CN112694918A - Biomass pressurized fluidized bed gasification and cyclone cracking composite gasification system - Google Patents
Biomass pressurized fluidized bed gasification and cyclone cracking composite gasification system Download PDFInfo
- Publication number
- CN112694918A CN112694918A CN202110141460.6A CN202110141460A CN112694918A CN 112694918 A CN112694918 A CN 112694918A CN 202110141460 A CN202110141460 A CN 202110141460A CN 112694918 A CN112694918 A CN 112694918A
- Authority
- CN
- China
- Prior art keywords
- gasification
- cyclone
- gasifier
- fly ash
- cracking
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/80—Other features with arrangements for preheating the blast or the water vapour
-
- 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
-
- 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
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
-
- 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
-
- 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
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological origin
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Industrial Gases (AREA)
Abstract
一种生物质加压流化床气化与旋风裂解的复合气化系统，涉及生物质气化技术领域，包括气化炉、高温旋风裂解炉、热量回收设备、旋风分离器、高温过滤器、料封阀、汽包和灰斗；气化炉从下至上分别包括排渣环管、气化剂喷管、气化炉气室、分布板、飞灰返料口II、气化炉密相段、生物质进料口、飞灰返料口I、二次气化剂喷管和气化炉稀相段，所述排渣环管用于将气化炉密相段床层内的灰渣排出气化炉，所述气化剂喷管用于向气化炉密相段床层内喷入气化剂；所述高温旋风裂解炉的固体出料口与料封阀的固体进料口连通，这种生物质加压流化床气化与旋风裂解的复合气化系统能够缩短气化反应时间，气化炉气化强度获得大幅提升，并生成更多可燃成分。
A composite gasification system of biomass pressurized fluidized bed gasification and cyclone cracking relates to the technical field of biomass gasification, including gasifier, high temperature cyclone cracking furnace, heat recovery equipment, cyclone separator, high temperature filter, Material sealing valve, steam drum and ash hopper; gasifier from bottom to top respectively includes slag discharge ring pipe, gasification agent nozzle, gasifier gas chamber, distribution plate, fly ash return port II, gasifier dense phase section, biomass feed port, fly ash return port I, secondary gasification agent nozzle and gasifier dilute phase section, the slag discharge loop is used to discharge the ash and slag in the bed layer of the gasifier dense phase section The gasification furnace, the gasification agent nozzle is used to spray the gasification agent into the bed layer of the dense phase section of the gasifier; the solid discharge port of the high temperature cyclone cracking furnace is communicated with the solid feed port of the material sealing valve, This composite gasification system of biomass pressurized fluidized bed gasification and cyclone cracking can shorten the gasification reaction time, greatly improve the gasification intensity of the gasifier, and generate more combustible components.
Description
The technical field is as follows:
the invention relates to the technical field of biomass gasification, in particular to a composite gasification system of biomass pressurized fluidized bed gasification and cyclone cracking.
Background art:
because the energy structure of China mainly takes fossil energy such as coal, oil and the like as main energy, the storage capacity of fossil fuel (coal, oil, natural gas) is limited, and the environmental problem generated in the utilization process is increasingly severe, the development of clean renewable energy is urgently needed, and biomass energy which is one of the renewable energy is clean energy which can be stored and transported, and the biomass energy has the advantages of wide resource distribution and large storage capacity, so the development potential is huge.
The biomass gasification technology is a thermochemical treatment technology, and the basic principle is that solid biomass is put into a gasification furnace for incomplete combustion, and gasification agents such as oxygen or water vapor are added in the conversion process to cause the solid biomass to have partial oxidation reaction, and then the solid biomass is combusted and gasified. Because the solid biomass raw material has special physical properties, the solid biomass raw material needs to be pretreated by crushing, adding a medium and the like before entering a gasification furnace for gasification. The pretreated raw materials are combusted in a gasification furnace, the generated heat is used for maintaining pyrolysis and reduction reaction, combustible mixed gas is finally obtained, and the gas is filtered to remove tar and impurities, so that the combustible mixed gas can be used for combustion, power generation, gas production or further synthesis of chemical products.
The patent application with the application number of 201110094281.8 and the publication number of CN102206514A relates to a two-section biomass cyclone pyrolysis gasifier. The gasification furnace consists of an upper cyclone high-temperature thermal cracking gasification chamber, a lower steam spraying pyrolysis gasification chamber, a screw feeder, a biomass gas discharge pipe, a gas fuel high-speed combustor and a slag box. The gasifier can greatly reduce the content of tar in the produced biomass gas, but the high-temperature (above 1600 ℃) anaerobic smoke generated by the high-speed gas fuel combustor consumes a large amount of fuel gas generated in the biomass gasification process, namely, the gas production of unit biomass consumption is greatly reduced, and meanwhile, in order to form a strong cyclone vortex, the high-temperature smoke is sprayed into the cyclone pyrolysis gasification chamber along the cyclone tangential direction at a high speed of more than 80m/s and close to the inner wall of the cyclone pyrolysis gasification chamber, and under the operation condition, the high-temperature smoke and biomass particles carried by the high-temperature smoke can seriously erode and abrade the inner wall of the cyclone.
The invention content is as follows:
in order to solve the technical problem, the invention provides a composite gasification system for biomass pressurized fluidized bed gasification and cyclone cracking.
The invention is realized by the following technical scheme:
a composite gasification system of biomass pressurized fluidized bed gasification and cyclone cracking is characterized by comprising a gasification furnace, a high-temperature cyclone cracking furnace, heat recovery equipment, a cyclone separator, a high-temperature filter, a material sealing valve, a steam pocket and an ash bucket; the gasification furnace comprises a slag discharging ring pipe, a gasification agent spray pipe, a gasification furnace air chamber, a distribution plate, a fly ash return port II, a gasification furnace dense-phase section, a biomass feed inlet, a fly ash return port I, a secondary gasification agent spray pipe and a gasification furnace dilute-phase section from bottom to top respectively, the slag discharging ring pipe is used for discharging ash in a bed layer of the gasification furnace dense-phase section out of the gasification furnace, and the gasification agent spray pipe is used for spraying a gasification agent into the bed layer of the gasification furnace dense-phase section; the solid discharge port of the high-temperature cyclone cracking furnace is communicated with the solid feed port of the material sealing valve, the solid discharge port of the material sealing valve is communicated with the dense-phase section bed layer of the gasification furnace through a fly ash return port I, the bottom outlet of the lower conical section of the cyclone separator is communicated with the top feed port of the ash bucket, the bottom discharge port of the ash bucket is communicated with the dense-phase section bed layer of the gasification furnace through a fly ash return port II, the solid discharge port of the high-temperature filter is communicated with the dense-phase section bed layer of the gasification furnace through the fly ash return port II, the biomass feed port is positioned above the distribution plate, the secondary gasification agent nozzle is positioned above the dense-phase section bed layer of the gasification furnace, the top outlet of the gasification furnace is communicated with the crude synthesis gas inlet of the high-temperature cyclone cracking furnace, the gasification agent feed port is arranged on the opposite, the water/steam side of the heat recovery device is communicated with the steam drum; a saturated water outlet at the bottom of the steam drum is communicated with a saturated water inlet of the heat recovery device, a saturated water/steam outlet at the top of the water/steam side of the heat recovery device is communicated with a saturated water/steam inlet at the bottom of the steam drum, a saturated steam outlet at the top of the steam drum is communicated with a saturated steam inlet of the heat recovery device, and an overheated steam outlet of the heat recovery device is respectively communicated with a gasifying agent inlet of the cyclone cracking furnace and a gasifying agent inlet of a gasification furnace air chamber and a gasifying agent spray pipe of the gasification furnace; the bottom of the heat recovery equipment is communicated to a gas-solid phase inlet of the cyclone separator, and an outlet at the top of the cyclone separator is communicated with a crude synthesis gas inlet of the high-temperature filter.
In another aspect of the invention, the heat recovery device is used for partially recovering sensible heat of the high-temperature dust-containing raw synthesis gas and by-producing superheated steam.
In another aspect of the invention, the cyclone is used to further separate a portion of the solid particles in the dusty raw synthesis gas.
In another aspect of the present invention, the high temperature filter is used to further filter out the semi-coke fly ash particles in the dust-containing raw synthesis gas that cannot be separated by the cyclone separator, and the semi-coke fly ash particles filtered out by the high temperature filter fall into the bottom cone section of the high temperature filter.
In another aspect of the present invention, the filter element of the high temperature filter is a metal filter element or a ceramic filter element.
In another aspect of the invention, the height of the dense phase bed of the gasifier is adjusted by controlling the slag removal rate; a central high-temperature area is arranged in a dense-phase bed layer of the gasification furnace, a gasification agent with certain oxygen concentration is sprayed into the central high-temperature area through a gasification agent spray pipe, the central high-temperature area is maintained at a higher temperature level than the average temperature of the dense-phase bed layer, and the central high-temperature area is used for burning and gasifying semi-coke fly ash particles with lower reactivity, which are collected from a high-temperature cyclone cracking furnace, a cyclone separator and a high-temperature filter in a filtering way; semicoke fly ash particles separated by the high-temperature cyclone cracking furnace enter a dense-phase bed layer of the gasification furnace from a fly ash return port I above the distribution plate, and semicoke fly ash particles separated by the cyclone separator and the high-temperature filter are introduced into a central high-temperature area of the dense-phase bed layer of the gasification furnace from a fly ash return port II; introducing the other part of gasifying agent into the gasification furnace gas chamber for maintaining the materials in the dense phase section bed layer above the distribution plate in a stable fluidized state; the biomass feed inlet is positioned above the distribution plate and is used for introducing a biomass raw material after the raw material pretreatment is finished; the secondary gasification agent nozzle is positioned above the bed layer of the dense-phase section of the gasification furnace, and secondary gasification agent is introduced to promote the solid-gas material above the dense-phase section of the gasification furnace to further generate gasification and tar cracking reaction; gasification of solid gas components in the gasification furnace, cracking reaction of macromolecular gases such as tar and the like and sedimentation of large-particle solids continue to occur in the dilute phase section of the gasification furnace.
In another aspect of the invention, the gas-solid phase material at the top outlet of the gasification furnace enters a high-temperature cyclone cracking furnace, a strand of cracking reaction catalyst is introduced between the top outlet of the gasification furnace and the high-temperature cyclone cracking furnace, and a strand of gasifying agent is introduced at the opposite side of the gas-solid phase feed inlet of the cylinder body of the high-temperature cyclone cracking furnace, so that fly ash and catalyst solid particles in the high-temperature cyclone cracking furnace are fully mixed with the gas-solid phase containing tar gas and the gasifying agent to generate violent reaction, and the catalytic cracking reaction of hydrocarbons such as tar and methane is generated while gas-solid separation is performed; feeding the semicoke fly ash which is separated from the high-temperature cyclone cracking furnace and contains catalyst particles and is not completely reacted into a material sealing valve, communicating the material sealing valve with a fly ash return port I which is close to the upper part of a distribution plate on a dense-phase bed layer of the gasification furnace through the material sealing valve, and continuously participating in reaction in the dense-phase bed layer of the gasification furnace; a gas-solid phase outlet at the top of the high-temperature cyclone cracking furnace is connected to heat recovery equipment, and the semicoke fly ash particles separated by the cyclone separator enter an ash bucket from an outlet at the bottom of a lower conical section of the cyclone separator; the top dust-containing crude synthesis gas after gas-solid separation by the cyclone separator enters a high-temperature filter, and semi-coke fly ash in the bottom conical sections of the ash hopper and the high-temperature filter is combined and conveyed to a fly ash discharge port II of the gasification furnace through carbon dioxide/air/nitrogen pneumatic conveying gas and enters a central high-temperature area of a bed layer of a dense-phase section of the gasification furnace to participate in combustion and gasification reactions.
In another aspect of the invention, the high temperature filter introduces oxygen, oxygen-enriched air or air gas below the dust removal filter element for forming a continuous smoldering state on the dust covered on the metal or ceramic high temperature filter element to reduce the pressure drop across the filter element.
The invention has the beneficial effects that:
the material adaptability is strong, the bed height is controllable, the bed material in the bed layer can quickly heat the added biomass feed, the gasification reaction time is shortened, the gasification strength of the gasification furnace is greatly improved, and more combustible components are generated;
by adopting the spouted fluidized bed gasification technology with the circulating return material, the carbon particles which are not completely reacted can return to the dense-phase bed layer of the gasification furnace or the central high-temperature area of the dense-phase bed layer in a pneumatic conveying mode through the return feeder for further reaction, thereby improving the gasification efficiency and the fuel gas heat value, simultaneously, the system has no extra fly ash to be discharged, and effectively solving the problems of discharge and treatment of the escape fly ash in the fluidized bed gasification system;
the bottom of the dilute phase section of the gasification furnace is provided with a secondary gasification agent nozzle, and the concentration of tar in the dust-containing crude synthesis gas entering the dilute phase section of the gasification furnace can be effectively reduced by further increasing the temperature of the dilute phase section of the gasification furnace;
the tar cracking catalyst is directly added to a high-temperature pipeline between an outlet at the top of the gasification furnace and the high-temperature cyclone cracking furnace, a strong rotational flow is formed by using high-temperature cyclone, and a stream of gasifying agent is introduced into the cyclone, so that fly ash and catalyst solid in the high-temperature cyclone are fully mixed with gas-solid containing tar gas and the gasifying agent, the reaction is violent, the catalytic cracking reaction of hydrocarbons such as tar and methane is generated during gas-solid separation, the reaction time is effectively prolonged due to the internal and external reverse rotational flow generated in the cyclone, the tar content in the outlet gas of the fluidized bed can be greatly reduced, and a subsequent gas purification system is simplified; the structure of the cyclone cracking furnace is very simple;
tar in the hot gas is completely removed, so that the hot gas subjected to dry dust removal is directly utilized, pollution to pipelines and equipment caused by tar condensation is avoided, and the heat efficiency of gas utilization is correspondingly improved;
the tar produced in the biomass gasification process can be effectively converted into low molecular weight gas products such as hydrogen, carbon monoxide and the like, and the effective gas yield of unit biomass consumption is correspondingly and effectively improved.
Description of the drawings:
fig. 1 is a schematic structural diagram of an apparatus according to embodiment 1 of the present invention.
Fig. 2 is a schematic structural diagram of an apparatus in embodiment 2 of the present invention.
FIG. 3 is a schematic view of the structure of the furnace body of the gasification furnace and the division of the regions in the furnace body of the gasification furnace.
In the drawings: 1. the device comprises a gasification furnace, 2, a high-temperature cyclone cracking furnace, 3, heat recovery equipment, 4, a cyclone separator, 5, a high-temperature filter, 6, a material sealing valve, 7, a steam pocket, 8, an ash bucket, 9, oxygen/oxygen-enriched air/water vapor (gasifying agent), 10, a secondary gasifying agent, 11, slag discharging, 12, raw material biomass, 13, a cracking reaction catalyst, 14, boiler feed water, 15, tar-removed synthesis gas, 16, oxygen/oxygen-enriched air, 17, a gasification furnace dilute phase section, 18, a secondary gasifying agent nozzle, 19, a gasification furnace dense phase section, 20, a fly ash return port I, 21, a distribution plate, 22, a gasifying agent spray pipe, 23, a slag discharging ring pipe, 24, a gasification furnace air chamber, 25, a fly ash return port II, 26 and a biomass feed port.
The specific implementation mode is as follows:
the following describes the embodiments of the present invention with reference to the drawings and examples:
in the description of the present invention, it is to be understood that the description indicating the orientation or positional relationship is based on the orientation or positional relationship shown in the drawings only for the convenience of describing the present invention and simplifying the description, and does not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the scope of the present invention.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "disposed," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Example 1
A composite gasification system of biomass pressurized fluidized bed gasification and cyclone cracking comprises a gasification furnace 1, a high-temperature cyclone cracking furnace 2, a heat recovery device 3, a cyclone separator 4, a high-temperature filter 5, a material sealing valve 6, a steam drum 7 and an ash bucket 8; the gasification furnace 1 comprises a slag discharging ring pipe, a gasification agent spray pipe, a gasification furnace air chamber, a distribution plate, a fly ash return port II, a gasification furnace dense-phase section, a biomass feed inlet, a fly ash return port I, a secondary gasification agent spray pipe and a gasification furnace dilute-phase section from bottom to top respectively, the slag discharging ring pipe is used for discharging ash in a gasification furnace dense-phase section bed layer, and the gasification agent spray pipe is used for spraying a gasification agent into the gasification furnace dense-phase section bed layer; the solid discharge port of the high-temperature cyclone cracking furnace is communicated with the solid feed port of the material sealing valve, the solid discharge port of the material sealing valve is communicated with the dense-phase section bed layer of the gasification furnace through a fly ash return port I, the bottom outlet of the lower conical section of the cyclone separator is communicated with the top feed port of the ash bucket, the bottom discharge port of the ash bucket is communicated with the dense-phase section bed layer of the gasification furnace through a fly ash return port II, the solid discharge port of the high-temperature filter is communicated with the dense-phase section bed layer of the gasification furnace through the fly ash return port II, the biomass feed port is positioned above the distribution plate, the secondary gasification agent nozzle is positioned above the dense-phase section bed layer of the gasification furnace, the top outlet of the gasification furnace is communicated with the crude synthesis gas inlet of the high-temperature cyclone cracking furnace, the gasification agent feed port is arranged on the opposite, the water/steam side of the heat recovery device is communicated with the steam drum; a saturated water outlet at the bottom of the steam drum is communicated with a saturated water inlet of the heat recovery device, a saturated water/steam outlet at the top of the water/steam side of the heat recovery device is communicated with a saturated water/steam inlet at the bottom of the steam drum, a saturated steam outlet at the top of the steam drum is communicated with a saturated steam inlet of the heat recovery device, and an overheated steam outlet of the heat recovery device is respectively communicated with a gasifying agent inlet of the cyclone cracking furnace and a gasifying agent inlet of a gasification furnace air chamber and a gasifying agent spray pipe of the gasification furnace; the bottom of the heat recovery equipment is communicated to a gas-solid phase inlet of the cyclone separator, and an outlet at the top of the cyclone separator is communicated with a crude synthesis gas inlet of the high-temperature filter. The heat recovery equipment 3 is used for partially recovering sensible heat of the high-temperature dust-containing crude synthesis gas and by-producing superheated steam. The cyclone 4 serves to further separate a part of the solid particles in the dusty raw synthesis gas. The high-temperature filter 5 is used for further filtering out semicoke fly ash particles in the dust-containing crude synthesis gas which cannot be separated by the cyclone separator 4, and the semicoke fly ash particles filtered out by the high-temperature filter 5 fall into the bottom conical section of the high-temperature filter 5. And the filter element of the high-temperature filter 5 is a metal filter element or a ceramic filter element. The height of a dense-phase section bed layer of the gasification furnace is adjusted by controlling the slag discharge rate; a central high-temperature area is arranged in a dense-phase bed layer of the gasification furnace, a gasification agent with certain oxygen concentration is sprayed into the central high-temperature area through a gasification agent spray pipe, the central high-temperature area is maintained at a higher temperature level than the average temperature of the dense-phase bed layer, and the central high-temperature area is used for burning and gasifying semi-coke fly ash particles with lower reactivity, which are collected from a high-temperature cyclone cracking furnace, a cyclone separator and a high-temperature filter in a filtering way; semicoke fly ash particles separated by the high-temperature cyclone cracking furnace enter a dense-phase bed layer of the gasification furnace from a fly ash return port I above the distribution plate, and semicoke fly ash particles separated by the cyclone separator and the high-temperature filter are introduced into a central high-temperature area of the dense-phase bed layer of the gasification furnace from a fly ash return port II; introducing the other part of gasifying agent into the gasification furnace gas chamber for maintaining the materials in the dense phase section bed layer above the distribution plate in a stable fluidized state; the biomass feed inlet is positioned above the distribution plate and is used for introducing a biomass raw material after the raw material pretreatment is finished; the secondary gasification agent nozzle is positioned above the bed layer of the dense-phase section of the gasification furnace, and secondary gasification agent is introduced to promote the solid-gas material above the dense-phase section of the gasification furnace to further generate gasification and tar cracking reaction; gasification of solid gas components in the gasification furnace, cracking reaction of macromolecular gases such as tar and the like and sedimentation of large-particle solids continue to occur in the dilute phase section of the gasification furnace. The gas-solid phase material at the top outlet of the gasification furnace 1 enters a high-temperature cyclone cracking furnace 2, a cracking reaction catalyst is introduced between the top outlet of the gasification furnace 1 and the high-temperature cyclone cracking furnace 2, and a gasifying agent is introduced at the opposite side of a gas-solid phase feed inlet of a cylinder body of the high-temperature cyclone cracking furnace 2, so that fly ash and catalyst solid particles in the high-temperature cyclone cracking furnace 2 are fully mixed with gas-solid phase containing tar gas and the gasifying agent to generate violent reaction, and the catalytic cracking reaction of hydrocarbons such as tar and methane is generated while gas-solid separation is performed; the semicoke fly ash which is separated from the high-temperature cyclone cracking furnace 2 and contains catalyst particles and is not completely reacted enters a material sealing valve 6, is communicated with a fly ash return port I which is close to the upper part of a distribution plate of a dense-phase bed layer of the gasification furnace 1 through the material sealing valve 6 and enters the dense-phase bed layer of the gasification furnace 1 to continuously participate in reaction; a gas-solid phase outlet at the top of the high-temperature cyclone cracking furnace 2 is connected to a heat recovery device 3, and the semicoke fly ash particles separated by the cyclone separator 4 enter an ash bucket 8 from an outlet at the bottom of a lower conical section of the cyclone separator 4; the top dust-containing crude synthesis gas after gas-solid separation by the cyclone separator 4 enters the high-temperature filter 5, and the semicoke fly ash in the conical sections at the bottom of the ash hopper 8 and the high-temperature filter 5 is combined and conveyed to a fly ash discharge port II of the gasification furnace 1 through carbon dioxide/air/nitrogen pneumatic conveying gas, and enters the central high-temperature region of the dense-phase bed layer of the gasification furnace 1 to participate in combustion and gasification reaction.
The composite gasification system of biomass pressurized fluidized bed gasification and cyclone cracking comprises a gasification furnace 1, a high-temperature cyclone cracking furnace 2, a heat recovery device 3, a cyclone separator 4, a high-temperature filter 5, a material sealing valve 6, a steam drum 7 and an ash bucket 8.
The gasification furnace 1 is composed of a slag discharging ring pipe, a gasification agent spray pipe, a gasification furnace air chamber, a distribution plate, a fly ash discharge hole II, a gasification furnace dense-phase section, a biomass feed inlet, a fly ash discharge hole I, a secondary gasification agent spray pipe and a gasification furnace dilute-phase section from bottom to top. Ash in the dense-phase bed layer of the gasification furnace is discharged out of the gasification furnace through a slag discharge ring pipe, and the height of the dense-phase bed layer of the gasification furnace can be correspondingly adjusted by controlling the slag discharge rate; a central high-temperature area is arranged in a dense-phase bed layer of the gasification furnace, a gasification agent with certain oxygen concentration is sprayed into the central high-temperature area through a gasification agent spray pipe, the central high-temperature area is maintained at a higher temperature level than the average temperature of the dense-phase bed layer, and the central high-temperature area is used for burning and gasifying semi-coke fly ash particles with lower reactivity, which are collected from a high-temperature cyclone cracking furnace, a cyclone separator and a high-temperature filter in a filtering way; semicoke fly ash particles separated by the high-temperature cyclone cracking furnace enter a dense-phase bed layer of the gasification furnace from a fly ash return port I above the distribution plate, and semicoke fly ash particles separated by the cyclone separator and the high-temperature filter are introduced into a central high-temperature area of the dense-phase bed layer of the gasification furnace from a fly ash return port II; introducing the other part of gasifying agent into the gasification furnace gas chamber for maintaining the materials in the dense phase section bed layer above the distribution plate in a stable fluidized state; the biomass feed inlet is positioned above and near the distribution plate and is used for introducing a biomass raw material after the raw material pretreatment is finished; the secondary gasification agent nozzle is positioned near the upper part of the bed layer of the dense-phase section of the gasification furnace, and secondary gasification agent is introduced to promote the solid-gas materials above the dense-phase section of the gasification furnace to further generate gasification and tar cracking reaction; gasification of solid gas components in the gasification furnace, cracking reaction of macromolecular gases such as tar and the like and sedimentation of large-particle solids continue to occur in the dilute phase section of the gasification furnace.
The gas-solid phase material at the top outlet of the gasification furnace 1 enters a high-temperature cyclone cracking furnace 2, a cracking reaction catalyst is introduced between the top outlet of the gasification furnace 1 and the high-temperature cyclone cracking furnace 2, and a gasifying agent is introduced at the opposite side of a gas-solid phase feed inlet of a cylinder body of the high-temperature cyclone cracking furnace 2, so that fly ash and catalyst solid particles in the high-temperature cyclone cracking furnace 2 are fully mixed with gas-solid phase containing tar gas and the gasifying agent to generate violent reaction, and the catalytic cracking reaction of hydrocarbons such as tar and methane is generated while gas-solid separation is performed; the semicoke fly ash which is separated from the high-temperature cyclone cracking furnace 2 and contains catalyst particles and is not completely reacted enters a material sealing valve 6, is communicated with a fly ash return port I which is close to the upper part of a distribution plate of a dense-phase bed layer of the gasification furnace 1 through the material sealing valve 6 and enters the dense-phase bed layer of the gasification furnace 1 to continuously participate in reaction; the top gas-solid phase outlet of the high-temperature cyclone cracking furnace 2 is connected to a heat recovery device 3.
The heat recovery device 3 is used for partially recovering sensible heat of the high-temperature dust-containing raw synthesis gas and by-producing superheated steam. The water/steam side of the heat recovery device 4 is in communication with a steam drum 7; the steam drum 7 maintains the liquid level thereof by supplementing boiler feed water; the saturated water outlet at the bottom of the steam drum 7 is communicated with the saturated water inlet of the heat recovery device 4, the saturated water/steam outlet at the top of the water/steam side of the heat recovery device 4 is communicated with the saturated water/steam inlet at the bottom of the steam drum 7, the saturated steam outlet at the top of the steam drum 7 is communicated with the saturated steam inlet of the heat recovery device 4, and the superheated steam outlet of the heat recovery device 4 is respectively communicated with the gasifying agent inlet of the cyclone cracking furnace 2 and the gasifying agent inlet of the gasification furnace air chamber and the gasifying agent spray pipe of the gasification furnace 1.
The dust-containing raw synthesis gas after partial cooling of the heat recovery device 3 is communicated from the bottom of the heat recovery device 3 to a gas-solid phase inlet of the cyclone separator 4, and the cyclone separator 4 is used for further separating partial solid particles in the dust-containing raw synthesis gas. The semicoke fly ash particles separated by the cyclone separator 4 enter an ash bucket 8 from an outlet at the bottom of the lower conical section of the cyclone separator 4; the top dust-containing crude synthesis gas after gas-solid separation by the cyclone separator 4 enters a high-temperature filter 5.
The high temperature filter 5 is used to further filter out the semi-coke fly ash particles in the dust-containing raw synthesis gas which cannot be separated by the cyclone 4. The semicoke fly ash particles filtered by the high-temperature filter 5 fall into the bottom conical section of the high-temperature filter 5; the raw synthesis gas after being filtered and dedusted by the high-temperature filter 5 does not contain tar, and can be directly utilized or utilized after being further purified.
The semicoke fly ash in the bottom conical sections of the ash bucket 8 and the high-temperature filter 5 is conveyed to a fly ash discharge port II of the gasification furnace 1 through pneumatic conveying gas such as carbon dioxide/air/nitrogen and the like, and enters a central high-temperature area of a dense-phase bed layer of the gasification furnace 1 to participate in combustion and gasification reactions.
The high-temperature filter 5 can be made of a metal filter element or a ceramic filter element.
Example 2
In the embodiment, a small amount of oxygen, oxygen-enriched air or air gas is introduced below the dust removal filter element of the high-temperature filter 5 in the embodiment 1 and is used for forming a continuous smoldering state on dust covered on the metal or ceramic high-temperature filter element so as to reduce the pressure drop on two sides of the filter element.
In summary, the above-mentioned embodiments are only preferred embodiments of the present invention, and all equivalent changes and modifications made in the claims of the present invention should be covered by the claims of the present invention.
Claims (8)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110141460.6A CN112694918B (en) | 2021-02-02 | 2021-02-02 | A composite gasification system of biomass pressurized fluidized bed gasification and cyclone cracking |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110141460.6A CN112694918B (en) | 2021-02-02 | 2021-02-02 | A composite gasification system of biomass pressurized fluidized bed gasification and cyclone cracking |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112694918A true CN112694918A (en) | 2021-04-23 |
| CN112694918B CN112694918B (en) | 2025-03-18 |
Family
ID=75516502
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110141460.6A Active CN112694918B (en) | 2021-02-02 | 2021-02-02 | A composite gasification system of biomass pressurized fluidized bed gasification and cyclone cracking |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112694918B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112646609A (en) * | 2021-02-02 | 2021-04-13 | 上海浦名能源科技有限公司 | Device and method for producing hydrogen by gasifying biomass |
| CN119709271A (en) * | 2024-12-31 | 2025-03-28 | 康泰斯（上海）化学工程有限公司 | Process for converting biomass particles into synthesis gas using a pressurized bubbling fluidized bed device |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202576365U (en) * | 2012-04-01 | 2012-12-05 | 陕西华祥能源科技集团有限公司 | Fluidized bed biomass and coal together gasified device |
| CN102977927A (en) * | 2012-11-07 | 2013-03-20 | 东南大学 | Apparatus for preparing synthesis gas based on dual fluidized bed biomass gasification and preparation method thereof |
| CN109022038A (en) * | 2018-09-30 | 2018-12-18 | 安徽科达洁能股份有限公司 | A kind of biomass fluid bed equipment for gasification and its gasification process |
| US20200224110A1 (en) * | 2019-01-16 | 2020-07-16 | China University Of Petroleum (East China) | Method of biomass grading pyrolysis gasification in a circulating fluidized bed |
| CN215209270U (en) * | 2021-02-02 | 2021-12-17 | 上海浦名能源科技有限公司 | Biomass pressurized fluidized bed gasification and cyclone cracking composite gasification system |
-
2021
- 2021-02-02 CN CN202110141460.6A patent/CN112694918B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202576365U (en) * | 2012-04-01 | 2012-12-05 | 陕西华祥能源科技集团有限公司 | Fluidized bed biomass and coal together gasified device |
| CN102977927A (en) * | 2012-11-07 | 2013-03-20 | 东南大学 | Apparatus for preparing synthesis gas based on dual fluidized bed biomass gasification and preparation method thereof |
| CN109022038A (en) * | 2018-09-30 | 2018-12-18 | 安徽科达洁能股份有限公司 | A kind of biomass fluid bed equipment for gasification and its gasification process |
| US20200224110A1 (en) * | 2019-01-16 | 2020-07-16 | China University Of Petroleum (East China) | Method of biomass grading pyrolysis gasification in a circulating fluidized bed |
| CN215209270U (en) * | 2021-02-02 | 2021-12-17 | 上海浦名能源科技有限公司 | Biomass pressurized fluidized bed gasification and cyclone cracking composite gasification system |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112646609A (en) * | 2021-02-02 | 2021-04-13 | 上海浦名能源科技有限公司 | Device and method for producing hydrogen by gasifying biomass |
| CN112646609B (en) * | 2021-02-02 | 2025-03-18 | 上海浦合绿碳清洁能源科技有限公司 | A device and method for producing hydrogen by biomass gasification |
| CN119709271A (en) * | 2024-12-31 | 2025-03-28 | 康泰斯（上海）化学工程有限公司 | Process for converting biomass particles into synthesis gas using a pressurized bubbling fluidized bed device |
| CN119709271B (en) * | 2024-12-31 | 2025-09-16 | 康泰斯（上海）化学工程有限公司 | Process for converting biomass particles into synthesis gas using pressurized bubbling fluidized bed equipment |
Also Published As
| Publication number | Publication date |
|---|---|
| CN112694918B (en) | 2025-03-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101970617B (en) | Method and device for converting carbonaceous raw materials | |
| CN101982528B (en) | Gasification device for classified gasification of moving bed, method for gasifying coal and applications thereof | |
| CN108946661B (en) | Method and system for preparing hydrogen through biomass gasification | |
| CN101245264A (en) | Single-bed self-heating pyrolysis gasification combustion reactor and pyrolysis gasification combustion method | |
| CN215209270U (en) | Biomass pressurized fluidized bed gasification and cyclone cracking composite gasification system | |
| CN103468322A (en) | Method for preparing hydrogen-rich gas by gasifying water vapor of solid organic matter | |
| CN102782099A (en) | System for removing fine particulates from syngas produced by gasifier | |
| CN107760377B (en) | Fluidized bed and fixed bed combined coal catalytic gasification reaction device and method thereof | |
| CN105838451A (en) | Method for gasifying pulverized coal step by step in double beds connected in series | |
| CN101440308B (en) | Fixed bed-fluidized bed serially connected gasification method and apparatus | |
| CN201241071Y (en) | Single-bed self-heating type thermal decomposition gasification combusting reactor | |
| CN112694918B (en) | A composite gasification system of biomass pressurized fluidized bed gasification and cyclone cracking | |
| CN100410352C (en) | A gasification process and device for co-gasification of biomass and coal | |
| CN201971798U (en) | Gasifying device for graded gasification moving bed | |
| CN108085063A (en) | A kind of low tar double bed gasification process and device | |
| CN102234545B (en) | A method for producing synthesis gas by gasification of carbonaceous materials | |
| CN112646609B (en) | A device and method for producing hydrogen by biomass gasification | |
| CN110229697A (en) | A kind of method and device of coal high-temperature gasification production synthesis gas | |
| KR101896122B1 (en) | Process and System for Gasification Using Dryer Integrated with Water-Gas Shift Catalyst | |
| CN107760385B (en) | Coal gasification device combining fluidized bed and molten bed and method thereof | |
| CN109294625B (en) | Fluidized gasification pre-oxidation reactor | |
| KR20140080453A (en) | Circulating Fluidized Bed Gasifier Equipped with Heat Exchanger Therein | |
| CN108774548A (en) | A kind of high temperature air steam gasification system and the method for producing high-quality synthesis gas | |
| CN110240944B (en) | Method and device for co-production of coal gas and semi-coke by atmospheric pressure and high temperature cracking of pulverized coal | |
| CN103484180B (en) | A kind of fire coal is from the technique of the catalytic gasification preparing natural gas of heat supply and system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20240729 Address after: 201400 Building 5, 936 Guoshun Road, Nanqiao Town, Fengxian District, Shanghai Applicant after: Shanghai Puhe Green Carbon Clean Energy Technology Co.,Ltd. Country or region after: China Address before: Room 1413, 515 Hankou Road, Huangpu District, Shanghai 200001 Applicant before: Shanghai Puming Energy Technology Co.,Ltd. Country or region before: China |
|
| TA01 | Transfer of patent application right | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |