CN107880938B - Preheating type staged gasification method and device - Google Patents

Preheating type staged gasification method and device Download PDF

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Publication number
CN107880938B
CN107880938B CN201610868168.3A CN201610868168A CN107880938B CN 107880938 B CN107880938 B CN 107880938B CN 201610868168 A CN201610868168 A CN 201610868168A CN 107880938 B CN107880938 B CN 107880938B
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preheating
preheated
fuel
gas
gasifying agent
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CN107880938A (en
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朱治平
王小芳
那永洁
高鸣
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Institute of Engineering Thermophysics of CAS
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Institute of Engineering Thermophysics of CAS
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    • 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
    • C10J3/466—Entrained flow processes
    • 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
    • C10J3/485—Entrained flow gasifiers
    • 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
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • 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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/62—Processes with separate withdrawal of the distillation products
    • 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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • 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
    • C10J2300/0936—Coal fines for producing producer gas

Abstract

The invention provides a preheating type grading gasification method, which comprises the following steps: a) Introducing the fuel (A) and the first gasifying agent (B) into a pre-preheating chamber (2) for preheating to generate a preheated gas-solid mixture (CD); b) The preheated gas-solid mixture (CD) is subjected to gas-solid separation through a separation device (3) to form reducing flue gas (C) and preheated fuel (D); c) Introducing a second gasifying agent (E) and preheated fuel (D) into an entrained-flow gasifier (1), and performing gasification reaction on the second gasifying agent (E) and the preheated fuel (D) to generate raw gas (G) and bottom slag (F); and d) collecting the reducing flue gas (C) and the raw gas (G), and discharging the bottom slag (F) out of the entrained-flow gasifier (1). The invention also provides a preheating type grading gasification device. The preheating type staged gasification method and device do not use a burner, and the method and device have the advantages of wide coal adaptability, simple coal preparation and rich CH in product gas 4 。

Description

Preheating type staged gasification method and device
Technical Field
The invention belongs to the technical field of gasification of carbon-containing raw materials, relates to a gasification method and a device of the carbon-containing raw materials, and particularly relates to an entrained-flow gasification method and a device adopting the same.
Background
In a process for producing synthesis gas or gasification gas, a carbonaceous feedstock is partially oxidized in a reactor. Taking coal as an example, the coal gasification technology is used as a clean coal technology with high efficiency, which is used for converting solid primary energy sources such as coal into gaseous clean secondary energy sources, and the technology is mainly applied to the fields of synthetic ammonia, synthetic methanol, hydrogen production, blast furnace reduction iron-making chemical industry metallurgy industry, combined cycle power generation devices, industrial and civil fuel gas and the like.
Classified according to the motion state of solid fuel, modern coal gasification processes mainly include moving bed (also called fixed bed) gasification, entrained flow gasification, and fluidized bed gasification. Wherein, the entrained flow coal gasifier has high reaction temperature, can adopt slag tapping, has high gasification strength, large production capacity and high carbon conversion rate, and becomes one of the main development directions of the prior coal gasification technology.
However, the entrained-flow gasifier has the following problems: (1) The burner has a complex structure, the service life is generally only three months to half a year, the burner must be replaced regularly, the operation economy is seriously affected, and the cost of the burner with longer service life is high; (2) Entrained flow gasifiers are limited in coal adaptability by factors such as ash content, moisture, reactivity and the like of coal; (3) In order to obtain higher reaction rate and carbon conversion rate, the granularity of the coal powder fed into the furnace is required to be more than 70% and less than 200 meshes, the preparation cost of the coal powder is higher, and the granularity requirement limits the use of lignite and high-ash coal; (4) In order to maintain high reaction temperature in the furnace, pure oxygen is often adopted as an oxidant, so that the oxygen consumption is high, and the economy is affected; (5) CH in product gas 4 Low content, not suitable for CH 4 The preparation of synthesis gas with high content requirement. In view of the above problems, the prior art attempts to improve burner life by improving burner performance and methane yield by hydrogenation catalysis, however, improving burner performance does not fundamentally solve the problems of entrained flow gasifiers, and the hydrogenation catalysis process increases costs.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a preheating type grading gasification method and a preheating type grading gasification device which are not limited by the service life of a burner and the problem of periodic replacement.
Another object of the invention is to provide a method for producing coal with wide adaptability, simple coal preparation, high gasification efficiency, high carbon conversion rate, and rich CH in the product gas 4 And no gasification technique using pure oxygen is required.
In order to achieve one of the above objects or purposes, the technical solution of the present invention is as follows:
according to an embodiment of one aspect of the present invention, there is provided a preheating-type staged gasification method including the steps of:
a) Introducing the fuel and the first gasifying agent into a pre-preheating chamber for preheating to generate a preheated gas-solid mixture;
b) The preheated gas-solid mixture is subjected to gas-solid separation through a separation device to form reducing smoke and preheated fuel;
c) Introducing the second gasifying agent and the preheated fuel into an entrained flow gasifier, and performing gasification reaction on the second gasifying agent and the preheated fuel to generate raw gas and bottom slag; and
d) Collecting the reducing smoke and the crude gas, and discharging the bottom slag out of the entrained flow gasifier.
According to a preferred embodiment of the invention, the preheating is a partial combustion reaction of the fuel with the first gasifying agent, the fuel being preheated by the heat of combustion.
According to a preferred embodiment of the present invention, the preheating type staged gasification process does not use burners.
According to a preferred embodiment of the invention, the pre-heating chamber is a circulating fluidized bed reactor.
According to a preferred embodiment of the invention, no bottom slag is discharged in the pre-heating chamber, and the preheated fuel produced in step b) is fed entirely into the entrained-flow gasifier.
According to a preferred embodiment of the invention, the reducing fumes are collected through a heat recovery and purification device to form a product gas.
According to a preferred embodiment of the invention, the temperature of the preheated gas-solid mixture is in the range of 800-1300 ℃.
According to a preferred embodiment of the invention, the first gasifying agent is air, oxygen-enriched air or pure oxygen, or a combination of one of the three with water vapor; and/or
The second gasifying agent is air, oxygen-enriched air or pure oxygen, or a combination of one of the three with water vapor.
According to a preferred embodiment of the present invention, the temperature of the first gasifying agent fed into the pre-heating chamber is normal temperature or has been preheated to 300-1200 ℃; and/or
The temperature of the second gasifying agent which is introduced into the entrained-flow gasifier is normal temperature or preheated to 300-1200 ℃.
According to a preferred embodiment of the invention, the first gasifying agent has been preheated to 600 ℃; and/or the second gasifying agent has been preheated to 600 ℃.
According to a preferred embodiment of the invention, the fuel is coal with a particle size of 0-2 mm.
According to a preferred embodiment of the invention, the separation device in step b) is one or more stages.
According to an embodiment of another aspect of the present invention, there is provided a preheating-type staged gasification device including a pre-preheating chamber, an entrained-flow gasification furnace, and a separation device;
wherein the pre-preheating chamber is provided with a fuel inlet, a first gasifying agent inlet and a preheated gas-solid mixture outlet;
the separation device is provided with a preheated gas-solid mixture inlet, a preheated fuel outlet and a reducing smoke outlet, and the preheated gas-solid mixture inlet is directly or indirectly communicated with the preheated gas-solid mixture outlet of the pre-preheating chamber;
the entrained-flow gasification furnace is provided with a preheating fuel inlet, a second gasifying agent inlet, a raw gas outlet and a bottom slag outlet, and the preheating fuel inlet is communicated with a preheating fuel outlet of the separation device.
According to a preferred embodiment of the invention, the preheating type staged gasification device has no burner.
According to a preferred embodiment of the invention, the pre-heating chamber is a circulating fluidized bed reactor.
According to a preferred embodiment of the invention, the pre-heating chamber comprises a preheating chamber furnace, further comprising a separator and a return, wherein a fuel inlet, a first gasifying agent inlet and a mixture outlet are provided on the preheating furnace; the separator is provided with a mixture inlet, a solid circulating material outlet and a preheated gas-solid mixture outlet, the material returning device is provided with a material returning device inlet and a material returning device outlet, the preheating furnace chamber is further provided with a material returning opening, the mixture outlet of the preheating furnace chamber is communicated with the mixture inlet of the separator, the solid circulating material outlet of the separator is communicated with the material returning device inlet of the material returning device, the material returning device outlet of the material returning device is communicated with the material returning opening of the preheating furnace chamber, and the preheated gas-solid mixture outlet of the separator is communicated with the preheated gas-solid mixture inlet of the separating device.
According to a preferred embodiment of the invention, no bottom slag outlet is provided in the pre-heating chamber.
According to a preferred embodiment of the present invention, the entrained-flow gasifier is a liquid slag-discharging entrained-flow gasifier or a solid slag-discharging entrained-flow gasifier.
According to a preferred embodiment of the invention, the pre-heating chamber is one or more.
According to a preferred embodiment of the invention, the separation device is one or more stages.
According to a preferred embodiment of the present invention, the preheating-type staged gasification device further comprises a heat recovery and purification device comprising a heat exchanger and a dust remover;
the heat recovery and purification device is provided with a reducing smoke inlet and a product gas outlet, and the reducing smoke inlet is communicated with a reducing smoke outlet of the separation device.
According to a preferred embodiment of the invention, the entrained-flow gasifier comprises a gasifier hearth, which further comprises an additional fuel inlet, which communicates with the ash discharge port of the dust separator.
The invention is provided with a preposed preheating chamber in front of the entrained flow gasifier, so that crushed coal with the particle size of 0-2 mm is preheated in advance before entering the gasifier. The temperature of the preheated fuel reaches 800-1300 ℃, and even if a burner is not used, the preheated fuel and the gasifying agent are respectively and independently introduced into the gasification furnace, a high-temperature zone can be rapidly formed, and the efficient gasification reaction is completed;
the coal particles finish volatile separation and water separation in the preheating process, the pores in the particles are increased, and the reaction surface area is increased, so that the gasifying agent is easy to diffuse to the reaction surfaces, the reactivity of the coal is improved, and the limitation of the entrained flow gasifier on the use of coal with high ash content, high water content and low reactivity is solved; meanwhile, volatile matters released by the coal particles are accumulated in the particles at high temperature in the preheating chamber, so that a larger pressure gradient is generated in the coal particles to cause the crushing of the coal particles, and the particle size of the fuel particles entering the gasification furnace after being preheated is reduced, thereby reducing the requirement of the whole gasification system on the particle size of the coal particles and greatly reducing the preparation cost of raw materials;
preferably, the preheating mode of partial combustion of coal in a preheating chamber is adopted, the preheating chamber is a highly anoxic reaction, the ratio of gasifying agent to coal is reduced to the oxygen amount/theoretical oxygen amount of fuel combustion=0.1-0.3 (the value is determined by the activity, heat value, preheating temperature and the like of the coal), the preheated product of the coal in the preheating chamber comprises high-temperature preheating fuel and high-temperature reducing flue gas, wherein the high-temperature preheating fuel contains a large amount of incompletely combusted carbon, and the high-temperature reducing flue gas is rich in CH 4 ，CH 4 The content is far higher than that in the conventional coal gasification product gas. The preheated product leaves the pre-preheating chamber and is separated by the separating device, and the high-temperature preheated fuel is completely sent into the entrained-flow bed gasifier to react with the gasifying agent introduced into the entrained-flow bed gasifier to obtain crude gas; the high-temperature reducing flue gas is collected as product gas after purification and heat recovery, and is rich in CH 4 The high-temperature reducing smoke of (C) is not fed into the entrained flow gasifier, CH 4 The gasification reaction in the entrained flow is mainly the reaction of carbon and gasifying agent, and compared with the conventional entrained flow gasification, the CH in the product gas is effectively increased 4 The content is as follows. In addition, because the high-temperature preheated fuel which enters the entrained-flow gasifier at 800-1300 ℃, oxygen-enriched air after preheating can be used as gasification agent of the gasifier instead of pure oxygen to maintain high reaction temperature in the gasifier, thereby improving the overall economy of the system.
Preferably, the circulating fluidized bed reactor is adopted as a preheating chamber, and the preheated fuel is taken away by a small amount of gas generated by partial combustion, and the rest of the fuel completely enters the entrained-flow bed gasifier; the preheating chamber has no slag discharge, and the carbon conversion rate and the thermal efficiency of the whole system are improved.
Drawings
FIG. 1 is a schematic diagram of a preheated staged gasification process according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of a preheated staged gasification device in accordance with an embodiment of the present invention; and
fig. 3 is a schematic view of a preheating-type staged gasification device in accordance with another embodiment of the present invention.
Detailed Description
Exemplary embodiments of the present invention are described in detail below with reference to the attached drawing figures, wherein the same or similar reference numerals denote the same or similar elements. Furthermore, in the following detailed description, for purposes of explanation, numerous specific details are set forth in order to provide a thorough understanding of the embodiments of the present disclosure. It may be evident, however, that one or more embodiments may be practiced without these specific details. In other instances, well-known structures and devices are shown in the drawings in order to simplify the drawings.
According to the present general inventive concept, there is provided a preheating type staged gasification method including the steps of:
a) Introducing the fuel and the first gasifying agent into a pre-preheating chamber for preheating to generate a preheated gas-solid mixture; b) The preheated gas-solid mixture is subjected to gas-solid separation through a separation device to form reducing smoke and preheated fuel; c) Introducing the second gasifying agent and the preheated fuel into an entrained flow gasifier, and performing gasification reaction on the second gasifying agent and the preheated fuel to generate raw gas and bottom slag; and d) collecting the reducing smoke and the raw gas, and discharging the bottom slag out of the entrained flow gasifier.
FIG. 1 is a schematic diagram of a preheated staged gasification process according to an embodiment of the invention, as shown in FIG. 1, the process of the invention comprising the steps of:
a) Introducing fuel (taking coal as an example) A and a first gasifying agent B into a pre-preheating chamber 2 for preheating to generate a preheated gas-solid mixture CD at 800-1300 ℃;
b) The preheated gas-solid mixture CD passes through a separation device 3 to realize gas-solid separation, so as to form high-temperature reducing flue gas C and high-temperature preheated fuel D;
c) All the high-temperature preheated fuel D is sent into the entrained-flow gasifier 1 to carry out gasification reaction with the second gasifying agent E which is introduced into the entrained-flow gasifier 1 at high temperature; the high-temperature reducing flue gas C is collected;
d) Raw gas G generated by gasification reaction in the entrained-flow gasifier 1 is collected, and bottom slag F is discharged out of the hearth.
Wherein the first gasifying agent B and the second gasifying agent E may be the following components or a combination of components: air, air + water vapor, oxygen-enriched air + water vapor, pure oxygen + water vapor, and the like. The selection of the second gasifying agent E is related to the components of the first gasifying agent B, the melting point of fuel ash, the temperature of the preheated fuel, the operating temperature, the slag discharging mode of the entrained flow bed and the like.
Wherein the separation device 3 in the step b) is one or more stages.
Wherein the bottom slag F may be liquid slag or solid slag.
Preferably, the temperature of the first gasifying agent B in the step a) is normal temperature or has been preheated to 300-1200 ℃. When the first gasifying agent B is pure oxygen, the air or oxygen-enriched air and the oxidant contain water vapor, the air or oxygen-enriched air can be preheated to 300-1200 ℃ before being introduced into the pre-preheating chamber, so that the reaction is facilitated.
Preferably, the preheating reaction in the step a) is a highly anoxic reaction, and the ratio of the first gasifying agent to the coal is reduced to an oxygen amount/fuel combustion theoretical oxygen amount of less than 0.2.
Preferably, the high-temperature preheated fuel separated by the separation devices at different stages in the step b) is sent to the hearth of the gasifier from different positions of the entrained-flow gasifier 1.
Preferably, the temperature of the second gasifying agent E in the step c) is normal temperature or has been preheated to 300-1200 ℃. When the second gasifying agent E is pure oxygen, the air or oxygen-enriched air and the oxidant contain water vapor, the second gasifying agent E can be preheated to 300-1200 ℃ to be more favorable for the preheating reaction.
In the embodiment of the invention, a pre-preheating chamber is arranged in front of the entrained-flow gasifier, so that crushed coal with the particle size of 0-2 mm is preheated before entering the entrained-flow gasifier. In the preheating chamber, the coal is partially combusted to release heat, and the fuel is heated to 800-1300 ℃; the heated coal is taken away by a very small amount of gas generated by partial combustion, the rest coal enters the entrained-flow bed gasifier completely, and the preheating chamber has no slag discharge; meanwhile, at high temperature, coal particles complete the processes of crushing, volatile separation and water separation, the pores in the particles are increased, the particle size is reduced, and the reactivity is improved; the coal is preheated to generate high-temperature preheated fuel and high-temperature reducing smoke, and the high-temperature reducing smoke can be used as product gas after being separated by a separation device and purified and heat recovered. Because the high-temperature reducing flue gas is generated by preheating coal under the highly anoxic condition, the flue gas is rich in CH 4 The effective gas component can not be consumed in the entrained flow gasifier, thereby effectively improving CH in the product gas 4 The content is as follows; the high-temperature preheated fuel is all sent into an entrained-flow bed gasifier to react with gasifying agent which is introduced into the entrained-flow bed gasifier, and crude gas is obtained. Wherein the gasifying agent can be preheated air, oxygen-enriched air, pure oxygen or a combination of the above components and water vapor.
Embodiments of the present invention have the following advantages:
1) By preheating coal and then gasifying, the entrained-flow gasification technology without adopting a burner is formed, and the technical problems of complex structure, short service life and high manufacturing cost of the burner in the conventional entrained-flow gasification technology are thoroughly solved.
2) The coal particles are activated in the preheating process, so that the reactivity is improved, and the limitation of the existing entrained flow gasification in the aspects of high ash fusion point, high ash content, high moisture and low reactivity of coal types is solved.
3) The coal particles with large particle size are thermally crushed in the preheating process, so that coal is not required to be prepared into pulverized coal, and the pulverized coal is only required to be crushed and sieved to 0-2 mm, thereby solving the problem of high preparation cost of the pulverized coal of the entrained-flow gasifier.
4) Because the high-temperature preheated fuel enters the entrained-flow gasifier, the preheated oxygen-enriched air can be used as the gasifying agent of the gasifier instead of pure oxygen to maintain the high reaction temperature in the gasifier, thereby improving the economy of the system.
5) CH generated in preheating process 4 Is directly recovered and does not participate in high-temperature reaction in the entrained-flow gasifier, thereby improving CH in the product gas 4 The content is as follows.
The coal gasification method of the invention not only can be used for gasifying raw coal, but also can be used for gasifying biomass, garbage and other carbon-based fuels.
In another aspect, according to the present general inventive concept, there is also provided a preheating type staged gasification device including a pre-preheating chamber, an entrained flow gasifier, and a separation device, wherein the pre-preheating chamber is provided with a fuel inlet and a first gasifying agent inlet, and a preheated gas-solid mixture outlet; the pre-preheating chamber is configured to enable the fuel and the first gasifying agent which are introduced into the pre-preheating chamber to undergo partial combustion reaction, preheat the fuel, generate reducing smoke and preheated fuel, and discharge the generated reducing smoke and preheated fuel through a preheated gas-solid mixture outlet; the separation device is provided with a preheated gas-solid mixture inlet, a preheated fuel outlet and a reducing smoke outlet, wherein the preheated gas-solid mixture inlet is directly or indirectly communicated with the preheated mixture outlet of the pre-preheating chamber, and the separation device is configured to separate the preheated gas-solid mixture received through the outlet of the pre-preheating chamber to form reducing smoke and preheated fuel; the gasification furnace hearth is provided with a preheating fuel inlet, a second gasifying agent inlet, a crude gas outlet and a bottom slag outlet, wherein the preheating fuel inlet is communicated with the preheating fuel outlet of the separation device, the gasification furnace hearth is configured to enable the preheating fuel introduced through the preheating fuel inlet to carry out gasification reaction with the second gasifying agent introduced through the second gasifying agent inlet to generate crude gas and bottom slag, the crude gas is discharged from the crude gas outlet, and the bottom slag is discharged from the bottom slag outlet.
Preferably, the preheating type classifying gasification device further comprises a heat recovery and purification device, wherein the heat recovery and purification device is provided with a reducing smoke inlet and a product gas outlet, the reducing smoke inlet is communicated with a reducing smoke outlet of the separation device, and the heat recovery and purification device is configured to recover heat of the reducing smoke and purify the reducing smoke to obtain product gas;
fig. 2 is a schematic view of a preheating type staged gasification device according to an embodiment of the present invention, as shown in fig. 2, the preheating type staged gasification device includes a pre-preheating chamber 2, an entrained flow gasifier 1, a separation device 3, and a heat recovery and purification device 4, the pre-preheating chamber 2 includes a preheating furnace 20, and further includes a separator 21 and a return 22 sequentially connected to the preheating furnace 20; the entrained-flow gasifier 1 comprises a gasifier hearth 10. Wherein, the inlet of the pre-preheating chamber 2 is arranged on the preheating hearth 20, and comprises a fuel inlet and a first gasifying agent inlet, and the outlet is a flue gas outlet of the separator 21. The pre-preheating chamber 2 is configured to perform partial combustion reaction on the fuel a and the first gasifying agent B introduced into the preheating furnace 20, preheat the fuel, generate a gas-solid mixture, separate the generated gas-solid mixture through the separator 21, form a preheated gas-solid mixture CD, and discharge the preheated gas-solid mixture CD from a flue gas outlet of the separator 21; a preheated gas-solid mixture CD inlet, a preheated fuel D outlet and a reducing flue gas C outlet are arranged on the separation device 3, the preheated gas-solid mixture CD inlet is directly or indirectly communicated with a flue gas outlet of the separator 21, and the separation device 3 is configured to separate the preheated gas-solid mixture CD received through the outlet of the pre-preheating chamber 2 to form reducing flue gas C and preheated fuel D; the heat recovery and purification device 4 is provided with a reducing smoke C inlet and a product gas C1 outlet, the reducing smoke inlet is communicated with a reducing smoke outlet of the separation device 3, and the heat recovery and purification device 4 is configured to recover heat of the reducing smoke C and purify the reducing smoke C to obtain the product gas C1; a preheating fuel inlet, a second gasifying agent inlet, a crude gas outlet and a bottom slag outlet are arranged on the gasification furnace hearth 10, the preheating fuel inlet is communicated with the preheating fuel outlet of the separation device 3, and the gasification furnace hearth 10 is provided with an IB168148F
The device is configured to generate a raw gas G and a bottom slag F by gasifying a preheated fuel D introduced through a preheated fuel inlet and a second gasifying agent E introduced through a second gasifying agent inlet, discharge the raw gas G from a raw gas outlet, and discharge the bottom slag F from a bottom slag outlet.
According to the preheating type staged gasification device of the embodiment, fuel (taking coal as an example) A and a first gasifying agent B react in a pre-preheating chamber 2 to generate a preheated gas-solid mixture CD with the temperature of 800-1300 ℃; the separation device 3 separates the high-temperature gas-solid mixture CD to form high-temperature reducing smoke C and high-temperature preheating fuel D; the heat recovery and purification device 4 recovers sensible heat in the high-temperature reducing flue gas C and removes dust and purifies the sensible heat to obtain product gas C1; the entrained-flow gasifier 1 is used for carrying out entrained-flow gasification reaction on the high-temperature preheated fuel D and the second gasifying agent E to obtain a final product.
As shown in fig. 2, there is no burner in the preheating type staged gasification device, preferably the pre-preheating chamber 2 is a circulating fluidized bed reactor, and no bottom slag outlet is provided in the pre-preheating chamber 2. Alternatively, the entrained-flow bed gasifier 1 may be a liquid slag-discharging entrained-flow bed gasifier or a solid slag-discharging entrained-flow bed gasifier. The number of the pre-preheating chambers 2 may be one or more, and the present invention does not limit the number of the pre-preheating chambers. The separation device 3 in the step b) is one or more stages.
According to the embodiment of the invention, the heat recovery and purification device 4 comprises a heat exchanger 41 and a dust remover 42, the heat exchanger 41 is positioned between the separation device 3 and the dust remover 42, the heat exchanger can be a heat exchange device such as an air preheater, a gas cooler and the like, a high-temperature gas inlet and a high-temperature gas outlet are arranged, the high-temperature gas inlet is communicated with a reducing smoke outlet of the separation device 3, the outlet is communicated with an inlet of the dust remover 42, the dust remover 42 can be a bag-type dust remover, the inlet of the dust remover is provided with an inlet, an ash outlet and a clean gas outlet, the inlet of the dust remover is communicated with the high-temperature gas outlet of the heat exchanger 41, the product gas C1 is discharged from the clean gas outlet after the reducing smoke C introduced into the dust remover 42 is dedusted, and the solid particles D1 are discharged from the ash outlet.
In the embodiment shown in FIG. 2, the gasifier hearth 10 also includes an additional fuel inlet that communicates with the ash discharge of the dust collector 42.
Further, the entrained-flow gasifier 1 may further include a water-cooled slag pool, on which a bottom slag inlet, a chilled water inlet, a slag discharge port and a cooling water outlet are disposed, the bottom slag outlet of the gasifier hearth 10 is communicated with the bottom slag inlet of the water-cooled slag pool, and the chilled water inlet is disposed near the bottom slag inlet.
According to this embodiment, during operation of the preheating type staged gasification device, fuel (coal) a is fed into the preheating furnace 20 of the circulating fluidized bed reactor (pre-preheating chamber 2) from the fuel inlet, oxygen-enriched air + water vapor first gasifying agent B preheated to 600 ℃ enters the preheating furnace 20 from the first gasifying agent inlet, and the ratio of the first gasifying agent B to the coal is reduced to oxygen amount/theoretical oxygen amount of fuel combustion=0.17. The two complete the preheating reaction in the preheating hearth 20, and the generated 950 ℃ high-temperature reducing flue gas C carries all the incompletely reacted small-particle carbon and ash to pass through the separator 21, wherein the incompletely reacted carbon and ash of larger particles are separated by the separator 21 and returned to the preheating hearth 20 through the returning charge device 22, so that the material circulation of a main circulation loop is formed; the rest of the small granular carbon and ash which are not fully reacted are carried by high-temperature reducing flue gas C as high-temperature preheated fuel D, enter a separation device 3 and complete gas-solid separation, wherein the high-temperature preheated fuel D enters a gasifier hearth 10 of the entrained-flow gasifier and undergoes high-temperature gasification reaction with oxygen-enriched air and steam gasifying agent which are preheated to 600 ℃ and are introduced into the gasifier hearth to generate gas rich in CO and H 2 Raw gas G and liquid slag F; the high-temperature reducing flue gas C containing a small amount of solid particles leaves the gasification system, is purified by the heat exchanger 41 and the bag-type dust collector and subjected to sensible heat recovery, is collected as product gas C1, and the solid particles D1 separated by the bag-type dust collector are sent into the entrained-flow gasifier as fuel. Because the high-temperature reducing flue gas C is generated after the coal is preheated under the highly anoxic condition, the flue gas is rich in CH 4 The high-temperature flue gas does not enter the entrained-flow gasifier any more, and the effective gas is not consumed, thereby effectively improving CH in the product gas 4 The content is as follows.
Fig. 3 is a schematic view of a preheating-type staged gasification device according to another embodiment of the present invention, which is substantially the same as the embodiment shown in fig. 2, and only the differences from the embodiment shown in fig. 2 are described below, except that: the embodiment shown in fig. 3 uses less active coal as fuel, fuel (coal) a is fed into the preheating furnace 20 of the circulating fluidized bed reactor (pre-preheating chamber 2) through a fuel inlet, and an air gasifying agent (first gasifying agent B) preheated to 600 ℃ enters the preheating furnace 20 through a first gasifying agent inlet, wherein the ratio of the first gasifying agent B to the fuel a is reduced to the oxygen amount/theoretical oxygen amount of fuel combustion=0.2. Wherein, the solid particles D1 separated by the bag-type dust collector 42 are directly discharged out of the system due to lower temperature, and are not fed into the entrained-flow gasifier any more as fuel, so as to ensure the reaction temperature in the entrained-flow gasifier to the greatest extent.
The preheating type graded gasification method and device of the invention do not need to adopt a burner, and thoroughly solve the technical problems of complex structure and short service life of the burner in the prior entrained flow gasification technology; solves the adaptability problem of coal with high ash fusion point, high ash content, high moisture and low reactivity; solves the problem of high preparation cost of the pulverized coal; pure oxygen is not needed to be used for the gasifying agent, so that the economy is improved; after the coal is preheated, all the coal enters the gasification furnace to participate in the reaction, so that the carbon conversion rate and the coal gas efficiency are improved.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes may be made in these embodiments without departing from the principles and spirit of the invention. The scope of applicability of the present invention is defined by the appended claims and equivalents thereof.
List of reference numerals:
a fuel (coal)
B first gasifying agent
Gas-solid mixture after CD preheating
C reducing flue gas
C1 Product gas
D preheating fuel
D1 Solid particles
E second gasifying agent
F bottom slag
G raw gas
1. Entrained flow gasification furnace
2. Prepositive preheating chamber
3. Separation device
4. Heat recovery and purification device
10. Gasification furnace hearth
20. Preheating hearth
21. Separator
22. Material returning device
41. Heat exchanger
42. Dust remover

Claims (10)

1. A preheating type staged gasification method, characterized in that the preheating type staged gasification method comprises the steps of:
a) Introducing the fuel (A) and the first gasifying agent (B) into a pre-preheating chamber (2) for preheating to generate a preheated gas-solid mixture (CD);
b) The preheated gas-solid mixture (CD) is subjected to gas-solid separation through a separation device (3) to form reducing flue gas (C) and preheated fuel (D);
c) Introducing a second gasifying agent (E) and preheated fuel (D) into an entrained-flow gasifier (1), and performing gasification reaction on the second gasifying agent (E) and the preheated fuel (D) to generate raw gas (G) and bottom slag (F); and
d) Collecting a reducing flue gas (C) and a raw gas (G), and discharging a bottom slag (F) out of the entrained-flow gasifier (1), wherein the reducing flue gas (C) is rich in CH 4 ；
Wherein no bottom slag is discharged in the pre-preheating chamber (2), all the preheated fuel (D) generated in the step b) enters the entrained-flow gasifier (1),
wherein the preheating reaction in the step a) is an anoxic reaction, the ratio of the first gasifying agent to the fuel is reduced to an oxygen amount/fuel combustion theoretical oxygen amount smaller than 0.2, and the partial combustion of the coal is exothermic in the preheating chamber;
wherein the temperature of the preheated gas-solid mixture (CD) is within the range of 800-1300 ℃;
the second gasifying agent (E) is air, oxygen-enriched air or pure oxygen, or a combination of one of the three with water vapor;
the fuel (A) is coal with the particle size of 0-2 mm;
the preheating type staged gasification method does not use a burner;
the pre-preheating chamber (2) is a circulating fluidized bed reactor.
2. The preheat type staged gasification method as claimed in claim 1, wherein: the preheating is that the fuel (A) and the first gasifying agent (B) are subjected to partial combustion reaction, and the fuel is preheated through combustion heat release.
3. The preheat type staged gasification method as claimed in claim 1, wherein: the reducing flue gas (C) is collected by a heat recovery and purification device (4) to form a product gas (C1).
4. A pre-heated staged gasification process as claimed in any one of claims 1 to 3, wherein: the first gasifying agent (B) is air, oxygen-enriched air or pure oxygen, or a combination of one of the three with water vapor.
5. The preheat type staged gasification method as claimed in claim 4, wherein: the temperature of the first gasifying agent (B) which is introduced into the pre-preheating chamber (2) is normal temperature or is preheated to 300-1200 ℃; and/or
The temperature of the second gasifying agent (E) which is introduced into the entrained-flow gasifier (1) is normal temperature or is preheated to 300-1200 ℃.
6. The preheat type staged gasification method as claimed in claim 5, wherein: the first gasifying agent (B) has been preheated to 600 ℃; and/or the second gasifying agent (E) has been preheated to 600 ℃.
7. A preheating type staged gasification device for executing the preheating type staged gasification method as claimed in claim 1, characterized in that the preheating type staged gasification device comprises a pre-preheating chamber (2), an entrained flow gasifier (1) and a separation device (3);
wherein the pre-preheating chamber (2) is provided with a fuel inlet, a first gasifying agent inlet and a preheated gas-solid mixture outlet;
the separation device (3) is provided with a preheated gas-solid mixture inlet, a preheated fuel outlet and a reducing smoke outlet, and the preheated gas-solid mixture inlet is directly or indirectly communicated with the preheated gas-solid mixture outlet of the pre-preheating chamber (2);
a preheating fuel inlet, a second gasifying agent inlet, a raw gas outlet and a bottom slag outlet are arranged on the entrained-flow gasifier (1), and the preheating fuel inlet is communicated with a preheating fuel outlet of the separation device (3);
wherein, a bottom slag outlet is not arranged in the pre-preheating chamber (2);
the preheating type grading gasification device is not provided with a burner;
the pre-preheating chamber (2) is a circulating fluidized bed reactor.
8. The preheat type staged gasification device as claimed in claim 7, wherein: the separation device (3) is one-stage or multi-stage.
9. The preheat type staged gasification device as claimed in claim 7, wherein: the preheating type grading gasification device also comprises a heat recovery and purification device (4), and the heat recovery and purification device (4) comprises a heat exchanger (41) and a dust remover (42);
the heat recovery and purification device (4) is provided with a reducing smoke inlet and a product gas outlet, and the reducing smoke inlet is communicated with a reducing smoke outlet of the separation device (3).
10. The preheat type staged gasification device as claimed in claim 7, wherein: the entrained-flow gasifier (1) comprises a gasifier hearth (10), and the gasifier hearth (10) further comprises an additional fuel inlet which is communicated with an ash discharge port of the dust remover (42).
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