CN215162419U - Circulating fluidized bed gasification device - Google Patents
Circulating fluidized bed gasification device Download PDFInfo
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- CN215162419U CN215162419U CN202120673107.8U CN202120673107U CN215162419U CN 215162419 U CN215162419 U CN 215162419U CN 202120673107 U CN202120673107 U CN 202120673107U CN 215162419 U CN215162419 U CN 215162419U
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Abstract
The utility model discloses a circulating fluidized bed gasification device, this circulating fluidized bed gasification device include fluidized bed reactor and gas-solid separation and system of returning. The fluidized bed reactor is provided with a first-stage gasifying agent inlet, a second-stage gasifying agent inlet and a mixture outlet, and the inner space of the fluidized bed reactor is divided into a dilute phase zone and a dense phase zone which are distributed from top to bottom; wherein the first stage gasification agent inlet is communicated with the dense phase zone; the second-stage gasifying agent inlet is communicated with the dilute phase zone; the mixture outlet is arranged at the top of the fluidized bed reactor. The gas-solid separation and return system is provided with a mixture inlet, a solid material outlet and a coal gas outlet, wherein the mixture inlet is communicated with the mixture outlet; the solid material outlet is communicated with the fluidized bed reactor. The utility model provides a problem of easy slagging scorification among the fluidized bed reactor operation process, when the flying dust is recycled, is improved flying dust conversion rate, can prolong the continuous stable operation cycle of device.
Description
Technical Field
The utility model belongs to the technical field of coal gasification, especially, relate to a circulating fluidized bed gasification equipment.
Background
The circulating fluidized bed coal gasification technology is a clean coal conversion technology, and has the advantages of strong coal adaptability, sufficient gas-solid mixing, high gasification reaction rate, uniform reaction temperature and the like, so that the circulating fluidized bed coal gasification technology is widely applied to the fields of industrial gas, synthetic ammonia and coal-made bulk chemicals. However, in the actual operation process of the circulating fluidized bed gasification furnace, there is a problem of large amount of fly ash, the amount of ash discharged out of the fluidized bed reactor in the form of fly ash accounts for 60-80% of the total ash amount, the carbon content in fly ash is between 30-60%, if the fly ash can not be reused, not only energy waste is caused, but also the fly ash disposal is difficult.
In the prior art, a high-efficiency cyclone separator and a dust remover are adopted to capture and recycle fly ash, and the main utilization ways are as follows: (1) burning, separating fine ash from the product gas, and feeding the separated fine ash into a boiler for burning to generate hot flue gas for producing water vapor or generating electricity; (2) secondary gasification, separating fine ash from the product gas, sending the separated fine ash into the entrained-flow bed reactor for high-temperature secondary gasification, introducing the generated gas into the entrained-flow bed reactor, and discharging ash from the lower part of the entrained-flow bed; (3) returning the fly ash to the fluidized bed reactor, forming a local high-temperature area in a dense-phase area at the bottom of the fluidized bed reactor, and converting the fly ash in the high-temperature area at the dense-phase area at the bottom of the fluidized bed reactor.
Although the reuse rate of the fly ash can be improved by adopting combustion and secondary gasification, an additional conversion device is required, so that the process is complex and the operation cost is increased; when the fly ash is returned to the fluidized bed reactor to form a high-temperature area in the dense-phase area for conversion, the dense-phase area has high material concentration and high material ash content (test results show that the material ash content is high and easy to slag, and the carbon content is high and difficult to slag under the same temperature condition) easily causes heat accumulation and slag bonding in an area with poor local fluidization, thereby influencing the long-period stable operation of the fluidized bed reactor.
SUMMERY OF THE UTILITY MODEL
Technical problem to be solved
In view of this, the utility model provides a circulating fluidized bed gasification equipment to solve among the prior art fluidized bed reactor bottom dense phase district easily the slagging scorification, can't realize the problem of fluidized bed reactor long period steady operation.
(II) technical scheme
The utility model provides a circulating fluidized bed gasification equipment, including fluidized bed reactor and gas-solid separation and the system of returning.
The fluidized bed reactor is provided with a first-stage gasifying agent inlet, a second-stage gasifying agent inlet and a mixture outlet, and the inner space of the fluidized bed reactor is divided into a dilute phase zone and a dense phase zone which are distributed from top to bottom; wherein the first stage gasification agent inlet is communicated with the dense phase zone; the second-stage gasifying agent inlet is communicated with the dilute phase zone; the mixture outlet is arranged at the top of the fluidized bed reactor.
The gas-solid separation and return system is provided with a mixture inlet, a solid material outlet and a coal gas outlet, wherein the mixture inlet is communicated with the mixture outlet; the solid material outlet is communicated with the fluidized bed reactor.
Optionally, the gas-solid separation and return system comprises: cyclone separator, returning charge ware, gas-solid separator, flying dust storage tank and flying dust conveyor.
The mixture inlet is arranged at the inlet of the cyclone separator, the solid material outlet comprises a primary returning port arranged at the outlet of the material returning device and a fly ash returning port communicated with the outlet of the fly ash conveying device, the primary returning port and the fly ash returning port are communicated with the inside of the fluidized bed reactor, and the coal gas outlet is arranged at the upper part of the gas-solid separation device. The gas phase outlet of the cyclone separator is communicated with the inlet of the gas-solid separation device, and the solid phase outlet of the cyclone separator is communicated with the inlet of the material returning device. The solid phase outlet of the gas-solid separation device is communicated with the inlet of the fly ash storage tank, and the outlet of the fly ash storage tank is communicated with the inlet of the fly ash conveying device.
Optionally, the primary returning port is communicated with a returning port arranged on the side wall of the fluidized bed reactor through a returning pipe; the fly ash returning port is arranged on the returning pipe and communicated with the returning pipe.
Optionally, an included angle α between a central axis of the fly ash returning port and a central axis of the return pipe is in a range of: 15 to 90 degrees.
Optionally, the primary returning port is communicated with a returning port arranged on the side wall of the fluidized bed reactor through a returning pipe; the fly ash returning port is arranged on the side wall of the fluidized bed reactor and is communicated with the dense phase region.
Optionally, the included angle β between the central axis of the fly ash returning port and the vertical central axis of the fluidized bed reactor is in the range of: 90 to 170 degrees.
Optionally, the primary returning port is communicated with a returning port arranged on the side wall of the fluidized bed reactor through a returning pipe; the fly ash returning port is arranged on the side wall of the fluidized bed reactor and is communicated with the dilute phase region.
Optionally, the secondary gasification agent inlet and the fly ash return port are integrated to form an inner and outer ring nozzle structure inlet, the inner ring of the inner and outer ring nozzle structure inlet is a fly ash conveying channel, and the outer ring of the inner and outer ring nozzle structure inlet is a secondary gasification agent conveying channel.
Optionally, the included angle γ between the central axis of the fly ash returning port and the axial central axis of the fluidized bed reactor is in the range of: 20 to 160 degrees.
Optionally, the number of the second-stage gasifying agent inlets is multiple, one or more layers of the second-stage gasifying agent inlets are arranged along the axial direction of the fluidized bed reactor, and the multiple second-stage gasifying agent inlets in each layer of the second-stage gasifying agent inlets are uniformly distributed and arranged along the circumferential direction of the fluidized bed reactor.
(III) advantageous effects
The utility model provides a circulating fluidized bed gasification equipment, with one-level gasification agent entry and fluidized bed reactor's dense phase district intercommunication, with second grade gasification agent entry and fluidized bed reactor's dilute phase district intercommunication, can realize letting in one-level gasification agent fluidized bed reactor's dense phase district, with oxygen-containing second grade gasification agent's dilute phase district, and then realize the ratio through adjustment one-level gasification agent and second grade gasification agent, make the interior temperature of stove be gradient distribution, the dense phase district of the easy slagging of control is at relatively lower temperature (being less than the softening temperature 150 ℃ of coal), the dilute phase district of the difficult slagging of is moved under higher temperature (the softening temperature point at the coal). Because the dilute phase zone is a fine particle material with higher carbon content, the material with high carbon concentration is not easy to bond, thereby being capable of safely and stably operating at higher temperature, solving the problem that the fluidized bed reactor is easy to slag during the operation process, realizing the reutilization of the fly ash, improving the conversion rate of the fly ash and simultaneously prolonging the continuous and stable operation period of the device.
In addition, compare in prior art adoption burning and secondary gasification's mode, the utility model provides a circulating fluidized bed gasification equipment under the condition that does not need extra equipment, has realized the flying dust and has recycled, simple process, and is with low costs.
Drawings
FIG. 1 is a schematic structural view of a circulating fluidized bed gasification apparatus according to an embodiment of the present invention.
Fig. 2 is a schematic structural view of a circulating fluidized bed gasification apparatus according to another embodiment of the present invention.
Fig. 3 is a schematic structural view of a circulating fluidized bed gasification apparatus according to another embodiment of the present invention.
Fig. 4 is a schematic structural view of a circulating fluidized bed gasification apparatus according to another embodiment of the present invention.
Description of reference numerals:
1. a fluidized bed reactor; 11. a dilute phase zone; 12. a dense phase zone; 13. a first-stage gasifying agent inlet; 14. a secondary gasification agent inlet; 15. a mixture outlet; 16. a feed pipe; 17. a slag discharge port; 18. returning the material port; 2. a gas-solid separation and return system; 20. a coal gas outlet; 21. a mixture inlet; 22. a solid material outlet; 211. a cyclone separator; 212. a material returning device; 213. a primary return port; 214. a material returning pipe; 221. a gas-solid separation device; 222. a fly ash storage tank; 223. a fly ash conveying device; 224. a fly ash return port; 3. an air distribution device.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in detail with reference to the accompanying drawings.
In realizing the utility model discloses an in-process discovery, flying dust reactivity is poor, will realize abundant conversion, need improve gasification temperature, and fluidized bed reactor 1 bottom dense phase district 12 gasification temperature has brought the risk of bed material reunion slagging scorification after rising, leads to fluidized bed reactor 1 behind the slagging scorification in the high temperature district to arrange the sediment pipeline and block up a large amount of bed materials, can't arrange the sediment and forced the parking. Above the dense phase zone 12 is a fine particulate material with a relatively high carbon content, which is not easily bonded, and thus can be safely and stably operated at a relatively high temperature. Based on this, in order to solve among the prior art fluidized bed reactor 1 bottom dense phase district 12 easy slagging scorification, can't realize the problem of the long period steady operation of fluidized bed reactor 1, the utility model provides a circulating fluidized bed gasification equipment.
FIG. 1 is a schematic structural view of a circulating fluidized bed gasification apparatus according to an embodiment of the present invention. As shown in fig. 1, the utility model provides a circulating fluidized bed gasification device, including two fluidized bed reactors 1 and gas-solid separation and return system 2 that are linked together.
The fluidized bed reactor 1 is provided with a first-stage gasifying agent inlet 13, a second-stage gasifying agent inlet 14 and a mixture outlet 15, and the inner space of the fluidized bed reactor 1 is divided into a dilute phase zone 11 and a dense phase zone 12 which are distributed from top to bottom; wherein, a primary gasifying agent inlet 13 is communicated with the dense-phase zone 12; the secondary gasification agent inlet 14 is communicated with the dilute phase zone 11; the mixture outlet 15 is provided at the top of the fluidized bed reactor 1.
The gas-solid separation and return system 2 is provided with a mixture inlet 21, a solid material outlet 22 and a coal gas outlet 20, wherein the mixture inlet 21 is communicated with the mixture outlet 15; the solid material outlet 22 communicates with the fluidized-bed reactor 1.
According to the embodiment of the present invention, the boundary line position of the dilute phase zone 11 and the dense phase zone 12 inside the fluidized bed reactor 1 is determined by measuring the pressure difference inside the fluidized bed reactor 1 in the operating state, the dense phase zone 12 has higher material concentration, and the pressure is greater than the pressure of the dilute phase zone 11. The bottom of the fluidized bed reactor 1 is also provided with an air distribution device 3, the side wall of the fluidized bed reactor 1 is provided with a feeding pipe 16 communicated with the dense-phase zone 12 and used for conveying fuel to the fluidized bed reactor 1, the air distribution device 3 is communicated with a first-stage gasifying agent inlet 13, and the bottom of the fluidized bed reactor 1 is also provided with a slag discharge port 17 used for discharging slag. The fuel is sent into a dense-phase zone 12 at the bottom of the fluidized bed reactor 1, oxygen-containing primary gasifying agent (water vapor, oxygen/air) is sent through a primary gasifying agent inlet 13 and an air distribution device 3 to form a local high-temperature zone, the fuel and the primary gasifying agent are in countercurrent contact and then carry out gasification reaction, solid bottom slag after the gasification reaction is discharged from a slag discharge port 17, part of solid particles carried by the gas leave from a mixture outlet 15 at the top of the fluidized bed reactor 1 and enter a gas-solid separation and return system 2 along a mixture inlet 21, fly ash returns to the inside of the fluidized bed reactor 1 along a solid material outlet 22 for secondary reaction after the gas-solid separation and return system 2 is subjected to the gas-solid separation, and coal gas is discharged along a coal gas outlet 20. In order to promote the conversion of the fly ash, a secondary gasifying agent (water vapor, oxygen/air) containing oxygen is fed into the secondary gasifying agent inlet 14 to form a local high-temperature area to promote the conversion of the fly ash.
The utility model discloses in, the dense phase district 12 that the one-level gasification agent lets in fluidized bed reactor 1, the dilute phase district 11 that the second grade gasification agent lets in fluidized bed reactor 1, oxygen content ratio through adjustment one-level gasification agent and second grade gasification agent (wherein oxygen content is 17% ~ 25% in the one-level gasification agent, oxygen content is 40% ~ 70% in the second grade gasification agent), make the stove internal temperature be gradient distribution, the dense phase district 12 of control easy slagging scorification is at relatively lower temperature (being less than the softening temperature 150 ℃ of coal), the dilute phase district 11 of difficult slagging scorification moves under higher temperature (the softening temperature point of coal).
The utility model provides a circulating fluidized bed gasification equipment, with one-level gasifying agent entry 13 and fluidized bed reactor 1's dense phase zone 12 intercommunication, with second grade gasifying agent entry 14 and fluidized bed reactor 1's dilute phase zone 11 intercommunication, can realize letting in fluidized bed reactor 1's dense phase zone 12 with one-level gasifying agent, with the dilute phase zone 11 that oxygen-bearing second grade gasifying agent lets in fluidized bed reactor 1, and then the realization is through the ratio of adjusting one-level gasifying agent and second grade gasifying agent, makes the interior temperature of stove be the gradient distribution. Because the dilute phase zone 11 is a fine particle material with higher carbon content, the material with high carbon concentration is not easy to bond, thereby being capable of safely and stably operating at higher temperature, solving the problem that the fluidized bed reactor 1 is easy to slag during the operation process, realizing the reutilization of the fly ash, improving the conversion rate of the fly ash and simultaneously prolonging the continuous and stable operation period of the device.
In addition, compare in prior art adoption burning and secondary gasification's mode, the utility model provides a circulating fluidized bed gasification equipment under the condition that does not need extra equipment, has realized the flying dust and has recycled, simple process, and is with low costs.
Fig. 2, 3 and 4 are schematic structural diagrams of a circulating fluidized bed gasification device according to other embodiments of the invention. As shown in fig. 2, 3, 4, optionally, the gas-solid separation and return system 2 comprises: a cyclone 211, a return feeder 212, a gas-solid separation device 221, a fly ash storage tank 222 and a fly ash conveying device 223.
The mixture inlet 21 is arranged at the inlet of the cyclone separator 211, the solid material outlet 22 comprises a primary return port 213 arranged at the outlet of the material returning device 212 and a fly ash return port 224 communicated with the outlet of the fly ash conveying device 223, the primary return port 213 and the fly ash return port 224 are communicated with the inside of the fluidized bed reactor 1, and the coal gas outlet 20 is arranged at the dilute phase outlet of the gas-solid separation device 221. The dilute phase outlet of the cyclone 211 is communicated with the inlet of the gas-solid separation device 221, and the concentrated phase outlet of the cyclone 211 is communicated with the inlet of the material returning device 212. The dense phase outlet of the gas-solid separation device 221 is communicated with the inlet of the fly ash storage tank 222, and the outlet of the fly ash storage tank 222 is communicated with the inlet of the fly ash conveying device 223.
The specific process implementation process of the utility model specifically comprises: fuel, such as qualified particle size pulverized coal (0-10mm), is fed into a dense phase zone 12 at the bottom of a fluidized bed reactor 1 from a feeding pipe 16, and is fed into an oxygen-containing primary gasifying agent (a mixed gas of water vapor and oxygen/air with the oxygen content of 17-25%) through a primary gasifying agent inlet 13 and an air distribution device 3 to form a local high temperature zone, the fuel and the primary gasifying agent are in countercurrent contact and then undergo gasification reaction, solid bottom slag after the gasification reaction is discharged from a slag discharge outlet 17, part of solid particles carried by the gas leave from a mixture outlet 15 at the top of the fluidized bed reactor 1, enter along a mixture inlet 21 and sequentially pass through a cyclone 211 and a gas-solid separation device 221 to realize gas-solid separation, solid materials separated by the cyclone 211 are returned into the fluidized bed reactor 1 through a return feeder 212 to undergo a circulating reaction, smaller solid particles not collected by the cyclone 211 enter the gas-solid separation device 221 in the form of fly ash to realize gas-solid separation, the fly ash separated by the gas-solid separation device 221 enters the fly ash storage tank 222, and is sent back to the fluidized bed reactor 1 by the fly ash conveying device 223 for secondary reaction, and the coal gas is discharged along the coal gas outlet 20. In order to promote the conversion of the fly ash, an oxygen-containing secondary gasifying agent (the mixed gas of water vapor and oxygen/air with the oxygen content of 40-70%) is fed along the secondary gasifying agent inlet 14 to form a local high-temperature region to promote the conversion of the fly ash, and the fly ash can complete the gasification conversion after passing through the high-temperature region, thereby realizing the recovery of carbon in the fly ash.
The fluidized bed reactor 1 is a coal gasification reaction device, and realizes the gasification of coal, circulating materials and fly ash and the discharge of bottom slag; the cyclone 211 and the gas-solid separation device 221 are used for collecting different particle solid materials in the coal gas and separating the gas-solid materials; the material returning device 212 returns the coarse particle materials separated by the cyclone separator 211 to the fluidized bed reactor; the fly ash storage tank 222 is used for storing fly ash separated by the gas-solid separation device 221; the fly ash conveying system is used for quantitatively returning the fine particle fly ash separated by the gas-solid separation device 221; the primary gasifying agent inlet 13 is used for introducing a primary gasifying agent, and the fluidization of solid materials in the reactor is maintained while the gasification reaction is carried out; the second-stage gasifying agent inlet 14 is used for introducing a second-stage gasifying agent, and a high-temperature area is formed in the dilute phase area 11 of the fluidized bed reactor 1 to promote the conversion of fine particle materials.
The uniform, continuous and stable conveying of the fly ash is the premise of stable operation of the fluidized bed reactor 1, the fly ash conveying system can adopt a feeder to control the feeding amount of the fly ash, and a conveying gas is communicated with an outlet pipeline of the feeder to convey the fly ash into the fluidized bed reactor 1.
According to the embodiment of the utility model, the fly ash generated by gasification is collected and then sent back to the fluidized bed reactor 1, and the transformation of carbon in the fly ash is realized by introducing an oxygen-containing gasification agent into the dilute phase zone 11 of the fluidized bed reactor 1 to form a high temperature zone. The device creates different temperature fields aiming at the difference of material reaction activity in different areas in the furnace, and ensures the long-period continuous and stable operation of the gasification furnace while realizing the conversion of fly ash.
According to the utility model discloses an embodiment, the flying dust contains the fine particle material of part fixed carbon after the multiple cycle in fluidized bed reactor 1, and its reactivity compares greatly reduced with the raw coal, needs higher temperature could reach high carbon conversion rate, therefore the flying dust return to fluidized bed reactor 1 in the back, needs to react under higher temperature. From the viewpoint of stable operation, it is preferable that the high-temperature zone is disposed in the dilute-phase zone 11 above the dense-phase zone 12. The fly ash returned to the initial position of the fluidized bed reactor 1 does not need to be in the dilute phase zone 11, and can be returned to the return pipe 214, the dense phase zone 12 at the upper part of the air distribution device 3 of the fluidized bed reactor 1, or directly returned to the dilute phase zone 11 above the dense phase zone 12.
In the embodiment shown in fig. 2, optionally, the primary returning port 213 is communicated with a returning port 18 arranged on the sidewall of the fluidized bed reactor 1 through a returning pipe 214; the fly ash returning port 224 is disposed on the return pipe 214, and the fly ash returning port 224 is communicated with the return pipe 214, and the fly ash returns to the fluidized bed reactor 1 through the fly ash returning port 224 and the return pipe 214.
Optionally, the fly ash returning opening 224 is a straight pipe section, the return pipe 214 is an inclined pipe section, and an included angle α between a central axis of the fly ash returning opening 224 and a central axis of the return pipe 214 is within a range of: 15 to 90 degrees. The fly ash contacts with a large amount of circulating materials in the return pipe 214 and is rapidly heated, so that the residence time in the furnace is increased, and the conversion of carbon in the fly ash is facilitated.
In the embodiment shown in fig. 3, optionally, the primary returning port 213 is communicated with a returning port 18 arranged on the sidewall of the fluidized bed reactor 1 through a returning pipe 214; the fly ash returning port 224 is disposed on the sidewall of the fluidized bed reactor 1, and the fly ash returning port 224 is communicated with the dense phase zone 12 and can be disposed between the air distribution device 3 and the material returning port 18.
Optionally, the fly ash returning port 224 is a straight pipe section, the flow direction is inclined upward, and the included angle β between the central axis of the fly ash returning port 224 and the vertical central axis of the fluidized bed reactor 1 is within the range: 90 to 170 degrees.
The fly ash enters the dense-phase region 12 at the speed of 15-20m/s under the carrying of the conveying gas, the gas-solid material moving at high speed increases the back mixing of the dense-phase region 12 at the bottom of the fluidized bed reactor 1, the bottom flow field is strengthened, and meanwhile, the fly ash exchanges heat with the high-temperature material in the dense-phase region 12, so that the fly ash is heated, the dense-phase region 12 runs in a relatively low-temperature environment, and the slagging risk is reduced. After the temperature of the fly ash is raised through the heat exchange in the dense-phase zone 12, the fly ash enters the dilute-phase zone 11 to contact with a secondary gasifying agent for further reaction at a higher temperature.
In the embodiment shown in fig. 4, optionally, the primary returning port 213 is communicated with a returning port 18 arranged on the sidewall of the fluidized bed reactor 1 through a returning pipe 214; a fly ash returning port 224 is provided on the side wall of the fluidized-bed reactor 1, and the fly ash returning port 224 communicates with the dilute phase zone 11, and optionally, the fly ash returning port 224 is provided above the feed pipe 16 or at substantially the same level as the secondary gasifying agent inlet 14.
Optionally, for the coal with poor reactivity, the secondary gasification agent inlet 14 and the fly ash returning port 224 are integrated to form an inner and outer ring nozzle structure inlet, one or more inlets may be provided according to different process conditions, and a plurality of inlets are uniformly arranged along the circumference of the fluidized bed reactor 1. The inner ring of the inlet of the inner and outer ring nozzle structure is a fly ash conveying channel, and the outer ring of the inlet of the inner and outer ring nozzle structure is a secondary gasifying agent conveying channel. The second-stage gasifying agent inlet 14 and the fly ash returning port 224 are integrated into one inlet, so that the fly ash and the second-stage gasifying agent can be fully contacted, the fly ash and the gasifying agent can be fully contacted to form a local high-temperature area by forming an inner-outer ring nozzle structure, the carbon in the fly ash is promoted to be rapidly converted, the second-stage gasifying agent is enabled to react with the fly ash to the maximum extent, and the gasifying agent and H in the furnace are reduced2、CO、CH4And the reaction of the effective gas improves the components of the effective gas in the coal gas.
Optionally, the fly ash returning port 224 is a straight pipe section, and an included angle γ between a central axis of the fly ash returning port 224 and a vertical central axis of the fluidized bed reactor 1 is in a range of: 20 to 160 degrees.
According to an embodiment of the present invention, the structure and operating parameters of the fly ash return port 224 vary with the return position. One or more fly ash returning ports 224 may be provided according to the amount of gasified fly ash, and a symmetrical arrangement may be selected when a plurality of returning ports are provided.
To extend the residence time of the fly ash, the secondary gasification agent inlet 14 may optionally be a tangential configuration. In addition, optionally, the number of the secondary gasification agent inlets 14 is multiple, and according to the difference of coal reactivity, the number of the secondary gasification agent inlets 14 is one or more layers along the axial direction of the fluidized bed reactor 1, each layer is 2-8, and the secondary gasification agent inlets 14 in each layer of the secondary gasification agent inlets 14 are uniformly distributed and arranged along the circumferential direction of the fluidized bed reactor 1.
The above-mentioned embodiments, further detailed description of the objects, technical solutions and advantages of the present invention, it should be understood that the above-mentioned embodiments are only specific embodiments of the present invention, and are not intended to limit the present invention, and any modifications, equivalent substitutions, improvements, etc. made within the spirit and principle of the present invention should be included in the scope of the present invention.
Claims (10)
1. A circulating fluidized bed gasification apparatus, comprising:
the fluidized bed reactor (1) is provided with a first-stage gasifying agent inlet (13), a second-stage gasifying agent inlet (14) and a mixture outlet (15), and the inner space of the fluidized bed reactor (1) is divided into a dilute phase zone (11) and a dense phase zone (12) which are distributed from top to bottom; wherein the primary gasification agent inlet (13) is communicated with the dense phase zone (12); the secondary gasification agent inlet (14) is communicated with the dilute phase zone (11); the mixture outlet (15) is arranged at the top of the fluidized bed reactor (1);
the gas-solid separation and return system (2) is provided with a mixture inlet (21), a solid material outlet (22) and a coal gas outlet (20), wherein the mixture inlet (21) is communicated with the mixture outlet (15); the solid material outlet (22) is communicated with the fluidized bed reactor (1).
2. The apparatus according to claim 1, wherein the gas-solid separation and return system (2) comprises:
a cyclone separator (211), a material returning device (212), a gas-solid separation device (221), a fly ash storage tank (222) and a fly ash conveying device (223);
the mixture inlet (21) is arranged at an inlet of the cyclone separator (211), the solid material outlet (22) comprises a primary returning port (213) arranged at an outlet of the material returning device (212) and a fly ash returning port (224) communicated with an outlet of the fly ash conveying device (223), the primary returning port (213) and the fly ash returning port (224) are communicated with the fluidized bed reactor (1), and the coal gas outlet (20) is arranged at the upper part of the gas-solid separation device (221);
the gas phase outlet of the cyclone separator (211) is communicated with the inlet of the gas-solid separation device (221), and the solid phase outlet of the cyclone separator (211) is communicated with the inlet of the material returning device (212);
the solid phase outlet of the gas-solid separation device (221) is communicated with the inlet of the fly ash storage tank (222), and the outlet of the fly ash storage tank (222) is communicated with the inlet of the fly ash conveying device (223).
3. The apparatus of claim 2, wherein: the primary return port (213) is communicated with a return port (18) arranged on the side wall of the fluidized bed reactor (1) through a return pipe (214); the fly ash returning port (224) is arranged on the returning pipe (214), and the fly ash returning port (224) is communicated with the returning pipe (214).
4. The apparatus of claim 3, wherein: the range of an included angle alpha between the central axis of the fly ash returning port (224) and the central axis of the returning pipe (214) is as follows: 15 to 90 degrees.
5. The apparatus of claim 2, wherein: the primary return port (213) is communicated with a return port (18) arranged on the side wall of the fluidized bed reactor (1) through a return pipe (214); the fly ash returning opening (224) is arranged on the side wall of the fluidized bed reactor (1), and the fly ash returning opening (224) is communicated with the dense-phase zone (12).
6. The apparatus of claim 5, wherein: the range of an included angle beta between the central axis of the fly ash returning port (224) and the vertical central axis of the fluidized bed reactor (1) is as follows: 90 to 170 degrees.
7. The apparatus of claim 2, wherein: the primary return port (213) is communicated with a return port (18) arranged on the side wall of the fluidized bed reactor (1) through a return pipe (214); the fly ash returning port (224) is arranged on the side wall of the fluidized bed reactor (1), and the fly ash returning port (224) is communicated with the dilute phase zone (11).
8. The apparatus of claim 7, wherein: the secondary gasification agent inlet (14) and the fly ash returning port (224) are integrated to form an inner ring and outer ring nozzle structure inlet, the inner ring of the inner ring and outer ring nozzle structure inlet is a fly ash conveying channel, and the outer ring of the inner ring and outer ring nozzle structure inlet is a secondary gasification agent conveying channel.
9. The apparatus of claim 7, wherein: the range of an included angle gamma between the central axis of the fly ash returning port (224) and the vertical central axis of the fluidized bed reactor (1) is as follows: 20 to 160 degrees.
10. The apparatus of claim 1 or 2, wherein: the secondary gasification agent inlets (14) are multiple, one or multiple layers of the secondary gasification agent inlets (14) are arranged along the axial direction of the fluidized bed reactor (1), and the secondary gasification agent inlets (14) in each layer of the secondary gasification agent inlets (14) are uniformly distributed and arranged along the circumferential direction of the fluidized bed reactor (1).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202120673107.8U CN215162419U (en) | 2021-04-01 | 2021-04-01 | Circulating fluidized bed gasification device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202120673107.8U CN215162419U (en) | 2021-04-01 | 2021-04-01 | Circulating fluidized bed gasification device |
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| CN215162419U true CN215162419U (en) | 2021-12-14 |
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2021
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