CN110923016A - Method and device for producing substitute natural gas from coal - Google Patents
Method and device for producing substitute natural gas from coal Download PDFInfo
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- CN110923016A CN110923016A CN201911276272.3A CN201911276272A CN110923016A CN 110923016 A CN110923016 A CN 110923016A CN 201911276272 A CN201911276272 A CN 201911276272A CN 110923016 A CN110923016 A CN 110923016A
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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
- C10J3/485—Entrained flow gasifiers
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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
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
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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
- Y02P20/10—Process efficiency
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Abstract
A method for producing substitute natural gas from coal and a device thereof belong to the technical field of producing substitute natural gas from coal. Raw material coal and a hydrogenation reaction gasifying agent are sprayed into a hydrogenation entrained-flow bed gasification furnace through a feeding nozzle together, a hydrogenation gasification reaction is carried out in the furnace, a hydrogenation gasification product enters a gas-solid separator for separation, solid semicoke obtained by separation is sent into a circulating fluidized bed gasification furnace through a pneumatic material returning valve and carries out a gasification reaction with the gasification reaction gasifying agent introduced from the lower part of a fluidized bed, hydrogen generated by the fluidized bed gasification furnace is sent into a coil heat exchanger of the hydrogenation gasification furnace to be heated and then is used as the gasifying agent of the hydrogenation gasification reaction again, ash generated by the fluidized bed gasification furnace is discharged from the bottom, and substitute natural gas which is rich in methane and is obtained by separation of the gas-solid separator is cooled through the coil heat exchanger to. The invention has the advantages of simple process flow, low investment cost, high process thermal efficiency and the like.
Description
Technical Field
The invention belongs to the technical field of substitute natural gas production by coal, and particularly relates to a method and a device for producing substitute natural gas by coupling an entrained-flow bed hydrogenation gasification furnace and a circulating fluidized bed gasification furnace.
Background
With the advance of urbanization process, the natural gas market in China enters a large-scale development stage, and the consumption of natural gas is rapidly increased. The method utilizes abundant coal resources in China to develop the synthetic natural gas prepared from coal, and is beneficial to reducing the dependence of China on imported natural gas resources, optimizing the energy consumption structure and guaranteeing the safety of natural gas supply.
The traditional coal-to-natural gas process flow comprises coal gasification, carbon monoxide conversion, synthesis gas purification and methanation reaction. The technological process is mature, industrialization is realized in the great plains of America in the eighties of the nineteenth century, most of nearly 50 coal-based natural gas projects planned to be built in China adopt the process, but the process is long, investment is large, and process thermal efficiency is low. The technology for preparing the substitute natural gas by direct coal hydrogasification is that under the conditions of (850-1000 ℃) and 7MPa, pulverized coal and hydrogen are simultaneously added into a gasification furnace, and methane-rich substitute natural gas is obtained by means of the stabilizing effect of the hydrogen on the release of free radicals in the coal pyrolysis stage and the reaction of the gasification stage and active carbon in semicoke. Compared with the traditional process, the process has the advantages of simple flow, low investment cost and higher thermal efficiency.
Because of the limitation of coal hydro-gasification reaction, the carbon conversion rate in the process of preparing substitute natural gas by direct hydro-gasification of coal is generally only 50-60%, the concentration of solid-phase particles in product gas is higher, and the carbon content in solid-phase products is higher. In order to separate the product gas from the solid particles, a cooling device is often provided below or after the gasification furnace in the prior art. The 'a chiller and a gasification furnace with the chiller' proposed by the Chinese utility model patent CN202144505U adopts the chiller arranged at the lower part of the gasification furnace to realize the separation of product gas and solid phase products. In the system and method for preparing natural gas substitute from coal, which is proposed in the Chinese patent invention CN101657525A, the hydro-gasification reaction product is firstly cooled in a radiation boiler, and then a cyclone separator and a candle filter are used for realizing the separation of gas phase products and solid particles.
The hydrogen source problem is the other key problem of the technology for preparing substitute natural gas by direct coal hydrogasification, most of the prior solid semicokes obtained by hydrogasification are cooled and then sent into another gasification furnace for steam gasification reaction, the generated synthesis gas is purified, cooled and separated to obtain hydrogen, and then the hydrogen is sent into a preheating furnace for preheating, and the hydrogen is sent into a coal hydrogasification furnace after reaching the temperature required by hydrogasification. In the process, the high-temperature solid-phase product of hydro-gasification needs to be cooled firstly to complete the separation from the gas-phase product, then the high-temperature solid-phase product enters the steam gasification furnace to be heated again to complete the gasification reaction to generate hydrogen, the hydrogen is preheated and then sent into the hydro-gasification furnace, and the utilization efficiency of energy and heat in the whole process is low.
Disclosure of Invention
The invention of the invention is: in order to overcome the defects in the prior art, the invention provides a method for producing substitute natural gas by coal and a device thereof.
The design concept of the invention is as follows: a method for producing substitute natural gas by coupling an entrained-flow bed hydrogenation gasification furnace and a circulating fluidized bed gasification furnace is provided, wherein semicoke generated by the entrained-flow bed hydrogenation gasification is used as a raw material of the circulating fluidized bed gasification furnace, and hydrogen generated by the circulating fluidized bed gasification furnace is used as a gasification agent of the entrained-flow bed hydrogenation gasification furnace.
The invention is realized by the following technical scheme.
An apparatus for producing substitute natural gas from coal, comprising an entrained-flow bed hydrogenation gasification furnace, a gas-solid separator, a pneumatic return valve and a circulating fluidized bed gasification furnace, wherein:
a sealing cover is arranged at an opening at the upper end of the entrained-flow bed hydrogenation gasification furnace, a feeding nozzle penetrates through the sealing cover and is communicated with a gasification chamber in an inner cavity of the entrained-flow bed hydrogenation gasification furnace, an annular interlayer is arranged on the side wall of the entrained-flow bed hydrogenation gasification furnace positioned around the gasification chamber, a coil heat exchanger is arranged in the annular interlayer, and the coil heat exchanger is spirally wound on the inner wall of the annular interlayer; a hydrogen inlet pipe and a product gas outlet pipe are arranged on the side wall of the entrained-flow bed hydrogenation gasification furnace and are positioned above the coil heat exchanger, a hydrogen outlet pipe and a high-temperature gas outlet pipe are arranged on the side wall of the entrained-flow bed hydrogenation gasification furnace and are positioned below the coil heat exchanger, the hydrogen inlet pipe and the hydrogen outlet pipe are respectively communicated with the gasification chamber, one ends of the product gas outlet pipe and the high-temperature gas outlet pipe are respectively communicated with the annular interlayer, and the other end of the high-temperature gas outlet pipe is communicated with an inlet of the gas-solid; a product outlet pipe is arranged at the bottom of the entrained-flow bed hydrogenation gasification furnace, one end of the product outlet pipe is communicated with the gasification chamber, and the other end of the product outlet pipe is communicated with an inlet of the gas-solid separator through a pipeline;
the gas-solid separator is vertically arranged, the middle part of the gas-solid separator is provided with a vertical pipe, the lower part of the vertical pipe is provided with a first pneumatic return valve, the first pneumatic return valve comprises a feeding section and a return section, the inlet of the feeding section is communicated with the lower part of the vertical pipe, the outlet of the return section is communicated with the circulating fluidized bed gasification furnace through a pipeline, a partition plate is arranged between the upper part of the feeding section and the upper part of the return section, an air distribution plate with an air cap is arranged below the feeding section and the return section, and an air chamber is arranged below the air distribution plate;
the top of the circulating fluidized bed gasification furnace is communicated with an inlet of a coal-gas separator, the top of the coal-gas separator is provided with a coal gas outlet pipe, the bottom of the coal-gas separator is provided with a pneumatic return valve II, and the coal-gas separator is communicated with the pneumatic return valve II; a feeding pipe and a circulating material returning pipe are arranged on the side wall of the lower portion of the hearth of the circulating fluidized bed gasification furnace, one end of the feeding pipe is communicated with the returning section, the other end of the feeding pipe is communicated with the hearth of the circulating fluidized bed gasification furnace, one end of the circulating material returning pipe is communicated with the hearth of the circulating fluidized bed gasification furnace, and the other end of the circulating material returning pipe is communicated with the pneumatic returning valve II; the lower part of the hearth of the circulating fluidized bed gasification furnace is provided with a conical air distribution plate, the lower part of the conical air distribution plate is communicated with one end of a discharge pipe, and the other end of the discharge pipe extends to the outside of the circulating fluidized bed gasification furnace; and a gas chamber is arranged below the conical air distribution plate, and a gasifying agent inlet pipe is arranged on the side wall of the circulating fluidized bed gasification furnace at the position of the gas chamber.
Furthermore, the first pneumatic return valve adopts water vapor as a medium, and the gas velocity in the first pneumatic return valve is 0.004-0.03 m/s.
Furthermore, the position of the conical air distribution plate is lower than the position of the feeding pipe communicated with the hearth of the circulating fluidized bed gasification furnace, and the position of the feeding pipe communicated with the hearth of the circulating fluidized bed gasification furnace is lower than the position of the circulating material return pipe communicated with the hearth of the circulating fluidized bed gasification furnace.
Further, the product outlet pipe is arranged as a Y-shaped tee.
A method for producing substitute natural gas using a coal-based substitute natural gas production plant, comprising the steps of:
s1, after the device is installed, feeding crushed raw material coal and a hydrogasification reaction gasifying agent into an entrained-flow bed hydrogasification furnace through a feeding nozzle, wherein the hydrogasification reaction gasifying agent is a mixed gas of hydrogen and oxygen; in the adding process, oxygen and part of hydrogen are subjected to combustion reaction at the position of a feeding nozzle, the rest hydrogen is heated by the combustion reaction, and the raw material coal and the rest hydrogen are subjected to hydro-gasification reaction in a gasification chamber;
s2, feeding a gas-phase product and a solid-phase product generated by the hydro-gasification reaction in the step S1 into a gas-solid separator through a product outlet pipe, separating the gas-phase product and the solid-phase product, and feeding the separated high-temperature solid-phase product into the circulating fluidized bed gasification furnace through a pneumatic material returning valve I and a feeding pipe under the condition of not reducing the temperature;
s3, in the circulating fluidized bed gasification furnace, a gasification agent of the gasification reaction is introduced into the bottom of the circulating fluidized bed gasification furnace through a gasification agent inlet pipe and a conical air distribution plate in sequence, the gasification agent of the gasification reaction and the high-temperature solid-phase product separated in the step S2 are subjected to the gasification reaction, and the gasification agent of the gasification reaction is a mixed gas of oxygen and water vapor; and discharging residues generated by the gasification reaction through a discharge pipe, discharging synthetic gas generated by the gasification reaction through a gas-gas separator after removing dust through a gas outlet pipe, sending clean hydrogen obtained after separation into the coil heat exchanger in the step S1 through a hydrogen inlet pipe again, exchanging heat with high-temperature product gas discharged from the upper part of the gas-solid separator, sending the clean hydrogen into the entrained flow bed hydrogenation gasification furnace through a feeding nozzle again to be used as a raw material of a hydrogenation gasification reaction gasifying agent, cooling substitute natural gas rich in methane through the coil heat exchanger to obtain product gas, and outputting the product gas through a product gas outlet pipe.
Further, in step S1, the particle size of the raw material coal is not greater than 200 mesh.
Further, in the step S1, the temperature of the hydrogen gas entering the feeding nozzle is 400-550 ℃.
Further, in the step S1, the mass ratio of the hydrogen gas to the raw coal entering the feeding nozzle is 0.1 to 0.5.
Further, in the step S1, the molar ratio of the oxygen to the hydrogen in the hydrogasification reaction gasifying agent is 0.005 to 0.02.
Further, in step S1, the oxygen and part of the hydrogen in the entrained flow hydro-gasifier near the feeding nozzle are combusted, and the remaining unreacted hydrogen is heated to 900-1200 ℃.
Further, in the step S1, the reaction temperature in the entrained-flow hydro-gasification furnace is 700-900 ℃, and the reaction pressure is 3-7 MPa.
Further, in the step S2, the temperature in the gas-solid separator is 650-850 ℃.
Further, in the step S3, the reaction temperature in the circulating fluidized bed gasification furnace is 800-.
Compared with the prior art, the invention has the beneficial effects that:
the invention fully considers the characteristics of the coal structure and combines the characteristics of the coal hydro-gasification reaction, adopts a staged conversion mode, and realizes the process of producing the substitute natural gas by the coal by reasonably and efficiently coupling the entrained-flow bed hydro-gasification furnace and the circulating fluidized bed gasification furnace. The product of coal hydro-gasification directly enters a gas-solid separator for separation, the high-temperature solid-phase semi-coke obtained by separation is directly sent into the circulating fluidized bed gasification furnace through a pneumatic return valve under the condition of not reducing the temperature, and because the temperature of the solid semi-coke is higher, only a small amount of oxygen needs to be introduced into the lower part of the circulating fluidized bed gasification furnace, and a small amount of carbon is combusted to reach the temperature required by steam gasification, so that the effective component in the synthesis gas is higher. Sensible heat carried by high-temperature gas-phase products is used for preheating raw material hydrogen by using a coil heat exchanger arranged in the entrained flow bed hydro-gasification furnace, so that hydrogen consumption in the hydro-gasification process is reduced. In addition, compared with the prior art, the method has the advantages of simple process, short flow, high process thermal efficiency and the like.
Drawings
FIG. 1 is a front sectional structural schematic view of the present invention;
fig. 2 is a schematic structural diagram of parts of the pneumatic material returning valve.
1-an entrained flow hydrogenation gasification furnace; 2-a gasification chamber; 3-a feed nozzle; 4-coil heat exchanger; 5-a hydrogen inlet pipe; 6-hydrogen outlet pipe; 7-product gas outlet pipe; 8-a product outlet pipe; 9-gas-solid separator; 10-a riser; 11-a ring-shaped interlayer; 12-a first pneumatic return valve; 13-a feeding section; 14-a material return section; 15-air distribution plate; 16-a wind chamber; 17-circulating fluidized bed gasification furnace; 18-a feeder tube; 19-a circulating material return pipe; 20-a conical air distribution plate; 21-a discharge pipe; 22-air chamber; 23-a gasification agent inlet pipe; 24-a coal gas separator; 25-gas outlet pipe; 26-a pneumatic material returning valve II; 27-high temperature gas outlet pipe.
Detailed Description
The present invention will be described in further detail with reference to specific embodiments by the attached drawings, and the following embodiments are only used as representative examples to clearly and completely explain the present invention, but the protection scope of the present invention is not limited by these embodiments.
An apparatus for producing substitute natural gas from coal, as shown in fig. 1 and 2, comprises an entrained flow hydro-gasification furnace 1, a gas-solid separator 9, a pneumatic return valve one 12 and a circulating fluidized bed gasification furnace 24, wherein:
a sealing cover is arranged at an opening at the upper end of the entrained-flow bed hydrogenation gasification furnace 1, a feeding nozzle 3 penetrates through the sealing cover and is communicated with a gasification chamber 2 in the inner cavity of the entrained-flow bed hydrogenation gasification furnace 1, an annular interlayer 11 is arranged on the side wall of the entrained-flow bed hydrogenation gasification furnace 1 positioned around the gasification chamber 2, a coil heat exchanger 4 is arranged in the annular interlayer 11, and the coil heat exchanger 4 is spirally wound on the inner wall of the annular interlayer 11; a hydrogen inlet pipe 5 and a product gas outlet pipe 7 are arranged on the side wall of the entrained-flow bed hydrogenation gasification furnace 1 and are positioned above the coil heat exchanger 4, a hydrogen outlet pipe 6 and a high-temperature gas outlet pipe 27 are arranged on the side wall of the entrained-flow bed hydrogenation gasification furnace 1 and are positioned below the coil heat exchanger 4, the hydrogen inlet pipe 5 and the hydrogen outlet pipe 6 are respectively communicated with the gasification chamber 2, one ends of the product gas outlet pipe 7 and the high-temperature gas outlet pipe 27 are respectively communicated with the annular interlayer 11, and the other end of the high-temperature gas outlet pipe 27 is communicated with an inlet of the gas-solid separator; a product outlet pipe 8 is arranged at the bottom of the entrained-flow bed hydrogenation gasification furnace 1, one end of the product outlet pipe 8 is communicated with the gasification chamber 2, and the other end of the product outlet pipe 8 is communicated with an inlet of a gas-solid separator 9 through a pipeline;
the gas-solid separator 9 is vertically arranged, the middle part of the gas-solid separator 9 is provided with a vertical pipe 10, the lower part of the vertical pipe 10 is provided with a first pneumatic return valve 12, the first pneumatic return valve 12 comprises a feeding section 13 and a return section 14, the inlet of the feeding section 13 is communicated with the lower part of the vertical pipe 10, the outlet of the return section 14 is communicated with a circulating fluidized bed gasification furnace 17 through a pipeline, a partition plate is arranged between the upper part of the feeding section 13 and the upper part of the return section 14, an air distribution plate 15 with an air cap is arranged below the feeding section 13 and the return section 14, and an air chamber 16 is arranged below the air distribution plate 15;
the top of the circulating fluidized bed gasification furnace 17 is communicated with an inlet of a coal-gas separator 24, a coal gas outlet pipe 25 is arranged at the top of the coal-gas separator 24, a pneumatic return valve II 26 is arranged at the bottom of the coal-gas separator 24, and the coal-gas separator 24 is communicated with the pneumatic return valve II 26; a feeding pipe 18 and a circulating material return pipe 19 are arranged on the side wall of the lower portion of the hearth of the circulating fluidized bed gasification furnace 17, one end of the feeding pipe 18 is communicated with the return section 14, the other end of the feeding pipe 18 is communicated with the hearth of the circulating fluidized bed gasification furnace 17, one end of the circulating material return pipe 19 is communicated with the hearth of the circulating fluidized bed gasification furnace 17, and the other end of the circulating material return pipe 19 is communicated with the pneumatic return valve II 26; the lower part of the hearth of the circulating fluidized bed gasification furnace 17 is provided with a conical air distribution plate 20, the lower part of the conical air distribution plate 20 is communicated with one end of a discharge pipe 21, and the other end of the discharge pipe 21 extends to the outside of the circulating fluidized bed gasification furnace 17; a gas chamber 22 is arranged below the conical air distribution plate 20, and a gasifying agent inlet pipe 23 is arranged on the side wall of the circulating fluidized bed gasification furnace 17 at the position of the gas chamber 22.
Further, the first pneumatic return valve 12 adopts water vapor as a medium, and the gas velocity in the first pneumatic return valve 12 is 0.004-0.03 m/s.
Further, the position of the conical air distribution plate 20 is lower than the position of the feeding pipe 18 communicated with the hearth of the circulating fluidized bed gasification furnace 17, and the position of the feeding pipe 18 communicated with the hearth of the circulating fluidized bed gasification furnace 17 is lower than the position of the circulating material return pipe 19 communicated with the hearth of the circulating fluidized bed gasification furnace 17.
Further, the product outlet pipe 8 is arranged as a Y-shaped tee.
A method for producing substitute natural gas using a coal-based substitute natural gas production plant, comprising the steps of:
s1, after the device is installed, feeding crushed raw material coal, hydrogen preheated to 500 ℃ and a small amount of oxygen into an entrained flow bed hydrogenation gasification furnace 1 through a feeding nozzle 3, wherein the oxygen and part of the hydrogen are subjected to combustion reaction at the position of the feeding nozzle 3 in the feeding process, the rest hydrogen is heated to 1000 ℃ through the combustion reaction, the raw material coal and the heated high-temperature hydrogen are subjected to hydrogenation gasification reaction in a gasification chamber 2, the temperature of the hydrogenation gasification reaction is 850 ℃, and the reaction pressure is 3-7 MPa;
s2, the gas-phase product and the solid-phase product generated by the hydro-gasification reaction in the step S1 enter a gas-solid separator 9 through a product outlet pipe 8 for separation, and the temperature in the gas-solid separator 9 is 650-850 ℃; the separated high-temperature solid phase product (solid semicoke) is directly sent into a circulating fluidized bed gasification furnace 17 through a pneumatic return valve I12 and a feeding pipe 18 under the condition of not reducing the temperature;
s3, in the circulating fluidized bed gasification furnace 17, the high-temperature solid-phase product separated in the step S2 and gasification reaction gasifying agents (water vapor and oxygen) introduced from a conical air distribution plate 20 at the bottom of the circulating fluidized bed gasification furnace 17 are subjected to gasification reaction, the temperature of the gasification reaction is 950 ℃, residues generated by the gasification reaction are discharged from a discharge pipe 21, synthetic gas generated by the gasification reaction is discharged from a gas outlet pipe 25 after dust is removed by a gas separator 24, the reaction temperature in the circulating fluidized bed gasification furnace 24 is 800-1000 ℃, the reaction pressure is 3-7MPa, and the gas flow rate is 2-6 m/S; the clean hydrogen obtained after the separation treatment is sent into the coil heat exchanger 4 in the step S1 again through the hydrogen inlet pipe 5 to exchange heat with the high-temperature product gas discharged from the upper part of the gas-solid separator 9, the temperature of the hydrogen flowing out from the hydrogen outlet pipe 6 is 500 ℃, and then the hydrogen is sent into the entrained flow bed hydrogenation gasification furnace 1 through the feeding nozzle 3 again to be used as the raw material of the gasification agent of the hydrogenation gasification reaction, and the substitute natural gas rich in methane is cooled through the coil heat exchanger 4 to obtain the product gas which is output through the product gas outlet pipe 7.
Further, in step S1, the particle size of the raw material coal is not greater than 200 mesh.
Further, in the step S1, the mass ratio of the hydrogen gas to the raw coal entering the feed nozzle 3 is 0.1 to 0.5.
Further, in the step S1, the gasification agent of the hydro-gasification reaction entering the feeding nozzle 3 is a mixed gas of oxygen and hydrogen, wherein the molar ratio of the oxygen to the hydrogen is 0.005-0.02.
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 changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are included in 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 (13)
1. The utility model provides a device of substitute natural gas is produced to coal, it includes entrained flow bed hydrogenation gasifier (1), gas-solid separator (9), pneumatic feed back valve and circulating fluidized bed gasifier (24), its characterized in that:
a sealing cover is arranged at an opening at the upper end of the entrained-flow bed hydrogenation gasification furnace (1), a feeding nozzle (3) penetrates through the sealing cover to be communicated with a gasification chamber (2) in the inner cavity of the entrained-flow bed hydrogenation gasification furnace (1), an annular interlayer (11) is arranged on the side wall of the entrained-flow bed hydrogenation gasification furnace (1) positioned around the gasification chamber (2), a coil heat exchanger (4) is arranged in the annular interlayer (11), and the coil heat exchanger (4) is spirally wound on the inner wall of the annular interlayer (11); a hydrogen inlet pipe (5) and a product gas outlet pipe (7) are arranged on the side wall of the entrained-flow bed hydrogenation gasification furnace (1) and are positioned above the coil heat exchanger (4), a hydrogen outlet pipe (6) and a high-temperature gas outlet pipe (27) are arranged on the side wall of the entrained-flow bed hydrogenation gasification furnace (1) and are positioned below the coil heat exchanger (4), the hydrogen inlet pipe (5) and the hydrogen outlet pipe (6) are respectively communicated with the gasification chamber (2), one ends of the product gas outlet pipe (7) and the high-temperature gas outlet pipe (27) are respectively communicated with the annular interlayer (11), and the other end of the high-temperature gas outlet pipe (27) is communicated with an inlet of the gas-solid separator (9); a product outlet pipe (8) is arranged at the bottom of the entrained-flow bed hydrogenation gasification furnace (1), one end of the product outlet pipe (8) is communicated with the gasification chamber (2), and the other end of the product outlet pipe (8) is communicated with an inlet of a gas-solid separator (9) through a pipeline;
the gas-solid separator (9) is vertically arranged, the middle part of the gas-solid separator (9) is provided with a vertical pipe (10), the lower part of the vertical pipe (10) is provided with a pneumatic return valve I (12), the pneumatic return valve I (12) comprises a feeding section (13) and a return section (14), the inlet of the feeding section (13) is communicated with the lower part of the vertical pipe (10), the outlet of the return section (14) is communicated with a circulating fluidized bed gasification furnace (17) through a pipeline, a partition plate is arranged between the upper part of the feeding section (13) and the upper part of the return section (14), an air distribution plate (15) with an air cap is arranged below the feeding section (13) and the return section (14), and an air chamber (16) is arranged below the air distribution plate (15);
the top of the circulating fluidized bed gasification furnace (17) is communicated with an inlet of a coal-gas separator (24), a coal gas outlet pipe (25) is arranged at the top of the coal-gas separator (24), a pneumatic material return valve II (26) is arranged at the bottom of the coal-gas separator (24), and the coal-gas separator (24) is communicated with the pneumatic material return valve II (26); a feeding pipe (18) and a circulating material return pipe (19) are arranged on the side wall of the lower portion of the hearth of the circulating fluidized bed gasification furnace (17), one end of the feeding pipe (18) is communicated with the return section (14), the other end of the feeding pipe (18) is communicated with the hearth of the circulating fluidized bed gasification furnace (17), one end of the circulating material return pipe (19) is communicated with the hearth of the circulating fluidized bed gasification furnace (17), and the other end of the circulating material return pipe (19) is communicated with the pneumatic return valve II (26); the lower part of a hearth of the circulating fluidized bed gasification furnace (17) is provided with a conical air distribution plate (20), the lower part of the conical air distribution plate (20) is communicated with one end of a discharge pipe (21), and the other end of the discharge pipe (21) extends to the outside of the circulating fluidized bed gasification furnace (17); a gas chamber (22) is arranged below the conical air distribution plate (20), and a gasifying agent inlet pipe (23) is arranged on the side wall of the circulating fluidized bed gasification furnace (17) positioned at the position of the gas chamber (22).
2. An apparatus for substitute natural gas production from coal as claimed in claim 1 wherein: the first pneumatic material returning valve (12) adopts water vapor as a medium, and the gas velocity in the first pneumatic material returning valve (12) is 0.004-0.03 m/s.
3. An apparatus for substitute natural gas production from coal as claimed in claim 1 wherein: the position of the conical air distribution plate (20) is lower than the position of the feed pipe (18) communicated with the hearth of the circulating fluidized bed gasification furnace (17), and the position of the feed pipe (18) communicated with the hearth of the circulating fluidized bed gasification furnace (17) is lower than the position of the circulating material return pipe (19) communicated with the hearth of the circulating fluidized bed gasification furnace (17).
4. An apparatus for substitute natural gas production from coal as claimed in claim 1 wherein: the product outlet pipe (8) is arranged into a Y-shaped three-way pipe.
5. A method of producing substitute natural gas using the coal substitute natural gas production plant of claim 1, comprising the steps of:
s1, after the device is installed, feeding crushed raw material coal and a hydrogasification reaction gasifying agent into an entrained-flow bed hydrogenation gasification furnace (1) through a feeding nozzle (3), wherein the hydrogasification reaction gasifying agent is a mixed gas of hydrogen and oxygen; in the adding process, oxygen and part of hydrogen are subjected to combustion reaction at the position of the feeding nozzle (3), the rest hydrogen is heated by the combustion reaction, and the raw material coal and the rest hydrogen are subjected to hydro-gasification reaction in the gasification chamber (2);
s2, feeding a gas-phase product and a solid-phase product generated by the hydro-gasification reaction in the step S1 into a gas-solid separator (9) through a product outlet pipe (8), separating the gas-phase product and the solid-phase product, and feeding the separated high-temperature solid-phase product into a circulating fluidized bed gasification furnace (17) through a pneumatic return valve I (12) and a feeding pipe (18) under the condition of not reducing the temperature;
s3, in the circulating fluidized bed gasification furnace (17), a gasification agent of a gasification reaction is introduced into the bottom of the circulating fluidized bed gasification furnace (17) through a gasification agent inlet pipe (23) and a conical air distribution plate (20) in sequence, the gasification agent of the gasification reaction and the high-temperature solid-phase product separated in the step S2 are subjected to a gasification reaction, and the gasification agent of the gasification reaction is a mixed gas of oxygen and water vapor; and residues generated by gasification reaction are discharged by a discharge pipe (21), the synthesis gas generated by the gasification reaction is discharged by a gas outlet pipe (25) after dust is removed by a gas-gas separator (24), the clean hydrogen obtained after separation treatment is sent into the coil heat exchanger (4) in the step S1 again through a hydrogen inlet pipe (5) to exchange heat with the high-temperature product gas discharged from the upper part of the gas-solid separator (9), and then the clean hydrogen is sent into the entrained flow bed hydrogenation gasification furnace (1) through a feeding nozzle (3) to be used as a raw material of the hydrogenation gasification agent of the gasification reaction, and the substitute natural gas rich in methane is cooled by the coil heat exchanger (4) to obtain the product gas which is output by a product gas outlet pipe (7).
6. The method of substitute natural gas production by a coal substitute natural gas production plant of claim 5, wherein: in step S1, the particle size of the raw material coal is not greater than 200 mesh.
7. The method of substitute natural gas production by a coal substitute natural gas production plant of claim 5, wherein: in the step S1, the temperature of the hydrogen gas entering the feeding nozzle (3) is 400-550 ℃.
8. The method of substitute natural gas production by a coal substitute natural gas production plant of claim 5, wherein: in the step S1, the mass ratio of the hydrogen to the raw material coal entering the feeding nozzle (3) is 0.1-0.5.
9. The method of substitute natural gas production by a coal substitute natural gas production plant of claim 5, wherein: in the step S1, the molar ratio of oxygen to hydrogen in the gasification agent for hydro-gasification reaction is 0.005 to 0.02.
10. The method of substitute natural gas production by a coal substitute natural gas production plant of claim 5, wherein: in the step S1, the oxygen and part of the hydrogen in the entrained-flow hydrogenation gasifier (1) near the feed nozzle (3) undergo a combustion reaction, and the remaining unreacted hydrogen is heated to 900-.
11. The method of substitute natural gas production by a coal substitute natural gas production plant of claim 5, wherein: in the step S1, the reaction temperature in the entrained-flow hydrogenation gasification furnace (1) is 700-900 ℃, and the reaction pressure is 3-7 MPa.
12. The method of substitute natural gas production by a coal substitute natural gas production plant of claim 5, wherein: in the step S2, the temperature in the gas-solid separator (9) is 650-850 ℃.
13. The method of substitute natural gas production by a coal substitute natural gas production plant of claim 5, wherein: in the step S3, the reaction temperature in the circulating fluidized bed gasification furnace (24) is 800-1000 ℃, the reaction pressure is 3-7MPa, and the gas flow rate is 2-6 m/S.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4326857A (en) * | 1978-06-15 | 1982-04-27 | Director-General Of Agency Of Industrial Science And Technology | Production of a gas of a high heating value from coal |
| CN103666577A (en) * | 2013-11-19 | 2014-03-26 | 中国科学院山西煤炭化学研究所 | Entrained-flow bed gasification furnace for coal hydrogenation |
| CN203768316U (en) * | 2014-01-16 | 2014-08-13 | 新奥科技发展有限公司 | Reaction device |
| CN203794852U (en) * | 2014-03-10 | 2014-08-27 | 重庆工商大学 | Gasification coal gas cooling and dust-collecting device for dry pulverized coal entrained-flow bed |
| CN109237467A (en) * | 2018-10-10 | 2019-01-18 | 贵州新能源开发投资股份有限公司 | A kind of circulating fluidized bed boiler returning charge valve |
-
2019
- 2019-12-12 CN CN201911276272.3A patent/CN110923016A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4326857A (en) * | 1978-06-15 | 1982-04-27 | Director-General Of Agency Of Industrial Science And Technology | Production of a gas of a high heating value from coal |
| CN103666577A (en) * | 2013-11-19 | 2014-03-26 | 中国科学院山西煤炭化学研究所 | Entrained-flow bed gasification furnace for coal hydrogenation |
| CN203768316U (en) * | 2014-01-16 | 2014-08-13 | 新奥科技发展有限公司 | Reaction device |
| CN203794852U (en) * | 2014-03-10 | 2014-08-27 | 重庆工商大学 | Gasification coal gas cooling and dust-collecting device for dry pulverized coal entrained-flow bed |
| CN109237467A (en) * | 2018-10-10 | 2019-01-18 | 贵州新能源开发投资股份有限公司 | A kind of circulating fluidized bed boiler returning charge valve |
Non-Patent Citations (1)
| Title |
|---|
| 周宝欣，常焕俊主编: "《循环流化床锅炉技术问答》", 30 June 2006, 北京：中国电力出版社 * |
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