EP0182992B1 - Energiegünstiges Verfahren zur Erzeugung von Synthesegas mit einem hohen Methangehalt - Google Patents

Energiegünstiges Verfahren zur Erzeugung von Synthesegas mit einem hohen Methangehalt Download PDF

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Publication number
EP0182992B1
EP0182992B1 EP85111795A EP85111795A EP0182992B1 EP 0182992 B1 EP0182992 B1 EP 0182992B1 EP 85111795 A EP85111795 A EP 85111795A EP 85111795 A EP85111795 A EP 85111795A EP 0182992 B1 EP0182992 B1 EP 0182992B1
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EP
European Patent Office
Prior art keywords
gas
synthesis gas
reactor
heated
methane
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
Application number
EP85111795A
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German (de)
English (en)
French (fr)
Other versions
EP0182992A2 (de
EP0182992A3 (en
Inventor
Peter Dr.-Ing. Heinrich
Klaus Dr.-Ing. Knop
Friedbert Dr.-rer. nat. Rübe
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.)
MAN Gutehoffnungshutte GmbH
Original Assignee
MAN Gutehoffnungshutte GmbH
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 MAN Gutehoffnungshutte GmbH filed Critical MAN Gutehoffnungshutte GmbH
Publication of EP0182992A2 publication Critical patent/EP0182992A2/de
Publication of EP0182992A3 publication Critical patent/EP0182992A3/de
Application granted granted Critical
Publication of EP0182992B1 publication Critical patent/EP0182992B1/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
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • C10J2300/1675—Integration of gasification processes with another plant or parts within the plant with the production of electricity making use of a steam turbine
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S48/00—Gas: heating and illuminating
    • Y10S48/01—Recirculation of gases produced to lower part of fuel bed

Definitions

  • the invention relates to a process for the production of synthesis gas, in which the synthesis gas obtained in a reactor by gasification of C-containing fuel and containing methane as a by-product is cooled in a regenerator and subjected to a gas treatment, and part of the gas as recycle gas is returned to the reactor is supplied together with combustion gas and C-containing fuel, the gas being heated by the regenerator before re-entering the reactor.
  • EP-A-108 198 Also known from EP-A-108 198 is a method for operating a gasification reactor for generating synthesis gas, in which, however, no methane is formed. Some of the waste heat from the synthesis gas generated is returned to the circuit after gas conditioning. In order to increase the economy, the cycle gas is heated by the exhaust gas heat of the reactor before re-entry into the gasification reactor. The heat exchange between hot synthesis gas and cold cycle gas takes place via heat exchangers.
  • the invention has for its object to provide a method for generating synthesis gas with a relatively high methane content, which has a particularly low energy consumption and can therefore be carried out particularly economically.
  • the process is also said to do without a conversion step and to provide a synthesis gas which is particularly suitable for direct ore reduction.
  • This object is achieved in a method according to the invention in that the gas is further cooled in the gas preparation in a 4-pole heat exchanger and a condenser, is subjected to a gas scrub to remove the main part of methane and carbon dioxide and after re-passage through the 4-pole heat exchanger is heated and fed to a heater, and that at least part of the additional process steam formed in the heater is fed to the gasification reactor.
  • the raw gas is cooled to the extent that it passes below its dew point after passing through the regenerator in the 4-pole heat exchanger and the condenser.
  • the heat energy extracted from the gas is not dissipated, but is fed back into the circuit at the points where the heat energy is required.
  • a hydrogen-rich synthesis gas for ore direct reduction can be produced in a simple manner, methane also being obtained as a valuable by-product, which is partly used to operate the heater and also as synthesis gas for producing chemical products, for. B. in the production of methanol, or can be used as fuel gas in other processes.
  • the method further provides that oxygen is introduced as combustion gas into the gasification reactor.
  • oxygen is introduced as combustion gas into the gasification reactor.
  • the oxygen improves the gasification behavior of the coal. It is advantageous for the energy balance of the process if part of the excess process steam energy is used to generate oxygen for the reactor.
  • carbon is fed to a fluidized bed reactor 1 in the form of fine-grained, reactive coal dust.
  • Highly heated process steam, oxygen and cycle gas are passed into the reactor 1 as gasifying agents for the coal dust.
  • the composition of the cycle gas is shown in Table 1, column 3.0.
  • the coal is gasified at a temperature of 800 ° C. and a pressure of 10 bar.
  • the ash produced during coal gasification is withdrawn from the bottom of the reactor.
  • the synthesis gas leaves the reactor overhead with a composition according to column 4.0, table 1.
  • the synthesis gas After passing through a fly ash or dust separator 2, the synthesis gas then enters the cooling element of a regenerator 3, in which it is cooled from 800 ° C. to 578 ° C.
  • a regenerator 3 Suitable regenerators that extract heat from a hot gas stream via a cooling element, store it and transfer the storage heat to another gas stream via a heating element are known to the person skilled in the art, for. B. known from blast furnace technology and glass production and therefore do not need to be described in particular.
  • the gas is cooled further in a 4-pole heat exchanger 4 and a condenser 5, in which the gas is cooled down to 60 ° C.
  • the condensate water accumulating in the condenser 5 is drained off.
  • the gas is subjected to a so-called PSA gas scrubbing at 6, through which the methane and carbon dioxide content of the synthesis gas is selectively separated from the gas stream.
  • PSA gas scrubbing is a well-known absorption process, in which certain, from one Gas flow to be separated gases are absorbed on a solid and then by a purge gas, for. B. nitrogen, are removed after depressurization. The separated methane and carbon dioxide are removed from the gas cycle and are available for other use.
  • Gas scrubbing 6 significantly increases the hydrogen content of the synthesis gas, as can be seen in Table 1, column 6.0.
  • the synthesis gas now has the gas composition that is required for the later ore reduction.
  • the synthesis gas is fed to a compressor 7 and then passes through the 4-pole heat exchanger 4 again, in which it is heated to 466 ° C.
  • the gas stream passes through a heater 8, in which the process steam required in the process is additionally generated and in which the synthesis gas is heated to a high level by burning part of the methane separated off in the gas scrubber 6 after passing through the heater 8, the synthesis gas enters the reduction reactor 9 at a temperature of 900 ° C.
  • the synthesis gas is partially oxidized during the reduction and then leaves the reactor 9 with a lower-hydrogen composition according to Table 1, column 3.0.
  • This so-called blast furnace gas is fed to the heating element of the regenerator 3, by means of which it is heated to 750 ° C. and is then re-introduced into the reactor 1 as a circulating gas.
  • the superheated steam generated in the heater 8 drives a steam turbine 10, the output of which covers practically the entire electrical energy requirement of the method. Part of the turbine power is used to produce the oxygen required in coal gasification by air separation at 11. The oxygen is then compressed and fed to the reactor 1.
  • the steam emerging from the steam turbine 10 is fed to the reactor 1 as process steam, it having previously been heated to 750 ° C. in the regenerator 3.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Industrial Gases (AREA)
EP85111795A 1984-10-27 1985-09-18 Energiegünstiges Verfahren zur Erzeugung von Synthesegas mit einem hohen Methangehalt Expired EP0182992B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19843439487 DE3439487A1 (de) 1984-10-27 1984-10-27 Energieguenstiges verfahren zur erzeugung von synthesegas mit einem hohen methangehalt
DE3439487 1984-10-27

Publications (3)

Publication Number Publication Date
EP0182992A2 EP0182992A2 (de) 1986-06-04
EP0182992A3 EP0182992A3 (en) 1987-01-21
EP0182992B1 true EP0182992B1 (de) 1988-11-02

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EP85111795A Expired EP0182992B1 (de) 1984-10-27 1985-09-18 Energiegünstiges Verfahren zur Erzeugung von Synthesegas mit einem hohen Methangehalt

Country Status (7)

Country Link
US (1) US4678480A (enrdf_load_stackoverflow)
EP (1) EP0182992B1 (enrdf_load_stackoverflow)
AU (1) AU578312B2 (enrdf_load_stackoverflow)
BR (1) BR8505349A (enrdf_load_stackoverflow)
DE (2) DE3439487A1 (enrdf_load_stackoverflow)
IN (1) IN166503B (enrdf_load_stackoverflow)
ZA (1) ZA857652B (enrdf_load_stackoverflow)

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DE3237334A1 (de) * 1982-10-08 1984-04-12 M.A.N. Maschinenfabrik Augsburg-Nürnberg AG, 4200 Oberhausen Verfahren zum betreiben eines reaktors zur erzeugung von synthesegas und vorrichtung zur durchfuehrung des verfahrens
DE3306371A1 (de) * 1983-02-24 1984-08-30 Bergwerksverband Gmbh, 4300 Essen Verfahren zur erzeugung eines methanreichen gasgemisches, insbesondere aus grubengas

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Publication number Publication date
EP0182992A2 (de) 1986-06-04
EP0182992A3 (en) 1987-01-21
AU4786585A (en) 1986-05-01
DE3439487C2 (enrdf_load_stackoverflow) 1987-09-24
BR8505349A (pt) 1986-08-05
DE3439487A1 (de) 1986-06-26
ZA857652B (en) 1986-05-28
DE3565996D1 (en) 1988-12-08
AU578312B2 (en) 1988-10-20
IN166503B (enrdf_load_stackoverflow) 1990-05-19
US4678480A (en) 1987-07-07

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