EP0117200B1 - Installation pour la transformation chimique d'un mélange gazeux contenant de l'hydrogène et des hydrocarbures - Google Patents

Installation pour la transformation chimique d'un mélange gazeux contenant de l'hydrogène et des hydrocarbures Download PDF

Info

Publication number
EP0117200B1
EP0117200B1 EP84400303A EP84400303A EP0117200B1 EP 0117200 B1 EP0117200 B1 EP 0117200B1 EP 84400303 A EP84400303 A EP 84400303A EP 84400303 A EP84400303 A EP 84400303A EP 0117200 B1 EP0117200 B1 EP 0117200B1
Authority
EP
European Patent Office
Prior art keywords
gas mixture
furnaces
installation
furnace
electric
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.)
Expired
Application number
EP84400303A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0117200A1 (fr
Inventor
Pierre Cros
Jean Louis Mingaud
Christian Plard
Jacques Vanrenterghem
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Electricite de France SA
Spie Batignolles SA
Original Assignee
Electricite de France SA
Spie Batignolles SA
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Electricite de France SA, Spie Batignolles SA filed Critical Electricite de France SA
Priority to AT84400303T priority Critical patent/ATE25100T1/de
Publication of EP0117200A1 publication Critical patent/EP0117200A1/fr
Application granted granted Critical
Publication of EP0117200B1 publication Critical patent/EP0117200B1/fr
Expired legal-status Critical Current

Links

Images

Classifications

    • 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
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • 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

Definitions

  • the present invention relates to an installation for the chemical transformation of a gas mixture containing in particular hydrocarbons and hydrogen.
  • This installation comprises reactors in which the above-mentioned mixture reacts according to globally endothermic reactions at temperatures between approximately 350 and 900 ° C., under high pressure and in the presence of a catalyst.
  • This installation also comprises an oven arranged upstream of each reactor to heat the gas mixture before its introduction into the reactor.
  • the furnaces for reheating the gaseous mixture of hydrocarbons and hydrogen are conventional furnaces supplied with liquid or gaseous fuel of fossil origin. These ovens include bundles of tubes of reduced section heated by combustion of fuel of fossil origin, in which the above-mentioned gas mixture is passed.
  • the aforementioned flame ovens are bulky mainly depending on the fact that a single ply of tubes surrounds the flame.
  • the object of the present invention is to create an installation which overcomes all the aforementioned drawbacks.
  • the installation targeted by the invention for the chemical transformation of a gaseous mixture containing in particular hydrogen and hydrocarbons comprises a succession of reactors for reacting the above-mentioned mixture according to globally endothermic reactions at temperatures between 400 and 900 ° C approximately, under high pressure and in the presence of a catalyst.
  • An oven is arranged upstream of each reactor to heat the gas mixture before its introduction into said reactor.
  • this installation is characterized in that the ovens are constituted by an enclosure comprising an inlet and an outlet of the gas mixture and containing one or more electrical resistance (s) for heating intended to be placed (s) in direct contact with the gas mixture introduced into this enclosure.
  • the ovens are constituted by an enclosure comprising an inlet and an outlet of the gas mixture and containing one or more electrical resistance (s) for heating intended to be placed (s) in direct contact with the gas mixture introduced into this enclosure.
  • Electric resistance heating furnaces thus replace furnaces supplied with fossil fuel, such as light or heavy fuel oil.
  • the installation comprises in parallel with each furnace supplied with fossil fuel an electric furnace constituted by an enclosure comprising a inlet and outlet of the gas mixture and one or more electrical heating resistors intended to be placed in direct contact with the gas mixture introduced into this enclosure, and means for passing the gas mixture at will either through the furnaces supplied with fuel fossil origin, either by electric resistance ovens.
  • FIG. 1 schematically represents an installation for the catalytic reforming of naphtha obtained by distillation of crude oil, intended to produce gasolines with a high octane number.
  • This installation includes 4 reactors R 1 , R 2 , R 3 , R 4 in which the reforming reactions are carried out between a gaseous mixture of hydrocarbons enriched in hydrogen at temperatures around 500 ° C, pressures between 15 and 30 bars and in the presence of a platinum-based catalyst.
  • each reactor R 1 , R 2 , R 3 , R 4 upstream of each reactor R 1 , R 2 , R 3 , R 4 is placed an oven F 1 , F 2 , F 3 , F 4 which makes it possible to preheat the mixture of hydrocarbons and hydrogen to the optimum temperature before this mixture enters the following reactor R 1 , R 2 , R 3 , R 4 .
  • the mixture 1 of hydrogen-enriched hydrocarbons is introduced into the first furnace F 1 by means of a pump 2.
  • the effluent 3 from the last reactor R 4 passes through heat exchangers 4 disposed upstream of the first furnace F 1 and arranged to carry out a heat exchange between this effluent 3 and the gas mixture 1 which is introduced into the first furnace F 1 .
  • This heat exchange makes it possible to preheat the initial gas mixture 1 before it enters the furnace F 1 .
  • the effluent 3 after this heat exchange is cooled in an air cooler 5 then in a water cooler 6, before entering a separator flask 7 in which the gas to be recycled is separated from the reformate.
  • This reformate is recovered at 8.
  • Part of the gas to be recycled 9 coming from the separator 7 is compressed by means of a compressor 10 which re-injects it downstream of the pump 2 to mix it with the starting naphtha.
  • the installation comprises, in parallel with each furnace F 1 ′ F z , F 3 , F 4 supplied with fossil fuel, an furnace F 5 , F e , F 7 , F 8 constituted by an enclosure 11, 12, 13, 14 comprising an inlet 15a, 16a, 17a, 18a and an outlet 15b, 16b, 17b, 18b and which contains electrical heating resistors 19, 20, 21, 22.
  • These heating resistors 19 to 22 are placed in direct contact with the gas mixture introduced into each of the electric ovens F 5 , F 6 , F 7 , F 8 .
  • These electric ovens F 5 , F e , F 7 , F 8 are constructed in such a way that the mixture of hydrogen and hydrocarbons passes through these ovens with a low pressure drop.
  • These electric ovens can be in accordance with that described in French patent No. 2,541,436 in the names of the applicants and which is entitled "Electric heating device by direct Joule effect to heat a gas mixture”.
  • the installation according to the invention comprises means for passing the gas mixture at will either through conventional ovens F 1 , F 2 , F 3 .
  • F 4 supplied with fossil fuel, either by electric resistance furnaces F 5 , F 6 , F 7 , F 8 .
  • These means are constituted (see FIGS. 2 and 3) by valves V 1 , V 2 ... V 4 , V5 placed at the inlet and at the outlet of conventional ovens F 1 , ... F 4 and of valves V 6 , V 7 ... V 9 , V 10 placed on the branches 23 ... 27 which extend between the conventional ovens F 1 ... F 4 and the electric ovens F 5 ... F 8 .
  • one or more additional heat exchangers 28 are placed on the branch 23 comprised between the outlet 4a of the first exchangers 4 and the inlet 15a of the first electric furnace F 5 .
  • These exchangers 28 are arranged to carry out an additional heat exchange between the gas mixture introduced into the first electric furnace F 5 and the gaseous effluent 3 coming from the last reactor R 4 .
  • Valves V 11 , V 12 placed upstream and downstream of the exchangers 28 on a circuit 29 connected with that of the effluent 3 and a valve V 13 placed on a bypass circuit 30 directly connected to the first exchangers 4, allow either to passing the effluent 3 through the exchangers 28 during the commissioning of the electric ovens F 5 ... F 8 , either directly and only in the first exchanger 4 during the commissioning of the conventional ovens F 1 ... F 4 .
  • the pressure drop caused by the exchanger (s) 28 is less than the reduction in pressure drop achieved during the commissioning of the electric ovens F 5 ... F 8 .
  • the reduction in pressure losses provides the installation with a credit for pressure losses which makes it possible to insert into the 'installation, one or more additional exchangers 28 which will allow the initial mixture to be brought by heat exchange with the effluent 3 from the last reactor R 4 at a temperature of 460 ° C or more before entering the first oven F 5 , instead of 427.5 ° when using conventional ovens.
  • the invention could include only electric ovens in total replacement of conventional ovens.
  • the installation could be specifically adapted to total operation with electric ovens.
  • the invention could relate only to a partial replacement of conventional ovens for one or more electric ovens.
  • the number of furnaces and reactors could be multiplied by correspondingly decreasing their respective sizes, in order to tend towards a quasi-isothermal temperature profile within the catalyst. This would allow better use of the catalyst, therefore a reduction in the overall volume of catalyst and thus a saving in the supply of catalyst, the cost of which is particularly high since it is based on noble and rare metals.
  • this pressure drop credit allows more efficient operation of the installation, in particular better use of the catalyst, by adapting the operating conditions of the unit, thus, for example, the lowering of the average pressure in the installation provides a higher yield of species.
  • the invention is applicable in all cases where a high power heating of a mixture of hydrocarbons and hydrogen is carried out under high pressure, upstream of one or more reactors in which the globally endothermic reactions take place. , at temperatures between 350 and 900 ° C approximately.
  • the invention can also be applied in particular to installations for the treatment of desulfurization of hydrogen hydrocarbons.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
EP84400303A 1983-02-21 1984-02-15 Installation pour la transformation chimique d'un mélange gazeux contenant de l'hydrogène et des hydrocarbures Expired EP0117200B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT84400303T ATE25100T1 (de) 1983-02-21 1984-02-15 Einrichtung zur chemischen umsetzung einer wasserstoff und kohlenwasserstoffe enthaltenden gasfoermigen mischung.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8302764 1983-02-21
FR8302764A FR2541133A1 (fr) 1983-02-21 1983-02-21 Installation pour la transformation chimique d'un melange gazeux contenant de l'hydrogene et des hydrocarbures

Publications (2)

Publication Number Publication Date
EP0117200A1 EP0117200A1 (fr) 1984-08-29
EP0117200B1 true EP0117200B1 (fr) 1987-01-21

Family

ID=9286101

Family Applications (1)

Application Number Title Priority Date Filing Date
EP84400303A Expired EP0117200B1 (fr) 1983-02-21 1984-02-15 Installation pour la transformation chimique d'un mélange gazeux contenant de l'hydrogène et des hydrocarbures

Country Status (9)

Country Link
US (1) US4746495A (https=)
EP (1) EP0117200B1 (https=)
JP (1) JPS59157179A (https=)
AT (1) ATE25100T1 (https=)
AU (1) AU2473284A (https=)
CA (1) CA1231909A (https=)
DE (2) DE117200T1 (https=)
FR (1) FR2541133A1 (https=)
ZA (1) ZA841124B (https=)

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4973453A (en) * 1988-02-05 1990-11-27 Gtg, Inc. Apparatus for the production of heavier hydrocarbons from gaseous light hydrocarbons
GB2401804B (en) * 2003-05-19 2006-09-27 Phoenix Chemicals Ltd Reactor
US7906013B2 (en) * 2006-12-29 2011-03-15 Uop Llc Hydrocarbon conversion process
KR101308510B1 (ko) * 2007-11-05 2013-09-12 동부대우전자 주식회사 히터 내장형 흡기관을 구비하는 건조기
US9279087B2 (en) * 2008-06-30 2016-03-08 Uop Llc Multi-staged hydroprocessing process and system
US8008534B2 (en) 2008-06-30 2011-08-30 Uop Llc Liquid phase hydroprocessing with temperature management
US8999141B2 (en) * 2008-06-30 2015-04-07 Uop Llc Three-phase hydroprocessing without a recycle gas compressor
CN101424447B (zh) * 2008-10-07 2011-02-02 艾欧史密斯(中国)热水器有限公司 混合能源恒温控制热水器
US8518241B2 (en) * 2009-06-30 2013-08-27 Uop Llc Method for multi-staged hydroprocessing
US8221706B2 (en) * 2009-06-30 2012-07-17 Uop Llc Apparatus for multi-staged hydroprocessing

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1915567A (en) * 1926-03-23 1933-06-27 Carter Russell Heating unit for hydrogenous and carbonaceous values recovery
US1868096A (en) * 1929-06-05 1932-07-19 Dreyfus Henry Manufacture of methyl alcohol
US2210257A (en) * 1939-08-12 1940-08-06 Universal Oil Prod Co Catalytic conversion of hydrocarbons
US2947682A (en) * 1956-12-03 1960-08-02 Sinclair Refining Co Method of producing a high octane gasoline by reforming a naphtha in two stages
US3128242A (en) * 1961-06-08 1964-04-07 Socony Mobil Oil Co Inc Isothermal-adiabatic catalytic hydrocarbon conversion
GB1267803A (en) * 1968-04-03 1972-03-22 Laporte Titanium Ltd Improvements in and relating to the heating of gases
US4166024A (en) * 1978-07-10 1979-08-28 Exxon Research & Engineering Co. Process for suppression of hydrogenolysis and C5+ liquid yield loss in a cyclic reforming unit
CA1082759A (en) * 1979-10-12 1980-07-29 Douglas E. Carl Alternative heating apparatus for use in a heating system having a fuel burner, particularly a forced- air central heating system
US4341167A (en) * 1980-10-29 1982-07-27 St John Eric P Energy conserving heating and cooling system for printing plant
FR2541436A1 (fr) * 1983-02-21 1984-08-24 Spie Batignolles Dispositif de chauffage electrique par effet joule direct pour chauffer un melange gazeux

Also Published As

Publication number Publication date
AU2473284A (en) 1984-08-30
FR2541133A1 (fr) 1984-08-24
EP0117200A1 (fr) 1984-08-29
ATE25100T1 (de) 1987-02-15
CA1231909A (en) 1988-01-26
JPS59157179A (ja) 1984-09-06
DE3462150D1 (en) 1987-02-26
FR2541133B1 (https=) 1985-04-19
US4746495A (en) 1988-05-24
ZA841124B (en) 1984-09-26
DE117200T1 (de) 1984-12-20

Similar Documents

Publication Publication Date Title
EP0117200B1 (fr) Installation pour la transformation chimique d'un mélange gazeux contenant de l'hydrogène et des hydrocarbures
DE60314432T2 (de) Festoxidbrennstoffzelle
JP5292389B2 (ja) 水素システムおよび水素システムの始動方法
US6977002B2 (en) Fuel reforming apparatus and the method of starting it
EP0655596B1 (fr) Procédé et installation de purification cryogénique d'hydrogène
EA021780B1 (ru) Комплексная система очистки биогаза с целью удаления воды, силоксанов, серы, кислорода, хлоридов и летучих органических соединений
FR2966814A1 (fr) Procede de production d'hydrogene par vaporeformage d'une coupe petroliere avec production de vapeur optimisee.
EP2061113B1 (de) Brennstoffzellensystem und Verfahren zu dessen Betrieb
FR3063181A1 (fr) Procede pour demarrer un ensemble de pile a combustible, et ensemble correspondant
AT406808B (de) Kraft-wärme-kopplungsanlage mit brennstoffzellen
EA010401B1 (ru) Способ работы газовой двигательной установки и системы подачи топлива газового двигателя
DE102008045147B4 (de) Effizientes Brennstoffzellensystem mit integrierter Gaserzeugung und zugehöriges Verfahren zur Regelung und Steuerung des Betriebes
JP2006322454A (ja) 燃料安定化システムおよび燃料供給システムの燃料安定化方法
EP0794150B1 (fr) Procédé et dispositif de craquage de l'ammoniac présent dans un gaz contenant de l'hydrogéne sulfuré
JPH02168570A (ja) 電気を発生する方法
CH700655A1 (fr) Procede et dispositif de traitement par oxydation par voie humide de dechets liquides contenant des charges en matieres minerales.
JP4873282B2 (ja) 改質方法および改質器
FR2887867A1 (fr) Installation combinee de production d'energie electrique et de production d'hydrogene
EP1942537B1 (de) Brennstoffzellensystem mit einer Regenerationseinrichtung für einen Reformer und zugehöriges Verfahren
KR100517953B1 (ko) 산소를 함유한 가스터어빈의 배기가스를 이용하여 연소실에 연소공기를 공급하는 방법 및 이를 이용한 공정설비
DE102011116981B4 (de) Abgasbehandlungssystem zum Behandeln von Abgas von einer Brennkraftmaschine
CA2307069A1 (en) Water-gas shift reactor warm-up
EP2711334B1 (fr) Procédé de production d'hydrogène pur à partir d'une charge hydrocarbonée dénaturée incluant une étape de désulfuration avec contrôle de température en amont du PSA
FR2622563A1 (fr) Procede de reformage de methanol impur et dispositif de mise en oeuvre
FR2831333A1 (fr) Dispositif d'alimentation en gaz d'une pile a combustible

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 19840220

AK Designated contracting states

Designated state(s): AT BE CH DE FR GB IT LI LU NL SE

ITCL It: translation for ep claims filed

Representative=s name: BARZANO' E ZANARDO ROMA S.P.A.

TCAT At: translation of patent claims filed
TCNL Nl: translation of patent claims filed
DET De: translation of patent claims
GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE CH DE FR GB IT LI LU NL SE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Effective date: 19870121

Ref country code: IT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED.

Effective date: 19870121

Ref country code: AT

Effective date: 19870121

REF Corresponds to:

Ref document number: 25100

Country of ref document: AT

Date of ref document: 19870215

Kind code of ref document: T

REF Corresponds to:

Ref document number: 3462150

Country of ref document: DE

Date of ref document: 19870226

NLV1 Nl: lapsed or annulled due to failure to fulfill the requirements of art. 29p and 29m of the patents act
PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 19920217

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 19920220

Year of fee payment: 9

Ref country code: CH

Payment date: 19920220

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: LU

Payment date: 19920225

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 19920228

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19920312

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 19920430

Year of fee payment: 9

EPTA Lu: last paid annual fee
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 19930215

Ref country code: GB

Effective date: 19930215

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Effective date: 19930216

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Effective date: 19930228

Ref country code: CH

Effective date: 19930228

Ref country code: BE

Effective date: 19930228

BERE Be: lapsed

Owner name: SPIE-BATIGNOLLES S.A.

Effective date: 19930228

Owner name: ELECTRICITE DE FRANCE SERVICE NATIONAL

Effective date: 19930228

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 19930215

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Effective date: 19931029

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Effective date: 19931103

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

EUG Se: european patent has lapsed

Ref document number: 84400303.8

Effective date: 19930912