EP0177676B1 - Réglage par récupération de la chaleur d'un procédé d'hydrogénation en suspension avec hydrogénation en phase gazeuse intégrée - Google Patents

Réglage par récupération de la chaleur d'un procédé d'hydrogénation en suspension avec hydrogénation en phase gazeuse intégrée Download PDF

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Publication number
EP0177676B1
EP0177676B1 EP85107962A EP85107962A EP0177676B1 EP 0177676 B1 EP0177676 B1 EP 0177676B1 EP 85107962 A EP85107962 A EP 85107962A EP 85107962 A EP85107962 A EP 85107962A EP 0177676 B1 EP0177676 B1 EP 0177676B1
Authority
EP
European Patent Office
Prior art keywords
hydrogenation
gas phase
phase
temperature
suspension
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 - Lifetime
Application number
EP85107962A
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German (de)
English (en)
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EP0177676A3 (en
EP0177676A2 (fr
Inventor
Eckard Dr. Wolowski
Frank Dr. Mirtsch
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.)
RAG AG
Original Assignee
Ruhrkohle AG
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Publication date
Application filed by Ruhrkohle AG filed Critical Ruhrkohle AG
Publication of EP0177676A2 publication Critical patent/EP0177676A2/fr
Publication of EP0177676A3 publication Critical patent/EP0177676A3/de
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Publication of EP0177676B1 publication Critical patent/EP0177676B1/fr
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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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes

Definitions

  • a process is also known in which hydrocarbon mixtures which are foreign to the process are advantageously used as grinding oils for mashing the coal instead of oils of process origin (EP-A-123161).
  • a defined phase equilibrium temperature is set in the intermediate separator in order to achieve the predetermined quantity splitting by partial condensation of the hydrogenation products from the bottom phase.
  • This temperature in the intermediate separator is set by cooling the hot bottom phase hydrogenation products in heat exchangers, coal mash and hydrogenation gas being heated by indirect heat exchange.
  • bypass lines are often used in technology on the heat exchanger in order to keep the heat transfer capacity of the system almost constant by means of controlled bypass valves despite incrusting heat exchangers.
  • the large overdimensioning of the heat exchangers for the clean state and the risk of a flange fan in hot high-pressure lines which have bypasses with a large control range are disadvantageous.
  • the temperature of the gas phase feedstocks has to be increased as the operating time increases due to the deactivation of the gas phase catalyst (e.g. 390 degrees Celsius to 430 degrees Celsius).
  • the invention has for its object to achieve a defined setting of the phase equilibrium temperature in the intermediate separator and a defined increase in the inlet temperature of the gas phase feedstocks with increasing runtime with economic heat recovery despite increasing unavoidable incrustation of the heat exchanger - especially at high mash temperatures.
  • This object is achieved in that in order to set the defined phase equilibrium temperature in the intermediate separator, the gaseous hydrogenation products from the bottom phase are cooled in a mash heat exchanger, a head cooler and a final cooler in front of the intermediate separator and the heating of the cold mash-hydrogenation gas mixture in Heat exchangers are carried out by indirect heat exchange with the hot hydrogenation products from the gas phase hydrogenation.
  • the temperature of the gas phase feedstocks must be raised gradually. This takes place - without an additional heating furnace - according to the invention in that the temperature level of the head cooler upstream of the intermediate separator is also increased as the mash heat exchanger progresses. At the same time, with increasing reduction in the heat transfer capacity of the mash heat exchanger, the waste heat generated from the bottom phase hydrogenation is transferred to the upstream mash preheating of the bottom phase hydrogenation via the path of gas phase hydrogenation and thus used economically.
  • the desired temperature in the intermediate separator is set by means of a final cooler, in which steam is expediently generated or hydrogenation gas is preheated.
  • the temperature level of the bottom phase gases / vapors entering the mash heat exchanger can also be reduced. This reduces the usual fast incrustation of clean pipes of the mash heat exchanger, since the max. occurring mash temperature (at the same averaged mash outlet temperature) is reduced.
  • the desired temperature of the starting materials for the gas phase hydrogenation can be set by means of a head cooler (incl. Bypass) after the bottom phase hydrogenation.
  • the bypass around the mash heat exchanger serves to limit the max. Mash outlet temperature of the mash heat exchanger (especially when the heat exchanger tubes are clean).
  • the start-up process is carried out quickly by heating the gas phase feedstocks using a head cooler behind the bottom phase hydrogenation.
  • the process is explained in more detail using two examples:
  • the gaseous and vaporous products from the bottom phase reactor 4 are partially cooled by means of mash heat exchanger 2 by indirect heat exchange, the mash-hydrogenation gas mixture being heated to the starting temperature of the bottom phase hydrogenation of approximately 440 ° C. on the heating side.
  • the bottom phase products are further cooled by indirect heat exchange in the head cooler 7 and in the final cooler 8.
  • the products from the bottom phase hydrogenation are divided into the solvent fraction (liquid) and the feed stream for the gas phase hydrogenation (gases / vapors). The latter is heated in the head cooler 7 and then in the indirect heat exchanger 10 to the gas phase reaction temperature of approximately 390 ° C.
  • the gas phase products are partially cooled by indirect heat exchange in the mash heat exchanger 1, whereby the mash-hydrogenation gas mixture is preheated.
  • the hydrogenation gas is preheated by further cooling of the gas phase products.
  • the entire process is self-sufficient in stationary operation.
  • the mash heating furnace 3 serves only as a start-up furnace.
  • the waste heat from the heat exchanger 8 is preferably used to generate MD steam or to preheat the hydrogenation gas.
  • head cooler 6 the gaseous and vaporous products can be used.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Industrial Gases (AREA)

Claims (5)

  1. Procédé d'hydrogénation en suspension avec hydrogénation indirecte en phase gazeuse, avec un ajustement parfaitement défini de la température dans le séparateur intermédiaire et dans le réacteur en phase gazeuse, pour une récupération rentable de la chaleur, caractérisé en ce que, pour ajuster à une valeur parfaitement définie la température d'équilibre de phase dans le séparateur intermédiaire, on refroidit les produits d'hydrogénation gazeux provenant de la phase en suspension dans un échangeur de chaleur de charbon broyé, un réfrigérant de tête et un réfrigérant terminal en amont du séparateur intermédiaire.
  2. Procédé selon la revendication 1, caractérisé en ce que, pour ajuster la température à une valeur parfaitement définie (séparateur intermédiaire) dans un réfrigérant de tête installé en aval de l'échangeur de chaleur de charbon broyé, on utilise en partie les chaleurs perdues des produits de la phase en suspension pour chauffer les substances utilisées pour l'hydrogénation en phase gazeuse, de sorte que l'on peut utiliser d'une manière économique les chaleurs perdues des produits en phase gazeuse, à niveau de température élevé, pour le préchauffage du charbon broyé de l'unité d'hydrogénation en suspension.
  3. Procédé selon la revendication 1, caractérisé en ce que, à l'aide du réfrigérant de tête installé en aval de l'unité d'hydrogénation en suspension, on utilise les chaleurs perdues des produits en suspension pour chauffer les substances utilisées pour l'hydrogénation en phase gazeuse, pour d'une part faire démarrer l'hydrogénation en phase gazeuse, et d'autre part ajuster à la valeur voulue la température d'entrée des substances utilisées en phase gazeuse.
  4. Procédé selon la revendication 1, caractérisé en ce que, pour ajuster la température de sortie du charbon broyé de l'échangeur de chaleur de charbon broyé, on utilise un réfrigérant de tête en aval de l'hydrogénation en suspension, ainsi qu'une dérivation pour éviter le préchauffeur de charbon broyé.
  5. Procédé selon la revendication 1, caractérisé en ce que, pour ajuster à la valeur voulue la température du séparateur intermédiaire, on utilise un réfrigérant terminal dans lequel il y a production de vapeur ou préchauffage de gaz d'hydrogénation.
EP85107962A 1984-09-13 1985-06-27 Réglage par récupération de la chaleur d'un procédé d'hydrogénation en suspension avec hydrogénation en phase gazeuse intégrée Expired - Lifetime EP0177676B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3433625 1984-09-13
DE3433625 1984-09-13

Publications (3)

Publication Number Publication Date
EP0177676A2 EP0177676A2 (fr) 1986-04-16
EP0177676A3 EP0177676A3 (en) 1988-03-02
EP0177676B1 true EP0177676B1 (fr) 1992-03-04

Family

ID=6245308

Family Applications (1)

Application Number Title Priority Date Filing Date
EP85107962A Expired - Lifetime EP0177676B1 (fr) 1984-09-13 1985-06-27 Réglage par récupération de la chaleur d'un procédé d'hydrogénation en suspension avec hydrogénation en phase gazeuse intégrée

Country Status (8)

Country Link
US (1) US4636300A (fr)
EP (1) EP0177676B1 (fr)
JP (1) JPS6172097A (fr)
AU (1) AU586430B2 (fr)
CA (1) CA1251753A (fr)
DE (1) DE3585485D1 (fr)
PL (1) PL255319A1 (fr)
ZA (1) ZA856989B (fr)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3741105A1 (de) * 1987-12-04 1989-06-15 Veba Oel Entwicklungs Gmbh Verfahren zur hydrierung fluessiger kohlenstoffhaltiger einsatzstoffe
DE3741104A1 (de) * 1987-12-04 1989-06-15 Ruhrkohle Ag Verfahren zur hydrierung fester kohlenstoffhaltiger einsatzstoffe
DE102018108989A1 (de) 2018-04-16 2019-10-17 Thyssenkrupp Ag Industrieanlage mit Anfahrofen und Verfahren zum Initiieren chemischer Reaktionen

Family Cites Families (34)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3823084A (en) * 1972-06-30 1974-07-09 W Schroeder Hydrogenation of coal
US3862108A (en) * 1973-01-02 1975-01-21 Hydrocarbon Research Inc Hydrogenation of residuum
US4099933A (en) * 1973-06-01 1978-07-11 Hydrocarbon Research, Inc. Process for the multiple zone gasification of coal
US3884649A (en) * 1973-10-29 1975-05-20 Inst Gas Technology Coal pretreater and ash agglomerating coal gasifier
US3926775A (en) * 1973-11-01 1975-12-16 Wilburn C Schroeder Hydrogenation of coal
US3950244A (en) * 1974-02-11 1976-04-13 Gulf Research & Development Company Process for treating a solid-containing liquid hydrocarbon oil
US3953180A (en) * 1974-07-11 1976-04-27 Hydrocarbon Research, Inc. Production of low BTU sulfur-free gas from residual oil
GB1482690A (en) * 1974-12-19 1977-08-10 Coal Ind Hydrogenation of coal
US4123502A (en) * 1975-02-06 1978-10-31 Heinz Holter Process for the purification of gas generated in the pressure gasification of coal
US4191539A (en) * 1976-06-07 1980-03-04 Institute Of Gas Technology Method for feeding caking coal particles to a gasifier
US4057402A (en) * 1976-06-28 1977-11-08 Institute Of Gas Technology Coal pretreatment and gasification process
DE2651253C2 (de) * 1976-11-10 1984-03-08 Saarbergwerke AG, 6600 Saarbrücken Verfahren zum Hydrieren von Kohle
DE2654635B2 (de) * 1976-12-02 1979-07-12 Ludwig Dr. 6703 Limburgerhof Raichle Verfahren zur kontinuierlichen Herstellung von Kohlenwasserstoffölen aus Kohle durch spaltende Druckhydrierung
DE2810479C2 (de) * 1977-03-12 1983-05-26 Kobe Steel, Ltd., Kobe, Hyogo Verfahren zum Trocknen von Roh-Braunkohle in einer mit flüssigen Kohlenwasserstoffen hergestellten Einsatz-Suspension
GB1604230A (en) * 1978-05-31 1981-12-02 Mobil Oil Corp Hydroprocessing coal liquids
US4331530A (en) * 1978-02-27 1982-05-25 Occidental Research Corporation Process for the conversion of coal
US4222844A (en) * 1978-05-08 1980-09-16 Exxon Research & Engineering Co. Use of once-through treat gas to remove the heat of reaction in solvent hydrogenation processes
DE2839461A1 (de) * 1978-09-11 1980-03-27 Bergwerksverband Gmbh Formmassen aus thermoplastischen kunststoffen und rueckstaenden der kohlehydrierung
US4189375A (en) * 1978-12-13 1980-02-19 Gulf Oil Corporation Coal liquefaction process utilizing selective heat addition
US4189374A (en) * 1978-12-13 1980-02-19 Gulf Oil Corporation Coal liquefaction process employing internal heat transfer
US4350582A (en) * 1979-10-18 1982-09-21 Chevron Research Company Two-stage coal liquefaction process with process-derived solvent
DE2945352A1 (de) * 1979-11-09 1981-05-27 Linde Ag, 6200 Wiesbaden Verfahren zur kohlehydrierung
US4421632A (en) * 1980-09-04 1983-12-20 Wuerfel Helmut Process for hydrogenation of coal
DE3042984C2 (de) * 1980-11-14 1986-06-26 Saarbergwerke AG, 6600 Saarbrücken Verfahren zum Hydrieren von Kohle
DE3101598A1 (de) * 1981-01-20 1982-08-26 Basf Ag, 6700 Ludwigshafen Verfahren zum hydrieren von kohle
US4400263A (en) * 1981-02-09 1983-08-23 Hri, Inc. H-Coal process and plant design
DE3105030A1 (de) * 1981-02-12 1982-09-02 Basf Ag, 6700 Ludwigshafen Verfahren zur kontinuierlichen herstellung von kohlenwasserstoffoelen aus kohle durch druckhydrierung in zwei stufen
DE3133562A1 (de) * 1981-08-25 1983-03-10 Fried. Krupp Gmbh, 4300 Essen "verfahren zur herstellung fluessiger kohlenwasserstoffe"
DE3141380A1 (de) * 1981-10-17 1983-05-05 GfK Gesellschaft für Kohleverflüssigung mbH, 6600 Saarbrücken Verfahren zum hydrieren von kohle
US4406744A (en) * 1981-11-16 1983-09-27 Clyde Berg Process for the production of hydrogenated tar and distillates and low sulfur coke from coal
US4411765A (en) * 1982-02-10 1983-10-25 Electric Power Development Co. Method for liquefying low rank coal
US4387015A (en) * 1982-09-30 1983-06-07 International Coal Refining Company Coal liquefaction quenching process
DE3300365A1 (de) * 1983-01-07 1984-07-12 Veba Oel Entwicklungsgesellschaft mbH, 4660 Gelsenkirchen-Buer Verfahren zum schwelen von hydrierrueckstaenden
DE3311552A1 (de) * 1983-03-30 1984-10-04 Veba Oel Entwicklungsgesellschaft mbH, 4660 Gelsenkirchen-Buer Verfahren zur hydrierung von kohle

Also Published As

Publication number Publication date
PL255319A1 (en) 1986-08-12
AU4485485A (en) 1986-03-20
AU586430B2 (en) 1989-07-13
JPS6172097A (ja) 1986-04-14
ZA856989B (en) 1986-04-30
EP0177676A3 (en) 1988-03-02
DE3585485D1 (de) 1992-04-09
US4636300A (en) 1987-01-13
CA1251753A (fr) 1989-03-28
JPH0569157B2 (fr) 1993-09-30
EP0177676A2 (fr) 1986-04-16

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