CN212236464U - Dust removing device for tar-containing fuel gas moving particle bed - Google Patents
Dust removing device for tar-containing fuel gas moving particle bed Download PDFInfo
- Publication number
- CN212236464U CN212236464U CN202022070542.XU CN202022070542U CN212236464U CN 212236464 U CN212236464 U CN 212236464U CN 202022070542 U CN202022070542 U CN 202022070542U CN 212236464 U CN212236464 U CN 212236464U
- Authority
- CN
- China
- Prior art keywords
- dust
- gas
- dust removal
- chamber
- filter material
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000000428 dust Substances 0.000 title claims abstract description 316
- 239000002245 particle Substances 0.000 title claims abstract description 148
- 239000002737 fuel gas Substances 0.000 title claims abstract description 27
- 239000000463 material Substances 0.000 claims abstract description 148
- 239000007789 gas Substances 0.000 claims abstract description 119
- 238000000926 separation method Methods 0.000 claims abstract description 9
- 239000007787 solid Substances 0.000 claims description 48
- 238000001914 filtration Methods 0.000 abstract description 13
- 239000000571 coke Substances 0.000 abstract description 11
- 239000008187 granular material Substances 0.000 abstract description 10
- 230000001105 regulatory effect Effects 0.000 abstract description 2
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- 238000000197 pyrolysis Methods 0.000 description 31
- 239000010410 layer Substances 0.000 description 13
- 238000000034 method Methods 0.000 description 13
- 238000010586 diagram Methods 0.000 description 9
- 239000002028 Biomass Substances 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- 239000003245 coal Substances 0.000 description 6
- 239000006004 Quartz sand Substances 0.000 description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 5
- 238000002309 gasification Methods 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 239000003034 coal gas Substances 0.000 description 4
- 239000002344 surface layer Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 229910052609 olivine Inorganic materials 0.000 description 2
- 239000010450 olivine Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000011335 coal coke Substances 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 239000002006 petroleum coke Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000004449 solid propellant Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
Images
Landscapes
- Filtering Of Dispersed Particles In Gases (AREA)
- Industrial Gases (AREA)
Abstract
The utility model discloses a contain tar fuel gas and remove granule bed dust collector belongs to filtering separation technical field. The movable particle bed dust removal device is composed of two dust removal chambers communicated through an inner component, each dust removal chamber is provided with a filter material inlet and a filter material outlet, the respective regulation and control of the filter material output of each dust removal chamber are realized by utilizing the shunting principle, and the adhesion stagnation of coke/tar filter materials and the formation of dead zones caused by the contact of fuel gas and the attachment of the coke/tar filter materials are avoided; and the porosity of the granular bed layer is regulated and controlled through independent input and movement of the filter material, so that the dust removal performance of the device is flexibly optimized. The utility model discloses utilize gas inlet, inner member and gas outlet to form the parallel flow or against current or cross-current and cross-current or two sections dust removal as an organic whole different operation mode's as an organic whole dust collector against current, realized that the high temperature contains the high-efficient dust removal of tar fuel gas, its simple structure, handling capacity are big, the stable performance, and the regulation nature is strong, the dust removal pressure drop is little, and the running cost is low.
Description
Technical Field
The utility model belongs to the technical field of filtering separation, a processing technology of dirty gas is related to, specifically a contain tar fuel gas and remove granule bed dust collector.
Background
The initial fuel gas generated in the thermal conversion (pyrolysis, gasification and the like) process of the solid fuel usually has high dust content, contains tar components with complex compositions, is extremely sensitive to temperature, is easy to block equipment and pipelines due to condensation or coking, and seriously hinders the stable operation of the thermal conversion equipment. In order to effectively solve the problem of fuel gas dust removal commonly existing in the thermal conversion technology, technologies such as high-temperature cyclone dust removal, ceramic/fiber filtration dust removal, electrostatic dust removal and particle bed dust removal are continuously proposed. Among them, the moving granular bed dust removal technology is considered as one of the most potential high temperature dust removal technologies due to the low cost of filter material, long service life, high dust removal efficiency, constant pressure drop and continuous operation.
Patent CN102716628A discloses a particulate dust removing filter and a dust removing filtering method. The filter body is composed of a shell with a cylindrical upper part and a conical lower part and an inner component of a tower-shaped baffle group. Solid particles are input through a feeding system which is positioned above the shell and consists of a feeding hole, a material layer height adjusting rod and an inner cylinder, and a particle layer is formed above the tower-shaped baffle group; the raw material gas is input through an air inlet pipe extending into the tower-shaped baffle plate group, then passes through an annular gap formed by the tower-shaped baffle plate group to be contacted with solid particles on the annular gap, and dust of the raw material gas is trapped. The clean gas after dust removal is discharged from the gas outlet, the solid particles fall along the side wall of the dust removal filter shell, and finally the solid particles carrying impurities are discharged from the discharge hole. Patent CN102908841A discloses a method and a device for dedusting and purifying low-temperature dry distillation coal gas. The center of the upper part of the shell of the disclosed granular bed filter is provided with a filter material granule inlet, two sides of the upper part are provided with a dry distillation coal gas outlet and a preheating flue gas outlet, two sides of the lower part are provided with a dust-containing dry distillation coal gas inlet and a preheating flue gas inlet, the upper part in the shell is provided with a filter material granule distributor, and the lower part is provided with a shutter gas distributor consisting of a plurality of layers of inclined blades. The dry distillation coal gas containing dust enters the granular bed filter from the air inlet, upwards passes through the filter material granular layer through the shutter gas distributor, the dust is discharged from the top purification dry distillation gas outlet after being trapped, and the filter material granular layer for trapping the dust downwards moves and is output to the filter.
The particle dust removal device and the particle dust removal method are provided for dust removal of the dust-containing fuel gas, particularly dust removal of the tar-containing and dust-containing fuel gas, but coke or tar is easily adhered to the filter material due to the fact that the tar in the fuel gas is easily coked or condensed when the tar is in high-temperature contact with the filter material, viscosity is increased, fluidity is reduced, particles of the filter material cannot be output timely and are continuously accumulated in the filter along with the dust removal process, the particles of the filter material cannot be smoothly fed and moved, a dead bed is formed, and finally the dust removal device cannot operate. It is also a common bottleneck problem which hinders the industrial application of the high-temperature moving particle layer filtering and dedusting technology.
SUMMERY OF THE UTILITY MODEL
The utility model provides a device and a method for removing dust of a tar-containing fuel gas movable particle bed at high temperature, aiming at the common problem of the prior particle bed dust removal technology.
The technical scheme of the utility model:
a dust removal device for a moving particle bed of fuel gas containing tar mainly comprises a dust removal chamber a1 and a dust removal chamber b2 which are filled with filter materials, wherein the filter materials form a particle bed in the dust removal chamber a1 and the dust removal chamber b 2; the dust chamber a1 and the dust chamber b2 are separated by a baffle a3, the middle part of the baffle a3 is replaced by an inner member 4, and the dust chamber a1 is communicated with the dust chamber b2 through a gas flow channel formed by the inner member 4; the upper part of the dust chamber a1 is provided with a filter material inlet a5, and the lower part is provided with a filter material outlet a 6; the dust removal chamber a1 is provided with a gas inlet 7, and the dust removal chamber a1 forms a gas-solid contact interface through a baffle b8 or a shutter structure a9, so that the gas inlet 7 is in a single-channel or multi-channel form; the gas inlet 7 is arranged at the upper part of the dust removal chamber a1 and is positioned above the inner member 4, so that a filter material between the gas inlet 7 and the inner member 4 forms a filter bed layer with gas-solid parallel flow; the second one is a filter bed layer which is arranged at the lower part of the dust chamber a1, is positioned below the inner member 4 and above the filter material outlet a6, and leads the filter material between the gas inlet 7 and the inner member 4 to form gas-solid countercurrent; the third is that the filter material is arranged in the middle of the dust chamber a1 and is at the same horizontal height with the center of the inner member 4, so that the filter material between the gas inlet 7 and the inner member 4 forms a filter bed layer of gas-solid radial cross flow. The upper part of the dust chamber b2 is provided with a filter material inlet b10, and the lower part is provided with a filter material outlet b 11; the dust removal chamber b2 is provided with a gas outlet 12, and the dust removal chamber b2 forms a gas-solid separation interface through a baffle c13 or a shutter structure b14, so that the gas outlet 12 is in a single-channel or multi-channel form; the gas outlet 12 is arranged in the middle of the dust removing chamber b2 in two ways, one way is that the gas outlet is arranged in the middle of the dust removing chamber b2 and is at the same horizontal height with the center of the inner member 4, so that the filter material between the gas outlet 12 and the inner member 4 forms a filter bed layer of gas-solid radial cross flow; the other is arranged at the upper part of the dust chamber b2 and is positioned above the inner member 4, so that the filter material between the gas outlet 12 and the inner member 4 forms a filter bed layer of gas-solid countercurrent; the filter material outlet a6 and the filter material outlet b11 are both positioned below the inner member 4 and are respectively connected with corresponding discharge valves.
The dust chamber a1 and the dust chamber b2 are arranged in parallel or arranged inside and outside;
the inner member 4 is a saddle-shaped shutter structure or a wedge-shaped screen structure;
the flow cross sections of the dust removing chamber a1 and the dust removing chamber b2 are rectangular structures, circular structures or circular ring structures;
the ratio of the filter cross-sectional areas of the particle beds in the dust removing chamber a1 and the dust removing chamber b2 is 5: 1-1: 5.
The dust removal method of the tar-containing fuel gas moving particle bed adopts the dust removal device of the tar-containing fuel gas moving particle bed, and comprises the following specific steps:
a part of high-temperature clean filter material enters a dust chamber a1 from a filter material inlet a5 to form a moving particle bed a; the other part of the high-temperature clean filter material enters a dust chamber b2 from a filter material inlet b10 to form a moving particle bed b. High-temperature fuel gas containing tar and dust enters a dust removal chamber a1 from a single-channel or multi-channel gas inlet 7, then flows in the same direction or in the opposite direction or in the radial direction with a filter material of a moving particle bed a between the gas inlet 7 and the inner member 4 in a staggered manner to form gas-solid parallel flow or countercurrent or cross flow particle bed for dust removal, at the moment, tar which is easy to coke/condense in the fuel gas is attached to the surface layer of the filter material, and meanwhile, part of dust is collected by the filter material. The fuel gas after primary dust removal passes through the inner component 4 and enters the dust removal chamber b2, and flows with the filter material of the moving particle bed b in a radial staggered or reverse direction to form gas-solid cross flow or countercurrent particle bed dust removal, and dust in the fuel gas is further captured. Finally, the clean gas after dust removal and the filter material of the moving particle bed b are separated in a dust removal chamber b2 and then discharged from a gas outlet 12 in a single-channel or multi-channel form; the filter material attached with coke/tar and dust in the dust chamber a1 and the filter material attached with dust in the dust chamber b2 are respectively output to the dust removal device from the filter material outlet a6 and the filter material outlet b11 under the control of respective discharge valves. Under the certain condition of dust collector, filter material and pending gas, through the exhaust speed of the filter material of control clean room a1 and clean room b2 respectively, can make the filter material that the mobility reduces because of adhering to coke/tar among the clean room a1 flow fast, prevent it from cohering the stagnation, ensure the steady movement of granule bed, the continuous steady operation of dust removal process to have higher dust collection efficiency.
The filter material is inert or solid particles with catalytic activity, and comprises one or more than two of natural ore, ceramic, coal gangue, charcoal, petroleum coke, coal coke or catalyst;
the filter materials in the dust chamber a1 and the dust chamber b2 are the same or different, the particle size distribution is the same or different, and the average size of the filter material particles in the dust chamber a1 is not smaller than that of the filter material particles in the dust chamber b 2; furthermore, the particle size range of the filter materials in the dust removal chamber a1 and the dust removal chamber b2 is 0.1-20 mm, preferably, the filter materials in the dust removal chamber a1 are large particles with the particle size of 2-8 mm, and the filter materials in the dust removal chamber b2 are small particles with the particle size of 1-4 mm. When the filter materials with two sizes are adopted, the high-temperature fuel gas containing tar and dust firstly contacts with the large-particle filter material, and the large-particle filter material has good fluidity because the angle of repose is smaller than that of small particles, so that the accumulation of the attached coke/tar filter material can be effectively prevented, and the dust removal process can be stably operated; the fuel gas after primary dust removal contacts with the small-particle filter material, and the dust collection efficiency is high because the porosity of the bed layer is smaller than that of the particle bed formed by large particles;
the dedusting temperature of the moving particle bed a and the moving particle bed b is not lower than the temperature of the gas to be treated entering the dedusting chamber a1 and the dedusting chamber b2, and is preferably equal to the temperature of the gas to be treated;
the moving speed ratio of the moving particle bed a to the moving particle bed b is 1.5: 1-10: 1;
the moving particle bed a and the moving particle bed b can also be used for the upgrading of tar-containing gas.
The utility model has the advantages that:
(1) the utility model discloses a remove granule bed dust collector through the method of reposition of redundant personnel, makes the filter material of supplying be divided into two the tunnel, forms cocurrent flow or against current or cross-flow dust removal granule bed and cross-flow or against current dust removal granule bed respectively, and the final filter material exports from respective filter material export with different moving speed under the regulation and control of bleeder valve, and it has solved because of tar coking/condensation attach to the filter material surface makes the filter material mobility poor and cohere the problem of stagnating and form the dead bed, has realized the continuous steady operation of dust removal process;
(2) the movable granular bed dust removal device of the utility model flexibly optimizes the dust removal performance of the device by independently inputting the filter material and movably regulating the porosity of the bed layer;
(3) the utility model discloses a remove granule bed dust collector collect the cocurrent flow, against current or cross-flow and against current or two sections dust removals as an organic whole of cross-flow, simple structure, convenient operation, handling capacity are big, adjust in a flexible way, and can couple the technical advantage of cocurrent flow, cross-flow and two kinds of dust removal modes against current, dust collection efficiency is high, stability is high, the pressure drop is little.
(4) The utility model discloses a remove granule bed dust removal method, filter material kind and size are nimble changeable, not only can realize the high-efficient dust removal of different kind fuel gas, can be according to the demand of target product moreover, and the heat conversion process fuses as an organic whole, realizes removing dust and tar, fuel gas and semicoke preparation or going on in step of upgrading.
Drawings
FIG. 1 is a schematic diagram of the device in parallel arrangement of dust chambers and in a parallel-cross flow operation mode.
FIG. 2 is a schematic diagram of the apparatus in parallel arrangement and co-current-counter-current operation mode.
FIG. 3 is a schematic diagram of the device in a counter-current-cross-current mode of operation with parallel dust chambers.
FIG. 4 is a schematic diagram of the apparatus in a counter-current-counter-current mode of operation with the chambers arranged in parallel.
FIG. 5 is a schematic diagram of the apparatus in a co-current-cross-current mode of operation arranged inside and outside the clean room.
FIG. 6 is a schematic diagram of the apparatus in a co-current-counter-current mode of operation arranged inside and outside the clean room.
FIG. 7 is a schematic diagram of the device in a counter-current-cross-current mode of operation arranged inside and outside the clean room.
FIG. 8 is a schematic diagram of the device in a counter-current-counter-current mode of operation arranged inside and outside the clean room.
FIG. 9 is a schematic diagram of the device in a cross-flow-cross-flow operation mode with dust chambers arranged in parallel.
In the figure: 1, a dust chamber a; 2, a dust removal chamber b; 3, a baffle plate a; 4 an inner member; 5, a filter material inlet a; 6, a filter material outlet a; 7 a gas inlet; 8 baffle b; 9 a louver a; 10 filter material inlet b; 11 a filter material outlet b; 12 a gas outlet; 13 a baffle c; 14 louvers b.
Detailed Description
The following further describes a specific embodiment of the present invention with reference to the drawings and technical solutions.
Example one
The moving particle bed dust removal device shown in figure 1 operates in a parallel arrangement of dust chambers in a co-current-cross-current mode of operation. The flow cross section of the dust chamber of the dust removing device of the embodiment is a rectangular structure, the dust chamber a1 and the dust chamber b2 are arranged in parallel, the ratio of the filtering cross sections of the particle bed is 5:1, and the inner member 4 is of a saddle-shaped shutter structure. During operation, quartz sand with the temperature of 500 ℃ and the particle size of 2-6 mm is input from a filter material inlet a5, and a moving particle bed a with the height of 150mm is formed in a dust chamber a 1; meanwhile, quartz sand with the temperature of 500 ℃ and the particle size of 1-4 mm is input from a filter material inlet b10, and a moving particle bed b with the bed height of 200mm is formed in the dust removal chamber b 2. Coal pyrolysis gas at 500 ℃ enters a dust removal chamber a1 from a gas inlet 7 in a single-channel form formed by a baffle b8 of a dust removal chamber a1 at a speed of 0.4m/s, the pyrolysis gas and a filter material of a particle bed a between the gas inlet 7 and an inner member 4 flow in the same direction after passing through a gas-solid contact interface of a moving particle bed a to form gas-solid co-flow particle bed for dust removal, tar which is easy to coke/condense in the pyrolysis gas is attached to the surface layer of the filter material, and part of dust is trapped by the filter material; the pyrolysis gas after preliminary dust removal passes through the inner component 4, enters the dust removal chamber b2 and flows in a radial direction in a staggered manner with the filter material of the moving particle bed b to form gas-solid cross flow particle bed dust removal, and dust in the pyrolysis gas is further captured. Finally, after the clean pyrolysis gas is separated from the moving particle bed b at the gas-solid separation interface of the dust removal chamber b2, the clean pyrolysis gas is discharged out of the device through a gas outlet 12 in a multi-channel form formed by a shutter b 14; under the regulation and control of the discharge valve, the filter material in the dust chamber a1 is output from the filter material outlet a6 to the dust removal device at the moving speed of 0.30m/h, and the filter material in the dust chamber b2 is output from the filter material outlet b11 to the dust removal device at the moving speed of 0.05 m/h. The dust removal device of the movable particle bed stably runs for 72 hours, and the dust removal efficiency is 99.7 percent.
Example two
As shown in FIG. 2, the operation principle of the moving particle bed dust removing device is that the dust removing chambers are arranged in parallel and in a parallel-countercurrent operation mode, the flow cross section of the dust removing chamber of the dust removing device of the embodiment is a circular structure, the dust removing chamber a1 and the dust removing chamber b2 are arranged in parallel, the ratio of the filtering cross sections of the particle bed is 1:1, and the inner member 4 is in a saddle-shaped shutter structure. During operation, the olivine catalyst with the temperature of 600 ℃ and the particle size of 4-8 mm is input from a filter material inlet a5, and a moving particle bed a with the bed height of 100mm is formed in the dust removal chamber a 1; meanwhile, the olivine catalyst with the temperature of 600 ℃ and the particle size of 2-4 mm is input from a filter material inlet b10, and a dust removal moving particle bed b with the bed height of 150mm is formed in the dust removal chamber b 2. The biomass pyrolysis gas at 600 ℃ enters a dust removal chamber a1 from a single-channel gas inlet 7 at a gas velocity of 0.3m/s, and after passing through a gas-solid contact interface of a moving particle bed a, the pyrolysis gas and a filter material of the particle bed a between the gas inlet 7 and the inner member 4 flow in the same direction to form gas-solid parallel flow particle bed dust removal, at the moment, tar which is easy to coke/condense in the pyrolysis gas is attached to the surface layer of the filter material, and meanwhile, part of dust is captured by the filter material; the pyrolysis gas after preliminary dust removal passes through the inner component 4, enters the dust removal chamber b2 and flows reversely with the filter material of the moving particle bed b to form gas-solid countercurrent particle bed dust removal, and dust in the pyrolysis gas is further captured at the moment. Finally, after the clean gas is separated from the moving particle bed b at the gas-solid separation interface of the dust chamber b2, the clean gas is discharged out of the device through a gas outlet 12 in a single-channel form formed by a baffle c 13; the filter material attached with coke/tar and dust in the dust chamber a1 is output from the filter material outlet a6 to the dust removal device at the moving speed of 0.45m/h, and the filter material attached with a large amount of dust in the dust chamber b2 is output from the filter material outlet b11 to the dust removal device at the moving speed of 0.30 m/h. The dust removal device of the movable particle bed stably runs for 96 hours, and the dust removal efficiency is 99.4 percent.
EXAMPLE III
Referring to the operation principle of the moving particle bed dust collector shown in fig. 3, the dust chambers are arranged in parallel, and the counter-current-cross-current operation mode is adopted, the flow cross section of the dust chamber of the dust collector of this embodiment is a rectangular structure, the dust chamber a1 and the dust chamber b2 are arranged in parallel, the ratio of the filtering cross sections of the particle bed is 4:1, and the inner member 4 is a saddle-shaped shutter structure. The 500 ℃ coal pyrolysis gas enters a dust removal chamber a1 through a gas inlet 7 in a multi-channel form formed by shutters a9 at the speed of 0.5m/s, and then flows reversely with a filter material of a particle bed a between the gas inlet 7 and the inner member 4 to form gas-solid countercurrent particle bed for dust removal. The pyrolysis gas after preliminary dust removal passes through the inner component 4, enters the dust removal chamber b2 and flows in a radial direction in a staggered manner with the filter material of the moving particle bed b to form gas-solid cross flow particle bed dust removal. The other operation and operation parameters are the same as those of the first embodiment. The dust removal device of the movable particle bed stably runs for 72 hours, and the dust removal efficiency is 99.5 percent.
Example four
Referring to the operation principle of the moving particle bed dust collector shown in fig. 4, the dust chambers are arranged in parallel, and the counter-current-counter-current operation mode is adopted, the flow cross section of the dust chamber of the dust collector of this embodiment is a circular structure, the dust chamber a1 and the dust chamber b2 are arranged in parallel, the ratio of the filtering cross sections of the particle bed is 2:1, and the inner member 4 is a saddle-shaped shutter structure. The 600 ℃ biomass pyrolysis gas enters a dust removal chamber a1 from a gas inlet 7 in a multi-channel form formed by shutters a9 at a gas speed of 0.4m/s, and then flows reversely with a filter material of a particle bed a between the gas inlet 7 and the inner member 4 to form gas-solid countercurrent particle bed for dust removal. The pyrolysis gas after preliminary dust removal passes through the inner component 4 and enters the dust removal chamber b2 to flow reversely with the filter material of the moving particle bed b, and gas-solid countercurrent particle bed dust removal is formed. The other operation and operation parameters are the same as those of the second embodiment. The dust removal device of the movable particle bed stably runs for 96 hours, and the dust removal efficiency is 99.7 percent.
EXAMPLE five
Referring to the operation principle of the moving particle bed dust removing device shown in fig. 5, which is a co-current-cross-current operation mode arranged inside and outside the dust removing chamber, the dust removing chamber of the dust removing device of this embodiment has a circular ring-shaped cross section, the dust removing chamber a1 is located inside the dust removing chamber b2, the ratio of the particle bed filtering cross section areas is 1:2, and the inner member 4 is a saddle-shaped louver structure. During operation, quartz sand with the temperature of 550 ℃ and the particle size of 2-4 mm is input from a filter material inlet a5, and a moving particle bed a with the height of 100mm is formed in a dust chamber a 1; meanwhile, the filter material is input from a filter material inlet b10, and a moving particle bed b with the bed height of 200mm is formed in the dust chamber b 2. The 550 ℃ coal pyrolysis gas enters the dust removal chamber a1 from a gas inlet 7 in a single channel form formed by a baffle b8 of the dust removal chamber a1 at a gas speed of 0.5m/s, the pyrolysis gas and the filter material of the particle bed a between the gas inlet 7 and the inner member 4 flow in the same direction after passing through a gas-solid contact interface of the moving particle bed a to form gas-solid co-flow particle bed for dust removal, tar which is easy to coke/condense in the pyrolysis gas is attached to the surface layer of the filter material, and part of dust is trapped by the filter material; the pyrolysis gas after preliminary dust removal passes through the inner component 4, enters the dust removal chamber b2 and flows in a radial direction in a staggered manner with the filter material of the moving particle bed b to form gas-solid cross flow particle bed dust removal, and dust in the pyrolysis gas is further captured. Finally, the clean pyrolysis gas is separated from the moving particle bed b at the gas-solid separation interface of the dust chamber b2 and then is discharged out of the device through a gas outlet 12 in a multi-channel form formed by a shutter b 14; under the regulation and control of the opening degree of the discharge valve, the filter materials collected by the dust chamber a1 and the annular dust chamber b2 are respectively output from the filter material outlet a6 and the filter material outlet b11 to the dust removal device at the moving speeds of 1.00m/h and 0.40 m/h. The dust removal device of the movable particle bed stably runs for 72 hours, and the dust removal efficiency is 99.2 percent.
EXAMPLE six
Referring to the operation principle of the moving particle bed dust collector shown in fig. 6, which is a co-current-counter-current operation mode with the inside and outside arrangement of the dust chamber, the dust chamber of the dust collector of this embodiment has a rectangular flow cross section, the dust chamber a1 is located inside the dust chamber b2, the ratio of the particle bed filter cross section is 1:5, and the inner member 4 has a saddle-shaped louver structure. During operation, semicoke with the temperature of 750 ℃ and the particle size of 2-8 mm is input from a filter material inlet a5, and a moving particle bed a with the bed height of 200mm is formed in a dust chamber a 1; meanwhile, quartz sand with the temperature of 750 ℃ and the particle size of 1-2 mm is input from a filter material inlet b10, and a moving particle bed b with the bed height of 180mm is formed in the dust removal chamber b 2. The biomass gasified gas at 750 ℃ enters a dust removal chamber a1 from a gas inlet 7 in a single-channel form at a gas speed of 0.3m/s, and after passing through a gas-solid contact interface of a moving particle bed a, the pyrolysis gas and the filter material of the particle bed a between the gas inlet 7 and the inner member 4 flow in the same direction to form gas-solid parallel flow particle bed dust removal; the gasified gas after primary dust removal passes through the inner member 4 and enters the dust removal chamber b2 to flow reversely with the filter material of the moving particle bed b, and gas-solid countercurrent particle bed dust removal is formed. Finally, after the clean gas is separated from the moving particle bed b at the gas-solid separation interface of the dust chamber b2, the clean gas is discharged out of the device through a gas outlet 12 in a single-channel form formed by a baffle c 13; the filter material in the dust chamber a1 is output from the filter material outlet a6 at a moving speed of 1.50m/h under the control of the discharge valve, and the filter material in the rectangular outer ring dust chamber b2 is collected and output from the filter material outlet b11 at a moving speed of 0.15m/h under the control of the discharge valve. The dust removal device of the movable particle bed stably runs for 48 hours, and the dust removal efficiency is 98.8 percent.
EXAMPLE seven
Referring to the operation principle of the moving particle bed dust removing device shown in fig. 7, which is a counter-current-cross-current operation mode with the inside and outside arrangement of the dust removing chamber, the flow cross section of the dust removing chamber of the dust removing device of this embodiment is a circular ring structure, the dust removing chamber a1 is located inside the dust removing chamber b2, the ratio of the filtering cross sections of the particle bed is 1:2, and the inner member 4 is a saddle-shaped louver structure. The filter material is semicoke with the temperature of 550 ℃ and the thickness of 2-4 mm; the 550 ℃ coal pyrolysis gas enters a dust removal chamber a1 from a gas inlet 7 in a multi-channel form formed by shutters a9 at a gas speed of 0.5m/s, and then flows reversely with a filter material of a particle bed a between the gas inlet 7 and the inner member 4 to form gas-solid countercurrent particle bed for dust removal. The pyrolysis gas after preliminary dust removal passes through the inner component 4 and enters the dust removal chamber b2 to flow with the filter material of the particle bed b in a radial cross flow manner, so that gas-solid cross flow particle bed dust removal is formed. Then, under the regulation and control of the opening degree of the discharge valve, the filter materials collected by the dust chamber a1 and the annular dust chamber b2 are respectively output from the filter material outlet a6 and the filter material outlet b11 to the dust removal device at the moving speeds of 1.20m/h and 0.40 m/h. The rest operation and operation parameters are the same as those of the fifth embodiment. The dust removal device of the movable particle bed stably runs for 72 hours, and the dust removal efficiency is 99.3 percent.
Example eight
Referring to the operation principle of the moving particle bed dust collector shown in fig. 8, which is a counter-current-counter-current operation mode with the inside and outside arrangement of the dust chamber, the dust chamber of the dust collector of this embodiment has a circular cross-section, the dust chamber a1 is located inside the dust chamber b2, the ratio of the filtering cross-sectional areas of the particle bed is 1:4, and the inner member 4 is a saddle-shaped louver structure. During operation, medical stone with the temperature of 800 ℃ and the particle size of 2-8 mm is input from a filter material inlet a5, and a moving particle bed a with the bed height of 180mm is formed in a dust chamber a 1; meanwhile, quartz sand with the temperature of 800 ℃ and the particle size of 1-2 mm is input from a filter material inlet b10, and a moving particle bed b with the bed height of 150mm is formed in the dust removal chamber b 2. The biomass gasification gas at 800 ℃ enters a dust removal chamber a1 through a gas inlet 7 in a multi-channel form formed by shutters a9 at a gas speed of 0.4m/s, and then flows reversely with semicoke of a particle bed a between the gas inlet 7 and the inner member 4 to form gas-solid countercurrent particle bed for dust removal. The gasified gas after primary dedusting enters a dedusting chamber b2 through the inner component 4 and flows reversely with the filter material of the particle bed b to form gas-solid countercurrent particle bed dedusting. Finally, after the clean gas is separated from the moving particle bed b at the gas-solid separation interface of the dust chamber b2, the clean gas is discharged out of the device through a gas outlet 12 in a single-channel form formed by a baffle c 13; the filter material in the dust chamber a1 is output from the filter material outlet a6 to the dust removal device at a moving speed of 1.50m/h under the control of the discharge valve, and the filter material in the annular dust chamber b2 is collected and then output from the filter material outlet b11 to the dust removal device at a moving speed of 0.75m/h under the control of the discharge valve. The dust removal device of the movable particle bed stably runs for 64 hours, and the dust removal efficiency is 99.0 percent.
Example nine
Referring to the operation principle of the moving particle bed dust removing device shown in fig. 9, the dust removing chambers are arranged in parallel, and the cross-flow operation mode is a cross-flow cross section of the dust removing chamber of the dust removing device of this embodiment is a rectangular structure, the dust removing chamber a1 is arranged in parallel with the dust removing chamber b2, the ratio of the filtering cross sections of the particle bed is 1:3, and the inner member 4 is a wedge-shaped screen structure. During operation, coal semicoke with the temperature of 800 ℃ and the particle size of 2-4 mm is input from a filter material inlet a5, and a moving particle bed a with the height of 150mm is formed in a dust chamber a 1; meanwhile, the olivine-supported nickel (5 wt%) catalyst with the temperature of 800 ℃ and the particle size of 0.2-2 mm is input from a filter material inlet b10, and a moving particle bed b with the bed height of 180mm is formed in a dust chamber b 2. The biomass gasified gas at 800 ℃ enters a dust removal chamber a1 from a gas inlet 7 in a multi-channel form at a gas speed of 0.7m/s, and then flows with the filter material of the particle bed a between the gas inlet 7 and the inner member 4 in a radial staggered manner to form gas-solid cross flow particle bed dust removal; the gasified gas after primary dust removal passes through the inner component 4 and enters the dust removal chamber b2 to flow in a radial direction in a staggered manner with the filter material of the moving particle bed b, so that dust removal of the gas-solid cross flow particle bed is realized. In addition, the tar in the gasified gas is catalytically reformed under the action of the semicoke and the catalyst while the dust is removed. Finally, the clean modified gasification gas and the filter material are separated in a dust removal chamber b2 and then are discharged from a gas outlet 12 in a multi-channel form; under the regulation and control of the opening degree of the discharge valve, the filter materials collected by the dust chamber a1 and the dust chamber b2 are respectively output from the filter material outlet a6 and the filter material outlet b11 to the dust removal device at the moving speeds of 1.20m/h and 0.40 m/h. The dust removal device of the movable particle bed stably runs for 72 hours, the compositions of biomass gasification gas generation before and after modification are shown in table 1, and the dust removal efficiency is 99.5%.
Table 1 composition of gasification of biomass to produce gas before and after upgrading in example nine
Claims (4)
1. The dust removal device for the moving granular bed of the fuel gas containing tar is characterized by mainly comprising a dust removal chamber a (1) and a dust removal chamber b (2) which are filled with filter materials, wherein the filter materials form a granular bed in the dust removal chamber a (1) and the dust removal chamber b (2); the dust chamber a (1) and the dust chamber b (2) are separated by a baffle plate a (3), the middle part of the baffle plate a (3) is replaced by an inner member (4), and the dust chamber a (1) is communicated with the dust chamber b (2) through a gas flow channel formed by the inner member (4); the upper part of the dust chamber a (1) is provided with a filter material inlet a (5), and the lower part is provided with a filter material outlet a (6); the dust removal chamber a (1) is provided with a gas inlet (7), and the dust removal chamber a (1) forms a gas-solid contact interface through a baffle b (8) or a shutter structure a (9) so that the gas inlet (7) is in a single-channel or multi-channel form; the position of the gas inlet (7) has three arrangement modes, the first mode is that the gas inlet is arranged at the upper part of the dust removal chamber a (1) and is positioned above the inner member (4), so that a filter material between the gas inlet (7) and the inner member (4) forms a filter bed layer with gas-solid parallel flow; the second one is arranged at the lower part of the dust removing chamber a (1), is positioned below the inner member (4) and above the filter material outlet a (6), and leads the filter material between the gas inlet (7) and the inner member (4) to form a filter bed layer of gas-solid countercurrent; the third is that the filter material is arranged in the middle of the dust removing chamber a (1) and is positioned at the same horizontal height with the center of the inner member (4), so that the filter material between the gas inlet (7) and the inner member (4) forms a gas-solid radial cross flow filter bed layer; the upper part of the dust chamber b (2) is provided with a filter material inlet b (10), and the lower part is provided with a filter material outlet b (11); the dust removal chamber b (2) is provided with a gas outlet (12), and the dust removal chamber b (2) forms a gas-solid separation interface through a baffle plate c (13) or a shutter structure b (14) to enable the gas outlet (12) to be in a single-channel or multi-channel form; the position of the gas outlet (12) has two setting modes, one mode is that the gas outlet is arranged in the middle of the dust removal chamber b (2) and is at the same horizontal height with the center of the inner member (4), so that a filter material between the gas outlet (12) and the inner member (4) forms a filter bed layer of gas-solid radial cross flow; the other is arranged at the upper part of the dust removing chamber b (2) and is positioned above the inner member (4), so that the filter material between the gas outlet (12) and the inner member (4) forms a filter bed layer of gas-solid countercurrent; the filter material outlet a (6) and the filter material outlet b (11) are both positioned below the inner member (4) and are respectively connected with the corresponding discharge valves.
2. The dust removing device for the tar-containing fuel gas moving particle bed according to claim 1, wherein the dust removing chamber a (1) and the dust removing chamber b (2) are arranged in parallel or arranged inside and outside.
3. The dust removal device for a moving particle bed of tar-containing fuel gas according to claim 1 or 2, wherein the inner member (4) is a saddle-shaped louver structure or a wedge-shaped screen structure; the circulation cross section of dust removal room a (1) and dust removal room b (2) is rectangular structure, circular structure or ring structure.
4. The dust removing device for the tar-containing fuel gas moving particle bed according to claim 1 or 2, wherein the ratio of the filter cross-sectional areas of the particle bed in the dust removing chamber a (1) and the dust removing chamber b (2) is 5:1 to 1: 5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022070542.XU CN212236464U (en) | 2020-09-21 | 2020-09-21 | Dust removing device for tar-containing fuel gas moving particle bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022070542.XU CN212236464U (en) | 2020-09-21 | 2020-09-21 | Dust removing device for tar-containing fuel gas moving particle bed |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN212236464U true CN212236464U (en) | 2020-12-29 |
Family
ID=73982653
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022070542.XU Active CN212236464U (en) | 2020-09-21 | 2020-09-21 | Dust removing device for tar-containing fuel gas moving particle bed |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN212236464U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112044195A (en) * | 2020-09-21 | 2020-12-08 | 大连理工大学 | Dust removal device and method for tar-containing fuel gas moving particle bed |
| TWI818637B (en) * | 2022-07-22 | 2023-10-11 | 國立中央大學 | Device and controlling method for filtering gas |
-
2020
- 2020-09-21 CN CN202022070542.XU patent/CN212236464U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112044195A (en) * | 2020-09-21 | 2020-12-08 | 大连理工大学 | Dust removal device and method for tar-containing fuel gas moving particle bed |
| TWI818637B (en) * | 2022-07-22 | 2023-10-11 | 國立中央大學 | Device and controlling method for filtering gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN212236464U (en) | Dust removing device for tar-containing fuel gas moving particle bed | |
| CN102908841B (en) | For method and the device of the purification of low-temperature pyrolysis coal gas dust removal | |
| CN1219857C (en) | Solid slag-discharing dry-powder air-current bed gasification process and apparatus | |
| CN106753491A (en) | A kind of solid thermal carriers activation coal gas flashing speed oven coal produces the system and method for coal tar, coal gas and semicoke | |
| CN110052093B (en) | Movable granular bed dust filtering device with automatic grain diameter layering and filter material layering replacement functions | |
| CN104474825B (en) | Multitube high-temperature electromagnetic floating bed dust remover | |
| CN111001239A (en) | Pyrolysis gas dust removal method and device | |
| CN104031693A (en) | Integrated device and process for carrying out desulfurization, dust removal and modification on coal-pyrolyzed gas | |
| CN209901527U (en) | Cyclone filtering combined pyrolysis gas dust removal device capable of adjusting flow velocity | |
| CN112044195A (en) | Dust removal device and method for tar-containing fuel gas moving particle bed | |
| CN107760344B (en) | System and method for preparing coal tar gas by coupling pulverized coal pyrolysis and dust removal | |
| CN109161392B (en) | External heating type rotary furnace coal pyrolysis device with internal dust removal function and method | |
| CN1090518C (en) | Fluid-bed sweetening | |
| CN111826210A (en) | High-temperature dust removal process and device for raw coke oven gas | |
| CN213866091U (en) | High-temperature raw gas movable particle bed dust removal device | |
| CN104593047A (en) | Adsorption desulphurization reaction apparatus and adsorption desulphurization method | |
| CN108325311B (en) | Method and device for prolonging continuous operation period of coal pyrolysis flue gas control treatment equipment | |
| CN112745868A (en) | Pyrolysis device, pyrolysis system and pyrolysis method for coal and biological carbonaceous raw materials | |
| CN212610462U (en) | High-temperature dust removal device for raw coke oven gas | |
| CN202087179U (en) | Petrifaction high-temperature smoke dedusting purification device | |
| CN111004637B (en) | Device for preparing high-quality fuel gas by pyrolyzing carbon-containing raw materials | |
| CN106010657A (en) | Low-tar gasification method for biomass and device for implementing method | |
| CN108913222B (en) | Pyrolysis gas treatment device and treatment method in pulverized coal pyrolysis tar production process | |
| CN109012010B (en) | Bubbling fluidized bed device for regenerating powdery sulfur-carrying activity Jiao Jiexi | |
| CN206408171U (en) | A kind of coal dust fast pyrolysis systems |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |