EP0318694A2 - Procédé d'hydrogénation de matières carbonées solides - Google Patents

Procédé d'hydrogénation de matières carbonées solides Download PDF

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Publication number
EP0318694A2
EP0318694A2 EP88117543A EP88117543A EP0318694A2 EP 0318694 A2 EP0318694 A2 EP 0318694A2 EP 88117543 A EP88117543 A EP 88117543A EP 88117543 A EP88117543 A EP 88117543A EP 0318694 A2 EP0318694 A2 EP 0318694A2
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EP
European Patent Office
Prior art keywords
gas
hydrogenation
stream
heat exchanger
phase
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.)
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Application number
EP88117543A
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German (de)
English (en)
Other versions
EP0318694A3 (fr
Inventor
Ulrich Bönisch
Alfons Feuchthofen
Eckhard Dr. Wolowski
Frank Dr. Mirtsch
Wolfdieter Klein
Claus Strecker
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
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 Ruhrkohle AG filed Critical Ruhrkohle AG
Publication of EP0318694A2 publication Critical patent/EP0318694A2/fr
Publication of EP0318694A3 publication Critical patent/EP0318694A3/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
    • 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
    • C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
    • C10G1/065—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation in the presence of a solvent

Definitions

  • the invention relates to a process for the hydrogenation of solid carbonaceous feedstocks according to the preamble of claim 1. Temperatures in the bottom phase reactor of about 400 to 500 ° C and in the gas phase reactor of about 370 to 450 ° C are typical, and the process pressure can be between 150 to 1200 bar can be selected.
  • a method is also known in which heavy oil is fed as a feed product to a preheater and in which a partial stream of the total amount of hydrogenation gas required, which is heated in a gas heat exchanger through which the hot separator head product flows, preheats the preheated mixture of heavy oil, additive and hydrogenation gas Entry into the bottom phase reactor is added (see. DE 35 23 709 Al).
  • This process with separate hydrogenation gas heating had also already been proposed for coal hydrogenation (cf. DE 35 05 553 Al).
  • the process-relevant parameters especially the defined inlet temperatures of the sump phase and gas phase reactors and the defined temperature in the intermediate separator - must be adjustable. These temperature settings are made more difficult by variable heat transfer rates due to contamination of the mash heat exchangers.
  • the special conditions for the joint heating of mash and hydrogenation gas in the heat exchangers when driving with integrated gas phase hydrogenation must be taken into account; because it is known that there is an increased risk of drying out of the heat exchanger due to oil stripping by hydrogenation gas due to changed solvent quality.
  • the exothermic heat of reaction from the sump phase and gas phase hydrogenation should be optimally used for heat recovery in order to achieve a heat-self-sufficient process or to keep the required additional heating small; the mash heating furnace should be avoided if possible, since this is one of the most critical components of any bottom phase hydrogenation.
  • the defined process temperatures in the gas phase reactor and in the intermediate separator are set by means of external cooling, but without taking into account the heat recovery and the variable heat transfer performance of the mash heat exchanger due to increasing pollution.
  • the increased risk of mash drying out in the heat exchangers is reduced by reducing the amount of hydrogenation gas in the mash heating path - the majority of the amount of hydrogenation gas is heated in separate gas heat exchangers; the setting of the two above So far, defined temperatures have not been taken into account.
  • the two methods have the disadvantage that the heat exchanger for heating the liquid / solid gas mixture after the gas phase reactor - d. H. is arranged at a comparatively lower temperature level - and therefore no maximum heating of the liquid / solid gas mixture is guaranteed.
  • the furnace for heating the liquid / solid gas mixture the so-called mash furnace, is reduced in capacity compared to the earlier hydrogenation processes, but it is not omitted.
  • the object of the invention is to design the process sequence so that, firstly, the process-relevant temperatures in the gas phase reactor and in the intermediate separator can be set despite variable heat exchange performance of the mash heat exchangers, secondly, drying out of the mash in the mash heat exchangers is avoided and thirdly, the reaction heats of the bottom phase and gas phase hydrogenation a self-sufficient or thermally optimized process can be used.
  • the defined temperature settings are made in the gas phase reactor and in the intermediate separator by gas heat exchangers with bypass operation, with indirect heat exchange taking place in the gas heat exchangers between the hot separator head product and the separately heated hydrogenation gas and the bypass being on the hydrogenation gas side.
  • the separate gas heating also eliminates the risk of mash drying.
  • the defined temperature setting in the gas phase reactor is also carried out according to the invention by a bypass on the mash heat exchanger on the hot separator head product side, which is arranged between the hot separator and the gas phase reactor, and by different feeds of vacuum gas oil on the path of the hot separator head product to the gas phase reactor.
  • optimal mash heating is achieved in that, using the heat of reaction from the bottom phase and gas phase hydrogenation, the hot separator top product transfers its heat to the mash-hydrogenation gas mixture by indirect heat exchange at a respectively high temperature level and to the hydrogenation gas to be heated separately at a respectively lower temperature level.
  • the hydrogenation gas furnace is then bypassed as a rule during normal operation and is only required for starting.
  • the mash stream (3) is passed through three heat exchangers (18), (19), (20) and the hydrogen gas stream (5) to be heated separately before entering the hydrogenation gas oven (24) three heat exchangers (21), (22), (23) in countercurrent to the hot separator head product (9).
  • the procedure can also be such that fresh hydrogen as a feed is provided for the mash stream and the cycle hydrogenating gas is provided for the second partial stream of the hydrogenation gas.
  • stream (9) in the downstream direction comes into heat exchange relationship with the mash stream (3) in heat exchanger (20) and the partial stream of hydrogenation gas (5) in heat exchanger (23) and passes through a reactor (27) for hydrogenation in the gas phase at a fixed bed contact .
  • the inlet temperature in the gas phase reactor (27) is, depending on the degree of contamination of the mash heat exchangers (18), (19) and (20), bypassing the heat exchangers (20) and (23) and via alternative vacuum gas oil feeds (32) in front of the heat exchangers (20) and ( 23) and by vacuum gas oil feed and quench gas feed in front of the gas phase reactor (27).
  • the product stream refined in reactor (27) passes through stream (10) heat exchanger (19) and heat exchanger (22) in heat exchange relationship with stream (3) or stream (5) and one Intermediate separator (28) with separation of a hot oil fraction (11).
  • the temperature in the intermediate separator (28) is set by bypassing in the heat exchanger (22).
  • the residual stream (12) drawn off by the separator (28) gives off in the heat exchangers (18) and (21) its remaining heat, which can be used for heating the feed products, to stream (3) and stream (5) and is transferred via a water cooler (31).
  • a gas scrubber can be provided in the usual way for working up the circulating hydrogen gas fraction. Such a work-up ensures a sufficient hydrogen partial pressure in the hydrogenation gas system by removing the C1 to C4 components which are soluble in the gas scrubbing by means of washing liquid.
  • the separate partial stream from the total amount of hydrogenation gas to be used can make up 20 to 95, preferably 40 to 80% of the total amount of hydrogenation gas required.
  • the defined temperature in the intermediate separator (28) is not via the gas heat exchanger (22) with bypass setting but set by means of the bypass procedure of the mash heat exchanger (19).
  • a comparatively larger exchange surface is required for the mash heat exchanger (19); however, the gas heat exchanger (22) is omitted.

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)
EP88117543A 1987-12-04 1988-10-21 Procédé d'hydrogénation de matières carbonées solides Withdrawn EP0318694A3 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19873741104 DE3741104A1 (de) 1987-12-04 1987-12-04 Verfahren zur hydrierung fester kohlenstoffhaltiger einsatzstoffe
DE3741104 1987-12-04

Publications (2)

Publication Number Publication Date
EP0318694A2 true EP0318694A2 (fr) 1989-06-07
EP0318694A3 EP0318694A3 (fr) 1990-03-21

Family

ID=6341870

Family Applications (1)

Application Number Title Priority Date Filing Date
EP88117543A Withdrawn EP0318694A3 (fr) 1987-12-04 1988-10-21 Procédé d'hydrogénation de matières carbonées solides

Country Status (4)

Country Link
EP (1) EP0318694A3 (fr)
JP (1) JPH01172491A (fr)
DE (1) DE3741104A1 (fr)
PL (1) PL158461B1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111849543A (zh) * 2020-07-08 2020-10-30 张家港保税区慧鑫化工科技有限公司 一种液相加氢进料预热系统及工艺

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10032316A1 (de) * 2000-07-04 2002-01-17 Studiengesellschaft Kohle Mbh Hydrierung/Hydrogenolyse von Steinkohle mit Boran-Katalysatoren

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0058327A2 (fr) * 1981-02-12 1982-08-25 BASF Aktiengesellschaft Procédé de préparation en continu d'huiles hydrocarburées à partir de charbon par hydrogénation sous pression
EP0177676A2 (fr) * 1984-09-13 1986-04-16 Ruhrkohle Aktiengesellschaft Réglage par récupération de la chaleur d'un procédé d'hydrogénation en suspension avec hydrogénation en phase gazeuse intégrée
DE3505553A1 (de) * 1985-02-18 1986-08-21 Veba Oel Entwicklungs-Gesellschaft mbH, 4650 Gelsenkirchen Verfahren zur vorbehandlung der einsatzprodukte fuer die kohlehydrierung

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2936008A1 (de) * 1979-09-06 1981-04-02 Saarbergwerke AG, 6600 Saarbrücken Verfahren zum hydrieren von kohle

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0058327A2 (fr) * 1981-02-12 1982-08-25 BASF Aktiengesellschaft Procédé de préparation en continu d'huiles hydrocarburées à partir de charbon par hydrogénation sous pression
EP0177676A2 (fr) * 1984-09-13 1986-04-16 Ruhrkohle Aktiengesellschaft Réglage par récupération de la chaleur d'un procédé d'hydrogénation en suspension avec hydrogénation en phase gazeuse intégrée
DE3505553A1 (de) * 1985-02-18 1986-08-21 Veba Oel Entwicklungs-Gesellschaft mbH, 4650 Gelsenkirchen Verfahren zur vorbehandlung der einsatzprodukte fuer die kohlehydrierung

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111849543A (zh) * 2020-07-08 2020-10-30 张家港保税区慧鑫化工科技有限公司 一种液相加氢进料预热系统及工艺

Also Published As

Publication number Publication date
PL158461B1 (pl) 1992-09-30
EP0318694A3 (fr) 1990-03-21
PL276161A1 (en) 1989-07-24
JPH01172491A (ja) 1989-07-07
DE3741104A1 (de) 1989-06-15

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