US20040067174A1 - Reactor for chemical conversion of a feedstock with heat inputs and feedstock/catalyst cross-circulation - Google Patents
Reactor for chemical conversion of a feedstock with heat inputs and feedstock/catalyst cross-circulation Download PDFInfo
- Publication number
- US20040067174A1 US20040067174A1 US10/432,773 US43277303A US2004067174A1 US 20040067174 A1 US20040067174 A1 US 20040067174A1 US 43277303 A US43277303 A US 43277303A US 2004067174 A1 US2004067174 A1 US 2004067174A1
- Authority
- US
- United States
- Prior art keywords
- feed
- reactor
- catalyst
- extraction
- catalytic
- 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.)
- Abandoned
Links
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 34
- 239000003054 catalyst Substances 0.000 title claims abstract description 32
- 239000000126 substance Substances 0.000 title claims abstract description 13
- 230000003197 catalytic effect Effects 0.000 claims abstract description 38
- 238000000605 extraction Methods 0.000 claims abstract description 21
- 238000010438 heat treatment Methods 0.000 claims abstract description 11
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 7
- 239000011949 solid catalyst Substances 0.000 claims abstract description 3
- 238000000034 method Methods 0.000 claims description 13
- 239000004215 Carbon black (E152) Substances 0.000 claims description 9
- 229930195733 hydrocarbon Natural products 0.000 claims description 9
- 150000002430 hydrocarbons Chemical class 0.000 claims description 9
- 238000006356 dehydrogenation reaction Methods 0.000 claims description 4
- 239000007789 gas Substances 0.000 description 7
- 239000012530 fluid Substances 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000003085 diluting agent Substances 0.000 description 2
- 239000013529 heat transfer fluid Substances 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- 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
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000004996 alkyl benzenes Chemical class 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000006057 reforming reaction Methods 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
Images
Classifications
-
- 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
- B01J8/0496—Heating or cooling the reactor
-
- 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
- B01J8/0403—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 fluid flow within the beds being predominantly horizontal
- B01J8/0423—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 fluid flow within the beds being predominantly horizontal through two or more otherwise shaped beds
- B01J8/0438—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 fluid flow within the beds being predominantly horizontal through two or more otherwise shaped beds the beds being placed next to each other
-
- 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
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
Definitions
- One method for obtaining a high conversion consists of introducing heating surfaces into the catalytic bed, or using a plurality of catalytic beds separated by zones for re-heating the reaction fluid.
- the catalyst is at least partially deactivated during the reaction, for example by coking, and must be extracted, continuously or at distinct time intervals, and replaced by new or regenerated catalyst.
- Processes such as catalytic hydrocarbon reforming are known in which the reaction feed successively traverses a plurality of catalytic bed reactors, with intermediate re-heating between the reactors to compensate for cooling of the reaction fluid due to the endothermic nature of the reaction.
- the catalyst moves from one reactor to another, as a co-current or as a counter-current to the feed before being regenerated and recycled.
- the catalyst is used efficiently and homogeneously coked before being regenerated.
- a first aim of the invention is to provide a reactor for carrying out a chemical conversion process in catalytic beds with means for supplying heat integrated into said reactor, and thus with a very compact reaction zone, combined with efficient use of the catalyst.
- a further aim of the invention is to provide a process for converting a feed (usually a hydrocarbon feed) undergoing an endothermic reaction using said reactor.
- the scope of the present invention also encompasses using a series of reactors at least one of which is in accordance with the present invention.
- the invention concerns a reactor for chemical conversion of a feed, said chemical conversion reactor containing a substantially vertical catalytic bed between an upper end and a lower end, and comprising in combination:
- said reactor comprises, close to its lower end, at least one means for extraction of the catalyst, which extraction is differentiated between an upstream portion and a downstream portion of said catalytic bed, with respect to the direction of flow of said feed.
- the reactor can be a reactor-exchanger with heating surfaces immersed in the catalytic bed; it can also comprise a plurality of catalytic beds separated by non-catalytic zones for heating the reaction feed. In each of these zones, the reaction feed traverses a heat exchanger, supplied with a heat transfer fluid.
- Heat transfer fluids that can be used include pressurised steam, for example between 0.5 MPa and 1.20 MPa, preferably between 0.6 MP and 1 MPa absolute, limits included, hydrogen or a hydrogen-containing gas such as a hydrogen-rich recycle gas, such as that used in certain processes to dilute the reaction feed to protect the catalyst. It is also possible to use the unconverted feed itself, or liquids such as molten salts or liquid sodium.
- the differentiated catalyst extraction means is normally selected from the group formed by continuous and discontinuous extraction means.
- the catalytic bed comprises a plurality of catalytic zones separated by noncatalytic zones for heating the feed.
- the most upstream catalyst extraction means differs from at least one downstream extraction means, and particularly that located the furthest downstream, in its lower extraction capacity (the concepts of upstream and downstream being with respect to the direction of flow of the feed).
- the invention also proposes a process for chemical conversion of a feed using a reactor as described above.
- the feed is a hydrocarbon feed, often with an added diluent (for example steam, hydrogen, nitrogen or a mixture of these gases).
- an added diluent for example steam, hydrogen, nitrogen or a mixture of these gases.
- the chemical conversion process is a process for catalytic dehydrogenation of a paraffinic hydrocarbon feed.
- FIG. 1 is a non-limiting representation of a reactor R in accordance with the invention used to carry out an endothermic reaction.
- the reaction feed is introduced into reactor R via a line 1 ; it traverses, in succession, a catalytic bed 3 a, then a heat exchanger 4 a, then a second catalytic bed 3 b, then a second heat exchanger 4 b, then a third and last catalytic bed 3 c, before leaving the reactor via a line 2 .
- the catalyst is introduced into the reactor at the head thereof via a line 9 . It is distributed into the three catalytic beds 3 a, 3 b, 3 c in which they flow under gravity in downflow mode.
- Each catalytic bed has a separate hopper for evacuating the catalyst: 7 a for bed 3 a, 7 b for bed 3 b and 7 c for bed 3 c.
- Extraction valves 8 a, 8 b, 8 c at the bottom of each of the catalytic beds can separately extract used catalyst flowing in each of the catalytic beds in series.
- the catalyst is evacuated via lines 80 a, 80 b and 80 c.
- Heat exchangers 4 a and 4 b are fed by heat transfer fluid introduced via lines 5 , 5 a and 5 b, this fluid leaving the exchanger via lines 6 a, 6 b and 6 .
- a substantially inert gas is introduced via lines 10 , 10 a and 10 b.
- the function of the gas is to provide a barrier gas to prevent feed passing from bed 3 a to bed 3 b and by-passing exchanger 4 a, and similarly preventing feed passing from bed 3 b to bed 3 c and by-passing exchanger 4 b.
- this gas can be a diluent for the fed, for example steam or a hydrogen-rich recycle gas.
- the feed pre-heated to the reaction temperature, traverses the three catalytic beds (or zones) 3 a, 3 b, 3 c in series, with two intermediate re-heating steps.
- the catalyst, introduced via line 9 , is extracted continuously or discontinuously via lines 80 a, 80 b, 80 c.
- the catalyst flowing in bed 3 c is preferably renewed more rapidly than that in bed 3 a.
- the catalyst ages more rapidly and deactivates and cokes more rapidly at the end of the reaction zone, i.e., in the downstream bed 3 c more than in the upstream bed 3 a.
- 3 c is renewed more rapidly than 3 b, which is itself renewed more rapidly than bed 3 a.
- the invention thus enables the catalyst to be used efficiently, which catalyst is extracted in a relatively constant state of deactivation.
- valves 8 a, 8 b, 8 c can be used to adjust the differentiated catalyst extraction.
- the reactors of the invention can contain 2 to about 20 catalytic zones separated by heat exchange zones.
- reaction fluid can also be introduced laterally and flow horizontally, as a crosswise current with the feed.
- the reactor of the invention can carry out chemical conversion of a feed in the presence of a catalyst while providing each of the catalytic zones with the necessary amount of heat. It also enables the at least partially deactivated catalyst to be extracted in a differentiated manner.
- the reactor of the invention can maintain a high catalytic activity and/or productivity for the desired product.
- the invention can in particular be employed for hydrocarbon reforming, for dehydrogenating ethylbenzene, and for dehydrogenating paraffins such as propane, n-butane, isobutane, primarily linear paraffins containing 10 to 14 carbon atoms, and for the production of olefins for the production of alkylbenzenes, or for other chemical reactions.
- paraffins such as propane, n-butane, isobutane, primarily linear paraffins containing 10 to 14 carbon atoms, and for the production of olefins for the production of alkylbenzenes, or for other chemical reactions.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US11/442,328 US7357855B2 (en) | 2000-11-29 | 2006-05-30 | Reactor for chemical conversion of a feed with added heat, and crosswise flow of feed and catalyst |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR00/15426 | 2000-11-29 | ||
| FR0015426A FR2817172B1 (fr) | 2000-11-29 | 2000-11-29 | Reacteur de conversion chimique d'une charge avec apports de chaleur et circulation croisee de la charge et d'un catalyseur |
| PCT/FR2001/003458 WO2002043851A1 (fr) | 2000-11-29 | 2001-11-07 | Reacteur de conversion chimique d'une charge avec apports de chaleur et circulation croisee de la charge et d'un catalyseur |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US11/442,328 Continuation US7357855B2 (en) | 2000-11-29 | 2006-05-30 | Reactor for chemical conversion of a feed with added heat, and crosswise flow of feed and catalyst |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US20040067174A1 true US20040067174A1 (en) | 2004-04-08 |
Family
ID=8857015
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US10/432,773 Abandoned US20040067174A1 (en) | 2000-11-29 | 2001-11-07 | Reactor for chemical conversion of a feedstock with heat inputs and feedstock/catalyst cross-circulation |
| US11/442,328 Expired - Fee Related US7357855B2 (en) | 2000-11-29 | 2006-05-30 | Reactor for chemical conversion of a feed with added heat, and crosswise flow of feed and catalyst |
Family Applications After (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US11/442,328 Expired - Fee Related US7357855B2 (en) | 2000-11-29 | 2006-05-30 | Reactor for chemical conversion of a feed with added heat, and crosswise flow of feed and catalyst |
Country Status (9)
| Country | Link |
|---|---|
| US (2) | US20040067174A1 (ja) |
| EP (1) | EP1339483B1 (ja) |
| JP (2) | JP4875283B2 (ja) |
| CA (1) | CA2430246C (ja) |
| DE (1) | DE60110625T2 (ja) |
| ES (1) | ES2242790T3 (ja) |
| FR (1) | FR2817172B1 (ja) |
| MX (1) | MXPA03004591A (ja) |
| WO (1) | WO2002043851A1 (ja) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2006034551A1 (en) * | 2004-09-28 | 2006-04-06 | The University Of Queensland | Magnetic field dosimeter |
| KR20210073562A (ko) * | 2018-10-15 | 2021-06-18 | 유오피 엘엘씨 | 가동 기간이 개선된 탈수소화 방법 |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102187055B (zh) * | 2008-10-13 | 2014-09-10 | 国际壳牌研究有限公司 | 用于加热地下地层的循环传热流体系统 |
| JP6327888B2 (ja) * | 2013-03-07 | 2018-05-23 | 新日鐵住金株式会社 | 石炭乾留ガスからの水素ガス製造装置および水素ガス製造方法 |
| KR101831507B1 (ko) * | 2016-01-05 | 2018-04-05 | 주식회사 효성 | 등온반응 유도용 자체 열공급 탈수소 반응기 |
| KR101815750B1 (ko) * | 2016-01-29 | 2018-01-31 | 주식회사 효성 | 탈수소 공정용 이동층 반응기 |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2534859A (en) * | 1946-04-18 | 1950-12-19 | Socony Vacuum Oil Co Inc | Method and apparatus for hydrocarbon conversion |
| US2865848A (en) * | 1952-09-24 | 1958-12-23 | Socony Mobil Oil Co Inc | Temperature control in hydrocarbon conversion processes |
| US4525482A (en) * | 1983-03-23 | 1985-06-25 | Toyo Engineering Corporation | Process for producing a gas containing methane |
| US4622210A (en) * | 1984-08-13 | 1986-11-11 | Standard Oil Company (Indiana) | Sulfur oxide and particulate removal system |
| US5525311A (en) * | 1994-05-02 | 1996-06-11 | Uop | Process and apparatus for controlling reaction temperatures |
| US5948240A (en) * | 1997-11-17 | 1999-09-07 | Uop Llc | Process for controlling reaction temperatures |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR877663A (fr) * | 1940-12-11 | 1942-12-14 | Metallgesellschaft Ag | Dispositif pour effectuer des réactions catalytiques exothermiques |
| DE2449789B1 (de) * | 1974-10-19 | 1976-03-11 | Deggendorfer Werft Eisenbau | Mehrstufiger Horden-Reaktor |
| JPS5223572A (en) * | 1975-08-15 | 1977-02-22 | Sumitomo Chem Co Ltd | Folded screen type reactor |
| JPS5260274A (en) * | 1975-11-12 | 1977-05-18 | Nippon Kokan Kk <Nkk> | Solid-vapor contact apparatus |
| JPS57177330A (en) * | 1981-04-27 | 1982-11-01 | Babcock Hitachi Kk | Apparatus for adsorbing sulfur dioxide |
| US5600052A (en) * | 1994-05-02 | 1997-02-04 | Uop | Process and apparatus for controlling reaction temperatures |
| US6228341B1 (en) * | 1998-09-08 | 2001-05-08 | Uop Llc | Process using plate arrangement for exothermic reactions |
| US6100436A (en) * | 1998-09-08 | 2000-08-08 | Uop Llc | Process and apparatus for controlling reaction temperatures with heating arrangement in series flow |
| FR2821283B1 (fr) * | 2001-02-28 | 2003-04-18 | Inst Francais Du Petrole | Procede et reacteur multi-etages catalytique a faible epaisseur avec echangeur thermique interne, et son utilisation |
-
2000
- 2000-11-29 FR FR0015426A patent/FR2817172B1/fr not_active Expired - Lifetime
-
2001
- 2001-11-07 EP EP01998396A patent/EP1339483B1/fr not_active Expired - Lifetime
- 2001-11-07 MX MXPA03004591A patent/MXPA03004591A/es active IP Right Grant
- 2001-11-07 JP JP2002545817A patent/JP4875283B2/ja not_active Expired - Fee Related
- 2001-11-07 DE DE60110625T patent/DE60110625T2/de not_active Expired - Lifetime
- 2001-11-07 WO PCT/FR2001/003458 patent/WO2002043851A1/fr not_active Ceased
- 2001-11-07 ES ES01998396T patent/ES2242790T3/es not_active Expired - Lifetime
- 2001-11-07 CA CA002430246A patent/CA2430246C/fr not_active Expired - Fee Related
- 2001-11-07 US US10/432,773 patent/US20040067174A1/en not_active Abandoned
-
2006
- 2006-05-30 US US11/442,328 patent/US7357855B2/en not_active Expired - Fee Related
-
2009
- 2009-10-16 JP JP2009238922A patent/JP2010051960A/ja not_active Ceased
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2534859A (en) * | 1946-04-18 | 1950-12-19 | Socony Vacuum Oil Co Inc | Method and apparatus for hydrocarbon conversion |
| US2865848A (en) * | 1952-09-24 | 1958-12-23 | Socony Mobil Oil Co Inc | Temperature control in hydrocarbon conversion processes |
| US4525482A (en) * | 1983-03-23 | 1985-06-25 | Toyo Engineering Corporation | Process for producing a gas containing methane |
| US4622210A (en) * | 1984-08-13 | 1986-11-11 | Standard Oil Company (Indiana) | Sulfur oxide and particulate removal system |
| US5525311A (en) * | 1994-05-02 | 1996-06-11 | Uop | Process and apparatus for controlling reaction temperatures |
| US5948240A (en) * | 1997-11-17 | 1999-09-07 | Uop Llc | Process for controlling reaction temperatures |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2006034551A1 (en) * | 2004-09-28 | 2006-04-06 | The University Of Queensland | Magnetic field dosimeter |
| KR20210073562A (ko) * | 2018-10-15 | 2021-06-18 | 유오피 엘엘씨 | 가동 기간이 개선된 탈수소화 방법 |
| KR102533922B1 (ko) * | 2018-10-15 | 2023-05-17 | 유오피 엘엘씨 | 가동 기간이 개선된 탈수소화 방법 |
Also Published As
| Publication number | Publication date |
|---|---|
| ES2242790T3 (es) | 2005-11-16 |
| FR2817172B1 (fr) | 2003-09-26 |
| US7357855B2 (en) | 2008-04-15 |
| DE60110625T2 (de) | 2005-11-10 |
| US20060216218A1 (en) | 2006-09-28 |
| JP2004531361A (ja) | 2004-10-14 |
| MXPA03004591A (es) | 2004-05-05 |
| DE60110625D1 (de) | 2005-06-09 |
| WO2002043851A1 (fr) | 2002-06-06 |
| CA2430246A1 (fr) | 2002-06-06 |
| FR2817172A1 (fr) | 2002-05-31 |
| CA2430246C (fr) | 2009-10-13 |
| JP4875283B2 (ja) | 2012-02-15 |
| EP1339483B1 (fr) | 2005-05-04 |
| JP2010051960A (ja) | 2010-03-11 |
| EP1339483A1 (fr) | 2003-09-03 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| AS | Assignment |
Owner name: INSTITUT FRANCAIS DU PETROLE, FRANCE Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:LENGLET, ERIC;BOUDET, NICOLAS;HOFFMANN, FREDERIC;REEL/FRAME:014719/0875;SIGNING DATES FROM 20030425 TO 20030428 |
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| STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION |