CN112920853A - Coal catalytic gasification reaction furnace and coal catalytic gasification reaction system - Google Patents
Coal catalytic gasification reaction furnace and coal catalytic gasification reaction system Download PDFInfo
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- CN112920853A CN112920853A CN202110156643.5A CN202110156643A CN112920853A CN 112920853 A CN112920853 A CN 112920853A CN 202110156643 A CN202110156643 A CN 202110156643A CN 112920853 A CN112920853 A CN 112920853A
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- gasification reaction
- oxidant
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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
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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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- 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
Abstract
A coal catalytic gasification reacting furnace and a coal catalytic gasification reacting system are provided, the coal catalytic gasification reacting furnace includes: a gasification reaction zone and a high-temperature melting zone are formed in the columnar shell, and the gasification reaction zone is positioned above the high-temperature melting zone; when a gasifying agent conveying device arranged at the bottom of the gasification reaction zone conveys the high-temperature gasifying agent towards the top of the gasification reaction zone, a gasifying agent rotational flow flowing to the high-temperature melting zone is formed in the gasification reaction zone; when the oxidant conveying device arranged at the top of the high-temperature melting zone conveys the high-temperature oxidant towards the bottom of the high-temperature melting zone, oxidant rotational flow flowing to the gasification reaction zone is formed in the high-temperature melting zone. The control difficulty of the material transfer and energy exchange process is reduced through the gasifying agent conveying device and the oxidant conveying device, and the environmental protection and the operation stability of the whole catalytic gasification are improved.
Description
Technical Field
The invention relates to the technical field of catalytic gasification, in particular to a coal catalytic gasification reaction furnace and a coal catalytic gasification reaction system.
Background
The gasification process is a process for converting carbonaceous materials into synthesis gas for power generation and production of chemical raw materials, the coal catalytic gasification for methane production is one of the most effective gasification processes, and the catalyst can synchronously catalyze carbohydrate reaction, water gas shift reaction and carbon monoxide hydrogenation methanation reaction, thereby realizing absorption-discharge thermal coupling and greatly improving the energy efficiency of the system.
Among the catalysts, alkali metals potassium and sodium have the best catalytic performance, but the cost is high, and the catalyst in the gasified ash needs to be recycled after being used, but the structure of a gasification system is complicated, so the high cost of the catalyst becomes a key factor for restricting the industrialization of the coal catalytic gasification technology. Therefore, in order to reduce the catalyst cost and simplify the catalyst recovery process, it is necessary to develop a low-cost catalyst system without recovery.
In the scheme of the prior art, by selecting low-cost alkali metal, alkaline earth metal salt or mixture as a coal gasification catalyst or applying industrial waste alkaline residue or waste alkaline liquor to coal catalytic gasification reaction, not only can the coal gasification reaction be effectively catalyzed, but also the pollution problem of waste can be solved. Moreover, the catalyst used is low in cost, and a catalyst recovery working section can be omitted. However, the dissolution of the metal catalyst in the catalytic gasification ash causes environmental pollution, so that the ash cannot be directly discharged, and the ash must be subjected to harmless treatment to realize resource utilization or direct discharge of the ash.
In order to realize the coal catalytic gasification process and the ash treatment process in the prior art, a plurality of reactors are generally adopted to form the whole device, different reactors realize different functions, but the material conveying and energy exchange among different reactors are difficult to realize, and the operation of the whole device is easy to cause instability.
Disclosure of Invention
Objects of the invention
The invention aims to provide a coal catalytic gasification reaction furnace and a coal catalytic gasification reaction system, which adopt low-cost recovery-free catalysts to treat raw material coal, and simultaneously, gasification agent conveying devices and oxidant conveying devices arranged in a gasification reaction zone and a high-temperature melting zone in the system can reduce the control difficulty of material transfer and energy exchange processes and improve the environmental protection and operation stability of the whole catalytic gasification.
(II) technical scheme
To solve the above problems, according to one aspect of the present invention, there is provided a coal catalytic gasification reaction furnace comprising: a cylindrical housing; a gasification reaction zone and a high-temperature melting zone are formed in the columnar shell, and the gasification reaction zone is positioned above the high-temperature melting zone; when a gasifying agent conveying device arranged at the bottom of the gasification reaction zone conveys a high-temperature gasifying agent towards the top of the gasification reaction zone, a gasifying agent rotational flow flowing to the high-temperature melting zone is formed in the gasification reaction zone; and when the oxidant conveying device arranged at the top of the high-temperature melting zone conveys the high-temperature oxidant towards the bottom of the high-temperature melting zone, oxidant rotational flow flowing to the gasification reaction zone is formed in the high-temperature melting zone.
Further, the output port of the gasifying agent conveying device faces the top of the gasification reaction zone; the output port of the oxidant conveying device faces the bottom of the high-temperature melting zone.
Further, the gasifying agent conveying device and the oxidant conveying device are arranged on the inner wall of the cylindrical shell; the axial included angle between the output port of the gasification agent conveying device and the cylindrical shell is 45-90 degrees; the output port of the gasification agent conveying device forms an included angle of 60-90 degrees with the cross section perpendicular to the axial direction; the axial included angle between the output port of the oxidant conveying device and the cylindrical shell is 15-50 degrees; the included angle between the output port of the oxidant conveying device and the cross section perpendicular to the axial direction is 45-90 degrees.
Further, the gasifying agent conveying device comprises: a plurality of gas distributors, a plurality of jet pipes, or a plurality of nozzles; the oxidant delivery device includes: a plurality of gas distributors, a plurality of jet pipes, or a plurality of nozzles; each gas distributor is located on the same horizontal plane, each jet pipe is located on the same horizontal plane, or each nozzle is located on the same horizontal plane.
Further, the high-temperature gasifying agent comprises: h2O and/or O2(ii) a The high-temperature oxidizing agent comprises: oxygen or oxygen-enriched steam.
Further, a molten liquid level is formed at the bottom of the high-temperature melting zone; and the oxidant swirls to flow into the position below the molten liquid level by a certain depth and then enters the gasification reaction zone along the inner wall surface of the columnar shell.
According to another aspect of the present invention, the present invention provides a coal catalytic gasification reaction system, including the coal catalytic gasification reaction furnace set forth above, further including: the system comprises a coal preparation unit, a coal gas purification unit and a slag discharge unit; an output port of the coal preparation unit is communicated with a feed port of the coal catalytic gasification reaction furnace so as to convey the prepared coal sample in the coal preparation unit to the coal catalytic gasification reaction furnace; a slag discharging port of the coal catalytic gasification reaction furnace is communicated with the slag discharging unit so as to convey liquid molten slag generated in the coal catalytic gasification reaction furnace to the slag discharging unit for treatment; an exhaust port of the coal catalytic gasification reaction furnace is communicated with an input port of the coal gas purification unit so as to convey the crude coal gas into the coal gas purification unit; and an ash outlet of the coal gas purification unit is communicated with the coal catalytic gasification reaction furnace so as to convey the fly ash back to a high-temperature melting zone of the coal catalytic gasification reaction furnace for circular treatment.
Further, the coal preparation unit prepares a coal sample by a catalyst loading method; the catalyst comprises: alkali metal sulfate, calcium oxide, calcium hydroxide, industrial waste caustic sludge or industrial waste lye; the method for loading the catalyst comprises the following steps: dry blending, impregnation or ion exchange.
Further, the slag discharging unit comprises: a granulator and heat exchange structure; the granulator is used for granulating the liquid molten slag into a solid state; the heat exchange structure is used for cooling the solid molten slag and recovering waste heat.
Further, the coal gas purification unit comprises the following components which are connected in sequence: a cyclone, a filter and a return; the cyclone separator is used for separating fly ash carried in the crude gas; the filter is used for collecting fly ash; the return device is used for conveying the fly ash back to a high-temperature melting area of the coal catalytic gasification reaction furnace.
Further, the method also comprises the following steps: a gas separation unit; the input port of the gas separation unit is communicated with the output port of the gas purification unit and is used for performing membrane separation or cryogenic separation on the crude gas after fly ash separation to obtain CO or H2(ii) a A first output port of the gas separation unit is communicated with the coal catalytic gasification reaction furnace and is used for completely removing the CO or the H2Or part of said CO or H2Conveying the coal to the coal catalytic gasification reaction furnace; the second output port of the gas separation unit is used for outputting the CO or the H2。
(III) advantageous effects
The technical scheme of the invention has the following beneficial technical effects:
the coal catalytic gasification furnace is internally provided with the gasification reaction zone and the high-temperature melting zone, the gasification agent cyclone channel and the oxidant cyclone channel are respectively formed in the gasification reaction zone and the high-temperature melting zone by adjusting the installation angle of the gasification agent conveying device arranged in the gasification reaction zone and the installation angle of the oxidant conveying device arranged in the high-temperature melting zone, and are matched with each other to convey catalytic gasification ash slag generated in the gasification reaction zone to the high-temperature melting zone, so that the full reaction of all residual carbon is ensured, heat is provided for the gasification reaction, and meanwhile, the catalytic gasification ash slag is subjected to harmless treatment; and simultaneously, the reaction in the gasification reaction zone and the high-temperature melting zone is enhanced.
In the coal catalytic gasification system provided by the invention, the coal preparation unit adopts low-cost raw materials or industrial waste alkali liquor as a catalyst to carry out catalyst loading treatment on the raw material coal, so that a catalyst recovery working section is omitted. The difficulty in controlling the processes of material transfer and energy exchange is reduced, and the environmental protection and the operation stability of the integral catalytic gasification are improved.
Drawings
FIG. 1 is a schematic structural diagram of a coal catalytic gasification reaction furnace provided by the present invention;
FIG. 2 is a schematic diagram of the arrangement position of a gasification agent conveying device provided by the invention;
FIG. 3 is a schematic gas flow diagram of a gasification reaction zone provided by the present invention;
FIG. 4 is a schematic diagram of the arrangement position of the oxidant delivery device provided by the present invention;
FIG. 5 is a schematic view of the gas flow direction of the high temperature melting zone provided by the present invention;
FIG. 6 is a schematic structural diagram of a catalytic coal gasification system provided by the present invention.
Reference numerals:
1-a cylindrical shell; 2-a gasification reaction zone; 3-a high temperature melting zone; 4-a feed inlet; 5-a gasification agent conveying device; 6-an oxidant delivery device; 7-a slag discharge port;
a-a coal preparation unit; b, a coal catalytic gasification reaction furnace; c-a gas purification unit; d, a slag discharging unit; e-gas separation; p-negative pressure zone.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in further detail with reference to the accompanying drawings in conjunction with the following detailed description. It should be understood that the description is intended to be exemplary only, and is not intended to limit the scope of the present invention. Moreover, in the following description, descriptions of well-known structures and techniques are omitted so as to not unnecessarily obscure the concepts of the present invention.
The present invention will be described in detail below with reference to the accompanying drawings and examples.
Fig. 1 is a schematic structural diagram of a coal catalytic gasification reaction furnace provided by the present invention, please refer to fig. 1.
In one embodiment of the present invention, a catalytic coal gasification reactor includes: the gasification device comprises a cylindrical shell 1, wherein a gasification reaction zone 2 and a high-temperature melting zone 3 are formed in the cylindrical shell 1, and the gasification reaction zone 2 is positioned above the high-temperature melting zone 3.
The gasification reaction zone 2 is used for carrying out high-temperature gasification and pyrolysis on the coal sample conveyed into the reaction furnace to generate crude gas rich in methane and obtain catalytic gasification ash; the raw gas can be directly used as product gas after being treated, and catalytic gasification ash falls into a high-temperature melting zone 3 below a gasification reaction zone 2 for harmless treatment.
Specifically, a feed inlet 4 is arranged at the top edge of the cylindrical shell 1, and a coal sample enters the gasification reaction zone 2 from the feed inlet 4. The bottom of the columnar shell 1 is also provided with an inverted cone-shaped slag discharge opening 7 for discharging catalytic gasification ash slag after harmless treatment.
The inner wall of the cylindrical shell 1 is provided with a gasifying agent conveying device 5, and the gasifying agent conveying device 5 is positioned at the bottom of the gasification reaction zone 2 and used for conveying a high-temperature gasifying agent to the gasification reaction zone 2, so that the high-temperature gasifying agent and the coal sample are subjected to high-temperature gasification reaction and pyrolysis reaction in the gasification reaction zone 2. Meanwhile, an oxidant conveying device 6 is arranged on the inner wall of the columnar shell 1, and the oxidant conveying device 6 is positioned at one end of the high-temperature melting zone 3 close to the gasification reaction zone 2 and is used for conveying a high-temperature oxidant into the high-temperature melting zone 3.
When the gasifying agent conveying device 5 conveys the high-temperature gasifying agent towards the top of the gasification reaction zone 2, a gasifying agent rotational flow flowing to the high-temperature melting zone 3 is formed in the gasification reaction zone 2; when the high-temperature oxidizing agent is fed toward the bottom of the high-temperature melting zone 3 by the oxidizing agent feeding device 6, a swirling flow of the oxidizing agent flowing to the gasification reaction zone 2 is formed in the high-temperature melting zone 3.
The catalytic gasification ash generated in the gasification reaction zone 2 can be driven by the gasification agent rotational flow to fall into the high-temperature melting zone 3, the catalytic gasification ash enters the high-temperature melting zone 3 and then undergoes gas-solid mixing and reaction with a high-temperature oxidant, and the oxidant rotational flow can enhance the gas-solid mixing and reaction. The bottom of the high-temperature melting zone 3 is also provided with a molten liquid level, and the oxidant rotational flow can also stir the molten liquid at the bottom of the high-temperature melting zone 3 to form more uniform molten components, which is beneficial to forming stable compositions and smoothly discharging slag.
In this embodiment, the oxidant swirls to flow a certain depth below the surface of the molten metal and then enters the gasification reaction zone 2 along the inner wall surface of the columnar shell 1. Specifically, the high-temperature combustion products generated by the reaction of the oxidant and the carbon residue rise along the inner wall surface of the cylindrical shell 1 and are mixed with the swirling high-temperature gasifying agent to form a negative pressure zone, so that the catalytic gasification ash falls to the high-temperature melting zone 3. Meanwhile, product gas generated by high-temperature combustion is mixed with a high-temperature gasifying agent at the bottom of the gasification reaction zone 2 and then continuously reacts with the raw material coal upwards.
The catalytic gasification ash enters the high-temperature melting zone 3 to be combusted with oxygen to generate high temperature, and the released heat is transferred to the gasification reaction zone 2 through gas to maintain the heat balance of the gasification reaction zone 2; and simultaneously, the catalytic gasification ash is melted at high temperature, so that the high-temperature gasification agent in the catalytic gasification ash is solidified into the catalytic gasification ash to form a glassy substance, and harmless treatment is achieved.
Optionally, the temperature of the high-temperature gasification reaction and the pyrolysis reaction in the gasification reaction zone 2 is 650-. Below this temperature range, high temperature gasification cannot be achieved, and above this temperature, the gasification reaction is destroyed. The temperature of the high-temperature melting in the high-temperature melting zone 3 is: 850 ℃ and 1200 ℃, below which the melting cannot be achieved, and above which the gasification reaction is destroyed.
Optionally, the high temperature gasifying agent comprises H2O and/or O2. The coal sample and the high-temperature gasifying agent generate a carbohydrate reaction, a shift reaction and a methanation reaction, and the reactions can be rapidly carried out under the action of the high-temperature gasifying agent, so that crude gas rich in methane and catalytic gasification ash residues are finally generated.
Optionally, the high temperature oxidant comprises oxygen or oxygen-enriched steam.
Optionally, the gasification agent delivery device 5 comprises a plurality of gas distributors, a plurality of jet pipes or a plurality of nozzles; the oxidizer delivery device 6 includes: a plurality of gas distributors, a plurality of jet pipes, or a plurality of nozzles; each gas distributor is located on the same horizontal plane, each jet pipe is located on the same horizontal plane, or each nozzle is located on the same horizontal plane.
Preferably, the present embodiment selects jet pipes or nozzles as the gasifying agent delivery device 5 and the oxidizing agent delivery device 6 to reduce the difficulty of delivering the solid and the gas.
The output port of the gasifying agent conveying device 5 faces the top of the gasification reaction zone 2, the output port of the oxidant conveying device 6 faces the bottom of the high-temperature melting zone 3, namely, the gasifying agent conveying device 5 is obliquely and upwardly arranged on the inner wall of the cylindrical shell 1, and the oxidant conveying device 6 is obliquely and downwardly arranged on the inner wall of the cylindrical shell 1.
Preferably, the axial included angle between the output port of the gasifying agent conveying device 5 and the cylindrical shell 1 is 45-90 degrees, and meanwhile, the included angle between the output port of the gasifying agent conveying device 5 and the section perpendicular to the axial direction of the cylindrical shell 1 is 60-90 degrees; the axial included angle between the output port of the oxidant conveying device 6 and the cylindrical shell 1 is 15-50 degrees, and meanwhile, the included angle between the output port of the oxidant conveying device 6 and the cross section vertical to the axial direction of the cylindrical shell 1 is 45-90 degrees.
Specifically, in order to form a swirling flow of the gasifying agent flowing to the high-temperature melting zone 3 in the gasification reaction zone 2, an axial included angle between the gasifying agent conveying device 5 and the cylindrical shell 1 needs to be defined, and an included angle between the gasifying agent conveying device 5 and a cross section perpendicular to the axial direction needs to be defined in a spatial range of the cylindrical shell 1. Meanwhile, in order to form oxidant rotational flow flowing to the gasification reaction zone 2 in the high-temperature melting zone 3, an axial included angle between the oxidant delivery device 6 and the cylindrical shell 1 needs to be limited, and an included angle between the oxidant delivery device 6 and a cross section perpendicular to the axial direction needs to be limited within a space range of the cylindrical shell 1.
It can be seen that the gasifying agent delivery device 5 and the oxidant delivery device 6 are both obliquely arranged on the inner wall of the cylindrical shell 1; meanwhile, in the preferred embodiment of the present invention, the inclination angle of the gasifying agent delivery means 5 is larger than that of the oxidizing agent delivery means 6, so that a desired gasifying agent swirling flow passage and an oxidant swirling flow passage are formed in the gasification reaction zone 2 and the high-temperature melting zone 3, respectively.
Specifically, the axial included angle between the gasifying agent conveying device 5 and the cylindrical shell 1 is larger than the axial included angle between the oxidant conveying device 6 and the cylindrical shell 1, and the included angle between the gasifying agent conveying device 5 and the cross section perpendicular to the axial direction is larger than the included angle between the oxidant conveying device 6 and the cross section perpendicular to the axial direction.
Fig. 2 is a schematic diagram of the arrangement position of the gasification agent delivery device provided by the present invention, fig. 4 is a schematic diagram of the arrangement position of the oxidant delivery device provided by the present invention, please refer to fig. 2 and fig. 4, in this embodiment, at least four gasification agent delivery devices 5 are included, and the four gasification agent delivery devices 5 are all located on the same plane and symmetrically distributed at intervals at the bottom of the gasification reaction zone 2. At least comprises three oxidant delivery devices 6, and the three oxidant delivery devices 6 are all positioned on the same plane and symmetrically distributed at the top of the high-temperature melting zone 3 at intervals. So that a uniform combustion reaction space is formed inside the high-temperature melting zone 3.
Fig. 3 is a schematic gas flow diagram of the gasification reaction zone provided by the present invention, please refer to fig. 3, the arrangement of the gasification agent conveying device 5 of the present embodiment is such that a rotational flow of the gasification agent is formed when the high temperature gasification agent is input into the gasification reaction zone 2, a negative pressure zone P is formed at the lower part of the gasification reaction zone 2, and a rotational flow channel for the catalytic gasification ash to fall to the high temperature melting zone 3 is further formed, so as to facilitate the catalytic gasification ash to fall to the high temperature melting zone 3. Meanwhile, the high-temperature gasification agent is promoted to be fully mixed with the coal powder and uniformly fluidized in the reaction furnace, so that the reaction is promoted to be fully carried out, and the temperature distribution in the gasification reaction zone 2 is uniform.
Fig. 5 is a schematic gas flow direction diagram of the high-temperature melting zone provided by the present invention, and as shown by a dotted arrow in fig. 5, the arrangement of the oxidant delivery device 6 can also enable the gas flow ejected from the oxidant delivery device 6 to form an oxidant rotational flow and then enter the gasification reaction zone 2 along the inner wall surface of the cylindrical shell 1.
Fig. 6 is a schematic structural diagram of a coal catalytic gasification system provided by the present invention, please refer to fig. 6. In another embodiment of the present invention, there is provided a coal catalytic gasification system, including: the system comprises a coal preparation unit A, a coal catalytic gasification reaction furnace B, a coal gas purification unit C and a slag discharge unit D.
The coal preparation unit A is used for carrying out low-cost catalyst loading on the selected raw material coal to obtain a coal sample conforming to the catalytic gasification reaction.
The coal catalytic gasification reaction furnace B is used for carrying out high-temperature gasification on the coal sample conveyed by the coal preparation unit A to generate crude gas and catalytic gasification ash, and carrying out high-temperature melting on the catalytic gasification ash generated by the high-temperature gasification to obtain harmless treatment.
The coal gas purification unit C is used for separating the crude coal gas conveyed by the coal catalytic gasification reaction furnace B, so that the crude coal gas can be used as product gas, and meanwhile, collecting the separated fly ash, and conveying the fly ash back to the coal catalytic gasification reaction furnace B for high-temperature melting again.
And the slag discharging unit D is used for collecting liquid molten slag generated by the coal catalytic gasification reaction furnace B, treating the liquid molten slag and discharging the treated liquid molten slag.
In this embodiment, the output port of the coal preparation unit a is connected with a star feeder, and the star feeder is communicated with the feed port 4 of the coal catalytic gasification reaction furnace B to convey the coal sample prepared in the coal preparation unit a to the coal catalytic gasification reaction furnace B.
Specifically, the coal preparation unit A carries out low-cost catalyst loading on the crushed and sieved raw material coal with the diameter of less than 2mm to obtain a coal sample.
Optionally, the low cost catalyst comprises an alkali metal sulfate, calcium oxide, calcium hydroxide, industrial spent caustic sludge or industrial spent caustic. Alkali metal sulfates include potassium, sodium; the industrial waste alkaline residue or industrial waste alkaline liquid comprises waste water containing alkali metals and organic matters, such as papermaking black liquid, high-salt waste water and the like.
Optionally, the method for carrying out catalyst loading comprises: dry blending, impregnation or ion exchange.
Optionally, the device for loading the catalyst may be any device capable of achieving sufficient and uniform mixing of the raw material coal and the catalyst, and includes: high speed mixers, belts or blenders.
In this embodiment, need dry to raw materials coal as necessary for raw materials coal satisfies coal sample feeding water content requirement, does not influence coal sample and carries.
And a slag discharge port 7 of the coal catalytic gasification reaction furnace B is communicated with a slag discharge unit D, and the generated liquid molten slag is conveyed into the slag discharge unit D. And a granulator is arranged in the slag discharging unit D, atomized water is introduced into the granulator through an atomizing nozzle after the liquid molten slag enters the granulator, so that the liquid molten slag is granulated into a solid state, and the atomized water introduced by the atomizing nozzle is converted into steam which is recycled as a high-temperature gasifying agent in the coal catalytic gasification reaction furnace B. And the slag discharging unit D is also provided with a water jacket heat exchange structure for cooling solid slag which is solidified into solid state and recovering waste heat. The solid ash can be directly discharged or used as building materials.
And an exhaust port of the coal catalytic gasification reaction furnace B is communicated with the coal gas purification unit C so as to convey the crude coal gas into the coal gas purification unit C, and a cyclone separator, a filter and a return device are arranged in the coal gas purification unit C. The cyclone separator is used for separating a part of fly ash carried in the raw gas, so that the dust content of the raw gas meets the requirement of product gas; the filter is used for collecting the fly ash separated by the cyclone separator; the returning device is used for conveying the collected fly ash back to the high-temperature melting zone 3 of the coal catalytic gasification reaction furnace B for recycling treatment.
Optionally, the dedusted raw gas is directly used as a product gas after being removed by an acid gas.
Preferably, the catalytic coal gasification system of the embodiment further comprises a gas separation unit E for separating the dedusted raw gas by membrane separation or cryogenic separation to obtain CO/H2The methane is completely returned to the coal catalytic gasification reaction furnace B or partially returned to the coal catalytic gasification reaction furnace B to generate methanation, so that the methane concentration is further improved, the heat released by the methanation reaction is provided for the endothermic carbohydrate reaction, and the high-efficiency utilization of energy is realized.
The invention aims to protect a coal catalytic gasification reaction furnace, which comprises: a gasification reaction zone 2 and a high-temperature melting zone 3 are formed in the columnar shell 1, and the gasification reaction zone 2 is positioned above the high-temperature melting zone 3; at least four gasifying agent conveying devices 5 are arranged on the inner wall of the cylindrical shell 1 at intervals, the gasifying agent conveying devices 5 are positioned at the bottom of the gasification reaction zone 2, and the output ports of the gasifying agent conveying devices 5 face the top of the gasification reaction zone 2 and are used for conveying high-temperature gasifying agents to the gasification reaction zone 2; at least three oxidant delivery devices 6 are arranged on the inner wall of the columnar shell 1 at intervals, the oxidant delivery devices 6 are positioned at the top of the high-temperature melting zone 3, and the output ports of the oxidant delivery devices 6 face the bottom of the high-temperature melting zone 3 and are used for delivering the high-temperature oxidant to the high-temperature melting zone 3. Still protect a coal catalytic gasification reaction system, including coal catalytic gasification reacting furnace B, still include: a coal preparation unit A, a coal gas purification unit C and a slag discharge unit D; an output port of the coal preparation unit A is communicated with a feed port of the coal catalytic gasification reaction furnace B so as to convey the coal sample prepared in the coal preparation unit A to the coal catalytic gasification reaction furnace B; a slag discharge port 7 of the coal catalytic gasification reaction furnace B is communicated with a slag discharge unit D so as to convey liquid molten slag generated in the coal catalytic gasification reaction furnace B to the slag discharge unit D for treatment; an exhaust port of the coal catalytic gasification reaction furnace B is communicated with an input port of the coal gas purification unit C so as to convey the crude coal gas to the coal gas purification unit C; the ash outlet of the coal gas purification unit C is communicated with the coal catalytic gasification reaction furnace B so as to convey the fly ash back to the high-temperature melting zone 3 of the coal catalytic gasification reaction furnace B for circular treatment.
It is to be understood that the above-described embodiments of the present invention are merely illustrative of or explaining the principles of the invention and are not to be construed as limiting the invention. Therefore, any modification, equivalent replacement, improvement and the like made without departing from the spirit and scope of the present invention should be included in the protection scope of the present invention. Further, it is intended that the appended claims cover all such variations and modifications as fall within the scope and boundaries of the appended claims or the equivalents of such scope and boundaries.
Claims (11)
1. A coal catalytic gasification reaction furnace, comprising:
a cylindrical housing;
a gasification reaction zone and a high-temperature melting zone are formed in the cylindrical shell, and the gasification reaction zone is positioned above the high-temperature melting zone;
when a gasifying agent conveying device arranged at the bottom of the gasification reaction zone conveys a high-temperature gasifying agent towards the top of the gasification reaction zone, a gasifying agent rotational flow flowing to the high-temperature melting zone is formed in the gasification reaction zone;
and when the oxidant conveying device arranged at the top of the high-temperature melting zone conveys the high-temperature oxidant towards the bottom of the high-temperature melting zone, oxidant rotational flow flowing to the gasification reaction zone is formed in the high-temperature melting zone.
2. The catalytic coal gasification reaction furnace according to claim 1,
the output port of the gasification agent conveying device faces the top of the gasification reaction zone;
the output port of the oxidant conveying device faces the bottom of the high-temperature melting zone.
3. The catalytic coal gasification reaction furnace according to claim 2,
the gasification agent conveying device and the oxidant conveying device are arranged on the inner wall of the cylindrical shell;
the axial included angle between the output port of the gasification agent conveying device and the cylindrical shell is 45-90 degrees;
the output port of the gasification agent conveying device forms an included angle of 60-90 degrees with the cross section perpendicular to the axial direction;
the axial included angle between the output port of the oxidant conveying device and the cylindrical shell is 15-50 degrees;
the included angle between the output port of the oxidant conveying device and the cross section perpendicular to the axial direction is 45-90 degrees.
4. The catalytic coal gasification reaction furnace according to claim 1,
the gasification agent conveying device comprises: a plurality of gas distributors, a plurality of jet pipes, or a plurality of nozzles;
the oxidant delivery device includes: a plurality of gas distributors, a plurality of jet pipes, or a plurality of nozzles;
each gas distributor is located on the same horizontal plane, each jet pipe is located on the same horizontal plane, or each nozzle is located on the same horizontal plane.
5. The catalytic coal gasification reaction furnace according to claim 1,
the high-temperature gasifying agent comprises: h2O and/or O2；
The high temperature oxidant includes: oxygen or oxygen-enriched steam.
6. The catalytic coal gasification reaction furnace according to claim 1,
a molten liquid level is formed at the bottom of the high-temperature melting zone;
and the oxidant swirls to flow into the position below the molten liquid level by a certain depth and then enters the gasification reaction zone along the inner wall surface of the columnar shell.
7. A coal catalytic gasification reaction system comprising the coal catalytic gasification reaction furnace according to any one of claims 1 to 6, further comprising: the system comprises a coal preparation unit, a coal gas purification unit and a slag discharge unit;
an output port of the coal preparation unit is communicated with a feed port of the coal catalytic gasification reaction furnace so as to convey the coal sample prepared in the coal preparation unit to the coal catalytic gasification reaction furnace;
a slag discharging port of the coal catalytic gasification reaction furnace is communicated with the slag discharging unit so as to convey liquid molten slag generated in the coal catalytic gasification reaction furnace to the slag discharging unit for treatment;
an exhaust port of the coal catalytic gasification reaction furnace is communicated with an input port of the coal gas purification unit so as to convey the crude coal gas into the coal gas purification unit;
and an ash outlet of the coal gas purification unit is communicated with the coal catalytic gasification reaction furnace so as to convey the fly ash back to a high-temperature melting zone of the coal catalytic gasification reaction furnace for circular treatment.
8. The coal catalytic gasification reaction system according to claim 7,
the coal preparation unit is used for preparing a coal sample by a catalyst loading method;
the catalyst comprises: alkali metal sulfate, calcium oxide, calcium hydroxide, industrial waste caustic sludge or industrial waste lye;
the method for loading the catalyst comprises the following steps: dry blending, impregnation or ion exchange.
9. The coal catalytic gasification reaction system according to claim 7,
the slag discharge unit comprises: a granulator and heat exchange structure;
the granulator is used for granulating the liquid molten slag into a solid state;
the heat exchange structure is used for cooling the solid molten slag and recovering waste heat.
10. The coal catalytic gasification reaction system according to claim 7,
the coal gas purification unit comprises the following components in sequential connection: a cyclone, a filter and a return;
the cyclone separator is used for separating fly ash carried in the crude gas;
the filter is used for collecting the fly ash;
the return device is used for conveying the fly ash back to a high-temperature melting area of the coal catalytic gasification reaction furnace.
11. The coal catalytic gasification reaction system of claim 7, further comprising: a gas separation unit;
the input port of the gas separation unit is communicated with the output port of the gas purification unit and is used for performing membrane separation or cryogenic separation on the crude gas after fly ash separation to obtain CO or H2；
A first output port of the gas separation unit is communicated with the coal catalytic gasification reaction furnace and is used for completely removing the CO or the H2Or part of said CO or H2Conveying the coal to the coal catalytic gasification reaction furnace;
the second output port of the gas separation unit is used for outputting the CO or the H2。
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| CN202110156643.5A CN112920853B (en) | 2021-02-04 | 2021-02-04 | Coal catalytic gasification reaction furnace and coal catalytic gasification reaction system |
| PCT/CN2021/084950 WO2022165972A1 (en) | 2021-02-04 | 2021-04-01 | Catalytic coal gasification reaction furnace and catalytic coal gasification reaction system |
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| CN101201167A (en) * | 2007-12-25 | 2008-06-18 | 哈尔滨工业大学 | Apparatus and method for gasification of refuse and hyperthermia melt processing of flying ash |
| CN102831945A (en) * | 2012-08-16 | 2012-12-19 | 中国科学院等离子体物理研究所 | Device and method for disposing low and medium-radioactivity solid waste by hot plasmas |
| CN107760379A (en) * | 2016-08-23 | 2018-03-06 | 中国石油化工股份有限公司 | Fluid bed and melting bed combined type catalytic coal gasification devices and methods therefor |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105038860A (en) * | 2015-07-10 | 2015-11-11 | 北京柯林斯达科技发展有限公司 | Swirl-flow type gasification furnace and swirl-flow type gasification process |
| CN107760385B (en) * | 2016-08-23 | 2020-12-01 | 中国石油化工股份有限公司 | Coal gasification device combining fluidized bed and molten bed and method thereof |
| CN107177384B (en) * | 2017-07-11 | 2020-06-19 | 新奥科技发展有限公司 | Catalytic gasification device, system and method |
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- 2021-04-01 WO PCT/CN2021/084950 patent/WO2022165972A1/en unknown
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101201167A (en) * | 2007-12-25 | 2008-06-18 | 哈尔滨工业大学 | Apparatus and method for gasification of refuse and hyperthermia melt processing of flying ash |
| CN102831945A (en) * | 2012-08-16 | 2012-12-19 | 中国科学院等离子体物理研究所 | Device and method for disposing low and medium-radioactivity solid waste by hot plasmas |
| CN107760379A (en) * | 2016-08-23 | 2018-03-06 | 中国石油化工股份有限公司 | Fluid bed and melting bed combined type catalytic coal gasification devices and methods therefor |
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| CN112920853B (en) | 2022-08-12 |
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