CN108129291A - A kind of processing system for polymethoxy dimethyl ether brine waste - Google Patents
A kind of processing system for polymethoxy dimethyl ether brine waste Download PDFInfo
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- CN108129291A CN108129291A CN201810112433.4A CN201810112433A CN108129291A CN 108129291 A CN108129291 A CN 108129291A CN 201810112433 A CN201810112433 A CN 201810112433A CN 108129291 A CN108129291 A CN 108129291A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C53/00—Saturated compounds having only one carboxyl group bound to an acyclic carbon atom or hydrogen
- C07C53/02—Formic acid
- C07C53/06—Salts thereof
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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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
-
- 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
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Crystallography & Structural Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention discloses a kind of processing systems for polymethoxy dimethyl ether brine waste.Including I effect evaporation heater, I effect evaporation separation chamber, II effect evaporation heater, II effect evaporation separation chamber, I effect separating pipe is communicated between the discharge port on I effect evaporation heater top and I effect evaporation separation chamber's side wall, I effect circulation pipe is connected between I effect evaporation separation chamber bottom and the feed inlet of I effect evaporation heater bottom end, waste water is communicated on I effect circulation pipe side wall and enters pipe, II effect separating pipe is communicated between the discharge port on II effect evaporation heater top and II effect evaporation separation chamber's side wall.Sodium formate is recycled while the process system processing waste water of the present invention, to realize environmental emission reduction and comprehensive utilization of resources.The COD of condensation waste water after present system desalination（COD）2000mg/L is down to hereinafter, the salt content of the condensation waste water after desalination drops to below 1000PPM.
Description
Technical field
The present invention relates to the sewage disposal of the discharge of polymethoxy dimethyl ether production, specifically a kind of processing polymethoxy two
Methyl ether brine waste process system.
Background technology
Polymethoxy dimethyl ether（DMM3~6）There is the novel environment-friendly fuel oil blend component of application prospect as a kind of pole, have
There is Cetane number high, oxygen content is high, and low temperature flow is good, can significantly improve the combustibility of diesel oil, improves the thermal efficiency, reduces vapour
The advantages such as the discharge of tail gas.
But one brine waste can be generated while polymethoxy dimethyl ether is produced.This strand of brine waste is dense because of saliferous
Degree is high, COD（COD）It is high, it is impossible to be routed directly to sewage-treatment plant, how to recycle this strand of brine waste is urgently
Problem to be solved.It is studied through experimental analysis, the salinity in this strand of brine waste is largely sodium formate, the COD in waste water
Essentially from COOHAerobic generation recycles sodium formate product by multiple-effect evaporation, Crystallization Separation, waste water is condensed after evaporation and is passed through
Sewage-treatment plant is sent to after cooling, so as to reach the protection of environment and comprehensive utilization of resources.
Invention content
Sodium formate is recycled while processing waste water in order to realize, the present invention provides a kind of for polymethoxy dimethyl ether saliferous
The processing system of waste water.
A kind of processing system for polymethoxy dimethyl ether brine waste includes the I effect effect evaporation point of evaporation heater 1, I
The effect evaporation of evaporation heater 3 and II separation chamber 4 is imitated from room 2, II, wherein the I effect effect evaporation of evaporation heater 1 and I separation chamber 2 is formed
I effect upgrading unit, II effect evaporation heater 3 and II effect evaporation separation chamber 4 form II effect upgrading unit, and I effect upgrading unit and
II effect upgrading unit series connection；
It is connected between the discharge port on I 1 top of effect evaporation heater and I effect evaporation 2 side wall of separation chamber by the first separating pipe 5, I effect is steamed
It is connected between hair 2 bottom of separation chamber and the feed inlet of I 1 bottom of effect evaporation heater by first circulation pipe 6；First circulation pipe 6 is also
It connects waste water and enters pipe 7；
It is connected between the discharge port on II 3 top of effect evaporation heater and the side wall of II effect evaporation separation chamber 4 by the second separating pipe 8,
It is connected between the bottom of II effect evaporation separation chamber 4 and the feed inlet of II 3 bottom of effect evaporation heater by second circulation pipe 9, I effect is steamed
Enter pipe 10 by secondary wastewater between the hair discharge port of separation chamber 2 and second circulation pipe 9 to connect；
The top of II effect evaporation separation chamber 4 connects the import of condenser 27 by pipeline, and the bottom of II effect evaporation separation chamber 4 leads to
Cross the import that shurry pump 13 connects crystallizer 11 with slurry pipe 12；The bottom of crystallizer 11 connects the import of centrifuge 15；
Centrifuge 15 isolates crystallization sodium formate and mother liquor；Mother liquor enters mother liquor surge tank 17；The outlet of mother liquor surge tank 17 passes through string
The mother liquor delivery pump 18 of connection divides for two-way, and a-road-through piping connects second circulation pipe 9, and another way is returned by processing waste water
Polymethoxy dimethyl ether device at source；The outlet of condenser 27 import of indirect steam condensate water pot 26, secondary steaming
The outlet indirect steam condensate pump 25 of vapour condensate liquid water pot 26；The shell-side outlet connection I effects of II effect evaporation heater 3 are cold
The import of condensate pump 24, the outlet of I effect condensate pumps 24 connect sewage disposal dress after exporting parallel connection with indirect steam condensate pump 25
It puts；
Be 2~5% by the salt content of processing waste water during work, the salt content of the condensation waste water after desalination drop to 1000PPM with
Under.
The technical solution further limited is as follows：
Pipe 7 is entered by waste water by processing waste water and enters first circulation pipe 6, being heated to 105~130 DEG C through I effect evaporation heater 1 send
Enter I effect evaporation separation chamber 2, after being concentrated by evaporation in I effect evaporation separation chamber 2 in waste water sodium formate a concentration of 10~20%, then by
Secondary wastewater enters pipe 10 and send to second circulation pipe 9, and being heated to 70~90 DEG C by II evaporation heater 3 is sent into II effect evaporation point
From room 4, the sodium formate concentrations after being concentrated by evaporation in II effect evaporation separation chamber 4 in slurry are 35~60%, II effect evaporation separation chamber
Pulp density in 4 is more than sodium formate saturated concentration, and sodium formate crystallization in part is precipitated, and slurry is sent by shurry pump 13 to crystallizer
11, cooling treatment is thickened by crystallizer 11, the solid content of slurry is 20~40%, then enters centrifuge 15 by gravity flow, from
Sodium formate and mother liquor are isolated in scheming 15, and mother liquor enters mother liquor surge tank 17, a part of mother liquor by mother liquor delivery pump 18 send to
Polymethoxy dimethyl ether device reuse, another part mother liquor return to second circulation pipe 9, and the I effects condensation waste water after desalination is imitated cold through I
Condensate pump 24 and II effects condensation waste water are sent to sewage-treatment plant after the pressurization in parallel of indirect steam condensate pump 25.
The II effect evaporation separation chamber 4 includes vaporization chamber and crystallisation chamber, can realize concentration, crystalline element process simultaneously.
I effect circulating pump 21 in the first circulation pipe 6 is installed, II effect circulating pump 22 is installed in second circulation pipe 9.
Reflux line 23 is connected between the slurry pipe 12 and second circulation pipe 9.
The advantageous effects of the present invention embody in the following areas：
(1) present system reasonable design, process equipment is simple, and operation and maintenance costs is low, and the condensation waste water after desalination contains
Salt amount drops to 1000PPM hereinafter, COD（COD）It is down to 2000mg/L and is filled hereinafter, reaching into biochemical sewage processing
The standard put.
Vaporization chamber and crystallisation chamber are set as one by (2) II effect upgrading units, simplify equipment flowsheet, investment reduction.
(3) be concentrated by evaporation using two effects, I effect be concentrated by evaporation after in waste water sodium formate a concentration of 10~20%, II effect is steamed
After hair concentration~45%, II effect upgrading unit heat source evaporates lack of gas using an effect, and heat utilization rate imitates evaporation than I and improves~10%.
(4) while sodium formate in recycling waste water, most of COD in waste water is eliminated（COD）, recycling
Sodium formate can be used as byproduct to sell, chemical oxygen demand of waste water（COD）Removal rate is more than 90%, is realizing that comprehensive utilization of resources is same
When effectively reduce cost for wastewater treatment.
Description of the drawings
Fig. 1 is the processing system figure of the present invention.
Serial number in upper figure：Imitate the effect evaporation separation of evaporation heater 3, II in the I effect effect evaporation of evaporation heater 1, I separation chamber 2, II
Room 4, the first separating pipe 5, first circulation pipe 6, waste water enter pipe 7, the second separating pipe 8, second circulation pipe 9, secondary wastewater entrance
Pipe 10, crystallizer 11, slurry pipe 12, shurry pump 13, the discharge nozzle 14 of crystallizer 11, centrifuge 15, mother liquor pipe 16, mother liquor buffering
Tank 17, mother liquor delivery pump 18, mother liquor delivery pipe 19, mother liquor pump 20, I effect circulating pump 21, II effect circulating pump 22, slurry reflux line
23, I effect condensate pumps 24, indirect steam condensate pump 25, indirect steam condensate water pot 26, condenser 27, vacuum system 28.
Specific embodiment
Below in conjunction with the accompanying drawings, the present invention is further described by embodiment.
Embodiment 1
Referring to Fig. 1, a kind of processing system for polymethoxy dimethyl ether brine waste includes the I effect effect of evaporation heater 1, I and steams
It sends out separation chamber 2, II and imitates the effect evaporation of evaporation heater 3 and II separation chamber 4, wherein the I effect effect evaporation of evaporation heater 1 and I separation chamber 2
I effect upgrading unit is formed, the II effect effect evaporation of evaporation heater 3 and II separation chamber 4 forms II effect upgrading unit, and I effect concentration is single
Member and II effect upgrading unit series connection.II effect evaporation separation chamber 4 includes vaporization chamber and crystallisation chamber, can realize that concentration, crystallization are single simultaneously
First process.
It is connected between the discharge port on I 1 top of effect evaporation heater and I effect evaporation 2 side wall of separation chamber by the first separating pipe 5, I
It is connected between effect evaporation 2 bottom of separation chamber and the feed inlet of I 1 bottom of effect evaporation heater by first circulation pipe 6；First circulation pipe
6, which also connect waste water, enters pipe 7；
It is connected between the discharge port on II 3 top of effect evaporation heater and the side wall of II effect evaporation separation chamber 4 by the second separating pipe 8,
It is connected between the bottom of II effect evaporation separation chamber 4 and the feed inlet of II 3 bottom of effect evaporation heater by second circulation pipe 9, I effect is steamed
Enter pipe 10 by secondary wastewater between the hair discharge port of separation chamber 2 and second circulation pipe 9 to connect；
I effect circulating pump 21 in first circulation pipe 6 is installed, II effect circulating pump 22 is installed in second circulation pipe 9.
The top of II effect evaporation separation chamber 4 connects the import of condenser 27, the bottom of II effect evaporation separation chamber 4 by pipeline
Portion connects the import of crystallizer 11 by shurry pump 13 with slurry pipe 12；The bottom of crystallizer 11 connect centrifuge 15 into
Mouthful；Centrifuge 15 isolates crystallization sodium formate and mother liquor；Mother liquor enters mother liquor surge tank 17；The outlet of mother liquor surge tank 17 passes through
The mother liquor delivery pump 18 of series connection divides for two-way, and a-road-through piping connects second circulation pipe 9, and another way is returned by processing waste water
Polymethoxy dimethyl ether device at source；The outlet of condenser 27 import of indirect steam condensate water pot 26, secondary
The outlet indirect steam condensate pump 25 of steam condensate water pot 26；The shell-side outlet connection I effects of II effect evaporation heater 3
The import of condensate pump 24, the outlet of I effect condensate pumps 24 connect sewage disposal after exporting parallel connection with indirect steam condensate pump 25
Device.
Reflux line 23 is connected between slurry pipe 12 and second circulation pipe 9.
During work, pipe 7 is entered by waste water by processing waste water and enters first circulation pipe 6, is heated to through I effect evaporation heater 1
105~130 DEG C are sent into I effect evaporation separation chambers 2, after being concentrated by evaporation in I effect evaporation separation chamber 2 in waste water sodium formate it is a concentration of
10~20%, then pipe 10 is entered by secondary wastewater and is given to second circulation pipe 9, being heated to 70~90 DEG C by II evaporation heater 3 send
Enter II effect evaporation separation chamber 4, the sodium formate concentrations after being concentrated by evaporation in II effect evaporation separation chamber 4 in slurry are 35~60%, II
Pulp density in effect evaporation separation chamber 4 is more than sodium formate saturated concentration, and sodium formate crystallization in part is precipitated, and slurry passes through shurry pump
13 send to crystallizer 11, thicken cooling treatment by crystallizer 11, the solid content of slurry is 20~40%, then by flowing into certainly
Enter centrifuge 15, centrifuge 15 isolates sodium formate and mother liquor, and mother liquor enters mother liquor surge tank 17, and a part of mother liquor passes through mother liquor
Delivery pump 18 send the reuse at by the source of processing waste water, and another part mother liquor returns to second circulation pipe 9, and the I effects after desalination are cold
Solidifying waste water is sent to sewage disposal through I effect condensate pumps 24 and II effects condensation waste water after the pressurization in parallel of indirect steam condensate pump 25
Device.
Embodiment 2
The present invention is implemented on 50,000 tons/year of polymethoxy dimethyl ethers, and the system structure of the present embodiment is the same as embodiment 1.
Brine waste from polymethoxy dimethyl ether device, 5~10t/h of water, water quality：Formaldehyde（50~100ppm）、
Methanol（50~100ppm）、NaOH（0.2%~1%）, sodium formate（Normal 2%~5%）.Brine waste is sent into first circulation pipe 6, warp
I effect evaporation heater 1 is sent into I and is imitated after being heated to 105~130 DEG C evaporates separation chamber 2, after evaporation section water, in brine waste
The concentration concentration of sodium formate is 10~20%（wt）.Waste water after I effect concentration is sent again to second circulation pipe 9, by II evaporation
Heater 3 is sent into II effect evaporation separation chamber 4 after being heated to 70~90 DEG C, sodium formate further concentrates 35~60%（wt）.Due to this
When slurry concentration be more than saturated concentration, have partial crystals precipitation.Slurry is sent by shurry pump 13 to crystallizer 11, through supercooling
But after crystallizing, the solid content about 20~40% in slurry.Then centrifuge 15 is entered by gravity flow, the solid being centrifuged out is
Sodium formate product, the mother liquor being centrifuged out are introduced into mother liquor surge tank 17, and a part of mother liquor is sent by mother liquor delivery pump 18 to quilt
Handle reuse at the source of waste water, another part mother liquor returns to second circulation pipe 9, and the condensation waste water after desalination send sewage disposal to fill
It puts；The COD of condensation waste water after desalination（COD）2000mg/L is down to hereinafter, the salt content of the condensation waste water after desalination
Drop to below 1000PPM.
Claims (5)
1. a kind of processing system for polymethoxy dimethyl ether brine waste, it is characterised in that：Including I effect evaporation heater
（1）, I effect evaporation separation chamber（2）, II effect evaporation heater（3）With II effect evaporation separation chamber（4）, wherein I effect evaporation heater
（1）With I effect evaporation separation chamber（2）Form I effect upgrading unit, II effect evaporation heater（3）With II effect evaporation separation chamber（4）It forms
II effect upgrading unit, and I effect upgrading unit and II effect upgrading unit series connection；
I effect evaporation heater（1）The discharge port on top and I effect evaporation separation chamber（2）By the first separating pipe between side wall（5）Even
It is logical, I effect evaporation separation chamber（2）Bottom and I effect evaporation heater（1）By first circulation pipe between the feed inlet of bottom（6）Connection；
First circulation pipe（6）It also connects waste water and enters pipe（7）；
II effect evaporation heater（3）The discharge port on top and II effect evaporation separation chamber（4）Side wall between by the second separating pipe（8）
Connection, II effect evaporation separation chamber（4）Bottom with II effect evaporation heater（3）By second circulation pipe between the feed inlet of bottom
（9）Connection, I effect evaporation separation chamber（2）Discharge port and second circulation pipe（9）Between pipe entered by secondary wastewater（10）Connection；
II effect evaporation separation chamber（4）Top condenser is connected by pipeline（27）Import, II effect evaporation separation chamber（4）'s
Bottom passes through shurry pump（13）With slurry pipe（12）Connect crystallizer（11）Import；Crystallizer（11）Bottom connect from
Scheming（15）Import；Centrifuge（15）Isolate crystallization sodium formate and mother liquor；Mother liquor enters mother liquor surge tank（17）；Mother liquor delays
Rush tank（17）Outlet by connect mother liquor delivery pump（18）It is divided into two-way, a-road-through piping connects second circulation pipe
（9）, another way return is by the polymethoxy dimethyl ether device at processing wastewater source；Condenser（27）Outlet it is secondary
Steam condensate (SC) tank（26）Import, indirect steam condensate liquid water pot（26）Outlet indirect steam condensate pump（25）；
II effect evaporation heater（3）Shell-side outlet connection I effect condensate pump（24）Import, I effect condensate pump（24）Outlet and two
Secondary steam condensate (SC) pump（25）Sewage-treatment plant is connected after outlet is in parallel；
Be 2~5% by the salt content of processing waste water during work, the salt content of the condensation waste water after desalination drop to 1000PPM with
Under.
2. it to be used for the processing system of polymethoxy dimethyl ether brine waste according to claim 1, it is characterised in that：It is handled
Waste water enters pipe by waste water（7）Into first circulation pipe（6）, through I effect evaporation heater（1）It is heated to 105~130 DEG C and is sent into I
Effect evaporation separation chamber（2）, in I effect evaporation separation chamber（2）After interior evaporation and concentration in waste water sodium formate a concentration of 10~20%, then
Pipe is entered by secondary wastewater（10）It send to second circulation pipe（9）, by II evaporation heater（3）It is heated to 70~90 DEG C and is sent into II
Effect evaporation separation chamber（4）, in II effect evaporation separation chamber（4）Sodium formate concentrations after interior evaporation and concentration in slurry are 35~60%, II
Effect evaporation separation chamber（4）Interior pulp density is more than sodium formate saturated concentration, and sodium formate crystallization in part is precipitated, and slurry passes through slurry
Pump（13）It send to crystallizer（11）, by crystallizer（11）Cooling treatment is thickened, the solid content of slurry is 20~40%, Ran Houtong
It crosses gravity flow and enters centrifuge（15）, centrifuge（15）Solid sodium formate and mother liquor are isolated, mother liquor enters mother liquor surge tank（17）,
A part of mother liquor passes through mother liquor delivery pump（18）It send to polymethoxy dimethyl ether device reuse, another part mother liquor returns to second and follows
Endless tube（9）, the I effect condensation waste water after desalination imitates condensate pump through I（24）Condensation waste water is imitated through indirect steam condensate pump with II
（25）Sewage-treatment plant is sent to after parallel connection pressurization.
3. polymethoxy dimethyl ether brine waste process system is handled according to claim 1, which is characterized in that described II
Effect evaporation separation chamber（4）Including vaporization chamber and crystallisation chamber, concentration, crystalline element process can be realized simultaneously.
4. polymethoxy dimethyl ether brine waste process system is handled according to claim 1, which is characterized in that described first
Circulation pipe（6）In I effect circulating pump is installed（21）, second circulation pipe（9）In II effect circulating pump is installed（22）.
5. polymethoxy dimethyl ether brine waste process system is handled according to claim 1, which is characterized in that the slurry
Pipe（12）With second circulation pipe（9）Between connect reflux line（23）.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810112433.4A CN108129291B (en) | 2018-02-05 | 2018-02-05 | Treatment system for salt-containing wastewater of polymethoxy dimethyl ether |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810112433.4A CN108129291B (en) | 2018-02-05 | 2018-02-05 | Treatment system for salt-containing wastewater of polymethoxy dimethyl ether |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108129291A true CN108129291A (en) | 2018-06-08 |
| CN108129291B CN108129291B (en) | 2020-09-29 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810112433.4A Active CN108129291B (en) | 2018-02-05 | 2018-02-05 | Treatment system for salt-containing wastewater of polymethoxy dimethyl ether |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109942131A (en) * | 2019-03-04 | 2019-06-28 | 鲁西化工集团股份有限公司氯碱化工分公司 | A kind of dimethylformamide production wastewater treatment and substance recovery process and device |
| CN110817999A (en) * | 2019-12-24 | 2020-02-21 | 江苏科本药业有限公司 | Integrated device and method for continuously pretreating high-COD high-salinity wastewater by adopting same |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203582647U (en) * | 2013-11-21 | 2014-05-07 | 东营市润成碳材料科技有限公司 | Polymethoxyl dimethyl ether production wastewater treatment system |
| WO2015080123A1 (en) * | 2013-11-27 | 2015-06-04 | 住友電気工業株式会社 | Waste water treatment method, membrane distillation module, and waste water treatment device |
-
2018
- 2018-02-05 CN CN201810112433.4A patent/CN108129291B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203582647U (en) * | 2013-11-21 | 2014-05-07 | 东营市润成碳材料科技有限公司 | Polymethoxyl dimethyl ether production wastewater treatment system |
| WO2015080123A1 (en) * | 2013-11-27 | 2015-06-04 | 住友電気工業株式会社 | Waste water treatment method, membrane distillation module, and waste water treatment device |
Non-Patent Citations (2)
| Title |
|---|
| 四川鑫达新能源有限公司: "《5万吨/年聚甲氧基二甲醚项目环保影响报告书》", 6 August 2016 * |
| 李国强: "多效蒸发结晶在硝酸钠废水处理中的应用", 《化工管理》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109942131A (en) * | 2019-03-04 | 2019-06-28 | 鲁西化工集团股份有限公司氯碱化工分公司 | A kind of dimethylformamide production wastewater treatment and substance recovery process and device |
| CN110817999A (en) * | 2019-12-24 | 2020-02-21 | 江苏科本药业有限公司 | Integrated device and method for continuously pretreating high-COD high-salinity wastewater by adopting same |
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| Publication number | Publication date |
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| CN108129291B (en) | 2020-09-29 |
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