WO2017092876A1 - Procédé et dispositif pour produire un agent de gazéification pour un processus de gazéification - Google Patents

Procédé et dispositif pour produire un agent de gazéification pour un processus de gazéification Download PDF

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Publication number
WO2017092876A1
WO2017092876A1 PCT/EP2016/025163 EP2016025163W WO2017092876A1 WO 2017092876 A1 WO2017092876 A1 WO 2017092876A1 EP 2016025163 W EP2016025163 W EP 2016025163W WO 2017092876 A1 WO2017092876 A1 WO 2017092876A1
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WO
WIPO (PCT)
Prior art keywords
gasification
agent
product gas
reactor
gasification reactor
Prior art date
Application number
PCT/EP2016/025163
Other languages
German (de)
English (en)
Inventor
Winfried Meier
Original Assignee
Wincip 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 Wincip Gmbh filed Critical Wincip Gmbh
Publication of WO2017092876A1 publication Critical patent/WO2017092876A1/fr

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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
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • 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
    • C10J3/80—Other features with arrangements for preheating the blast or the water vapour
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F23G5/46—Recuperation of heat
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1253—Heating the gasifier by injecting hot gas
    • 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
    • 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
    • C10J2300/1637—Char combustion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/301—Treating pyrogases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/304—Burning pyrosolids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/40—Gasification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/10—Combustion in two or more stages
    • F23G2202/104—Combustion in two or more stages with ash melting stage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying

Definitions

  • the present invention relates to a method and a combined gasification and combustion plant for producing a gasification agent for a gasification process and for producing a product gas by gasification of at least one carbon support, wherein in the gasification process in a fluidized bed of a gasification reactor with supply of the gasification agent, a product gas by gasification of liquid, solid or pasty carbon carriers with a calorific value greater than 12 MJ / kg.
  • Fluidized bed gasification is a proven process that is used primarily in the field of coal gasification, but also in the field of gasification of biomass and / or other carbonaceous feedstocks.
  • the fine-grained carbon support to be gasified is introduced into a fluidized bed material, and a gasification agent flows through it from below through a distributor plate. After exceeding a minimum fluidization velocity of the gas, a stationary fluidized bed with a defined surface is formed. Above the fluidized bed there is a hot reaction zone through which the gas released from the fluidized bed flows and in which the gas can continue to react. As the gas velocity increases, the fluidized bed expands, resulting in a uniform distribution of the solids over the reactor height.
  • the bed material entrained by the synthesis gas or product gas the so-called "fly ash" is separated from the product gas in a hot cyclone downstream of the gasification reactor and returned to the gasification reactor.
  • the thermal performance of fluidized bed gasifiers is usually in the range between 1 MWthermisch and well over 100 MWthermisch-
  • the solids content in the product gas is greater due to the higher flow rates in the gasification reactor than fixed bed gasifiers, also the burnout of the ash is usually poor.
  • this consists of approximately 80% carbon, which negatively affects the cold gas efficiency of the gasification process.
  • Gasification is an endothermic process in which heat is added to the gasification reactor at a high temperature level.
  • autothermal gasification the heat of reaction required for the gasification process is provided by partial oxidation of the carbonaceous feedstock inside the gasifier. The partial oxidation of the carbon carrier leads to a reduction in the Kalkgas strictlysgrades the gasification process.
  • the heat of reaction for the endothermic gasification process which must be provided by partial oxidation of the carbonaceous support, also changes.
  • the setting of an optimal amount of oxygen for the gasification process is technically complex, especially when air is used as a gasification agent. In this case, it comes through the nitrogen content of the air to cool the gasification process and a more or less strong dilution of the product gas by the modified amount of the gasification agent.
  • the production of a product gas with a substantially constant calorific value is therefore only possible to a limited extent.
  • the gasification of low calorific solid fuels usually requires a pre-sorting to weed out the gasification process interfering components from the solid fuel. Subsequently, the remaining solid fuel usually needs to be crushed to achieve low particulate matter before it is gasified. In order to achieve a higher calorific value of the gas coming from the gasification reactor, the solid fuels are also dried before gasification. Since the gasification process is complicated and is made even more difficult by a non-constant fuel composition, the cost-effectiveness of the energetic use of low calorific fuels by gasification is usually not given. In addition, a synthesis gas is usually generated with a low calorific value, which limits the potential uses of the synthesis gas.
  • Object of the present invention is to provide a method and a combined gasification and combustion plant each of the aforementioned type available that enable energy recovery of low calorific fuels with high efficiency and low demands on the process engineering.
  • the object of the present invention is moreover to provide a method and an installation of the type mentioned above which, with simple process control and low technical complexity, enable the production of a synthesis gas or product gas with a high calorific value and with which a achieve high cold gas efficiency of the gasification process.
  • the method and the system should allow the production of a synthesis gas or product gas with a substantially constant calorific value even if there is a change in the amount and / or composition of the carbon support used for the gasification in a simple manner.
  • the firing is at least one further, not originating from the gasification carbon carrier with a calorific value (at 25 ° C) of less than 12 MJ / kg, in particular of less than 10 MJ / kg, more particularly of less than 8 MJ / kg, supplied in the furnace low-calorific fuels, various types of slags, for example, from waste incineration, or any other materials, such as scrap tires, settlement waste, sewage sludge, biomass, calorific-free materials for slag improvement and the like, can be burned.
  • a calorific value at 25 ° C
  • a gasification agent is generated from the low calorific fuel and from the product gas and / or from the gasification reactor discharged carbonaceous residues and forwarded for heat transfer to the gasification reactor.
  • the inventive method the production of a gasification agent for a gasification process of carbon carriers with a calorific value of greater than 12 MJ / kg by combustion of low calorific fuels in a separate from the gasification process combustion process.
  • the calorific value of the low calorie carbon carrier is preferably in the range of 2.5 to 12 MJ / kg.
  • the firing it is also possible for the firing to be fed, if required, in addition to a further (non-gaseous) carbon carrier not originating from the gasification process and having a calorific value of greater than 12 MJ / kg.
  • a further (non-gaseous) carbon carrier not originating from the gasification process and having a calorific value of greater than 12 MJ / kg.
  • low calorific fuels as carbon carriers in the furnace opens up the possibility of using low calorific fuels to produce a gasification agent and thus of highly efficient operation of the gasification process in which carbon carriers with a calorific value of greater than 12 MJ / kg are gasified and a synthesis gas to produce with high calorific value.
  • the energetic use of low calorific fuels in the furnace at very high firing temperatures even with changing fuel composition procedurally simple feasible and easy to control and regulated.
  • the synthesis or product gas is produced in a fluidized bed gasifier, in particular in a circulating fluidized bed, wherein the main components of the synthesis gas are hydrogen, carbon monoxide and optionally methane and other hydrocarbons.
  • the gasification reactor then leads to direct heat transfer between the gasification agent and the gasification zone with the carbon support to be gasified, wherein the gasification agent in the gasification reactor mixed with the atmosphere of the gasification reactor.
  • carbonaceous residues are removed from the synthesis gas and / or from the gasification reactor and burned in a separate furnace while supplying an oxidizing agent.
  • the flue gas from the furnace is then used as a gasification agent and at least partially, preferably completely, fed to the gasification reactor.
  • the synthesis gas produced can be a raw material for the chemical industry and / or be used as fuel.
  • the plant according to the invention has at least one gasification reactor operating on the principle of fluidized-bed gasification, in particular a circulating fluidized-bed gasifier, at least one furnace spatially separate from the gasification reactor and at least one separating device for separating carbonaceous residues the gasification reactor and / or for the deposition of carbonaceous residues from the synthesis gas.
  • the furnace it comes according to the invention for the oxidation of carbon fractions of the residues resulting from the gasification process.
  • the furnace thus supplies the gasification agent for the fluidized-bed reactor and the gasification energy in the form of heat, wherein the flue gas of the furnace can essentially comprise carbon dioxide and optionally oxygen and water vapor.
  • the heat of reaction required for the endothermic gasification process can be provided at least partially, preferably completely without internal partial oxidation of the carbon support used, which leads to an improvement in the cold gas efficiency of the gasification process.
  • the process is designed so that at least 90%, in particular at least 80%, of the heat of reaction required for the endothermic gasification process is provided by the heat of the gasification agent. Further preferably, the heat of reaction required for the endothermic gasification process is completely covered by the heat of the gasification agent.
  • the carbon dioxide contained in the gasification agent can then be reacted in the gasification reactor with the carbon of the carbon support according to the Boudouard equilibrium to carbon monoxide.
  • the inventive production of the gasification agent from carbonaceous residues of the gasification process allows it to be at least 90% by weight, preferably at least 95% by weight, more preferably 98% by weight or more, of the carbonaceous feed introduced into the gasifier Converting carbon into a synthesis or product gas.
  • By combusting the gasification residues in the furnace it is possible to operate the fluidized-bed gasification largely independent of the fuel quality of the carbon support used for the gasification process. In particular, it is not necessary to conduct the gasification process so that a certain high carbon conversion is achieved in the gasification in the fluidized bed.
  • the inventive method and the system according to the invention are therefore also suitable for the use of carbon carriers with a comparatively lower calorific value for the gasification process.
  • the furnace thus offers the possibility of operating the entire plant gas-and cost-optimized, with simple process control and low technical effort. Since the gasification process in the gasification reactor and the combustion process in the furnace can be controlled independently of one another, the process according to the invention is extremely flexible in the work area.
  • the system according to the invention may comprise a control and / or regulating device for controlling and / or regulating the operation of the gasification reactor on the one hand and the operation of the furnace on the other hand.
  • a coordinated control and / or regulation of the gasification process and the firing process can be achieved a high efficiency and a simple process management.
  • the method according to the invention can be achieved in a range of preferably 40% to 100% of the achievable gas capacity of the gasification a stable stable gas quality even with changing composition of the one used in the furnace low-calorific fuels and / or the higher-calorific fuels used in the gasification process.
  • the calorific value of the carbon support used for the gasification process is greater than 12 MJ / kg.
  • the calorific value specification refers to a temperature of 25 ° C and is the maximum usable amount of heat in a combustion, in which there is no condensation of the water vapor contained in the exhaust gas, based on the amount of carbon support used.
  • carbon carriers with a lower calorific value can additionally be used in the gasification process.
  • the combustion of the carbonaceous residues from the product gas and / or from the gasification reactor takes place in at least one combustion chamber.
  • a melting furnace is provided, which is operated at such temperatures that at least a portion of the ash is obtained molten and can be removed in this state from the furnace.
  • glazing of the formed ash can occur.
  • a furnace an open-hearth furnace, a melting chamber furnace, a cyclone furnace or a cycloidal furnace can be used.
  • a Schmelzhunt mecanicung is provided.
  • slag granules from smelting furnaces are a sought-after raw material, for example for road construction or in the stone-earth industry.
  • slime obtained by the method according to the invention Similar to the fly ash from power plants and blast furnace slag from steel production.
  • the temperature during combustion of the carbonaceous residues from the synthesis or product gas and / or from the gasification reactor in the furnace should be as high as possible. It is preferably provided that the gasification agent at a temperature of at least 1200 ° C, preferably at least 1400 ° C, more preferably at least 1500 ° C, more preferably at least 1600 ° C, or at least 1800 ° C, enters the gasification reactor. In principle, the temperature of the gasifying agent may also be greater than 2000 ° C. when it enters the gasification reactor.
  • the furnace is designed as a melting furnace, so that high gasification agent temperatures can be achieved.
  • the combustion of the carbonaceous residues in a melting chamber also offers the advantage of a simple import / export of fuels into the melting chamber at high operating pressures of the furnace.
  • the molten discharge prevents the formation of slag residues in the melting chamber, so that the combustion of the carbonaceous residues in the melting chamber is less maintenance-intensive.
  • the gasification reactor can also be supplied directly with oxygen and / or steam and / or optionally also with air, the supply of oxygen resulting in a partial oxidation of the carbon support used in the gasification reactor and thus for the endothermic gasification process required heat of reaction only to a (certain) proportion on the gasification agent from the furnace and to a (different) proportion by partial oxidation is provided inside the gasifier.
  • the product gas composition can be favorably influenced.
  • the carbon support used for the gasification process is introduced particulate into the gasification reactor and may have an average particle diameter or particle diameter of less than or equal to 5 mm, preferably of less than or equal to 2 mm.
  • the plant according to the invention has at least one preferably automatically operated separation device, which may be part of the gasification reactor.
  • corresponding transport means are provided to transport the coarse ash from the gasification reactor to the furnace.
  • the fly ash discharged with the product gas is separated from the product gas and burned in the furnace.
  • appropriate separation and transport facilities are provided.
  • the fly ash charge of the product gas may be between 30 g / Nm 3 to 120 g / Nm 3 , preferably between 40 g / Nm 3 and 100 g / Nm 3 .
  • the mean particle diameter of the fly ash may be less than 100 ⁇ m, preferably less than 60 ⁇ m, more preferably less than 45 ⁇ m.
  • the carbon content of the fly ash can be between 30% by weight and 70% by weight, preferably between 40% by weight and 60% by weight.
  • the product gas can be cooled and cleaned after exiting the gasification reactor.
  • the product gas can first be cooled in at least one cooling device to a temperature of from 300 ° C. to 500 ° C., preferably from 350 ° C. to 400 ° C.
  • the plant according to the invention can for this purpose have a waste heat boiler, in which the product gas is cooled. This sediments a subset of the fly ash.
  • the product gas may be cooled to a temperature of less than 80 ° C, preferably less than 60 ° C.
  • fly ash and hydrocarbons, such as tar compounds can be separated from the recycle water of the quencher.
  • the cold Product gas can be filtered in a filter device, for example in a wet electrostatic precipitator to separate flue dust.
  • a further cooling of the product gas to a temperature of less than 40 ° C, in particular of less than 30 ° C, can be carried out in a further downstream cooling device to reduce the water content of the product gas.
  • the product gas can then be compressed, for example to a system pressure of 2 bar abs .
  • the gasification agent from the furnace may contain carbon dioxide and oxygen as main components, which depends in particular on the choice of the oxidizing agent for the furnace.
  • the carbon dioxide content of the gasifying agent may be in the range between 60% by volume and 100% by volume, preferably between 70% by volume and 100% by volume.
  • the oxygen content of the gasifying agent may be up to 40% by volume, preferably up to 30% by volume.
  • the gasification temperature may be in the range between 800 ° C and 1100 ° C, preferably in the range between 950 ° C and 1000 ° C. This makes it possible to prevent the formation of tar as much as possible. Since the temperature in the furnace is preferably much higher, a cooling of the gasification agent can be provided after exiting the furnace and before it enters the gasification reactor, the waste heat obtained in this case being obtained at a high temperature level and can be further used in terms of process technology. In particular, the cooling of the gasification agent before it enters the gasification reactor can be controlled and / or regulated as a function of the heat of reaction required for the gasification process. In principle, however, it can also be provided to supply the gasification agent to the gasification process without intermediate cooling directly at the temperature level of the furnace.
  • the combustion of the carbonaceous residues in the furnace is preferably carried out with oxygen of high purity, preferably with pure oxygen.
  • the oxygen content of the oxidant supplied to the furnace may preferably be more than 90% by volume, more preferably more than 95% by volume, particularly preferably more than 99% by volume.
  • the furnace can be operated in particular at temperatures between 1500 ° C and 2200 ° C, preferably between 1700 ° C and 2000 ° C, in particular in a melting chamber.
  • the furnace can be operated at overpressure be, in particular at a pressure of greater than 1, 5 bar a b S , in particular at a pressure of greater than 2 bar a bs-
  • the pressure level of the furnace may be above the pressure level of the gasification process, wherein the oxidizing agent used for the firing a sufficiently high pressure can be compressed to compensate for all subsequent system pressure losses.
  • the gas delivery of the gasification agent to the gasification reactor is then ensured solely because of the overpressure of the oxidizing agent. Thus, no additional compression of the gasifying agent is required before entering the gasification reactor.
  • the carbon content of the combustion residue is preferably less than 5% by weight, more preferably less than 2% by weight, particularly preferably less than 1% by weight.
  • the pressure of the gasifying agent before entering the gasification reactor can be in the range between 1.5 to 2.5 bar a b S , preferably in the range between 1.6 to 2.0 bar a bs. At this pressure level, the gasification process can also run off.
  • an inert gas in particular carbon dioxide
  • simple control and / or regulation of the gasification temperature is possible, which simplifies the production of a product gas with a substantially constant calorific value.
  • FIG. 1 schematically shows a process for product gas production by gasification of liquid, solid or pasty carbon carriers 1 in a circulating fluidized bed, wherein the carbon carrier 1 gasified by supplying a gasification agent 2 in a gasification reactor 3 of a combined gasification and combustion plant 4 and thereby a product gas 5 is generated.
  • the gasification reactor 3 has a recycle cyclone to recycle solids from the product gas 5 into the gasification reactor 3.
  • the product gas 5 may have a solids content between 40 and 200 g / Nm 3 , preferably between 60 and 140 g / Nm 3 .
  • the product gas 5 is cooled and purified after flowing through the recycle cyclone in a gas purification device 6.
  • the gas cleaning device 6 may have at least one cooling device for cooling the product gas 5, in particular a waste heat boiler, in order at least partially to sediment fly ash transported with the product gas 5 from the gasification reactor 3.
  • the product gas 5 may be cooled to a temperature of, for example, 350 ° C to 400 ° C.
  • the gas cleaning device 6, a further cooling device for the subsequent even greater cooling of the product gas 5, in particular to temperatures of 60 ° C or less have.
  • at least one quencher can be provided, wherein fly ash and hydrocarbons, possibly tar compounds, can be separated from the circulating water of the quencher.
  • the gas cleaning device 6 may have at least one filter device, for example a wet electrostatic filter, in order to purify the product gas 5 from the fly-ash.
  • the purified product gas 5 can be cooled by a further cooling device, not shown, to temperatures of less than 40 ° C, in particular of less than 30 ° C, to reduce the water content of the product gas 5.
  • a compression of the purified and dried product gas can be provided with a compressor, not shown, wherein the product gas 5 can be compressed, for example, to a pressure of about 2 bar a b S and is available for other applications.
  • a furnace 9 designed as a melting chamber.
  • Grobasche 1 1 can be removed from the gasification reactor 3 and the furnace 9 are supplied.
  • the gasification agent 2 is generated.
  • the oxidizing agent 10 is preferably pure oxygen.
  • Ashes from the gasification process and residues from product gas purification contain carbon in high concentrations. This carbon is added the combined gasification and combustion plant 4 used to produce preferably a pure flue gas flue gas as a gasification agent 2 at a temperature of preferably 1700 ° C to 2000 ° C.
  • the gasification agent 2 essentially comprises carbon dioxide and oxygen, the combustion of the residues in the furnace 9 preferably taking place in the case of excess oxygen.
  • At least one further carbon carrier 12 such as slag, scrap tires, municipal waste, sewage sludge or biomass or the like, is fed to the combustion 9 and burnt there.
  • a use of low calorific or low calorific fuels is provided as a further carbon carrier 12 in the combined gasification and combustion plant 4.
  • vitrified slag 14 is obtained, which preferably has a carbon content of well below 1 wt .-% and is versatile reusable.
  • the gasification agent 2 emerging from the melting chamber can optionally be cooled in a heat exchanger 13 in order to control and / or regulate the heat of reaction supplied to the gasification process in terms of height.
  • a heat exchanger 13 From the heat exchanger 13 and optionally in the cooling of the product gas 5 in the gas cleaning device 6 released heat 15 is available as process waste heat for further use.
  • at least one further gasification agent 16, in particular oxygen can be supplied to the gasification reactor 3 in order to provide additional heat of reaction by partial oxidation of the carbon support 1 in the gasification reactor 3.
  • the addition of steam 17 may be provided for the gasification process in order to change the composition of the product gas 5.
  • an inert gas 18, in particular of carbon dioxide, to the gasification reactor 3 may be provided in order to influence the temperature of the gasification process and / or the product gas composition in the desired manner.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention concerne un procédé pour produire un agent de gazéification (2) pour un processus de gazéification et pour produire un gaz de réaction en effectuant la gazéification d'au moins un support de carbone (1). Dans le processus de gazéification, un gaz de réaction (5) est produit en effectuant la gazéification de supports de carbone (1) liquides, solides ou pâteux ayant un pouvoir calorifique supérieur à 12 MJ/kg dans un lit fluidisé d'un réacteur de gazéification (3) et en introduisant l'agent de gazéification (2), un combustible peu calorifique ayant un pouvoir calorifique compris entre 2,5 et 12 MJ/kg, tel que des scories, par exemple issues de la combustion de déchets, ou par exemple des pneus usagés, des déchets municipaux, des boues d'épuration, de la biomasse et des résidus carbonés évacués du gaz de réaction (5) et/ou du réacteur de gazéification (3) étant brûlés afin de produire l'agent de gazéification (2) dans un foyer à cendres fondues (9) séparé en introduisant un agent d'oxydation (10) et l'agent de gazéification (2) généré étant acheminé au moins en partie, de préférence intégralement, au réacteur de gazéification (3) par transfert de chaleur direct.
PCT/EP2016/025163 2015-12-04 2016-12-02 Procédé et dispositif pour produire un agent de gazéification pour un processus de gazéification WO2017092876A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102015015594.6A DE102015015594A1 (de) 2015-12-04 2015-12-04 Verfahren und Anlage zur Synthesegaserzeugung durch Vergasung von flüssigen, festen oder pastösen Kohlenstoffträgern in einer Wirbelschicht,
DE102015015594.6 2015-12-04

Publications (1)

Publication Number Publication Date
WO2017092876A1 true WO2017092876A1 (fr) 2017-06-08

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Citations (4)

* Cited by examiner, † Cited by third party
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US4696678A (en) * 1981-03-06 1987-09-29 Agency Of Industrial Science And Technology Method and equipment for gasification of coal
EP0489226A1 (fr) * 1990-12-06 1992-06-10 Lentjes Ag Procédé et installation pour améliorer la combustion de la masse du lit pendant le chauffage du lit fluidisé
DE19652770A1 (de) 1996-12-18 1998-06-25 Metallgesellschaft Ag Verfahren zum Vergasen fester Brennstoffe in der zirkulierenden Wirbelschicht
WO2006123018A1 (fr) * 2005-05-18 2006-11-23 Foster Wheeler Energia Oy Procede et appareil pour la gazeification de materiaux carbones

Family Cites Families (1)

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Publication number Priority date Publication date Assignee Title
JPS5776088A (en) * 1980-10-31 1982-05-12 Nippon Kokan Kk <Nkk> Coal gasification using powdered coal and its device

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4696678A (en) * 1981-03-06 1987-09-29 Agency Of Industrial Science And Technology Method and equipment for gasification of coal
EP0489226A1 (fr) * 1990-12-06 1992-06-10 Lentjes Ag Procédé et installation pour améliorer la combustion de la masse du lit pendant le chauffage du lit fluidisé
DE19652770A1 (de) 1996-12-18 1998-06-25 Metallgesellschaft Ag Verfahren zum Vergasen fester Brennstoffe in der zirkulierenden Wirbelschicht
WO2006123018A1 (fr) * 2005-05-18 2006-11-23 Foster Wheeler Energia Oy Procede et appareil pour la gazeification de materiaux carbones

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