CN214830161U - Solid fuel pretreatment device and utilization device - Google Patents
Solid fuel pretreatment device and utilization device Download PDFInfo
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- CN214830161U CN214830161U CN202121182882.XU CN202121182882U CN214830161U CN 214830161 U CN214830161 U CN 214830161U CN 202121182882 U CN202121182882 U CN 202121182882U CN 214830161 U CN214830161 U CN 214830161U
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Abstract
The utility model provides a solid fuel preprocessing device, including cloth wind section and broken section, wherein: the air distribution section is of a cylindrical structure and comprises a bottom part and a top part, the bottom part is gradually enlarged towards the top part, and the crushing section is of a cylindrical structure and is communicated with the top part of the air distribution section; the bottom of the air distribution section is provided with an air distribution device, and the side wall of the air distribution section is provided with a plurality of secondary air pipes for distributing air to the solid fuel pretreatment device; the broken section includes interconnect's straight section of thick bamboo section and round platform section, and straight section of thick bamboo section intercommunication air distribution section, many broken tuber pipes have been arranged to straight section of thick bamboo section lateral wall for let in broken wind in to the broken section, the feed inlet has been arranged to round platform section lateral wall, and the top of round platform section is provided with the discharge gate, is used for exporting the fuel of preliminary treatment. The utility model also provides a solid fuel utilizes device. The utility model discloses a structure and the design of cloth wind form the broken and tangential broken field of granule collision, and the millimeter level granule that will give into is broken for the hot carbonaceous solid powder of micron order.
Description
Technical Field
The utility model relates to a fuel energy chemical industry technical field, concretely relates to solid fuel preprocessing device and utilize device.
Background
The traditional pulverized coal combustion or dry powder gasification technology requires that raw material coal needs to be dried and pulverized, so that the production cost is greatly improved, and the coal type adaptability of the pulverized coal combustion and dry powder gasification technology is reduced.
In addition, when anthracite with lower activity and semicoke with low volatile content are used as fuels, the problems of insufficient combustion, low burnout rate and the like generally exist in the traditional pulverized coal combustion technology. Although preheat combustion technology improves the combustion efficiency of such carbonaceous fuels by preheating, a drying and pulverizing unit is still required. In addition, the fluidized bed preheater needs to add additional bed materials for preheating the powdery carbon-containing solid fuel due to the limitation of the flow characteristics of the fluidized bed preheater, and has higher requirements on operation control. When anthracite with lower activity and semicoke with low volatile content are used as gasification raw materials, the dry powder gasification technology has the problems of low carbon conversion rate and the like. The preheating gasification is a gasification technology which adopts a preheating mode to firstly carry out the preliminary gasification of drying, pyrolysis, modification and the like on the carbon-containing solid fuel, and then introduce the coal gas generated by the preliminary gasification and the incompletely reacted modified semicoke into an entrained flow bed for carrying out high-temperature gasification reaction. The gasification technology can greatly reduce the requirements on the particle size and the water content of the coal as fired, and correspondingly reduces the cost for preparing gas by coal gasification. Therefore, some researchers at home and abroad research and apply engineering to preheating gasification. However, the problems of large particle size of semicoke entering an entrained flow bed, low solid material concentration, low carbon conversion rate and the like exist in the prior preheating gasification.
The independent treatment investment and operation cost of organic waste which is generated in coal chemical industry and is difficult to treat, such as organic waste liquid, tar, carbon-containing waste residue, oil residue and the like are very high, the dry powder entrained flow bed cannot treat the organic waste liquid, and the coal water slurry can treat part of the organic waste liquid, but the slurry forming performance of the coal water slurry and the operation stability of a gasification furnace can be influenced.
SUMMERY OF THE UTILITY MODEL
Technical problem to be solved
The utility model provides a solid fuel preprocessing device and utilize device to solve the raw materials coal that exists among the prior art or preheat the combustion technology and all need pass through drying and powder process, traditional pulverized coal combustion technology combustion efficiency is on the low side and gasification carbon conversion rate is on the low side, and current preheat the combustion technology and need additionally supply the bed material, and the not good technical problem of preprocessing effect.
(II) technical scheme
An aspect of the utility model provides a solid fuel preprocessing device, including cloth wind section 1 and broken section 2, wherein: the air distribution section 1 is of a cylindrical structure and comprises a bottom part and a top part, the bottom part is gradually enlarged towards the top part, and the crushing section 2 is of a cylindrical structure and is communicated with the top part of the air distribution section 1; the bottom of the air distribution section 1 is provided with an air distribution device 11, and the side wall of the air distribution section 1 is provided with a plurality of secondary air pipes 13 for distributing air to the solid fuel pretreatment device; broken section 2 includes interconnect's straight section of thick bamboo section and round platform section, and straight section of thick bamboo section intercommunication air distribution section 1, many broken tuber pipes 21 have been arranged to straight section of thick bamboo section lateral wall for let in broken wind in to broken section 2, the feed inlet 22 has been arranged to round platform section lateral wall, and the top of round platform section is provided with the discharge gate, is used for exporting the fuel of preliminary treatment.
Optionally, the number of the secondary air ducts 13 is at least one, each layer of the secondary air ducts 13 is arranged into at least two layers and is located on the same cross section of the air distribution section 1, and a projection of a central axis of each layer of the secondary air ducts 13 in the horizontal direction is tangent to the same preset tangent circle.
Optionally, the radius of the preset tangent circle is between the radius of the air distribution device 11 and the radius of the cross section where the secondary air pipe 13 intersects with the air distribution section 1.
Optionally, the number of the crushing air pipes 21 is at least one, each layer of the crushing air pipes 21 is arranged into at least two layers, and the central axis of the outlet of each crushing air pipe 21 intersects with a point in the straight cylinder section.
Optionally, the central axis of each layer of crushing air pipes 21 is located on the same cross section of the straight cylinder section; wherein each layer of the crushing air pipes 21 is provided with odd number, and the central axis of the outlet of the odd number of the crushing air pipes 21 points to the axis of the straight cylinder section; or, each layer of crushing air pipes 21 is even, and the central axes of the outlets of the even crushing air pipes 21 are collinear in pairs and point to the axis of the straight cylinder section.
Optionally, the number of the crushing air pipes 21 is at least one, each layer of the crushing air pipes 21 is arranged to be even, the central axis of the outlet of each crushing air pipe 21 is located on the same cross section of the straight cylinder section, the central axes of every two adjacent crushing air pipes 21 on each layer of the crushing air pipes 21 intersect at one point, the intersection point is located on the circumference which has the same radius as the air distribution device 11 and has the circle center on the axis of the straight cylinder section, and each layer of the crushing air pipes 21 is in a central symmetry structure.
Optionally, an included angle β between two generatrices of the axial cross section of the air distribution section 1 is 25 to 55 degrees; the included angle alpha between the central axis of the outlet of the secondary air pipe 13 and the cross section of the air distribution section 1 ranges from 0 degree to 75 degrees, and the included angle gamma between the central axis of the outlet of the feeding port 22 and the cross section of the crushing section 2 ranges from 45 degrees to 75 degrees.
Optionally, the side wall of the air distribution section 1 close to the bottom is further provided with a slag discharge port 12, and the side wall of the circular truncated cone section of the crushing section 2 is further provided with a material return port 23.
Optionally, the solid fuel pretreatment device further comprises a transportation section 3, a gas-solid separator 4 and a material returning device 5 which are sequentially communicated, wherein: the conveying section 3 is communicated with the discharge port, the top of the conveying section 3 is provided with a conveying section outlet 32, the gas-solid separator 4 is provided with a gas-solid phase inlet 41, a gas-solid phase outlet 43 and a solid phase outlet 42, the conveying section outlet 32 is connected with the gas-solid phase inlet 41, the material returning device 5 is provided with a material returning inlet 51 communicated with the solid phase outlet 42, and a material returning outlet 52 communicated with the material returning port 23 is further arranged.
Optionally, a feed inlet 31 is provided in the middle of the transport section 3 for adding organic waste liquid, organic waste or solid organic waste.
Optionally, the height difference between the material returning port 23 and the crushing air pipe 21 in the vertical direction is less than or equal to 1 m.
Optionally, the crushing air pipe 21 is located in the return port 23, and the crushing air pipe 21 and the return port 23 share a common central axis.
Optionally, the gas-solid separator 4 is of a cyclone separator structure, the solid-gas ratio of the gas-solid phase inlet 41 is 4-30 kg/kg, and the gas-solid separator 4 can fully capture particles larger than 100 μm.
Optionally, the side wall of the gas-solid separator 4 near the solid phase outlet 42 is provided with a separation air pipe 44, and the separation air pipe 44 is used for rotationally distributing air and shearing and crushing internal materials.
Optionally, the separation air duct 44 is at least one layer, each layer of separation air duct 44 is arranged to be at least two and located on the same cross section of the gas-solid separator 4, the central axis of the outlet of each separation air duct 44 does not pass through the axis of the gas-solid separator 4, and each layer of separation air duct 44 is tangent to a separation air duct tangent circle whose diameter is smaller than or equal to the diameter of the cross section where the layer of separation air duct 44 intersects with the gas-solid separator 4, and the center of the separation air duct tangent circle is located on the axis of the gas-solid separator 4.
The utility model discloses another aspect provides a solid fuel utilizes device, including the unit and the powder reactor of preheating that communicate each other, wherein: the preheating unit is formed by sequentially connecting the air distribution section 1, the crushing section 2, the conveying section 3, the gas-solid separator 4 and the material returning device 5; the gas phase outlet 43 is connected to the powder reactor, and reacts in the powder reactor.
Optionally, the powder reactor is an entrained flow gasification unit for gasifying the internal pretreated fuel with the introduced fourth gas a 4.
Optionally, the powder reactor is a combustion unit for organizing the combustion of the pre-treated fuel.
(III) advantageous effects
Compared with the prior art, the utility model provides a solid fuel preprocessing device and utilize device has following beneficial effect at least:
(1) the utility model discloses pass through structure and cloth wind formal design at cloth wind section and broken section and form broken and the broken field of tangential granule collision, the millimeter level granule that will give the income is broken for the micron order hot carbon-containing solid powder who satisfies the low reaches unit demand. The preheating and the activation of the carbon-containing solid fuel are completed while the crushing is carried out, so that the coal adaptability of the combustion and gasification technology taking the coal dust as the raw material is improved; and will dry, crocus and preheat the coupling and be a preprocessing device, reduced manufacturing cost by a wide margin.
(2) The pretreatment device takes millimeter-scale solid fuel as raw material, and solves the problems that the prior pre-gasification technology takes micron-scale powder as raw material, extra bed material needs to be supplemented, the operation regulation and control requirements are high and the like through air distribution, crushing and solid fuel circulation.
(3) The organic waste is decomposed and gasified by utilizing the large circulation multiplying power and heat capacity of the circulating fluidized bed, and the organic waste and coke powder generated by preheating and gasification are used as raw materials for entrained flow gasification. The gasification method can well solve the problem of organic waste generated in the coal chemical industry at present, is well coupled with coal chemical industry technologies such as coal-based natural gas, coking, coal liquefaction and the like, and realizes clean production of the coal chemical industry.
Drawings
Fig. 1 is a schematic view showing a structure of a solid fuel pretreatment device according to a first embodiment of the present invention;
figure 2 schematically illustrates a top view of a secondary air duct according to a first embodiment of the present invention;
fig. 3 schematically shows a top view of a crushing air duct according to a first embodiment of the invention;
fig. 4 schematically shows a top view of a crushing air duct according to a second embodiment of the invention;
fig. 5 is a view schematically showing the structure of a solid fuel pretreatment device according to a third embodiment of the present invention;
fig. 6 schematically shows a structure diagram of a coupling of a crushing air pipe and a material returning port according to a third embodiment of the present invention;
FIGS. 7A and 7B schematically show a structural view and a sectional view of a gas-solid separator according to a fourth embodiment of the present invention;
fig. 8 is a view schematically showing the structure of a solid fuel utilization apparatus according to an embodiment of the present invention;
fig. 9 is a view schematically showing the structure of a solid fuel utilization apparatus according to another embodiment of the present invention;
fig. 10 schematically shows a flow chart of a pretreatment method of a solid fuel pretreatment device according to a first embodiment of the present invention;
fig. 11 is a flowchart schematically showing a pretreatment method of a solid fuel pretreatment device according to a third embodiment of the present invention;
fig. 12 schematically shows a flow chart of a pretreatment method of a solid fuel pretreatment device according to a fourth embodiment of the present invention.
[ description of reference ]
1-air distribution section; 11-air distribution device; 13-secondary air pipe; 12-a slag discharge port; 2-a crushing section; 21-crushing air pipes; 22-a feed port; 23-returning the material port; 3-a transport section; 31-a feed inlet; 32-an outlet of the transport section; 4-gas-solid separator; 41-gas solid phase inlet; 42-solid phase outlet; 43-gas phase outlet; 44-a separation air duct; 5-a material returning device; 51-a return inlet; 52-a return outlet; a1 — first gas; a2 — second gas; a3 — third gas; a4 — fourth gas; a5 — fifth gas; g2-coal gas; AS-fly ash; s-organic waste; f-carbon-containing solid fuel; h-coarse particles; g1-preheating flue gas; c, preheating the materials; g3, smoke.
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.
An aspect of the present invention provides a solid fuel pretreatment device for pretreating a carbonaceous solid fuel.
Fig. 1 schematically shows a structural view of a solid fuel pretreatment device according to a first embodiment of the present invention. As shown in fig. 1, the solid fuel pretreatment device may include a wind distribution section 1 and a crushing section 2, the wind distribution section 1 is a cylindrical structure including a bottom portion and a top portion, the bottom portion is gradually enlarged toward the top portion, and the crushing section 2 is a cylindrical structure and is communicated with the top portion of the wind distribution section 1.
Wherein, the bottom of the air distribution section 1 is provided with an air distribution device 11 for pushing the internal materials to flow upwards. The air distribution device 11 is composed of an air chamber and an air cap, or the air distribution device 11 is a jet flow nozzle.
In this embodiment, the included angle β between the two generatrices of the axial cross-section of the air distribution section 1 is 25 ° to 55 °. Further, the included angle β preferably ranges from 20 ° to 40 °. Alternatively, the wind distribution section 1 may be, for example, a circular truncated cone or a truncated pyramid.
It can be understood that, in the embodiment of the present invention, the axial section is a section parallel to the axial line, and the cross section is a section perpendicular to the axial line. And a secondary air pipe 13 is arranged on the side wall of the air distribution section 1 and used for distributing air to the solid fuel pretreatment device.
In this embodiment, the included angle α between the central axis of the outlet of the secondary air pipe 13 and the cross section of the air distribution section 1 is 0 ° to 75 °. Further, the included angle α preferably ranges from 10 ° to 50 °.
The crushing section 2 comprises a straight barrel section and a circular truncated cone section which are connected with each other, the straight barrel section is communicated with the air distribution section 1, and the side wall of the straight barrel section is provided with a crushing air pipe 21 for introducing crushing air into the crushing section 2.
The side wall of the circular table section is provided with a feeding opening 22 for feeding the carbon-containing solid fuel F to be preheated. The angle gamma between the central axis of the outlet of the feeding opening 22 and the cross section of the crushing section 2 is in the range of 45-75 deg.
As shown in fig. 2, it shows a top view of the secondary air duct according to the first embodiment of the present invention. The structure of the secondary air duct shown in fig. 2 will be further explained with reference to fig. 1. Wherein, the secondary air pipe 13 is at least one layer, and each layer of the crushing air pipes 21 is arranged into at least two and is positioned on the same cross section of the air distribution section 1. The central axis of each layer of secondary air pipe 13 is tangent to the same preset tangent circle.
Further, the radius of the same preset tangent circle is between the radius of the air distribution device 11 and the radius of the cross section of the intersection of the secondary air pipe 13 and the air distribution section 1.
Referring to fig. 2, the central axis of each layer of secondary air duct 13 is tangent to the same preset tangent circle, and R1 is equal to or smaller than the radius of the preset tangent circle, R is equal to or smaller than R, where R represents the radius of the cross section of the intersection of the secondary air duct 13 and the air distribution segment 1, and R1 represents the radius of the air distribution device 11.
Preferably, each layer of secondary air pipes 13 is in a central symmetrical structure.
Therefore, the secondary air pipe 13 adopts a tangent circle form, coarse particles descending along the side wall are conveyed to the center of the air distribution section, meanwhile, tangential air distribution strengthens tangential crushing and movement of the coarse particles, the gasification agent is rapidly diffused, and slagging caused by local high temperature is avoided.
As shown in fig. 3, which shows a top view of the crushing flue pipe of the first embodiment of the present invention. The structure of the crushing air duct shown in fig. 3 will be further explained with reference to fig. 1. Wherein, broken tuber pipe 21 is at least one deck, and every layer broken tuber pipe 21 arranges to at least two, and the export central axis of every broken tuber pipe 21 intersects in a straight section of thick bamboo one point.
The central axis of each layer of crushing air pipes 21 is positioned on the same cross section of the straight cylinder section. Wherein each layer of the crushing air pipes 21 is provided with odd number, and the central axis of the outlet of the odd number of the crushing air pipes 21 points to the axis of the straight cylinder section; or, each layer of crushing air pipes 21 is even, and the central axes of the outlets of the even crushing air pipes 21 are collinear in pairs and point to the axis of the straight cylinder section.
Preferably, each layer of crushing air pipes 21 are arranged into 2-8 air pipes, and each layer of crushing air pipes 21 are circumferentially and uniformly arranged on the straight cylinder section.
Therefore, the crushing air pipe 21 distributes air in an opposite impact mode, and gas can collide with solid fuel particles ascending from the center through solid fuel particles at the edge wall carried in the opposite impact mode to form a particle crushing area, so that the particles are conveniently crushed.
Preferably, the crushing ductwork 21 is provided in the transition region of the straight cylindrical section connecting the dense phase zone and the dilute phase zone.
In this embodiment, the top of the circular truncated cone section is further provided with a discharge hole for outputting the pretreatment fuel.
It can be understood that, as shown in fig. 1, according to the solid fuel pretreatment device provided in this embodiment, the carbonaceous solid fuel is pretreated and then introduced into the reactor through the discharge port for reaction. Wherein the reactor is a pulverized coal furnace, an entrained flow bed or a kiln.
The second embodiment of the present invention further provides a solid fuel pretreatment device, and for brevity, the same or similar features as those of the first embodiment will not be described again, and only the features different from those of the first embodiment will be described below.
As shown in fig. 4, a top view of a crushing flue pipe according to a second embodiment of the present invention is shown. The structure of the crushing air duct shown in fig. 4 will be further explained with reference to fig. 1. The number of the broken air pipes 21 is at least one, the broken air pipes 21 on each layer are arranged into even numbers, the central axis of the outlet of each broken air pipe 21 is located on the same cross section of the straight cylinder section, the central axes of every two adjacent broken air pipes 21 on each layer of broken air pipes 21 are intersected at one point, the intersection point is located on the circumference which has the same radius as the air distribution device 11 and has the circle center on the axis of the straight cylinder section, and each layer of broken air pipes 21 is of a central symmetry structure.
Preferably, the included angle between the central axes of every two adjacent crushing air pipes 21 on each layer of crushing air pipes 21 is a right angle.
Therefore, in the present embodiment, the crushing air pipes 21 are in a corner collision structure, and the two intersecting crushing air pipes carry solid particles to collide and crush on the same plane, and collide and crush again with the upward particles, so as to enhance the frequency and strength of particle collision and crushing in a large space. Moreover, the structure is beneficial to collision and crushing among particles in a large-size crushing section.
The third embodiment of the present invention also provides a solid fuel pretreatment device, and for brevity, the same or similar features as those of the first or second embodiment will not be described again, and only the features different from those of the first and second embodiments will be described below.
As shown in fig. 5, there is shown a structural view of a solid fuel pretreatment device according to a third embodiment of the present invention. The solid fuel pretreatment device can comprise an air distribution section 1, a crushing section 2, a conveying section 3, a gas-solid separator 4 and a material returning device 5.
In this embodiment, the air distribution section 1 and the crushing section 2 are the same as those of the first embodiment, and are not described again. The crushing section 2 is communicated with a conveying section 3, a gas-solid separator 4 and a material returning device 5 in sequence.
The side wall of the air distribution section 1 close to the bottom is also provided with a slag discharge port 12, and the side wall of the circular truncated cone section of the crushing section 2 is also provided with a material return port 23. Among other things, the slag tap 12 is used to discharge coarse particles H, which may include coarse slag or gangue, for example, and which are relatively difficult to break or have a relatively high ash content, out of the solid fuel pretreatment device.
The conveying section 3 is communicated with a discharge port, and a feed port 31 is arranged in the middle of the conveying section 3 and is used for adding organic waste S, such as organic waste liquid, organic waste or solid organic waste.
It should be noted that the number of the feed opening 31 may be 1, and the organic waste liquid, the organic waste, or the solid organic waste is all fed through the feed opening 31. The feed opening 31 may be plural, and each of various types of organic waste liquid, organic waste or solid organic waste is fed through each feed opening 31 individually. The organic waste S is organic waste liquid, tar, carbon-containing waste residue or oil residue generated in the coal chemical industry, and the utility model is not limited.
Preferably, the feed port 31 is provided in the dilute phase zone in the middle of the transport section 3. Therefore, the added organic waste liquid and organic waste can be rapidly heated and dispersed by utilizing the high circulation multiplying power and the material concentration of the circulating fluidized bed, and the phenomena of slag bonding and agglomeration are avoided.
In this embodiment, the top of the transportation section 3 is provided with a transportation section outlet 32, the gas-solid separator 4 is provided with a gas-solid phase inlet 41, a gas-phase outlet 43 and a solid phase outlet 42, the transportation section outlet 32 is connected with the gas-solid phase inlet 41, the material returning device 5 is provided with a material returning inlet 51 communicated with the solid phase outlet 42, and then the coarse solid fuel separated by the gas-solid separator 4 can enter the material returning device 5 through the solid phase outlet 42.
The return feeder 5 is formed by a zigzag pipeline and is also provided with a return outlet 52 communicated with the return port 23.
In this embodiment, the gas-solid separator 4 is a cyclone separator structure, the solid-gas ratio at the gas-solid phase inlet 41 is 4-30 kg/kg, and the gas-solid separator 4 can collect all particles larger than 100 μm.
The material returning device 5 is a non-mechanical material returning device. Preferably, the return feeder 5 is a U-shaped return feeder or a J-valve.
Preferably, the height difference between the material returning opening 23 and the crushing air pipe 21 in the vertical direction is less than or equal to 1 m. The structure is more beneficial to collision and crushing of returned materials among particles, particle collision in a particle collision area is strengthened, and the phenomenon that the returned materials are discharged through the slag discharge port 12 due to insufficient crushing caused by too low position of the material return port is avoided, so that the carbon content of bottom slag is high.
The present embodiment is through air distribution section 1, crushing section 2, and transport section 3, gas-solid separator 4 and returning charge ware 5 link to each other in proper order, constitute circulation circuit jointly, can realize the cyclic utilization of carbonaceous solid fuel, and returning charge export 52 communicates the returning charge mouth 23 of crushing section 2, catches the coarse grain that leaves crushing section 2 again and returns, and reentrant crushing section 2 continues to carry out the breakage to the dwell time of coarse grain at preprocessing device has been prolonged.
Alternatively, as shown in fig. 6, the crushing air pipe 21 is located in the return port 23, and the crushing air pipe 21 and the return port 23 share a common central axis. It can be seen that the jet air passing through the breaker ducts 21 entrains the returning material and participates in the particle impact in the impact zone. The coupling structure of the crushing air pipe 21 and the material returning port 23 improves the efficiency of the crushing air pipe 21 for carrying solid particles, and strengthens collision crushing of the returned materials.
The fourth embodiment of the present invention further provides a solid fuel pretreatment device, and for brevity, the same or similar features as those of the previous embodiment will not be described again, and only the features different from those of the previous embodiment will be described below.
As shown in fig. 7A and 7B, there are shown a structural view and a sectional view of a gas-solid separator according to a fourth embodiment of the present invention.
In this embodiment, the side wall of the gas-solid separator 4 near the solid phase outlet 42 is provided with a separation air duct 44, and the separation air duct 44 is used for rotationally distributing air and shearing and crushing internal materials.
The number of the separation air pipes 44 is at least one, each layer of the separation air pipes 44 is arranged into at least two layers and is located on the same cross section of the gas-solid separator 4, the central axis of the outlet of each separation air pipe 44 does not pass through the axis of the gas-solid separator 4, each layer of the separation air pipe 44 is tangent to a separation air pipe tangent circle with a diameter less than or equal to the diameter of the cross section of the intersection of the layer of the separation air pipe 44 and the gas-solid separator 4, and the center of the tangent circle of the separation air pipe is located on the axis of the gas-solid separator 4.
Further, each layer of the separation air duct 44 has a central symmetrical structure.
When the particle size of the solid fuel entering the gas-solid separator 4 is still coarse and does not reach the proper particle size of the solid fuel entering the downstream unit, the present embodiment further enhances the shearing and crushing among particles by adding the separation air duct 44 on the bottom side wall of the gas-solid separator 4.
According to the present general inventive concept, another aspect of the present invention provides a solid fuel utilization device.
As shown in fig. 8, a structural diagram of a carbon-containing solid fuel utilization apparatus according to an embodiment of the present invention is shown. The solid fuel utilization device consists of a preheating unit and a powder reactor which are communicated with each other, wherein the preheating unit is formed by sequentially connecting an air distribution section 1, a crushing section 2, a conveying section 3, a gas-solid separator 4 and a material returning device 5 in the embodiment.
It should be noted that the internal structural form of the preheating unit is similar to that of the solid fuel pretreatment device of the foregoing embodiment, and the achieved technical effects are also similar, and for specific details, reference is made to the foregoing embodiment, and no further description is given here.
In this embodiment, the powder reactor is an entrained-flow bed gasification unit, the gas phase outlet 43 is connected to the entrained-flow bed gasification unit, and the entrained-flow bed gasification unit is configured to perform a gasification reaction on the internal pretreated fuel and the introduced fourth gas a 4.
Under the gas-solid separation action of the gas-solid separator 4, the preheated material C and the preheated coal gas G1 with the particle size less than or equal to 100 mu m enter the entrained flow gasification unit through the gas phase outlet 43 and undergo high-temperature gasification reaction with the fourth gas A4 to produce coal gas G2, first fly ash AS and slag R.
Wherein the fourth gas A4 is pure oxygen and water vapor, and the oxygen concentration is 50-100%.
According to the general inventive concept, there is also provided a solid fuel utilization device of another embodiment.
As shown in fig. 9, a structural view of a solid fuel utilization apparatus according to another embodiment of the present invention is shown. The solid fuel utilization device consists of a preheating unit and a combustion unit which are communicated with each other, wherein the preheating unit is formed by sequentially connecting an air distribution section 1, a crushing section 2, a conveying section 3, a gas-solid separator 4 and a material returning device 5 in the embodiment.
It should be noted that the internal structural form of the preheating unit is similar to that of the solid fuel pretreatment device of the foregoing embodiment, and the achieved technical effects are also similar, and for specific details, reference is made to the foregoing embodiment, and no further description is given here.
In this embodiment, the powder reactor is a combustion unit for organizing the combustion of the pre-processed fuel. That is, the gas phase outlet 43 is connected to a combustion unit for combustion reaction of the high temperature fuel entering the inside with the sixth gas a 6.
Under the gas-solid separation action of the gas-solid separator 4, the preheated material C and the preheated coal gas G1 with the particle size less than or equal to 100 mu m enter the combustion unit through the gas phase outlet 43 and undergo combustion reaction with the sixth gas A6 to produce flue gas G3, fly ash AS-2 and slag R-2.
Wherein the sixth gas A6 is oxygen, or oxygen + CO2Or air, the oxygen concentration is 21% -100%.
The slag R-2 may be in a non-molten state or in a molten state.
According to the present general inventive concept, another aspect of the present invention is to provide a method for pretreating solid fuel, which is based on the foregoing description, the solid fuel pretreatment apparatus according to the first embodiment of the present invention pretreats solid fuel.
As shown in fig. 10, in the present embodiment, the solid fuel pretreatment method may include:
s101, the carbonaceous solid fuel F is passed into the crushing section 2 via the feed opening 22.
The particle diameter of the carbonaceous solid fuel F fed through the feed port 22 is 0 to 6mm, preferably 0 to 2 mm. The carbonaceous solid fuel F enters the crushing section 2 by gravity or pneumatic transport.
S102, the first gas A1 enters the solid fuel pretreatment device through the air distribution device 11, and the materials converged at the bottom of the air distribution section 1 are fluidized.
Wherein, the first gas A1 fluidizes the materials converged at the bottom through the air distribution device 11 to form an internal circulation of the materials with an upward center and downward side walls.
The first gas A1 comprises air, oxygen-enriched air and water vapor or pure oxygen and water vapor, and the concentration range of the oxygen is 21-80%. Preferably, the concentration of oxygen in the first gas a1 ranges from 21% to 50%.
S103, enabling the second gas A2 to enter a solid fuel pretreatment device through a secondary air pipe 13 to tangentially crush and mix the solid fuel;
the second gas A2 is quickly mixed with descending solid fuel in a tangential mode through the secondary air pipe 13, and carries the solid fuel to move towards the bottom center in a tangential mode, so that the solid fuel is converged towards the center and is sheared and crushed.
The second gas A2 comprises air, air + water vapor, air + flue gas or pure oxygen + water vapor, and the concentration range of oxygen is less than or equal to 21%. Preferably, the concentration of oxygen in the second gas A2 is in the range of ≦ 10%.
In the step, the wind speed range of the secondary wind pipe 13 is 15-40 m/s, preferably 18-30 m/s. The apparent wind speed range of the cross section of the wind distribution section 1 is 0.5 m/s-2.5 m/s, preferably 1.0 m/s-2.0 m/s.
And S104, allowing the third gas A3 to enter the solid fuel pretreatment device through the crushing air pipe 21 in a high-speed jet mode, and carrying the solid fuel at the side wall to collide with the solid fuel particles ascending from the center to be crushed.
The crushing wind pipe 21 is arranged on a transition area of the straight cylinder section of the crushing section 2, which is connected with the dense phase area and the dilute phase area. The third gas A3 is introduced into the crushing wind pipe 21 in the form of high-speed jet flow, and carries solid fuel particles at the side wall to violently collide with the particles ascending from the center to form a particle crushing area.
After the collision crushed fine particles are pretreated, the fine particles are carried to a downstream powder reactor by gas to carry out combustion or gasification reaction; the coarse particles move downward with the internally circulating solid fuel.
In this step, the third gas A3 is air, oxygen-enriched air + water vapor or pure oxygen + water vapor, and the concentration range of oxygen is 21% -80%. Preferably, the concentration of oxygen in the third gas a3 ranges from 30% to 60%.
The wind speed range of the wind distribution of the crushing wind pipe 21 is 30m/s to 200m/s, and the preferable wind speed range is 50m/s to 100 m/s. The apparent wind speed range of the outlet of the crushing section 2 is 4m/s to 10m/s, preferably 5m/s to 8m/s through the air supplement of the crushing air pipe.
And S105, discharging the crushed and preheated high-temperature fuel through a discharge hole.
Because the top of the circular platform section is provided with the discharge hole, the high-temperature fuel generated in the air distribution section 1 and the crushing section 2 is discharged through the discharge hole.
Therefore, the solid fuel pretreatment method of the embodiment realizes forced internal circulation and crushing of the solid fuel and separation of coarse and fine particles by means of the structures or air distribution designs of the air distribution section 1 and the crushing section 2, and improves the retention time and treatment time of the coarse particles in the section.
The pretreatment method of the solid fuel in the embodiment utilizes the reaction and crushing space formed by the air distribution section 1 and the crushing section 2, and the carbon-containing solid fuel forms stronger internal circulation and stronger mass and heat transfer in the space through the structure and the air distribution mode. And the thermal stress formed after the carbon-containing solid fuel is heated and a crushing field formed by collision are fully utilized to crush the carbon-containing solid fuel into fine powder meeting the particle size range required by the downstream process. In addition, the internal circulation of the carbon-containing solid fuel formed by the air distribution strengthens the collision frequency of coarse particles, prolongs the retention time of the coarse particles in the pretreatment device and prolongs the separation of the coarse particles and the coarse particles.
According to the present general inventive concept, another aspect of the present invention is to provide a method for pretreating solid fuel, which is based on the foregoing, and a solid fuel pretreatment apparatus according to a third embodiment of the present invention pretreats solid fuel.
As shown in fig. 11, in the present embodiment, the solid fuel pretreatment method may include:
s201, the carbonaceous solid fuel F is passed into the crushing section 2 via the feed opening 22.
S202, enabling the first gas A1 to enter the solid fuel pretreatment device through the air distribution device 11, and fluidizing the materials converged at the bottom of the air distribution section 1.
S203, the second gas A2 enters the solid fuel pretreatment device through the secondary air pipe 13, and the solid fuel is tangentially crushed and mixed.
S204, the third gas A3 enters the solid fuel pretreatment device through the crushing air pipe 21, and the solid fuel at the entrainment side wall collides with the solid fuel particles ascending from the center to be crushed.
Steps S201 to S204 of this embodiment are the same as steps S101 to S104 of the previous embodiment, and are not described again here.
S205, the organic waste material S is introduced into the conveying section 3 through the feed opening 31.
The middle part of the transportation section 3 is provided with a feed opening 31, and therefore, the organic waste S is introduced into the transportation section 3 through the feed opening 31.
Preferably, a feeding port 31 is arranged in a dilute phase zone in the middle of the conveying section, and the added organic waste S can be rapidly heated and dispersed by utilizing the high circulation rate and material concentration of the circulating fluidized bed, so that the phenomena of slag bonding and agglomeration are avoided.
S206, the preheated and crushed high-temperature fuel in the conveying section 3 enters the gas-solid separator 4 from the conveying section outlet 32, and after gas-solid separation, qualified high-temperature fuel is discharged from the gas phase outlet 43 of the gas-solid separator 4.
In the step, high-temperature gas fuel generated in the air distribution section 1 and the crushing section 2 is introduced into the conveying section 3 communicated with the crushing section 2, the high-temperature gas fuel and part of gas enter the gas-solid separator 4 from the conveying section outlet 32 at the top of the conveying section 3, and part of the high-temperature fuel escapes through the gas phase outlet 43 and can enter the powder reactor or other devices.
S207, the circulating solid particles separated by the gas-solid separator 4 enter the return feeder 5 from the solid phase outlet 42.
Since the separator inlet 41 of the gas-solid separator 4 is used for trapping particles with a size > 100 μm, the material concentration is now quite large, so that part of the high temperature fuel will be trapped by the gas-solid separator 4 due to agglomeration of the solid particles and enter the return feeder 5 via the solid phase outlet 42.
S208, the circulating solid particles in the return feeder 5 are returned to the crushing section 2 through the return port 23.
Through the steps S207-S208, under the action of gas-solid separation, the circulating solid particles collected by the gas-solid separator 4 return to the air distribution section 1 and the crushing section 2 through the return feeder 5, and the materials are continuously preheated and crushed, so that the recycling of the solid fuel is realized.
And S209, discharging part of coarse particles H in the air distribution section 1 through the slag discharge port 12.
So far, after the solid fuel is recycled, coarse particles H which are difficult to break and have high ash content, such as coarse slag and gangue, are discharged through a bottom slag discharge port 12.
According to the solid fuel pretreatment method, the air distribution section 1, the crushing section 2, the transportation section 3, the gas-solid separator 4 and the material returning device 5 are sequentially connected to realize the circulation of the carbon-containing solid fuel, so that coarse particles leaving the crushing section 2 are captured back and enter the crushing section again to continue crushing, the retention time of the coarse particles in the pretreatment device is prolonged, and the pretreatment effect is further improved.
According to the present general inventive concept, another aspect of the present invention is to provide a method for pretreating solid fuel, which is based on the foregoing, in a fourth embodiment of the present invention.
As shown in fig. 12, in the present embodiment, the solid fuel pretreatment method may include:
s301, introducing the carbon-containing solid fuel F into the crushing section 2 through the feeding port 22;
s302, enabling the first gas A1 to enter a solid fuel pretreatment device through an air distribution device 11, and fluidizing the material converged at the bottom of an air distribution section 1;
s303, enabling the second gas A2 to enter a solid fuel pretreatment device through a secondary air pipe 13, and tangentially crushing and mixing the solid fuel;
s304, enabling the third gas A3 to enter a solid fuel pretreatment device through a crushing air pipe 21, and enabling solid fuel at the entrainment side wall to collide with solid fuel particles ascending from the center to be crushed;
s305, introducing the organic waste S into a conveying section 3 through a feed inlet 31;
s306, the preheated and crushed high-temperature fuel in the conveying section 3 enters the gas-solid separator 4 from the conveying section outlet 32, and after gas-solid separation, qualified high-temperature fuel is discharged from the gas phase outlet 43 of the gas-solid separator 4;
s307, introducing a fifth gas A5 into the separation air pipe 44 to strengthen the shearing and crushing of the particles in the gas-solid separator 4;
s308, circulating solid particles separated by the gas-solid separator 4 enter the material returning device 5 from the solid phase outlet 42;
s309, returning residual circulating solid particles in the material returning device 5 to the crushing section 2 through the material returning opening 23;
and S310, discharging part of coarse particles H in the air distribution section 1 through the slag discharge port 12.
Steps S301 to S306 and S308 to S310 of the present embodiment are the same as steps S201 to S209 of the previous embodiment, respectively, and are not described herein again. Only the features thereof different from the foregoing embodiment will be described below.
In step S307, the present embodiment is provided with a separation wind pipe 44 on the sidewall of the gas-solid separator 4, so that when the particle size of the solid fuel entering the gas-solid separator 4 is still coarse and does not reach the suitable particle size of the solid fuel entering the downstream unit, the fifth gas a5 is introduced into the separation wind pipe 44 to enhance the shearing and breaking among the particles.
The fifth gas A5 is air, water vapor, air + water vapor, or pure oxygen + water vapor, and the oxygen concentration range is less than or equal to 30%. Preferably, the oxygen concentration in the fifth gas A5 is in the range of ≦ 10%.
The wind speed range of the separation wind pipe 44 is 20 m/s-50 m/s.
Therefore, the pretreatment method for the solid fuel provided by the embodiment further enhances the shearing and crushing synchronously performed in the gas-solid separation process, improves the effect of the gas-solid separator, and further improves the pretreatment effect.
To sum up, the embodiment of the utility model provides a solid fuel preprocessing device and utilize device forms the broken and tangential broken field of granule collision through structure and cloth wind formal design at cloth wind section and broken section, and the broken micron order hot carbon-containing solid powder for satisfying the low reaches unit demand of millimeter level granule that will give into. The preheating and the activation of the carbon-containing solid fuel are completed while the crushing is carried out, so that the coal adaptability of the combustion and gasification technology taking the coal dust as the raw material is improved; and will dry, crocus and preheat the coupling and be a preprocessing device, reduced manufacturing cost by a wide margin.
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 (18)
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| CN115368937A (en) * | 2022-08-12 | 2022-11-22 | 北京中瀚能源有限公司 | Pretreatment device, combustion device and combustion method for low-calorific-value solid fuel |
| CN115404112A (en) * | 2021-05-28 | 2022-11-29 | 中国科学院工程热物理研究所 | Solid fuel pretreatment device, utilization device and pretreatment method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115404112A (en) * | 2021-05-28 | 2022-11-29 | 中国科学院工程热物理研究所 | Solid fuel pretreatment device, utilization device and pretreatment method |
| CN115404112B (en) * | 2021-05-28 | 2024-09-17 | 中国科学院工程热物理研究所 | Solid fuel pretreatment device, utilization device and pretreatment method |
| CN115368937A (en) * | 2022-08-12 | 2022-11-22 | 北京中瀚能源有限公司 | Pretreatment device, combustion device and combustion method for low-calorific-value solid fuel |
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