CN110684562A - Gasification furnace with radiation heat exchange and gasification method - Google Patents

Gasification furnace with radiation heat exchange and gasification method Download PDF

Info

Publication number
CN110684562A
CN110684562A CN201810734782.XA CN201810734782A CN110684562A CN 110684562 A CN110684562 A CN 110684562A CN 201810734782 A CN201810734782 A CN 201810734782A CN 110684562 A CN110684562 A CN 110684562A
Authority
CN
China
Prior art keywords
heat exchange
chamber
gasification
slag
synthesis gas
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.)
Pending
Application number
CN201810734782.XA
Other languages
Chinese (zh)
Inventor
毛炜
黄萍
张燕
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.)
Beijing Aerospace Maiwei Technology Co Ltd
Original Assignee
Beijing Aerospace Maiwei Technology Co Ltd
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 Beijing Aerospace Maiwei Technology Co Ltd filed Critical Beijing Aerospace Maiwei Technology Co Ltd
Priority to CN201810734782.XA priority Critical patent/CN110684562A/en
Priority to PCT/CN2018/122284 priority patent/WO2020006994A1/en
Publication of CN110684562A publication Critical patent/CN110684562A/en
Pending legal-status Critical Current

Links

Images

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
    • C10J3/485—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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/52—Ash-removing devices
    • 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
    • C10J3/52—Ash-removing devices
    • C10J3/526—Ash-removing devices for 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
    • C10J3/72—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
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/74—Construction of shells or jackets
    • C10J3/76—Water jackets; Steam boiler-jackets
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
  • Gasification And Melting Of Waste (AREA)

Abstract

The invention relates to a gasification furnace with radiation heat exchange and a gasification method. The top of the gasification chamber is provided with a burner connecting port, raw material coal and pure oxygen are injected into the gasification chamber through a burner to carry out coal gasification reaction, and the reacted crude synthesis gas and molten ash slag flow downwards to enter a slag discharging port. The airflow and the molten ash entering the radiation heat exchange chamber are still kept in a rotational flow shape under the constraint of a special rotational flow structure of the slag discharging port, the follow-up property of the ash and the airflow in the crude synthesis gas is kept, the collision between the ash and the inner wall of the radiation heat exchanger is reduced, and the probability that the ash is randomly diffused to the inner wall surface of the radiation heat exchange chamber is greatly reduced. Meanwhile, the heat exchange screen on the inner wall surface of the radiation heat exchanger deflects at a certain angle along the rotational flow direction, so that the slag passing drift diameter is increased, the disturbance of the inner edge of the heat exchange screen to air flow is weakened, and the risk of slag deposition is structurally reduced.

Description

Gasification furnace with radiation heat exchange and gasification method
Technical Field
The invention belongs to the technical field of coal chemical industry, and particularly relates to a gasification furnace with radiation heat exchange and a gasification method.
Background
Since the twenty-first century, the coal chemical industry in China enters a high-speed development stage, the fixed bed gasification technology, the fluidized bed gasification technology and the entrained flow bed gasification technology are developed sufficiently, and new technology and new process are developed continuously like bamboo shoots in spring after rain. Through the verification of industrial devices and the screening of markets, the entrained-flow bed gasification technology becomes the mainstream gasification technology for various chemicals made from coal, the technology is far superior to other gasification technologies in the aspects of energy conservation and emission reduction, and the technology is in the front of the industry in the aspect of large-scale devices, and the daily coal treatment capacity of a single gasification furnace reaches 3000 tons.
The entrained flow gasification technology comprises a chilling process and a waste boiler process from the aspects of energy recovery and temperature reduction measures of the crude synthesis gas.
The chilling process means that the crude synthesis gas at 1300-1600 ℃ directly enters a water bath at 200-250 ℃ from the outlet of the gasification chamber, and the high-temperature crude synthesis gas is rapidly cooled to a low temperature. The process has the characteristics that the device is stable, the operation is simple, the gasification furnace can run for a long period, but the high-temperature sensible heat of the crude synthesis gas is not fully utilized in the gasification process, the crude synthesis gas at 1300-1600 ℃ is directly chilled to about 220 ℃, the high-temperature sensible heat is converted into low-temperature saturated steam, and the energy efficiency index is low. In addition, in order to ensure that the gasification furnace operates stably, factories mostly operate according to the maximum capacity of a chilling water pump, so that the amount of black water discharged out of the gasification furnace is greatly increased, more energy in high-temperature synthesis gas is brought to a flash evaporation system, and a large amount of low-grade steam containing ash is produced. In the flash evaporation system, only the grey water preheating and deaerator water replenishing preheating can consume part of steam, and the rest part of steam cannot be replenished into a low-pressure steam pipe network due to dust, and can only be emptied in place, so that the economic efficiency of a factory is reduced.
The waste pot process comprises a full waste pot process and a half waste pot process. The total waste boiler process means that crude synthesis gas at 1300-1600 ℃ passes through the radiation waste boiler and the convection waste boiler from the outlet of the gasification chamber in sequence, the temperature at the outlet of the convection waste boiler is reduced to about 350 ℃, and the effective gas (CO + H) per thousand standard squares is2) 0.7-0 part of high-temperature superheated steam can be produced as a byproductAnd 9t, optimizing the energy efficiency index. However, the water-gas ratio (water vapor amount/dry gas amount) in the process synthesis gas is only 0.2-0.3, and the process is more suitable for IGCC combined power generation, if a chemical product is used, a large amount of steam, especially a hydrogen production product, needs to be supplemented into the system in a conversion device, the water-gas ratio needs to be increased to about 1.0, the amount of the steam which is a net byproduct of the device is greatly reduced, and the produced economic benefit cannot make up for the increased device investment. In addition, the existing full-waste boiler process has extremely strict requirements on the coal quality of raw material coal, parameters including ash content, volatile matter content, ash melting point, viscosity-temperature characteristics, silicon-aluminum ratio, potassium-sodium content and the like need to be stabilized within a narrow range through coal blending of various coals, and localization of the raw material coal cannot be realized.
The semi-waste pot flow refers to that coarse synthesis gas at 1300-1600 ℃ is subjected to heat exchange from the outlet of the gasification chamber only through a radiation waste pot, a certain amount of saturated steam is byproduct and then cooled to 700-900 ℃, and the temperature is chilled in a water bath, wherein the water-gas ratio of the synthesis gas after being chilled is equivalent to that of the chilling flow. Along with the difference of the operation conditions, the water-gas ratio is generally between 0.8 and 1.2, so that the steam can not be supplemented or only a small amount of steam can be supplemented in the conversion section, and the process flow is more effective and accords with the chemical production.
In the domestic gasification device, the mature process only comprises a chilling process and a full waste pot process, and a half waste pot process is still in a research and development or test operation stage. The waste boiler is integrated with a gasification device which is started and contains the waste boiler, and the reasons of slag blockage and dust accumulation of the waste boiler, leakage of a heat exchange tube and the like are important reasons of short operation period and poor stability of the device. Therefore, how to efficiently utilize the high-temperature sensible heat of the raw synthesis gas and ensure that the gasification furnace can stably operate for a long period is still an unsolved problem in the technical field.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a gasification furnace with radiation heat exchange and long operation period and good stability and a gasification method.
The technical scheme adopted by the invention is as follows:
a gasification furnace with radiation heat exchange comprises a shell and a furnace body arranged in the shell, wherein the furnace body comprises a gasification chamber, a radiation heat exchange chamber and a chilling chamber which are coaxially arranged from top to bottom;
the gasification chamber comprises a burner connecting port positioned at the top, a slag discharge port with rotational flow positioned at the bottom and a gasification reaction chamber positioned between the top and the bottom, and the gasification reaction chamber is provided with a water-cooled wall;
the wall surface of the radiation heat exchange chamber is a membrane water-cooling wall, the upper part of the inner side of the membrane water-cooling wall is provided with an injection device, and the injection device comprises a plurality of annular cooling spray heads which are arranged in a layered manner; the inner wall surface of the membrane water-cooling wall is provided with a plurality of heat exchange screens; a flow guide exhaust cylinder is arranged at the lower part of the radiation heat exchange chamber, and the flow guide exhaust cylinder is of an inverted cone structure;
the chilling chamber is positioned below the diversion exhaust funnel, and a chilling spray nozzle is arranged at the top of the chilling chamber.
The inner diameter of the slag discharging opening is smaller than that of the gasification reaction chamber, and the ratio of the inner diameter of the slag discharging opening to that of the gasification reaction chamber is 1: 3-1: 8.
The inner diameter of the slag discharging opening is smaller than that of the radiation heat exchange chamber, and the ratio of the inner diameter of the slag discharging opening to that of the radiation heat exchange chamber is 1: 3-1: 8.
And a rotational flow guide groove in the same direction as the air flow is arranged in the slag discharging opening.
The included angle alpha between the contraction inclined plane of the flow guide exhaust cylinder and the horizontal direction is 65-75 degrees.
The projection of the membrane water-cooling wall in the horizontal direction is circular or polygonal.
When the projection of the membrane water-cooling wall on the horizontal plane is circular, the heat exchange screen has a deflection angle beta relative to the radial direction of the membrane water-cooling wall;
when the projection of the membrane water-cooling wall on the horizontal plane is a polygon, the heat exchange screen has a deflection angle beta relative to the perpendicular line of the membrane water-cooling wall.
The deflection angle beta is in the range of 0-45 deg.
The chilling spray nozzle is annularly arranged on the inner wall of the chilling chamber.
A water-cooled wall boiler water inlet N4 of the gasification chamber is arranged on the shell and corresponds to the lower part of the gasification chamber, and a steam-water outlet N3 of the water-cooled wall of the gasification chamber is arranged on the shell and corresponds to the upper part of the gasification chamber;
the top of the shell is provided with a burner connecting pipe opening N1, and the bottom of the shell is provided with a gasification furnace slag discharge opening N2.
The boiler is characterized in that a membrane water-cooling wall boiler water inlet is formed in the shell and corresponds to the bottom of the radiation heat exchange chamber, a membrane water-cooling wall steam-water outlet is formed in the shell and corresponds to the top of the radiation heat exchange chamber, a side area cooling water inlet is formed in the shell and corresponds to the upper portion of the radiation heat exchange chamber, and the side area cooling water inlet is communicated with the cooling spray head.
And a chilling water inlet is arranged on the shell and corresponds to the top of the chilling chamber, and the chilling water inlet is communicated with the chilling spray nozzle.
A gasification method based on the gasification furnace comprises the following steps:
(a) injecting raw material coal and pure oxygen into a gasification reaction chamber through a gasification burner for coal gasification reaction, and making the reacted high-temperature crude synthesis gas and molten-state ash swirl to flow downwards into a slag discharging port with swirl;
(b) under the action of the rotational flow structure of the slag discharging port with rotational flow, the high-temperature crude synthesis gas and the molten state ash slag entering the radiation heat exchange chamber still keep rotational flow shape;
(c) in the radiation heat exchange chamber, high-level heat energy of high-temperature crude synthesis gas and molten ash slag is absorbed by a film-type water-cooled wall and a heat exchange screen, the temperature of the crude synthesis gas is reduced, and the ash slag is converted into a solid state from a molten state;
(d) the crude synthesis gas and the solid ash after the high-level heat energy is recovered by the radiation heat exchange chamber enter a chilling chamber water bath, and the crude synthesis gas is rapidly humidified and cooled and is separated from the solid ash; the crude synthesis gas is washed and then sent out, and solid ash is discharged from the bottom of the gasification furnace.
In the step (a), the coal gasification reaction temperature is 1300-1600 ℃, and the temperature of the high-temperature crude synthesis gas after the reaction is 1300-1600 ℃.
In the step (d), the temperature of the crude synthesis gas after the high-level heat energy is recovered by the radiation heat exchange chamber is 700-900 ℃.
The invention has the beneficial effects that:
1. the invention relates to a gasification furnace with radiation heat exchange, which comprises a gasification chamber, a radiation heat exchange chamber and a chilling chamber which are coaxially arranged from top to bottom in sequence. The top of the gasification chamber is provided with a burner connecting port, raw material coal and pure oxygen are injected into the gasification chamber through a burner to carry out coal gasification reaction, and the reacted crude synthesis gas and molten ash slag flow downwards to enter a slag discharging port. The airflow and the molten ash entering the radiation heat exchange chamber are still kept in a rotational flow shape under the constraint of a special rotational flow structure of the slag discharging port, the following performance of the ash and the airflow is enhanced, and the probability of randomly diffusing the ash to the inner wall surface of the radiation heat exchange chamber is greatly reduced. Meanwhile, the heat exchange screen on the inner wall of the radiation heat exchanger deflects at a certain angle along the rotational flow direction, so that the slag passing drift diameter is increased, the disturbance of the inner edge of the heat exchange screen to air flow is weakened, and the risk of slag deposition is structurally reduced.
2. In the radiation heat exchange chamber, the carbon which is not completely reacted and the generated CO2Still in the process of the Boolean reaction, CO and the injected water are subjected to a shift reaction, so that the effective gas (CO + H) in the raw synthesis gas at the outlet of the radiant heat exchanger2) The content is increased by 1-2%, and the hydrogen-carbon ratio (H)2/CO) is improved by 0.1, and the gasification performance is improved.
3. According to the invention, a group of annular and layered injection devices are arranged on the inner side of the membrane water-cooling wall at the upper part of the radiation heat exchange chamber, and a low-temperature region (lower than 900 ℃) close to the membrane water-cooling wall and a core high-temperature region (higher than 900 ℃) positioned in the center are formed by medium injection, so that edge region cooling is realized. The side area cooling technology can effectively reduce the wall surface temperature of the top area of the radiation heat exchange chamber and ensure that the radiation heat exchange chamber can run for a long period. In the central area of the crude synthesis gas, the temperature is still high, the radiation heat exchange capacity is strong, and the high radiation heat exchange efficiency is ensured.
4. According to the invention, the radiation heat exchange screen with the deflection angle is additionally arranged on the inner side of the membrane water-cooling wall of the radiation heat exchange chamber, so that the heat exchange area of the radiation waste boiler with unit height is increased, the eddy flow formed by the swirling crude synthesis gas and ash residues on the edge of the innermost side of the heat exchange screen is avoided, the slag passing diameter is increased on the premise of not increasing the size of equipment, and the risk of slag bonding and ash deposition is structurally reduced.
5. The high-temperature sensible heat of the crude synthesis gas is recovered in the radiation heat exchange chamber, the temperature of the crude synthesis gas before chilling is still higher than the desublimation temperature of alkali metal oxides such as potassium, sodium and the like and salts thereof, and the problem of slag blockage caused by high alkali metal content is avoided. The requirements on parameters such as viscosity-temperature characteristics and ash content of the raw material coal are wide, and the usable raw materials comprise lignite, bituminous coal, anthracite, coal coke, petroleum coke and the like, so that the localization of the raw material coal can be realized.
6. The gasification furnace recovers the high-temperature sensible heat of the crude synthesis gas, improves the utilization efficiency of energy, and has effective gas (CO + H) per thousand standard squares2) The byproduct of 4-12 MPa saturated steam is 0.5-1.0 t, the water-gas ratio of the synthetic gas at the outlet of the gasification furnace is equivalent to that of the chilling process gasification technology in the prior art, and the consumption of a downstream working section is not increased. Meanwhile, the chilling water flow is reduced to 30-70% of the chilling process, the load of a flash evaporation section is reduced, the water circulation amount is correspondingly reduced, the overall economic benefit is increased, and the effective gas cost per unit volume is reduced by about 10%.
7. The gasification furnace provided by the invention fundamentally solves the problems of slag bonding and ash accumulation in the radiation heat exchange process, and ensures that the device realizes 'stable growth and full excellence'.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
Fig. 1 is a schematic structural diagram of a gasifier with radiant heat exchange provided in embodiment 1 of the present invention;
FIG. 2 is a schematic structural diagram of a section of a straight cylinder part of a radiation heat exchange chamber provided by the embodiment 1 of the invention;
fig. 3 is a schematic structural diagram of a gasifier with radiant heat exchange provided in embodiment 2 of the present invention;
fig. 4 is a structural schematic diagram of a straight cylinder part section of a radiation heat exchange chamber provided by the embodiment 2 of the invention.
In the figure, 1-a gasification burner, 2-a gasification reaction chamber, 3-a water-cooled wall, 4-a slag discharging opening with rotational flow, 5-a cooling spray nozzle, 6-a membrane water-cooled wall, 7-a radiation heat exchange chamber, 8-a shell, 9-a guide exhaust funnel, 10-a chilling spray nozzle, 11-a chilling chamber water bath and 12-a heat exchange screen;
n1-a burner connecting pipe orifice, N2-a gasifier deslagging port, N3-a gasification chamber water-cooled wall steam-water outlet, N4-a gasification chamber water-cooled wall boiler water inlet, N5-a membrane water-cooled wall steam-water outlet, N6-a side area cooling water inlet, N7-a membrane water-cooled wall boiler water inlet, N8-a chilling water inlet, N9-a synthetic gas outlet, N9' -a synthetic gas and black water mixed discharge port and N10-a gasifier black water discharge port.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the technical solutions of the present invention will be described in detail below. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments, which can be derived by a person skilled in the art from the examples given herein without any inventive step, are within the scope of the present invention.
Example 1
The embodiment provides a gasifier with radiant heat exchange, the structure of which is shown in fig. 1, and the gasifier comprises a shell 8 and a furnace body arranged in the shell 8, wherein the furnace body comprises a gasification chamber, a radiant heat exchange chamber 7 and a chilling chamber which are sequentially and coaxially arranged from top to bottom.
The gasification chamber comprises a burner connecting port positioned at the top, a slag tap 4 with rotational flow positioned at the bottom and a gasification reaction chamber 2 positioned between the top and the bottom, the burner connecting port is connected with a gasification burner 1, and the gasification reaction chamber 2 is provided with a water-cooled wall 3; a water-cooled wall boiler water inlet N4 of the gasification chamber is arranged on the shell 8 corresponding to the lower part of the gasification chamber, and a steam-water outlet N3 of the water-cooled wall of the gasification chamber is arranged on the shell 8 corresponding to the upper part of the gasification chamber; the top of the shell 8 is provided with a burner connecting pipe opening N1. Raw material coal and pure oxygen are injected into a gasification chamber through a burner to carry out coal gasification reaction at 1300-1600 ℃, the raw material coal and the pure oxygen are constrained by a special rotational flow structure of the gasification burner 1, the reacted crude synthesis gas and molten ash are rotated and flow downwards, large-particle slag is thrown to the inner wall surface of a water-cooled wall 3 to form a protective slag layer, when the slag layer reaches a certain thickness, the thickness of the slag layer is not increased, and the inner wall surface is not cooled, and a liquid slag layer flows downwards to enter a slag outlet. The crude gas and part of the fine particle ash slag also flow out of the gasification reaction chamber 2 and enter a slag discharging port.
And a rotational flow guide groove in the same direction as the air flow is arranged in the slag discharging opening. The inner diameter of the slag discharging port is smaller than that of the gasification reaction chamber 2, and the ratio of the inner diameter of the slag discharging port to the inner diameter of the gasification reaction chamber 2 is 1: 3-1: 8; the inner diameter of the slag discharging opening is smaller than that of the radiation heat exchange chamber 7, and the ratio of the inner diameter of the slag discharging opening to that of the radiation heat exchange chamber 7 is 1: 3-1: 8. The reason for this is that: the lower slag hole 4 with rotational flow is a connecting channel between the gasification reaction chamber 2 and the radiation heat exchange chamber 7, the inner diameter of the lower slag hole is far smaller than the inner diameter of the gasification reaction chamber 2 above the lower slag hole and the inner diameter of the radiation heat exchange chamber 7 below the lower slag hole, the flow field of the high-temperature crude synthesis gas and the fused ash slag in the gasification furnace is firstly contracted and then expanded, the flow speed at the contracted position is fastest, a rotational flow guide groove with the same rotational direction as the airflow is arranged in the lower slag hole, when the high-temperature crude synthesis gas and the fused ash slag pass through at high speed, the rotational flow strength of the airflow is enhanced, the circumferential movement speed of the airflow is increased, and the flow field of the crude synthesis gas discharged from the lower slag hole under different operation conditions is in. The device can avoid the radial rapid random diffusion of the crude synthesis gas after the crude synthesis gas is discharged from the slag discharge port, maintain the following performance of ash residues and air flow in the crude synthesis gas, reduce the collision between the ash residues and the inner wall of the radiation heat exchanger, and greatly reduce the ash deposition and slagging tendency of the crude synthesis gas and the ash residues after entering the radiation heat exchange chamber 7.
The wall surface of the radiation heat exchange chamber 7 is a membrane water-cooling wall 6, and the projection of the membrane water-cooling wall 6 in the horizontal direction is circular. And a spraying device is arranged at the upper part of the inner side of the membrane water-cooled wall 6, and the spraying device comprises a plurality of annular cooling spray heads 5 which are arranged in a layered mode. And (3) spraying a medium (cooling water is used as a spraying medium in the embodiment) by using the cooling spray head 5 to form a low-temperature area (lower than 900 ℃) close to the membrane water wall 6 and a core high-temperature area (higher than 900 ℃) positioned in the center, so that edge area cooling is realized. A membrane water wall boiler water inlet N7 is arranged on the shell 8 and corresponding to the bottom of the radiation heat exchange chamber 7, a membrane water wall steam-water outlet N5 is arranged on the shell 8 and corresponding to the top of the radiation heat exchange chamber 7, a side area cooling water inlet N6 is arranged on the shell 8 and corresponding to the upper part of the radiation heat exchange chamber 7, and the side area cooling water inlet N6 is communicated with the cooling spray head 5.
The edge area cooling technology has the following characteristics: (1) the surface temperature of the membrane type water-cooled wall 6 is low, so that the membrane type water-cooled wall cannot be directly contacted with high-temperature crude synthesis gas, and the long-period operation of equipment is guaranteed; (2) after the cooling of the jet medium, the ash slag at the edge area of the crude synthesis gas is converted from liquid state to solid state, even if the ash slag contacts the heat exchange surface, the ash slag can not form bonding slag, only loose dry ash can be attached, and the ash slag falls off by the vibration or the driving force of the equidirectional airflow; (3) the central high-temperature area still keeps strong radiation capability, and the heat exchange effect is equivalent to that of the scheme of not increasing the cooling of the edge area; (4) the edge region cooling scheme only influences the movement locus of small particle solids at the boundary of the airflow, has little influence on the movement locus of large particles and the central particles of the airflow, and greatly reduces the probability of the contact of molten ash and the heat exchange surface.
A flow guide exhaust cylinder 9 is arranged at the lower part of the radiation heat exchange chamber 7, and the flow guide exhaust cylinder 9 is of an inverted cone structure; an included angle alpha between a contraction inclined plane of the flow guide exhaust cylinder 9 and the horizontal direction is 60-75 degrees, and alpha is larger than the repose angle of ash at the temperature, and under the condition, only a small amount of solid ash particles can be attached to the inner wall surface of the flow guide exhaust cylinder 9. Under the drive of the airflow flowing in the same direction, the adhered solid ash particles collide with new solid ash particles in the airflow to fall off. Therefore, the guide exhaust funnel 9 has no working condition that a large amount of solid ash is accumulated and the opening of the funnel is blocked to influence slag discharge.
In order to enhance the effect of radiation heat exchange, as shown in fig. 2, a plurality of heat exchange screens 12 are arranged on the inner wall surface of the membrane water-cooling wall 6. The diameter of the tangent circle formed by the inner edge of the heat exchange screen 12 is defined as the diameter of the slag passing, i.e. the clear space diameter through which the ash can pass unimpeded, within which diameter the molten ash does not touch the radiant heat exchange chamber 7 internals. The preferable slag passing diameter is 1.5-2 times larger than the inner diameter of the slag discharging opening.
In order to ensure that the diameter of the shell of the gasification furnace is not increased and the diameter of the slag is increased, the heat exchange screen 12 deflects to a certain angle (beta) from the original radial direction vertical to the circular membrane type water-cooled wall 6 to the direction of the forward swirling flow. The method specifically comprises the following steps: the projection of the membrane water-cooling wall 6 on the horizontal plane is circular, and the heat exchange screen 12 has a deflection angle beta relative to the radial direction of the membrane water-cooling wall 6; the value range of the deflection angle beta is 0-45 degrees. The deflection direction of the heat exchange screen 12 is consistent with the swirling direction of the high-temperature crude synthesis gas and ash slag, the deflection angle beta is adjustable, and the angle control value is adjusted according to different operation coal types and different operation conditions. After the heat exchange screen 12 is deflected for a certain angle, the total radiation heat exchange area is basically kept unchanged, the diameter of the slag passing is increased from d2 to d3, and the net area of the circulation of the crude synthesis gas and the ash slag is further increased. In addition, the inner edge of the heat exchange screen 12 is not perpendicular to the circumferential motion of the swirling crude synthesis gas any more, so that turbulence at the position of the gas flow boundary is not increased, the flow shape of the crude synthesis gas is kept basically unchanged, the collision probability of ash fine particles and the surface of the heat exchange screen 12 is reduced, and the ash deposition tendency is weakened.
After radiation heat exchange, the temperature of the crude synthesis gas is reduced from 1300-1600 ℃ to 700-900 ℃, ash slag is completely converted into solid from molten state, and each thousand square of effective gas (CO + H)2) The byproduct of saturated steam with pressure of 4-12 MPa is 0.5-1.0 t. The steam can enter a steam pipe network with a corresponding grade after being superheated by a heat device to be used as power steam.
The chilling chamber is located below the diversion exhaust funnel 9, a chilling chamber water bath 11 is arranged at the lower part of the chilling chamber, a plurality of chilling spray nozzles 10 are arranged at the top of the chilling chamber, the chilling spray nozzles 10 are annularly arranged, a chilling water inlet N8 is arranged at the top of the chilling chamber on the shell 8 and corresponds to the chilling chamber, and the chilling water inlet N8 is communicated with the chilling spray nozzles 10.
A large amount of quench water is sprayed into the interior of the furnace at the top of the quench chamber through said quench nozzles 10. The method comprises the steps of fully mixing crude synthesis gas at the temperature of about 700-900 ℃ with chilling water, quickly cooling to 200-230 ℃, fully mixing impacted water drops, the crude synthesis gas and ash, allowing the synthesis gas to flow out of a gasification furnace from a synthesis gas outlet N9 at the upper part of a chilling chamber through gas-liquid separation, and allowing the synthesis gas to enter a downstream washing device. Gasified black water passes through a chilling chamber water bath 11, is discharged from a gasification furnace black water discharge port N10 at the lower part of the chilling chamber, and is sent to a flash evaporation system for energy recovery; the ash slag is discharged from a gasification furnace slag discharge port N2 arranged at the bottom. The high-temperature crude synthesis gas and the ash slag sequentially pass through the gasification reaction chamber 2, the lower slag hole 4 with rotational flow and the radiation heat exchange chamber 7 and enter the chilling chamber water bath 11, and the high-temperature crude synthesis gas and the ash slag have certain rotational flow effect when passing through each chamber or channel, and the rotational flow directions are kept consistent. Through accounting, for the gasification device with the same gas production rate, the consumption of the chilling water in the semi-waste boiler process is about 30-70% of that in the chilling process, and the energy-saving effect is obvious.
Example 2
The embodiment provides another gasifier with radiant heat exchange, and the structure of the gasifier is shown in fig. 3, and the gasifier comprises a shell 8 and a furnace body arranged in the shell 8, wherein the furnace body comprises a gasification chamber, a radiant heat exchange chamber 7 and a chilling chamber which are coaxially arranged from top to bottom in sequence.
The gasification chamber comprises a burner connecting port positioned at the top, a slag tap 4 with rotational flow positioned at the bottom and a gasification reaction chamber 2 positioned between the top and the bottom, the burner connecting port is connected with a gasification burner 1, and the gasification reaction chamber 2 is provided with a water-cooled wall 3; a water-cooled wall boiler water inlet N4 of the gasification chamber is arranged on the shell 8 corresponding to the lower part of the gasification chamber, and a steam-water outlet N3 of the water-cooled wall of the gasification chamber is arranged on the shell 8 corresponding to the upper part of the gasification chamber; the top of the shell 8 is provided with a burner connecting pipe opening N1. Raw material coal and pure oxygen are injected into a gasification chamber through a burner to carry out coal gasification reaction at 1300-1600 ℃, the raw material coal and the pure oxygen are constrained by a special rotational flow structure of the gasification burner 1, the reacted crude synthesis gas and molten ash are rotated and flow downwards, large-particle slag is thrown to the inner wall surface of a water-cooled wall 3 to form a protective slag layer, when the slag layer reaches a certain thickness, the thickness of the slag layer is not increased, and the inner wall surface is not cooled, and a liquid slag layer flows downwards to enter a slag outlet. The crude gas and part of the fine particle ash slag also flow out of the gasification reaction chamber 2 and enter a slag discharging port.
And a rotational flow guide groove in the same direction as the air flow is arranged in the slag discharging opening. The inner diameter d1 of the slag discharging port is smaller than the inner diameter of the gasification reaction chamber 2, and the ratio of the inner diameter d1 of the slag discharging port to the inner diameter of the gasification reaction chamber 2 is 1: 3-1: 8; the inner diameter d1 of the slag discharging port is smaller than the inner diameter of the radiation heat exchange chamber 7, and the ratio of the inner diameter d1 of the slag discharging port to the inner diameter of the radiation heat exchange chamber 7 is 1: 3-1: 8. The reason for this is that: the lower slag hole 4 with rotational flow is a connecting channel between the gasification reaction chamber 2 and the radiation heat exchange chamber 7, the inner diameter d1 of the lower slag hole is far smaller than the inner diameter of the gasification reaction chamber 2 above the lower slag hole and the inner diameter of the radiation heat exchange chamber 7 below the lower slag hole, the flow field of the high-temperature crude synthesis gas and the fused ash slag in the gasification furnace is expanded after being contracted, the flow speed at the contracted position is fastest, a rotational flow guide groove with the same rotational direction as the airflow is arranged in the lower slag hole, when the high-temperature crude synthesis gas and the fused ash slag pass through at high speed, the rotational flow strength of the airflow is enhanced, the circumferential movement rate of the airflow is increased, and the flow field of the crude synthesis gas discharged from the lower slag hole under different operation conditions is in a. The device can avoid the radial rapid random diffusion of the crude synthesis gas after the crude synthesis gas is discharged from the slag discharge port, maintain the following performance of ash residues and air flow in the crude synthesis gas, reduce the collision between the ash residues and the inner wall of the radiation heat exchanger, and greatly reduce the ash deposition and slagging tendency of the crude synthesis gas and the ash residues after entering the radiation heat exchange chamber 7.
The wall surface of the radiation heat exchange chamber 7 is a membrane water-cooling wall 6, and the projection of the membrane water-cooling wall 6 in the horizontal direction is a regular polygon. Preferably, the projection of the membrane water wall 6 in the horizontal direction in the present embodiment is a regular octagon; and a spraying device is arranged at the upper part of the inner side of the membrane water-cooled wall 6, and the spraying device comprises a plurality of annular cooling spray heads 5 which are arranged in a layered mode. And (3) spraying a medium (cooling water is used as a spraying medium in the embodiment) by using the cooling spray head 5 to form a low-temperature area (lower than 900 ℃) close to the membrane water wall 6 and a core high-temperature area (higher than 900 ℃) positioned in the center, so that edge area cooling is realized. A membrane water wall boiler water inlet N7 is arranged on the shell 8 and corresponding to the bottom of the radiation heat exchange chamber 7, a membrane water wall steam-water outlet N5 is arranged on the shell 8 and corresponding to the top of the radiation heat exchange chamber 7, a side area cooling water inlet N6 is arranged on the shell 8 and corresponding to the upper part of the radiation heat exchange chamber 7, and the side area cooling water inlet N6 is communicated with the cooling spray head 5.
The edge area cooling technology has the following characteristics: (1) the surface temperature of the membrane type water-cooled wall 6 is low, so that the membrane type water-cooled wall cannot be directly contacted with high-temperature crude synthesis gas, and the long-period operation of equipment is guaranteed; (2) after the spraying medium is cooled, the ash slag at the edge area of the crude synthesis gas is converted into a solid state from a liquid state, bonding slag is not formed even if the ash slag contacts the heat exchange surface, only loose dry ash can be hung, and the ash slag falls off by the vibration or the driving force of the equidirectional airflow; (3) the central high-temperature area still keeps strong radiation capability, and the heat exchange effect is equivalent to that of the scheme of not increasing the cooling of the edge area; (4) the edge region cooling scheme only influences the movement locus of small particle solids at the boundary of the airflow, has little influence on the movement locus of large particles and the central particles of the airflow, and greatly reduces the probability of the contact of molten ash and the heat exchange surface.
A flow guide exhaust cylinder 9 is arranged at the lower part of the radiation heat exchange chamber 7, and the flow guide exhaust cylinder 9 is of an inverted cone structure; an included angle alpha between a contraction inclined plane of the flow guide exhaust cylinder 9 and the horizontal direction is 60-75 degrees, and alpha is larger than the repose angle of ash at the temperature, and under the condition, only a small amount of solid ash particles can be attached to the inner wall surface of the flow guide exhaust cylinder 9. Under the drive of the airflow flowing in the same direction, the adhered solid ash particles collide with new solid ash particles in the airflow to fall off. Therefore, the guide exhaust funnel 9 has no working condition that a large amount of solid ash is accumulated and the opening of the funnel is blocked to influence slag discharge.
In order to enhance the effect of radiation heat exchange, as shown in fig. 4, a plurality of heat exchange screens 12 are arranged on the inner wall surface of the membrane water-cooling wall 6. The diameter of the tangent circle formed by the inner edge of the heat exchange screen 12 is defined as the diameter of the slag passing, i.e. the clear space diameter through which the ash can pass unimpeded, within which diameter the molten ash does not touch the radiant heat exchange chamber 7 internals. The preferable slag passing diameter is 1.5-2 times larger than the inner diameter of the slag discharging opening.
In order to ensure that the diameter of the shell of the gasification furnace is not increased and the diameter of the slag is increased, the heat exchange screen 12 deflects to a certain angle (beta) from the direction vertical to the regular polygonal membrane type water-cooled wall 6 to the direction of the forward swirling flow. The method specifically comprises the following steps: the projection of the membrane water-cooling wall 6 on the horizontal plane is a polygon, and the heat exchange screen 12 has a deflection angle beta relative to the perpendicular line of the membrane water-cooling wall 6; the value range of the deflection angle beta is 0-45 degrees. The deflection direction of the heat exchange screen 12 is consistent with the swirling direction of the high-temperature crude synthesis gas and ash slag, the deflection angle beta is adjustable, and the angle control value is adjusted according to different operation coal types and different operation conditions. After the heat exchange screen 12 is deflected for a certain angle, the total radiation heat exchange area is basically kept unchanged, the diameter of the slag passing is increased from d2 to d3, and the net area of the circulation of the crude synthesis gas and the ash slag is further increased. In addition, the edge of the heat exchange screen 12 is not perpendicular to the circumferential motion of the swirling crude synthesis gas any more, so that the turbulence of the boundary position of the gas flow is not increased, the flow shape of the crude synthesis gas is kept basically unchanged, the collision probability of ash fine particles and the surface of the heat exchange screen 12 is reduced, and the ash deposition tendency is weakened.
After radiation heat exchange, the temperature of the crude synthesis gas is reduced from 1300-1600 ℃ to 700-900 ℃, ash slag is completely converted into solid from molten state, and each thousand square of effective gas (CO + H)2) The byproduct of saturated steam with pressure of 4-12 MPa is 0.5-1.0 t. The steam can enter a steam pipe network with a corresponding grade after being superheated by a heat device to be used as power steam.
The chilling chamber is located below the diversion exhaust funnel 9, a chilling chamber water bath 11 is arranged at the lower part of the chilling chamber, a plurality of chilling spray nozzles 10 are arranged at the top of the chilling chamber, the chilling spray nozzles 10 are annularly arranged, a chilling water inlet N8 is arranged at the top of the chilling chamber on the shell 8 and corresponds to the chilling chamber, and the chilling water inlet N8 is communicated with the chilling spray nozzles 10.
A large amount of quench water is sprayed into the interior of the furnace at the top of the quench chamber through said quench nozzles 10. Compared with the gasification furnace in the embodiment 1, the gasification furnace in the embodiment does not have a gas-liquid separation space, small water drops after impact, the crude synthesis gas and ash slag are fully mixed and enter the chilling chamber water bath 11, and the mixture is discharged out of the gasification furnace through a synthesis gas and black water mixed discharge port N9' at the middle lower part of the chilling chamber water bath 11. And then a separation tank is independently arranged outside the gasification furnace, the crude synthesis gas at the top of the separation tank enters a washing device, and black water and ash at the bottom of the separation tank are sent to a flash evaporation system for recovery. Compared with the gasification furnace in the embodiment 1, the gasification furnace in the embodiment can effectively reduce the overall height.
The high-temperature crude synthesis gas and the ash slag sequentially pass through the gasification reaction chamber 2, the lower slag hole 4 with rotational flow and the radiation heat exchange chamber 7 and enter the chilling chamber water bath 11, and the high-temperature crude synthesis gas and the ash slag have certain rotational flow effect when passing through each chamber or channel, and the rotational flow directions are kept consistent. Through accounting, for the gasification device with the same gas production rate, the consumption of the chilling water in the semi-waste boiler process is about 30-70% of that in the chilling process, and the energy-saving effect is obvious.
The above description is only for the specific embodiments of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art can easily conceive of the changes or substitutions within the technical scope of the present invention, and all the changes or substitutions should be covered within the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the appended claims.

Claims (10)

1. The gasification furnace with the radiant heat exchange function is characterized by comprising a shell (8) and a furnace body arranged in the shell (8), wherein the furnace body comprises a gasification chamber, a radiant heat exchange chamber (7) and a chilling chamber which are coaxially arranged from top to bottom in sequence;
the gasification chamber comprises a burner connecting port positioned at the top, a slag discharging port (4) with rotational flow positioned at the bottom and a gasification reaction chamber (2) positioned between the top and the bottom, and the gasification reaction chamber (2) is provided with a water-cooled wall (3);
the wall surface of the radiation heat exchange chamber (7) is a membrane water-cooling wall (6), the upper part of the inner side of the membrane water-cooling wall (6) is provided with an injection device, and the injection device comprises a plurality of annular cooling spray heads (5) which are arranged in a layered manner; the inner wall surface of the membrane water-cooling wall (6) is provided with a plurality of heat exchange screens (12); a flow guide exhaust cylinder (9) is arranged at the lower part of the radiation heat exchange chamber (7), and the flow guide exhaust cylinder (9) is of an inverted cone structure;
the chilling chamber is positioned below the diversion exhaust funnel (9), and a chilling spray nozzle (10) is arranged at the top of the chilling chamber.
2. The gasification furnace with the radiant heat exchange function according to claim 1, wherein the inner diameter of the slag tapping hole is smaller than that of the gasification reaction chamber (2), and the ratio of the inner diameter of the slag tapping hole to that of the gasification reaction chamber (2) is 1: 3-1: 8.
3. The gasification furnace with the radiant heat exchange function according to claim 1, wherein the inner diameter of the slag discharging port is smaller than that of the radiant heat exchange chamber (7), and the ratio of the inner diameter of the slag discharging port to that of the radiant heat exchange chamber (7) is 1: 3-1: 8.
4. The gasification furnace with radiant heat exchange according to claim 1, characterized in that a guide groove with the same rotational direction as the airflow is arranged in the lower slag hole (4).
5. The gasification furnace with radiant heat exchange according to claim 1, wherein an included angle α between a contraction inclined surface of the flow guide exhaust cylinder (9) and a horizontal direction is 60-75 °.
6. The gasification furnace with radiant heat exchange according to claim 1, characterized in that the projection of the membrane water wall (6) in the horizontal direction is circular or polygonal.
7. The gasifier with radiant heat exchange according to claim 6, characterized in that when the projection of the membrane water wall (6) on the horizontal plane is circular, the heat exchange screen (12) has a deflection angle β with respect to the radial direction of the membrane water wall (6);
when the projection of the membrane water-cooling wall (6) on the horizontal plane is a polygon, the heat exchange screen (12) has a deflection angle beta relative to the perpendicular line of the membrane water-cooling wall (6).
8. The gasification furnace with radiant heat exchange according to claim 7, wherein the deflection angle β is in a range of 0 to 45 °.
9. A gasifier with radiative heat exchange according to claim 1, characterized in that the quench nozzle (10) is arranged annularly to the inner wall of the quench chamber.
10. A gasification method based on the gasification furnace according to any one of claims 1 to 9, comprising the steps of:
(a) raw material coal and pure oxygen are injected into a gasification reaction chamber (2) through a gasification burner (1) for coal gasification reaction, and high-temperature crude synthesis gas and molten-state ash slag after reaction swirl and flow downwards into a slag discharging port (4) with swirl;
(b) under the action of the rotational flow structure of the slag discharging port (4) with rotational flow, the high-temperature crude synthesis gas and the molten state ash slag entering the radiation heat exchange chamber (7) still keep rotational flow shape;
(c) in the radiation heat exchange chamber (7), high-level heat energy of high-temperature crude synthesis gas and molten ash slag is absorbed by the film-type water-cooled wall (6) and the heat exchange screen (12), the temperature of the crude synthesis gas is reduced, and the ash slag is converted into a solid state from a molten state;
(d) the crude synthesis gas and solid ash slag after high-level heat energy recovery through the radiation heat exchange chamber (7) enter a chilling chamber water bath (11), the crude synthesis gas is rapidly humidified and cooled, and gas-solid separation is realized between the crude synthesis gas and the solid ash slag; the crude synthesis gas is washed and then sent out, and solid ash is discharged from the bottom of the gasification furnace.
CN201810734782.XA 2018-07-06 2018-07-06 Gasification furnace with radiation heat exchange and gasification method Pending CN110684562A (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
CN201810734782.XA CN110684562A (en) 2018-07-06 2018-07-06 Gasification furnace with radiation heat exchange and gasification method
PCT/CN2018/122284 WO2020006994A1 (en) 2018-07-06 2018-12-20 Gasifier employing radiant heat exchange technique and gasification method

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201810734782.XA CN110684562A (en) 2018-07-06 2018-07-06 Gasification furnace with radiation heat exchange and gasification method

Publications (1)

Publication Number Publication Date
CN110684562A true CN110684562A (en) 2020-01-14

Family

ID=69060018

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201810734782.XA Pending CN110684562A (en) 2018-07-06 2018-07-06 Gasification furnace with radiation heat exchange and gasification method

Country Status (2)

Country Link
CN (1) CN110684562A (en)
WO (1) WO2020006994A1 (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113930261A (en) * 2021-11-04 2022-01-14 宁夏神耀科技有限责任公司 Gasification furnace equipment and method for producing carbon monoxide
CN114525154A (en) * 2022-02-11 2022-05-24 安徽科达洁能股份有限公司 Glass body melting gasification furnace, gasification system and gasification method

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113072980B (en) * 2021-04-28 2021-12-07 宁夏神耀科技有限责任公司 Downward full waste boiler entrained flow bed gasification equipment of superheated steam and coal chemical system

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH11257094A (en) * 1998-03-16 1999-09-21 Electric Power Dev Co Ltd Coal gasification power generation system
CN201376954Y (en) * 2008-12-29 2010-01-06 北京航天万源煤化工工程技术有限公司 Solid fuel gasification unit
CN202092088U (en) * 2010-12-24 2011-12-28 上海锅炉厂有限公司 Novel radiation type waste heat boiler
CN202730088U (en) * 2012-09-06 2013-02-13 神华集团有限责任公司 Entrained-flow bed solid slag discharge gasification device
CN203128511U (en) * 2012-12-11 2013-08-14 中国东方电气集团有限公司 Integrated beam-like radiation preheating mixed type energy utilization device with smoke gas chilling
CN204434565U (en) * 2015-02-04 2015-07-01 中国五环工程有限公司 With the vapourizing furnace of radiation waste pot
CN208586256U (en) * 2018-07-06 2019-03-08 北京迈未科技有限公司 A kind of gasification furnace with radiation heat transfer

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113930261A (en) * 2021-11-04 2022-01-14 宁夏神耀科技有限责任公司 Gasification furnace equipment and method for producing carbon monoxide
CN113930261B (en) * 2021-11-04 2022-08-26 宁夏神耀科技有限责任公司 Gasification furnace equipment and method for producing carbon monoxide
CN114525154A (en) * 2022-02-11 2022-05-24 安徽科达洁能股份有限公司 Glass body melting gasification furnace, gasification system and gasification method
CN114525154B (en) * 2022-02-11 2024-03-29 安徽科达洁能股份有限公司 Glass body melting gasification furnace, gasification system and gasification method

Also Published As

Publication number Publication date
WO2020006994A1 (en) 2020-01-09

Similar Documents

Publication Publication Date Title
CN108410510B (en) Integrated coal gasifier for ash removal of waste boiler
CN100577775C (en) Coal gasification device for circulating fluidized bed and manufacturing method thereof
CN108342227B (en) Synthetic gas sensible heat recovery device and recovery method and gasifier
CN102492486B (en) Double-sided water-wall cylinder-type synthetic gas cooler
CN110684562A (en) Gasification furnace with radiation heat exchange and gasification method
CN102786992B (en) Radiation heat-convection integrated synthesis gas cooler
CN102213409A (en) Double-barrel water cooled wall type radiation waste boiler with adjusting function and industrial application thereof
CN106221814B (en) A kind of colm water cooling fireplace segmented couples gasification installation and gasification process
CN103874748B (en) Non-melt and partial melting type airflow bed gasification furnace
Wang et al. Development and demonstration plant operation of an opposed multi-burner coal-water slurry gasification technology
CN111763535A (en) Method and device for preparing fuel gas or synthesis gas by biomass fluidized bed gasification
CN101665724A (en) Water-coal-slurry gasification method and gasification furnace
CN207031371U (en) Synthesis gas soaks washing system
CN105779014B (en) J-type airflow bed gasification furnace
CN208762459U (en) A kind of fluid bed powder coal gasification device of flying dust zero-emission
CN208586256U (en) A kind of gasification furnace with radiation heat transfer
CN107760385B (en) Coal gasification device combining fluidized bed and molten bed and method thereof
CN202936392U (en) Radiation and convection heat exchange integrated synthesis gas cooler
CN108753367A (en) A kind of the fluid bed powder coal gasification device and technique of flying dust zero-emission
CN204455022U (en) Slag circulation of vital energy in the wrong direction flowing water Quench vapourizing furnace
CN102952588B (en) High-temperature synthetic gas chilling method for gasification furnace
CN103937552B (en) A kind of three-section type entrained flow bed coal hydrogenation gasification stove and combined operation system
CN208279578U (en) A kind of synthesis gas heat recovering device and gasification furnace
CN210176800U (en) Gasification furnace for pulverized coal gasification coupling double-tube-screen radiation waste boiler
CN104498105B (en) Chilling type single waste pan reactor

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination