CN109096066B - Method and device for removing and recycling ethylene glycol butyl ether in coating wastewater - Google Patents
Method and device for removing and recycling ethylene glycol butyl ether in coating wastewater Download PDFInfo
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Abstract
The invention provides a method and a device for removing and recovering ethylene glycol monobutyl ether in coating wastewater, which comprises the following steps: the method comprises the following steps: preheating a waste water raw material, rectifying, cooling the tower top fraction obtained by rectification to 60-90 ℃ to obtain condensate, standing and phase splitting the obtained condensate, wherein the temperature in a phase splitting tank is always kept above 60 ℃ in the phase splitting process, and the rectified heavy component is waste water without ethylene glycol butyl ether; step two: the light phase component is high-concentration ethylene glycol monobutyl ether, and the heavy phase component returns to the rectifying tower for rectification. The invention overcomes the problems of high treatment difficulty and poor economical efficiency of coating wastewater, damage to the structure of butyl cellosolve during treatment, low solvent recovery purity and recovery rate and the like in the prior art, and removes and recovers the butyl cellosolve in the wastewater under the conditions of wide looseness, simplicity and low energy consumption.
Description
Technical Field
The invention belongs to the field of wastewater treatment in the coating industry, and particularly relates to a method and a device for removing and recovering ethylene glycol monobutyl ether in coating wastewater.
Background
Ethylene glycol butyl ether, boiling point 171.1 deg.C, colorless flammable liquid, can be mixed and dissolved with water, acetone, benzene, carbon tetrachloride, ethanol and n-heptane in any proportion. Because of its excellent solubility, it is widely used in the fields of paints, inks, metal cleaners and dye dispersants, mainly as solvents for cellulose nitrate, lacquers, quick-drying paints, varnishes, enamels and paint removers and auxiliary solvents for improving emulsification properties.
The waste water produced in the industry contains low-concentration ethylene glycol monobutyl ether inevitably, and the direct discharge of the waste water causes great pollution to the environment and loss of ethylene glycol monobutyl ether materials. The prior treatment method is to add selective solvent into the mixture for azeotropic distillation, obtain azeotrope of the selective solvent and water at the tower top and obtain high-purity ethylene glycol monobutyl ether at the tower bottom. However, the method has high energy consumption, less recovered butyl cellosolve and no economy. Chinese patent 201510427215.6 mentions that the low energy consumption degradation is realized by oxidizing ethylene glycol butyl ether waste water with nitric acid waste water, but the method can damage the structure of ethylene glycol butyl ether, which causes material loss, and the method has great limitation, and the treated waste water can be acidic, which causes new pollution.
Disclosure of Invention
In view of the above, the present invention aims to provide a method and an apparatus for removing and recovering butyl glycol ether from coating wastewater, so as to overcome the problems of high coating wastewater treatment difficulty, poor economy, damage to butyl glycol ether structure during treatment, low solvent recovery purity and recovery rate, and the like in the prior art, and remove and recover butyl glycol ether from wastewater under the conditions of looser width, simplicity and low energy consumption.
In order to achieve the purpose, the technical scheme of the invention is realized as follows:
a method for removing and recovering ethylene glycol monobutyl ether in coating wastewater comprises the following steps:
the method comprises the following steps: preheating a waste water raw material, rectifying, cooling the tower top fraction obtained by rectification to 60-90 ℃ to obtain condensate, standing and phase splitting the obtained condensate, wherein the temperature in a phase splitting tank is always kept above 60 ℃ in the phase splitting process, and the rectified heavy component is waste water without ethylene glycol butyl ether;
step two: the light phase component is high-concentration ethylene glycol monobutyl ether, and the heavy phase component returns to the rectifying tower for rectification.
Further, the rectification process is operated at atmospheric or slightly positive pressure.
Furthermore, the concentration of the ethylene glycol butyl ether in the wastewater raw material is less than or equal to 10%.
The invention also provides a device for removing and recovering ethylene glycol monobutyl ether in coating wastewater, which comprises a rectifying tower, a condenser and a split-phase reflux tank, wherein the top of the rectifying tower is a tower discharge hole, a tower body is provided with a tower feed inlet and a tower reflux hole, the condenser comprises two pipelines, materials pass through a first pipeline of the condenser and then enter the rectifying tower through the tower feed inlet, the tower discharge hole is connected with a second pipeline of the condenser and then is connected with a tank inlet of the split-phase reflux tank, the split-phase reflux tank comprises a tank inlet, a heavy component tank outlet and a light component tank outlet, and the heavy component tank outlet is connected with the tower reflux hole. The rectifying tower can adopt a plate tower or a packed tower.
Furthermore, two ends of a first pipeline of the condenser are respectively provided with a first condenser inlet and a first condenser outlet, two ends of a second pipeline of the condenser are respectively provided with a second condenser inlet and a second condenser outlet, and the raw material enters the condenser through the first condenser inlet and then enters the rectifying tower after reaching the feeding hole of the tower from the first condenser outlet; the tower discharge port is connected with the inlet of a second condenser, and the outlet of the second condenser is connected with the tank inlet of the split-phase reflux tank.
Further, the tank inlet is located at the top of the split-phase reflux tank, the heavy component tank outlet and the light component tank outlet are located at the bottom of the split-phase reflux tank, a separation plate is arranged between the heavy component tank outlet and the light component tank outlet, the height of the separation plate is lower than that of the split-phase reflux tank in the vertical direction, and the tank inlet is located on one side, in the vertical direction, of the separation plate, where the heavy component tank outlet is arranged.
Further, the tower bottom of the rectifying tower is provided with a tower bottom outlet and a tower bottom reboiler. The bottoms reboiler may be a forced circulation reboiler or a thermosiphon reboiler.
Furthermore, a reflux pump is arranged between the outlet of the heavy component tank and the reflux port of the tower. The feed was delivered to the condenser by a feed pump. The feed pump and the reflux pump adopt peristaltic pumps, the peristaltic pumps can provide feed with stable flow, and the phenomenon that the gas-liquid balance in the rectifying tower is damaged due to flow fluctuation is avoided. The tower body, the pipeline and the split-phase reflux tank of the rectifying tower are insulated by adopting polyurethane insulation pipes.
Further, a tail condenser is arranged between the condenser and the split-phase reflux tank.
The content of ethylene glycol monobutyl ether in the wastewater raw material is less than or equal to 10 percent, the wastewater raw material is preheated by a condensing medium channel of a condenser and then pumped into a rectifying tower from a tower feed inlet in the tower for rectification, mixed fraction extracted from the tower top enters the condenser through a second condenser inlet and is condensed to 60-90 ℃, condensate obtained from the second condenser inlet is extracted into a phase-splitting reflux tank and is kept still for phase splitting in the phase-splitting reflux tank, the temperature in the phase-splitting reflux tank is kept above 60 ℃ all the time in the phase-splitting process, heavy-phase component leaves the phase-splitting reflux tank through a heavy-component tank outlet and then is pumped back to the rectifying tower through a reflux pump for reflux, light-phase component containing high-concentration ethylene glycol monobutyl ether is extracted from a light-component tank outlet, and wastewater containing no ethylene glycol monobutyl ether. The rectifying tower carries out azeotropic distillation operation under normal pressure or slight positive pressure.
The heavy phase components obtained from the phase-splitting reflux tank are all pumped into a tower feed inlet of the rectifying tower as reflux liquid. The content of butyl cellosolve in the waste water at the bottom outlet of the rectifying tower is below 100 ppm. The content of ethylene glycol monobutyl ether in the light phase component extracted from the light component tank outlet of the phase separation reflux tank is 50-80%.
Compared with the prior art, the method and the device for removing and recovering the ethylene glycol monobutyl ether in the coating wastewater have the following advantages:
(1) the invention provides a brand-new device for removing and recycling the ethylene glycol butyl ether in the coating wastewater, which ensures that the process of removing the ethylene glycol butyl ether from the low-concentration ethylene glycol butyl ether wastewater is simple and loose, is easy to operate, has low energy consumption, high solvent removal rate and small zero-emission wastewater evaporation capacity, and can continuously and stably produce for a long period;
(2) according to the invention, by utilizing the special property that the ethylene glycol monobutyl ether aqueous solution in azeotropic composition has phase splitting at the temperature of more than 60 ℃, the phase splitting reflux tank is skillfully designed, so that the fraction at the top of the tower is subjected to phase splitting in the phase splitting reflux tank, and the high-concentration ethylene glycol monobutyl ether is recovered while the low-concentration ethylene glycol monobutyl ether in the wastewater is efficiently removed;
(3) the invention adopts the condenser preheating technology to preheat the raw material of the wastewater, thereby avoiding the heat consumption caused by preheating the raw material, in addition, the invention has small evaporated wastewater amount, and the operation mode of heavy phase reflux avoids the condition that the energy consumption is increased because high-concentration ethylene glycol monomethyl ether participates in the reflux.
Drawings
FIG. 1 is a schematic structural diagram of a device for removing and recovering butyl glycol ether in coating wastewater.
1-a rectifying tower; 101-tower discharge port; 102-column feed inlet; 103-column reflux inlet; 104-a bottom outlet; 105-a bottoms reboiler; 2-a condenser; 201-first condenser inlet; 202-first condenser outlet; 203-a second condenser inlet; 204-a second condenser outlet; 3-split-phase reflux tank; 301-tank inlet; 302-heavy ends tank outlet; 303-outlet of light component tank; 304-a divider plate; 4-tail condenser.
Detailed Description
Unless defined otherwise, technical terms used in the following examples have the same meanings as commonly understood by one of ordinary skill in the art to which the present invention belongs. The test reagents used in the following examples, unless otherwise specified, are all conventional biochemical reagents; the experimental methods are conventional methods unless otherwise specified.
The present invention will be described in detail with reference to the following examples and FIG. 1.
The utility model provides a device of ethylene glycol butyl ether in desorption and recovery coating waste water, including rectifying column 1, condenser 2 and split phase reflux jar 3, the top of the tower of rectifying column 1 is tower discharge gate 101, the body of the tower is provided with tower feed inlet 102 and tower backward flow mouth 103, include two pipelines in the condenser 2, the material enters into rectifying column 1 through tower feed inlet 102 behind the first pipeline of condenser 2, the second pipeline of condenser 2 is connected to tower discharge gate 101, then connect the jar import 301 of split phase reflux jar 3, split phase reflux jar 3 includes jar import 301, heavy component jar export 302 and light component jar export 303, heavy component jar export 302 is connected with tower backward flow mouth 103. The two ends of a first pipeline of the condenser 2 are respectively provided with a first condenser inlet 201 and a first condenser outlet 202, the two ends of a second pipeline of the condenser 2 are respectively provided with a second condenser inlet 203 and a second condenser outlet 204, raw materials enter the condenser 2 through the first condenser inlet 201, then enter the rectifying tower 1 after reaching the tower feed inlet 102 from the first condenser outlet 202; the column outlet 101 is connected to a second condenser inlet 203 and a second condenser outlet 204 is connected to a tank inlet 301 of the isolated phase reflux tank 3. The jar import 301 is located the top of split phase backward flow jar 3, and heavy ends jar export 302 and light ends jar export 303 are located the bottom of split phase backward flow jar 3, and is provided with division board 304 between heavy ends jar export 302 and the light ends jar export 303, and division board 304 highly is less than the height of split phase backward flow jar 3 in vertical direction, and jar import 301 lies in one side that division board 304 has set up heavy ends jar export 302 in vertical direction.
A wastewater raw material enters through a first condenser inlet 201 of a condenser 3 and then flows out of the condenser 3 through a first condenser outlet 202, then enters into a rectifying tower 1 through a tower feed inlet 102 until the liquid level is 2/3 of the total liquid level of a tower kettle of the rectifying tower 1, feeding is stopped, heating medium is introduced into a reboiler 105, normal-pressure azeotropic rectification is carried out, after the material in the rectifying tower 1 is rectified, mixed fraction extracted from the tower top is condensed to 60-90 ℃ through a condenser 2 and a tail condenser 4, condensate is extracted into a phase separation reflux tank 3, the temperature in the phase separation reflux tank 3 is always kept above 60 ℃, the mixed fraction is subjected to phase separation in the phase separation reflux tank 3, heavy phase fraction returns to the rectifying tower 1 through a reflux pump, light phase fraction is extracted from a light phase tank outlet 303, and wastewater after desolventization is extracted from a tower bottom outlet 104.
And a tail condenser 4 is arranged between the condenser 2 and the split-phase reflux tank 3. Since the temperature of the mixed fraction taken out from the top of the column is not sufficiently lowered to a predetermined value during the heat exchange in the condenser 2, the temperature needs to be lowered again before entering the phase separation reflux drum 3.
The wastewater raw materials adopted in the following examples and comparative examples are all from a certain paint company in Sichuan, and the content (mass fraction) of each component in the wastewater raw materials is respectively as follows: 89.82% of water, 10.08% of butyl cellosolve and 0.1% of other impurities. The following examples all adopt the apparatus for removing and recovering butyl cellosolve from coating waste water according to the present invention. The detection devices adopted by the raw materials, the fractions and the kettle liquid are respectively an FL9790II type gas chromatograph and a nonpolar 60m capillary column, and the detection method adopts an internal standard method.
Comparative example 1
A glass rectifying tower 1 with the diameter of 30mm and the height of 1.5m is selected for an experiment, 1500ml of raw materials are pumped into a 2L tower kettle, room-temperature circulating water is introduced into a condensing medium channel of a tail condenser 4, a heating medium is introduced into a reboiler 105, normal-pressure rectification is carried out, the temperature of the rectifying tower 1 is 100.1 ℃, the temperature of the tower top is 96.2 ℃, the reflux ratio is 50, 48ml of fraction is extracted from a phase-splitting reflux tank 3, the fraction is not layered, the content of ethylene glycol butyl ether in a light phase is detected to be 15.11%, and after 40% of the fraction is extracted, the ethylene glycol butyl ether residue in the kettle liquid of the rectifying tower is detected to be 6.56%.
Example 1
A glass rectifying tower with the diameter of 30mm and the height of 1.5m is selected for an experiment, 1500ml of raw materials are pumped into a 2L tower kettle, 60 ℃ hot water is introduced into a condensing medium channel of a tail condenser 4, a heating medium is introduced into a reboiler 105, the normal pressure rectification is carried out, the temperature of the tower kettle of the rectifying tower 1 is 100.1 ℃, the temperature of the tower top is 96.2 ℃, fractions are subjected to phase splitting in a phase splitting reflux tank 3, heavy phases are returned to the tower kettle of the rectifying tower 1, and the volume of the phase splitting is larger than that of the light phases: and (3) detecting that the content of ethylene glycol butyl ether in the light phase is 58.6 percent and detecting that the residual quantity of the ethylene glycol butyl ether in the kettle liquid is 32ppm when about 20 percent of the light phase fraction is extracted.
Example 2
A glass rectifying tower with the diameter of 30mm and the height of 1.5m is selected for an experiment, 1500ml of raw materials are pumped into a 2L tower kettle, 80 ℃ hot water is introduced into a condensing medium channel of a tail condenser 4, a heating medium is introduced into a reboiler 105, the normal pressure rectification is carried out, the temperature of the tower kettle of the rectifying tower 1 is 100.0 ℃, the temperature of the tower top is 96.1 ℃, fractions are subjected to phase splitting in a phase splitting reflux tank 3, heavy phases are returned to the tower kettle of the rectifying tower 1, and the volume of the phase splitting is larger than that of the light phases: and (3.5) detecting that the content of ethylene glycol butyl ether in the light phase is 66.8 percent and detecting that the residual quantity of the ethylene glycol butyl ether in the kettle liquid is 47ppm when about 15 percent of the fraction of the light phase is extracted.
Example 3
A glass rectifying tower with the diameter of 30mm and the height of 1.5m is selected for an experiment, 1500ml of raw materials are pumped into a 2L tower kettle, 90 ℃ hot water is introduced into a condensing medium channel of a tail condenser 4, a heating medium is introduced into a reboiler 105, the normal pressure rectification is carried out, the temperature of the tower kettle of the rectifying tower 1 is 100.0 ℃, the temperature of the tower top is 96.1 ℃, fractions are subjected to phase splitting in a phase splitting reflux tank 3, heavy phases are returned to the tower kettle of the rectifying tower 1, and the volume of the phase splitting is larger than that of the light phases: and (3) detecting that the content of ethylene glycol butyl ether in the light phase is 74.3% when the heavy phase is 1:4 and the content of the extracted light phase fraction is about 15%, and detecting the residual quantity of the ethylene glycol butyl ether in the kettle liquid to be 13 ppm.
Example 4
A glass rectifying tower with the diameter of 80mm and the height of 1.5m is selected for an experiment, 1500ml of raw materials are pumped into a 2L tower kettle, 90 ℃ hot water is introduced into a condensing medium channel of a tail condenser 4, a heating medium is introduced into a reboiler 105, the normal pressure rectification is carried out, the temperature of the tower kettle of the rectifying tower 1 is 100.0 ℃, the temperature of the tower top is 96.1 ℃, fractions are subjected to phase splitting in a phase splitting reflux tank 3, heavy phases are returned to the tower kettle of the rectifying tower 1, and the volume of the phase splitting is larger than that of the light phases: and (3) detecting that the content of ethylene glycol butyl ether in the light phase is 76.6% when the heavy phase is 1:4, and detecting that the residual quantity of the ethylene glycol butyl ether in the kettle liquid is 11ppm when about 15% of the light phase fraction is extracted.
The embodiment shows that the content of the butyl cellosolve in the waste water raw material can be reduced to a level below 100ppm by adopting the method of normal pressure rectification and split-phase extraction, and simultaneously, 50-80% of high-concentration butyl cellosolve fraction is obtained at the tower top, so that the problem of environmental pollution caused by the butyl cellosolve contained in the waste water is solved, and the butyl cellosolve can be efficiently recovered.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (8)
1. A method for removing and recovering ethylene glycol monobutyl ether in coating wastewater is characterized in that: the method comprises the following steps:
the method comprises the following steps: preheating a waste water raw material, rectifying, cooling the tower top fraction obtained by rectification to 60-90 ℃ to obtain condensate, standing and phase splitting the obtained condensate, wherein the temperature in a phase splitting tank is always kept above 60 ℃ in the phase splitting process, and the rectified heavy component is waste water without ethylene glycol butyl ether;
step two: the light phase component is high-concentration ethylene glycol monobutyl ether, and the heavy phase component returns to the rectifying tower for rectification;
device of ethylene glycol butyl ether in desorption and recovery coating waste water, including rectifying column (1), condenser (2) and split phase reflux jar (3), the top of the tower of rectifying column (1) is tower discharge gate (101), the body of the tower is provided with tower feed inlet (102) and tower backward flow mouth (103), include two pipelines in condenser (2), the material enters into rectifying column (1) through tower feed inlet (102) behind the first pipeline of condenser (2), the second pipeline of condenser (2) is connected in tower discharge gate (101), then jar import (301) of connecting split phase reflux jar (3), split phase reflux jar (3) are including jar import (301), heavy component jar export (302) and light component jar export (303), heavy component jar export (302) are connected with tower backward flow mouth (103).
2. The method for removing and recovering butyl cellosolve from coating wastewater according to claim 1, wherein the method comprises the following steps: the rectification process is operated at atmospheric or slightly positive pressure.
3. The method for removing and recovering butyl cellosolve from coating wastewater according to claim 1, wherein the method comprises the following steps: the concentration of the ethylene glycol monobutyl ether in the wastewater raw material is less than or equal to 10 percent.
4. The method for removing and recovering butyl cellosolve from coating wastewater according to claim 1, wherein the method comprises the following steps: the two ends of a first pipeline of the condenser (2) are respectively provided with a first condenser inlet (201) and a first condenser outlet (202), the two ends of a second pipeline of the condenser (2) are respectively provided with a second condenser inlet (203) and a second condenser outlet (204), raw materials enter the condenser (2) through the first condenser inlet (201), and then enter the rectifying tower (1) after reaching the tower feeding port (102) from the first condenser outlet (202); the tower discharge port (101) is connected with a second condenser inlet (203), and a second condenser outlet (204) is connected with a tank inlet (301) of the split-phase reflux tank (3).
5. The method for removing and recovering butyl cellosolve from coating wastewater according to claim 1, wherein the method comprises the following steps: the tank inlet (301) is located at the top of the split-phase backflow tank (3), the heavy component tank outlet (302) and the light component tank outlet (303) are located at the bottom of the split-phase backflow tank (3), a separation plate (304) is arranged between the heavy component tank outlet (302) and the light component tank outlet (303), the height of the separation plate (304) is lower than that of the split-phase backflow tank (3) in the vertical direction, and the tank inlet (301) is located on one side of the separation plate (304) in the vertical direction, wherein the heavy component tank outlet (302) is arranged.
6. The method for removing and recovering butyl cellosolve from coating wastewater according to claim 1, wherein the method comprises the following steps: the tower bottom of the rectifying tower (1) is provided with a tower bottom outlet (104) and a tower bottom reboiler (105).
7. The method for removing and recovering butyl cellosolve from coating wastewater according to claim 1, wherein the method comprises the following steps: a reflux pump is arranged between the heavy component tank outlet (302) and the tower reflux inlet (103).
8. The method for removing and recovering butyl cellosolve from coating wastewater according to claim 1, wherein the method comprises the following steps: a tail condenser (4) is arranged between the condenser (2) and the split-phase reflux tank (3).
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Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1803757A (en) * | 2006-01-18 | 2006-07-19 | 华南理工大学 | Ethyl acetate dehydrating extraction method |
| CN101254444A (en) * | 2007-12-05 | 2008-09-03 | 南京大学 | Catalytic reaction, rectification integrated technique and special-purpose equipment |
| CN101337884A (en) * | 2008-08-08 | 2009-01-07 | 德纳（南京）化工有限公司 | Method for preparing 2-Butoxyethyl acetate by continuous esterification reaction |
| CN101475478A (en) * | 2009-01-20 | 2009-07-08 | 江苏怡达化工有限公司 | Method for synthesizing ethylene glycol monobutyl ether acetate |
| CN101684064A (en) * | 2009-07-21 | 2010-03-31 | 厦门中坤化学有限公司 | Environment-friendly process for producing dihydromyrcenol by using dihydromyrcene hydration reaction |
| CN102584751A (en) * | 2012-01-09 | 2012-07-18 | 天津凯赛特科技有限公司 | Process and reaction system for preparing furfuraldehyde by reaction rectification method |
| CN102863316A (en) * | 2012-09-27 | 2013-01-09 | 安徽淮化股份有限公司 | Ethylene glycol production device |
| CN106431812A (en) * | 2016-09-21 | 2017-02-22 | 青岛科技大学 | Method and device for separating methylbenzene-methanol-water azeotrope using extractive distillation |
| CN107739300A (en) * | 2017-10-23 | 2018-02-27 | 黄河三角洲京博化工研究院有限公司 | A kind of process for producing high-purity isobutene and ethylene glycol mono-tert-butyl ether |
| CN207552209U (en) * | 2017-10-23 | 2018-06-29 | 黄河三角洲京博化工研究院有限公司 | A kind of process unit for producing ethylene glycol mono-tert-butyl ether |
-
2018
- 2018-09-29 CN CN201811152263.9A patent/CN109096066B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1803757A (en) * | 2006-01-18 | 2006-07-19 | 华南理工大学 | Ethyl acetate dehydrating extraction method |
| CN101254444A (en) * | 2007-12-05 | 2008-09-03 | 南京大学 | Catalytic reaction, rectification integrated technique and special-purpose equipment |
| CN101337884A (en) * | 2008-08-08 | 2009-01-07 | 德纳（南京）化工有限公司 | Method for preparing 2-Butoxyethyl acetate by continuous esterification reaction |
| CN101475478A (en) * | 2009-01-20 | 2009-07-08 | 江苏怡达化工有限公司 | Method for synthesizing ethylene glycol monobutyl ether acetate |
| CN101684064A (en) * | 2009-07-21 | 2010-03-31 | 厦门中坤化学有限公司 | Environment-friendly process for producing dihydromyrcenol by using dihydromyrcene hydration reaction |
| CN102584751A (en) * | 2012-01-09 | 2012-07-18 | 天津凯赛特科技有限公司 | Process and reaction system for preparing furfuraldehyde by reaction rectification method |
| CN102863316A (en) * | 2012-09-27 | 2013-01-09 | 安徽淮化股份有限公司 | Ethylene glycol production device |
| CN106431812A (en) * | 2016-09-21 | 2017-02-22 | 青岛科技大学 | Method and device for separating methylbenzene-methanol-water azeotrope using extractive distillation |
| CN107739300A (en) * | 2017-10-23 | 2018-02-27 | 黄河三角洲京博化工研究院有限公司 | A kind of process for producing high-purity isobutene and ethylene glycol mono-tert-butyl ether |
| CN207552209U (en) * | 2017-10-23 | 2018-06-29 | 黄河三角洲京博化工研究院有限公司 | A kind of process unit for producing ethylene glycol mono-tert-butyl ether |
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