實施例中,反應係使芳香族化合物中之芳香環氫化。
用於程序中之觸媒及反應條件將取決於所進行之反應。例如,當反應係醛之氫化時,可使用銅/碳或銅/鉻觸媒且反應可以自約140°C至約200°C之溫度及高於環境壓力至少1 MPa之壓力進行。針對二烯之選擇性氫化,可使用鈀或氧化鋁觸媒且反應可以自約20°C至約130°C之溫度及高於環境壓力約0.5 MPa至約2 MPa之壓力進行。
圖3中示意性繪示根據本發明之第一態樣之實施例之液體/氣體反應器。反應器31包括藉由分離壁43彼此分離之初級觸媒床32及次級觸媒床33。次級觸媒床33位於中心,使得初級觸媒床32圍繞次級觸媒床33形成環形。氣體經由管線34供應至反應器,管線34經分支以將初級氣流34a提供至初級觸媒床32且將單獨次級氣流34b提供至次級觸媒床33。各分支34a、34b可具有用於個別控制氣體至初級及次級觸媒床32、33之流速之各自構件(未展示)。
新鮮進料經由管線35供應且與回收產物流36之一部分52混合以提供初級進料流41。初級進料流41經供應至初級觸媒床32,其中在初級進料流41與初級氣流34a之間發生反應。回收產物流36之另一部分經提供至次級進料流42。次級進料流42經供應至次級觸媒床33,其中在次級進料流42與次級氣流34b之間發生另外反應。
廢氣經由管線37自反應器31之底部移除。來自初級觸媒床32之至少部分轉化產物經由管線38使用泵39收回。在經由管線36回收至初級及次級進料流41、42之前,至少部分轉化產物流之溫度由加熱器/冷卻器40調節。來自次級觸媒床33之更完全轉化產物經由管線44收集。
初級及次級觸媒床32、33具有反應物在其中進入之入口端(大體上以45展示)及產物及過量反應物在其中離開之出口端(大體上以46展示)。次級觸媒床33包括蓋47 (在圖5中更詳細展示)以將次級觸媒床33之入口端與初級觸媒床32之入口端隔離。次級進料流42及次級氣流34b經供應至由蓋47界定之腔內之次級觸媒床33以允許單獨流速之氣體供應至初級及次級觸媒床32、33。在不希望受理論限制之情況下,可認為個別控制氣體至初級及次級觸媒床之流速允許減輕通過初級及次級觸媒床之不同壓力降效應以確保一致反應速率且因此確保一致且提高之總轉化率,與任何壓力降差無關。
本發明之反應器可用於經由Cu/Cr或Cu/C觸媒將脂肪族C
2-C
20醛氫化為對應醇。針對此反應,一般在兩個觸媒床中使用相同觸媒。基於進料,停留時間將為約0.1小時至約10小時。觸媒床之溫度將在約100°C至約200°C之範圍內且絕對壓力將為約0.1 MPa至約5 MPa。替代地,反應可經由鎳觸媒進行,在此情況中,基於進料,停留時間將為約0.1小時至約10小時。反應將以自約70°C至約150°C之溫度及自約0.1 MPa至約5 MPa之絕對壓力進行。
據信至少部分轉化產物流之回收有利地限制跨反應器之升溫。可藉由限制升溫來限制出口溫度。此具有限制或避免副產物形成之益處且可提供改良選擇性。另外,避免低入口溫度。此係有益的,因為在反應可開始之前,低入口溫度將需要反應器入口中之大感應區。然而,回收率較佳地不大於所需,因為此用產物過度稀釋反應物且降低觸媒之效力。
不論使用哪種觸媒系統,回收率將較佳地在新鮮進料速率之約1倍至約50倍之間。觸媒床可經設定大小使得液體表觀速度在約0.2 cm/s至約20 cm/s之範圍內。氫氣一般將以約等於或高達約兩倍化學計量要求之數量進給。由於脂肪族C
2-C
20醛之氫化係放熱反應,所以冷卻器40將用於自回收產物流移除反應之熱。
圖4中示意性繪示本發明之另一實施例。圖4中所展示之反應器很大程度上相同於圖3中所展示之反應器,其中新增導管48用於將產物自次級觸媒床33之出口端導引至由擋板49形成之堰,擋板49偏移至反應器31之底部之一側。堰被來自次級觸媒床33之產物淹沒,使得任何溢流與來自初級觸媒床32之部分轉化產物混合且經由管線38回收。堰被來自次級觸媒床33之產物淹沒可防止來自初級觸媒床32之產物進入。堰上可存在頂部,使得來自初級觸媒床32之部分轉化產物由頂部偏轉且不進入經由管線44回收之產物。來自堰之產物經由管線44回收。
圖5中展示反應器31之頂部之更詳細近視圖。次級觸媒床33包括蓋47,其包括由分離壁43之延伸部形成之連續側壁50。蓋47進一步包括可移除帽51,其允許根據需要接取次級觸媒床33,諸如更換觸媒。蓋47亦包括用於在側壁50與帽51之間形成氣密密封之墊片52。蓋界定次級觸媒床33之入口端上方之腔,次級氣流34b及次級進料流42經供應至腔中。此使次級氣流34b與供應至初級觸媒床32之入口端之初級氣流34a保持分離,且允許個別控制初級及次級氣流34a、34b之流速。
實例 不同壓力降對反應器效能之 效應
用導致不同壓力降之不同次級觸媒床條件調查圖2中所展示之反應器之效能。反應器用於將丁醛氫化為丁醇。
初級及次級觸媒床各具有10,000 mm之相同床長度。初級觸媒床具有1000 mm之直徑。反應器之頂部處之壓力係3 Mpa,而反應器之底部處之壓力很大程度上依據通過初級觸媒床之壓力降而變化,壓力降由厄貢方程式計算。假定恆溫設定為150°C。在不同床條件(實例1至3)下量測氫氣通過次級觸媒床之流速。
比較實例 1
比較實例1係參考實例。次級觸媒床之粒徑及填料相同於初級觸媒床以導致通過初級及次級觸媒床之相同壓力降。粒子之液壓直徑係1.6755 mm且空隙率係0.38。
比較實例 2
比較實例2用於量測在使空隙率保持相同時改變次級觸媒床之粒徑之效應。次級催化床之粒徑(1.4904 mm)小於初級催化床之粒徑(1.6755 mm)。兩個床之空隙率相同於比較實例1 (即,0.38)。例如,更小粒子可由在將觸媒裝載至反應器中期間粒子之非所要磨損導致。觸媒粒子之各裝載將略有不同,且因此非所要磨損程度可因裝載而不同。
比較實例 3
比較實例3用於量測在使粒徑保持相同時改變次級觸媒床之空隙率之效應。次級觸媒床具有大於初級觸媒床之空隙率(0.38)之空隙率(0.40)。兩個床之粒徑相同於比較實例1 (即,1.6755 mm)。例如,當觸媒粒子裝載至反應器中時,不同空隙率可因觸媒粒子之不同緊實度而發生。觸媒粒子之各裝載將略有不同,且因此緊實度可因裝載而更改。
表1展示在比較實例1至3之各者中透過次級觸媒床達成之流速。
表 1
次級觸媒床中之條件 | 比較實例1 | 比較實例2 | 比較實例3 | |||
氣體 | 液體 | 氣體 | 液體 | 氣體 | 液體 | |
液壓粒徑(mm) | 1.6755 | 1.4903 | 1.6755 | |||
床空隙率 | 0.38 | 0.38 | 0.40 | |||
流速(kg/h) | 100 | 40,000 | 81 | 40,000 | 122 | 40,000 |
在比較實例2中,氫氣通過次級觸媒床之流量減少,其可導致反應速率降低以導致轉化率降低、次級觸媒之使用效力降低及反應器效能降低。
在比較實例3中,氫氣通過次級觸媒床之流量增加,其可導致較差選擇性、停留時間減少及/或轉化率降低。其亦可提供氫氣繞過初級觸媒床之路線且導致更少氫氣流少通過初級觸媒床以導致初級反應器床之轉化率降低及反應器效能降低。
提供單獨初級及次級氣流之效應
與上述實例相比,在根據本發明之反應器中,如圖3中所展示,通過初級及次級之壓力降可經獨立控制。此外,初級及次級觸媒床各具有10,000 mm之相同床長度。初級觸媒床具有1000 mm之直徑。初級觸媒床之頂部處之壓力係3 Mpa,而反應器之底部處之壓力很大程度上依據通過初級觸媒床之壓力降而變化,壓力降由厄貢方程式計算。次級觸媒床之頂部處之壓力經控制以保持通過次級觸媒床之恆定流速。假定恆溫設定為150°C。
實例 4
實例4係比較實例1之重複,但其中圖3中所展示之反應器及次級觸媒床之頂部處之壓力經控制以保持通過次級觸媒床之恆定流速。
實例 5
實例5係比較實例2之重複,但其中圖3中所展示之反應器及次級觸媒床之頂部處之壓力經控制以保持通過次級觸媒床之恆定流速。
實例 6
實例6係比較實例3之重複,但其中圖3中所展示之反應器及次級觸媒床之頂部處之壓力經控制以保持通過次級觸媒床之恆定流速。
表2展示在實例4至6之各者中透過次級觸媒床達成之流速。
表 2
次級觸媒床中之條件 | 實例4 | 實例5 | 實例6 | |||
氣體 | 液體 | 氣體 | 液體 | 氣體 | 液體 | |
液壓粒徑(mm) | 1.6755 | 1.4903 | 1.6755 | |||
床空隙率 | 0.38 | 0.38 | 0.40 | |||
流速(kg/h) | 100 | 40,000 | 100 | 40,000 | 100 | 40,000 |
因為本發明允許獨立控制次級觸媒床之頂部處之壓力以保持通過次級觸媒床之恆定流速,所以不會發生與比較實例相關之上述問題且在所有實例中維持最佳反應器效能。
1:主反應器
2:精加工反應器
3:管線
4:管線
5:管線
6:冷卻器
7:管線
8:液體/氣體分離器
9:管線
10:管線
11:管線
12:管線
21:填充床液體/氣體反應器
22:初級觸媒床
23:次級觸媒床
24:進料流
25:進料流
26:新鮮進料
27:回收產物
28:氣流
31:反應器
32:初級觸媒床
33:次級觸媒床
34:管線
34a:初級氣流/分支
34b:次級氣流/分支
35:管線
36:回收產物流/管線
37:管線
38:管線
39:泵
40:加熱器/冷卻器
41:初級進料流
42:次級進料流
43:分離壁
44:管線
45:入口端
46:出口端
47:蓋
48:導管
49:擋板
50:側壁
51:帽
52:部分/墊片
圖1展示自先前技術知悉之液體/氣體反應器之實例;
圖2展示自先前技術知悉之液體/氣體反應器之另一實例;
圖3展示根據本發明之實施例之液體/氣體反應器;
圖4展示根據本發明之另一實施例之液體/氣體反應器;及
圖5展示根據本發明之實施例之液體/氣體反應器之近視圖。
31:反應器
32:初級觸媒床
33:次級觸媒床
34:管線
34a:初級氣流/分支
34b:次級氣流/分支
35:管線
36:回收產物流/管線
37:管線
38:管線
39:泵
40:加熱器/冷卻器
41:初級進料流
42:次級進料流
43:分離壁
44:管線
45:入口端
46:出口端
47:蓋
52:部分
Claims (20)
- 一種液體/氣體反應器,其包括: (a)初級觸媒床,其具有入口端及出口端; (b)用於向該初級觸媒床之該入口端供應初級進料流之構件,該初級進料流包括新鮮進料及回收之至少部分轉化液體產物; (c)次級觸媒床,其具有入口端及出口端,該次級觸媒床實質上垂直延伸通過該初級觸媒床; (d)用於向該次級觸媒床之該入口端供應次級進料流之構件,該次級進料流包括回收之至少部分轉化液體產物; (e)用於自該初級觸媒床之該出口端收集至少部分轉化液體產物且將該至少部分轉化液體產物之至少一部分回收至該初級觸媒床及次級觸媒床之該入口端之構件; (f)分離壁,其位於該初級觸媒床與次級觸媒床之間; (g)用於僅向該初級觸媒床之該入口端供應初級氣流之構件;及 (h)用於僅向該次級觸媒床之該入口端供應次級氣流之構件。
- 如請求項1之反應器,其進一步包括用於個別控制該初級氣流之流速及該次級氣流之流速之構件。
- 如請求項1或請求項2之反應器,其中該次級觸媒床位於該初級觸媒床之中心,使得該初級觸媒床圍繞該次級觸媒床形成環形。
- 如前述請求項中任一項之反應器,其中該分離壁由絕緣材料製成。
- 如前述請求項中任一項之反應器,其中該次級觸媒床包括用於將該次級觸媒床之該入口端與該初級觸媒床之該入口端隔離之蓋,且其中該次級氣流及該次級進料流供應至該蓋內之該次級觸媒床之該入口端。
- 如請求項5之反應器,其中該蓋包括該初級及次級觸媒床上方之該分離壁之延伸部。
- 如請求項5或請求項6之反應器,其中該蓋包括可移除帽。
- 如請求項7之反應器,其中該蓋進一步包括用於與該可移除帽形成氣密密封之墊片。
- 如前述請求項中任一項之反應器,其進一步包括用於自該次級觸媒床之該出口端收集產物流之構件。
- 如請求項9之反應器,其中用於自該次級觸媒床之該出口端收集產物流之該構件包含用於將該產物流自該次級觸媒床轉移至該反應器之接收部分之導管,該接收部分與該初級觸媒床之該出口端隔離。
- 如前述請求項中任一項之反應器,其中回收來自該初級觸媒床之該出口端之所有該至少部分轉化產物,其中一部分回收至該初級觸媒床之該入口端且一部分回收至該次級觸媒床之入口端。
- 如前述請求項中任一項之反應器,其進一步包括用於調節至少部分轉化液體產物之該回收流之溫度之構件。
- 如前述請求項中任一項之反應器,其進一步包括用於個別控制該初級進料流之該流速及該次級進料流之該流速之構件。
- 如前述請求項中任一項之反應器,其中進料流比係次級進料流流速與初級進料流流速之比率,其中床橫截面積比係次級觸媒床橫截面積與初級觸媒床橫截面積之比率,且其中該床橫截面積比係該進料流比之0.5倍至2倍。
- 如請求項14之反應器,其中該床橫截面積比係1:1。
- 一種使用如請求項1至15中任一項之反應器進行氣體/液體反應之程序,該程序包括以下步驟: (a)向該反應器之該初級觸媒床之該入口端供應初級進料流,該初級進料流包括新鮮進料及回收之至少部分轉化液體產物; (b)向該初級觸媒床之該入口端供應初級氣流; (c)允許在該初級觸媒床中發生反應; (d)自該初級觸媒床之該出口端收集至少部分轉化液體產物流; (e)將該至少部分轉化液體產物流之至少一部分回收至該初級進料流; (f)將該至少部分轉化液體產物流之至少一部分回收至該反應器之該次級觸媒床之該入口端; (g)向該次級觸媒床之該入口端供應次級氣流; (h)允許在該次級觸媒床中發生反應; (i)自該次級觸媒床收集該產物流,與來自該初級觸媒床之該出口端之該至少部分轉化液體產物流分離。
- 如請求項16之程序,其中回收來自該初級觸媒床之所有該至少部分轉化液體產物。
- 如請求項16或請求項17之程序,其包括在回收之前加熱或冷卻該至少部分轉化液體產物流之額外步驟。
- 如請求項16至18中任一項之程序,其中個別控制該初級氣流之流速及該次級氣流之流速。
- 如請求項16至19中任一項之程序,其中該反應係將醛氫化為醇、將二烯或炔選擇性氫化為烯烴或使芳香族化合物中之芳香環氫化。
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GBGB2202363.4A GB202202363D0 (en) | 2022-02-22 | 2022-02-22 | Reactor |
GB2202363.4 | 2022-02-22 |
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TW112106208A TW202345967A (zh) | 2022-02-22 | 2023-02-21 | 反應器 |
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GB (2) | GB202202363D0 (zh) |
TW (1) | TW202345967A (zh) |
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GB202404300D0 (en) | 2024-03-26 | 2024-05-08 | Johnson Matthey Davy Technologies Ltd | Process for the production of 2-alkylalkanol |
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DK165946C (da) * | 1985-03-21 | 1993-07-05 | Haldor Topsoe As | Reformingproces under varmeudveksling og reaktor dertil |
US6793698B1 (en) * | 2001-03-09 | 2004-09-21 | Uop Llc | Fuel processor reactor with integrated pre-reforming zone |
EP2085354B1 (en) * | 2006-09-05 | 2019-02-20 | Panasonic Corporation | Hydrogen generating apparatus and fuel cell system |
JP4740277B2 (ja) * | 2008-03-18 | 2011-08-03 | アイシン精機株式会社 | 改質装置 |
GB201102551D0 (en) | 2011-02-14 | 2011-03-30 | Davy Process Techn Ltd | Reactor |
US8609912B2 (en) * | 2011-02-16 | 2013-12-17 | Exxonmobil Research And Engineering Company | Processing of feedstocks in separated reactor volumes |
GB201813431D0 (en) * | 2018-08-17 | 2018-10-03 | Weedon Geoffrey Gerald | Process & apparatus for steam reforming |
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WO2023161612A1 (en) | 2023-08-31 |
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