CN114774169B - Gasification device, gasification method, and thermochemical reaction device - Google Patents
Gasification device, gasification method, and thermochemical reaction device Download PDFInfo
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- CN114774169B CN114774169B CN202210454699.3A CN202210454699A CN114774169B CN 114774169 B CN114774169 B CN 114774169B CN 202210454699 A CN202210454699 A CN 202210454699A CN 114774169 B CN114774169 B CN 114774169B
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- 238000002309 gasification Methods 0.000 title claims abstract description 278
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 147
- 238000000034 method Methods 0.000 title claims abstract description 28
- 239000000463 material Substances 0.000 claims abstract description 146
- 239000002994 raw material Substances 0.000 claims abstract description 66
- 238000000926 separation method Methods 0.000 claims description 117
- 239000003795 chemical substances by application Substances 0.000 claims description 83
- 239000007787 solid Substances 0.000 claims description 62
- 239000007790 solid phase Substances 0.000 claims description 62
- 239000002245 particle Substances 0.000 claims description 51
- 239000007789 gas Substances 0.000 claims description 33
- 239000012071 phase Substances 0.000 claims description 24
- 230000008520 organization Effects 0.000 claims description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 13
- 229910052760 oxygen Inorganic materials 0.000 claims description 13
- 239000001301 oxygen Substances 0.000 claims description 13
- 238000009826 distribution Methods 0.000 claims description 7
- 238000004891 communication Methods 0.000 claims description 6
- 230000005587 bubbling Effects 0.000 claims description 5
- 230000008569 process Effects 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 238000002347 injection Methods 0.000 claims description 3
- 239000007924 injection Substances 0.000 claims description 3
- 238000005507 spraying Methods 0.000 claims description 2
- 238000007664 blowing Methods 0.000 claims 2
- 239000010881 fly ash Substances 0.000 description 45
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 16
- 229910052799 carbon Inorganic materials 0.000 description 15
- 239000003245 coal Substances 0.000 description 15
- 238000002485 combustion reaction Methods 0.000 description 15
- 239000010419 fine particle Substances 0.000 description 13
- 239000002956 ash Substances 0.000 description 10
- 239000011343 solid material Substances 0.000 description 10
- 239000002893 slag Substances 0.000 description 9
- 230000009471 action Effects 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 238000006555 catalytic reaction Methods 0.000 description 6
- 230000009257 reactivity Effects 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 230000005484 gravity Effects 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 230000002776 aggregation Effects 0.000 description 3
- 238000004220 aggregation Methods 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 239000011362 coarse particle Substances 0.000 description 3
- 238000005243 fluidization Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000002844 melting Methods 0.000 description 3
- 230000008018 melting Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- RNFJDJUURJAICM-UHFFFAOYSA-N 2,2,4,4,6,6-hexaphenoxy-1,3,5-triaza-2$l^{5},4$l^{5},6$l^{5}-triphosphacyclohexa-1,3,5-triene Chemical compound N=1P(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP=1(OC=1C=CC=CC=1)OC1=CC=CC=C1 RNFJDJUURJAICM-UHFFFAOYSA-N 0.000 description 2
- 239000003570 air Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000003063 flame retardant Substances 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000010866 blackwater Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000012768 molten material Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
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- 230000007704 transition Effects 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
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
- C10J3/72—Other features
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a gasification device, a gasification method and a thermochemical reaction device. Wherein, the lifting section is provided with a first gasification raw material inlet and a first gasification agent inlet; the descending section is provided with a descending section material inlet which is used for introducing a second gasifying agent, and the bottom of the descending section is connected with the top of the lifting section; the lifting section and the descending section form a gasification furnace hearth; the hearth outlet is arranged at the joint of the lifting section and the descending section.
Description
Technical Field
The invention relates to the technical field of gasification, in particular to a gasification device, a gasification method and a thermochemical reaction device.
Background
The existing thermochemical reaction device has the problems of low burnout rate and low combustion efficiency when treating the flame-retardant materials; the method of water chilling is also commonly adopted in solid melting treatment, so that a large amount of black water needs to be treated, and serious environmental treatment pressure is brought; single-reaction catalysis is generally adopted in catalytic reaction, so that the catalytic reaction process flow is long, the number of reaction devices is large, and waste heat cannot be effectively applied to the reaction, thereby bringing the problems of low system efficiency, low thermal efficiency and the like.
Coal gasification is a typical thermochemical reaction, is one of core technologies of clean and efficient utilization technologies of coal, and is the basis for developing coal chemical process industries such as coal-based chemicals, coal-based clean raw materials, industrial fuel gas, poly-generation systems and the like.
The current coal gasification technology of raw materials can be divided into the following modes according to gas-solid flow: fixed bed gasification techniques, fluidized bed gasification techniques, and entrained flow gasification techniques. The fluidized bed coal gasification technology can utilize crushed coal with the diameter of 0-10 mm, does not need a complex coal preparation system, and has low coal preparation cost; the gasification strength is large and is generally 2-3 times of that of a fixed bed; air may be used as the gasifying agent; the raw gas has high outlet temperature and almost no tar and phenols. Compared with the traditional fluidized bed coal gasification technology, the circulating fluidized bed coal gasification technology developed in recent years has the characteristics of high circulation rate, higher gasification strength, more sufficient gas-solid mixing, more uniform reaction temperature and the like, so that the single-furnace gasification gauge is larger, and the adaptability to coal types is stronger. However, the method has the technical problems of large fly ash quantity, high carbon content and the like.
Aiming at the technical problems, for example, two-stage or multi-stage cyclone separators can be used for improving the gas-solid separation efficiency in series, so that the fly ash amount is reduced. In practice, however, the furnace gasification temperature is low enough to gasify the returned fly ash, which is affected by the axial and temperature distribution of the furnace ash concentration, but only to increase the residence time of the fly ash in the system and to break the fly ash into finer materials, so that the cyclone cannot capture them.
Further, in order to solve the problem that the returned fly ash cannot react rapidly, the fly ash trapped by the secondary separator may be gasified at a high temperature by means of melt gasification, for example, the fly ash is trapped by the secondary gas-solid separator, and then gasified at a high temperature by means of entrained flow melt gasification, and the generated liquid slag and high temperature gas are introduced into the middle lower part of the circulating fluidized bed. Because the concentration of the lower particles in the circulating fluidized bed is higher and the ash content is high, the problems of slag bonding and over-temperature are easily caused when liquid slag is introduced, and the fly ash trapped by the second-stage gas-solid separator has small particle size, light weight and small amount and cannot stably enter the entrained flow bed to carry out melt gasification, the novel problem of unstable operation of the circulating fluidized bed is brought.
In summary, in the existing coal gasification technology, the technical problems of large fly ash amount, high fly ash carbon content and the like exist, the existing technical means of series connection of two-stage or multi-stage separators cannot well solve the problems of large fly ash amount and high carbon content, and the problems of slag bonding and over-temperature caused by direct feeding of slag into the bottom of a hearth can not be realized by performing entrained flow melt gasification treatment on the fly ash, although the fly ash amount and the fly ash carbon content can be reduced.
Disclosure of Invention
In view of the above, the present invention provides a gasification device, gasification method and thermochemical reaction device to at least partially solve the above technical problems.
In one aspect, the invention provides a gasification apparatus comprising a lifting section, a lowering section, and a furnace outlet.
A lifting section provided with a first gasification raw material inlet and a first gasification agent inlet;
the descending section is provided with a descending section material inlet which is used for introducing a second gasifying agent, and the bottom of the descending section is connected with the top of the lifting section; the lifting section and the descending section form a gasification furnace hearth;
the hearth outlet is arranged at the joint of the lifting section and the descending section.
According to an embodiment of the invention, the downleg feed inlet is further for introducing a second gasification feedstock.
According to an embodiment of the invention, the downer feed inlet is formed by a second gasifying agent inlet and a second gasifying raw material inlet.
According to an embodiment of the invention, the second gasifying agent inlet is arranged around the second gasifying raw material inlet.
According to an embodiment of the invention, the second gasifying agent inlets are provided in plurality, and the plurality of second gasifying agent inlets are arranged in a circumferential array distribution form with the second gasifying raw material inlet as a center.
According to an embodiment of the invention, the second gasifying agent inlet and the second gasifying raw material inlet are arranged as coaxial channels, wherein the second gasifying raw material inlet is a central channel and the second gasifying agent inlet is an annular channel surrounding the second gasifying raw material inlet.
According to an embodiment of the invention, the material inlet of the drop leg is arranged at the top end or at the upper side of the drop leg.
According to an embodiment of the invention, the device further comprises a separation device.
The separation device comprises a first inlet, a first material outlet and a second material outlet, wherein the first inlet is communicated with the hearth outlet;
the lifting section is also provided with a first material returning opening which is communicated with the first material outlet; the descending section is also provided with a second material returning opening which is communicated with the second material outlet.
According to an embodiment of the invention, the separation device comprises a first separation device and a second separation device.
The first separation device comprises a first inlet, a first solid phase outlet and a first gas phase outlet, wherein the first solid phase outlet and the first material outlet are of the same structure;
the second separation device comprises a second inlet, a second solid phase outlet and a second gas phase outlet, wherein the second inlet is communicated with the first gas phase outlet, and the second solid phase outlet and the second material outlet are of the same structure.
According to an embodiment of the invention, wherein the separation device further comprises a third separation device comprising a third inlet, a third solid phase outlet and a third gas phase outlet, wherein the third inlet and the second gas phase outlet are in communication, wherein the third solid phase outlet is in communication with the descending section.
According to an embodiment of the invention, wherein the third solid phase outlet communicates with the second return opening in the descending section.
According to an embodiment of the present invention, the first and second return devices are further included.
The first solid phase outlet is communicated with the first material returning opening through the first material returning device; and/or
The second solid phase outlet is communicated with the second returning opening through the second returning device.
According to the embodiment of the invention, the gas-solid separation efficiency of the first separation device is lower than that of the second separation device.
According to an embodiment of the invention, wherein:
the gas-solid separation efficiency of the first separation device is 50% -90%;
the gas-solid separation efficiency of the second separation device is 98% -100%;
The numerical range of the stress-resistant pressure difference of the second separation device is as follows: and is more than or equal to 2kPa.
According to an embodiment of the invention, the material inlet of the descending section and the second return opening share the same inlet structure.
According to an embodiment of the invention, the lifting section is a fluidized bed or a bubbling bed or a circulating fluidized bed, and the descending section is an entrained flow bed.
Another aspect of the invention provides a gasification process comprising:
introducing the first gasification raw material and the first gasifying agent into a lifting section in a hearth of the gasification furnace, and introducing the second gasifying agent into a descending section in the hearth of the gasification furnace, so that the first gasification raw material, the first gasifying agent and the second gasifying agent perform gasification reaction in the hearth of the gasification furnace, and the lifting section forms a first gasification reaction zone and the descending section forms a second gasification reaction zone;
the temperature of the second gasification reaction zone is higher than that of the first gasification reaction zone, the bottom of the descending section is connected with the top of the lifting section, and a hearth outlet is arranged at the connection part of the lifting section and the descending section.
According to an embodiment of the invention, wherein:
The temperature range of the second gasification reaction zone is: 950-preset ash flow temperature FT;
The temperature range of the first gasification reaction zone is: 750-pre-ash softening temperature ST-150 ℃.
According to an embodiment of the present invention, the method further includes:
The second gasification feedstock is passed to a downleg such that the second gasification feedstock and the second gasifying agent undergo a gasification reaction in the downleg.
According to an embodiment of the invention, wherein:
The second gasification raw material and/or the second gasifying agent are introduced into the core area of the high-temperature reaction of the descending section after being accelerated by the jet flow.
According to an embodiment of the invention, wherein:
The average residence time of the second gasification raw material and/or the second gasification agent in the second gasification reaction zone is 1 to 5s.
According to an embodiment of the present invention, the method further includes:
discharging a product of gasification reaction in a hearth of the gasification furnace through a hearth outlet, and introducing the product into a separation device for gas-solid separation to generate a first material and a second material, wherein the particle size of the first material and the particle size of the second material are larger than each other;
introducing the first material into the lifting section;
the second material is passed to the drop section.
According to an embodiment of the invention, wherein:
the material flow direction of the second gasification reaction zone is opposite to the material flow direction of the first gasification reaction zone.
According to an embodiment of the invention, wherein:
The oxygen concentration of the first gasifying agent is 21% -50%;
the oxygen concentration of the second gasifying agent is 21-100%.
In yet another aspect, the invention provides a solid material thermochemical reaction device comprising:
a lifting section provided with a first solid material inlet and a first gas inlet;
The descending section is provided with a descending section material inlet which is used for introducing second gas, and the bottom of the descending section is connected with the top of the lifting section; the lifting section and the descending section form a thermochemical reaction area;
The outlet of the reaction zone is arranged at the joint of the lifting section and the descending section.
According to an embodiment of the invention, the drop leg feed inlet may also be used for feeding a second solid material.
According to the embodiment of the invention, in the hearth, the gasification agent and the raw materials are introduced to automatically form the circulation of materials in the hearth, and under the action of gravity, the larger particle materials sink to the lifting section, and the smaller particle materials rise to the descending section. By constructing relatively independent reaction areas in the hearth of the gasification furnace, gasification reaction of the hard-to-react materials such as gasification fly ash is realized, and the efficiency of the gasification furnace is improved. A descending section material inlet is additionally arranged on the descending section, and gasifying agent is sprayed into the descending section of the hearth of the gasification furnace, so that gasification combustion reaction occurs to generate a large amount of heat, a local high-temperature area is formed on the descending section, and the temperature of the descending section is higher than that of the lifting section. By constructing an independent local high-temperature region at the top of the hearth, high-temperature reaction conditions are conveniently provided for fine particle solid particles with poor reactivity, the high temperature can promote the gasification of the fly ash, and the carbon conversion rate of the fine particle fly ash can be improved.
Drawings
FIG. 1 is a system configuration diagram of a gasification apparatus according to an embodiment of the present invention;
FIG. 2 is a system configuration diagram of a gasification apparatus according to another embodiment of the present invention;
FIG. 3A is a schematic illustration of an arrangement of a second gasifying agent inlet and a second gasifying feed inlet in accordance with an embodiment of the present invention;
FIG. 3B is a schematic illustration of an arrangement of a second gasifying agent inlet and a second gasifying feed inlet in accordance with another embodiment of the present invention;
FIG. 3C is a schematic illustration of an arrangement of a second gasifying agent inlet and a second gasifying feed inlet in accordance with yet another embodiment of the present invention.
Reference numerals illustrate:
1. A gasification furnace hearth; 11. a descent section; 12. a lifting section; 13. a furnace outlet; 14. a first return port; 15. a second return port; 2. a first separation device; 3. a second separation device; 4. a gasification reaction organization device;
F. A first vaporized feedstock; g1, a first gasifying agent; g2, a second gasifying agent; s2, a second gasification raw material; p, gasifying products; s, fly ash.
Detailed Description
The present invention will be further described in detail below with reference to specific embodiments and with reference to the accompanying drawings, in order to make the objects, technical solutions and advantages of the present invention more apparent.
In one aspect, the invention provides a gasification apparatus comprising a lifting section, a lowering section, and a furnace outlet.
A lift section provided with a first gasifying raw material inlet and a first gasifying agent inlet;
the descending section is provided with a descending section material inlet which is used for introducing a second gasifying agent, and the bottom of the descending section is connected with the top of the lifting section; the lifting section and the descending section form a gasification furnace hearth;
the hearth outlet is arranged at the joint of the lifting section and the descending section.
FIG. 1 is a system configuration diagram of a gasification apparatus according to an embodiment of the present invention.
The gasification apparatus according to the embodiment of the present invention will be described below with reference to fig. 1.
As shown in fig. 1, the gasification apparatus includes a gasification furnace hearth 1. Wherein the gasifier hearth 1 provides a gasification reaction zone. The furnace chamber of the gasification furnace 1 is divided into an upper descending section 11 and a lower lifting section 12, wherein the lower lifting section 12 can be a fluidized bed, a bubbling bed, a circulating fluidized bed and the like. A furnace outlet 13 is provided between the lifting section 12 and the lowering section 11.
The bottom of the descending section 11 is connected with the top of the lifting section 12, the height ratio range of the lifting section 12 to the descending section 11 is 2-5 times, the hearth outlet 13 is positioned at the middle upper part of the hearth, and the junction of the lifting section 12 and the descending section 11 is arranged.
The bottom of the lifting section 12 is provided with a first gasifying agent inlet for introducing a first gasifying agent G1 into the hearth of the gasification furnace; the middle lower part of the lifting section 12 is provided with a first gasification raw material inlet for introducing a first gasification raw material F into a gasification furnace hearth, wherein the gasification raw material is a solid raw material, such as coal, semicoke, gasification carbon residue and the like.
The upper descending section 11 and the lower lifting section 12 are spaces with the inner parts being directly communicated, namely, two reaction areas are actually formed into a whole reaction area, and the two reaction areas are naturally formed according to different flow states of materials in a hearth of the gasification furnace.
Because the concentration of the material particles in the lower space of the hearth of the gasification furnace is higher, the back mixing degree is higher under the action of gravity, and the material particles are in a fluidization (bubbling, fluidization and circulating fluidization) state, and a first gasification reaction zone is formed in the lifting section 12; the materials in the upper space of the hearth of the gasification furnace are in a gas-solid homodromous motion state, the back mixing degree is lower, the concentration of the particles of the materials is lower, and the descending section 11 forms a second gasification reaction zone. The gases and the solid particles which are not fully reacted and are produced in the descending section 11 and the lifting section 12 are discharged through the furnace outlet 13 of the furnace.
According to an embodiment of the invention, the drop leg 11 is provided with a drop leg feed inlet for introducing the second gasifying agent G2.
According to the embodiment of the invention, the material circulation in the hearth can be automatically formed by introducing gasifying agent and raw materials, and under the action of gravity, the larger granular material is positioned in the lifting section 12, and the smaller granular material is lifted to the descending section 11. By constructing relatively independent reaction areas in the hearth of the gasification furnace, gasification reaction of the hard-to-react materials such as gasification fly ash is realized, and the efficiency of the gasification furnace is improved. Specifically, the gasification furnace is divided into an upper region and a lower region, and the partition between the lower lifting section 12 and the upper descending section 11 is realized through the hearth outlet 13 of the gasification furnace arranged on the side wall surface of the gasification furnace, wherein the descending section 11 can be used for carrying out gasification combustion reaction on fine solid particles which are difficult to gasify. Furthermore, a descending section material inlet is additionally arranged on the descending section 11, and gasifying agent is sprayed into the descending section 11 of the hearth of the gasification furnace, so that gasification combustion reaction occurs to generate a large amount of heat, a local high-temperature area is formed in the descending section 11, and the temperature of the descending section 11 is higher than that of the lifting section 12. By constructing an independent local high-temperature zone at the top of the hearth, the gasification temperature of the local high-temperature zone can be conveniently and maximally increased to FT (ash flow temperature), high-temperature reaction conditions are provided for fine particle solid particles with poor reactivity, the high temperature can promote the gasification of the fly ash, and the carbon conversion rate of the fine particle fly ash can be improved. The fly ash with different particle sizes is differentially and graded for use through the descending section 11 and the lifting section 12, so that the fly ash with different particle sizes is ensured to be subjected to tissue reaction respectively in a proper temperature range and a raw material particle size range, gasification reaction grading and heat aggregation are realized, and the fly ash carbon conversion rate of the whole system is improved.
According to the embodiment of the invention, a low-temperature reaction area with relatively low temperature and gas-solid upward flow is constructed in the lifting section 12, a high-temperature reaction area with high temperature and gas-solid downward flow is constructed in the descending section 11, and strong mass transfer, heat transfer and reaction among gas, gas-solid and solid are formed at the joint of the lifting section and the descending section. The reaction device can be applied to the step combustion of flame-retardant materials, realizes the combustion of the materials and the aggregation of combustion heat, and improves the combustion efficiency; the method can also be applied to solid melting treatment, and can be used for realizing chilling, crushing and waste heat recovery of molten materials by utilizing the reaction temperature and flow difference of a lifting section and a descending section, so that the heat efficiency and the treatment efficiency of the system are improved; the catalyst can also be applied to catalytic reaction, and the reaction temperature and the material particle size difference of the lifting section and the descending section are utilized to meet the temperature requirements of different catalysts in the chemical reaction process, so that the integration of catalytic reaction is realized, and the catalytic conversion efficiency is improved.
According to embodiments of the invention, the downleg feed inlet may also be used to feed the second gasification feedstock S2, and the downleg feed inlet may include a second gasification agent inlet and a second gasification feedstock inlet. The second gasifying agent inlet and the second gasifying raw material inlet may be integrated or separately provided, and together constitute the gasification reaction organization apparatus 4.
For example, the downer feed inlet may be formed by a collection of a second gasifying agent inlet and a second gasifying feed inlet to form the gasification reaction organizing apparatus 4.
The gasification reaction organization apparatus 4 is communicated with the descending section 11. The second gasification raw material inlet of the gasification reaction organization apparatus 4 is used for injecting the second gasification raw material S2 into the descending section 11. The second gasifying agent inlet of the gasifying reaction organizing device 4 is used for feeding the second gasifying agent G2 into the descending section 11. In a preferred technical scheme, the second gasification raw material S2 and the second gasifying agent G2 generate gasification combustion reaction in the descending section 11, and the temperature of the descending section 11 is further higher than the temperature of the lifting section 12 through gasification combustion of raw material tissues, so that the gasification combustion reaction is further enhanced, and the carbon conversion rate is improved.
According to an embodiment of the invention the position of the drop leg material inlet is arranged at the top or upper side of the drop leg 11.
According to embodiments of the present invention, a second gasifying agent inlet may be provided around the second gasifying feed inlet to facilitate a more uniform blending of gasifying agent and feed, allowing a more complete gasification combustion reaction to occur to generate a significant amount of heat, thereby creating a localized high temperature zone in the downleg 11.
Fig. 3A, 3B, and 3C are schematic views of an arrangement of a second gasifying agent inlet and a second gasifying raw material inlet according to an embodiment of the present invention.
As shown in fig. 3A, for example, the second gasifying agent inlet and the second gasifying raw material inlet may be provided as coaxial channels, wherein the second gasifying raw material inlet is a central channel, and the second gasifying agent inlet is an annular channel surrounding the second gasifying raw material inlet.
As shown in fig. 3B, for example, a plurality of second gasifying agent inlets may be provided, and the plurality of second gasifying agent inlets may be arranged in a circumferential array distribution with the second gasifying material inlet as a center. An included angle alpha is formed between the center line of the second gasifying agent inlet and the center line of the second gasifying raw material inlet, and the range of the included angle alpha is 1-45 degrees.
As shown in fig. 3C, for example, the second gasifying agent inlet may be provided on the side wall of the upper part of the gasification reaction tissue apparatus 4, the distance between the center line of the second gasifying agent inlet and the top of the gasification reaction tissue apparatus 4 is h, the length of h is in the range of < 1/3r, and r is the diameter of the gasification reaction tissue apparatus 4.
According to the embodiment of the present invention, when the second gasifying agent inlet and the second gasifying raw material inlet are integrally provided, the gasification reaction organizing device 4 may be a nozzle, may be a cold burner or a hot burner, and is used for better organizing the gasification combustion reaction of the second gasifying raw material S2 and the second gasifying agent G2 in the descending section 11.
According to the embodiment of the invention, the second gasifying agent G2 is one of air, oxygen-enriched air and oxygen, or the mixture of one of the three with water vapor and carbon dioxide, and the oxygen concentration range is 21-100%.
According to an embodiment of the invention, the device further comprises a separation device.
Wherein the separation device comprises a first inlet, a first material outlet and a second material outlet, and the first inlet is communicated with the hearth outlet 13; the lifting section 12 is further provided with a first material returning opening 14, and the first material returning opening 14 is communicated with the first material outlet; the descending section 11 is also provided with a second return opening 15, and the second return opening 15 is communicated with a second material outlet.
According to an embodiment of the present invention, the separation device may be a primary separation device, or a secondary separation device, or a multi-stage separation device having two or more stages.
In the case of the first-stage separator, the solid phase outlet (first material outlet) of the first-stage separator is communicated with the first return port 14, and the gas phase outlet (second material outlet) of the first-stage separator is communicated with the second return port 15.
Under the condition that the separation device is a two-stage separation device, after solid particles are separated twice, solid particles (raw materials which are not completely gasified) with different particle sizes (statistical average particle sizes) are separated at each stage of separation device, the particle sizes are gradually decreased, the primary solid-phase materials and the secondary solid-phase materials are respectively separated through the two-stage separation device, the primary solid-phase materials with larger particle sizes are returned to the first gasification reaction zone of the lifting section 12 through the first material outlet, and the secondary solid-phase materials with smaller particle sizes are returned to the second gasification reaction zone of the descending section 11 through the second material outlet.
According to the embodiment of the invention, the incompletely reacted solid particles with different particle sizes are separated by the separation device and are divided into two or more stages according to the particle size, for example, coarse particle solid particles and fine particle solid particles are respectively returned to different areas of the gasification device, the coarse particle solid particles have better reactivity, the coarse particle solid particles are returned to the lifting section 12 at the bottom, namely the first gasification reaction zone, the fine particle solid particles have poorer reactivity, and the fine particle solid particles are returned to the descending section 11 at the upper part, namely the second gasification reaction zone, so that the grading utilization of the carbon-containing solid particles is realized, the tissue reaction of the solid particles with different particle sizes in a proper temperature range and a proper particle size range of raw materials is ensured, and the solid particles are integrated into a whole, so that the grading of the gasification reaction and the aggregation of heat are realized, and the carbon conversion rate of the whole system can be improved.
According to an embodiment of the present invention, as shown in fig. 1, in the above system, the separation device is a two-stage separation device, and includes a first separation device 2 and a second separation device 3 that are in communication with each other. Separating the primary solid-phase material and the secondary solid-phase material by a two-stage separation device, returning the primary solid-phase material with larger particle size to the first gasification reaction zone, and returning the secondary solid-phase material with smaller particle size to the second gasification reaction zone. Specifically, the first separation device 2 is used for generating a first-stage gas-phase material and a first-stage solid-phase material after performing gas-solid separation on the primary fly ash particles, and returning the first-stage solid-phase material to the lifting section 12; the second separation device 3 is used for generating a secondary gas phase material and a secondary solid phase material after gas-solid separation is carried out on the primary gas phase material, and returning the secondary solid phase material to the descending section 11.
According to an embodiment of the invention, in particular, the first separation device 2 comprises a first inlet, a first solid phase outlet and a first gas phase outlet, wherein the first solid phase outlet is the first material outlet; the first inlet of the first separation device 2 is communicated with a hearth outlet 13, and the first solid phase outlet of the first separation device 2 is communicated with a first return opening 14 arranged on the lifting section 12 and used for returning the first-stage solid phase material to the lifting section 12. Primary fly ash particles generated by gasification reaction in the gasification device 1 leave through a hearth outlet 13 and enter the first separation device 2, a large amount of primary solid phase materials are captured under the separation action of the first separation device 2, and return to a first material return port 14 arranged in a dilute phase zone or a transition zone of dilute phase and dense phase zone of the hearth of the gasification device 1 through a conveying channel, so that the primary solid phase materials are returned to the lifting section 12.
According to an embodiment of the invention, the second separation device 3 comprises a second inlet, a second solid phase outlet and a second gas phase outlet, the second solid phase outlet being the second material outlet. The second inlet of the second separation device 3 is communicated with the first gas outlet of the first separation device 2, the second solid phase outlet of the second separation device 3 is communicated with the second material returning opening 15 arranged on the descending section 11, and the second solid phase material is returned to the descending section 11. The first gas phase material from the gas phase outlet of the first separator 2 is subjected to gas-solid separation by the second separator 3 to generate a second gas phase material (gasification product P and fly ash S) and a second solid phase material, and the second solid phase material is returned to the descending section 11.
According to the embodiment of the invention, the system of the embodiment of the invention adopts a mode of connecting two stages of gas-solid separation in series to realize two stages of separation of fly ash materials, and solid raw materials captured by the gas-solid separator are returned to different positions of a hearth of the gasification furnace through the grading material returning component to carry out gasification reactions at different temperatures, so that the system separation efficiency of the circulating fluidized bed grading gasification device is improved; and the fine solid materials trapped by the secondary gas-solid separation device and the fly ash escaped from the system are gasified at high temperature by arranging a local high-temperature area at the top of the hearth of the gasification device, so that the fly ash amount and the fly ash carbon content of the circulating fluidized bed staged gasification device are greatly reduced.
Under the condition that the separation device is more than two stages of separation devices, the first-stage solid-phase material and the second-stage solid-phase material are separated through the first separation device and the second separation device respectively, the first-stage solid-phase material with larger particle size is returned to the first gasification reaction zone, and the second-stage solid-phase material with smaller particle size is returned to the second gasification reaction zone. The separation device after the secondary separation device is collectively called a third separation device, which comprises a third inlet, a third solid phase outlet and a third gas phase outlet, wherein the third inlet is communicated with the second gas phase outlet of the second separation device 3, and the third solid phase outlet is communicated with the descending section.
In particular, the third solid phase outlet of the third separation device may communicate with the second return opening 15 in the descending section, sharing one return opening with the second separation device 3, and the third separation device may also return material alone through other return openings, the third solid phase outlet communicating with other return openings (different from the second return opening 15) provided in the descending section.
According to an embodiment of the invention, the apparatus further comprises a first and a second return. The first solid phase outlet of the first separation device 2 is communicated with the first material returning opening 14 through a first material returning device; and/or the second solid phase outlet of the second separation device 3 is in communication with the second return opening 15 via a second return.
According to the embodiment of the present invention, it is preferable that the gas-solid separation efficiency of the first separation device 2 is lower than the gas-solid separation efficiency of the second separation device 3.
Wherein: the gas-solid separation efficiency of the first separation device 2 is 50% -90%; the gas-solid separation efficiency of the second separation device 3 is 98% -100%.
According to the embodiment of the invention, the gas-solid separation part of the first separation device 2 is a low-separation-efficiency and low-resistance gas-solid separator, preferably the gas-solid separation efficiency ranges from 60% to 80%, and the resistance is 20% to 75% of that of a conventional cyclone separator. The return means of the first separation device 2 are non-mechanical return devices including, but not limited to, U-valves, J-valves, N-valves and L-valves, preferably U-valves.
The second separation device 3 may be composed of a group of gas-solid separation devices, or may be composed of a plurality of groups of gas-solid separation devices connected in series. The gas-solid separation part of the second separation device 3 is a high-efficiency gas-solid separator.
According to the embodiment of the invention, the first separation device is set to have lower separation efficiency, so that the fly ash with smaller particle size can be prevented from being caught back to the bottom first gasification reaction zone (the temperature of the bottom first gasification reaction zone is lower and is unfavorable for the regasification of the fine particle fly ash), and the second separation device is set to be an efficient separation device, so that the fine particle fly ash containing carbon in the fly ash of gasification products can be returned to a local high-temperature zone at the upper part of the hearth as much as possible, the high-temperature gasification reaction can be further carried out, and the overall carbon conversion rate is improved.
According to the embodiment of the invention, the second separation device adopts a high-inverse differential pressure returning device, and the numerical range of the inverse differential pressure is as follows: and the pressure difference is more than or equal to 2kPa, the higher material returning pressure difference can be overcome, and the anti-cross-ventilation effect is better.
According to an embodiment of the invention, the second separation device 3 returns the secondary solid phase material to the descending section 11, specifically by the following two ways:
in one way, referring to fig. 1, as shown in fig. 1, the second solid phase outlet of the second separation device 3 is communicated with a second return port 15 (middle or lower part of the furnace) arranged at the descending section 11, and the second solid phase material is returned to the descending section 11 through the second return port 15.
In the embodiment of the invention, the second way of returning the secondary solid phase material to the drop leg 11 is seen in fig. 2. In this case, the material inlet of the descending section and the second return port share the same inlet structure.
FIG. 2 is a system configuration diagram of a gasification apparatus according to another embodiment of the present invention.
As shown in fig. 2, the gasification apparatus structure shown in this embodiment is substantially the same as that shown in fig. 1, except that the second solid phase outlet of the second separation apparatus 3 is communicated with the second gasification raw material inlet of the gasification reaction organizing apparatus 4. In this case, the gasification raw material is a mixture of the second gasification raw material S2 and the second solid phase material separated by the second separation device 3, and the second gasification raw material S2, the second solid phase material and the second gasifying agent G2 are injected into the descending stage 11 together by the organization action of the gasification reaction organization device 4. The second gasification raw material S2 may be all or part of fly ash S generated by the gasification device itself through the separation device, or may be a mixture of fly ash S and other solid or gas raw materials.
According to the embodiment of the invention, the secondary solid-phase material, the second gasification raw material S2 and the second gasification agent G2 are sprayed into the descending section 11 together through the organization action of the gasification reaction organization device 4, so that the fine-particle secondary solid-phase fly ash material can be positioned in a high-temperature area of jet flow of the spraying device 4, and a high-temperature gasification reaction can be timely generated, thereby being beneficial to full gasification of the fine-particle fly ash and stable operation of the gasification reaction organization device 4.
Another aspect of the present invention provides a method for gasification using the gasification apparatus described above, which is described below with reference to fig. 1, the gasification method comprising:
The first gasification raw material F and the first gasification agent G1 are introduced into the lifting section 12 of the gasification furnace hearth 1, and the second gasification agent G2 is introduced into the descending section 11 of the gasification furnace hearth 1, so that gasification reaction of the first gasification raw material F, the first gasification agent G1 and the second gasification agent G2 occurs in the gasification furnace hearth 1, and the lifting section 12 forms a first gasification reaction zone and the descending section 11 forms a second gasification reaction zone. Wherein the temperature of the second gasification reaction zone is higher than that of the first gasification reaction zone, the bottom of the descending section 11 is connected with the top of the lifting section 12, and a hearth outlet 13 is arranged at the connection part of the lifting section 12 and the descending section 11.
According to an embodiment of the invention, the lifting section 12 is a fluidized bed or a bubbling bed or a circulating fluidized bed, and the lowering section 11 is an entrained flow bed.
According to an embodiment of the present invention, the above-described method further includes injecting the second gasification raw material S2 and the second gasification agent G2 into the second gasification reaction zone through the gasification reaction organization apparatus so that the temperature of the second gasification reaction zone is higher than the temperature of the first gasification reaction zone by the combustion heat release of the second gasification raw material S2 and the second gasification agent G2 in the second gasification reaction zone.
Wherein, the first gasifying agent G1 can be mixed gas of one of air, oxygen-enriched air and oxygen, water vapor and carbon dioxide, and the oxygen concentration is 21-50%; the second gasifying agent G2 is a mixed gas of one of air, oxygen-enriched air and oxygen, water vapor and carbon dioxide, and the oxygen concentration is 21-100%.
According to an embodiment of the invention, the temperature range of the first gasification reaction zone is: the operation apparent wind speed of the first gasification reaction zone is 2 m/s-8 m/s at the temperature of 750-150 ℃ which is the softening temperature ST-150 of the preset ash. The temperature range of the second gasification reaction zone is: 950-preset ash flow temperature FT; the second gasification raw material S2 and/or the second gasifying agent G2 are introduced into the core area of the high-temperature reaction of the descending section 11 after being accelerated by jet flow; the average residence time of the second gasification raw material S2 and/or the second gasifying agent in the second gasification reaction zone is 1 to 5S. The preset ash softening temperature ST and the preset ash flowing temperature FT are related to the types of the fly ash particles, and can be measured according to a related measuring method in national standards.
According to the embodiment of the invention, by adding the gasification reaction organization device 4, the gasification agent and the raw material are sprayed into the descending section 11 through the gasification reaction organization device 4, a local high-temperature zone can be formed in the descending section 11, so that the temperature of the descending section 11 is higher than that of the lifting section 12, the fine solid materials and the fine solid raw materials S2 trapped by the gas-solid separation device 3 are subjected to high-temperature gasification reaction in the local high-temperature zone, the highest gasification temperature can reach FT (ash flow temperature), and the fine particle fly ash is returned to the upper high-temperature second gasification reaction zone due to poor reactivity, and the high temperature can promote the fly ash gasification, so that the carbon conversion rate of the fine particle fly ash can be improved.
According to an embodiment of the invention, the material flow direction of the second gasification reaction zone is opposite to the material flow direction of the first gasification reaction zone. Specifically, the injection direction of the gasification reaction organization device 4 can be set to be from the top of the hearth to the bottom of the hearth, the gasification device 1 can adopt a fluidized bed, and the air outlet direction of the air distribution device in the fluidized bed can be from the bottom of the hearth to the top of the hearth. The relatively independent gasification reaction areas are constructed in the hearth, the flow directions of the two reaction areas are opposite, slag produced by the high-temperature gasification reaction of the second gasification reaction area flows to the lower part of the hearth under the action of high-temperature gas entrainment and gravity, the slag is quickly mixed with the upward gas-solid materials from the first gasification reaction area in opposite directions, the chilling effect is realized, and liquid slag formed by the upper fly ash is dispersed into solid fine slag through the opposite flushing of the high-speed material flow from the lower part of the hearth and the material flow from the upper part, so that the stable operation of high-temperature gasification is facilitated.
According to the embodiment of the invention, the method further comprises the steps of discharging products of the gasification reaction in the hearth 1 of the gasification furnace through the hearth outlet 13, and introducing the products into a separation device for gas-solid separation to generate a first material and a second material, wherein the particle size of the first material and the particle size of the second material are larger than each other; passing the first material into the lifting section 12; the second material is passed to the drop leg 11.
According to the embodiment of the invention, by adopting the method, the gasified coarse and fine materials are gasified in a grading way by adopting a grading separation and material returning method, the coarse materials which are easy to trap and gasify are sent into a hearth part of the circulating bed, the circulating bed materials are utilized for circulation, the reaction residence time is prolonged, and the gasification efficiency is improved; and (3) conveying the fine materials which are difficult to capture and gasify into the hearth part of the entrained flow hearth to carry out high-temperature rapid gasification, so that the solid particles with different particle size distributions in the circulating fluidized bed are gasified in a grading manner, and the gasification efficiency and the carbon conversion rate of the system are improved.
In yet another aspect, the invention provides a solid material thermochemical reaction device comprising a lifting section, a lowering section, and a reaction zone outlet.
Wherein the lifting section is provided with a first solid material inlet and a first gas inlet; the descending section is provided with a descending section material inlet which is used for introducing second gas, and the bottom of the descending section is connected with the top of the lifting section; the lifting section and the descending section form a thermochemical reaction area; the outlet of the reaction zone is arranged at the joint of the lifting section and the descending section.
The above-mentioned solid material thermochemical reaction device may be a gasification device described in the above-mentioned embodiment of the present invention, and the structural form thereof is not described herein.
The solid material thermochemical reaction device is not limited to the gasification reaction scene, and can be used for other thermochemical reaction scenes, such as combustion, solid melting treatment and catalytic reaction.
The foregoing description of the embodiments has been provided for the purpose of illustrating the general principles of the invention, and is not meant to limit the invention thereto, but to limit the invention thereto, and any modifications, equivalents, improvements and equivalents thereof may be made without departing from the spirit and principles of the invention.
Claims (20)
1. A gasification apparatus comprising:
the lifting section is provided with a first gasification raw material inlet and a first gasification agent inlet and is a fluidized bed;
The descending section is provided with a descending section material inlet which is used for introducing a second gasifying agent, and the bottom of the descending section is connected with the top of the lifting section; the lifting section and the descending section form a gasification furnace hearth; the first gasification raw material, the first gasification agent and the second gasification agent are subjected to gasification reaction in the hearth of the gasification furnace, so that the lifting section forms a first gasification reaction zone, and the descending section forms a second gasification reaction zone; the temperature of the second gasification reaction zone is higher than the temperature of the first gasification reaction zone;
the hearth outlet is arranged at the joint of the lifting section and the descending section;
the descending section material inlet is arranged at the top end or the upper side surface of the descending section, forms a gasification reaction organization device, and is also used for spraying a second gasification raw material into the descending section;
The injection direction of the gasification reaction organization device is set to be from the top of the hearth to the bottom of the hearth, and the air outlet direction of the air distribution device in the lifting section is set to be from the bottom of the hearth to the top of the hearth for blowing air, so that the material flowing direction of the second gasification reaction zone is opposite to the material flowing direction of the first gasification reaction zone.
2. The gasification apparatus of claim 1, wherein:
The descending section material inlet is formed by integrating a second gasifying agent inlet and a second gasifying raw material inlet.
3. The gasification apparatus of claim 2, wherein:
The second gasifying agent inlet is disposed around the second gasifying feed inlet.
4. A gasification apparatus according to claim 3 wherein:
the second gasifying agent inlets are arranged in a plurality of circumferentially-arrayed mode by taking the second gasifying raw material inlet as a center.
5. A gasification apparatus according to claim 3 wherein:
The second gasifying agent inlet and the second gasifying raw material inlet are arranged as coaxial channels, wherein the second gasifying raw material inlet is a central channel, and the second gasifying agent inlet is an annular gap channel surrounding the second gasifying raw material inlet.
6. The gasification apparatus according to any one of claims 1 to 5, further comprising:
the separation device comprises a first inlet, a first material outlet and a second material outlet, wherein the first inlet is communicated with the hearth outlet;
The lifting section is further provided with a first material returning opening, and the first material returning opening is communicated with the first material outlet; the descending section is further provided with a second material returning opening, and the second material returning opening is communicated with the second material outlet.
7. The gasification apparatus of claim 6, wherein the separation apparatus comprises:
The first separation device comprises the first inlet, a first solid phase outlet and a first gas phase outlet, wherein the first solid phase outlet and the first material outlet are of the same structure;
The second separation device comprises a second inlet, a second solid phase outlet and a second gas phase outlet, wherein the second inlet is communicated with the first gas phase outlet, and the second solid phase outlet and the second material outlet are of the same structure.
8. The gasification apparatus of claim 7, wherein the separation apparatus further comprises:
and a third separation device comprising a third inlet, a third solid phase outlet, and a third gas phase outlet, wherein the third inlet and the second gas phase outlet are in communication, wherein the third solid phase outlet is in communication with the drop leg.
9. The gasification apparatus of claim 8, wherein:
The third solid phase outlet is communicated with a second material returning port in the descending section.
10. The gasification apparatus of claim 7, further comprising:
The first solid phase outlet is communicated with the first material returning opening through the first material returning device; and/or
The second solid phase outlet is communicated with the second material returning opening through the second material returning device.
11. The gasification apparatus of claim 7, wherein:
The gas-solid separation efficiency of the first separation device is lower than that of the second separation device.
12. The gasification apparatus of claim 11, wherein:
the gas-solid separation efficiency of the first separation device is 50% -90%;
the gas-solid separation efficiency of the second separation device is 98% -100%;
the numerical range of the stress-resistant pressure difference of the second separation device is as follows: and is more than or equal to 2kPa.
13. The gasification apparatus of claim 6, wherein:
the descending section material inlet and the second material returning opening share the same inlet structure.
14. The gasification apparatus of claim 6, wherein:
the lifting section is a bubbling bed or a circulating fluidized bed, and the descending section is an entrained flow bed.
15. A gasification process comprising:
Introducing a first gasification raw material and a first gasifying agent into a lifting section in a gasification furnace hearth and introducing a second gasifying agent into a descending section in the gasification furnace hearth so that the first gasification raw material, the first gasifying agent and the second gasifying agent undergo gasification reaction in the gasification furnace hearth, and the lifting section forms a first gasification reaction zone and the descending section forms a second gasification reaction zone; the lifting section is a fluidized bed;
and passing a second gasification feedstock to the downleg such that the second gasification feedstock and the second gasification agent undergo a gasification reaction in the downleg; wherein the second gasification raw material and the second gasification agent are injected through a descending section material inlet arranged at the top end or the upper side surface of the descending section;
The temperature of the second gasification reaction zone is higher than that of the first gasification reaction zone, the bottom of the descending section is connected with the top of the lifting section, and a hearth outlet is arranged at the joint of the lifting section and the descending section;
The injection direction of the gasification reaction organization device is set to be from the top of the hearth to the bottom of the hearth, and the air outlet direction of the air distribution device in the lifting section is set to be from the bottom of the hearth to the top of the hearth for blowing air, so that the material flowing direction of the second gasification reaction zone is opposite to the material flowing direction of the first gasification reaction zone.
16. The method according to claim 15, wherein:
the temperature range of the second gasification reaction zone is as follows: 950-preset ash flow temperature FT;
The temperature range of the first gasification reaction zone is as follows: 750 ℃ to a preset ash softening temperature ST-150 ℃.
17. The method according to claim 15, wherein:
The second gasification raw material and/or the second gasifying agent are introduced into the core area of the high-temperature reaction of the descending section after being accelerated by jet flow.
18. The method according to claim 15, wherein:
the average residence time of the second gasification raw material and/or the second gasification agent in the second gasification reaction zone is 1-5 s.
19. The method of any of claims 15-18, further comprising:
Discharging a product of gasification reaction in a hearth of the gasification furnace through the hearth outlet, and introducing the product into a separation device for gas-solid separation to generate a first material and a second material, wherein the particle size of the first material is larger than that of the second material;
Introducing the first material into the lifting section;
and introducing the second material into the descending section.
20. The gasification process of claim 19, wherein:
the oxygen concentration of the first gasifying agent is 21% -50%;
the oxygen concentration of the second gasifying agent is 21-100%.
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| CN106190317A (en) * | 2016-07-22 | 2016-12-07 | 新奥科技发展有限公司 | The preparation method of coal gasifier, gasification system and activated coke |
| CN106675658A (en) * | 2016-12-15 | 2017-05-17 | 华北电力大学 | Device and method for high-flux circulating fluidized bed low-rank coal gasifying |
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| CN106675658A (en) * | 2016-12-15 | 2017-05-17 | 华北电力大学 | Device and method for high-flux circulating fluidized bed low-rank coal gasifying |
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