CN114485224B - Self-cleaning fluidized bed heat exchanger particle continuous circulation recovery method - Google Patents
Self-cleaning fluidized bed heat exchanger particle continuous circulation recovery method Download PDFInfo
- Publication number
- CN114485224B CN114485224B CN202011147888.3A CN202011147888A CN114485224B CN 114485224 B CN114485224 B CN 114485224B CN 202011147888 A CN202011147888 A CN 202011147888A CN 114485224 B CN114485224 B CN 114485224B
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- liquid
- solid
- fluidized bed
- pipe
- 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
- 239000002245 particle Substances 0.000 title claims abstract description 79
- 238000004140 cleaning Methods 0.000 title claims abstract description 43
- 238000000034 method Methods 0.000 title claims abstract description 13
- 238000011084 recovery Methods 0.000 title description 12
- 239000007787 solid Substances 0.000 claims abstract description 71
- 238000004064 recycling Methods 0.000 claims abstract description 20
- 239000007921 spray Substances 0.000 claims abstract description 14
- 239000007788 liquid Substances 0.000 claims description 41
- 238000009826 distribution Methods 0.000 claims description 33
- 239000007791 liquid phase Substances 0.000 claims description 16
- 238000003860 storage Methods 0.000 claims description 12
- 238000007789 sealing Methods 0.000 claims description 7
- 239000008247 solid mixture Substances 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 239000011148 porous material Substances 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 230000001502 supplementing effect Effects 0.000 claims description 2
- 239000000463 material Substances 0.000 claims 2
- 239000013589 supplement Substances 0.000 abstract description 2
- 239000011324 bead Substances 0.000 description 7
- 230000008901 benefit Effects 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000007790 solid phase Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- GFQYVLUOOAAOGM-UHFFFAOYSA-N zirconium(iv) silicate Chemical compound [Zr+4].[O-][Si]([O-])([O-])[O-] GFQYVLUOOAAOGM-UHFFFAOYSA-N 0.000 description 3
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 2
- -1 polyoxymethylene Polymers 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 229930040373 Paraformaldehyde Natural products 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000007806 chemical reaction intermediate Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000010431 corundum Substances 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 239000010432 diamond Substances 0.000 description 1
- 229910003460 diamond Inorganic materials 0.000 description 1
- 229920006351 engineering plastic Polymers 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 229920006324 polyoxymethylene Polymers 0.000 description 1
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 1
- 239000004810 polytetrafluoroethylene Substances 0.000 description 1
- 229910052573 porcelain Inorganic materials 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D13/00—Heat-exchange apparatus using a fluidised bed
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28G—CLEANING OF INTERNAL OR EXTERNAL SURFACES OF HEAT-EXCHANGE OR HEAT-TRANSFER CONDUITS, e.g. WATER TUBES OR BOILERS
- F28G9/00—Cleaning by flushing or washing, e.g. with chemical solvents
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The invention discloses a self-cleaning fluidized bed heat exchanger for continuously and circularly recycling particles and a particle recycling method of the self-cleaning fluidized bed heat exchanger. The auxiliary spray pipe supplements and balances the kinetic energy of liquid-solid particles from the main pipeline to realize the recycling of the particles in the self-cleaning fluidized bed heat exchanger, thereby realizing the effective recycling of the solid particles.
Description
Technical Field
The invention belongs to the field of chemical industry, in particular to the field of long-period operation of chemical heat exchange equipment, and relates to a particle recycling method of a self-cleaning fluidized bed heat exchanger, which is widely applied to recycling of solid particles in the traditional heat exchanger and pipeline blockage removal process.
Background
Heat exchangers are widely used in petroleum, chemical, energy industries, and the like. However, as the service time increases, dirt adhesion phenomenon is inevitably present in the heat exchanger, so that the heat exchange efficiency of the heat exchanger is reduced, the resistance is increased, and the normal operation of the heat exchanger is affected.
The particle recycling method of the self-cleaning fluidized bed heat exchanger is developed, has the advantages of high particle recycling rate, energy conservation and environmental protection, and can effectively improve the economic benefit of production enterprises.
Whether the solid particles can effectively circulate and uniformly distribute in the fluidized bed heat exchanger in the liquid phase flow velocity range of the heat exchanger is a precondition for restricting the normal operation and large-scale industrial application of the fluidized bed heat exchanger. In the traditional external circulation type fluidized bed heat exchanger, due to pipeline resistance and distribution thereof, solid particles are easily sealed by a liquid column to which a horizontal pipe flows in a circulation process in a downcomer, so that the pipeline fluid of the downcomer is locally short-circuited, the effective circulation of the solid particles is prevented, and the application of the external circulation type fluidized bed heat exchanger is influenced. Document CN202709856U discloses a horizontal liquid-solid circulating fluidized bed heat exchanger using a Kenics static mixer. The fluidized bed heat exchanger solid particles cannot be effectively circulated and can only be used for a horizontal heat exchanger. Document US6350928 discloses an external circulation fluidized bed heat exchanger, which is not provided with a definite solid particle circulation component, and the heat exchanger has weak capability of maintaining a heat transfer effect or cannot normally run in an operation period. Document CN102921179 discloses an external circulation type fluidized bed heat exchanger, which adopts a reducing nozzle between a down pipe and a horizontal pipe to generate negative pressure to realize the circulation of solid particles, and the external circulation type fluidized bed heat exchanger of the structure relates to a nozzle structure, and the matched process conditions have smaller operation elastic space, so that the effective circulation of the solid particles is difficult to realize.
Disclosure of Invention
The invention provides a continuous circulating and recycling device for particles of a fluidized bed heat exchanger, which realizes the circulating and recycling of the particles in the self-cleaning fluidized bed heat exchanger by supplementing and balancing the kinetic energy of liquid-solid particles from a main pipeline through an auxiliary spray pipe, and solves the problems in a targeted way.
The invention aims to solve the technical problem that solid particles of an external circulating type fluidized bed heat exchanger cannot be continuously recycled in the prior art, and provides a self-cleaning type fluidized bed heat exchanger particle continuous recycling device. The recovery device has the advantages of high recovery rate of solid particles, energy conservation and environmental protection.
To solve the above technical problems, a first aspect of the present invention provides a self-cleaning fluidized bed heat exchanger for continuously recycling particles, comprising:
a solid charging tank for storing solid particles;
The heat exchanger tube array is connected with the solid charging tank sequentially through a lower tube box and a main path tube;
The liquid-solid separator is connected with the heat exchanger tube array through a pipeline and an upper tube box and is used for carrying out liquid-solid separation on the liquid-solid mixture from the heat exchanger tube array;
The solid separated by the liquid-solid separator enters a cleaning tank through a pipeline, and the cleaned solid is returned to the solid charging tank;
the liquid obtained by separation of the liquid-solid separator enters a liquid storage tank through a pipeline;
The liquid storage tank is also connected with the heat exchanger tube array through a pipeline and a lower tube box;
wherein, be provided with auxiliary nozzle in the lower pipe case, auxiliary nozzle includes:
one end of the branch pipe is connected with the branch feeding device and is used for receiving branch feeding liquid from the outside;
one end of the circular column is connected with the other end of the branch pipe;
the other end of the circular column is provided with a connecting circular ring sheet, the connecting circular ring sheet and the circular column are concentric and coaxial, one end of the connecting circular ring sheet is connected with the circular column in a sealing way, and the other end of the connecting circular ring sheet is connected with the lower pipe box in a sealing way.
In a preferred embodiment of the present invention, the upper plane of the circular column is symmetrically distributed with distribution holes.
In a preferred embodiment of the present invention, the ratio of the equivalent surface diameter of the distribution Kong Dengbi to the annular column width is 0.1 to 0.9; the porosity of the distribution holes is 0.2-1.
In further preferred embodiments of the present invention, a filter screen is distributed on the upper surface of the distribution hole, and the ratio of the pore diameter of the filter screen to the diameter of the particle is 0.2-0.9.
In a preferred embodiment of the present invention, the bypass pipe is configured such that a ratio of a liquid phase flow rate to a main pipe flow rate is 0.5 to 10.
In a preferred embodiment of the invention, the fluidized bed heat exchanger further comprises a distributor arranged at 1/3-2/3 of the position of the lower pipe box.
In a further preferred embodiment of the present invention, the distributor is one of a flat plate type, a tarpaulin type, a rotary vane type or a combination type.
The invention also provides a metering method of particle recovery rate of the self-cleaning fluidized bed heat exchanger, which adopts the technical scheme for solving the technical problems.
The particle recovery rate calculation formula:
Particle recovery = mass of collected particles/amount of solid particles added 100%
Drawings
FIG. 1 is a schematic view of a particle recovery flow of a self-cleaning fluidized bed heat exchanger according to the present invention.
In FIG. 1, a solid charging tank; 2: a heat exchanger tube array; 3: a liquid-solid separator; 4: a liquid storage tank; 5: a cleaning tank; 6: a liquid circulation pump; 7: a bypass pump; 8: a lower pipe box; 9: a pipe feeding box; 10: a particulate filter plate; 11: a horizontal tube; 12: a drop tube valve; 13: a down pipe; 14: a pre-wash valve; 15, cleaning liquid; 16: a blanking valve; 17: washing residual liquid; 18: an auxiliary spray pipe; 19: a check valve; 20: feeding liquid into a branch; 21: a main pipe; 22: a distributor; 23: a horizontal pipe valve; 24: a liquid storage valve; 25: a main way valve; 26: and a discharge valve.
The upper pipe box 9 is connected with the liquid-solid separator 3, the liquid-solid separator 3 is separated into three paths, one path of solid phase is connected with the descending pipe 13, the other path of solid phase is connected with the cleaning tank 5, solid phase particles separated by the liquid-solid separator 3 enter the solid charging tank 1 for recycling after being washed by the cleaning liquid 15 in the cleaning tank 5, and the washing residual liquid 17 returns to the liquid storage tank 4; one path of liquid phase from the liquid-solid separator 3 is connected with a liquid storage tank 4 from the upper part of the particle filter plate 10, the liquid storage tank 4 is connected with a liquid circulating pump 6, and the liquid circulating pump 6 is connected with a horizontal pipe 11. The branch feeding liquid 20 is pumped out by the branch pump 7 and enters the lower pipe box 8 through the auxiliary spray pipe 18. The liquid-solid particles enter the lower tube box from the main tube 21 and then are converged in the lower tube box 8 with the liquid phase sprayed out from the auxiliary spray tube, and enter the heat exchanger tube array 2 after passing through the distribution plate 22.
Fig. 2 is a schematic structural view of the auxiliary nozzle. Wherein 27 is a branch pipe, 28 is a circular column, 29 is a distribution hole, and 30 is a connecting circular sheet. The connecting circular ring piece 30 is concentric and coaxial with the circular ring column 28, and the outer edge of the connecting circular ring piece 30 is connected with the lower pipe box 8 in a sealing way. The plane of the circular column 28 is symmetrically provided with distribution holes 29. The branch feeding liquid 20 is pumped by the branch pump 7, enters the circular column 28 through the branch pipe 27, and is ejected out of the distribution holes 29 on the plane of the circular column 28, thereby entering the lower pipe box 8.
Detailed Description
The invention will be further described with reference to the accompanying drawings.
In order to make the technical scheme and advantages of the present invention more clear, the scheme in the present invention will be clearly and completely described by examples.
As shown in fig. 1, a self-cleaning fluidized bed heat exchanger for continuous recycling of particles, comprising: the device comprises a solid charging tank (1), a heat exchanger tube nest (2), a liquid-solid separator (3), a liquid storage tank (4), a cleaning tank (5), a liquid circulating pump (6), a bypass pump (7), a lower tube box (8), a horizontal tube (11), a lower tube (13), a blanking valve (16) and an auxiliary spray tube (18); one end of the horizontal pipe (11) is connected with the lower pipe box (8), the other end of the horizontal pipe is connected with the liquid circulating pump (6), one end of the lower pipe box (8) is connected with the horizontal pipe (11), and the other end of the lower pipe box is connected with the auxiliary spray pipe (18); a down pipe (13) communicated with the liquid-solid separator (3) and a blanking valve (16) communicated with the solid charging tank (1) are connected on a horizontal pipe (11) between the liquid circulating pump (6) and the lower pipe box (8).
In the technical scheme, the auxiliary spray pipe (18) comprises a branch pipe (27), a circular column (28) and a connecting circular sheet (30).
In the technical scheme, the auxiliary spray pipe (18), the branch pipe (27) is connected with the lower pipe box (8), and the branch feeding liquid enters the circular column (28) through the branch pipe (27), and the circular column (28) is positioned in the lower pipe box (8).
In the technical scheme, the ratio of the width of the circular column (28) to the diameter of the main path pipe (21) of the auxiliary spray pipe (18) is not lower than 0.5.
In the above technical scheme, the auxiliary spray pipe (18) is characterized in that distribution holes (29) are symmetrically distributed on the upper plane of the circular ring column (28).
In the technical scheme, the distribution holes (29) are of a central symmetrical structure; preferably at least one or a combination of more than one of round, diamond, regular hexagon and regular octagon. The ratio of the equivalent surface diameter of the distribution holes (29) to the width of the circular ring column (28) is 0.1-0.9; the porosity of the distribution holes (29) is 0.2-1.
In the technical scheme, the upper surface of the distribution holes (29) is distributed with a filter screen, and the ratio of the pore diameter of the filter screen to the diameter of the particles is 0.2-0.9.
In the technical scheme, the inner wall of the circular column (28) is connected with the outlet of the main pipeline (21).
In the technical scheme, the outlet of the main pipeline (21) does not exceed the upper plane of the circular column (28), and the ratio of the height of the outlet of the main pipeline (21) from the upper plane of the circular column (28) to the height of the circular column (28) is 0-0.5.
In the technical scheme, the connecting circular ring piece (30) is concentric and coaxial with the circular ring column (28), the inner wall of the connecting circular ring piece (30) is connected with the circular ring column (28) in a sealing way, and the outer edge of the connecting circular ring piece (30) is connected with the lower pipe box (8) in a sealing way.
In the technical scheme, the ratio of the liquid phase flow of the bypass pipe (27) to the flow of the main pipe (21) is 0.5-10.
In the above technical scheme, the distributor (22) is one of a planar plate type, a canopy head type, a rotary vane type, a rotary flow type or a combined type. Preferably, the flat-plate straight-tube combined distributor is arranged at 1/3-2/3 position of the lower pipe box (8), and the distributor (22) is arranged at the position of the lower pipe box.
In the technical scheme, the cleaning solution (15) used by the cleaning tank (5) is one of a reaction intermediate product or a reaction end product.
In the technical scheme, the liquid-solid separator (3) is selected from one of a gravity sedimentation type separator or a cyclone separator.
In the technical scheme, the particle filter plate (10) is arranged in the liquid-solid separator (3) and is positioned below the pipe orifice, inside the pipe orifice or inside the pipe of the liquid pipeline.
In the above technical scheme, the ratio of the aperture of the particle filter plate to the particle diameter is preferably 0.2-0.9.
In the above technical solution, the solid particles used in the fluidized bed heat exchanger are preferably inert particles that do not react with the medium in the application system, and the bulk density of the solid particles is greater than the density of the liquid phase. Still more preferably one or more of zirconium silicate beads, corundum spheres, porcelain spheres, aluminum oxide beads, zirconium silicate beads, glass beads, steel balls, engineering plastics, polyoxymethylene particles, polytetrafluoroethylene particles, small stones, chopped metal wires, rubber spheres, more preferably glass beads, aluminum oxide beads and zirconium silicate beads. The average grain diameter of the particles is 1 mm-5 mm; the average volume solid content of the particles in the fluidized bed heat exchanger is 0.1-6%.
In the technical scheme, the operation range of the circulating water flow rate in the heat exchanger tube nest 2 of the fluidized bed heat exchanger is preferably 0.8-4 m/s.
According to the self-cleaning fluidized bed heat exchanger adopting the technical scheme, under the power supplement effect of the auxiliary spray pipe (18), the liquid-solid mixture in the main pipeline (21) and the liquid pumped out by the branch pump (7) enter the heat exchanger tube array (2) through the lower pipeline box (8); the liquid-solid mixture flows out from the upper pipe box (9) through the heat exchanger tube array (2) and enters the liquid-solid separator (3); part of separated liquid circulating water overflows from the particle filter plate (10) and then enters the liquid storage tank (4), and the other part enters the cleaning tank (5); under the cleaning action of the cleaning liquid (15), the solid particles finish cleaning in the cleaning tank (5) and enter the solid charging tank (1), and the recycling of the solid particles is finished.
The process according to the invention is further illustrated below with reference to examples.
Example 1
A self-cleaning fluidized bed heat exchanger for continuously and circularly recycling particles shown in figure 1 is adopted. The fluidized bed heat exchanger is internally provided with 40 heat exchange tubes, each tube is 1000mm long, the tube diameter is phi 22 multiplied by 1.5mm, and the tubes are arranged in a square shape. The diameter of the horizontal pipe is 50mm, the diameter of the descending pipe is 25mm, the diameter of the main pipe is 50mm, and the diameter of the lower pipe box is 400mm. The solid particles were 10000g of zirconia having a diameter of about 3 mm. The liquid phase is water. The flow rate of the main pipeline is 4m 3/h.
In the auxiliary spray pipe, the pipe diameter of the branch pipe is 50mm. The inner diameter of the circular column is 50mm, the outer diameter of the circular column is 150mm, the width of the circular column is 100mm, and the ratio of the width of the circular column to the diameter of the main pipeline is 2. The center of the upper plane of the circular column is symmetrically provided with circular distribution holes, the equivalent diameter of the surface of the distribution Kong Dengbi is 50mm, the ratio of the equivalent diameter of the surface of the distribution Kong Dengbi to the width of the circular column is 0.5, 4 distribution holes are arranged, and the porosity of the distribution holes is 0.5. The ratio of the aperture of the filter screen to the diameter of the particles in the distribution holes is 0.5, the height of the outlet of the main pipeline from the upper plane of the circular column is 5mm, and the ratio of the height of the outlet of the main pipeline from the upper plane of the circular column to the height of the circular column is 0.05. The liquid phase flow rate of the branch pipe is 4 m 3/h, and the ratio of the liquid phase flow rate of the branch pipe to the flow rate of the main pipe is 1. Under the condition, after stable operation, solid particles collected at the outlet of the discharge valve are 8352 g, and the particle recovery rate is 83.52%.
Examples 2 to 12
A self-cleaning fluidized bed heat exchanger for continuously and circularly recycling particles shown in figure 1 is adopted. Based on example 1, the ratio of the width of the circular column to the diameter of the main pipe (R1), the ratio of the equivalent diameter of the surface of the distribution Kong Dengbi to the width of the circular column (R2), the porosity of the distribution holes (S), the ratio of the diameter of the filter screen in the distribution holes to the diameter of the particles (R3), the ratio of the height of the pipeline outlet from the upper plane of the circular column to the height of the circular column (R4), and the ratio of the liquid phase flow of the branch pipe to the flow of the main pipe (R5) were changed. After steady operation, the mass (M) of solid particles collected at the outlet of the metering valve was measured and the results are shown in table 1.
TABLE 1
Examples 13 to 14
The particle recovery device of the self-cleaning fluidized bed heat exchanger shown in fig. 1 is adopted. The distribution pore type (A) was changed, and the results thereof are shown in Table 2.
TABLE 2
Comparative example 1
A self-cleaning fluidized bed heat exchanger as shown in fig. 1, which is recovered from the continuous circulation of particles, is used. The fluidized bed heat exchanger is internally provided with 40 heat exchange tubes, each tube is 1000mm long, the tube diameter is phi 22 multiplied by 1.5mm, and the tubes are arranged in a square shape. The diameter of the horizontal pipe is 50mm, and the diameter of the descending pipe is 25mm. The liquid phase is water. On the basis of the embodiment 1, the liquid phase flow of the main pipeline is reserved, and the auxiliary nozzle structure is removed. After stable operation, the mass of the solid particles collected by the outlet of the metering valve finds that the particles are not circulated in the heat exchanger and cannot be recycled.
Comparative examples 2 to 6
The particle recovery device of the self-cleaning fluidized bed heat exchanger shown in fig. 1 is adopted. Based on example 1, the ratio of the width of the circular column to the diameter of the main pipe (R1), the ratio of the equivalent diameter of the surface of the distribution Kong Dengbi to the width of the circular column (R2), the porosity of the distribution holes (S), the ratio of the diameter of the filter screen in the distribution holes to the diameter of the particles (R3), the ratio of the height of the pipeline outlet from the upper plane of the circular column to the height of the circular column (R4), and the ratio of the liquid phase flow of the branch pipe to the flow of the main pipe (R5) were changed. After steady operation, the mass (M) of solid particles collected at the outlet of the metering valve was measured and the results are shown in table 3. As is clear from Table 3, the circulation effect was poor.
TABLE 3 Table 3
Comparative example 7
The particle recovery device of the self-cleaning fluidized bed heat exchanger shown in fig. 1 is adopted. The fluidized bed heat exchanger is internally provided with 40 heat exchange tubes, each tube is 1000mm long, the tube diameter is phi 22 multiplied by 1.5mm, and the tubes are arranged in a square shape. The diameter of the horizontal pipe is 50mm, and the diameter of the descending pipe is 25mm. The liquid phase is water. Based on example 1, only the ratio of the bypass liquid phase flow to the main flow was changed. After stable operation, the mass of the solid particles collected by the outlet of the metering valve finds that the particles are not circulated in the heat exchanger and cannot be recycled.
Claims (9)
1. A self-cleaning fluidized bed heat exchanger for continuous recycling of particles, comprising:
a solid charging tank for storing solid particles;
The heat exchanger tube array is connected with the solid charging tank sequentially through a lower tube box and a main path tube;
The liquid-solid separator is connected with the heat exchanger tube array through a pipeline and an upper tube box and is used for carrying out liquid-solid separation on the liquid-solid mixture from the heat exchanger tube array;
The solid separated by the liquid-solid separator enters a cleaning tank through a pipeline, and the cleaned solid is returned to the solid charging tank;
the liquid obtained by separation of the liquid-solid separator enters a liquid storage tank through a pipeline;
The liquid storage tank is also connected with the heat exchanger tube array through a pipeline and a lower tube box;
wherein, be provided with auxiliary nozzle in the lower pipe case, auxiliary nozzle includes:
one end of the branch pipe is connected with the branch feeding device and is used for receiving branch feeding liquid from the outside;
one end of the circular column is connected with the other end of the branch pipe;
The other end of the circular column is provided with a connecting circular ring sheet, the connecting circular ring sheet and the circular column are concentric and coaxial, one end of the connecting circular ring sheet is connected with the circular column in a sealing way, and the other end of the connecting circular ring sheet is connected with the lower pipe box in a sealing way; distribution holes are symmetrically distributed on the upper plane of the circular column,
The inner wall of the circular column is connected with the outlet of the main path pipe, the outer wall of the circular column is connected with the outlet of the branch path pipe, the distribution holes are distributed on the upper plane between the inner wall and the outer wall of the circular column, the branch path material adding liquid enters the circular column through the branch path pipe, then is sprayed out from the distribution holes on the plane of the circular column, and the liquid-solid mixture in the main path pipe and the branch path material adding liquid from the branch path pipe enter the heat exchanger column through the lower pipe box together.
2. The fluidized bed heat exchanger according to claim 1, wherein the distribution Kong Dengbi has a surface equivalent diameter to annular column width ratio of 0.1 to 0.9; the porosity of the distribution holes is 0.2-1.
3. The fluidized bed heat exchanger according to claim 2, wherein a filter screen is distributed on the upper surface of the distribution holes, and the ratio of the pore diameter of the filter screen to the particle diameter is 0.2-0.9.
4. A fluidized bed heat exchanger according to claim 3 wherein the bypass tube is arranged to have a liquid phase flow to main tube flow ratio of 0.5 to 10.
5. The fluidized bed heat exchanger according to any one of claims 1 to 4, wherein the fluidized bed heat exchanger further comprises a distributor installed at 1/3 to 2/3 positions of the down tube box.
6. The fluidized bed heat exchanger according to claim 5, wherein the distributor is one of a flat plate type, a tarpaulin head type, a vane type, a swirl type, or a combination type.
7. A method for recycling particles of a self-cleaning fluidized bed heat exchanger, which adopts the self-cleaning fluidized bed heat exchanger as claimed in any one of claims 1 to 6, comprising;
under the power supplementing effect of the auxiliary spray pipe, the liquid-solid mixture in the main pipeline and the branch pipeline feeding liquid from the branch pipeline enter the heat exchanger tube array through a lower pipeline box;
the liquid-solid mixture and the branch feeding liquid are mixed and then flow out from the upper pipe box to enter the liquid-solid separator through the heat exchanger tube array; the liquid circulating water separated by the liquid-solid separator enters a liquid storage tank, and the separated solid particles enter the cleaning tank; under the cleaning action of the cleaning liquid, the solid particles finish cleaning in the cleaning tank and enter the solid charging tank to finish the recycling of the solid particles.
8. The method of claim 7, wherein the operating range of the circulating water flow rate in the heat exchanger tube array is 0.8-4 m/s.
9. The method according to claim 7 or 8, wherein the solid particles have an average particle diameter of 1mm to 5mm; and the average volume solid content of the solid particles in the fluidized bed heat exchanger is 0.1-6%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011147888.3A CN114485224B (en) | 2020-10-23 | 2020-10-23 | Self-cleaning fluidized bed heat exchanger particle continuous circulation recovery method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011147888.3A CN114485224B (en) | 2020-10-23 | 2020-10-23 | Self-cleaning fluidized bed heat exchanger particle continuous circulation recovery method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114485224A CN114485224A (en) | 2022-05-13 |
| CN114485224B true CN114485224B (en) | 2024-05-03 |
Family
ID=81471023
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011147888.3A Active CN114485224B (en) | 2020-10-23 | 2020-10-23 | Self-cleaning fluidized bed heat exchanger particle continuous circulation recovery method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114485224B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116123898B (en) * | 2023-03-01 | 2024-05-17 | 平顶山泰克斯特高级润滑油有限公司 | Fluidized bed heat exchanger for lubricating oil dewaxing process |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20120020810A (en) * | 2010-08-31 | 2012-03-08 | 한국에너지기술연구원 | Self-cleaning method of circulating fluidized bed with multiple vertical tubes with solid particle storage tank and its self-cleaning type circulating fluidized bed with multiple vertical tubes |
| CN102744173A (en) * | 2012-07-05 | 2012-10-24 | 西安交通大学 | Solid particle pre-whirl mixing pneumatic acceleration device and method |
| US8709335B1 (en) * | 2009-10-20 | 2014-04-29 | Hanergy Holding Group Ltd. | Method of making a CIG target by cold spraying |
| CN105413905A (en) * | 2015-12-10 | 2016-03-23 | 北京七星华创电子股份有限公司 | Two-phase-flow atomized-spray washing device and two-phase-flow atomized-spray washing method |
| CN106440869A (en) * | 2016-08-30 | 2017-02-22 | 朱清敏 | Self-cleaning cyclic heat-exchange device |
| CN107764110A (en) * | 2016-08-23 | 2018-03-06 | 中国石油化工股份有限公司 | The outer circulation type fluid-bed heat exchanger that solid particle fully circulates |
| CN107764109A (en) * | 2016-08-23 | 2018-03-06 | 中国石油化工股份有限公司 | Automatically cleaning fluid-bed heat exchanger |
| CN107764107A (en) * | 2016-08-23 | 2018-03-06 | 中国石油化工股份有限公司 | The method that outer circulation type fluid-bed heat exchanger solid particle fully circulates |
| WO2019097932A1 (en) * | 2017-11-16 | 2019-05-23 | 株式会社Ihi | Energy storage device |
| CN209181517U (en) * | 2018-09-30 | 2019-07-30 | 朝阳市荣富陶瓷有限公司 | A kind of ceramic kiln burning oxygen-enriched combustion-supporting energy saver |
-
2020
- 2020-10-23 CN CN202011147888.3A patent/CN114485224B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8709335B1 (en) * | 2009-10-20 | 2014-04-29 | Hanergy Holding Group Ltd. | Method of making a CIG target by cold spraying |
| KR20120020810A (en) * | 2010-08-31 | 2012-03-08 | 한국에너지기술연구원 | Self-cleaning method of circulating fluidized bed with multiple vertical tubes with solid particle storage tank and its self-cleaning type circulating fluidized bed with multiple vertical tubes |
| CN102744173A (en) * | 2012-07-05 | 2012-10-24 | 西安交通大学 | Solid particle pre-whirl mixing pneumatic acceleration device and method |
| CN105413905A (en) * | 2015-12-10 | 2016-03-23 | 北京七星华创电子股份有限公司 | Two-phase-flow atomized-spray washing device and two-phase-flow atomized-spray washing method |
| CN107764110A (en) * | 2016-08-23 | 2018-03-06 | 中国石油化工股份有限公司 | The outer circulation type fluid-bed heat exchanger that solid particle fully circulates |
| CN107764109A (en) * | 2016-08-23 | 2018-03-06 | 中国石油化工股份有限公司 | Automatically cleaning fluid-bed heat exchanger |
| CN107764107A (en) * | 2016-08-23 | 2018-03-06 | 中国石油化工股份有限公司 | The method that outer circulation type fluid-bed heat exchanger solid particle fully circulates |
| CN106440869A (en) * | 2016-08-30 | 2017-02-22 | 朱清敏 | Self-cleaning cyclic heat-exchange device |
| WO2019097932A1 (en) * | 2017-11-16 | 2019-05-23 | 株式会社Ihi | Energy storage device |
| CN209181517U (en) * | 2018-09-30 | 2019-07-30 | 朝阳市荣富陶瓷有限公司 | A kind of ceramic kiln burning oxygen-enriched combustion-supporting energy saver |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114485224A (en) | 2022-05-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102336849B (en) | Olefin polymerization reactor | |
| CN106504811B (en) | A kind of long-term release filtration system of containment | |
| CN114485224B (en) | Self-cleaning fluidized bed heat exchanger particle continuous circulation recovery method | |
| CN105233605A (en) | Dust removing and purifying device for smoke of boiler | |
| CN108079708A (en) | A kind of circulation scrubbing tower gas distributor and its design method | |
| CN205164393U (en) | Boiler flue gas dust -removal and purification device | |
| CN202028315U (en) | Horizontal type washing tank | |
| CN202356007U (en) | Flue gas purifying recovery system | |
| CN210613282U (en) | Organosilicon unloading tail gas clean-up tower | |
| CN218248691U (en) | Efficient concentration device used in wet synthesis | |
| CN111089286A (en) | Scale prevention and removal circulating fluidized bed heat exchanger and scale prevention and removal circulating method | |
| CN103908930A (en) | Method for cleaning distribution plate of fluidized bed reactor and control system of method | |
| CN211384390U (en) | Efficient dust-containing tail gas washing dust pelletizing system | |
| CN219141625U (en) | Circulation cleaning system of fluidized bed heat exchanger | |
| CN112811568A (en) | Heterogeneous catalysis supercritical water oxidation reactor | |
| CN208553531U (en) | A kind of the mixer wash mill and mixer washing system of dust-laden synthesis gas | |
| CN202590565U (en) | Purifying equipment for acid making with flue gas | |
| CN112591884A (en) | Double-cyclone water distributor and anaerobic reactor | |
| CN102198356B (en) | Dust removal washing and purification device for industrial waste gas | |
| CN215995924U (en) | Combined type washing tower and hydrogen fluoride reactor | |
| CN114405029B (en) | Powder sprayer for producing powdery monoammonium phosphate by high tower | |
| CN209997439U (en) | spandex tail gas purification recovery unit | |
| CN214973043U (en) | High salt waste water bypass flue gas enrichment facility | |
| CN109654912B (en) | Horizontal fluidized bed heat exchanger with particle shell pass | |
| CN203017982U (en) | Spraying and desulfurizing tower capable of preventing wall flow |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |