CN217173631U - Pulverized coal hydrogasification and biomass pyrolysis coupling device - Google Patents
Pulverized coal hydrogasification and biomass pyrolysis coupling device Download PDFInfo
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological origin
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Abstract
The utility model provides a buggy hydro-gasification and living beings pyrolysis coupling device, the device includes: a first stage reaction zone and a second stage reaction zone; wherein, the bottom of the first-stage reaction zone is provided with a necking structure for separating pyrolysis gas and semicoke generated by coal hydro-gasification reaction in the first-stage reaction zone; the second section reaction zone is arranged below the first section reaction zone, and the inlet of the second section reaction zone is connected with the necking structure; and a biomass channel is arranged in the second-stage reaction zone and used for inputting biomass into the second-stage reaction zone from bottom to top so that the biomass is reversely contacted and mixed with the semicoke received at the inlet of the second-stage reaction zone and is subjected to co-gasification reaction. The utility model discloses both can guarantee the hydro-gasification semicoke under high temperature state, can guarantee the intensive mixing and the gasification time of semicoke and living beings simultaneously again for it is more abundant to gasify the reaction altogether.
Description
Technical Field
The utility model relates to a coal hydrogasification technical field particularly, relates to a buggy hydrogasification and living beings pyrolysis coupling device.
Background
The coal and biomass co-pyrolysis combustion technology is developed to meet the urgent requirements on the energy current situation of rich coal, poor oil, less gas and huge biomass yield in partial areas and on environmental protection, so that the advantages of coal and biomass resources can be exerted, the clean and efficient utilization of coal and the conversion from low-grade biomass fuel to high-grade fuel can be realized, and the quality of pyrolysis liquid and gas products can be improved.
The supply of biomass is influenced by seasons, the scale of biomass independent gasification is limited, the energy density of the biomass is low, the independent gasification temperature is low, more tar is generated during gasification, the utilization efficiency of the biomass is reduced, and the stable operation of the gasification process is adversely affected. Therefore, the research on the co-gasification of the coal and the biomass breaks through the limitation of the selection of the gasification raw materials, and a new way is provided for the co-gasification of the solid raw materials with different sources and characteristics. Among them, biomass refers to various organisms produced by photosynthesis using the atmosphere, water, land, and the like, i.e., all living and growing organic substances, and is generally called biomass.
Although the technical routes applicable to biomass gasification/pyrolysis are various and can be classified into fixed bed gasification, fluidized bed gasification and entrained flow gasification depending on the reactor used, the entrained flow gasification furnace is not suitable for the biomass feedstock. The entrained flow bed utilizes the jet entrainment principle in fluid mechanics, and the coal powder and the gasifying agent medium are sprayed into the gasification furnace through the nozzle, and the jet flow causes entrainment and high-temperature turbulence, so that the intensive mixing is continuously performed to generate the full gasification reaction. However, the problems of low biomass density, difficult grinding and the like cause that large-particle biomass is difficult to be fully mixed and completely pyrolyzed and gasified in the entrained flow bed, the retention time in the existing entrained flow bed is limited, the inside of the large-particle biomass is difficult to be fully pyrolyzed to generate heavy tar, the problems of high-temperature slag flowing erosion damage of the furnace wall lining, difficult oil-gas separation and the like are easily caused, and the development of the commercialization of the technology is hindered. Even in the mixed feeding mode, due to the fact that the biomass is low in general density, the biomass and the coal powder are mixed and enter the entrained flow bed to be mixed unevenly, the coal powder and the biomass pyrolysis temperature are different (coal is decomposed at 600 ℃ and biomass is decomposed at more than 100 ℃ to generate tar), meanwhile, the tar is attached to the surface of the coal powder, the problems of overflow of coal volatile components, mutual interference and the like are affected, and the requirements on equipment such as a nozzle of a gasification furnace are high.
The hydro-gasification semi-coke has the characteristics of porosity, extremely few volatile components (less than 5 percent), small density and the like, and is closer to the biomass because the semi-coke is considered to be used as a heat source to provide the biomass for co-gasification (the hydro-gasification semi-coke can continue to carry out the secondary gasification of the semi-coke at high temperature).
However, through existing research, it is known that heat needs to be absorbed in biomass gasification, the biomass gasification provides pyrolysis temperature and sufficient pyrolysis time, tar generated in the gasification process is avoided as far as possible, pollution to a post system is avoided, and application difficulty is reduced. The semicoke generated after hydro-gasification is chilled, the temperature of the semicoke after the chilling is 600-700 ℃, and considering that the gas-solid heat transfer efficiency is low and the biomass particles are large, the semicoke temperature needs to be increased and the mixing time of the semicoke and the biomass needs to be increased on the basis of the prior art so as to achieve the optimal gasification effect.
The difficulty in the prior art is as follows:
as the reactions of rapid hydrogenation pyrolysis, secondary pyrolysis of volatile components, hydrogenation gasification of active semicoke and the like occur in sequence in the hydrogenation gasification reaction process, methane, light aromatic oil products with high added values and clean semicoke are finally generated. However, the pulverized coal is fully pyrolyzed at a higher reaction temperature to form a large amount of small molecular fragments which are mainly methane-rich gas and light oil products. However, at a continuous high temperature, the molecules of the oil product are easy to generate secondary reaction, namely, the cracking of the tar component and the condensation polymerization of the tar component. Researches show that when the temperature is lower, the cracking reaction is stronger than the polycondensation reaction, the yield of light oil is increased, and the quality of oil products is better. Cracking of heavy components and light oil results in a decrease in heavy and light oil yields with increasing temperature. When the temperature is kept higher, the polycondensation reaction is stronger than cracking, so that the yield of heavy oil is increased, the quality of oil products is poorer, the viscosity is high, the oil-gas separation is not facilitated, and the dust content is high. Therefore, the rapid cooling (less than 500 ℃) after pyrolysis is beneficial to ensuring the quality of oil products and facilitating the oil-gas separation in the later working section. But the low temperature is not beneficial to the secondary reaction of the semicoke and the co-gasification with the biomass. If the temperature of the generated synthesis gas is kept, oil molecules generated by fast pyrolysis of the hydro-gasification coal powder are easy to generate secondary reaction, the quality of the hydro-gasification oil is reduced, the problem of heavy tar generated by biomass gasification cannot be avoided, the post-treatment difficulty is increased, and the economy of the hydro-gasification technology is reduced. Therefore, the production of biomass tar can be effectively reduced by keeping the temperature of the semicoke (above 800 ℃), but the quality of oil products produced by primary pyrolysis of hydro-gasification is influenced, the proportion of heavy tar in hydro-gasification oil products is increased, a device is polluted, and the difficulty in separating a rear system is increased.
In addition, the middle part of the existing hydrogenation gasification furnace is only a semicoke falling area after being chilled, so that the semicoke and the biomass cannot be fully mixed, and only the semicoke and the biomass can fall to the bottom of the furnace and cannot be uniformly mixed by directly spraying the biomass and the like.
Disclosure of Invention
In view of this, the utility model provides a buggy hydro-gasification and living beings pyrolysis coupling device aims at solving the high temperature and leads to heavy oil productivity to increase and be unfavorable for oil-gas separation, low temperature are unfavorable for semicoke secondary reaction and living beings problem of gasifying altogether in the current hydro-gasification stove.
The utility model provides a buggy hydro-gasification and living beings pyrolysis coupling device, the device includes: a first stage reaction zone and a second stage reaction zone; the bottom of the first-stage reaction zone is provided with a necking structure and is used for separating pyrolysis gas and semicoke generated by coal hydro-gasification reaction in the first-stage reaction zone so that the pyrolysis gas flows upwards and is discharged, and the semicoke moves downwards and is discharged to the outside of the first-stage reaction zone; the second-stage reaction zone is arranged below the first-stage reaction zone, and an inlet of the second-stage reaction zone is connected with the necking structure and is used for receiving the semicoke discharged by the necking structure; and a biomass channel is arranged in the second-stage reaction zone and used for inputting biomass into the second-stage reaction zone from bottom to top so that the biomass descends and carries out co-gasification reaction after being in reverse contact and mixed with the semicoke received at the inlet of the second-stage reaction zone.
Further, in the coupling device for coal powder hydro-gasification and biomass pyrolysis, a second inner cylinder is arranged outside the biomass channel in the second-stage reaction zone, and an annular reaction zone is formed between the second inner cylinder and the biomass channel, so that biomass and semicoke are reversely contacted and mixed, and then descend in the annular reaction zone for co-gasification reaction; and an ash and slag shunting disc is arranged below the second inner cylinder on the biomass channel and is used for separating ash and gasified gas generated by co-gasification reaction so as to enable the gasified gas to move upwards from the outside of the second inner cylinder and be discharged.
Further, according to the coupling device for coal powder hydro-gasification and biomass pyrolysis, the upper surface of the ash splitter disc is provided with an air outlet pipeline for discharging purge air so as to prevent the surface of the ash splitter disc from hardening.
Further, according to the coupling device for coal powder hydro-gasification and biomass pyrolysis, a first jacket is arranged outside the biomass channel below the ash and slag diverter plate, and an annular cold area channel is formed between the first jacket and the shell of the biomass channel and used for conveying a cooling medium to cool the biomass conveyed in the biomass channel; and a first annular scavenging gas channel is arranged on the periphery of the first jacket and used for inputting scavenging gas into the gas outlet pipeline.
Further, above-mentioned buggy hydro-gasification and biomass pyrolysis coupling device, be in the second section reaction zone the outside of second inner tube is equipped with the third inner tube, the third inner tube with form the air guide intermediate layer that is used for carrying the gasification gas between the second inner tube, the third inner tube with form second annular sweeping gas passageway between the casing of second section reaction zone, its with first annular sweeping gas passageway is linked together, and the sweeping gas is in from last to carrying down in the second annular sweeping gas passageway, and carry out the heat transfer with the gasification gas in the air guide intermediate layer in the second annular sweeping gas passageway to after making sweeping gas temperature and gasification gas phase adaptation, inputing to the pipeline of giving vent to anger through first annular sweeping gas passageway, spout.
Further, in the coupling device for coal powder hydro-gasification and biomass pyrolysis, the outer diameter of the ash splitter disc is larger than the diameter of the second inner cylinder and smaller than the diameter of the third inner cylinder, and a necking part is arranged at the bottom of the third inner cylinder.
Further, in the coupling device for coal powder hydro-gasification and biomass pyrolysis, the connection surface between the ash and slag splitter disc and the biomass channel and the plane where the bottom end of the second inner cylinder is located are arranged in parallel and level.
Further, the coupling device for coal powder hydro-gasification and biomass pyrolysis comprises a necking structure and a gas-liquid separator, wherein the necking structure comprises: a first throat and a second throat; wherein the second necking is arranged below the first necking, and the second necking is at least partially arranged in the second-stage reaction zone and used for preventing the gas in the second-stage reaction zone from rising into the first-stage reaction zone.
Further, according to the coupling device for coal powder hydrogasification and biomass pyrolysis, the first section reaction area is internally provided with the first inner cylinder and is divided into the reaction area in the cylinder and the annular exhaust area, coal powder input into the first section reaction area is subjected to coal hydrogasification reaction in the reaction area in the cylinder, generated pyrolysis gas is separated from semicoke, the separated pyrolysis gas flows upwards and is discharged from the annular exhaust area, and the separated semicoke falls and is discharged from the necking structure.
Further, according to the coupling device for coal powder hydro-gasification and biomass pyrolysis, the upper part of the shell of the first-stage reaction zone is provided with the exhaust port, and the exhaust port is provided with the quenching gas device for quenching pyrolysis gas.
The coupling device for coal powder hydro-gasification and biomass pyrolysis provided by the utility model adopts a necking structure as a hydro-gasification pyrolysis gas and semicoke separation structure, the pyrolysis gas generated by the coal powder in the first-stage reaction zone is separated from the semicoke, so that the pyrolysis gas flows upwards to be discharged after being separated, the separated semicoke continuously falls to be discharged, meanwhile, the separation of the pyrolysis gas and the semicoke can lead the pyrolysis gas and the semicoke to be at different temperatures, thereby realizing the rapid cooling of the pyrolysis gas, avoiding the secondary reaction of the pyrolysis gas generated by the primary pyrolysis of hydrogenation, and realizing that the semicoke enters the second section reaction zone at high temperature so as to realize the mixing of the semicoke and the biomass sprayed in the second section reaction zone at high temperature, the hydro-gasification semicoke and the biomass are fully mixed and co-gasified under the condition of the existing furnace length, so that a new way of co-gasification of the biomass and the coal is widened; simultaneously, the biomass channel inputs the living beings to the top of second section reaction zone from bottom to top, can input through the mode of spouting, adopt down to spout the mode promptly, make living beings mix at the top of second section reaction zone with the semicoke, form a material interface, the mixing of living beings and semicoke can be realized to this interface, and the living beings that can input from bottom to top still can weaken the semicoke descending speed through the impact, increase and mix with the semicoke and both whereabouts time, make the gasification reaction altogether more abundant, the problem that the high temperature leads to heavy oil productivity to increase to be unfavorable for oil gas separation in the current hydrogenation gasifier, low temperature is unfavorable for semicoke secondary reaction and living beings to gasify altogether is solved.
Further, through the setting of lime-ash reposition of redundant personnel dish and pipeline etc. of giving vent to anger, can avoid because the large granule that leads to the fact behind semicoke and the living beings co-gasification with harden, reduce the condition of this kind of clamp dirt of gas simultaneously, realize gaseous dust removal, avoid causing the pollution to the back system, reduce the pressure of the gaseous dust removal workshop section of back system.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention. Also, like reference numerals are used to refer to like parts throughout the drawings. In the drawings:
fig. 1 is a schematic structural diagram of a coupling device for coal powder hydro-gasification and biomass pyrolysis according to an embodiment of the present invention;
fig. 2 is a schematic structural view of an ash diverter tray provided by the embodiment of the present invention;
FIG. 3 is a schematic structural view of a jacket structure below the ash tray according to the embodiment of the present invention;
fig. 4 is a top view of a jacket structure below the ash tray according to the embodiment of the present invention.
Detailed Description
Exemplary embodiments of the present disclosure will be described in more detail below with reference to the accompanying drawings. While exemplary embodiments of the present disclosure are shown in the drawings, it should be understood that the present disclosure may be embodied in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the disclosure to those skilled in the art. It should be noted that, in the present invention, the embodiments and features of the embodiments may be combined with each other without conflict. The present invention will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.
The biomass gasification/pyrolysis device generally has the problems of low gas heat value and gasification efficiency in products, large heat loss per se and corrosion of biomass alkali metal to a reactor and subsequent equipment, particularly the existence of tar in the products is one of main factors restricting the wide application of the device, the tar can be condensed in downstream equipment of a gasification furnace to cause the fault of a mechanical system, and simultaneously the tar also takes away energy to reduce the gas heat value.
The lower fixed carbon content of the biomass itself, as well as the high volatiles and moisture make the biomass more prone to tar formation during gasification. Biomass tar can not only be compressed but also has a very complex composition.
Biomass pyrolysis can be classified into low-temperature slow pyrolysis, medium-temperature fast/medium/slow pyrolysis, high-temperature fast pyrolysis and the like according to the heating rate and the pyrolysis final temperature of biomass, generally, low pyrolysis temperature, low heating rate and long residence time are mainly used for increasing the yield of solid biomass coke to the maximum extent, the yields of three-phase products generated at medium pyrolysis temperature and medium heating rate are equivalent, and fast pyrolysis at a temperature higher than 700 ℃ is mainly based on gas products. Therefore, the high-temperature fast biomass is beneficial to reducing the tar content in the biomass gasification/pyrolysis product, and the entrained flow gasification process is more in line with the requirement of fast heating of the biomass.
The coal hydro-gasification process comprises a hydro-pyrolysis process in which volatile components are quickly separated out after coal is quickly heated and a coal coke hydro-gasification process in which residual coke reacts with hydrogen to generate methane. Hydrogen and coal powder enter from the top of the gasification furnace, are chilled after the reaction section is finished, process gas is discharged from the middle of the gasification furnace, can be used as a natural gas raw material after methane is separated, and the hydrogen circulates back to the hydrogen buffer tank and then continuously enters the gasification furnace together with the coal powder to perform hydro-gasification reaction. Typically, hydro-gasification processes require an external source of hydrogen to supply the hydrogen to meet the hydrogen consumption during the reaction. The quenched semicoke (with the temperature of 600-700 ℃) falls to the bottom of the gasification furnace.
In this embodiment, in order to realize the rapid cooling of the pyrolysis gas and the entering of the semicoke and the biomass co-gasification region at a high temperature, a coupling device for coal powder hydro-gasification and biomass pyrolysis is provided as follows.
Referring to fig. 1, it is a schematic structural diagram of a coal powder hydro-gasification and biomass pyrolysis coupling device provided in an embodiment of the present invention. As shown, the apparatus may be a gasifier apparatus, i.e. a hydro-gasifier apparatus, comprising: a first stage reaction zone 1 and a second stage reaction zone 2; wherein,
the bottom of the first-stage reaction zone 1 is provided with a necking structure 11 for separating pyrolysis gas and semicoke generated by coal hydro-gasification reaction in the first-stage reaction zone 1, so that the pyrolysis gas flows upwards (relative to the position shown in fig. 1) and is discharged, and the semicoke moves downwards (relative to the position shown in fig. 1) and is discharged to the outside of the first-stage reaction zone 1. Specifically, throat structure 11 is as hydrogenation gasification pyrolysis gas and semicoke isolating construction for the pyrolysis gas that coal powder carries out hydrogenation gasification reaction in first section reaction zone 1 and semicoke separation, so that the separation of pyrolysis gas is to upwards flow in order to discharge, and the semicoke of separation continues to fall in order to discharge, and simultaneously, the separation of pyrolysis gas and semicoke can be so that pyrolysis gas and semicoke are in different temperatures, and then can realize the rapid cooling of pyrolysis gas, still can realize that the semicoke gets into second section reaction zone 2 under high temperature. In the present embodiment, the bottom of the throat structure 11 is provided with a coke discharge port to discharge the semicoke; the outer wall of the first stage reaction zone 1 can be formed by enclosing a shell, and the upper part of the shell of the side wall of the first stage reaction zone 1 is provided with an exhaust port 12 for exhausting separated pyrolysis gas; the arrangement of the necking structure 11 can help the concentrated discharge of the semicoke, and meanwhile, the reduction of the conveying area is beneficial to reducing the gas entrainment in the semicoke and reducing the entering of a pyrolysis product into a lower structure.
The second stage reaction zone 2 is arranged below the first stage reaction zone 1 (relative to the position shown in fig. 1), and an inlet (a top end opening shown in fig. 1) of the second stage reaction zone 2 is connected with the reducing structure 11 and is used for receiving the semicoke discharged from the reducing structure 11; and a biomass channel 21 is arranged in the second-stage reaction zone 2 and is used for inputting biomass into the second-stage reaction zone 2 from bottom to top so that the biomass descends and carries out co-gasification reaction, namely secondary gasification reaction, after being reversely contacted and mixed with the semicoke received at the inlet of the second-stage reaction zone 2. Specifically, the semicoke discharged in the throat structure 11 in a falling mode is directly discharged to the top of the second-stage reaction zone 2 through the inlet of the second-stage reaction zone 2; and, the biomass channel 21 inputs the biomass to the top of the second section reaction zone 2 from bottom to top, and can input the biomass in a spraying mode, namely a downward spraying mode is adopted, so that the biomass and the semicoke are mixed at the top of the second section reaction zone 2 to form a material interface, the biomass and the semicoke can be mixed at the interface, the biomass which can be input from bottom to top can also reduce the descending speed of the semicoke through impact to increase the mixing with the semicoke and the falling time of the semicoke, and the co-gasification reaction is more sufficient.
With reference to fig. 1, in order to increase the speed of the hydro-gasification reaction between the pulverized coal and the hot hydrogen in the first-stage reaction zone, preferably, a first inner cylinder 13 is disposed in the first-stage reaction zone 1, the first-stage reaction zone 1 is divided into a reaction zone 14 in the cylinder and an annular exhaust zone 15, the pulverized coal input into the first-stage reaction zone 1 is subjected to the coal hydro-gasification reaction in the reaction zone 14 in the cylinder, the generated pyrolysis gas is separated from the semicoke, the separated pyrolysis gas flows upward from the annular exhaust zone 15 and is exhausted, and the separated semicoke falls and is exhausted from the throat structure 11. During specific implementation, the first inner cylinder 13 can realize the hydropyrolysis of high-temperature hydrogen and coal powder in a limited cross section, and the mixed concentration of the coal powder and the high-temperature hydrogen in a unit area can be increased in the limited cross section of the inner cylinder, so that the coal powder is fully pyrolyzed, and the coal powder and the hot hydrogen are subjected to rapid hydropyrolysis. Wherein, the necking structure 11 is arranged at the lower part of the first inner cylinder 13 so as to discharge the semicoke generated in the first inner cylinder 13, the temperature is higher than 800 ℃, and the temperature of the semicoke is ensured; primary pyrolysis gas, namely pyrolysis gas generated in a reaction zone 14 in the cylinder, is discharged from an exhaust port 12 arranged on the side wall, and is easy to chill to form a lower temperature region compared with the upper discharge, and the exhaust port positioned at the upper part is closer to the first inner cylinder 13, so that the temperature of the outer wall of the first inner cylinder 13 is influenced, and the influence is generated on the reaction zone in the first inner cylinder 13, therefore, the exhaust port 12 is arranged on the side wall of the shell of the first-stage reaction zone 1, and the influence of the chilling of the pyrolysis gas on the reaction zone in the first inner cylinder can be avoided; preferably, a quenching gas device is arranged at the exhaust port 12 to quench, i.e. rapidly cool, the pyrolysis gas, so as to avoid secondary reaction of the pyrolysis gas.
With continued reference to fig. 1, in the present embodiment, the throat structure 11 includes: a first throat 111 and a second throat 112; wherein the second throat 112 is disposed below the first throat 111, and the second throat 112 is disposed at least partially in the second-stage reaction zone 2 for preventing the gas in the second-stage reaction zone 2 from rising into the first-stage reaction zone 1. In specific implementation, the first throat 111 is an a-b section, and the second throat 112 is a b-c section, and the connection between the two sections is connected to the inlet of the second-stage reaction zone 2, however, the present invention is not limited thereto, and in other embodiments, the connection position between the throat structure 11 and the inlet of the second-stage reaction zone 2 may be other suitable positions, for example, on the outer wall of the second throat 112 or on the outer wall of the first throat 111, only the second throat 112 is ensured to be at least partially disposed in the second-stage reaction zone 2, so as to not only achieve separation between the semicoke and the pyrolysis gas, but also effectively avoid the gas after mixing the biomass and the semicoke from rising to interfere with the reaction in the first-stage reaction zone 1.
In this embodiment, the second-stage reaction zone 2 may be a jacket structure.
As shown in fig. 1, a second inner cylinder 22 is provided outside the biomass passage 21 in the second-stage reaction zone 2, and an annular reaction zone 23 is formed between the second inner cylinder 22 and the biomass passage 21, so that the biomass and the semicoke are mixed by counter-contact, and then descend in the annular reaction zone 23 to perform co-gasification reaction. In specific implementation, the second inner cylinder 22, namely d-f, can be sleeved outside the biomass channel 21, so that an annular reaction zone 23 is formed between the second inner cylinder 22 and the biomass channel 21, and the semicoke and the biomass are mixed in a d-d interface area to form a material interface; the second inner cylinder 22 is arranged to mix the semicoke and the biomass in a limited space, namely the annular reaction zone 23, for heat transfer, the generated gasified gas, the semicoke and the biomass can be mixed to the maximum extent and fall to the bottom of the second-stage reaction zone 2, so that a higher gas-solid ratio can be ensured, and the biomass is gasified to generate ash slag and gasified gas.
As shown in fig. 1, a third inner tube 24 is provided outside the second inner tube 22 in the second-stage reaction zone 2, that is, e, an air guide interlayer 25 for conveying gasification gas is formed between the third inner tube 24 and the second inner tube 22, a second annular purge gas channel 26 is formed between the third inner tube 24 and the shell of the second-stage reaction zone 2 for conveying purge gas, and the purge gas is conveyed from top to bottom in the second annular purge gas channel 26 and exchanges heat with the gasification gas in the air guide interlayer 25 in the second annular purge gas channel 26, so that the temperature of the purge gas is adapted to the gasification gas phase. In specific implementation, the upper part of the second-stage reaction zone 2 is provided with a biomass channel 21, an annular reaction zone 23, a gas guide interlayer 25 and a second annular purge gas channel 26 which are arranged at the central position from inside to outside in sequence to form a jacket structure. In this embodiment, the bottom of the third drum 24 can be provided with a choke portion 241 to further improve the separation between ash and gasified gas, so that the ash is discharged from the bottom of the choke portion 242.
In the present embodiment, in order to separate ash and gasified air, preferably, an ash splitter 27, i.e. g-h, may be disposed at the bottom of the second-stage reaction zone 2, especially at the lower part of the second inner cylinder 22, and the ash splitter 22 may be disposed on the biomass channel 21, and both may be disposed coaxially, i.e. the ash splitter 27 is disposed below the second inner cylinder 22 on the biomass channel 21, and is used for separating ash and gasified air generated by co-gasification reaction, so that the gasified air moves up and is discharged from the outside of the second inner cylinder 21, thereby reducing the pressure of the gas dust removal section of the post-system and avoiding pollution to the post-system. In order to improve the separation effect between ash and gasified gas, preferably, the outer diameter of the ash splitter disc 27 is larger than the diameter of the second inner cylinder 23 and smaller than the diameter of the third inner cylinder 24, namely, the i-i expanding surface i is positioned at the outer side of the air guide interlayer f-f, namely the second inner cylinder 23, so that the separation of semicoke + biological gasified ash and generated gasified gas is facilitated, and the gasified gas is discharged from the jacket spaces d-d and e-e; the g-g connecting surface between the ash and slag shunting disc 27 and the biomass channel 21 and the f-f plane where the bottom end of the second inner cylinder 22 is located are arranged in parallel, namely the f-f interface and the g-g interface in the second-stage reaction zone are kept flat, so that the separation of semicoke and biological gasification ash and generated gasification gas can be facilitated, and the gasification gas is upwards discharged from the gas guide interlayer.
In this embodiment, the gasified gas, the semicoke and the biomass are dropped to the bottom of the gasifier, that is, the bottom of the second-stage reaction zone 2, outside the biomass channel 21, and because the biomass and the semicoke have low density, the gasified gas is mainly ash, and the ash is accumulated on the bottom of the gasifier, and because the water content of part of the biomass is large, the problem of local hardening and the like may occur. As shown in fig. 2, the upper surface of the ash diverter tray 27 is provided with an air outlet pipe 271 for discharging the purge air to prevent the occurrence of the hardening of the surface of the ash diverter tray 27. During specific implementation, the air outlet pipe 271 can be vertically arranged, so that the air outlet direction of the blowing gas is vertical upward, and the small flow can ensure that ash slag after the semicoke and the biomass are gasified does not harden on the surface of the ash slag diverter plate 27. In order to avoid the interference between gases, the sweeping gas mainly comprises product synthesis gas, inert gas and the like. Wherein, the upper surface of ash tray 27 can be provided with a plurality of air outlet pipes 271, and the arrangement position of air outlet pipes 271 can be determined according to the actual situation, for example, the upper surface of the whole ash tray 27 is arranged at intervals.
In this embodiment, the bottom of the ash tray 27 may be provided with a jacket structure for conveying the purge gas, the biomass, etc. respectively.
As shown in fig. 1, 3 and 4, because the biomass pipe 21 for conveying the biomass upwards is in the semicoke and biomass co-gasification area, the biomass channel is a biomass pneumatic conveying channel, i.e., biomass transport by gas, that is, transport by gas entraining biomass, the area keeps higher gasification temperature (600-, therefore, a first jacket 272 is provided outside the biomass passage 21 below the ash diverter tray 27, i.e., j, which forms an annular cold zone channel 273 with the housing of the biomass channel 21, the cooling medium is used for conveying the biomass conveyed in the biomass channel 21 to cool so as to avoid blockage caused by pyrolysis of the biomass during conveying.
With continued reference to fig. 1, 3 and 4, the outer circumference of the first jacket 272 is sleeved with a second jacket 274, i.e., h-i, and a first annular purge gas channel 275 is formed between the second jacket 274 and the first jacket 272 for inputting purge gas into the gas outlet pipe 271. In specific implementation, the inlet of the second annular purge gas channel 26 is communicated with the first annular purge gas channel 275 to receive the purge gas input by the second annular purge gas channel 26 and send the purge gas upwards; and the outlet of the first annular purge gas channel 275 is communicated with the gas outlet pipe 271 so as to be ejected through the gas outlet pipe 271, that is, the second annular purge gas channel 26 is communicated with the first annular purge gas channel 275, the purge gas is conveyed from top to bottom in the second annular purge gas channel 2, and exchanges heat with the gasified gas in the gas guide interlayer in the second annular purge gas channel 26, so that the purge gas is adapted to the gasified gas phase, and then is input into the gas outlet pipe 271 through the first annular purge gas channel 275 from bottom to top and ejected. Wherein, realize the heat transfer between sweep gas and the gasification gas through second annular sweep gas passageway 26 for the gas temperature is that sweep gas temperature and gasification gas temperature are unanimous (500 ℃) basically, in gas enters into first annular sweep gas passageway 275 from the bottom pipeline, by bottom semicoke + biomass gasification back lime-ash reposition of redundant personnel dish 27 blowout, gas temperature more than 200 ℃, can avoid local semicoke + the granule adhesion and the hardening that moisture and a small amount of tar oil etc. caused in the biomass ash-ash, make moisture and the further pyrolysis of tar midget rid of with reverse air current impact, further avoid becoming the possibility that large granule and hardening are formed.
In this embodiment, the upper surface of the ash diverter tray 27 may be provided with an air outlet pipe 271 at a position corresponding to the first annular purge air passage 275 and/or the annular cold zone passage 273, for example, the air outlet pipe 271 may communicate with the first annular purge air passage 275 through a passage built in the ash diverter tray 27 to realize the flow of the purge air.
In summary, the coupling device for coal powder hydrogasification and biomass pyrolysis provided in this embodiment uses the necking structure 11 as a separation structure for hydrogasification pyrolysis gas and semicoke, the pyrolysis gas generated by the coal powder in the first-stage reaction zone 1 is separated from the semicoke, so that the pyrolysis gas flows upwards to be discharged after being separated, the separated semicoke continuously falls to be discharged, meanwhile, the separation of the pyrolysis gas and the semicoke can lead the pyrolysis gas and the semicoke to be at different temperatures, thereby realizing the rapid cooling of the pyrolysis gas, avoiding the secondary reaction of the pyrolysis gas generated by the primary pyrolysis of hydrogenation, and realizing that the semicoke enters the second section reaction zone 2 at high temperature so as to realize the mixing of the semicoke and the biomass sprayed in the second section reaction zone 2 at high temperature, the hydro-gasification semicoke and the biomass are fully mixed and co-gasified under the condition of the existing furnace length, so that a new way of co-gasification of the biomass and the coal is widened; meanwhile, the biomass is input into the top of the second section reaction zone 2 from bottom to top through the biomass channel 21, and can be input through a spraying mode, namely a downward spraying mode is adopted, so that the biomass and the semicoke are mixed at the top of the second section reaction zone 2 to form a material interface, the mixing of the biomass and the semicoke can be realized through the interface, the falling speed of the semicoke can be reduced through impact on the biomass input from bottom to top, the mixing with the semicoke and the falling time of the semicoke can be increased, and the co-gasification reaction can be more sufficient.
Further, through the arrangement of the ash and slag splitter 27 and the air outlet pipeline 271, the large particles and hardening caused by co-gasification of the semicoke and the biomass can be avoided, the dust-clamping condition of gas is reduced, gas dust removal is realized, pollution to a rear system is avoided, and the pressure of a gas dust removal working section of the rear system is reduced.
It should be noted that in the description of the present invention, the terms of direction or positional relationship indicated by the terms "upper", "lower", "left", "right", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, which are only for convenience of description, and do not indicate or imply that the device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.
Furthermore, it should be noted that, in the description of the present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally 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 by those skilled in the art according to specific situations.
It will be apparent to those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (10)
1. The utility model provides a buggy hydro-gasification and biomass pyrolysis coupling device which characterized in that includes: a first stage reaction zone and a second stage reaction zone; wherein,
the bottom of the first-stage reaction zone is provided with a necking structure and is used for separating pyrolysis gas and semicoke generated by coal hydro-gasification reaction in the first-stage reaction zone so that the pyrolysis gas flows upwards and is discharged, and the semicoke moves downwards and is discharged to the outside of the first-stage reaction zone;
the second-stage reaction zone is arranged below the first-stage reaction zone, and an inlet of the second-stage reaction zone is connected with the necking structure and is used for receiving the semicoke discharged by the necking structure;
and a biomass channel is arranged in the second-stage reaction zone and used for inputting biomass into the second-stage reaction zone from bottom to top so that the biomass descends and carries out co-gasification reaction after being in reverse contact and mixed with the semicoke received at the inlet of the second-stage reaction zone.
2. The coupling device for coal powder hydro-gasification and biomass pyrolysis according to claim 1,
a second inner cylinder is arranged outside the biomass channel in the second section reaction zone, and an annular reaction zone is formed between the second inner cylinder and the biomass channel, so that biomass and semicoke are reversely contacted and mixed, and then descend in the annular reaction zone and carry out co-gasification reaction;
and an ash and slag shunting disc is arranged below the second inner cylinder on the biomass channel and is used for separating ash and gasified gas generated by co-gasification reaction so as to enable the gasified gas to move upwards from the outside of the second inner cylinder and be discharged.
3. The coupling device for coal powder hydro-gasification and biomass pyrolysis according to claim 2,
and an air outlet pipeline is arranged on the upper surface of the ash shunting disc and used for discharging scavenging air so as to prevent the surface of the ash shunting disc from being hardened.
4. The coupling device for coal powder hydro-gasification and biomass pyrolysis according to claim 3,
a first jacket is arranged outside the biomass channel below the ash shunting disc, an annular cold area channel is formed between the first jacket and the shell of the biomass channel and used for conveying a cooling medium so as to cool the biomass conveyed in the biomass channel;
and a first annular scavenging gas channel is arranged on the periphery of the first jacket and used for inputting scavenging gas into the gas outlet pipeline.
5. The coupling device for coal powder hydro-gasification and biomass pyrolysis according to claim 4,
the interior second section reaction zone the outside of second inner tube is equipped with the third inner tube, the third inner tube with form the air guide intermediate layer that is used for carrying the gasification gas between the second inner tube, the third inner tube with form second annular sweeping gas passageway between the casing of second section reaction zone, its with first annular sweeping gas passageway is linked together, and the sweeping gas is in from last transport down in the second annular sweeping gas passageway, and carry out the heat transfer with the gasification gas in the air guide intermediate layer in the second annular sweeping gas passageway to make in sweeping gas temperature and gasification gas phase adaptation, through first annular sweeping gas passageway input to the pipeline of giving vent to anger, spout.
6. The coupling device for coal powder hydro-gasification and biomass pyrolysis according to claim 4,
the outer diameter of the ash shunting disc is larger than the diameter of the second inner cylinder and smaller than the diameter of the third inner cylinder, and a necking part is arranged at the bottom of the third inner cylinder.
7. The coupling device for coal powder hydro-gasification and biomass pyrolysis according to claim 2,
and the ash and slag shunting disc is arranged in parallel and level with the plane of the connecting surface between the biomass channel and the bottom end of the second inner cylinder.
8. The coupling device for coal powder hydro-gasification and biomass pyrolysis according to any one of claims 1 to 7, wherein the throat structure comprises: a first throat and a second throat; wherein,
the second necking is arranged below the first necking, and at least part of the second necking is arranged in the second-stage reaction zone and used for preventing gas in the second-stage reaction zone from rising into the first-stage reaction zone.
9. The coupling device for coal powder hydro-gasification and biomass pyrolysis according to any one of claims 1 to 7,
the coal gasification device is characterized in that a first inner cylinder is arranged in the first section reaction area, the first section reaction area is divided into a reaction area in the cylinder and an annular exhaust area, coal powder input into the first section reaction area is subjected to coal hydro-gasification reaction in the reaction area in the cylinder, generated pyrolysis gas is separated from semicoke, the separated pyrolysis gas flows upwards and is discharged from the annular exhaust area, and the separated semicoke falls and is discharged from the necking structure.
10. The coupling device for coal powder hydro-gasification and biomass pyrolysis according to any one of claims 1 to 7,
and the upper part of the shell of the first-stage reaction zone is provided with an exhaust port, and the exhaust port is provided with a chilling gas device for chilling pyrolysis gas.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN116116843A (en) * | 2023-01-09 | 2023-05-16 | 西安西热锅炉环保工程有限公司 | Device for cleaning biomass powder at bottom of biomass silo |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116116843A (en) * | 2023-01-09 | 2023-05-16 | 西安西热锅炉环保工程有限公司 | Device for cleaning biomass powder at bottom of biomass silo |
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