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 PDF

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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
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US
United States
Prior art keywords
feed
reactor
catalyst
extraction
catalytic
Prior art date
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Abandoned
Application number
US10/432,773
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English (en)
Inventor
Eric Lenglet
Nicolas Boudet
Frederic Hoffmann
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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Assigned to INSTITUT FRANCAIS DU PETROLE reassignment INSTITUT FRANCAIS DU PETROLE ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: BOUDET, NICOLAS, HOFFMANN, FREDERIC, LENGLET, ERIC
Publication of US20040067174A1 publication Critical patent/US20040067174A1/en
Priority to US11/442,328 priority Critical patent/US7357855B2/en
Abandoned legal-status Critical Current

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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
    • B01J8/0496—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.

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  • 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)
US10/432,773 2000-11-29 2001-11-07 Reactor for chemical conversion of a feedstock with heat inputs and feedstock/catalyst cross-circulation Abandoned US20040067174A1 (en)

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

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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

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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 (de)
EP (1) EP1339483B1 (de)
JP (2) JP4875283B2 (de)
CA (1) CA2430246C (de)
DE (1) DE60110625T2 (de)
ES (1) ES2242790T3 (de)
FR (1) FR2817172B1 (de)
MX (1) MXPA03004591A (de)
WO (1) WO2002043851A1 (de)

Cited By (2)

* Cited by examiner, † Cited by third party
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)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BRPI0920141A2 (pt) * 2008-10-13 2017-06-27 Shell Int Research sistema e método para tratar uma formação de subsuperfície.
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)

* Cited by examiner, † Cited by third party
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)

* Cited by examiner, † Cited by third party
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

Patent Citations (6)

* Cited by examiner, † Cited by third party
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)

* Cited by examiner, † Cited by third party
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
US7357855B2 (en) 2008-04-15
JP2004531361A (ja) 2004-10-14
CA2430246C (fr) 2009-10-13
DE60110625T2 (de) 2005-11-10
EP1339483A1 (de) 2003-09-03
JP2010051960A (ja) 2010-03-11
WO2002043851A1 (fr) 2002-06-06
FR2817172A1 (fr) 2002-05-31
FR2817172B1 (fr) 2003-09-26
JP4875283B2 (ja) 2012-02-15
MXPA03004591A (es) 2004-05-05
DE60110625D1 (de) 2005-06-09
CA2430246A1 (fr) 2002-06-06
EP1339483B1 (de) 2005-05-04
ES2242790T3 (es) 2005-11-16
US20060216218A1 (en) 2006-09-28

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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

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION