CN219972069U - Treatment device for decomposed waste liquid of coking plant - Google Patents
Treatment device for decomposed waste liquid of coking plant Download PDFInfo
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- CN219972069U CN219972069U CN202320938214.8U CN202320938214U CN219972069U CN 219972069 U CN219972069 U CN 219972069U CN 202320938214 U CN202320938214 U CN 202320938214U CN 219972069 U CN219972069 U CN 219972069U
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- 239000007788 liquid Substances 0.000 title claims abstract description 78
- 238000004939 coking Methods 0.000 title claims abstract description 20
- 239000002699 waste material Substances 0.000 title claims abstract description 18
- 238000002425 crystallisation Methods 0.000 claims abstract description 67
- 230000008025 crystallization Effects 0.000 claims abstract description 65
- 230000001105 regulatory effect Effects 0.000 claims abstract description 9
- 230000003472 neutralizing effect Effects 0.000 claims abstract description 7
- 239000012528 membrane Substances 0.000 claims description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- 239000000463 material Substances 0.000 claims description 13
- 239000012452 mother liquor Substances 0.000 claims description 11
- 238000007710 freezing Methods 0.000 claims description 10
- 238000001914 filtration Methods 0.000 claims description 9
- 230000008014 freezing Effects 0.000 claims description 9
- 238000005273 aeration Methods 0.000 claims description 7
- 238000005260 corrosion Methods 0.000 claims description 5
- 230000007797 corrosion Effects 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 4
- 239000011521 glass Substances 0.000 claims description 4
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 3
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 3
- 238000000354 decomposition reaction Methods 0.000 claims description 2
- 239000010908 plant waste Substances 0.000 claims 1
- 239000002351 wastewater Substances 0.000 description 26
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 9
- 229910052938 sodium sulfate Inorganic materials 0.000 description 9
- 235000011152 sodium sulphate Nutrition 0.000 description 9
- 239000000243 solution Substances 0.000 description 7
- 239000011269 tar Substances 0.000 description 7
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 6
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 6
- 239000013078 crystal Substances 0.000 description 6
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 238000000034 method Methods 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 239000000701 coagulant Substances 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- NESLWCLHZZISNB-UHFFFAOYSA-M sodium phenolate Chemical compound [Na+].[O-]C1=CC=CC=C1 NESLWCLHZZISNB-UHFFFAOYSA-M 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000012670 alkaline solution Substances 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 3
- 239000012267 brine Substances 0.000 description 3
- 239000000084 colloidal system Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000007667 floating Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 235000010265 sodium sulphite Nutrition 0.000 description 3
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 3
- XTEGARKTQYYJKE-UHFFFAOYSA-M Chlorate Chemical compound [O-]Cl(=O)=O XTEGARKTQYYJKE-UHFFFAOYSA-M 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000011280 coal tar Substances 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 229920002943 EPDM rubber Polymers 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000004925 denaturation Methods 0.000 description 1
- 230000036425 denaturation Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 231100000086 high toxicity Toxicity 0.000 description 1
- 238000000265 homogenisation Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-M phenolate Chemical compound [O-]C1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-M 0.000 description 1
- 229940031826 phenolate Drugs 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000009700 powder processing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000001953 recrystallisation Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- Physical Water Treatments (AREA)
Abstract
The utility model discloses a treatment device for decomposed waste liquid of a coking plant, which comprises a pretreatment part and a crystallization part; the pretreatment part comprises a regulating tank, a neutralizing tank, an air floatation tank and a filter which are connected; the crystallization part comprises a crystallization separator communicated with the filter, the crystallization separator is connected with a refrigerating device and a separating device, the refrigerating device comprises a refrigerating unit, the refrigerating unit is communicated with the crystallization separator through a circulating pipeline, the separating device comprises a centrifugal machine communicated with the crystallization separator, and a liquid outlet end of the centrifugal machine is communicated with a liquid inlet end of the crystallization separator through a centrifugal mother liquid return pipeline.
Description
Technical Field
The utility model relates to the technical field of sewage treatment, in particular to a treatment device for decomposed waste liquid of a coking plant.
Background
Coal tar is one of the important byproducts of coal chemical enterprises, and the components of the coal tar are quite complex. A certain amount of sodium phenolate waste water is generated in the deep processing production process of tar. The COD, phenol and other contents in the waste water are too much, and the waste water belongs to the waste water which is difficult to degrade. At present, coal chemical enterprises refer to a coking wastewater treatment method to treat tar deep processing wastewater. However, coking wastewater belongs to high-nitrogen wastewater, tar deep processing wastewater is high-carbon wastewater, the characteristics of key pollutants of the coking wastewater and the tar deep processing wastewater are different, and the same treatment process directly causes that a large amount of dilution water is needed in the treatment process of the tar processing wastewater. The increase in the amount of dilution water means that enterprises pay higher drainage costs each year, bringing certain economic and environmental pressures to the enterprises.
The formation process of the heavy brine is as follows: adding alkaline solution into naphthalene oil, which is a product of a tar processing plant, to extract phenol in the naphthalene oil, wherein the phenol is dissolved in the alkaline solution, the naphthalene oil and the alkaline solution are separated to obtain sodium phenolate, then adding a proper amount of dilute sulfuric acid into the sodium phenolate, reacting the sulfuric acid with the alkaline to obtain sodium sulfate aqueous solution, floating the phenol on the sodium sulfate aqueous solution, and separating to obtain crude phenol and heavy sodium sulfate aqueous solution, wherein each tar processing plant directly discharges the brine without treatment, so as to pollute the land.
The sodium phenolate wastewater is wastewater generated by coarse powder processing. The production wastewater belongs to high-toxicity degradation-resistant high-concentration organic pollution wastewater, contains 200000mg/l of salt, 2500-5000mg/l of phenol and a plurality of other harmful substances. If the waste is directly discharged without treatment, serious environmental pollution is caused.
Disclosure of Invention
The utility model aims to provide a treatment device for decomposed waste liquid of a coking plant, which is used for solving the problems in the background technology.
In order to achieve the above purpose, the present utility model provides the following technical solutions:
a treatment device for decomposed waste liquid of a coking plant comprises a pretreatment part and a crystallization part;
the pretreatment part comprises a regulating tank 1, a neutralizing tank 2, an air floatation tank 3 and a filter 5 which are connected;
the crystallization part comprises a crystallization separator communicated with the filter, the crystallization separator is connected with a refrigerating device and a separating device, the refrigerating device comprises a refrigerating unit, the refrigerating unit is communicated with the crystallization separator through a circulating pipeline, the separating device comprises a centrifugal machine communicated with the crystallization separator, and the liquid outlet end of the centrifugal machine is communicated with the liquid inlet end of the crystallization separator through a centrifugal mother liquor backflow pipeline.
As a further scheme of the utility model: an aeration device is arranged in the regulating tank, a dosing device is arranged on the neutralizing tank, and a venturi mixer is arranged at the liquid inlet end of the air floatation tank.
As a further scheme of the utility model: the device is characterized in that a first middle tank is arranged between the rear end of the air floatation tank and the filter, the liquid outlet end of the filter is connected with a second middle tank, and the liquid outlet end of the second middle tank is communicated with the crystallization separator.
As a further scheme of the utility model: the filter adopts a membrane filter device, the filtering membrane is made of PTFE material, the pore diameter of the filtering membrane is 0.1-0.5 mu m, and the framework of the filtering membrane is made of corrosion-resistant material.
As a further scheme of the utility model: the crystallization separator is provided with a circulating system, the circulating system comprises a circulating liquid inlet, a circulating liquid outlet and a circulating pipeline communicated with the circulating liquid inlet and the circulating liquid outlet, and the circulating liquid inlet and the circulating liquid outlet are communicated with the freezing unit through the circulating pipeline.
As a further scheme of the utility model: the upper end of the crystallization separator is provided with an overflow port, and the overflow port is communicated with the freezing unit through a pipeline.
As a further scheme of the utility model: the overflow port is connected with an overflow pipe, the rear end of the overflow pipe is connected with a buffer water tank, and the liquid outlet end of the buffer water tank is communicated with the refrigerating unit and the circulating system.
As a further scheme of the utility model: and the crystallization separator is provided with a concentrated solution inlet which is communicated with the second intermediate tank through a concentrated solution pipeline.
As a further scheme of the utility model: the crystallization separator lower extreme is equipped with crystallization material feed opening, crystallization material feed opening with centrifuge intercommunication, centrifuge's play liquid end is connected with centrifugal mother liquor buffer tank through centrifugal mother liquor return line, be equipped with concentrate inlet on the crystallization separator, centrifugal mother liquor buffer tank through the pipeline with concentrate import intercommunication.
As a further scheme of the utility model: at least one sight glass is arranged on the crystallization separator.
Compared with the prior art, the utility model has the beneficial effects that:
1. the utility model sets up the freezing crystallization unit to crystallize and separate out sodium sulfate, the energy consumption of freezing crystallization is very low, because the energy consumption of solution refrigeration and freezing is several times smaller than its evaporation heat, only need the electric energy to run; the service life of the equipment is long, and the corrosion degree of the wastewater to the equipment is reduced to the minimum because the freezing and crystallizing system operates at low temperature; the normal pressure low temperature operation is carried out, and the system has no potential safety hazard; the possibility of material denaturation or volatilization does not exist, and the solution does not change the components like high-temperature evaporation in the low-temperature crystallization process; by adopting precooling heat exchange, the energy can be effectively utilized, the operation cost is low, and the operation stability is good.
2. The utility model has the advantages that the high-efficiency crystallization separator is arranged, the crystal forming time is shortened, the concentration of concentrated substances is increased, the crystal particle size is increased, and the subsequent separation and precipitation are facilitated. The high-efficiency crystallization separator is provided with internal circulation to accelerate the internal cold exchange, quickly reduce the system temperature, promote the growth and precipitation of crystals and separate the crystals;
3. the water quality of the water inlet regulating tank is equalized by adopting an aeration mode. On one hand, water quality equalization can be carried out, and on the other hand, sodium sulfite in the wastewater can be oxidized into sodium sulfate in an aeration mode so as to be removed in a subsequent working section; and meanwhile, an air floatation tank is used for removing substances such as oil, suspended matters, colloid particles and the like in the wastewater. The air floatation tank adopts inorganic coagulant and dissolved air micro-bubbles to float upwards to remove impurities, and the inorganic coagulant is added by a Venturi mixer, so that the mixing effect is better.
Drawings
FIG. 1 is a schematic diagram of a processing system according to the present embodiment;
FIG. 2 is a schematic diagram of the connecting lines of the crystallization separator according to the present embodiment.
In the figure: 1-regulating tank, 2-neutralizing tank, 3-air floatation tank, 4-first intermediate tank, 5-filter, 6-second intermediate tank, 7-crystallization separator, 8-freezing unit, 9-centrifuge, 10-overflow port, 11-circulating liquid inlet, 12-circulating liquid outlet, 13-concentrated liquid inlet, 14-crystallization material feed opening, 15-overflow pipe, 16-buffer water tank, 17-circulating pipeline, 18-concentrated liquid pipeline, 19-centrifugal mother liquid reflux pipeline, 20-centrifugal mother liquid buffer tank and 21-sight glass.
Detailed Description
The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
Referring to fig. 1-2, in an embodiment of the present utility model, a treatment apparatus for decomposing waste liquid in a coking plant includes a pretreatment portion and a crystallization portion;
the pretreatment part comprises a regulating tank 1, a neutralizing tank 2, an air floatation tank 3 and a filter 5 which are connected, wherein an aeration device is arranged in the regulating tank 1, so that on one hand, water quality equalization can be carried out, on the other hand, sodium sulfite in the wastewater can be oxidized into sodium sulfate in an aeration mode to be removed in a subsequent working section, a dosing device is arranged on the neutralizing tank 2, and substances such as oil, suspended matters and colloid particles in the wastewater are removed in the air floatation tank. The air floatation tank adopts an inorganic coagulant and dissolved air micro-bubbles to float upwards to remove impurities, the inorganic coagulant is added by a Venturi mixer, the mixing effect is better, a first middle tank 4 is arranged between the rear end of the air floatation tank 3 and a filter 5, the liquid outlet end of the filter 5 is connected with a second middle tank 6, the filter 5 adopts a special membrane to carry out filtering operation, full-quantity filtering is adopted, the whole PLC process is automatically operated, the membrane adopts PTFE materials, and the membrane can resist corrosion of free chlorine and chlorate in brine for a long time; the pore diameter of the membrane is 0.1-0.5 mu m, and the membrane has extremely high porosity and higher filtration and permeation quantity; the thickness of the film is large, and the film is of a one-step molding structure, has no compound and lap joint, can avoid the rupture of the lap joint, and has higher mechanical strength; the membrane component skeleton adopts corrosion-resistant ethylene propylene diene monomer rubber, and the flexible skeleton greatly improves the back cleaning effect; the membrane has smaller filter tube diameter, so that the specific surface area of the filter membrane is larger, and the filter with the same volume can be filled with more filter membranes to increase the filter area; the membrane has the highest temperature resistance of less than or equal to 200 ℃, acid and alkali resistance, oxidation resistance, no adhesion, easy cleaning, high efficiency and high strength.
The crystallization part comprises a crystallization separator 7 communicated with a filter 5, the liquid outlet end of a second intermediate tank 6 is communicated with the crystallization separator 7, the crystallization separator 7 is connected with a refrigerating device and a separating device, the refrigerating device comprises a refrigerating unit 8, the refrigerating unit 8 is communicated with the crystallization separator 7 through a circulating pipeline 17, in the embodiment, a circulating system is arranged on the crystallization separator 7, the circulating system comprises a circulating liquid inlet 11, a circulating liquid outlet 12 and a circulating pipeline 17 communicated with the circulating liquid inlet 11 and the circulating liquid outlet 12, the circulating liquid inlet 11 and the circulating liquid outlet 12 are both communicated with the refrigerating unit 8 through the circulating pipeline 17, the upper end of the crystallization separator 7 is provided with an overflow port 10, the overflow port 10 is communicated with the refrigerating unit 8 through a pipeline, the overflow port 10 is connected with an overflow pipe 15, the rear end of the overflow pipe 15 is connected with a buffer water tank 16, and the liquid outlet end of the buffer water tank 16 is communicated with the refrigerating unit 8 and the circulating system
The separation device comprises a centrifugal machine 9 communicated with the crystallization separator 7, the liquid outlet end of the centrifugal machine 9 is communicated with the liquid inlet end of the crystallization separator 7 through a centrifugal mother liquor backflow pipeline 19, the crystallization separator 7 is provided with a concentrated liquid inlet 13, the concentrated liquid inlet 13 is communicated with the second intermediate tank 6 through a concentrated liquid pipeline 18, the lower end of the crystallization separator 7 is provided with a crystallization material discharging opening 14, the crystallization material discharging opening 14 is communicated with the centrifugal machine 9, the liquid outlet end of the centrifugal machine 9 is connected with a centrifugal mother liquor buffer tank 20 through a centrifugal mother liquor backflow pipeline 19, the crystallization separator 7 is provided with a concentrated liquid inlet 13, the centrifugal mother liquor buffer tank 20 is communicated with the concentrated liquid inlet 13 through a pipeline, and in addition, the crystallization separator 7 is provided with at least one sight glass 21, so that the internal crystallization condition can be observed at any time.
When the utility model is used, the waste liquid and the waste water of the phenolate decomposition of the coking plant enter the regulating tank 1 from the previous working section, are homogenized and oxidized in the regulating tank 1 through the aeration device, and oxidize sodium sulfite into sodium sulfate; the waste water after the homogenization is pumped into a neutralization tank 2, and sodium hydroxide is added into the neutralization tank 2 to adjust the PH value of the waste water to 8-9. And then the wastewater is pumped to an air floatation tank 3, ferric trichloride is added into a venturi mixer at the water inlet end of the air floatation tank 3 for coagulation and flocculation, and impurities are removed by micro-bubble floating, so that oil, suspended matters, colloid particles and the like in the wastewater are removed. The air-floating water enters the first intermediate tank 4, and is pumped into the filter 5 by a pump to further remove tiny suspended matters and the like. The effluent of the filter 5 enters a second intermediate tank 6, is pumped into a high-efficiency crystallization separator 7 through a pump, is subjected to cold energy exchange through a refrigerating system, so that sodium sulfate is separated out when the temperature of the concentrated solution is reduced to the design temperature, and flows into a centrifugal machine 9 for centrifugal separation when the concentration of the concentrated solution reaches a certain crystal concentration, and the sodium sulfate is separated from the system. The dilute concentrated water returns to the front end through an overflow pipe 15 for precooling, and the centrifugal mother liquor returns to the high-efficiency crystallization separator 7 through a centrifugal mother liquor return pipeline 19 for recrystallization. The high-efficiency crystallization separator 7 is provided with an internal circulation system, so that the internal cold exchange can be quickened, the system temperature is quickly reduced, and the growth and precipitation of crystals are promoted and separated.
It will be evident to those skilled in the art that the utility model is not limited to the details of the foregoing illustrative embodiments, and that the present utility model may be embodied in other specific forms without departing from the spirit or essential characteristics thereof. The present embodiments are, therefore, to be considered in all respects as illustrative and not restrictive, the scope of the utility model being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. Any reference sign in a claim should not be construed as limiting the claim concerned.
Furthermore, it should be understood that although the present disclosure describes embodiments, not every embodiment is provided with a separate embodiment, and that this description is provided for clarity only, and that the disclosure is not limited to the embodiments described in detail below, and that the embodiments described in the examples may be combined as appropriate to form other embodiments that will be apparent to those skilled in the art.
Claims (10)
1. A decomposing waste liquid treatment device of a coking plant is characterized by comprising a pretreatment part and a crystallization part;
the pretreatment part comprises an adjusting tank (1), a neutralizing tank (2), an air floatation tank (3) and a filter (5) which are connected;
the crystallization part comprises a crystallization separator (7) communicated with the filter (5), the crystallization separator (7) is connected with a refrigerating device and a separating device, the refrigerating device comprises a refrigerating unit (8), the refrigerating unit (8) is communicated with the crystallization separator (7) through a circulating pipeline (17), the separating device comprises a centrifugal machine (9) communicated with the crystallization separator (7), and the liquid outlet end of the centrifugal machine (9) is communicated with the liquid inlet end of the crystallization separator (7) through a centrifugal mother liquor backflow pipeline (19).
2. The coking plant decomposed waste liquid treatment device according to claim 1, wherein an aeration device is arranged in the regulating tank (1), a dosing device is arranged on the neutralizing tank (2), and a venturi mixer is arranged at the liquid inlet end of the air floatation tank (3).
3. The coking plant decomposed waste liquid treatment device according to claim 1, wherein a first middle tank (4) is arranged between the rear end of the air floatation tank (3) and the filter (5), the liquid outlet end of the filter (5) is connected with a second middle tank (6), and the liquid outlet end of the second middle tank (6) is communicated with the crystallization separator (7).
4. The coking plant decomposed waste liquid treatment device according to claim 1, wherein the filter (5) is a membrane filter device, a filtering membrane of the membrane filter device is made of PTFE material, the pore diameter of the filtering membrane of the membrane filter device is 0.1-0.5 μm, and a framework of the filtering membrane is made of corrosion-resistant material.
5. The coking plant decomposed waste liquid treatment device according to claim 1, wherein the crystallization separator (7) is provided with a circulation system, the circulation system comprises a circulation liquid inlet (11), a circulation liquid outlet (12) and a circulation pipeline (17) communicated with the circulation liquid inlet (11) and the circulation liquid outlet (12), and the circulation liquid inlet (11) and the circulation liquid outlet (12) are communicated with the freezing unit (8) through the circulation pipeline (17).
6. The coking plant decomposed waste liquid treatment device according to claim 1, wherein the upper end of the crystallization separator (7) is provided with an overflow port (10), and the overflow port (10) is communicated with the freezing unit (8) through a pipeline.
7. The coking plant decomposed waste liquid treatment device according to claim 6, wherein the overflow port (10) is connected with an overflow pipe (15), the rear end of the overflow pipe (15) is connected with a buffer water tank (16), and the liquid outlet end of the buffer water tank (16) is communicated with the freezing unit (8) and the circulating system.
8. A coking plant decomposed waste liquid treatment device according to claim 3, wherein the crystallization separator (7) is provided with a concentrated liquid inlet (13), and the concentrated liquid inlet (13) is communicated with the second intermediate tank (6) through a concentrated liquid pipeline (18).
9. The coking plant decomposed waste liquid treatment device according to claim 1, wherein a crystallization material discharging opening (14) is formed in the lower end of the crystallization separator (7), the crystallization material discharging opening (14) is communicated with the centrifugal machine (9), a centrifugal mother liquid buffer tank (20) is connected to the liquid outlet end of the centrifugal machine (9) through a centrifugal mother liquid backflow pipeline (19), a concentrated liquid inlet (13) is formed in the crystallization separator (7), and the centrifugal mother liquid buffer tank (20) is communicated with the concentrated liquid inlet (13) through a pipeline.
10. A plant waste decomposition liquid treatment device according to claim 1, wherein said crystallization separator (7) is provided with at least one sight glass (21).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320938214.8U CN219972069U (en) | 2023-04-21 | 2023-04-21 | Treatment device for decomposed waste liquid of coking plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320938214.8U CN219972069U (en) | 2023-04-21 | 2023-04-21 | Treatment device for decomposed waste liquid of coking plant |
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| Publication Number | Publication Date |
|---|---|
| CN219972069U true CN219972069U (en) | 2023-11-07 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320938214.8U Active CN219972069U (en) | 2023-04-21 | 2023-04-21 | Treatment device for decomposed waste liquid of coking plant |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219972069U (en) |
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