CN107337308A - The device and its technique of glycerine are extracted in a kind of high-salt wastewater concentrate from Epoxy Resin Unit - Google Patents
The device and its technique of glycerine are extracted in a kind of high-salt wastewater concentrate from Epoxy Resin Unit Download PDFInfo
- Publication number
- CN107337308A CN107337308A CN201710561343.9A CN201710561343A CN107337308A CN 107337308 A CN107337308 A CN 107337308A CN 201710561343 A CN201710561343 A CN 201710561343A CN 107337308 A CN107337308 A CN 107337308A
- Authority
- CN
- China
- Prior art keywords
- level
- thin film
- glycerine
- receiving slit
- concentration
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- 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
- C02F1/08—Thin film 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
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- 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
- C02F2001/007—Processes including a sedimentation step
Abstract
The present invention relates to the device and its technique that glycerine is extracted in a kind of high-salt wastewater concentrate from Epoxy Resin Unit, belong to sewage treatment area.The present invention uses one-level forced evaporation and secondary thin film evaporation concentration technique, reclaims glycerine.Glycerine is concentrated to 35%~60% concentration by the mother liquor of glycerol content 20 ~ 35% through primary concentration device, then by two level film evaporation technique by glycerol concentration to 80%~85%；Finally again by three-level film evaporation technique by glycerol concentration to 95% and more than.Environmental problem and the wasting of resources during invention not only avoids evaporation concentrated solution as dangerous liquid waste processing, and improve the quality of solid salt.
Description
Technical field
The present invention relates to the device and its technique that glycerine is extracted in a kind of high-salt wastewater concentrate from Epoxy Resin Unit, category
In sewage treatment area.
Background technology
Epoxy resin is that bisphenol-A and epoxychloropropane generate epoxy resin crude product in the presence of sodium hydroxide, is produced
The a large amount of sodium chloride of by-product in journey, and finally discharge in form of an aqueous solutions, high saliferous, the difficult waste water of high organic matter are formed, this
The mixture of effluent part category high concentrated organic wastewater and inorganic wastewater, composition is extremely complex, can be divided mainly into 3 major classes：(1) have
If glycerine that macromolecular intermediate product in machine owner's epoxy resin production process, a small amount of raw material not reacted completely are formed and
Aged resin etc.；(2) ion such as Na+、Cl-、OH-Deng from raw materials for production and the accessory substance of reaction；(3) water is production process
Water that middle catalyst liquid caustic soda is brought into, generation water and washings etc..In general, about 1.5 can be produced by producing 1 ton of epoxy resin product
The high saliferous of ton, high organic wastewater, seriously limit the development of the sector.
At present, the high saliferous of domestic effective epoxy resin, the advanced handling process technology of high organic wastewater are usually
By high saliferous, high organic wastewater is preprocessed, evaporates, crystallization technique, obtains solid salt, centrifuge mother liquor loops back to evaporation
System, the high boiling point organic compound such as glycerine does not export in the circulatory system in the method, as the higher boilings such as long-term circulation, glycerine have
Machine thing is constantly enriched with evaporation process, not only influences the stability of evaporation equipment production, and need periodically by the steaming containing high salt
Hair concentrate is handled with specific incinerator, and processing cost is high, secondly gained salt poor quality, it is impossible to high-quality salt is obtained,
This phenomenon is inevitable in Epoxy Resin Unit high-salt wastewater evaporation process, governs the hair of epoxy resin industry
Exhibition.
Concentrate after being evaporated present invention is generally directed to Epoxy Resin Unit high-salt wastewater, work is recycled using recycling
Skill, not only glycerine is extracted from concentrate, obtain glycerin by-product product, turn waste into wealth, and can also obtained high-quality
Nacl, while reduce secondary pollution danger waste liquid amount, reach the doulbe-sides' victory of economic value and social value.
The content of the invention
The purpose of the present invention is to overcome above-mentioned weak point, there is provided one kind solves Epoxy Resin Unit high-salt wastewater evaporation skill
The method of the concentration raffinate problem of art, the concentrate that it is obtained after being evaporated using Epoxy Resin Unit high-salt wastewater, will be dense as starting point
Glycerine in contracting liquid extracts, the glycerol concentration two level extracted can reach 80% and more than, three-level can reach 95% and more than,
Environmental problem and the wasting of resources when not only avoid evaporation concentrated solution as dangerous liquid waste processing, and improve solid salt
Quality.
Technical scheme, the device of glycerine, bag are extracted in a kind of high-salt wastewater concentrate from Epoxy Resin Unit
Include one-level feed pump, primary concentration device, one-level discharging pump, settler, the first centrifuge, the first stirring receiving slit, two level charging
Pump, two level thin film evaporator, stirred tank, two level discharging pump, standing groove, the second centrifuge, the second stirring receiving slit, three-level charging
Pump, three-level thin film evaporator, glycerine receiving slit, waste residue groove；
The one-level feed pump is connected with primary concentration device and one-level discharging pump successively, and one-level discharging pump is connected with settler, is sunk
Drop device, it is connected respectively with the first centrifuge and the first stirring receiving slit；
The first stirring receiving slit is connected with two level feed pump, and two level feed pump is connected with two level thin film evaporator, and two level is thin
Film evaporator is connected with stirred tank and two level discharging pump successively；Two level discharging pump be connected with standing groove, and standing groove is respectively with second
Centrifuge and the second stirring receiving slit connection；
The second stirring receiving slit is connected with three-level feed pump, and three-level feed pump connects with glycerine receiving slit and waste residue groove respectively
Connect.
The one-level feed pump is fed by concentration liquid bath；The primary concentration device, two level thin film evaporator and three-level
Thin film evaporator is connected with vacuum condensing system respectively.
The vacuum condensing system includes vacuum equipment, condenser and receiving slit；Wherein, vacuum equipment connects with condenser
Connect, condenser is connected with receiving slit；The primary concentration device, two level thin film evaporator and three-level thin film evaporator respectively with very
Null device connects with condenser；
Receiving slit in the vacuum condensing system being connected with three-level thin film evaporator is glycerine receiving slit.
The technique that glycerine is extracted in the high-salt wastewater concentrate from Epoxy Resin Unit, step are as follows：
（1）Evaporation：The high-salt wastewater collected in base epoxy resin device is obtained containing 20%~30% glycerine once through evaporation
Concentrate；
（2）Primary concentration：By step（1）Concentrate of gained entered one-level charging and is pumped into primary concentration device, with steam plus
Hot primary concentration device, temperature of charge is risen to 70~140 DEG C, concentration is evaporated under the conditions of 0.1~-0.080MPa, by one
After the glycerine of secondary concentrate is concentrated to 40%~60% concentration, the settler with insulation is delivered to one-level discharging pump；Stand, be heavy
Drop, lower floor's salt slurry enter the first centrifuge, and centrifugation obtains solid salt and returns to front evaporator system；Centrifuge mother liquor and upper strata concentration hydrorrhea
It flow to the first stirring receiving slit and obtains secondary concentration liquid, with steam or hot water heating；
（3）Secondary thin film evaporation：By step（2）Gained secondary concentration liquid is delivered to two level thin film evaporator by two level feed pump
Further concentrated by rotary scraper type thin film evaporation；With steam or heat-conducting oil heating, the evaporation of two level thin film evaporator
The glycerine of secondary concentration liquid is concentrated to by the Stress control of system in 0.05~-0.085MPa, temperature control at 90~160 DEG C
80%~85% concentration, the stirred tank with insulation is flowed into certainly, be incubated by the jacket steam of stirred tank, conveyed by two level discharging pump
To groove is stood, the lower floor's liquid for standing groove enters the second centrifuge, the supernatant liquid overflow of centrifuge mother liquor and standing groove to second
Stirring receiving slit obtains concentrate three times, with steam or hot water heating；
（4）Thin film evaporation three times：By step（3）Concentrate is delivered to three-level thin film evaporator to gained by three-level feed pump three times
Further refine, with steam or heat-conducting oil heating, the Stress control of three-level thin film evaporator system -0.07~-
0.095MPa, for temperature control at 160 DEG C~200 DEG C, the condensed device of top gas of three-level thin film evaporator is cooled to glycerine
Receiving slit, the bottom of three-level thin film evaporator obtain waste residue.
The glycerol concentration finally given be 95% and more than.
Beneficial effects of the present invention：
1st, using one-level forced evaporation and secondary thin film evaporation evaporation concentration technique, glycerine is reclaimed.The mother of glycerol content 20 ~ 35%
Glycerine is concentrated to 35%~60% concentration by liquid through primary concentration device, then by two level film evaporation technique by glycerol concentration to 80%
~85%；Finally again by three-level film evaporation technique by glycerol concentration to 95% and more than；
2nd, vapo(u)rization system uses negative pressure, reduces the requirement of thermal source；
3rd, feed liquid realizes the separation of solid salt and crude glycerine by centrifuge after evaporating, and glycerine can be sold outside, have certain economy
Value；
4th, automatically controlled using DCS, convenient operation and management, security and stability is high.
5th, recovering and reutilizing waste water caused by dual evaporation improves the recycling rate of waterused of water, the reduction of waste liquid in production
Substantially, liquid waste processing expense is saved；
6th, the stability of vapo(u)rization system is improved, significantly extends the cycle of operation.
Brief description of the drawings
Fig. 1 is apparatus of the present invention schematic diagram.
Description of reference numerals：1st, one-level feed pump；2nd, primary concentration device；3rd, one-level discharging pump；4th, settler；5th, first from
Scheming；6th, the first stirring receiving slit；7th, two level feed pump；8th, two level thin film evaporator；9th, stirred tank；10th, two level discharging pump；
11st, groove is stood；12nd, the second centrifuge；13rd, the second stirring receiving slit；14th, three-level feed pump；15th, three-level thin film evaporator；16、
Glycerine receiving slit；17th, waste residue groove；18th, liquid bath is concentrated；19th, vacuum condensing system；191st, vacuum equipment；192nd, condenser；193、
Receiving slit.
Embodiment
Embodiment 1
As shown in figure 1, the device of glycerine is extracted in a kind of high-salt wastewater concentrate from Epoxy Resin Unit, including one-level feed pump
1st, primary concentration device 2, one-level discharging pump 3, settler 4, the first centrifuge 5, first stirring receiving slit 6, two level feed pump 7, two
Level thin film evaporator 8, stirred tank 9, two level discharging pump 10, standing groove 11, the second centrifuge 12, second stirring receiving slit 13, three
Level feed pump 14, three-level thin film evaporator 15, glycerine receiving slit 16, waste residue groove 17；
The one-level feed pump 1 is connected with primary concentration device 2 and one-level discharging pump 3 successively, and one-level discharging pump 3 connects with settler 4
Connect, settler 4, be connected respectively with the first centrifuge 5 and the first stirring receiving slit 6；
The first stirring receiving slit 6 is connected with two level feed pump 7, and two level feed pump 7 is connected with two level thin film evaporator 8, and two
Level thin film evaporator 8 is connected with stirred tank 9 and two level discharging pump 10 successively；Two level discharging pump 10 is connected with standing groove 11, is stood
Groove 11 is connected with the second centrifuge 12 and the second stirring receiving slit 13 respectively；
It is described second stirring receiving slit 13 is connected with three-level feed pump 14, three-level feed pump 14 respectively with glycerine receiving slit 16 and give up
Slag chute 17 connects.
The one-level feed pump 1 is fed by concentration liquid bath 18；The primary concentration device 2, the and of two level thin film evaporator 8
Three-level thin film evaporator 15 is connected with vacuum condensing system 19 respectively.
The vacuum condensing system 19 includes vacuum equipment 191, condenser 192 and receiving slit 193；Wherein, vacuum equipment
191 are connected with condenser 192, and condenser 192 is connected with receiving slit 193；The primary concentration device 2, the and of two level thin film evaporator 8
Three-level thin film evaporator 15 connects with vacuum equipment 191 and condenser 192 respectively；
Receiving slit 193 in the vacuum condensing system 19 being connected with three-level thin film evaporator 15 is glycerine receiving slit 16.
Certain the Epoxy Resin Unit high-salt wastewater of Application Example 1
The mother liquor 500kg/h of glycerol content 20%, through primary concentration device 2（80 DEG C of operating temperature, operating pressure 20KPa）Evaporation, one
It is 184kg/h that level inspissator 2 top, which obtains steam condensate (SC), and the bottom of primary concentration device 2 obtains concentrate 316kg/h, into the
One centrifuge 5, solid salt about 60kg/h, a concentrate about 266kg/h, glycerol content（Quality）About 37.6%；
Secondary concentration liquid passes through two level thin film evaporator 8 again（150 DEG C of temperature, pressure 70KPa）, top obtains steam condensate (SC)
117kg/h, bottom obtain concentrate 149kg/h, and into centrifuge, the kg/h of solid salt about 29.5, secondary concentration liquid is about
119.5kg/h, wherein glycerol concentration about 82.6%, secondary concentration liquid is finally by the evaporation technique of three-level thin film evaporator 15（Temperature
190 DEG C, press 10KPa）, it is 94.5kg/h that top, which obtains glycerine condensate liquid, and bottom waste residue is about 25kg/h.
Certain the Epoxy Resin Unit high-salt wastewater of Application Example 2
The mother liquor 800kg/h of glycerol content 25%, through primary concentration device 3（90 DEG C of operating temperature, operating pressure 25KPa）Evaporation, it is dense
It is 270kg/h to obtain steam condensate (SC) at the top of contracting device, and inspissator bottom obtains concentrate 530kg/h, into centrifuge, solid salt
About 95kg/h, a concentrate about 435kg/h, glycerol content（Quality）About 48%, secondary concentration liquid passes through two level thin film evaporation again
Technology（175 DEG C of temperature, pressure 60KPa）, top obtains steam condensate (SC) 152kg/h, and bottom obtains concentrate 283kg/h, entered
Enter centrifuge, solid salt about 54kg/h, secondary concentration liquid about 229kg/h, wherein glycerol concentration about 87%, secondary concentration liquid is last
Pass through three-level film evaporation technique（185 DEG C of temperature, press 5KPa）, it is 206kg/h that top, which obtains glycerine condensate liquid, and bottom waste residue is about
For 23kg/h.
Claims (5)
1. the device of glycerine is extracted in a kind of high-salt wastewater concentrate from Epoxy Resin Unit, it is characterized in that：Fed including one-level
Pump（1）, primary concentration device（2）, one-level discharging pump（3）, settler（4）, the first centrifuge（5）, first stirring receiving slit（6）、
Two level feed pump（7）, two level thin film evaporator（8）, stirred tank（9）, two level discharging pump（10）, stand groove（11）, second centrifugation
Machine（12）, second stirring receiving slit（13）, three-level feed pump（14）, three-level thin film evaporator（15）, glycerine receiving slit（16）, it is useless
Slag chute（17）；
The one-level feed pump（1）Successively with primary concentration device（2）With one-level discharging pump（3）Connection, one-level discharging pump（3）With sinking
Device drops（4）Connection, settler（4）, respectively with the first centrifuge（5）With the first stirring receiving slit（6）Connection；
The first stirring receiving slit（6）With two level feed pump（7）Connection, two level feed pump（7）With two level thin film evaporator（8）
Connection, two level thin film evaporator（8）Successively with stirred tank（9）With two level discharging pump（10）Connection；Two level discharging pump（10）With it is quiet
Put groove（11）Connection, stand groove（11）Respectively with the second centrifuge（12）With the second stirring receiving slit（13）Connection；
The second stirring receiving slit（13）With three-level feed pump（14）Connection, three-level feed pump（14）Respectively with glycerine receiving slit
（16）With waste residue groove（17）Connection.
2. the device of glycerine is extracted from Epoxy Resin Unit high-salt wastewater concentrate as claimed in claim 1, it is characterized in that：Institute
State one-level feed pump（1）By concentration liquid bath（18）Fed；The primary concentration device（2）, two level thin film evaporator（8）With three
Level thin film evaporator（15）Respectively and vacuum condensing system（19）Connection.
3. the device of glycerine is extracted from Epoxy Resin Unit high-salt wastewater concentrate as claimed in claim 2, it is characterized in that：Institute
State vacuum condensing system（19）Including vacuum equipment（191）, condenser（192）And receiving slit（193）；Wherein, vacuum equipment
（191）With condenser（192）Connection, condenser（192）With receiving slit（193）Connection；The primary concentration device（2）, two level it is thin
Film evaporator（8）With three-level thin film evaporator（15）Respectively and vacuum equipment（191）And condenser（192）Connection；
Described and three-level thin film evaporator（15）The vacuum condensing system of connection（19）In receiving slit（193）As glycerine receives
Groove（16）.
4. the technique of glycerine, its feature are extracted described in one of claim 1-3 from Epoxy Resin Unit high-salt wastewater concentrate
It is that step is as follows：
（1）Evaporation：The high-salt wastewater collected in base epoxy resin device is obtained containing 20%~30% glycerine once through evaporation
Concentrate；
（2）Primary concentration：By step（1）Concentrate of gained entered one-level feed pump（1）It is sent into primary concentration device（2）, use
Steam heats primary concentration device（2）, temperature of charge is risen to 70~140 DEG C, is evaporated under the conditions of 0.1~-0.080MPa
Concentration, after the glycerine of a concentrate is concentrated into 35%~60% concentration, with one-level discharging pump（3）It is delivered to the sedimentation with insulation
Device（4）；Stand, sedimentation, lower floor's salt slurry enters the first centrifuge（5）, centrifuge and obtain solid salt return front evaporator system；Centrifugation is female
Liquid and upper strata concentrate overflow are to the first stirring receiving slit（6）Secondary concentration liquid is obtained, with steam or hot water heating；
（3）Secondary thin film evaporation：By step（2）Gained secondary concentration liquid passes through two level feed pump（7）It is delivered to the steaming of two level film
Send out device（8）Further concentrated by rotary scraper type thin film evaporation；With steam or heat-conducting oil heating, two level thin film evaporator
（8）Vapo(u)rization system Stress control in 0.05~-0.085MPa, temperature control is at 90~160 DEG C, by the sweet of secondary concentration liquid
Oil is concentrated to 80%~85% concentration, flows into the stirred tank with insulation certainly（9）, by stirred tank（9）Jacket steam insulation, pass through
Two level discharging pump（10）It is delivered to standing groove（11）, stand groove（11）Lower floor's liquid enter the second centrifuge（12）, centrifugation mother
Liquid and standing groove（11）Supernatant liquid overflow to second stirring receiving slit（13）Concentrate three times is obtained, is added with steam or hot water
Heat；
（4）Thin film evaporation three times：By step（3）Concentrate passes through three-level feed pump to gained three times（14）It is delivered to the steaming of three-level film
Send out device（15）Further refine, with steam or heat-conducting oil heating, three-level thin film evaporator（15）The Stress control of system-
0.07~-0.095MPa, temperature control is at 160 DEG C~200 DEG C, three-level thin film evaporator（15）The condensed device of top gas
（192）It is cooled to glycerine receiving slit（16）, three-level thin film evaporator（15）Bottom obtain waste residue.
5. the technique of glycerine is extracted from Epoxy Resin Unit high-salt wastewater concentrate as claimed in claim 4, it is characterized in that：Most
The glycerol concentration obtained eventually be 95% and more than.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710561343.9A CN107337308B (en) | 2017-09-12 | 2017-09-12 | Device and process for extracting glycerin from epoxy resin device high-salinity wastewater concentrated solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710561343.9A CN107337308B (en) | 2017-09-12 | 2017-09-12 | Device and process for extracting glycerin from epoxy resin device high-salinity wastewater concentrated solution |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107337308A true CN107337308A (en) | 2017-11-10 |
| CN107337308B CN107337308B (en) | 2020-09-25 |
Family
ID=60218654
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710561343.9A Active CN107337308B (en) | 2017-09-12 | 2017-09-12 | Device and process for extracting glycerin from epoxy resin device high-salinity wastewater concentrated solution |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107337308B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110228828A (en) * | 2018-03-05 | 2019-09-13 | 南通星辰合成材料有限公司 | A kind of epoxy resin high-salt wastewater concentration purification system and its method of purification |
| CN110540332A (en) * | 2019-09-24 | 2019-12-06 | 东海岸环境科技无锡有限公司 | fluorine-containing and chlorine-containing sewage treatment process |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106517626A (en) * | 2016-11-30 | 2017-03-22 | 江苏迈安德节能蒸发设备有限公司 | Sodium sulfate wastewater treatment process |
| CN106809999A (en) * | 2017-03-17 | 2017-06-09 | 黄山清源环境工程技术服务有限公司 | Epoxy resin high-concentration waste water processing system |
| CN206395987U (en) * | 2016-08-26 | 2017-08-11 | 陕西海山能源发展有限公司 | A kind of device for handling high-salt wastewater |
| CN107032429A (en) * | 2017-04-13 | 2017-08-11 | 江苏瑞升华能源科技有限公司 | A kind of reverse osmosis thick water treatment system and handling process |
-
2017
- 2017-09-12 CN CN201710561343.9A patent/CN107337308B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN206395987U (en) * | 2016-08-26 | 2017-08-11 | 陕西海山能源发展有限公司 | A kind of device for handling high-salt wastewater |
| CN106517626A (en) * | 2016-11-30 | 2017-03-22 | 江苏迈安德节能蒸发设备有限公司 | Sodium sulfate wastewater treatment process |
| CN106809999A (en) * | 2017-03-17 | 2017-06-09 | 黄山清源环境工程技术服务有限公司 | Epoxy resin high-concentration waste water processing system |
| CN107032429A (en) * | 2017-04-13 | 2017-08-11 | 江苏瑞升华能源科技有限公司 | A kind of reverse osmosis thick water treatment system and handling process |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110228828A (en) * | 2018-03-05 | 2019-09-13 | 南通星辰合成材料有限公司 | A kind of epoxy resin high-salt wastewater concentration purification system and its method of purification |
| CN110540332A (en) * | 2019-09-24 | 2019-12-06 | 东海岸环境科技无锡有限公司 | fluorine-containing and chlorine-containing sewage treatment process |
| CN110540332B (en) * | 2019-09-24 | 2021-09-07 | 东海岸环境科技无锡有限公司 | Fluorine-containing and chlorine-containing sewage treatment process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107337308B (en) | 2020-09-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104817481B (en) | Technological method for recovering DMSO from DMSO aqueous solution | |
| CN105906122A (en) | Treatment technology of high-organic matter high-salt wastewater and treatment device thereof | |
| CN107619078B (en) | Device for treating acidic wastewater by adopting concentration stripping method | |
| CN103012321A (en) | Method and system thereof for synthesizing epoxy chloropropane by dichloropropanol | |
| CN104628664A (en) | Method for continuously producing benzotriazole | |
| CN107337308A (en) | The device and its technique of glycerine are extracted in a kind of high-salt wastewater concentrate from Epoxy Resin Unit | |
| CN101955546B (en) | Process for producing cellulose ether by directly separating and recovering diluent | |
| CN204400884U (en) | 1,5-pentamethylene diamine continuously purification device | |
| CN103012332B (en) | Use the method for packing tower distillation separation of tetrahydrofuran-methanol-water solvent slop | |
| CN104109078A (en) | Method for recovering ethanol in analginum production | |
| CN104130105B (en) | The method that in D-4-methylsulfonylphserine serine ethyl ester production, ethanol is recycled | |
| CN101333200A (en) | Method for synthesizing 5-hydroxymethyl-furfural | |
| CN105777555A (en) | Continuous purifying device of 1,5-pentanediamine, and method thereof | |
| CN107311878A (en) | A kind of device for reclaiming glycine waste liquid and the method for reclaiming glycine waste liquid | |
| CN104926690A (en) | Method and device for recycling and refining acetonitrile in ceftriaxone sodium synthesis | |
| CN106831472A (en) | A kind of DMF salt bearing liquid wastes recovery process and system | |
| CN108314637B (en) | Preparation method and production device of thioacetic acid | |
| CN106830143A (en) | A kind of lithium battery presoma prepares the high salt method of wastewater treatment containing lithium for producing | |
| CN107673979A (en) | The recoverying and utilizing method of halogenation short chain quaternary ammonium waste salt | |
| CN104478734B (en) | The method that in AKD production, crude product triethylamine recycles | |
| CN104876817B (en) | A kind of method that use succinic acid fermentation liquor extracts succinic acid | |
| CN104726122B (en) | Technology for producing modified pitch by one-step heating | |
| CN204151176U (en) | The multi-effect evaporation system of coal chemical engineering equipment strong brine | |
| CN107473927B (en) | Preparation process of biphenyl dichlorobenzyl | |
| CN206143108U (en) | Retrieve polyether glycol and potassium dihydrogen phosphate's device in follow polyether glycol filter residue |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20230420 Address after: 5 / F, 277 Huqingping Road, Minhang District, Shanghai, 201105 Patentee after: Wuxi Blue Ocean Engineering Design Co.,Ltd. Shanghai Branch Address before: No. 59 Xiuxi Road, Binhu District, Wuxi City, Jiangsu Province, 214125 Patentee before: WUXI LAHIGH ENGINEERING DESIGN CO.,LTD. |
|
| TR01 | Transfer of patent right |