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WO1982000656A1 - Procede d'hydrogenation de charbon - Google Patents

Procede d'hydrogenation de charbon Download PDF

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Publication number
WO1982000656A1
WO1982000656A1 PCT/DE1981/000125 DE8100125W WO8200656A1 WO 1982000656 A1 WO1982000656 A1 WO 1982000656A1 DE 8100125 W DE8100125 W DE 8100125W WO 8200656 A1 WO8200656 A1 WO 8200656A1
Authority
WO
WIPO (PCT)
Prior art keywords
hydrogenation
reaction
vapors
gases
hydrogen
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.)
Ceased
Application number
PCT/DE1981/000125
Other languages
German (de)
English (en)
Inventor
Ag Saarbergwerke
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.)
Saarbergwerke AG
Original Assignee
Saarbergwerke AG
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 Saarbergwerke AG filed Critical Saarbergwerke AG
Publication of WO1982000656A1 publication Critical patent/WO1982000656A1/fr
Anticipated expiration legal-status Critical
Ceased 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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • C10G1/083—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts in the presence of a solvent

Definitions

  • the invention relates to a process for the hydrogenation of coal, in which coal is stirred with a grinding oil to a paste, pumped to pressure, heated to the light-off temperature of the hydrogenation and hydrogenated in a reactor system consisting of a plurality of reaction chambers connected in series in the presence of catalyst and hydrogen and in which the hydrogenation product withdrawn from the reactor system is broken down into a gaseous or vaporous and a solid-containing liquid phase and the individual phases are passed on for further working up.
  • the coal is pumped to hydrogenation pressure in the form of a suspension of approximately equal parts of coal and grinding oil together with the catalyst and approximately 50% of the required hydrogen, then onto the On Spring temperature of the hydrogenation heated and then hydrogenated in a reactor system consisting of several reaction rooms connected in series.
  • the residual hydrogen still required for the hydrogenation is fed as cold gas to the control of the exothermic hydrogenation reactions.
  • the hydrogenation product obtained at the outlet of the reactor system is broken down into a gaseous or vaporous and a solids-containing liquid phase in a downstream hot separator and processed further in the further parts of the plant to give the desired end products.
  • the invention has for its object to improve the economy of a method for coal hydrogenation of the type mentioned by reducing investment and operating costs.
  • This object is achieved in that at least between two reaction spaces from what is there Hydrogen intermediate separated at least part of the gases and vapors and the remaining product is fed to the downstream reactor.
  • the procedure according to the invention now enables the hydrogenation reactions to be carried out at a pressure reduced by the sum of the partial pressures of the separated hydrogen-free gases and vapors.
  • the hydrogen required for the hydrogenation reactions at a certain pressure was replaced by the gases and vapors, such as e.g. Methane, carbon monoxide, carbon dioxide, naphtha vapors, water vapor, etc., greatly diluted, so that to maintain the hydrogen supply for the hydrogenation, a total pressure increased by the partial pressures of the components mentioned was necessary.
  • these gases and vapors can no longer contribute to the dilution of the hydrogen, so that the hydrogenation reactions can be carried out at a lower pressure.
  • a further advantage is that the distillates in the naphtha and medium oil range, which are formed in vapor form and are present in vapor form, as well as evaporated parts of the grinding oil, no longer pass through the entire reactor system, but rather are separated from the hydrogenation intermediate product immediately after their formation.
  • the residence time of these components in the reactor system is therefore considerable is reduced, thereby reducing the occurrence of undesired cleavage reactions which, with additional hydrogen consumption, lead to further gas and vapor formation.
  • the removed gases and vapors can no longer act as supercritical extractants in subsequent reaction spaces, as a result of which less heavy distillates which are liquid under the hydrogenation conditions are removed from the liquid phase and are thus retained as an important hydrogen intermediate carrier for the system.
  • the molecular hydrogen preferably does not attach directly to the coal. Rather, distillates that are present are initially further hydrogenated in an intermediate step, but these then pass on the hydrogen to the coal in the atomic state.
  • Another important advantage of the new process is that, owing to the reduced gas and steam throughput through the reactor system, the degree of filling of the individual reaction spaces and thus their reaction space utilization is considerably increased. With the same coal throughput, the individual reaction spaces can now be made smaller, which leads to a further saving in investment costs.
  • the gases and vapors can be separated off from the hydrogenation intermediate either directly at the top or within the respective reaction space or in one between two reactors separators. At least partially, the separated gases and vapors can then be fed to the withdrawing top product of the hot separator downstream of the reactor system and can be worked up together with it.
  • fresh hydrogen is added in finely divided form to each reaction space of the reactor system, the amount of hydrogen metered in expediently corresponding approximately to the hydrogen consumption in the respective reaction space, i.e. just as much hydrogen is supplied as is necessary to maintain the hydrogen partial pressure required for the implementation.
  • the fresh hydrogen is expediently fed in without prior heating, so that it can contribute to temperature stabilization and thus to the desired isothermal mode of operation.
  • the fresh hydrogen can be supplied by admixing to the hydrogenation intermediate product flowing to the respective reaction space and / or by direct feeding into the reaction space.
  • a device for carrying out the process contains a reactor system consisting of several reaction rooms connected in series and a hot separator connected downstream of the reactor system and is characterized in that a separator is arranged at least between two reaction rooms of the reactor system, the head of which is connected via a controllable gas or steam line communicates with the gas or steam extraction line of the hot separator and its sump via a further line with the lower region of the subsequent reaction space.
  • fresh coal, catalyst and rubbing oil are fed via lines 1, 2 and 3 to a mixing container 4 and mixed there to a slurry.
  • the ratio of fresh coal to grinding oil is approximately 1: 1.
  • the coal pulp is pumped by means of a high-pressure pump 5 to approximately the hydrogenation pressure of approximately 250 bar and intimately mixed with hot gases and vapors in a mixing zone 6, the origin of which is explained further below.
  • the product of the mixing zone 6 is broken down into its phases in a separator 7.
  • the gas or vapor phase from the top of the separator which in addition to water vapor, carbon monoxide, carbon dioxide, methane and other gases, the distillates produced in the Contains naphtha and medium oil area is cooled in a heat exchanger 9 against fresh hydrogen.
  • Some of the distillates which condense out are fed via lines 22 and 3 to the mixing container 4 as grinding oil, while the remaining residual product flows via line 23 to a work-up (not shown here).
  • the bottom product of the separator 7 contains the entire fresh coal to be hydrogenated and the catalyst. It is fed to the first reaction chamber 11 of a reactor system consisting of two reaction chambers 11 and 15 by means of a feed pump 8 together with the hydrogen supplied via a line 10.
  • the hydrogenation intermediate product obtained at the top of the first hydrogenation reactor 11 contains, as solid components, the as yet unreacted coal, the ash already present and the catalyst, heavy distillate oils and bitumen as liquid components and, as gaseous and vaporous components, essentially methane and other low-boiling hydrocarbons, carbon monoxide , Carbon dioxide, water vapor, naphtha and medium oil vapors, etc.
  • the hot top product of the hot separator flows together with the gases and vapors from line 13 to the mixing tube 6 and mixes there intimately with the fresh coal pulp.
  • the coal pulp is strongly heated in direct heat exchange, so that complex heat exchangers and also the otherwise usual preheater for heating the coal pulp to the light-off temperature of the hydrogenation can be dispensed with.
  • the bottom product of the hot separator 17 is fed via a line 19 into a vacuum distillation system 24.
  • the resulting vacuum residue is drawn off via a line 21, while the vacuum oil obtained is at least partially made available as a grinding oil for the fresh coal via a line 20.
  • the reactor system does not consist of several reaction spaces connected in series, but only of a single reactor, it proves to be expedient that in the reactor to separate gases and vapors formed before they have flowed through the entire reactor. This can be done, for example, by one or more gas collection funnels arranged one above the other in the reactor, through which the gases and vapors are collected and removed from the reactor separately from the remaining reactor contents.

Landscapes

  • 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)

Abstract

Procede d'hydrogenation de charbon, cette hydrogenation s'effectuant en presence d'un catalyseur et d'hydrogene, dans un systeme de reacteur, qui se compose d'une suite de dispositifs de reaction connectes en serie (11, 15); le procede se distingue par le fait qu'au moins entre deux de ces dispositifs de reaction (11, 15) l'on extrait du produit d'hydrogenation intermediaire obtenu dans ces dispositifs de reaction au moins un courant partiel de gaz et de vapeurs, le courant gazeux restant etant alors introduit seul dans le reacteur proprement dit; les reactions d'hydrogenation s'effectuent alors dans ce reacteur a une pression absolue inferieure a la norme, la valeur de cette pression etant diminuee par la somme des pressions partielles que fournirait l'extraction; en effet, ces gaz et vapeurs extraites ne contiennent plus d'hydrogene et dilueraient l'hydrogene dans le reacteur. Le passage reduit de gaz et de vapeur au travers du systeme de reacteur permet en outre d'augmenter le degre de remplissage et d'assurer ainsi un meilleur rendement des dispositifs de reaction (11, 15). Pour une meme quantite de charbon traite, il est possible de cette maniere de reduire la dimension des dispositifs de reaction (11, 15), ce qui, a nouveau, permet d'obtenir une economie serieuse dans les couts d'investissement et de fabrication.
PCT/DE1981/000125 1980-08-21 1981-08-17 Procede d'hydrogenation de charbon Ceased WO1982000656A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3031477A DE3031477C2 (de) 1980-08-21 1980-08-21 Verfahren zum Hydrieren von Kohle
DE3031477800821 1980-08-21

Publications (1)

Publication Number Publication Date
WO1982000656A1 true WO1982000656A1 (fr) 1982-03-04

Family

ID=6110059

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/DE1981/000125 Ceased WO1982000656A1 (fr) 1980-08-21 1981-08-17 Procede d'hydrogenation de charbon

Country Status (3)

Country Link
AU (1) AU549040B2 (fr)
DE (1) DE3031477C2 (fr)
WO (1) WO1982000656A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1984002347A1 (fr) * 1982-12-16 1984-06-21 Gfk Kohleverfluessigung Gmbh Procede pour hydrogener du charbon
CN104877700A (zh) * 2015-06-08 2015-09-02 中美新能源技术研发（山西）有限公司 一种新型粉煤热解加氢反应器及热解加氢反应方法
WO2016128187A1 (fr) * 2015-02-13 2016-08-18 Siemens Aktiengesellschaft Procédé pour réaliser une synthèse chimique et réacteur de synthèse

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3534565A1 (de) * 1984-09-29 1986-04-03 Nippon Kokan K.K., Tokio/Tokyo Verfahren zum verfluessigen von kohle

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE591099C (de) * 1928-04-16 1934-01-16 Bataafsche Petroleum Verfahren zur Herstellung von fluessigen bzw. niedriger siedenden Produkten aus Kohle, Teeren, Mineraloelen u. dgl.
US3594305A (en) * 1970-01-23 1971-07-20 Sun Oil Co Process for hydrogenation of coal
DE2651253A1 (de) * 1976-11-10 1978-05-11 Saarbergwerke Ag Verfahren zum hydrieren von kohle
DE2711105A1 (de) * 1977-03-15 1978-09-28 Saarbergwerke Ag Verfahren zum verfluessigen von kohle

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3640816A (en) * 1969-12-08 1972-02-08 Gulf Research Development Co Multiple stage process for producing light liquids from coal

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE591099C (de) * 1928-04-16 1934-01-16 Bataafsche Petroleum Verfahren zur Herstellung von fluessigen bzw. niedriger siedenden Produkten aus Kohle, Teeren, Mineraloelen u. dgl.
US3594305A (en) * 1970-01-23 1971-07-20 Sun Oil Co Process for hydrogenation of coal
DE2651253A1 (de) * 1976-11-10 1978-05-11 Saarbergwerke Ag Verfahren zum hydrieren von kohle
DE2711105A1 (de) * 1977-03-15 1978-09-28 Saarbergwerke Ag Verfahren zum verfluessigen von kohle

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1984002347A1 (fr) * 1982-12-16 1984-06-21 Gfk Kohleverfluessigung Gmbh Procede pour hydrogener du charbon
WO2016128187A1 (fr) * 2015-02-13 2016-08-18 Siemens Aktiengesellschaft Procédé pour réaliser une synthèse chimique et réacteur de synthèse
AU2016218191B2 (en) * 2015-02-13 2018-04-19 Siemens Aktiengesellschaft Method for carrying out a chemical synthesis and synthesis reactor
US10562003B2 (en) 2015-02-13 2020-02-18 Siemens Aktiengesellschaft Chemical synthesis and synthesis reactors
CN104877700A (zh) * 2015-06-08 2015-09-02 中美新能源技术研发（山西）有限公司 一种新型粉煤热解加氢反应器及热解加氢反应方法

Also Published As

Publication number Publication date
AU549040B2 (en) 1986-01-09
DE3031477C2 (de) 1986-09-18
AU7532881A (en) 1982-03-17
DE3031477A1 (de) 1982-03-25

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