EP0117200A1 - Einrichtung zur chemischen Umsetzung einer Wasserstoff und Kohlenwasserstoffe enthaltenden gasförmigen Mischung - Google Patents

Einrichtung zur chemischen Umsetzung einer Wasserstoff und Kohlenwasserstoffe enthaltenden gasförmigen Mischung Download PDF

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Publication number
EP0117200A1
EP0117200A1 EP84400303A EP84400303A EP0117200A1 EP 0117200 A1 EP0117200 A1 EP 0117200A1 EP 84400303 A EP84400303 A EP 84400303A EP 84400303 A EP84400303 A EP 84400303A EP 0117200 A1 EP0117200 A1 EP 0117200A1
Authority
EP
European Patent Office
Prior art keywords
ovens
gas mixture
installation
supplied
oven
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.)
Granted
Application number
EP84400303A
Other languages
English (en)
French (fr)
Other versions
EP0117200B1 (de
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/de
Application granted granted Critical
Publication of EP0117200B1 publication Critical patent/EP0117200B1/de
Expired legal-status Critical Current

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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 to react the above-mentioned mixture according to globally endothermic reactions at temperatures of 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 an inlet and an outlet for the gaseous 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 of fossil origin, or by the electric resistance furnaces.
  • 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. These reactions are generally endothermic.
  • 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 includes in parallel with each furnace F 1 , F 2 , F 3 , F 4 supplied with fossil fuel, an furnace F 5 , F 6 , F 7 , F 8 constituted by an enclosure 11, 12, 13, 14 comprising an inlet 15a , 16a, 17a, 18a and an output 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 6 , 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 may conform to that described in French patent application No. 83 02763 of 21.2.1983, 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, or through the ovens with electrical resistances F 5 , F 6 , F 7 , F 8 .
  • These means are constituted (see FIGS. 2 and 3) by valves V I , V 2 ... V 4 , V 5 placed at the inlet and at the outlet of conventional ovens F 1 , ... F 4 and of the valves V 6 , V 7 ... Vg, V 10 placed on the branches 23 ... 27 which extend between the conventional ovens F I ... 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 1 to be carried by the heat exchange with the effluent 3 coming from the last reactor R 4 at a temperature of 460 ° C. or more before it enters 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.
  • 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.
  • the lowering of the average pressure in the installation makes it possible to obtain a higher yield of gasolines.
  • the invention is applicable in all cases where 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 Einrichtung zur chemischen Umsetzung einer Wasserstoff und Kohlenwasserstoffe enthaltenden gasförmigen Mischung Expired EP0117200B1 (de)

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
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
FR8302764 1983-02-21

Publications (2)

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

Family

ID=9286101

Family Applications (1)

Application Number Title Priority Date Filing Date
EP84400303A Expired EP0117200B1 (de) 1983-02-21 1984-02-15 Einrichtung zur chemischen Umsetzung einer Wasserstoff und Kohlenwasserstoffe enthaltenden gasförmigen Mischung

Country Status (9)

Country Link
US (1) US4746495A (de)
EP (1) EP0117200B1 (de)
JP (1) JPS59157179A (de)
AT (1) ATE25100T1 (de)
AU (1) AU2473284A (de)
CA (1) CA1231909A (de)
DE (2) DE3462150D1 (de)
FR (1) FR2541133A1 (de)
ZA (1) ZA841124B (de)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DK202530282A1 (en) * 2025-05-06 2026-04-23 Topsoe As Electrical heating in low carbon processes

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
US8999141B2 (en) * 2008-06-30 2015-04-07 Uop Llc Three-phase hydroprocessing without a recycle gas compressor
US8008534B2 (en) 2008-06-30 2011-08-30 Uop Llc Liquid phase hydroprocessing with temperature management
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

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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

Family Cites Families (9)

* 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
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

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DK202530282A1 (en) * 2025-05-06 2026-04-23 Topsoe As Electrical heating in low carbon processes

Also Published As

Publication number Publication date
FR2541133B1 (de) 1985-04-19
ATE25100T1 (de) 1987-02-15
DE117200T1 (de) 1984-12-20
DE3462150D1 (en) 1987-02-26
CA1231909A (en) 1988-01-26
US4746495A (en) 1988-05-24
AU2473284A (en) 1984-08-30
FR2541133A1 (fr) 1984-08-24
JPS59157179A (ja) 1984-09-06
EP0117200B1 (de) 1987-01-21
ZA841124B (en) 1984-09-26

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