CN111621335A - Coal catalytic gasification system - Google Patents
Coal catalytic gasification system Download PDFInfo
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- CN111621335A CN111621335A CN202010490316.9A CN202010490316A CN111621335A CN 111621335 A CN111621335 A CN 111621335A CN 202010490316 A CN202010490316 A CN 202010490316A CN 111621335 A CN111621335 A CN 111621335A
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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
- C10J3/48—Apparatus; Plants
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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
- C10J3/58—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
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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
- C10J3/58—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
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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
- C10J3/72—Other features
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
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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
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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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
- C10J3/72—Other features
- C10J3/86—Other features combined with waste-heat boilers
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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
- 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
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
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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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
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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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0983—Additives
- C10J2300/0986—Catalysts
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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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
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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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
- C10J2300/1628—Ash post-treatment
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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Abstract
The disclosure relates to the technical field of coal gasification, and provides a coal catalytic gasification system. The system comprises a first gasification furnace, a second gasification furnace and a coal gas purification and separation unit; the lower end of the first gasification furnace is communicated with the upper end of the second gasification furnace; the first gasification furnace is provided with a first feed inlet for feeding coal, a first air inlet for introducing synthetic gas and steam and an air outlet connected with the coal gas purification and separation unit, the second gasification furnace is provided with a second feed inlet, a second air inlet for introducing steam and oxygen and a slag discharge port for discharging ash slag, and the middle part of the first gasification furnace is provided with a discharge port connected with the second feed inlet; the reaction temperature of the second gasification furnace is higher than that of the first gasification furnace, so that the first gasification furnace is more favorable for carrying out water gas shift reaction and methanation reaction, and the second gasification furnace is more favorable for carrying out coal gasification reaction, so that each reaction reaches the optimal reaction condition, each reaction effect is favorably improved, and high methane generation rate and high carbon conversion rate are realized.
Description
Technical Field
The disclosure relates to the technical field of coal gasification, in particular to a coal catalytic gasification system.
Background
In the technical field of coal gasification, the coal catalytic gasification technology is an advanced third-generation coal gasification technology taking methane as a target product, and the technical principle of the technology is that under the action of a multifunctional catalyst, coal and gasification media (steam and oxygen) simultaneously generate three reactions of coal gasification reaction, water gas shift reaction and methanation reaction in one reactor, so that endothermic reaction and exothermic reaction are effectively coupled, and the methane yield and the system energy efficiency are greatly improved.
However, the reactor adopted by the technology is a pressurized fluidized bed gasification furnace, although coal gasification reaction, water gas shift reaction and methanation reaction occur simultaneously in one gasification furnace to realize heat coupling, the optimal conditions of the three reactions are greatly different, and the following problems can be caused:
the reaction conditions are different, the reaction time is controlled by the reaction with the slowest rate when three reactions are carried out in the same reactor, the coal gasification reaction is endothermic and needs to be carried out at a higher temperature, the water gas shift reaction and the methanation reaction are exothermic and need to be carried out at a lower temperature, and the reaction rates are greatly different under the same temperature, pressure and atmosphere, so that the whole reaction time is limited by the reaction with the slowest rate, high methane generation rate and high carbon conversion rate cannot be simultaneously realized within the time allowed by an industrial device, and the large-scale device is not facilitated. In addition, in the prior art, the coal is catalyzed and gasified to be aerobic gasification, mixed gas of water vapor and oxygen is introduced to the bottom of the gasification furnace to serve as a gasification agent, the synthesis gas generated by the reaction can be directly contacted with the oxygen in the gasification furnace, and the oxygen and the synthesis gas are combusted to cause the loss of the synthesis gas and the slagging of materials in the furnace.
Disclosure of Invention
To solve the above technical problem or at least partially solve the above technical problem, the present disclosure provides a coal catalytic gasification system that achieves a high methane generation rate and a high carbon conversion rate.
The present disclosure provides a coal catalytic gasification system, comprising a first gasification furnace, a second gasification furnace and a coal gas purification and separation unit; the lower end of the first gasification furnace is communicated with the upper end of the second gasification furnace;
the first gasification furnace is provided with a first feed inlet for feeding coal, a first air inlet for introducing synthetic gas and steam and an air outlet connected with the coal gas purification and separation unit, the second gasification furnace is provided with a second feed inlet, a second air inlet for introducing steam and oxygen and a slag discharge port for discharging ash slag, and the middle part of the first gasification furnace is provided with a discharge port connected with the second feed inlet.
Optionally, the gas purification and separation unit comprises a cryogenic separation unit, and the cryogenic separation unit is used for separating each component gas in the raw gas.
Optionally, the system further comprises a gas mixer, steam is introduced into an inlet of the gas mixer, the inlet of the gas mixer is connected with an outlet of the cryogenic separation unit, and an outlet of the gas mixer is connected with the first gas inlet.
Optionally, a heat exchanger is arranged between the first gasification furnace and the cryogenic separation unit, the heat exchanger comprises a first heat exchange cavity and a second heat exchange cavity, an inlet and an outlet of the first heat exchange cavity are correspondingly connected with the gas outlet and an inlet of the cryogenic separation unit, and an inlet and an outlet of the second heat exchange cavity are correspondingly connected with an outlet and a first gas inlet of the cryogenic separation unit.
Optionally, a waste heat boiler is arranged between the heat exchanger and the cryogenic separation unit, the waste heat boiler is provided with a third heat exchange cavity and a fourth heat exchange cavity, an inlet and an outlet of the third heat exchange cavity are correspondingly connected with an outlet of the first heat exchange cavity and an inlet of the cryogenic separation unit, and an inlet and an outlet of the fourth heat exchange cavity are correspondingly connected with a water inlet and a steam outlet.
Optionally, the gasification furnace further comprises a cyclone dust removal device, an inlet of the cyclone dust removal device is connected with the gas outlet, a gas outlet of the cyclone dust removal device is connected with the gas purification and separation unit, and a dust outlet of the cyclone dust removal device is connected with the second gasification furnace.
Optionally, the material discharging unit is further included, the material discharging unit comprises a first material discharging tank and a second material discharging tank, the discharging port is connected with the first material discharging tank, the second material discharging tank is connected with the second feeding port, a first switch valve is arranged between the first material discharging tank and the second material discharging tank, and a second switch valve is arranged between the second material discharging tank and the second feeding port.
Optionally, the ash slag processing unit comprises a first buffer tank and a second buffer tank, the first buffer tank is connected with the slag discharge port, a third switch valve is arranged between the first buffer tank and the second buffer tank, and the second buffer tank is provided with a fourth switch valve for discharging slag.
Optionally, the coal conveying unit is further included and is connected with the first feeding hole.
Compared with the prior art, the technical scheme provided by the embodiment of the disclosure has the following advantages: the first gasification furnace is an anaerobic reaction gasification furnace, the second gasification furnace is an aerobic reaction gasification furnace, the fluidizing gas of the first gasification furnace is synthetic gas and steam, and the fluidizing gas of the second gasification furnace is steam and oxygen; the second gasification furnace can generate an aerobic combustion reaction relative to the first gasification furnace, so that the reaction temperature of the second gasification furnace is higher than that of the first gasification furnace, and the first gasification furnace is more favorable for performing water gas shift reaction and methanation reaction on the basis of the reaction temperature, and the second gasification furnace is more favorable for performing coal gasification reaction, so that each reaction reaches the optimal reaction condition, each reaction effect is favorably improved, and high methane generation rate and high carbon conversion rate are realized; meanwhile, the first gasification furnace is oxygen-free, so that the loss of the synthesis gas caused by the combustion of oxygen and the synthesis gas is avoided; and the synthesis gas generated by the reaction of the second gasification furnace is directly introduced into the first gasification furnace from bottom to top, so that the methanation reaction of the first gasification furnace is further generated while the reaction temperature is provided for the first gasification furnace, and the high-efficiency utilization of energy sources and the methane yield are improved.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the present disclosure and together with the description, serve to explain the principles of the disclosure.
In order to more clearly illustrate the embodiments or technical solutions in the prior art of the present disclosure, the drawings used in the description of the embodiments or prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without inventive exercise.
FIG. 1 is a schematic diagram of a system according to an embodiment of the disclosure;
FIG. 2 is a schematic view of a discharge unit;
fig. 3 is a schematic view of an ash handling unit.
Wherein, 1, a first gasification furnace; 11. a first feed port; 12. a first air inlet; 13. an air outlet; 14. a discharge outlet; 2. a second gasification furnace; 21. a second feed port; 22. a second air inlet; 23. a slag discharge port; 3. a cryogenic separation unit; 4. a gas mixer; 5. a heat exchanger; 6. a waste heat boiler; 7. a cyclone dust removal device; 8. a discharge unit; 81. a first discharging tank; 82. a second discharge tank; 83. a first on-off valve; 84. a second on-off valve; 9. an ash treatment unit; 91. a first cache tank; 92. a second cache tank; 93. a third on-off valve; 94. a fourth switching valve; 10. a coal conveying unit.
Detailed Description
In order that the above objects, features and advantages of the present disclosure may be more clearly understood, aspects of the present disclosure will be further described below. It should be noted that the embodiments and features of the embodiments of the present disclosure may be combined with each other without conflict.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present disclosure, but the present disclosure may be practiced in other ways than those described herein; it is to be understood that the embodiments disclosed in the specification are only a few embodiments of the present disclosure, and not all embodiments.
As shown in fig. 1, a coal catalytic gasification system includes a first gasification furnace 1, a second gasification furnace 2 and a coal gas purification and separation unit; the lower end of the first gasification furnace 1 is communicated with the upper end of the second gasification furnace 2; the first gasification furnace 1 is provided with a first feed inlet 11 for feeding coal, a first gas inlet 12 for introducing synthetic gas and steam, and a gas outlet 13 connected with the coal gas purification and separation unit, the second gasification furnace 2 is provided with a second feed inlet 21, a second gas inlet 22 for introducing steam and oxygen, and a slag discharge port 23 for discharging ash, and the middle part of the first gasification furnace 1 is provided with a discharge port 14 connected with the second feed inlet 21.
Compared with the prior art, the first gasification furnace 1 is an anaerobic reaction gasification furnace, the second gasification furnace 2 is an aerobic reaction gasification furnace, the fluidized gas of the first gasification furnace 1 is synthetic gas and steam, and the fluidized gas of the second gasification furnace 1 is steam and oxygen; the second gasification furnace 2 can generate an aerobic combustion reaction relative to the first gasification furnace 1, so that the reaction temperature of the second gasification furnace 2 is higher than that of the first gasification furnace 1, and the first gasification furnace 1 is more favorable for performing water gas shift reaction and methanation reaction, and the second gasification furnace 2 is more favorable for performing coal gasification reaction, so that each reaction reaches the optimal reaction condition, each reaction effect is favorably improved, and high methane generation rate and high carbon conversion rate are realized; meanwhile, the first gasification furnace 1 is free of oxygen, so that the loss of the synthesis gas caused by the combustion of oxygen and the synthesis gas is avoided; and the synthesis gas generated by the reaction of the second gasification furnace 2 is directly introduced into the first gasification furnace 1 from bottom to top, so that the first gasification furnace 1 further generates methanation reaction while providing reaction temperature for the first gasification furnace 1, thereby realizing the high-efficiency utilization of energy and improving the yield of methane.
Coal gasification reaction: c + H2O→CO+H2
Water gas shift reaction: CO + H2O→CO2+H2
Methanation reaction: CO + H2→CH4+H2O。
In some embodiments, as shown in fig. 1, the gas purification separation unit comprises a cryogenic separation unit 3, and the cryogenic separation unit 3 is used for separating each component gas in the raw gas. The coal gas purification and separation unit can adopt a low-temperature methanol washing process to separate tar in the crude coal gas, and then adopts the cryogenic separation unit 3, the principle of the cryogenic separation unit 3 is a low-temperature rectification method which is a separation device commonly used in the prior art, and the cryogenic separation unit 3 is adopted to separate methane in the crude coal gas.
In some embodiments, as shown in FIG. 1, a gas mixer 4 is further included, an inlet of gas mixer 4 is fed with steam, and an inlet of gas mixer 4 is connected to an outlet of cryogenic separation unit 3, and an outlet of gas mixer 4 is connected to first gas inlet 12. The gas mixer 4 can also be equipped with a booster pump, the deep cooling separation unit 3 separates methane in the raw gas to obtain synthesis gas, the gas mixer 4 mixes steam and the synthesis gas discharged from the deep cooling separation unit 3 to obtain mixed gas, the mixed gas is used as a gasifying agent and a fluidizing agent to enter the bottom of the first gasification furnace 1 through the first gas inlet 12 through the booster pump, the mixed gas and semicoke at the bottom are subjected to gasification reaction, the synthesis gas discharged from the deep cooling separation unit 3 is subjected to cyclic reaction, hydrogen and carbon monoxide in the synthesis gas are fully utilized to convert the synthesis gas into methane, and the methane generation rate is improved.
In some embodiments, as shown in fig. 1, a heat exchanger 5 is disposed between the first gasification furnace 1 and the cryogenic separation unit 3, the heat exchanger 5 includes a first heat exchange chamber and a second heat exchange chamber, an inlet and an outlet of the first heat exchange chamber are correspondingly connected to the gas outlet 13 and the inlet of the cryogenic separation unit 3, and an inlet and an outlet of the second heat exchange chamber are correspondingly connected to the outlet of the cryogenic separation unit 3 and the first gas inlet 12. The cryogenic separation unit 3 is in a low-temperature state with the synthesis gas obtained after the methane in the crude gas is separated, the synthesis gas is required to be heated at the moment, the influence on the reaction temperature when the low-temperature synthesis gas enters the first gasification furnace 1 is avoided, the crude gas discharged from the gas outlet 13 is cooled by the heat exchanger 5, so that the crude gas can be separated more efficiently when entering the cryogenic separation unit 3, meanwhile, the synthesis gas discharged from the cryogenic separation unit 3 is heated by waste heat, and the stability of the reaction temperature of the first gasification furnace 1 is ensured.
In some embodiments, as shown in fig. 1, a waste heat boiler 6 is disposed between the heat exchanger 5 and the cryogenic separation unit 3, the waste heat boiler 6 is provided with a third heat exchange cavity and a fourth heat exchange cavity, an inlet and an outlet of the third heat exchange cavity are correspondingly connected with an outlet of the first heat exchange cavity and an inlet of the cryogenic separation unit 3, and an inlet and an outlet of the fourth heat exchange cavity are correspondingly a water inlet and a steam outlet. The crude gas cooled by heat exchange of the heat exchanger 5 still has higher temperature, the crude gas is further cooled by the waste heat boiler 6, meanwhile, steam is obtained by utilizing waste heat, and the steam can be used as a gasifying agent and is introduced into the first gasifying furnace 1 and the second gasifying furnace 2.
In some embodiments, as shown in fig. 1, the gasifier further comprises a cyclone dust collector 7, an inlet of the cyclone dust collector 7 is connected with the gas outlet 13, a gas outlet of the cyclone dust collector 7 is connected with the gas purification and separation unit, and a dust outlet of the cyclone dust collector 7 is connected with the second gasifier 2. The raw gas discharged from the gas outlet 13 has a certain amount of dust, and the dust is separated by the cyclone dust collector 7 and discharged into the second gasification furnace 2, so that the dust is reacted thoroughly, and the carbon conversion rate is improved.
In some embodiments, as shown in fig. 1 and fig. 2, the discharging unit 8 is further included, the discharging unit 8 includes a first discharging tank 81 and a second discharging tank 82, the discharging port 14 is connected to the first discharging tank 81, the second discharging tank 82 is connected to the second feeding port 21, a first switch valve 83 is disposed between the first discharging tank 81 and the second discharging tank 82, and a second switch valve 84 is disposed between the second discharging tank 82 and the second feeding port 21. During the reaction, the temperature and the air pressure of the second gasification furnace 2 are both higher than those of the first gasification furnace 1, so the discharge unit 8 is arranged to facilitate the discharge from the discharge port 14 to the second feed port 21, the first switch valve 83 and the second switch valve 84 are firstly closed, the semicoke is discharged to the first discharge tank 81 through the discharge port 14, when the set amount is reached, the first switch valve 83 is opened, the semicoke is discharged to the second discharge tank 82 through the first discharge tank 81, at this time, the first switch valve 83 is closed, the second discharge tank 82 is pressurized, the second switch valve 84 is opened again, and the semicoke is discharged to the second gasification furnace 2 through the second feed port 21.
In some embodiments, as shown in fig. 1 and 3, the ash processing unit 9 is further included, the ash processing unit 9 includes a first buffer tank 91 and a second buffer tank 92, the first buffer tank 91 is connected to the slag discharge port 23, a third on-off valve 93 is disposed between the first buffer tank 91 and the second buffer tank 92, and the second buffer tank 92 is provided with a fourth on-off valve 94 for discharging slag. Ash discharged from the slag discharge port 23 is high-temperature ash, cooling water can be introduced through the first buffer tank 91 and the second buffer tank 92 to cool the high-temperature ash, the first buffer tank 91 and the second buffer tank 92 are both provided with pressure relief exhaust ports, the third on-off valve 93 and the fourth on-off valve 94 are firstly closed, the ash is discharged to the first buffer tank 91 through the slag discharge port 23, when the set amount is reached, the third on-off valve 93 is opened, semicoke is discharged to the second buffer tank 92 through the first buffer tank 91, the third on-off valve 93 is closed at the moment, pressure relief is performed on the second buffer tank 92, the fourth on-off valve 94 is opened again, and the ash is discharged to a subsequent processing unit to perform catalyst recovery or other processing.
In some embodiments, as shown in fig. 1, a coal conveying unit 10 is further included, and the coal conveying unit 10 is connected to the first feeding port 11 to supply pulverized coal to the first gasification furnace 1.
As shown in fig. 1, the working process of one embodiment of the present invention is as follows:
the coal conveying unit 10 conveys coal powder to a first gasification furnace 1 through a first feed port 11, steam and synthesis gas are introduced into the bottom of the first gasification furnace 1 through a first gas inlet 12, wherein the reaction temperature of the middle part of the first gasification furnace 1 is 550-650 ℃, the reaction temperature of the lower part of the first gasification furnace 1 is 650-750 ℃, the coal powder falls from the upper part to the middle part to generate pyrolysis reaction to generate tar and methane, the coal powder continuously falls from the middle part to the lower part to generate gasification reaction with the synthesis gas and the steam, wherein the gasification reaction mainly comprises water gas shift reaction and methanation reaction, and semicoke generated by the reaction is gathered at the lower part of the first gasification furnace 1;
under the action of the airflow of the synthesis gas and the steam introduced from the bottom, the semicoke overflows from a discharge port 14 in the middle, and then enters a second gasification furnace 2 through a second feed port 21, the steam and the oxygen are introduced from the bottom of the second gasification furnace 2 through a second air inlet 22, the reaction temperature of the second gasification furnace 2 is 750-850 ℃, the semicoke and the steam and the oxygen generate gasification reaction and combustion reaction, wherein the gasification reaction mainly comprises the coal gasification reaction, the ash generated after the reaction is discharged to an ash treatment unit 9 from a slag discharge port 22 at the bottom, the air pressure of the second gasification furnace 2 is higher than that of the first gasification furnace 1, the synthesis gas generated after the reaction is directly introduced into the bottom of the first gasification furnace 1 from bottom to top to provide the reaction temperature for the first gasification furnace 1, the synthesis gas from the second gasification furnace 2, the steam introduced through a first air inlet 12 and the synthesis gas jointly serve as a gasification agent and a fluidizing medium for the semicoke at the lower part, ensuring that the gasification furnace 1 fully performs methanation reaction and improving the methane generation rate;
the method comprises the following steps that crude gas generated by a first gasification furnace 1 is dedusted by a cyclone dedusting device 7 and then discharged to a heat exchanger 5, the heat exchanger 5 cools the crude gas and heats synthetic gas discharged by a cryogenic separation unit 3, the heated synthetic gas is discharged to a gas mixer 4 and then enters the first gasification furnace 1, the cooled crude gas is subjected to heat exchange by a waste heat boiler 5 to realize heat recovery, tar is separated by a low-temperature methanol washing process and then discharged to the cryogenic separation unit 3, and the cryogenic separation unit 3 separates methane in the crude gas to obtain residual synthetic gas.
It is noted that, in this document, relational terms such as "first" and "second," and the like, may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.
The foregoing are merely exemplary embodiments of the present disclosure, which enable those skilled in the art to understand or practice the present disclosure. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the disclosure. Thus, the present disclosure is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (9)
1. A coal catalytic gasification system is characterized by comprising a first gasification furnace (1), a second gasification furnace (2) and a coal gas purification and separation unit; the lower end of the first gasification furnace (1) is communicated with the upper end of the second gasification furnace (2);
first gasifier (1) be provided with be used for advancing first feed inlet (11) of coal, be used for letting in first air inlet (12) of synthetic gas and steam and with gas outlet (13) that the coal gas purification separation unit is connected, second gasifier (2) are provided with second feed inlet (21), are used for letting in second air inlet (22) of steam and oxygen and are used for row's cinder notch (23) of discharge lime-ash, the middle part of first gasifier (1) be provided with bin outlet (14) that second feed inlet (21) are connected.
2. The catalytic coal gasification system of claim 1, wherein the gas purification and separation unit comprises a cryogenic separation unit (3), and the cryogenic separation unit (3) is used for separating each component gas in the raw gas.
3. A catalytic coal gasification system according to claim 2, further comprising a gas mixer (4), wherein the inlet of the gas mixer (4) is fed with steam, and the inlet of the gas mixer (4) is connected with the outlet of the cryogenic separation unit (3), and the outlet of the gas mixer (4) is connected with the first gas inlet (12).
4. The coal catalytic gasification system according to claim 3, wherein a heat exchanger (5) is arranged between the first gasification furnace (1) and the cryogenic separation unit (3), the heat exchanger (5) comprises a first heat exchange cavity and a second heat exchange cavity, the inlet and the outlet of the first heat exchange cavity correspond to the gas outlet (13) and the inlet connection of the cryogenic separation unit (3), and the inlet and the outlet of the second heat exchange cavity correspond to the outlet of the cryogenic separation unit (3) and the first gas inlet (12) connection.
5. A catalytic coal gasification system according to claim 4, wherein a waste heat boiler (6) is arranged between the heat exchanger (5) and the cryogenic separation unit (3), the waste heat boiler (6) is provided with a third heat exchange chamber and a fourth heat exchange chamber, the inlet and outlet of the third heat exchange chamber correspond to the outlet of the first heat exchange chamber and the inlet connection of the cryogenic separation unit (3), and the inlet and outlet of the fourth heat exchange chamber correspond to a water inlet and a steam outlet.
6. The coal catalytic gasification system of claim 1, further comprising a cyclone dust collector (7), wherein an inlet of the cyclone dust collector (7) is connected with the gas outlet (13), a gas outlet of the cyclone dust collector (7) is connected with the gas purification and separation unit, and a dust outlet of the cyclone dust collector (7) is connected with the second gasification furnace (2).
7. A coal catalytic gasification system according to claim 1, further comprising a discharge unit (8), wherein the discharge unit (8) comprises a first discharge tank (81) and a second discharge tank (82), the discharge port (14) is connected with the first discharge tank (81), the second discharge tank (82) is connected with the second feed port (21), a first switch valve (83) is arranged between the first discharge tank (81) and the second discharge tank (82), and a second switch valve (84) is arranged between the second discharge tank (82) and the second feed port (21).
8. The coal catalytic gasification system according to claim 1, further comprising an ash handling unit (9), wherein the ash handling unit (9) comprises a first buffer tank (91) and a second buffer tank (92), the first buffer tank (91) is connected with the slag discharge port (23), a third on/off valve (93) is arranged between the first buffer tank (91) and the second buffer tank (92), and the second buffer tank (92) is provided with a fourth on/off valve (94) for discharging slag.
9. A catalytic coal gasification system according to claim 1 further comprising a coal conveying unit (10), the coal conveying unit (10) being connected to the first feed opening (11).
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| CN202010490316.9A CN111621335A (en) | 2020-06-02 | 2020-06-02 | Coal catalytic gasification system |
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Application publication date: 20200904 |