CN211445385U - Contain organic solvent's salt waste water evaporation equipment - Google Patents
Contain organic solvent's salt waste water evaporation equipment Download PDFInfo
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- CN211445385U CN211445385U CN201921860931.3U CN201921860931U CN211445385U CN 211445385 U CN211445385 U CN 211445385U CN 201921860931 U CN201921860931 U CN 201921860931U CN 211445385 U CN211445385 U CN 211445385U
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Abstract
According to the evaporation equipment for the salt-containing wastewater containing the organic solvent, the raw material preheater, the evaporation heater, the evaporation crystallizer, the hypergravity bed and the condenser which are sequentially connected are arranged along the material direction, and the hypergravity bed is also connected with the distillation heating kettle; a material steam outlet of the evaporation heater is connected with the evaporation crystallizer through a feeding pipe, the evaporation crystallizer is connected with a feed back port of the evaporation heater through a circulating pipe, and a forced circulating pump is arranged on the circulating pipe; the material steam outlet at the top of the evaporative crystallizer is connected with the feed inlet of the supergravity bed, and the material steam outlet at the top of the supergravity bed is connected with the feed inlet of the condenser. The invention recovers the low boiling point organic chemical solvent mixed in water during evaporation, so that the organic solvent can be recycled, and the material cost is saved for users. The evaporation equipment and the evaporation process thereof separate the organic solvent in the wastewater in advance, reduce the content of organic matters in the recovered water and reduce the consumption cost of subsequent biochemical treatment.
Description
Technical Field
The invention relates to the technical field of wastewater evaporation and distillation treatment equipment, in particular to salt-containing wastewater evaporation equipment containing an organic solvent.
Background
Most of the waste water in chemical plants contains certain salt, which affects the propagation of microorganisms in the waste water treatment, and the salt in the waste water needs to be removed for the biochemical treatment. Some waste water contains a certain amount of low-boiling-point organic solvent, a common waste water evaporator only removes salt in the waste water, the recovered water still contains a certain amount of organic solvent, and the biochemical treatment consumes too much medicament.
The existing common wastewater evaporation process can condense an organic chemical solvent mixed with water easily soluble along with water vapor when the organic chemical solvent is evaporated, and the organic chemical solvent mixed with water in recovered water still has higher COD, and still has certain difficulty in subsequent biochemical treatment.
The single-effect or multi-effect evaporator is a process equipment with wider application. It can make materials such as solution, etc. through evaporating partial water content to raise solution concentration, so that the concentration of the solution containing solute can be up to supersaturation, so that the solute can be crystallized and separated out. The method has the advantages of high speed, high efficiency, few working procedures and labor saving, and can meet the requirements of various chemical processes. Has wide prospect in chemical industry, light industry, building material, food, forest chemical industry, medicine, biochemistry and other industries.
Disclosure of Invention
The invention provides the salt-containing wastewater evaporation equipment which is simple in structure and convenient to use and contains the organic solvent, so as to make up the defects of the prior art.
The invention is realized by the following technical scheme:
the invention discloses an evaporation device for salt-containing wastewater containing an organic solvent, which is characterized in that:
a raw material preheater, an evaporation heater, an evaporation crystallizer, a hypergravity bed and a condenser which are connected in sequence are arranged along the material direction, and the hypergravity bed is also connected with a distillation heating kettle;
the raw material preheater is connected with a feed inlet of the evaporation heater;
a material steam outlet of the evaporation heater is connected with the evaporation crystallizer through a feeding pipe, the evaporation crystallizer is connected with a feed back port of the evaporation heater through a circulating pipe, and a forced circulating pump is arranged on the circulating pipe;
the material steam outlet at the top of the evaporative crystallizer is connected with the feed inlet of the hypergravity bed, the material steam outlet at the top of the hypergravity bed is connected with the feed inlet of the condenser, the discharge outlet of the condenser is connected with the organic liquid recovery tank and the reflux port of the hypergravity bed through a three-way pipe, a part of low-boiling-point organic matter materials are collected, and meanwhile, a part of the materials which reflux are circularly condensed in the hypergravity bed are kept in gas-liquid balance.
The separation chamber at the bottom of the evaporative crystallizer is connected with the inlet of a salt slurry pump, and the outlet of the salt slurry pump is connected with a thickener, so that the residual salt slurry after evaporation is discharged.
The liquid outlet at the bottom of the hypergravity bed is connected with the feed inlet of the distillation still, the steam outlet at the top of the distillation still is connected with the feed inlet of the hypergravity bed, and the distillation still circularly heats materials in the hypergravity bed to keep gas-liquid balance in the hypergravity bed.
The raw material preheater, the evaporation heater and the evaporation crystallizer are all heated by steam.
The hypergravity bed can be replaced by a distillation column or a rectification column.
The inlet and the outlet of the forced circulation pump are respectively connected with the circulation pipe through a corrugated pipe.
And a flowmeter is connected between the three-way pipe and the organic liquid recovery tank, and a flowmeter is connected between the three-way pipe and a reflux port of the supergravity bed.
The discharge port of the raw material preheater is connected with the feed port of the evaporation heater through a feeding pipe, a circulating pipe and a forced circulating pump in sequence; the condensed water outlet of the evaporation heater is connected with the heat source inlet of the raw material preheater through a condensed water pipe and a drain valve group, and the raw material preheater is also provided with a heat source water outlet.
The evaporation equipment and the evaporation process have the advantages that the low-boiling-point organic chemical solvent mixed in water is recovered during evaporation, so that the organic solvent is recycled, and the material cost is saved for users. The evaporation equipment and the evaporation process thereof separate the organic solvent in the wastewater in advance, reduce the content of organic matters in the recovered water and reduce the consumption cost of subsequent biochemical treatment (adding medicaments).
The equipment is a set of combined evaporation equipment of forced circulation evaporation and a hypergravity bed, solves the problem of organic solvent recovery, improves the material recovery rate, reduces the subsequent treatment cost, enables sewage to reach the standard and discharge, and achieves the effects of safety, environmental protection and energy conservation.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
In the figure: the system comprises a raw material preheater, a vaporization heater, a forced circulation pump, a vaporization crystallizer, a salt slurry pump, a distillation heating kettle, a supergravity bed, a condenser, a corrugated pipe and a flowmeter, wherein the raw material preheater, the vaporization heater, the forced circulation pump, the evaporation crystallizer, the salt slurry pump, the distillation heating kettle, the supergravity bed, the condenser, the corrugated pipe and the flowmeter are arranged in sequence from 1 to 7. 11 feeding pipes, 12 circulating pipes, 13 condensed water pipes and 14 drain valve groups.
Detailed Description
The attached drawing is an embodiment of the invention.
The invention relates to a salt-containing wastewater evaporation device containing an organic solvent,
a raw material preheater 1, an evaporation heater 2, an evaporation crystallizer 4, a hypergravity bed 7, a condenser 8 and a distillation heating kettle 6 which are connected in sequence are arranged along the direction of the material;
the raw material preheater 1 is connected with a feed inlet of the evaporation heater 2;
a material steam outlet of the evaporation heater 2 is connected with an evaporation crystallizer 4 through a feeding pipe, the evaporation crystallizer 4 is connected with a feed back port of the evaporation heater 2 through a circulating pipe 12, and a forced circulating pump 3 is arranged on the circulating pipe;
the material steam outlet at the top of the evaporative crystallizer 4 is connected with the feed inlet of the hypergravity bed 7, the material steam outlet at the top of the hypergravity bed 7 is connected with the feed inlet of the condenser 8, the discharge outlet of the condenser 8 is connected with the organic liquid recovery tank 9 and the reflux port of the hypergravity bed 7 through a three-way pipe, a part of low-boiling-point organic matter materials are collected, and meanwhile, a part of the materials are refluxed and circularly condensed in the hypergravity bed, so that the gas-liquid balance is kept.
The separation chamber at the bottom of the evaporative crystallizer 4 is connected with the inlet of a salt slurry pump 5, and the outlet of the salt slurry pump is connected with a thickener, so that the residual salt slurry after evaporation is discharged.
The liquid outlet at the bottom of the hypergravity bed 7 is connected with the feed inlet of the distillation still 6, the steam outlet at the top of the distillation still is connected with the feed inlet of the hypergravity bed, and the distillation still circularly heats materials in the hypergravity bed to keep gas-liquid balance in the hypergravity bed.
The raw material preheater 1, the evaporation heater 2 and the evaporation crystallizer 4 are heated by steam.
The hypergravity bed can be replaced by a distillation column or a rectification column.
The inlet and outlet of the forced circulation pump are respectively connected with the circulation pipe through a corrugated pipe 9.
A flowmeter 10 is connected between the three-way pipe and the organic liquid recovery tank, and the flowmeter 10 is connected between the three-way pipe and a reflux port of the supergravity bed.
The discharge port of the raw material preheater 1 is connected with the feed port of the evaporation heater 2 through a feeding pipe 11, a circulating pipe 12 and a forced circulation pump 3; the condensed water outlet of the evaporation heater is connected with the heat source inlet of the raw material preheater through a condensed water pipe 13 and a drain valve group 14, and the raw material preheater is also provided with a heat source water outlet.
The heating temperature of the raw material preheater 1 is 50-60 ℃ (because the quantity of condensed water is limited), the heating temperature of the evaporation heater 2 is 100 ℃, the heating temperature of the evaporation crystallizer 4 is 100 ℃, the heating temperature of the distillation heating kettle 6 is 100 ℃, and the condensing temperature of the condenser 8 is 78-82 ℃; the highest temperature in the hypergravity bed 7 is 100 ℃, and the inside of the hypergravity bed is normal pressure. The supergravity bed has different heights and temperatures, the topmost vapor has the lowest temperature, namely the low-boiling-point organic solvent and less water vapor, so that the supergravity bed separates the low-boiling-point solvent. The bottom liquid in the distillation kettle is water, so that the separation of the low-boiling-point solvent and the water is realized.
The condensing reflux ratio of the low boiling point organic solvent discharged from the condenser is 5:1-7:1, namely, one sixth to one eighth of the organic solvent is collected, and one fifth to seven eighth of the organic solvent is refluxed to the supergravity bed. After a period of evaporation operation, the water liquid discharged from the supergravity bed does not contain the low-boiling point solvent, and the low-boiling point solvent can be recycled, so that the raw material consumption is saved for users, and the production cost is reduced.
The distillation heating kettle 6 is used for circularly heating materials in the supergravity bed, heating the liquid materials returned by reflux, keeping a continuous evaporation state, keeping gas-liquid balance in the supergravity bed, and connecting the bottom of the distillation heating kettle with an evaporation water discharge pipe.
The salt-containing wastewater evaporation equipment containing the organic solvent adopts an automatic control device or a manual control mode. The automatic control device is the prior art.
The working process of the equipment is as follows: raw materials in the raw material preheater 1 enter an evaporation heater 2 and an evaporation crystallizer 4 through a feeding pump, the materials are circularly heated in the evaporation heater 2 and the evaporation crystallizer 4 through a circulating pump 3, steam generated in the evaporation crystallizer 4 after heating enters a supergravity bed 7, distillation operation is carried out in the supergravity bed, the temperature is reduced to a certain extent, organic solvents with low boiling points are distilled out in the supergravity bed, a part of low-boiling-point organic solvents are collected and recycled after being condensed in a condenser, and the other part of low-boiling-point organic solvents flow back to the supergravity bed; discharging the bottom liquid (recovered water) discharged from the supergravity bed into subsequent treatment, performing circulating distillation in a distillation heating kettle, detecting, directly discharging if no other organic matters exist, performing biochemical treatment if organic matters with boiling points higher than that of water exist, and discharging after reaching the standard.
The material concentration in the separation chamber at the bottom of the evaporation crystallizer is gradually increased, solid salt is separated out after supersaturation is achieved, salt slurry is formed at the lower part of the separation chamber, and the salt slurry is pumped into subsequent treatment equipment through a salt slurry pump.
In the hypergravity bed, water vapor and organic matter vapor with the boiling point higher than water are cooled to form liquid, the organic matter vapor with the boiling point lower than the water enters a condenser and then is condensed to form liquid, one part of the liquid is collected after being discharged, the other part of the liquid flows back to the hypergravity bed, the temperature in the hypergravity bed is reduced, and the gas-liquid balance in the hypergravity bed is maintained. The liquid discharged from the bottom of the hypergravity bed is heated into steam by the distillation heating kettle and then is input into the hypergravity bed, so that the temperature in the hypergravity bed is increased, and the gas-liquid balance in the hypergravity bed is maintained.
Claims (8)
1. The utility model provides a contain salt waste water evaporation equipment of organic solvent which characterized in that: a raw material preheater, an evaporation heater, an evaporation crystallizer, a hypergravity bed and a condenser which are connected in sequence are arranged along the material direction, and the hypergravity bed is also connected with a distillation heating kettle;
the raw material preheater is connected with a feed inlet of the evaporation heater;
a material steam outlet of the evaporation heater is connected with the evaporation crystallizer through a feeding pipe, the evaporation crystallizer is connected with a feed back port of the evaporation heater through a circulating pipe, and a forced circulating pump is arranged on the circulating pipe;
the material steam outlet at the top of the evaporative crystallizer is connected with the feed inlet of the hypergravity bed, the material steam outlet at the top of the hypergravity bed is connected with the feed inlet of the condenser, the discharge outlet of the condenser is connected with the organic liquid recovery tank and the reflux port of the hypergravity bed through a three-way pipe, a part of materials are collected, and a part of materials are refluxed to the hypergravity bed.
2. The evaporation equipment of the waste water containing salt and organic solvent of claim 1, characterized in that:
the separation chamber at the bottom of the evaporative crystallizer is connected with the inlet of a salt slurry pump, and the outlet of the salt slurry pump is connected with a thickener, so that the residual salt slurry after evaporation is discharged.
3. The evaporation equipment of the waste water containing salt and organic solvent of claim 1, characterized in that: the liquid outlet at the bottom of the hypergravity bed is connected with the feed inlet of the distillation still, the steam outlet at the top of the distillation still is connected with the feed inlet of the hypergravity bed, and the distillation still circularly heats materials in the hypergravity bed to keep gas-liquid balance in the hypergravity bed.
4. The evaporation equipment of the waste water containing salt and organic solvent of claim 1, characterized in that: the raw material preheater, the evaporation heater and the evaporation crystallizer are all heated by steam.
5. The evaporation equipment of the waste water containing salt and organic solvent of claim 1, characterized in that: the hypergravity bed can be replaced by a distillation column or a rectification column.
6. The evaporation equipment of the waste water containing salt and organic solvent of claim 1, characterized in that: the inlet and the outlet of the forced circulation pump are respectively connected with the circulation pipe through a corrugated pipe.
7. The evaporation equipment of the waste water containing salt and organic solvent of claim 1, characterized in that: and a flowmeter is connected between the three-way pipe and the organic liquid recovery tank, and a flowmeter is connected between the three-way pipe and a reflux port of the supergravity bed.
8. The evaporation equipment of the waste water containing salt and organic solvent of claim 1, characterized in that: the discharge port of the raw material preheater is connected with the feed port of the evaporation heater through a feeding pipe, a circulating pipe and a forced circulating pump; the condensed water outlet of the evaporation heater is connected with the heat source inlet of the raw material preheater through a condensed water pipe and a drain valve group, and the raw material preheater is also provided with a heat source water outlet.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201921860931.3U CN211445385U (en) | 2019-10-31 | 2019-10-31 | Contain organic solvent's salt waste water evaporation equipment |
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| CN201921860931.3U CN211445385U (en) | 2019-10-31 | 2019-10-31 | Contain organic solvent's salt waste water evaporation equipment |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112337130A (en) * | 2020-10-22 | 2021-02-09 | 中北大学 | Device and method for supergravity direct crystallization |
| CN113023994A (en) * | 2021-03-18 | 2021-06-25 | 河南绿水青山环保科技有限公司 | Chemical wastewater treatment and recycling device |
| CN113480095A (en) * | 2021-07-13 | 2021-10-08 | 吴桥县六合德利化工有限责任公司 | Anisaldehyde wastewater recovery treatment process |
| CN114259744A (en) * | 2022-02-11 | 2022-04-01 | 江山力凡蒸发器科技有限公司 | Multiple-effect evaporation crystallization equipment |
-
2019
- 2019-10-31 CN CN201921860931.3U patent/CN211445385U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112337130A (en) * | 2020-10-22 | 2021-02-09 | 中北大学 | Device and method for supergravity direct crystallization |
| CN113023994A (en) * | 2021-03-18 | 2021-06-25 | 河南绿水青山环保科技有限公司 | Chemical wastewater treatment and recycling device |
| CN113023994B (en) * | 2021-03-18 | 2024-04-26 | 河南绿水青山环保科技有限公司 | Chemical wastewater treatment and recycling device |
| CN113480095A (en) * | 2021-07-13 | 2021-10-08 | 吴桥县六合德利化工有限责任公司 | Anisaldehyde wastewater recovery treatment process |
| CN114259744A (en) * | 2022-02-11 | 2022-04-01 | 江山力凡蒸发器科技有限公司 | Multiple-effect evaporation crystallization equipment |
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| Date | Code | Title | Description |
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| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: A salt containing wastewater evaporation equipment containing organic solvent Effective date of registration: 20211230 Granted publication date: 20200908 Pledgee: Shandong Qihe Rural Commercial Bank Co.,Ltd. west market Banking Office Pledgor: Shandong Luli Medicine Chemical Equipment Manufacturing Installation Co.,Ltd. Registration number: Y2021980017115 |
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| PE01 | Entry into force of the registration of the contract for pledge of patent right |