CN107083260A - A kind of double bed gasification installation and method - Google Patents
A kind of double bed gasification installation and method Download PDFInfo
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- CN107083260A CN107083260A CN201710338635.6A CN201710338635A CN107083260A CN 107083260 A CN107083260 A CN 107083260A CN 201710338635 A CN201710338635 A CN 201710338635A CN 107083260 A CN107083260 A CN 107083260A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/28—Other processes
- C10B47/30—Other processes in rotary ovens or retorts
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
- C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
- C10B49/06—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated according to the moving bed type
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
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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
- 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
- C10J3/74—Construction of shells or jackets
- C10J3/76—Water jackets; Steam boiler-jackets
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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
- 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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- 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
- C10J2300/0959—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
- C10J2300/12—Heating the gasifier
- C10J2300/1215—Heating the gasifier using synthesis gas as fuel
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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
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
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- Combustion & Propulsion (AREA)
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Abstract
The present invention relates to a kind of double bed gasification installation, including：Pyrolysis oven, gasification furnace and pyrolysis gas condensation separator, the low-quality tar that the difficulty for being pyrolyzed generation is utilized, which is rejoined, generates synthetic gas or water-gas in high-temperature gasification stove, and tar ingredients in the synthetic gas or water-gas produced by reducing, improve gas quality, the amount of pollutant in coal gas is reduced simultaneously, coal gas subsequent treatment difficulty is reduced.Simultaneously, because pyrolysis gas is after cooling liquid, the tar only liquefied out is again introduced into gasification furnace to gasify again, and the pyrolysis coal gas for the rich hydrocarbons that can not gasify is no longer participate in gasifying but is directly mixed into and mixes with the mixed gas and water-gas of generation, so as to reduce the destruction to hydrocarbons in pyrolysis coal gas, these hydrocarbon-rich materials have been transferred in mixed gas, greatly improve calorific value of gas and quality.
Description
Technical field
The invention belongs to gasification technology field, and in particular to a kind of double bed gasification installation and method.
Background technology
Double bed gasification technology is usually to be pyrolyzed solid fuel in advance, and then pyrolysis product is fed again into gasification furnace again
Gasification is produced the impurity content such as tar in synthetic gas so as to effectively reduction, improved to obtain synthetic gas or water-gas
Gas quality, and the discharge of the pollutants such as phenol water is reduced, and the calorific value of produced synthetic gas is improved, it is a kind of extremely important
Gasification technology, be especially suitable under the relatively low operating mode being difficult by of tar quality that low order pyrolysis of coal is produced, can be effectively by low product
Utilized after the gasification of matter tar.
At present, traditional double bed gasification technology is usually and the pyrolysis gas produced after pyrolysis is sent directly into gasification furnace in height
Cracking gasification again under temperature, so as to obtain the products such as the synthetic gas or water-gas that impurity is relatively low, calorific value is higher, such technical staff
Skill is simpler, and the thermal efficiency is higher, and cold gas efficiency is higher, still, but by the hydro carbons in pyrolysis gas or low boiling aromatic ring class material
The materials such as hydrogen and carbon monoxide are directly translated into Deng the higher material of calorific value, the very high organic substance of calorific value in coal gas is reduced
Content, make acquisition calorific value of gas be difficult to greatly improve.
Therefore, the calorific value such as a kind of hydro carbons that can retain in pyrolysis gas or low boiling aromatic ring class material how is designed higher
The problem of material turns into this area urgent need to resolve.
The content of the invention
In view of the deficiencies of the prior art, the present invention provides a kind of double bed gasification installation and method, the difficulty of generation will be pyrolyzed
The low-quality tar utilized is rejoined in high-temperature gasification stove, generation synthetic gas or water-gas, and is reduced and produced
Tar ingredients in raw synthetic gas or water-gas；Meanwhile, pyrolysis gas is after cooling liquid, and the tar only liquefied out is again
Gasify again in secondary entrance gasification furnace, and the pyrolysis coal gas of rich hydrocarbons is without gasifying again, but directly with generation
Mixed gas and water-gas mixing, so as to obtain mixed gas.
To solve the above problems, the technical solution adopted by the present invention is：
A kind of double bed gasification installation, it is characterised in that including：Pyrolysis oven, gasification furnace and pyrolysis gas condensation separator, its
In, the charging aperture of described pyrolysis oven is connected with feeding system, the pyrolysis oven go out semicoke mouthful and gasification furnace enter semicoke mouth
It is connected, the pyrolysis oven goes out to be pyrolyzed entering to be pyrolyzed gas port and being connected for gas port and pyrolysis gas condensation separator；
The tar mouthful that enters of the gasification furnace is connected with the hydraulic fluid port that discharges of the coke of the pyrolysis gas condensation separator, the gasification furnace
Air inlet agent mouthful is connected with the high temperature gasification agent mouthful that goes out of pyrolysis gas condensation separator, and the gasification furnace goes out gas port, pyrolysis air cooling
The gas port that goes out to be pyrolyzed of solidifying separator is connected with gas pipe net system respectively；
The low temperature gasification agent mouthful of entering of the pyrolysis gas condensation separator is connected with supply agent system pipe network system, the heat
The high temperature gasification agent mouthful of going out of condensation separator of venting one's spleen is connected with the air inlet agent mouth of gasification furnace.
Further, in addition to synthetic gas cooler, it is connected with the gasification furnace, gaspipe line system respectively, uses
The mixed gas discharged in cooling from gasification furnace.
Further, the pyrolysis oven is moving bed pyrolysis stove, and it goes out semicoke mouthful by returning charge battered leg and the gas of gasification furnace
The semicoke mouthful that enters for changing burner hearth is connected, and it enters heat carrier mouthful and is connected with the dipleg of the separator of gasification furnace.
Further, the gasification furnace is circle fluidized-bed gasification furnace, including gasification hearth and separator, the recycle stream
The returning charge for changing bed gasification furnace is realized by moving bed.
Further, the pyrolysis gas condensation separator is the cyclone separator with outer cooling jacket, and it is empty that it enters low temperature
Gas port is connected with for air system, and it goes out high temperature air mouthful and is connected with the air scoop that enters of gasification furnace.
Further, synthetic gas cooler is shell and tube water cooler, and what it entered gas port and gasification furnace goes out gas port phase
Even, the synthetic gas cooler go out gas port, pyrolysis gas condensation separator go out to be pyrolyzed gas port respectively with the coal gas
Pipe network system is connected, and its water inlet is connected with Cooling Water system, and what it went out steam port and pyrolysis gas condensation separator goes out high temperature
After gasifying agent mouthful connection, then it is connected with the air inlet agent mouthful of gasification furnace.
Further, the pyrolysis oven is revolving bed pyrolysis oven, and it enters gas port and is connected with gas pipe net system, its smoke
Gas port is connected with the air inlet agent mouthful of gasification furnace；The gasification furnace is grace gasification furnace, including gasification hearth, separator, returning charge
Device, its air inlet agent mouthful is connected with oxygen system.
Further, the cooling nozzle that enters of the pyrolysis gas condensation separator is connected with Cooling Water system.
Further, the synthetic gas cooler enter synthetic gas mouthful and the separator of gasification furnace go out gas port phase
Even, the synthetic gas cooler go out gas port, pyrolysis gas condensation separator go out to be pyrolyzed gas port respectively with gaspipe network
System be connected, its water inlet is connected with the cooling nozzle that goes out of pyrolysis gas condensation separator, the synthetic gas cooler go out steaming
After the smoke gas port of steam ports and pyrolysis oven, oxygen system are connected, then it is connected with the air inlet agent mouthful of the gasification hearth of gasification furnace.
There is provided a kind of double bed gasification process for another aspect of the present invention, it is characterised in that comprises the following steps：
Step 1：Solid fuel is added in pyrolysis oven and is pyrolyzed, semicoke and pyrolysis gas is produced, the semicoke of generation leads to
Cross semicoke passage and enter gasification furnace, the pyrolysis gas of generation enters pyrolysis gas condensation separator by pyrolysis gas passage；
Step 2：Pyrolysis gas enter in pyrolysis gas condensation separator exchanged heat with gasifying agent and be cooled into tar liquid and
Can not the liquefied Gaseous materials pyrolysis coal gas rich in hydrocarbons, the tar liquid of generation is discharged to from pyrolysis gas condensation separator
In gasification furnace, and gasifying agent is with being heated to form high temperature gasification agent after pyrolysis gas heat exchange and being drained into through passage in gasification furnace；
Step 3：Semicoke, tar, the high temperature gasification agent being discharged into gasification furnace react generation synthetic gas or water at high temperature
Coal gas；
Step 4：The high―temperature nuclei coal gas or water-gas discharged from gasification furnace directly or through after cooling with from pyrolysis gas
The pyrolysis coal gas that condensation separator goes out to be pyrolyzed gas port discharge is mixed into the mixed gas rich in hydrocarbons.
The beneficial effects of the present invention are：There is provided a kind of double bed gasification installation and method, the difficult of generation will be pyrolyzed and utilized
Low-quality tar rejoin in high-temperature gasification stove, generation synthetic gas or water-gas, and produced by reducing
Tar ingredients in synthetic gas or water-gas, improve gas quality；The amount of pollutant in coal gas is reduced simultaneously, is reduced
Coal gas subsequent treatment difficulty.Meanwhile, pyrolysis gas is after cooling liquid, and the tar only liquefied out is again introduced into weight in gasification furnace
New gasification, and the pyrolysis coal gas of rich hydrocarbons is without gasifying again, but mixed gas and water-gas directly with generation
Mixing, so as to obtain mixed gas, so as to reduce the destruction to hydrocarbons in pyrolysis coal gas, these hydrocarbon-rich materials are transferred to
In mixed gas, calorific value of gas and quality are greatly improved.
Brief description of the drawings
Fig. 1 is double bed gasification installation schematic diagram of the present invention.
Fig. 2 is moving bed pyrolysis stove double bed gasification installation schematic diagram of the present invention.
Fig. 3 is revolving bed pyrolysis oven double bed gasification installation schematic diagram of the present invention.
Wherein, 1, pyrolysis oven 2, gasification furnace 3, pyrolysis gas condensation separator 4, synthetic gas cooling gas 21, gasification furnace
Thorax 22, separator 23, material returning device, a, low-order coal b, semicoke c, pyrolysis gas d, tar e, pyrolysis coal gas f, Cryogenic air
G, high temperature air h, high―temperature nuclei coal gas i, low temperature synthetic gas j, the synthetic gas m rich in hydrogen species, steam n, gasifying agent
U, cooling water t, high-temperature water v, flue gas w, oxygen s, vapor A, solid fuel B, pyrolysis gas C, pyrolysis coal gas D, half
Burnt E, high temperature gasification agent F, tar G, low temperature gasification agent H, synthetic gas or water-gas I mixed gases.
Embodiment
In order that those skilled in the art more fully understand technical scheme, with reference to specific embodiment to this
Invention is described in further detail.
According to an aspect of the present invention, the invention provides a kind of double bed gasification installation, Fig. 1 gasifies for double bed of the present invention
Schematic device, as shown in figure 1, including：Pyrolysis oven, gasification furnace and pyrolysis gas condensation separator, wherein, described pyrolysis oven
Charging aperture is connected with feeding system, and the semicoke mouthful that goes out of the pyrolysis oven is connected with the semicoke mouthful that enters of gasification furnace, the pyrolysis oven
Go out to be pyrolyzed entering to be pyrolyzed gas port and being connected for gas port and pyrolysis gas condensation separator；The gasification furnace enters tar mouthful and the pyrolysis gas
The hydraulic fluid port that discharges of the coke of condensation separator is connected, and the air inlet agent mouthful of the gasification furnace goes out high-temperature gasification with pyrolysis gas condensation separator
Agent mouthful is connected, the gasification furnace go out gas port, pyrolysis gas condensation separator go out to be pyrolyzed gas port respectively with gas pipe net system
It is connected.
During double bed gasification installation work of the present invention, solid fuel is added in pyrolysis oven be pyrolyzed first, produce half
Burnt and pyrolysis gas, the semicoke of generation enters gasification furnace by semicoke passage, and the pyrolysis gas of generation enters heat by pyrolysis gas passage
Vent one's spleen condensation separator；Then pyrolysis gas enters in pyrolysis gas condensation separator and is exchanged heat with gasifying agent and be cooled into liquid Jiao
Oil and can not liquefied Gaseous materials rich in hydrocarbons be pyrolyzed coal gas, the tar liquid of generation is from pyrolysis gas condensation separator
It is discharged in gasification furnace, and gasifying agent is with being heated to form high temperature gasification agent after pyrolysis gas heat exchange and being drained into through passage in gasification furnace；So
Semicoke, tar, the high temperature gasification agent being discharged into afterwards in gasification furnace react generation synthetic gas or water-gas at high temperature；Finally from gas
The high―temperature nuclei coal gas or water-gas that change fire grate goes out go out pyrolyzing coal directly or through after cooling and from pyrolysis gas condensation separator
The pyrolysis coal gas of gas port discharge is mixed into the mixed gas rich in hydrocarbons.
Thus the low-quality tar that the difficulty for being pyrolyzed generation is utilized is rejoined to generate in high-temperature gasification stove and closed by the present invention
Into coal gas or water-gas, and tar ingredients in synthetic gas or water-gas produced by reducing, improve coal gas product
Matter, while reducing the amount of pollutant in coal gas, reduces coal gas subsequent treatment difficulty.Simultaneously as pyrolysis gas is through supercooling
After liquefaction, the tar only liquefied out is again introduced into gasification furnace to gasify again, and the pyrolysis for the rich hydrocarbons that can not gasify
Coal gas is no longer participate in gasifying but is directly mixed into and mixes with the mixed gas and water-gas of generation, so as to reduce to pyrolyzing coal
The destruction of hydrocarbons in gas, these hydrocarbon-rich materials have been transferred in mixed gas, greatly improve calorific value of gas and quality.
According to a particular embodiment of the invention, synthetic gas cooler is selectable device, according to the specific of the present invention
Embodiment, including synthetic gas cooler, it is connected with the gasification furnace, gaspipe line system respectively, for cooling down from gasification
The mixed gas that fire grate goes out.
According to a particular embodiment of the invention, pyrolysis oven of the invention has a multiple choices, and with the connection of other devices
Mode is not particularly limited, in the specific embodiment one of the present invention, and the pyrolysis oven is moving bed pyrolysis stove, and it goes out semicoke mouthful
It is connected by returning charge battered leg with the semicoke mouthful that enters of the gasification hearth of gasification furnace, it enters the material of heat carrier mouthful and the separator of gasification furnace
Leg is connected.
According to a particular embodiment of the invention, gasification furnace of the invention has a multiple choices, and with the connection of other devices
Mode is not particularly limited, in the specific embodiment one of the present invention, and the gasification furnace is circle fluidized-bed gasification furnace, including gas
Change burner hearth and separator, the returning charge of the circle fluidized-bed gasification furnace is realized by moving bed.
According to a particular embodiment of the invention, pyrolysis gas condensation separator of the invention has a multiple choices, and and other
The connected mode of device is not particularly limited, in the specific embodiment one of the present invention, and the pyrolysis gas condensation separator is band
There is the cyclone separator of outer cooling jacket, it enters Cryogenic air mouthful and is connected with for air system, and it goes out high temperature air mouthful and gasification
The air scoop that enters of stove is connected.
According to a particular embodiment of the invention, synthetic gas cooler of the invention has multiple choices, and is filled with other
The connected mode put is not particularly limited, in the specific embodiment one of the present invention, and synthetic gas cooler is shell and tube water cooling
Device, it enters gas port and is connected with the gas port that goes out of gasification furnace, and the go out gas port, pyrolysis gas condensation of the synthetic gas cooler divide
The gas port that goes out to be pyrolyzed from device is connected with the gas pipe net system respectively, and its water inlet is connected with Cooling Water system, and it goes out
Steam port and pyrolysis gas condensation separator go out after high temperature gasification agent mouth be connected, then are connected with the air inlet agent mouth of gasification furnace.
According to a particular embodiment of the invention, pyrolysis oven of the invention and gasification furnace have multiple choices, and are filled with other
The connected mode put is not particularly limited, in the specific embodiment two of the present invention, and the pyrolysis oven is revolving bed pyrolysis oven, its
Enter gas port with gas pipe net system to be connected, its smoke gas port is connected with the air inlet agent mouthful of gasification furnace；The gasification furnace is grace
Moral gasification furnace, including gasification hearth, separator, material returning device, its air inlet agent mouthful are connected with oxygen system.
According to a particular embodiment of the invention, the connected mode of pyrolysis gas condensation separator and other devices is not limited especially
System, in the specific embodiment two of the present invention, the pyrolysis gas condensation separator enters cooling nozzle and Cooling Water system phase
Even, cooling water is provided for pyrolysis gas condensation separator.
According to a particular embodiment of the invention, the connected mode of synthetic gas cooling gas and other devices is not limited especially
System, in the specific embodiment two of the present invention, the separator for entering synthetic gas mouthful and gasification furnace of the synthetic gas cooler
The gas port that goes out be connected, the go out gas port, pyrolysis gas condensation separator of the synthetic gas cooler go out to be pyrolyzed gas port point
It is not connected with gas pipe net system, its water inlet is connected with the cooling nozzle that goes out of pyrolysis gas condensation separator, the synthetic gas
After the smoke gas port for going out steam port and pyrolysis oven of cooler, oxygen system are connected, then enter with the gasification hearth of gasification furnace
Gasifying agent mouthful is connected.
According to an aspect of the present invention, the invention provides a kind of double bed gasification process, it is characterised in that including following
Step：
Step 1：Solid fuel is added in pyrolysis oven and is pyrolyzed, semicoke and pyrolysis gas is produced, the semicoke of generation leads to
Cross semicoke passage and enter gasification furnace, the pyrolysis gas of generation enters pyrolysis gas condensation separator by pyrolysis gas passage；
Step 2：Pyrolysis gas enter in pyrolysis gas condensation separator exchanged heat with gasifying agent and be cooled into tar liquid and
Can not the liquefied Gaseous materials pyrolysis coal gas rich in hydrocarbons, the tar liquid of generation is discharged to from pyrolysis gas condensation separator
In gasification furnace, and gasifying agent is with being heated to form high temperature gasification agent after pyrolysis gas heat exchange and being drained into through passage in gasification furnace；
Step 3：Semicoke, tar, the high temperature gasification agent being discharged into gasification furnace react generation synthetic gas or water at high temperature
Coal gas；
Step 4：The high―temperature nuclei coal gas or water-gas discharged from gasification furnace directly or through after cooling with from pyrolysis gas
The pyrolysis coal gas that condensation separator goes out to be pyrolyzed gas port discharge is mixed into the mixed gas rich in hydrocarbons.
Embodiment one
The present embodiment is elaborated using 10t/h recirculating fluidized beds-moving bed double bed low order coal gasification as specific embodiment
This patent.
Wherein, the present embodiment is using air and water vapour as gasifying agent, and the device used in the present embodiment is as shown in Fig. 2 main
Including：Pyrolysis oven 1, gasification furnace 2, pyrolysis gas condensation separator 3 and synthetic gas cooler 4.
Described pyrolysis oven 1 is moving bed pyrolysis stove, and its coal feed point is connected with coal-supply system；It goes out semicoke mouthful by returning charge
Battered leg enters semicoke mouthful with the gasification hearth 21 of gasification furnace 2 and is connected；It enters the dipleg phase of heat carrier mouthful and the separator 22 of gasification furnace 2
Even；It goes out to be pyrolyzed entering to be pyrolyzed gas port and being connected for gas port and pyrolysis gas condensation separator 3.
Described gasification furnace 2 is circle fluidized-bed gasification furnace, mainly includes gasification hearth 21 and separator 22, wherein, follow
The returning charge of ring fluidized-bed gasification furnace is realized by moving bed.Gasification furnace enters going out for tar mouthful and pyrolysis gas condensation separator 3
Tar mouthful is connected, and the air inlet agent mouthful of gasification furnace goes out high temperature air mouthful and synthetic gas cooling with pyrolysis gas condensation separator 3
The steam port that goes out of device 4 is connected, the gasification hearth 21 of gasification furnace go out gas port and the separator 22 of gasification furnace 2 enter gas port phase
Even；The air inlet of the separator 22 of gasification furnace 2 is connected with the gas port that goes out of gasification hearth 21, gasification furnace go out gas port with synthesis
The air inlet of gas cooler 4 is connected.
Described pyrolysis gas condensation separator 3 is the cyclone separator with outer cooling jacket, and it enters to be pyrolyzed gas port and heat
The gas port that goes out to be pyrolyzed of solution stove 1 is connected；Its hydraulic fluid port that discharges of the coke is connected with the tar mouthful that enters of the gasification hearth 21 of gasification furnace 2；It goes out pyrolysis
Gas port and synthetic gas cooler 4 go out gas port and gas pipe net system is connected, enter Cryogenic air mouthful and supply air system
It is connected；It goes out high temperature air mouthful and is connected with the air scoop that enters of gasification furnace 2.
Described synthetic gas cooler is shell and tube water cooler, and it goes out gas port and goes out heat with pyrolysis gas condensation separator 3
Solution gas port is connected with gas pipe net system；Its water inlet is connected with Cooling Water system；It goes out steam port and condensed with pyrolysis gas
Separator 3 go out high temperature air mouthful, the air inlet agent mouthful of gasification furnace 2 is connected.
The double bed gasification process of the present embodiment one, as shown in Fig. 2 specifically including following steps：
1) low-order coal a is added to the heat for being pyrolyzed and being produced 7t/h semicoke b and 3t/h in pyrolysis oven 1 with 10t/h
Vent one's spleen and c and discharge out of pyrolysis oven 1；
2) the semicoke b of discharge is entered in the gasification hearth 21 of gasification furnace 2 and from pyrolysis gas condensation separation out of pyrolysis oven 1
The 0.5t/h of device 3 tar d reacts generation 20000Nm at high temperature with high temperature air n together3/ h 900 DEG C of synthesis coal
Gas h, the composition and its content of synthetic gas are mainly：29.6vol.% CO, 5vol.% H2, 0.5vol.% CH4、
0.1% C2-C4 hydrocarbons, 15vol.% CO2And 49.8vol.% N2, its calorific value is 1100kcal/Nm3.Produce
Synthetic gas h is discharged into after separator 22 carries out gas solid separation half for discharging, isolating from separator 22 from gasification hearth 21
Burnt heat carrier enters pyrolysis oven 1 and used as heat carrier；
3) the pyrolysis gas c of discharge enters the Cryogenic air f with 20 DEG C in pyrolysis gas condensation separator 3 out of pyrolysis oven 1
Heat exchange be cooled into 0.5t/h temperature be 250 DEG C liquid tar d and 2.5t/h temperature be 250 DEG C can not be liquefied
Gaseous materials pyrolysis coal gas e rich in hydrocarbons is simultaneously discharged out of pyrolysis gas condensation separator 3, wherein, it is pyrolyzed the master of coal gas
It is 60vol.% H to want composition and content2, 35vol.% CH4With 5vol.% C2-C4 hydrocarbons, its density is
0.8kg/h, calorific value is 3800kcal/Nm3, become high temperature air g that temperature is 220 DEG C while Cryogenic air f is heated and discharge；
4) the tar d of discharge enters the semicoke b in gasification furnace and from pyrolysis oven 1 out of pyrolysis gas condensation separator 3
Generate synthetic gas h with gasifying agent n reactions at high temperature together；
5) after the high temperature air g of discharge is mixed with the steam m discharged from synthetic gas 4 out of pyrolysis gas condensation separator 3
Form gasifying agent n and enter and used in gasification hearth 22；
6) synthetic gas is entered after being discharged from the high―temperature nuclei coal gas h of gasification furnace 2 from the separator 22 of gasification furnace 2 cold
But in device 4 by into the low temperature synthetic gas i that temperature is 150 DEG C, then and the pyrolysis coal gas e from pyrolysis gas condensation separator 3
The mixed gas j rich in hydrocarbons is mixed into, mixed gas j main component and content are：25.8vol.% CO,
12.2vol.% H2, 5vol.% CH4, 0.7% C2-C4 hydrocarbons, 13vol.% CO2And 43.3vol.%
N2, calorific value is 1467kcal/Nm3。
By the present embodiment, the synthetic gas of acquisition from gasification furnace discharge when temperature be 900 DEG C, at these elevated temperatures, close
It has been cleaved substantially into the tar in coal gas, content is low in synthetic gas, meanwhile, it is also basic in the pyrolysis gas obtained through supercooling
Tar liquid is not contained.Therefore, tar content is relatively low in the two mixed gas being mixed into；Meanwhile, pyrolysis coal gas without
Gasification furnace participates in reaction again, the destruction to hydrocarbons in pyrolysis coal gas is reduced, after pyrolysis coal gas is mixed with synthetic gas
Mixed gas calorific value be about 1467kcal/Nm3, and the calorific value that tradition gasification is produced is general in 1000-1200kcal/Nm3Coal
Gas, therefore the calorific value of mixed gas is significantly higher than the coal gas that tradition gasifies.In addition, pyrolysis gas is after air is cooled down, its sensible heat
Being reclaimed and entered in gasification furnace by air is used for synthetic gas production, has reclaimed the sensible heat of pyrolysis gas.
Embodiment two
10t/h fluid bed-revolving bed double bed low order coal gas of the present embodiment using gasifying agent as air and water vapor mixture
Turn to specific embodiment.Wherein, the present embodiment is using oxygen-rich silicon dioxide carbon gas and water vapour as gasifying agent.
Fig. 3 is revolving bed pyrolysis oven double bed gasification installation schematic diagram of the present invention, as shown in figure 3, the double bed gas of the present embodiment
Makeup, which is put, mainly to be included：Pyrolysis oven 1, gasification furnace 2 and pyrolysis gas condensation separator 3 and synthetic gas cooler 4.
Wherein, described pyrolysis oven 1 is revolving bed pyrolysis oven, and its coal feed point is connected with coal-supply system；Its go out semicoke mouthful with
The semicoke mouthful that enters of the gasification hearth 21 of gasification furnace 2 is connected；It enters to fire gas port is connected with gas pipe net system；It goes out to be pyrolyzed gas port
Enter to be pyrolyzed gas port and be connected with pyrolysis gas condensation separator 3；Its smoke gas port is connected with the air inlet agent mouthful of gasification furnace 2.
Described gasification furnace 2 is grace gasification furnace, mainly includes gasification hearth 21 and separator 22 and material returning device 23.Gasification
The tar mouthful that enters of stove 2 is connected with the hydraulic fluid port that discharges of the coke of pyrolysis gas condensation separator 3, air inlet agent mouthful and the revolving bed heat of gasification furnace 2
Solve the exhanst gas outlet of stove 1, oxygen system with the steam port that goes out of synthetic gas cooler 4 to be connected, the gasification hearth 21 of gasification furnace 2
The gas port that enters for going out gas port with the separator 22 of gasification furnace 2 is connected；Gasification furnace goes out gas port and pyrolysis gas condensation separator 3
Go out to be pyrolyzed gas port, pyrolysis oven 1 enter gas port and be connected with gas pipe net system.
Described pyrolysis gas condensation separator 3 go out to be pyrolyzed gas port and synthetic gas cooler 4 go out gas port and coal
Gas pipe network system is connected, and enters cooling nozzle and is connected with Cooling Water system, goes out cooling nozzle and synthetic gas cooler water inlet
It is connected.
Described synthetic gas cooler 4 enter synthetic gas mouthful and the separator 22 of gasification furnace 2 go out gas port and heat
The gas port of entering of solution stove 1 is connected, and goes out gas port and is connected with the pyrolysis gas port and gas pipe net system of pyrolysis gas condensation separator 3
It is connected, water inlet is connected with the cooling water that goes out of pyrolysis gas condensation separator 3, goes out steam port and the gasification hearth 21 of gasification furnace 1
Air inlet agent mouthful, the smoke gas port of pyrolysis oven 1 are connected with oxygen system.
The double bed gasification process of the present embodiment two, as shown in figure 3, specifically including following steps：
1) burning in pyrolysis oven 1 will be passed into from the high―temperature nuclei coal gas h of gasification furnace 2 as fuel, be that pyrolysis oven is carried
Its pyrolysis oven is simultaneously warming up to 600 DEG C by heating load, and the temperature that burning is produced is discharged for 800 DEG C of flue gas v from pyrolysis oven 1, described
Flue gas is mainly carbon dioxide and water vapour.
2) low-order coal a is added to the semicoke b and 3t/h for being pyrolyzed and producing 7t/h in pyrolysis oven 1 at 600 DEG C with 10t/h
Pyrolysis gas c and discharge out of pyrolysis oven 1.
3) it is passed through from the flue gas v of the discharge of pyrolysis oven 1 after being mixed in gasification furnace 2 with oxygen w and water vapour s as gasifying agent n
Use.
4) the semicoke b of discharge is entered in the gasification hearth 21 of gasification furnace 2 and from pyrolysis gas condensation separation out of pyrolysis oven 1
The 0.5t/h of device 3 tar d together with gaseous mixture that the oxygen content that is made up of oxygen w, water vapour s and flue gas v is 80%
Agent n reacts generation 18000Nm at high temperature3/ h 900 DEG C of synthetic gas h, the composition and its content of synthesis are mainly：
5.6vol.% CO, 29vol.% H2, 0.5vol.% CH4, 0.1% C2-C4 hydrocarbons, 39vol.% CO2,
Its calorific value is 1600kcal/Nm3.Synthetic gas g, h of generation are discharged into separator 22 from gasification hearth 21 and carry out gas-solid point
Discharged from after from separator 22.
5) the pyrolysis gas c discharged out of pyrolysis oven 1 enters cold with cooling water u heat exchange in pyrolysis gas condensation separator 3
But into 0.5t/h temperature be 250 DEG C liquid tar d and 2.5t/h temperature be 250 DEG C can not it is liquefied be rich in hydro carbons
The Gaseous materials pyrolysis coal gas e of material is simultaneously discharged out of pyrolysis gas condensation separator 3.Wherein, pyrolysis coal gas e main component and
Content is 60vol.% H2, 35vol.% CH4With 5vol.% C2-C4 hydrocarbons, its density is 0.8kg/h, calorific value
For 3800kcal/Nm3.And heating becomes the high-temperature water t that temperature is 60 DEG C after cooling water heat exchange.
6) the tar d of discharge enters the semicoke b in gasification furnace 2 and from pyrolysis oven 1 out of pyrolysis gas condensation separator 3
Generate synthetic gas h with gasifying agent n reactions at high temperature together.
7) the pyrolysis coal gas e of discharge is synthesized with from the low temperature of synthetic gas cooler 4 out of pyrolysis gas condensation separator 3
Coal gas i is mixed into high heating value gas j, then by gas pipe net system for users to use.Wherein, the main component of mixed gas
And content is：4.8vol.% CO, 33.4vol.% H2, 5.5vol.% CH4, 0.8% C2-C4 hydrocarbons,
22.1vol.% CO2And 22.1vol.% N2, calorific value is 2100kcal/Nm3。
8) exchanged heat from being partly into synthetic gas cooler 4 for coal gas of high temperature h of gasification furnace 2 with high-temperature water t
And be cooled into low temperature synthetic gas e that temperature is 60 DEG C and discharge, it is 160 DEG C of steaming that the high-temperature water t after heat exchange, which becomes temperature,
Vapour s is simultaneously discharged.
9) gasifying agent n is mixed into from the steam s and oxygen w and flue gas v of synthetic gas cooler 4 to be passed through in gasification furnace 2
Use, be mixed into high heating value gas j from the low temperature synthetic gas i and pyrolysis coal gas e of synthetic gas cooler 4, and be passed through coal
Gas pipe network system is for users to use.
By the present embodiment, it in the same manner as in Example 1, can both make in coal gas that tar content is very low, can reduce in coal gas again
The destruction of hydrocarbons, can greatly improve calorific value of gas.
A kind of double bed gasification installation provided by the present invention is described in detail with method above, it is used herein
Embodiment is set forth to the principle and embodiment of the application, and the explanation of above example is only intended to help and understands this Shen
Method and its core concept please；Simultaneously for those of ordinary skill in the art, according to the thought of the application, specific real
Apply and will change in mode and application, in summary, this specification content should not be construed as the limit to the application
System.
Claims (10)
1. a kind of double bed gasification installation, it is characterised in that including：Pyrolysis oven, gasification furnace and pyrolysis gas condensation separator, wherein,
The charging aperture of described pyrolysis oven is connected with feeding system, the pyrolysis oven go out semicoke mouthful and gasification furnace enter semicoke mouth
It is connected, the pyrolysis oven goes out to be pyrolyzed entering to be pyrolyzed gas port and being connected for gas port and pyrolysis gas condensation separator；
The tar mouthful that enters of the gasification furnace is connected with the hydraulic fluid port that discharges of the coke of the pyrolysis gas condensation separator, the air inlet of the gasification furnace
Agent mouthful is connected with the high temperature gasification agent mouthful that goes out of pyrolysis gas condensation separator, and the gasification furnace goes out gas port, pyrolysis gas condensation point
The gas port that goes out to be pyrolyzed from device is connected with gas pipe net system respectively；
The low temperature gasification agent mouthful of entering of the pyrolysis gas condensation separator is connected with supply agent system pipe network system, the pyrolysis gas
The high temperature gasification agent mouthful that goes out of condensation separator is connected with the air inlet agent mouthful of gasification furnace.
2. double bed gasification installation according to claim 1, it is characterised in that also including synthetic gas cooler, it is distinguished
It is connected with the gasification furnace, gaspipe line system, for cooling down the mixed gas discharged from gasification furnace.
3. double bed gasification installation according to claim 1, it is characterised in that the pyrolysis oven is moving bed pyrolysis stove, its
Go out semicoke mouthful by returning charge battered leg with the semicoke mouthful that enters of the gasification hearth of gasification furnace to be connected, it enters point of heat carrier mouthful and gasification furnace
Dipleg from device is connected.
4. double bed gasification installation according to claim 1, it is characterised in that the gasification furnace gasifies for recirculating fluidized bed
Stove, including gasification hearth and separator, the returning charge of the circle fluidized-bed gasification furnace are realized by moving bed.
5. double bed gasification installation according to claim 1, it is characterised in that the pyrolysis gas condensation separator is with outer
The cyclone separator of cooling jacket, it enters Cryogenic air mouthful and is connected with for air system, and it goes out high temperature air mouthful and gasification furnace
Enter air scoop to be connected.
6. double bed gasification installation according to claim 2, it is characterised in that synthetic gas cooler is shell and tube water cooling
Device, it enters gas port and is connected with the gas port that goes out of gasification furnace, and the go out gas port, pyrolysis gas condensation of the synthetic gas cooler divide
The gas port that goes out to be pyrolyzed from device is connected with the gas pipe net system respectively, and its water inlet is connected with Cooling Water system, and it goes out
Steam port and pyrolysis gas condensation separator go out after high temperature gasification agent mouth be connected, then are connected with the air inlet agent mouth of gasification furnace.
7. double bed gasification installation according to claim 1, it is characterised in that the pyrolysis oven is revolving bed pyrolysis oven, its
Enter gas port with gas pipe net system to be connected, its smoke gas port is connected with the air inlet agent mouthful of gasification furnace；The gasification furnace is grace
Moral gasification furnace, including gasification hearth, separator, material returning device, its air inlet agent mouthful are connected with oxygen system.
8. double bed gasification installation according to claim 1, it is characterised in that the pyrolysis gas condensation separator enters cooling
The mouth of a river is connected with Cooling Water system.
9. double bed gasification installation according to claim 2, it is characterised in that the synthetic gas cooler enters to synthesize coal
Gas port is connected with the gas port that goes out of the separator of gasification furnace, and the go out gas port, pyrolysis gas condensation of the synthetic gas cooler divide
The gas port that goes out to be pyrolyzed from device is connected with gas pipe net system respectively, and its water inlet goes out cooling water with pyrolysis gas condensation separator
Mouthful be connected, after the smoke gas port for going out steam port and pyrolysis oven of the synthetic gas cooler, oxygen system are connected, then with gas
The air inlet agent mouthful for changing the gasification hearth of stove is connected.
10. one kind utilizes the method for any described double bed gasification installation of claim 1 ~ 9, it is characterised in that including following step
Suddenly：
Step 1：Solid fuel is added in pyrolysis oven and is pyrolyzed, semicoke and pyrolysis gas is produced, the semicoke of generation passes through half
Burnt passage enters gasification furnace, and the pyrolysis gas of generation enters pyrolysis gas condensation separator by pyrolysis gas passage；
Step 2：Pyrolysis gas, which is entered in pyrolysis gas condensation separator, to exchange heat with gasifying agent and is cooled into tar liquid and can not
The liquefied Gaseous materials pyrolysis coal gas rich in hydrocarbons, the tar liquid of generation is discharged to gasification from pyrolysis gas condensation separator
In stove, and gasifying agent is with being heated to form high temperature gasification agent after pyrolysis gas heat exchange and being drained into through passage in gasification furnace；
Step 3：Semicoke, tar, the high temperature gasification agent being discharged into gasification furnace react generation synthetic gas or water-gas at high temperature；
Step 4：The high―temperature nuclei coal gas or water-gas discharged from gasification furnace are condensed directly or through after cooling and from pyrolysis gas
The pyrolysis coal gas that separator goes out to be pyrolyzed gas port discharge is mixed into the mixed gas rich in hydrocarbons.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107474879A (en) * | 2017-09-07 | 2017-12-15 | 北京神雾电力科技有限公司 | For fine coal fast pyrogenation and the system and method for gasification |
| CN107502388A (en) * | 2017-09-11 | 2017-12-22 | 哈尔滨工业大学 | Two sections of low temperature gasification device and methods based on low order fuel autocatalysis |
| CN109852431A (en) * | 2019-03-06 | 2019-06-07 | 中聚信海洋工程装备有限公司 | A kind of ciculation fluidized double bed heating gas station and its gas-made technology |
| CN110699126A (en) * | 2019-11-05 | 2020-01-17 | 西安热工研究院有限公司 | Double-bed pyrolysis gasification device and method for municipal solid waste |
| CN113061472A (en) * | 2021-04-22 | 2021-07-02 | 南京年达炉业科技有限公司 | Biomass pyrolysis gas treatment device and method |
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2017
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107474879A (en) * | 2017-09-07 | 2017-12-15 | 北京神雾电力科技有限公司 | For fine coal fast pyrogenation and the system and method for gasification |
| CN107502388A (en) * | 2017-09-11 | 2017-12-22 | 哈尔滨工业大学 | Two sections of low temperature gasification device and methods based on low order fuel autocatalysis |
| CN107502388B (en) * | 2017-09-11 | 2020-07-07 | 哈尔滨工业大学 | Two-stage low-temperature gasification device and method based on low-order fuel autocatalysis |
| CN109852431A (en) * | 2019-03-06 | 2019-06-07 | 中聚信海洋工程装备有限公司 | A kind of ciculation fluidized double bed heating gas station and its gas-made technology |
| CN109852431B (en) * | 2019-03-06 | 2020-11-06 | 中聚信海洋工程装备有限公司 | Circulating fluidized double-bed hot gas station and gas making process thereof |
| CN110699126A (en) * | 2019-11-05 | 2020-01-17 | 西安热工研究院有限公司 | Double-bed pyrolysis gasification device and method for municipal solid waste |
| CN113061472A (en) * | 2021-04-22 | 2021-07-02 | 南京年达炉业科技有限公司 | Biomass pyrolysis gas treatment device and method |
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