CN113772769A - Evaporation device and method for removing dichloromethane in high-salinity wastewater - Google Patents
Evaporation device and method for removing dichloromethane in high-salinity wastewater Download PDFInfo
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- CN113772769A CN113772769A CN202111139877.5A CN202111139877A CN113772769A CN 113772769 A CN113772769 A CN 113772769A CN 202111139877 A CN202111139877 A CN 202111139877A CN 113772769 A CN113772769 A CN 113772769A
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- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 title claims abstract description 242
- 239000002351 wastewater Substances 0.000 title claims abstract description 89
- 238000001704 evaporation Methods 0.000 title claims abstract description 44
- 230000008020 evaporation Effects 0.000 title claims abstract description 43
- 238000000034 method Methods 0.000 title claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 88
- 238000009833 condensation Methods 0.000 claims abstract description 41
- 230000005494 condensation Effects 0.000 claims abstract description 41
- 239000007788 liquid Substances 0.000 claims abstract description 23
- 150000003839 salts Chemical class 0.000 claims abstract description 11
- 238000002360 preparation method Methods 0.000 claims abstract description 10
- 230000000694 effects Effects 0.000 claims description 25
- 238000010438 heat treatment Methods 0.000 claims description 17
- 239000011552 falling film Substances 0.000 claims description 10
- 230000001105 regulatory effect Effects 0.000 claims description 9
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- 238000000926 separation method Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 claims 27
- 239000013078 crystal Substances 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 description 4
- 230000009290 primary effect Effects 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 3
- YDVNLQGCLLPHAH-UHFFFAOYSA-N dichloromethane;hydrate Chemical group O.ClCCl YDVNLQGCLLPHAH-UHFFFAOYSA-N 0.000 description 2
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- 229920002284 Cellulose triacetate Polymers 0.000 description 1
- NNLVGZFZQQXQNW-ADJNRHBOSA-N [(2r,3r,4s,5r,6s)-4,5-diacetyloxy-3-[(2s,3r,4s,5r,6r)-3,4,5-triacetyloxy-6-(acetyloxymethyl)oxan-2-yl]oxy-6-[(2r,3r,4s,5r,6s)-4,5,6-triacetyloxy-2-(acetyloxymethyl)oxan-3-yl]oxyoxan-2-yl]methyl acetate Chemical compound O([C@@H]1O[C@@H]([C@H]([C@H](OC(C)=O)[C@H]1OC(C)=O)O[C@H]1[C@@H]([C@@H](OC(C)=O)[C@H](OC(C)=O)[C@@H](COC(C)=O)O1)OC(C)=O)COC(=O)C)[C@@H]1[C@@H](COC(C)=O)O[C@@H](OC(C)=O)[C@H](OC(C)=O)[C@H]1OC(C)=O NNLVGZFZQQXQNW-ADJNRHBOSA-N 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/043—Details
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
- C07C17/383—Separation; Purification; Stabilisation; Use of additives by distillation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/36—Organic compounds containing halogen
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
Abstract
The invention provides an evaporation device for removing dichloromethane in high-salinity wastewater and a preparation method thereof; one of them kind gets rid of evaporation plant of dichloromethane in high salt waste water, including former water pitcher, the output of former water pitcher passes through the raw water pump and connects the pre-heater input, evaporation plant's input is connected to the output of one-level pre-heater, evaporation plant's output is connected and is finally imitated condensation processing apparatus, last condensation processing apparatus connects tail gas processing apparatus and organic liquid export. The evaporator provided by the invention comprises an evaporation device and a tail gas secondary condensation device, and the evaporator can be a single-effect evaporator, a double-effect evaporator, a triple-effect evaporator and the like, and can also be an MVR evaporator; meanwhile, the waste water is separated into water without dichloromethane, salt crystals, organic liquid mainly containing dichloromethane and discharged tail gas through an evaporator.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to an evaporation device and method for removing dichloromethane in high-salinity wastewater.
Background
Methylene dichloride is an organic solvent widely used in industrial production, and is mainly used as a raw material for producing cellulose triacetate films, and is also used as a paint remover and an extracting agent for medicine production, metal degreasing and paint removal, an adhesive, pesticide, chemical production and other fields.
Meanwhile, in the production and manufacturing processes of medicines, coatings and the like, a large amount of dichloromethane wastewater with different concentrations is often generated, and the conventional biochemical sludge method is not good for treatment due to the fact that dichloromethane has accumulation and biological toxicity to organisms. Therefore, if the dichloromethane can be separated from the waste water and refined into high-purity products, the dual requirements of green chemical industry and environmental protection can be met.
The conventional treatment process is rectification and evaporative crystallization, and although the same treatment effect can be achieved, the invention simultaneously achieves the purposes of separating dichloromethane and evaporating high-salt wastewater by a set of device, and can obviously reduce equipment investment and reduce operation energy consumption.
The person skilled in the art is dedicated to solving the above technical drawbacks.
Disclosure of Invention
The invention aims to provide an evaporation device capable of removing dichloromethane in high-salt wastewater and a preparation method thereof, which are used for separating dichloromethane in dichloromethane-water-salt residue (containing other solid matters) systems with different concentrations and realizing high-purity recycling and comprehensive utilization of energy. The invention can recover and obtain the dichloromethane with the content of more than 80 percent (wt), and has low energy consumption, short process flow and less investment.
In order to achieve the purpose, the invention adopts the following technical scheme:
the utility model provides an get rid of evaporation plant of dichloromethane in high salt waste water, its characterized in that, includes former water pitcher, the output of former water pitcher passes through the raw water pump and connects the one-level pre-heater input, evaporation plant's input is connected to the output of one-level pre-heater, evaporation plant's output is connected and is finally imitated condensation processing apparatus, last condensation processing apparatus connects tail gas processing apparatus and organic liquid export.
Preferably, the evaporation device comprises at least one set of heating device and one set of gas-liquid separation device;
each set of heating device comprises a heater, a circulating pump and a separating device; the output end of the heater is connected with the input end of the adjacent heating device through the separating device;
the input end of a heater in the heating device is respectively connected with the output ends of the fresh steam pipe and the primary preheater, the output end of a separating device in the heating device of the tail sleeve is connected with the input end of the heater device, and the output end of the circulating heating device is connected with the final-effect condensation treatment device.
Preferably, the circulation heater device comprises a circulation heater, a three-effect forced circulation pump and a three-effect separator; the input end of the circulating heater is connected with the output end of the separating device in the heating device of the last sleeve, the output end of the circulating heater is connected with the input end of the triple-effect separator, the output end of the triple-effect separator is connected with the other input end of the circulating heater through the triple-effect forced circulation pump, the other output end of the triple-effect separator is connected with the input end of the last-effect condensation processing device, and the third output end of the triple-effect separator is connected with the material outlet.
Preferably, the last effect condensation processing apparatus includes the last effect condenser, evaporation plant's output is connected to the input of last effect condenser, the output of last effect condenser passes through the input of vacuum pump connection one-level tail gas condenser, the input of second grade tail gas condenser is connected to the output of one-level tail gas condenser, tail gas processing apparatus is connected to the output of second grade tail gas condenser, the input of organic liquid jar is connected respectively to another output of one-level tail gas condenser and second grade tail gas condenser, the output of organic liquid jar is connected with the machine liquid export through organic liquid pump.
Preferably, the output end of a heater in the first set of heating device is connected with the input end of a first condensate water tank, the output end of the first condensate water tank is connected with the input end of a second-stage preheater through a condensate water pump, and the output end of the second-stage preheater is connected with an evaporation condensate water discharge pipe; the third output end of the second-effect heater is connected with the input end of the second condensation water tank, the output end of the second condensation water tank is connected with the input end of the last-effect condenser, the output end of the last-effect condenser is connected with the input end of the second condensation water tank, the other output end of the second condensation water tank is connected with the input end of the first-stage preheater through the second condensation water pump, and the output end of the first-stage preheater is connected with the other evaporation condensation water discharge pipe.
The invention also provides an evaporation preparation method for removing dichloromethane in high-salinity wastewater, which comprises the following steps:
the method comprises the following steps: the method comprises the following steps of (1) sequentially conveying a wastewater solution containing 0.5-80% (wt) of dichloromethane and 0.1-20% (wt) of other soluble salts or solid matters from a raw water tank 7 to a primary preheater and a secondary preheater through a raw water pump 11, wherein the temperature reaches 50-90 ℃, then the wastewater enters a bin of a first-effect heater, the wastewater flows in a falling film in the first-effect heater through a first-effect circulating pump, fresh steam provides a heat source for the first-effect heater, and the wastewater is separated into secondary steam containing dichloromethane and a wastewater concentrated solution in a first-effect separator;
step two: the waste water concentrated solution enters a double-effect heater through an adjusting valve, the waste water flows in a falling film mode in a tubular heater through a double-effect circulating pump, secondary steam generated by the first effect provides a heat source for the double-effect heater, and the secondary steam and the waste water concentrated solution containing dichloromethane are separated in a double-effect separator;
step three: the waste water concentrated solution enters a forced circulation heater through a regulating valve, the waste water is forced to flow in a tubular heater through a three-effect forced circulation pump, secondary steam generated by the two-effect provides a heat source for the forced circulation heater, and the secondary steam and the waste water concentrated solution containing dichloromethane are separated in a three-effect separator;
step four: the secondary steam containing dichloromethane generated in the triple-effect separator enters an end-effect condenser, water is condensed by circulating cooling water, and the residual dichloromethane gas and a small part of non-condensable gas enter a vacuum pump;
step five: after the first-effect fresh steam condensed water is condensed, the condensed water automatically flows into a first condensed water tank, is conveyed to a second-stage preheater through a first condensed water pump pipeline, exchanges heat with waste water and then is discharged out of an evaporation device;
step six: the secondary steam condensate water of the second effect automatically flows into the shell pass of the forced circulation heater through a pipeline, and automatically flows into a condensate water tank II and a final effect condenser through a pipeline after being combined with the condensate water flowing into the circulation heater from the three-effect separator; condensed water also enters a condensed water tank II, is pumped to a primary preheater through a condensed water pump for heat exchange and is discharged through an evaporation condensed water discharge pipe;
step seven: conveying dichloromethane gas to the shell side of a primary tail gas condenser through a vacuum pump, and introducing cold water into the tube side at the temperature of 10 ℃. Cooling the gas to 20 ℃, condensing more than 80% of dichloromethane gas in a primary tail gas condenser, wherein the purity can reach more than 99%, and continuously condensing the rest dichloromethane gas in a secondary tail gas condenser;
step eight: cold water is introduced into the tube side of the secondary tail gas condenser at the temperature of-15 ℃. The gas temperature is cooled to-5 ℃, more than 10% of dichloromethane gas is condensed in a first-stage tail gas condenser, the purity can reach more than 10%, and the residual dichloromethane gas is discharged to a tail gas treatment system as tail gas.
Preferably, in the first step, waste water with the flow rate of 5 tons/hour and the flow rate of 3 wt% of dichloromethane, 95.5 wt% of water and 1.5% of salt residues (containing other solid matters) enters a bin of a first-effect heater after being preheated to 70 ℃ by a first-stage preheater and a second-stage preheater, the waste water flows in a falling film mode in the first-effect heater through a first-effect circulating pump, fresh steam provides a heat source for the first-effect heater at 115 ℃, and the waste water is separated into secondary steam (99 ℃,1.5 tons/hour) containing dichloromethane and a waste water concentrated solution (103 ℃,3.5 tons/hour) in a first-effect separator.
Preferably, in the second step, the concentrated wastewater (103 ℃,3.5 tons/hour) enters a double-effect heater through a regulating valve, the wastewater flows in a tube-type heater in a falling film manner through a double-effect circulating pump, secondary steam (99 ℃,1.5 tons/hour) generated in the first effect provides a heat source for the double-effect heater, and the wastewater is separated into the secondary steam (80 ℃,1.5 tons/hour) containing dichloromethane and the concentrated wastewater (85 ℃,2 tons/hour) in a double-effect separator.
Preferably, the wastewater concentrated solution in the third step enters the forced circulation heater through the regulating valve, the wastewater is forced to flow in the tubular heater through the three-effect forced circulation pump, secondary steam (80 ℃,1.5 tons/hour) generated by the second effect provides a heat source for the forced circulation heater, the wastewater is separated into the secondary steam (50 ℃,1.5 tons/hour) containing dichloromethane and the wastewater concentrated solution (60 ℃,0.5 tons/hour) in the three-effect separator, and the wastewater concentrated solution is discharged out of the system.
Preferably, the incondensable gas such as dichloromethane discharged from the two-effect separator in the sixth step and the secondary steam (50 ℃,1.5 tons/hour) containing dichloromethane generated in the three-effect separator enter a final-effect condenser together, circulating cooling water (32 ℃, 220 tons/hour) is used for condensing water, and the residual dichloromethane gas and a small part of the incondensable gas enter a vacuum pump.
The existing wastewater treatment process has the characteristics of long equipment flow, complex process and high operation energy consumption, and compared with the prior art, the invention has the following beneficial effects:
1. the evaporator comprises an evaporation device and a tail gas secondary condensation device.
2. The evaporator can be single-effect, double-effect, triple-effect and the like, and can also be an MVR evaporator.
3. The waste water is separated into water without dichloromethane, salt crystals, organic liquid mainly containing dichloromethane and discharged tail gas by an evaporator.
Drawings
FIG. 1 is a schematic flow diagram of an evaporation preparation method for removing dichloromethane from high-salinity wastewater according to the present invention.
The numbers in the figure are as follows:
1. a primary heater; 2. a dual-effect heater; 3. a circulation heater; 4. a first effect separator; 5. a two-effect separator; 6. a three-effect separator; 7. a raw water tank; 8. a first condensate tank; 9. a second condensed water tank; 10. an organic liquid tank; 11. a raw water pump; 12. a one-effect circulation pump; 13. a two-effect circulating pump; 14. a triple-effect forced circulation pump; 15. a first condensate pump; 16. a second condensate pump; 17. a vacuum pump; 18. an organic liquid pump; 19. a primary preheater; 20. a secondary preheater; 21. a last effect condenser; 22. a first-stage tail gas condenser; 23. and a secondary tail gas condenser.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments.
As shown in fig. 1, the evaporation device for removing dichloromethane from high-salinity wastewater provided by the invention comprises a raw water tank 7, a primary preheater 19, a secondary preheater 20, an evaporation device and a final-effect condensation device; the evaporation device comprises two sets of heating devices and a set of gas-liquid separation device; each set of heating device comprises a heater, a circulating pump and a separating device; wherein the heater comprises a first-effect heater 1 and a second-effect heater 2, the circulating pump comprises a first-effect circulating pump 12 and a second-effect circulating pump 13, and the separating device comprises a first-effect separator 4 and a second-effect separator 5; the circulating heater device comprises a circulating heater 13, a three-effect forced circulating pump 14 and a three-effect separator 6; the final-effect condensation treatment device comprises a final-effect condenser 21, a primary tail gas condenser 22 and a secondary tail gas condenser 23;
the output end of the raw water tank 7 is connected with the input end of a primary preheater 19 through a raw water pump 11, the output end of the primary preheater 19 is connected with the input end of a secondary preheater 20, the output end of the secondary preheater 20 is connected with the input end of a primary-effect heater 1, the output end and the other input end of the primary-effect heater 1 are connected with the input end and the output end of a primary-effect circulating pump 12, and the other output end of the primary-effect heater 1 is connected with the input end of a secondary-effect heater 2 through a primary separator 4; the output end and the other input end of the double-effect heater 2 are connected with the input end and the output end of the double-effect circulating pump 13; the other output end of the two-effect heater 2 is connected with the input end of the circulating heater 3 through the second-stage separator 5, the output end of the circulating heater 3 is connected with the input end of the three-effect separator 6, the output end of the three-effect separator 6 is connected with the other input end of the circulating heater 3 through the three-effect forced circulation pump 14, the other output end of the three-effect separator 6 is connected with a material outlet, and the third output end of the three-effect separator 6 is connected with the input end of the final-effect condenser 21;
the other output of end effect condenser 21 passes through vacuum pump 17 and connects the input of one-level tail gas condenser 22, the input of second grade tail gas condenser 23 is connected to the output of one-level tail gas condenser 22, tail gas processing apparatus is connected to the output of second grade tail gas condenser 23, the input of organic liquid jar 10 is connected respectively to another output of one-level tail gas condenser 22 and another output of second grade tail gas condenser 23, the output of organic liquid jar 10 is connected with the machine liquid export through organic liquid pump 18.
Further, the output end of the first-effect heater 1 is connected with the input end of a first condensate water tank 8, the output end of the first condensate water tank 8 is connected with the input end of a second-stage preheater 20 through a first condensate water pump 15, and the other output end of the second-stage preheater 20 is connected with an evaporation condensate water discharge pipe; the third output end of the second-effect heater 2 is connected with the input end of the second condensation water tank 9, the output end of the second condensation water tank 9 is connected with the input end of the last-effect condenser 21, the output end of the last-effect condenser 21 is connected with the input end of the second condensation water tank 9, the other output end of the second condensation water tank 9 is connected with the input end of the first-stage preheater 19 through the second condensation water pump 16, and the output end of the first-stage preheater 19 is connected with the other evaporation condensation water discharge pipe.
The invention provides an evaporation preparation method for removing dichloromethane in high-salinity wastewater, which comprises the following specific steps:
the method comprises the following steps: waste water containing 3 wt% of dichloromethane, 95.5 wt% of water and 1.5% of salt residues (containing other solid matters) and having a flow rate of 5 tons/hour enters a bin of a primary heater 1 after being preheated to 70 ℃ by a primary preheater 19 and a secondary preheater 20, the waste water flows in the primary heater 1 in a falling film mode through a primary circulating pump 12, fresh steam (115 ℃) provides a heat source for the primary heater 1, and the waste water is separated into secondary steam (99 ℃,1.5 tons/hour) containing dichloromethane and a waste water concentrated solution (103 ℃,3.5 tons/hour) in a primary separator 4.
Step two: the waste water concentrated solution (103 ℃,3.5 tons/hour) enters the double-effect heater 2 through the regulating valve, the waste water flows in a falling film manner in the tubular heater through the double-effect circulating pump 13, secondary steam (99 ℃,1.5 tons/hour) generated in the first effect provides a heat source for the double-effect heater 2, and the waste water is separated into the secondary steam (80 ℃,1.5 tons/hour) containing dichloromethane and the waste water concentrated solution (85 ℃,2 tons/hour) in the double-effect separator 5.
Step three: the waste water concentrated solution enters the forced circulation heater 3 through the regulating valve, the waste water is forced to flow in the tubular heater through the three-effect forced circulation pump 14, secondary steam (80 ℃,1.5 tons/hour) generated by the two effects provides a heat source for the forced circulation heater 3, the waste water is separated into the secondary steam (50 ℃,1.5 tons/hour) containing dichloromethane and the waste water concentrated solution (60 ℃,0.5 tons/hour) in the three-effect separator 6, and the waste water concentrated solution is discharged out of the system.
Step four: the incondensable gas such as dichloromethane and the like discharged by the double-effect heater and the secondary steam (50 ℃,1.5 tons/hour) containing dichloromethane generated in the triple-effect separator 6 enter a final-effect condenser together, the water is condensed by circulating cooling water (32 ℃, 220 tons/hour), and the residual dichloromethane gas and a small part of incondensable gas enter a vacuum pump 17.
Step five: the dichloromethane gas is sent to the shell side of a primary tail gas condenser 22 through a vacuum pump 17, and cold water is introduced into the tube side at the temperature of 10 ℃. Cooling the gas to 20 ℃, condensing more than 80% of dichloromethane gas in a primary tail gas condenser 22, wherein the purity can reach more than 99% at 0.15 ton/h; the remaining dichloromethane gas continues to enter the secondary tail gas condenser 23 for condensation.
Step six: cold water is introduced into the tube pass of the secondary tail gas condenser 23 at the temperature of-15 ℃. The gas temperature is cooled to-5 ℃, more than 10% of dichloromethane gas is condensed in a primary tail gas condenser 22, the purity can reach more than 10%, and the residual dichloromethane gas is discharged to a tail gas treatment system as tail gas.
The evaporator provided by the invention comprises an evaporation device and a tail gas secondary condensation device, and the evaporator can be a single-effect evaporator, a double-effect evaporator, a triple-effect evaporator and the like, and can also be an MVR evaporator; meanwhile, the waste water is separated into water without dichloromethane, salt crystals, organic liquid mainly containing dichloromethane and discharged tail gas through an evaporator. The evaporation preparation method for removing the dichloromethane in the high-salt wastewater is used for separating the dichloromethane in dichloromethane-water-salt residue (containing other solid matters) systems with different concentrations, thereby realizing high-purity recycling and comprehensive utilization of energy. The invention can recover and obtain the dichloromethane with the content of more than 80 percent (wt), and has low energy consumption, short flow of the preparation method and less investment.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", and the like, indicate orientations and positional relationships based on those shown in the drawings, and are used only for convenience of description and simplicity of description, and do not indicate or imply that the equipment or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be considered as limiting the present invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless specifically defined otherwise.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.
Claims (10)
1. The utility model provides an get rid of evaporation plant of dichloromethane in high salt waste water, its characterized in that, includes former water pitcher (7), the output of former water pitcher (7) passes through raw water pump (11) and connects one-level pre-heater (19) input, evaporation plant's input is connected to the output of one-level pre-heater (19), evaporation plant's output is connected and is finally imitated condensation processing apparatus, last condensation processing apparatus connects tail gas processing apparatus and organic liquid export.
2. The evaporation device for removing the dichloromethane in the high-salinity wastewater according to claim 1, wherein the evaporation device comprises at least one set of heating device and one set of gas-liquid separation device;
each set of heating device comprises a heater, a circulating pump and a separating device; the output end of the heater is connected with the input end of the adjacent heating device through the separating device;
the input end of a heater in the heating device is respectively connected with the output ends of a fresh steam pipe and a primary preheater (19), the output end of a separating device in the heating device of the last sleeve is connected with the input end of a circulating heater device, and the output end of the circulating heater device is connected with a last effect condensation treatment device.
3. The evaporation plant for removing dichloromethane from high-salinity wastewater according to claim 1, characterized in that the circulating heater device comprises a circulating heater (13), a three-effect forced circulating pump (14) and a three-effect separator (6); the input of circulation heater (13) is connected the output of separator among the heating device of last cover, the input of triple effect separator (6) is connected to the output of circulation heater (13), the output of triple effect separator (6) is through triple effect forced circulation pump (14) another input of connecting circulation heater (13), the input of end effect condensation processing apparatus is connected to another output of triple effect separator (6), the material export is connected to the third output of triple effect separator (6).
4. The evaporation device for removing dichloromethane in high-salinity wastewater according to claim 1, wherein the last-effect condensation treatment device comprises a last-effect condenser (21), an input end of the last-effect condenser (21) is connected with an output end of the evaporation device, an output end of the last-effect condenser (21) is connected with an input end of a first-stage tail gas condenser (22) through a vacuum pump (17), an output end of the first-stage tail gas condenser (22) is connected with an input end of a second-stage tail gas condenser (23), an output end of the second-stage tail gas condenser (23) is connected with a tail gas treatment device, the other output ends of the first-stage tail gas condenser (22) and the second-stage tail gas condenser (23) are respectively connected with an input end of the organic liquid tank (10), and an output end of the organic liquid tank (10) is connected with an organic liquid outlet through an organic liquid pump (18).
5. The evaporation device for removing the dichloromethane in the high-salinity wastewater according to claim 1, characterized in that the output end of the heater in the first set of heating device is connected with the input end of a first condensation water tank (8), the output end of the first condensation water tank (8) is connected with the input end of a second-stage preheater (20) through a first condensation water pump (15), and the output end of the second-stage preheater (20) is connected with an evaporation condensation water discharge pipe; the third output end of the two-effect heater (2) is connected with the input end of a second condensation water tank (9), the output end of the second condensation water tank (9) is connected with the input end of a final-effect condenser (21), the output end of the final-effect condenser (21) is connected with the input end of the second condensation water tank (9), the other output end of the second condensation water tank (9) is connected with the input end of a first-stage preheater (19) through a second condensation water pump (16), and the output end of the first-stage preheater (19) is connected with the other evaporation condensation water discharge pipe.
6. An evaporation preparation method for removing dichloromethane in high-salinity wastewater is characterized by comprising the following steps:
the method comprises the following steps: the method comprises the following steps of (1) sequentially conveying a wastewater solution containing 0.5-80 wt% of dichloromethane and 0.1-20 wt% of other soluble salts or solid matters from a raw water tank (7) through a raw water pump (11) to a primary preheater (19) and a secondary preheater (20) at the temperature of 50-90 ℃, then conveying the wastewater solution into a bin of a primary heater (1), enabling the wastewater to flow in a falling film mode in the primary heater (1) through a primary circulating pump (12), providing a heat source for the primary heater (1) by using fresh steam, and separating the wastewater solution into secondary steam containing dichloromethane and a wastewater concentrated solution in a primary separator (4);
step two: the waste water concentrated solution enters a double-effect heater (2) through a regulating valve, the waste water flows in a falling film manner in a tubular heater through a double-effect circulating pump (13), secondary steam generated by the first effect provides a heat source for the double-effect heater (2), and the secondary steam and the waste water concentrated solution containing dichloromethane are separated in a double-effect separator (5);
step three: the waste water concentrated solution enters the forced circulation heater (3) through the regulating valve, the waste water is forced to flow in the tubular heater through the three-effect forced circulation pump (14), the secondary steam generated by the two effects provides a heat source for the forced circulation heater (3), and the secondary steam and the waste water concentrated solution containing dichloromethane are separated in the three-effect separator (6);
step four: the secondary steam containing dichloromethane generated in the triple-effect separator (6) enters a final-effect condenser (21), water is condensed by circulating cooling water, and the residual dichloromethane gas and a small part of non-condensable gas enter a vacuum pump (17);
step five: after the first-effect fresh steam condensate water is condensed, the condensate water automatically flows into a condensate water tank I (8), is conveyed to a secondary preheater (20) through a condensate water pump I (15) pipeline, exchanges heat with wastewater and is discharged out of an evaporation device;
step six: the secondary steam condensate water automatically flows into the shell pass of the forced circulation heater (3) through a pipeline, is combined with condensate water flowing into the circulation heater (3) from the triple-effect separator (6), and then automatically flows into a condensate water tank II (9) and a final-effect condenser (21) through a pipeline; condensed water also enters a second condensed water tank (9), is sent to a first-stage preheater (19) through a condensed water pump (16) for heat exchange and is discharged through an evaporated condensed water discharge pipe;
step seven: the dichloromethane gas is sent to the shell side of a primary tail gas condenser (22) through a vacuum pump (17), and cold water is introduced into the tube side at the temperature of 10 ℃. Cooling the gas to 20 ℃, condensing more than 80% of dichloromethane gas in a primary tail gas condenser (22), wherein the purity can reach more than 99%, and continuously feeding the rest dichloromethane gas into a secondary tail gas condenser (23) for condensation;
step eight: cold water is introduced into the tube pass of the secondary tail gas condenser (23) at the temperature of-15 ℃. The gas temperature is cooled to-5 ℃, more than 10 percent of dichloromethane gas is condensed in a primary tail gas condenser (22), the purity can reach more than 10 percent, and the residual dichloromethane gas is discharged to a tail gas treatment system as tail gas.
7. The preparation method of claim 8, wherein in the first step, the wastewater with a flow rate of 5 tons/hour, including 3% (wt) of dichloromethane, 95.5% of water and 1.5% of salt residues (including other solids), is preheated to 70 ℃ by the first-stage preheater (19) and the second-stage preheater (20) and then enters a bin of the first-effect heater (1), the wastewater is made to flow in a falling film manner in the first-effect heater (1) by the first-effect circulating pump (12), fresh steam is used for providing a heat source for the first-effect heater (1) at 115 ℃, and the wastewater is separated into secondary steam (99 ℃,1.5 tons/hour) including dichloromethane and a wastewater concentrated solution (103 ℃,3.5 tons/hour) in the first-effect separator (4).
8. The preparation method of claim 8, wherein in the second step, the concentrated wastewater (103 ℃,3.5 tons/hr) enters the double-effect heater (2) through the regulating valve, the wastewater flows in a tube type heater in a falling film manner through the double-effect circulating pump (13), secondary steam (99 ℃,1.5 tons/hr) generated in the first effect provides a heat source for the double-effect heater (2), and the wastewater is separated into the secondary steam (80 ℃,1.5 tons/hr) containing dichloromethane and the concentrated wastewater (85 ℃,2 tons/hr) in the double-effect separator (5).
9. The method for removing methylene dichloride from high-salinity wastewater according to claim 8, wherein the wastewater concentrated solution in the third step enters the forced circulation heater (3) through a regulating valve, the wastewater is forced to flow in the tubular heater through a three-way forced circulation pump (14), secondary steam (80 ℃,1.5 tons/hour) generated in the second step provides a heat source for the forced circulation heater (3), the wastewater is separated into the secondary steam (50 ℃,1.5 tons/hour) containing methylene dichloride and the wastewater concentrated solution (60 ℃,0.5 tons/hour) in a three-way separator (6), and the wastewater concentrated solution is discharged out of the system.
10. The method for removing methylene dichloride from high-salinity wastewater through evaporation according to claim 8, wherein the incondensable gases such as methylene dichloride discharged from the two-effect separator (5) in the sixth step and the secondary steam (50 ℃,1.5 tons/hour) containing methylene dichloride generated in the three-effect separator (6) enter the final-effect condenser (21), the cooling water is circulated (32 ℃, 220 tons/hour) to condense water, and the residual methylene dichloride gas and a small part of the incondensable gases enter the vacuum pump (17).
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