EP0151399A2 - Distribution du gaz d'hydrogène dans des unités de liquéfaction de charbons - Google Patents

Distribution du gaz d'hydrogène dans des unités de liquéfaction de charbons Download PDF

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Publication number
EP0151399A2
EP0151399A2 EP85100277A EP85100277A EP0151399A2 EP 0151399 A2 EP0151399 A2 EP 0151399A2 EP 85100277 A EP85100277 A EP 85100277A EP 85100277 A EP85100277 A EP 85100277A EP 0151399 A2 EP0151399 A2 EP 0151399A2
Authority
EP
European Patent Office
Prior art keywords
gas
hydrogenation
hydrogen
coal liquefaction
coal
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
EP85100277A
Other languages
German (de)
English (en)
Other versions
EP0151399B1 (fr
EP0151399A3 (en
Inventor
Eckard Dr.-Ing. Wolowski
Hans-Friedrich Tamm
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
Priority claimed from DE19843401650 external-priority patent/DE3401650A1/de
Application filed by Ruhrkohle AG filed Critical Ruhrkohle AG
Publication of EP0151399A2 publication Critical patent/EP0151399A2/fr
Publication of EP0151399A3 publication Critical patent/EP0151399A3/de
Application granted granted Critical
Publication of EP0151399B1 publication Critical patent/EP0151399B1/fr
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
    • 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

  • the invention relates to a hydrogenation gas flow in coal liquefaction plants, light and medium oil obtained after the hydrogenation being refined.
  • Dried coal is usually mashed with solvent and hydrogenated with the addition of hydrogen.
  • the reaction products are separated in the separators downstream of the hydrogenation reactors. Gases and vapors are drawn off overhead in the hot separator; a liquid phase, which contains the solids, is removed from the sump into the vacuum distillation.
  • the top product of the hot separator is fed to the downstream cold separator. Together with the KOHLEUL, water is obtained as the liquid phase, from which the valuable ingredients (ammonia, phenol) are obtained in subsequent process stages.
  • the overhead gas phase of the cold separator is put into circulation and discharge gas after an oil wash carried out under process pressure.
  • the circuit oas is returned to the hvdrieruno with a circuit aa compressor after the pressure has been lost.
  • the Ausschleusoas is ⁇ reiniot in a gas scrubber and in a Tieftem D eratur- zerleounasanlaae in hydrogen, fuel gas, LPG and SNG disassembled.
  • the hydrogen fraction is mixed with the fresh hydrogen from the hydrogenation.
  • the COAL OIL In atmospheric distillation, the COAL OIL is separated into light, medium and heavy oil.
  • the heavy oil is returned as a solvent to the mashing mixture.
  • the light and medium oil fractions are each subjected to a hydrogenating refining in order to remove sulfur, nitrogen and similar undesirable additives. This is done after adding water
  • the raw light or raw medium oil evaporates and is introduced into fixed bed reactors. Refining is carried out on the Co-Mo or Ni-Mo catalyst layers.
  • hydrogen fluoride is introduced into the hydrogenation reactors.
  • the emerging refined products are cooled in heat exchangers and single-seated by fresh water and separated into raffinate, water and gas in separators.
  • the state of the art is to return a portion of the H 2 -rich excess gas to the fresh hydrogen for refining as a recycle gas after compensation for the pressure loss with a recycle gas compressor and to discharge the other excess gas portion for cleaning and recovery of the hydrogen and the gaseous hydrocarbons and to supply appropriate process stages.
  • the solid-containing residue of the hot separator is topped in a vacuum distillation.
  • the heavy oil obtained is together with heavy and medium oil from the atm. Distillation as a solvent returned to the mash.
  • Synthesis gas (CO + H x ) is obtained from the residue from the vacuum distillation in a gasification stage or, after conversion and gas scrubbing, hydrogen hydrogen.
  • the deficit can be covered by coal gasification with downstream conversion and gas cleaning or external supply.
  • the invention has for its object to simplify the Hydrierqas Office and improve it economically.
  • this is achieved in that the total amount of gases obtained in the refining stages (20 + 21) is fed to the fresh hydrogen for hydrogenation.
  • the organic (C 1 -C 4 ) and inorganic (CO, CO 2 , H 2 S) gaseous compounds contained in the gas in addition to the hydrogen produced during refining impair the hydrogenation of the coal in the present concentration
  • they are discharged or extracted with the same gaseous compounds that are additionally formed during the hydrogenation of the coal via gas scrubbing and low-temperature separation.
  • the hydrogenation gas guide according to the invention is shown in the form of a flow diagram.
  • Dried coal is mashed with solvent in a slurry (1) and hydrogenated in a reactor (2) with the addition of hydrogen.
  • a phase separation is carried out in the hot separator (3) downstream of the hydrogenation reactor (2).
  • the gases and vapors are drawn off overhead.
  • a liquid phase, which contains the solids, is removed from the sump into the vacuum distillation (5).
  • the top product of the hot separator is passed into the cold separator (4).
  • water is produced here, which is pumped off separately to recover valuable ingredients (ammonia, phenol).
  • the KOHLEOL is drawn off and atmospheric with the addition of stripping steam in one atm. Distillation (6) distilled. Light and medium oil of atm. Distillation is fed to separate refining stages (21 and 22).
  • the gas phase leaving the cold separator at the top is divided in an oil scrubber (7) into recirculated and discharged gas.
  • the discharge gas is cleaned in a gas scrubber (8) and broken down into hydrogen, heating gas, SNG and LPG in a low-temperature separation plant (9).
  • the solid-containing liquid phase obtained in the hot separator is topped in vacuum distillation (5).
  • the resulting heavy oil is extracted from the atm together with heavy and medium oil. Distillation as solvent in the slurry (1).
  • Hydrogen hydrogen is obtained from the residue from the vacuum distillation in a gasification stage (10) synthesis gas (CO + H z ) or in a conversion and gas scrubbing (11).
  • the cycle gas obtained from the ul wash (7) is compressed to the necessary operating pressure by a cycle gas compressor (27).
  • the total amount of hydrogen-rich gases emerging from the refining stages (21 + 22) is fed in again. These gases are fed as a mixture to the hydrogenation (2) and compressed by a compressor (28) to the operating pressure required for the hydrogenation.
  • the raw light oil is refined in two stages with the addition of 3,138 kg / h (stage I) and 2,587 kg / h (stage II) hydrogen with a purity of 98.5% by volume at 60 bar.
  • stage I 3,138 kg / h
  • stage II 2,587 kg / h
  • hydrogen-rich gas phase total amount 5,629 kg / h
  • This amount of gas is fed directly to the hydrogenation gas.
  • the raw oil is refined in one step with the addition of 9,873 kg / h of hydrogen (98.5% by volume), also at 60 bar.
  • the gas produced in the downstream separator (9,565 kg / h is in turn fed directly to the coal hydrogenation.
  • the hydrogen content of the hydrogenation gas flowing through the refining stages drops to 98.0 vol.% In the case of the light oil or to 97.5 vol .% for middle oil.
  • H 2 partial pressures are significantly higher than that of the hydrogenation gas from the coal hydrogenation (216,252 kg / h, 85% by volume), so that feeding is possible without problems.

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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
EP85100277A 1984-01-19 1985-01-12 Distribution du gaz d'hydrogène dans des unités de liquéfaction de charbons Expired EP0151399B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19843401650 DE3401650A1 (de) 1983-12-10 1984-01-19 Hydriergasfuehrung in kohleverfluessigungsanlagen
DE3401650 1984-01-19

Publications (3)

Publication Number Publication Date
EP0151399A2 true EP0151399A2 (fr) 1985-08-14
EP0151399A3 EP0151399A3 (en) 1987-05-13
EP0151399B1 EP0151399B1 (fr) 1989-08-02

Family

ID=6225291

Family Applications (1)

Application Number Title Priority Date Filing Date
EP85100277A Expired EP0151399B1 (fr) 1984-01-19 1985-01-12 Distribution du gaz d'hydrogène dans des unités de liquéfaction de charbons

Country Status (10)

Country Link
EP (1) EP0151399B1 (fr)
JP (1) JPS60161483A (fr)
AU (1) AU582133B2 (fr)
BR (1) BR8500578A (fr)
CA (1) CA1239366A (fr)
DD (1) DD236340A5 (fr)
DE (1) DE3572001D1 (fr)
PL (1) PL141658B1 (fr)
SU (1) SU1473714A3 (fr)
ZA (1) ZA85428B (fr)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3519830A1 (de) * 1985-06-03 1986-12-18 Ruhrkohle Ag, 4300 Essen Verfahren zur kohlehydrierung mit integrierten raffinationsstufen
ITMI20032207A1 (it) * 2003-11-14 2005-05-15 Enitecnologie Spa Procedimento integrato per la conversione di cariche contenenti carbone in prodotti liquidi.
CN1257252C (zh) * 2004-07-30 2006-05-24 神华集团有限责任公司 一种煤炭直接液化的方法

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4179352A (en) * 1975-08-07 1979-12-18 Exxon Research & Engineering Co. Coal liquefaction process
JPS5681390A (en) * 1979-12-07 1981-07-03 Chiyoda Chem Eng & Constr Co Ltd Multistage hydrogenation treatment of coal
US4400263A (en) * 1981-02-09 1983-08-23 Hri, Inc. H-Coal process and plant design
CA1199293A (fr) * 1982-06-17 1986-01-14 Chevron Research And Technology Company Hydrotraitement bi-etage des petroles lourds, avec recyclage des residus

Also Published As

Publication number Publication date
SU1473714A3 (ru) 1989-04-15
EP0151399B1 (fr) 1989-08-02
EP0151399A3 (en) 1987-05-13
DE3572001D1 (en) 1989-09-07
ZA85428B (en) 1986-04-30
CA1239366A (fr) 1988-07-19
JPS60161483A (ja) 1985-08-23
AU3772085A (en) 1985-07-25
DD236340A5 (de) 1986-06-04
AU582133B2 (en) 1989-03-16
PL141658B1 (en) 1987-08-31
BR8500578A (pt) 1985-09-24
PL251583A1 (en) 1985-11-05

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