EP2408881A1 - Gazéification de charbon avec production supplémentaire de matériaux utiles - Google Patents

Gazéification de charbon avec production supplémentaire de matériaux utiles

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Publication number
EP2408881A1
EP2408881A1 EP09841670A EP09841670A EP2408881A1 EP 2408881 A1 EP2408881 A1 EP 2408881A1 EP 09841670 A EP09841670 A EP 09841670A EP 09841670 A EP09841670 A EP 09841670A EP 2408881 A1 EP2408881 A1 EP 2408881A1
Authority
EP
European Patent Office
Prior art keywords
carbon
compounds
process according
gasification
beryllium
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.)
Withdrawn
Application number
EP09841670A
Other languages
German (de)
English (en)
Other versions
EP2408881A4 (fr
Inventor
Heinrich Morhenn
Leslaw Mleczko
Oliver Felix-Karl Schlueter
Verena Haverkamp
Fei Liu
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.)
Amina LLC LP
Original Assignee
Bayer Technology and Engineering Shanghai Co Ltd
Bayer Technology Services 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 Bayer Technology and Engineering Shanghai Co Ltd, Bayer Technology Services GmbH filed Critical Bayer Technology and Engineering Shanghai Co Ltd
Publication of EP2408881A1 publication Critical patent/EP2408881A1/fr
Publication of EP2408881A4 publication Critical patent/EP2408881A4/fr
Withdrawn legal-status Critical Current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
    • C10H—PRODUCTION OF ACETYLENE BY WET METHODS
    • C10H21/00—Details of acetylene generators; Accessory equipment for, or features of, the wet production of acetylene
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/90—Carbides
    • C01B32/914—Carbides of single elements
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/90—Carbides
    • C01B32/914—Carbides of single elements
    • C01B32/935—Carbides of alkali metals, strontium, barium or magnesium
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/90—Carbides
    • C01B32/914—Carbides of single elements
    • C01B32/942—Calcium carbide
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/08—Continuous processes with ash-removal in liquid state
    • 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
    • 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
    • C10J3/72—Other features
    • 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
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0943—Coke
    • 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
    • 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
    • C10J2300/0983—Additives
    • 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
    • C10J2300/0983—Additives
    • C10J2300/0996—Calcium-containing inorganic materials, e.g. lime
    • 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
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1628—Ash post-treatment
    • C10J2300/1634—Ash vitrification
    • 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
    • C10J2300/1838—Autothermal gasification by injection of oxygen or steam

Definitions

  • the present invention relates to a process for gasifying carbon-containing gasification materials which is characterized in that compounds are added which form carbides under the process conditions. These carbides can be used for the synthesis of useful materials, such as for example acetylene.
  • Carbides of alkali metals and alkaline earth metals and processes for their production are known from the prior art (see, for example, Ullmann's Encyclopedia of Industrial Chemistry, 2005, WileyVCH Verlag GmbH & Co. KGaA, Weinheim, "Calcium Carbide”).
  • Calcium carbide has become particularly important industrially. It can be obtained in an electric-arc furnace at 1,800 - 2,100 0 C from calcium oxide and coke. This process consumes high quantities of energy, in particular because during the production of the electricity a large proportion of the primary energy is lost. Carbon monoxide is obtained as a by-product:
  • Calcium carbide can also be produced by the direct reaction of coke with calcium oxide and oxygen (see, for example,US 2794706). In this reaction carbon monoxide is also produced as a by-product:
  • sodium carbonate can also be used (see, for example, US 2642347A):
  • the formation of sodium carbide from sodium oxide and carbon already takes place at temperatures of ⁇ 1,000 0 C and the formation of sodium oxide from sodium carbonate already begins at 1,000 0 C.
  • the production of sodium carbide from sodium oxide or sodium carbonate and carbon can therefore be carried out at considerably lower temperatures than the production of calcium carbide from calcium oxide and carbon.
  • Sodium carbide has a considerably higher vapour pressure (1 bar at 700 0 C) than the starting products sodium oxide or sodium carbonate.
  • the reactions for the production of sodium carbonate are therefore usually carried out in such a manner that sodium carbide is discharged from the reaction chamber together with carbon monoxide and is then separated from the gas stream by cooling.
  • Sodium carbide can be reacted similarly to calcium carbide to produce acetylene and sodium hydroxide.
  • the hydroxides obtained during the liberation of acetylene are important raw materials.
  • Calcium hydroxide is used in large quantities for the production of building materials and cement. It is also used for the desulphurization of flue gases and in the chemical industry, for example for the production of sodium carbonate by the Solvay process.
  • Sodium hydroxide is an important product for the chemical industry. Relatively large quantities of sodium hydroxide are also used in other fields than in the chemical industry, such as for example in the production of paper and in the processing of bauxite ores.
  • hydroxides remaining after the formation of acetylene can also be reconverted into the corresponding oxides or carbonates and thus recycled into the reaction as starting products.
  • recycling by appropriately purifying and/or discharging a fraction of the oxdies/carbonates the excessive accumulation of by-products in the circulated oxides/hydroxides is avoided.
  • Acetylene is an important product in industrial organic chemistry.
  • vinyl halides and polyvinyl halides such as for example vinyl chloride and polyvinyl chloride, are produced.
  • acetic acid vinyl acetate and polyvinyl acetate are produced, and by the addition of alcohol, vinyl ether and polyvinyl ether.
  • Cyclooctatetraene acrylic acid, acetic acid, 1,3- and 1 ,4-butanediol, propargyl alcohol, 2- butine-l,4-diol, vinyl ethine, succinic acid, neoprene, chloroprene, vinyl ester, polyvinyl ester, higher alcohols and monochloroethanoic acid are also synthesized from acetylene.
  • Acetylene is less frequently used for producing benzene, butadiene, ethanol, acrylonitrile and polyacrylonitrile, vinyl halides, acrylic acid and acetaldehyde.
  • Carbides of alkali metals and alkaline earth metals are therefore important compounds for the production of organic compounds. This equally applies to the carbides of aluminium and beryllium, which can be reacted with water or acids to form methane.
  • Carbon gasification refers to a number of processes for converting coal, in which carbon- containing compounds are reacted with oxygen and optionally also with water or steam and at temperatures of from 800 0 C to 2,000°C and pressures of up to 100 bar.
  • syngas synthesis gas
  • This reaction produces not only energy-rich carbon monoxide gas but also the energy necessary for the gasification reactions.
  • Hydrogen gas is also formed as an additional important component of the gasification. Hydrogen is formed from carbon and water at the temperatures prevailing in the gasification process.
  • this reaction is systematically induced by the addition of water and steam.
  • the hydrogen bound in the material to be gasified contributes towards the hydrogen fraction of the synthesis gas.
  • Methane is also formed by the direct reaction of carbon with hydrogen
  • Oxygen is obtained by known processes such as the liquefaction of air or pressure swing adsorption.
  • gas mixtures with an oxygen content of at least 90%, and preferably 95 - 98%, are used, the remaining components preferably being water, CO 2 ,
  • the synthesis gas obtained in the gasification of carbon-containing materials can be used for energy production usually after removing undesired secondary components such as hydrogen sulphide.
  • One preferred application is, for example, the use of synthesis gas as a fuel for operating a combination of a gas turbine and a steam turbine which incorporates electricity generation.
  • the synthesis gas can also be used as a raw material for other chemical syntheses. Suitable processes are, in particular, catalytic conversion into hydrocarbons (the Fischer-Tropsch synthesis) or methanol.
  • This hydrogen can be used for chemical syntheses, such as for example for the synthesis of ammonia, or also as an energy source, for example for the operation of gas turbines.
  • Slag and ash When coal is gasified, its mineral components form slag and ash. Slag and ash can be used commercially as useful materials, such as for example as fillers for cement or for the production of road surfaces. Frequently ash does, however, have to be laboriously disposed of.
  • the pressures and the gasification temperatures vary depending on the process employed and are optimized according to the starting materials used and the required gas quality.
  • the gasification temperatures are in the range from 800 to higher than 2,000°C.
  • the pressure employed can be in the range from 2 to higher than 100 bar. In some earlier known processes atmospheric pressure is employed.
  • Gasification in a fluidized bed reactor is carried out by introducing the granular gasification material in the lower region of the reactor via a screw or in the form of a paste mixed with water or oil.
  • the gasification material is vortexed by introducing oxygen and, where applicable, steam and then reacted. In this process additional oxygen and, where applicable, steam, can be introduced in the upper region of the fluidized bed.
  • the reaction gas escapes at the top of the reactor. Solids entrained by the gas are removed in a cyclone and recycled into the reaction.
  • Non-gasifiable components are discharged in the form of ash at the base of the reactor.
  • Temperatures of 800 - 1 ,200°C and pressures of from atmospheric pressure to 30 bar are commonly used for the gasification of coal in fluidized bed reactors.
  • Temperatures of 1 ,200 to higher than 2,000°C and pressures of between atmospheric pressure and 100 bar are commonly used for the gasification of coal in entrained flow reactors.
  • molten bath reactor In a molten bath reactor the material to be gasified and oxygen are fed into a melt. The synthesis gas escapes above the melt and non-gasifiable components are discharged via the melt.
  • the molten bath reactor has so far not been used on an industrial scale.
  • the hot, dust-containing crude gases are freed from dust and cooled.
  • Various types of equipment such as for example cyclones, scrubbers, electrofilters and candle filters, are used for the removal of dust.
  • cooling such as for example heat exchangers, quenching with water or quenching with recycled, cooled synthesis gas.
  • Gasification processes require complicated equipment and a high input of capital.
  • the economic efficiency of gasification depends not only on the cost of the raw material employed and the cost of the gasification process but also on the value of the products produced by gasification.
  • coal gasification can be combined with the production of carbides, the carbides allowing the production of additional useful products and thereby increasing the economic efficiency of coal gasification.
  • the present invention therefore relates to a process for gasifying carbon-containing gasification materials by partial oxidation, characterized in that compounds of alkali metals and/or alkaline earth metals and/or compounds of aluminium and/or beryllium are added to the carbon-containing gasification materials with the result that the slags and/or ash obtained by gasification contain quantities of carbides of the respective alkali metals and/or alkaline earth metals and/or aluminium and/or beryllium.
  • the addition of compounds of alkali metals and/or alkaline earth metals and/or aluminium and/or beryllium produces additional useful products, i.e. carbides, which can in turn be reacted to form useful secondary products, thereby increasing the economic efficiency of coal gasification.
  • Compounds of alkali metals and/or alkaline earth metals and/or aluminium and/or beryllium which can be used are, for example, their oxides, peroxides, hydroxides, carbonates and/or bicarbonates and/or mixtures thereof. In the presence of carbon-containing gasification materials and oxygen they react to form the corresponding carbides. Preferably oxides, peroxides, hydroxides, bicarbonates and/or carbonates of the alkali metals and/or alkaline earth metals are used.
  • one or more compounds from the series comprising calcium oxide, sodium oxide, sodium carbonate and sodium hydroxide are used.
  • carbide precursors compounds of alkali metals and/or alkaline earth metals and/or of aluminium and/or beryllium, which react to form the corresponding carbides in the presence of carbon-containing gasification materials and oxygen, are referred to as carbide precursors.
  • the carbides can in turn be used for the production of acetylene and/or methane by reaction with water and/or an acid.
  • Carbon-containing gasification materials are understood to be materials with a high content of carbon.
  • Examples of carbon-containing compounds are hard coal, brown coal, peat, anthracite, bituminous coal, low-volatile steam coal, coke, charcoal, petroleum coke, other refinery residues, biomass, industrial waste, household refuse, etc. or mixtures thereof.
  • the carbon-containing gasification materials are partially oxidized with oxygen at temperatures of between 1,000 0 C and 2,500 0 C, while adding one or more carbide precursors.
  • the pressure is between 1 bar and 100 bar.
  • Reactors already known for the gasification of carbon-containing gasification materials are fundamentally also suitable for the combination, according to the invention, of gasification and carbide production. Modifications may have to be made in order to cater for the specific features of carbide formation.
  • the temperature in the reactor must be selected in such a manner that it is sufficiently high for the formation of carbides. Temperatures of >l,800°C are necessary for the formation of calcium carbide, whereas temperatures of about 1 ,000 0 C are sufficient for the formation of sodium carbide from sodium oxide.
  • the gasification reaction is carried out preferably with oxygen or gas mixtures with an oxygen content of >90%.
  • Carbides with a high vapour pressure such as for example sodium carbide, are for example removed from the reactor via the gas stream.
  • the carbide is then removed by separation by cooling the synthesis gas. Cooling is carried out by means of processes known to the skilled man, such as for example via heat exchangers or by quenching with cooled synthesis gas.
  • Carbides with a low vapour pressure are predominantly discharged in the form of a melt.
  • Methods of treating the melt are known to the skilled man from the production of carbide by the electrothermal process and from metallurgical engineering.
  • a fraction of the carbides with a low vapour pressure may escape from the reactor in the form of small particles in the gas stream. These particles are removed in separators arranged downstream, together with additional fine dust. Carbide-containing fine dust can be used for acetylene production.
  • the starting products must be dried as far as possible before being fed into the reactor.
  • the content of moisture is below 5%.
  • the carbide precursor and the carbon-containing gasification material are preferably finely ground and intimately mixed prior to partial oxidation.
  • the grinding of the starting products can be carried out prior to, during or after mixing.
  • a finely ground product is understood to be a product in which the average particle diameter of the particles forming the product is smaller than 1 mm.
  • the maximum diameters of the particles are used for determining the average particle diameter. As is known to the skilled man, these maximum particle diameters can be determined, for example, from photomicrographs of a random sample.
  • the average diameter is understood to be the arithmetic average. In the following the average particle diameter is therefore to be understood to be the arithmetic average of the maximum particle diameters of a random sample.
  • the average particle diameter of at least one of the starting products is preferably less than 500 ⁇ m, particularly preferably less than 100 ⁇ m, and very particularly preferably less than 50 ⁇ m.
  • An intimate mixture is understood to mean that a random sample of the mixture in a quantity of 100 g reflects the weight ratio of the starting products with a maximum deviation of +/- 10%, preferably +/- 5% and particularly preferably +/- 1%.
  • the mixture of the carbide precursors is compacted into larger units. It can for example be agglomerated into pellets or briquettes.
  • the carbide precursor is mixed only with a fraction A of the carbon-containing compound fed into the gasification reaction.
  • the mixture is then fed into the reactor together with another fraction B.
  • fractions can be introduced jointly, optionally after further mixing, or separately, optionally at different points in the reactor.
  • fraction A it is possible for a different, preferably more carbon-rich, gasification material, to be used for fraction A than for fraction B.
  • a gasification product with a carbon content of >80%, and particularly preferably >88%, such as for example coke, petroleum coke or anthracite coal is used as fraction A.
  • the carbide precursor is mixed with the fraction of the carbon-containing compound with a carbon content of >80% in such a manner that the quantities of carbon and alkali metal or alkaline earth metal required for the carbide formation are present in an equivalent, stoichiometric molar ratio, with a maximum deviation of +/-
  • the ratio between the components comprising the carbon-containing gasification material, including fractions A and B, oxygen and the carbide precursor must be selected in such a manner that the temperature required for the formation of the carbide is reached.
  • the crude synthesis gas and other highly volatile components issue from the reactor in the form of a hot gas.
  • the ash fraction is discharged in the form of a molten slag, precipitated ash and/or fine dust in the gas stream.
  • the carbide formed is discharged together with the slag and/or it leaves the reactor in the gas stream in the form of fine dust and/or, in the case of more readily volatile carbides, such as for example sodium carbide, in the form of a gas.
  • Carbide-containing slag is discharged from the reactor preferably in the form of a melt in crucibles and worked up by processes known to the skilled man from the production of calcium carbide.
  • the calcium carbide discharged in the fine dust is removed by a process known to the skilled man from the field of coal gasification.
  • Gaseous carbides are condensed by cooling. This can take place for example by quenching the hot gas stream with cooled synthesis gas.
  • the flue ash ensures that sufficient crystallization seeds are present.
  • the condensed carbide is removed by known processes together with the flue ash, although care must be taken to ensure that the carbide does not come into contact with water or moisture, in order to avoid the (premature) production of acetylene.
  • carbide-containing slags and/or carbide-containing fine dust are obtained, both of which can also contain fractions of the carbide precursors originally employed.
  • the content of carbide depends on the content of ash of the carbon-containing compound, the proportion of carbide precursors and the reaction conditions such as temperature, pressure and residence time.
  • the content of carbide can however be lower, such as for example 50-80% or even 10-50%. According to the invention it is important for acetylene and/or methane, and preferably acetylene, to be obtained economically from the carbide-containing slag or the carbide- containing fine dust by reacting it with water and/or acid.
  • the resulting carbide- containing slag and/or ash is reacted in a subsequent step with water and/or an acid.
  • acetylene is preferably obtained.
  • the process according to the invention is characterized in that the gasification of coal is combined with the synthesis of carbides.
  • the process according to the invention therefore provides the advantage of the improved utilization of the available product and energy resources by the production of additional useful products, such as for example acetylene.
  • the synthesis gas obtained in the process according to the invention can be used, optionally after further treatment, for known applications, such as for example for the generation of electricity in a combined gas and steam power plant or for the synthesis of additional products such as methanol, ammonia or hydrocarbons by the Fischer-Tropsch process.
  • the process according to the invention can also be combined with a conventional process for producing synthesis gas, such as for example by generating only a portion of the required synthesis gas in the process according to the invention and generating another portion by conventional gasification methods.
  • the synthesis gas streams from the various sources can then be combined and used for a joint application.
  • the invention is explained in more detail hereinbelow with the aid of examples, without, however, being limited thereto.
  • the quantities mentioned in the examples are approximate values which can in individual cases vary by up to 100%, depending on the starting products, reactors and process conditions employed.
  • Nm 3 of oxygen are introduced centrally and an additional 5 kg/h of steam are injected in the peripheral regions via several annularly distributed jets.
  • the temperature in the centre is about 2,100°C and it falls to about l,600°C towards the edges.
  • a fluidized bed reactor with 3 cyclone separators and recycling of the solids separated in the first cyclone is set in operation with dried brown coal.
  • the introduction of the starting products is adjusted in such a manner that per 100 kg/h of the mixture of sodium carbonate and petroleum coke about 100 kg/h of dried brown coal are introduced into the reactor.
  • 100 m 3 /h of oxygen are injected in the bottom region of the fluidized bed reactor and another 80 m 3 /h in the upper third of the fluidized bed.
  • the pressure in the reactor is 3 bar.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Inorganic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

La présente invention concerne un procédé de gazéification de composés contenant du carbone, caractérisé en ce que des composés qui forment des carbures dans les conditions du procédé sont ajoutés. Ces carbures peuvent être utilisés pour la synthèse de matériaux utiles tels que par exemple l'acétylène.
EP09841670A 2009-03-18 2009-03-18 Gazéification de charbon avec production supplémentaire de matériaux utiles Withdrawn EP2408881A4 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/CN2009/000294 WO2010105385A1 (fr) 2009-03-18 2009-03-18 Gazéification de charbon avec production supplémentaire de matériaux utiles

Publications (2)

Publication Number Publication Date
EP2408881A1 true EP2408881A1 (fr) 2012-01-25
EP2408881A4 EP2408881A4 (fr) 2012-02-29

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CN103449437A (zh) * 2013-08-27 2013-12-18 北京化工大学 一种生物质燃料生产电石的方法
CN103708462A (zh) * 2013-12-25 2014-04-09 北京神雾环境能源科技集团股份有限公司 制备电石的方法
DE102015202683A1 (de) * 2015-02-13 2016-08-18 Siemens Aktiengesellschaft Verfahren zum Betreiben eines mit fossilen Brennstoffen betriebenen Kraftwerkes und Kraftwerk zur Verbrennung fossiler Brennstoffe
DE102016200078A1 (de) * 2016-01-07 2017-07-27 Siemens Aktiengesellschaft Verfahren und Vorrichtung zum Speichern elektrischer Energie mittels eines chemischen Speichers
CN110387263B (zh) * 2018-08-13 2024-03-26 沈阳化工股份有限公司 乙炔发生器装置及排渣控制方法

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