CN107118181B - Device and method for producing refined ethylene oxide - Google Patents
Device and method for producing refined ethylene oxide Download PDFInfo
- Publication number
- CN107118181B CN107118181B CN201610104471.6A CN201610104471A CN107118181B CN 107118181 B CN107118181 B CN 107118181B CN 201610104471 A CN201610104471 A CN 201610104471A CN 107118181 B CN107118181 B CN 107118181B
- Authority
- CN
- China
- Prior art keywords
- tower
- absorption water
- product
- section
- aldehyde
- 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.)
- Active
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/32—Separation; Purification
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D303/00—Compounds containing three-membered rings having one oxygen atom as the only ring hetero atom
- C07D303/02—Compounds containing oxirane rings
- C07D303/04—Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Epoxy Compounds (AREA)
Abstract
The invention provides a device and a method for producing refined ethylene oxide, wherein the device comprises: an EO product tower, an EO aldehyde discharging tower, a condenser, a reflux tank and an EO reflux pump; the top of the EO product tower is sequentially connected with a condenser, a reflux tank and an EO reflux pump, and an outlet pipeline of the EO reflux pump is connected with the top of the EO product tower; an EO aldehyde discharging line is arranged on the side line of the EO product tower and connected with the EO aldehyde discharging tower, and an EO aldehyde discharging tower top gas phase line is connected with the EO product tower; wherein, an EO-rich absorption water refining cavity is arranged in the EO product tower body; the EO-rich absorption water refining cavity sequentially comprises an EO refining section, an EO concentration section and an EO stripping section from top to bottom, wherein the EO refining section, the EO concentration section and the EO stripping section are communicated with each other through a vapor phase and a liquid phase. By adopting the device and the method, the operation safety of the device is improved, and meanwhile, the occupied area and the investment are saved; and the comprehensive utilization of energy is more reasonable, and the operation cost is reduced.
Description
Technical Field
The invention relates to the field of ethylene oxide production, and in particular relates to a device and a method for producing refined ethylene oxide.
Background
In recent years, the domestic ethylene oxide market is in full demand and the price is always high, and the ethylene glycol is totally low due to the impact of the ethylene glycol imported from the middle east and the ethylene glycol prepared from coal. Therefore, an ethylene oxide device which mainly produces refined ethylene oxide and produces a small amount of ethylene glycol as a byproduct is built, the investment is lower than that of a conventional ethylene oxide/ethylene glycol (EO/EG) device, and the product benefit is better.
Therefore, the development of a process flow mainly for producing refined EO with high safety and low energy consumption becomes a key direction for research of various technical providers.
The prior device for producing and refining ethylene oxide has complex flow and more devicesAnd the energy consumption is large. FIG. 1 is a process for producing purified ethylene oxide, which is provided in patent publication CN201410131283.3, the apparatus comprising: EO stripping/rectifying tower, EO refining tower and CO2A stripping column; the top of the EO stripping/rectifying tower is connected with a feed inlet in the middle of the EO refining tower, the top of the EO refining tower is sequentially connected with a condenser, a reflux tank and an EO reflux pump, the outlet of the EO reflux pump is divided into a pipeline a and a pipeline b, the pipeline a is connected with the top of the EO refining tower, and the pipeline b and the outlet pipeline of the EO refining tower kettle pump are merged and then sent to an ethylene glycol production working section; the side of the EO refining tower is provided with an ethylene oxide extraction line connected with CO2A stripping column. The method comprises the following steps:
1) the EO-rich absorption water from the EO absorption tower enters an EO stripping/rectifying tower for rectification, and the EO with high concentration is stripped at the top of the EO stripping/rectifying tower and sent to an EO refining tower;
2) after the EO refining tower top material flow is condensed and refluxed, one part of the EO refining tower top material flow returns to the EO refining tower top, and the other part of the EO refining tower top material flow is combined with the EO refining tower kettle material flow and then sent to a rear ethylene glycol working section;
3) feeding ethylene oxide extracted from the side of the EO refining tower into CO2A stripping tower for removing light components contained therein; CO 22EO gas containing light components at the top of the stripping tower and EO refining tower top gas are sent into an EO refining tower condenser together for condensation and recycling, and CO2And extracting a refined EO product from the kettle of the stripping tower.
Wherein, a stream of material is led out from the middle part of the EO refining tower and is used as the reflux of the EO stripping/rectifying tower after being pumped and boosted; in addition, CO2The refined EO product extracted from the stripper tower is pumped to a finished product tank area after being pressurized.
Compared with other existing processes, the process is improved, but the process is still relatively complex, especially the number of rotating devices is large, four pumps for delivering the EO-containing medium are easy to cause EO leakage when the operation is improper, and the EO belongs to a highly toxic and explosive medium, so the use of the rotating devices is reduced as much as possible from the safety point of view. In the process, the lean EO absorption water in the kettle of the stripping/rectifying tower is used as an EO refining tower reboiler and CO after being boosted by a pump2After the heat source of the reboiler of the stripping tower is used, the heat source is combined and returned to the EO absorption tower, and although the energy-saving design is considered, the energy of the lean EO absorption water is utilizedIs not optimal. In addition, the process requires the setting of CO2The purpose of the stripper is to further remove light components, such as CO, contained therein2。
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a device and a method for producing refined ethylene oxide. Compared with the existing process, the device and the process of the invention are simpler, especially the rotating equipment is less, the device safety is improved, and the energy utilization is more optimized.
In order to achieve the above object, the present invention provides an apparatus for producing purified ethylene oxide, comprising: an EO product tower, an EO aldehyde discharging tower, a condenser, a reflux tank and an EO reflux pump; the EO product tower is provided with an EO product tower reboiler, and the EO aldehyde-discharging tower is provided with an EO aldehyde-discharging tower reboiler; the top of the EO product tower is sequentially connected with a condenser, a reflux tank and an EO reflux pump, and an outlet pipeline of the EO reflux pump is connected with the top of the EO product tower; an EO aldehyde discharging line is arranged on the side line of the EO product tower and connected with the EO aldehyde discharging tower, and an EO aldehyde discharging tower top gas phase line is connected with the EO product tower;
wherein, an EO-rich absorption water refining cavity is arranged in the EO product tower body; the EO-rich absorption water refining cavity sequentially comprises an EO refining section, an EO concentration section and an EO stripping section from top to bottom, wherein the EO refining section, the EO concentration section and the EO stripping section are communicated with each other through a vapor phase and a liquid phase; a refined EO product extraction line is arranged on the side line of the EO product tower, and an EO-poor absorption water discharge line is arranged at the bottom of the EO-rich absorption water refining cavity.
In the present invention, the term EO stands for ethylene oxide, and refined EO stands for refined ethylene oxide.
In accordance with the present invention, the refined EO product is withdrawn from the side line of the EO product column and can be gravity fed to the finishing tank field, thereby reducing rotating equipment.
In accordance with the present invention, an EO-lean absorption water discharge line is used to discharge EO-lean absorption water, which may be treated by various methods in the art. To recover heat, the apparatus preferably further comprises an EO-lean absorption water flash tank disposed within the EO product column body in an EO-lean absorption water flash chamber located below the EO-rich absorption water polishing chamber, or the EO-lean absorption water flash tank is disposed separately from the EO product column; the lean EO absorption water discharge line is connected to the bottom of the lean EO absorption water flash tank. Wherein, the lean EO absorption water flash tank is arranged in a lean EO absorption water flash chamber, which is a more preferable embodiment, and can further save the occupied area of the device.
Various means and means of effecting flashing may be employed in accordance with the present invention, preferably a steam ejector is provided, the inlet line of which is connected to the top of the EO-depleted absorption water flash drum and the outlet line of which is connected to the lower part of the EO-enriched absorption water refining chamber. The process steam is flashed by depressurizing the steam ejector, which is used as stripping steam for the EO stripping section in the EO product column, along with motive steam from the ejector.
According to the invention, the process side of the condenser is preferably provided with a light component non-condensable gas discharge line for releasing the light components.
In order to fully utilize the heat, preferably, the bottom outlet of the lean EO absorption water flash chamber or the lean EO absorption water flash tank is connected with an EO product tower kettle pump and then divided into two branches, wherein one branch is connected with an EO aldehyde removal tower reboiler.
The manner in which the sections in the EO rich absorption water refining chamber communicate in accordance with the present invention may be any of a variety of conventional manners known in the art. For example, a vapor lifting tray is arranged between each section to communicate vapor phase; and a liquid phase extraction line is also arranged on the steam raising tray so as to lead the liquid phase into the lower section from the upper section and communicate the liquid phases of all the sections.
The present invention also provides a process for producing purified ethylene oxide using the above apparatus, which comprises:
(1) the EO-rich absorption water from the front EO absorption section enters the upper part of an EO stripping section of an EO product tower, EO stripping, EO concentration and EO refining are sequentially carried out in the EO product tower, and a refined EO product is extracted from the lateral line of the EO product tower;
(2) the EO product overhead material flow is collected in a reflux tank after being partially condensed by a condenser, and returns to the top of the EO product through an EO reflux pump;
(3) and (3) extracting aldehyde-containing EO from the side line of the EO product tower, sending the EO into an EO aldehyde-discharging tower, removing aldehyde-containing impurities, returning the gas phase to the EO product tower, and pumping the EO aldehyde-discharging tower residue into a rear glycol production working section.
When the device is provided with the lean EO absorption water flash tank and the steam ejector, the steam ejector is used for depressurizing to flash the process steam, the steam and the power steam of the steam ejector are used as the stripping steam of the EO stripping section, the use amount of fresh stripping steam is reduced, and meanwhile, the temperature of the lean EO absorption water is reduced, so that the energy-saving effect is achieved.
According to a preferred embodiment of the invention, the light components (including CO) which are not condensed after partial condensation2Ethylene, etc.) is discharged through a light component non-condensable gas discharge pipeline arranged on the process side of the condenser and can be returned to the front section for recycling treatment.
According to the present invention, the aldehyde-containing EO is preferably withdrawn from a riser tray between the EO concentration section and the EO polishing section.
According to a preferred embodiment of the invention, the flashed lean EO absorption water is pumped up and at least partially used as a heat source for the EO rejection column reboiler, and may be combined and returned to the front EO absorption section.
According to the invention, process condensate or desalted water is added to the EO concentration stage to reduce overhead entrainment of impurities, such as aldehydes.
The specific conditions of each stage of the process in the invention can be conventional process conditions in the field, and can be flexibly selected by a person skilled in the art according to the needs. For the purpose of using the reactor EO capacity as much as possible for the production of refined EO, the following process conditions are preferably employed: the pressure of the EO-rich absorption water refining cavity is 0.26-0.3 MPaG (gauge pressure), and the temperature is 47-145 ℃; the pressure of the EO aldehyde discharging tower is 0.285-0.29 MPaG, and the temperature is 49-51 ℃. The pressure of the lean EO absorption water flash tank is 0.22-0.24 MPaG, and the temperature is 135-140 ℃.
By adopting the device and the method, more than 90 percent of the EO productivity of the reactor can be used for producing refined EO, and the rest part is used for producing glycol. Through the process optimization, the device structure is more compact, the equipment, particularly the rotating equipment, is greatly reduced, the operation safety of the device is improved, and meanwhile, the occupied area and the investment are saved; and the comprehensive utilization of energy is more reasonable, and the operation cost is reduced.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The above and other objects, features and advantages of the present invention will become more apparent by describing in more detail exemplary embodiments thereof with reference to the attached drawings, in which like reference numerals generally represent like parts throughout.
FIG. 1 is a schematic diagram of a prior art apparatus for producing refined ethylene oxide.
FIG. 2 is a schematic view of an apparatus for producing purified ethylene oxide according to an embodiment of the present invention.
Description of the reference numerals
1 EO stripping/rectifying tower 2 EO stripping/rectifying tower reboiler
3 EO stripping/rectifying tower kettle pump and 4 EO stripping/rectifying tower reflux pump
5 EO rectifying tower 6 EO rectifying tower reboiler 7 EO rectifying tower kettle pump
8 condenser 9 reflux tank 10 EO reflux pump
11 CO2Stripping column 12 CO2Stripper reboiler 13 CO2Stripping tower kettle pump
14 EO-rich absorption water 15 steam 16 process condensate or desalted water
17 lean EO absorption Water 18 Cooling Water 19 aldehyde-containing EO discharge
20-refined EO product 21 light component non-condensable gas discharge pipeline
22 EO PRODUCT COLUMN 23 EO ALDEHYDE-DISCHARGING COLUMN 24 STEAM EMITTER
25 rich EO absorbs water refining chamber 26 poor EO and absorbs water flash distillation chamber
27 EO refining section 28 EO concentration section 29 EO stripping section
30 lean EO absorbs water flash tank 31 EO product column reboiler
32 EO product tower kettle pump 33 EO aldehyde discharging tower reboiler 34 EO aldehyde discharging tower kettle pump
Detailed Description
The technical solution of the present invention will be further explained with reference to the drawings in the embodiments of the present invention. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments obtained by a person skilled in the art without any inventive step based on the embodiments of the present invention belong to the protection scope of the present invention.
Examples
An apparatus for producing purified ethylene oxide as shown in FIG. 2 was used. The device includes: EO product column 22 and EO aldehyde rejection column 23; the EO product tower 22 is provided with an EO product tower reboiler 31, and the EO aldehyde discharging tower 23 is provided with an EO aldehyde discharging tower reboiler 33;
the top of the EO product tower 22 is sequentially connected with a condenser 8, a reflux tank 9 and an EO reflux pump 10, an outlet pipeline of the EO reflux pump 10 is connected with the top of the EO product tower 22, and a light component non-condensable gas discharge pipeline 21 is arranged on the process side of the condenser 8;
after the outlet at the bottom of the EO product tower 22 is connected with an EO product tower kettle pump 32, one of the EO product tower kettle pumps is connected with an EO aldehyde-discharging tower reboiler 33 and is combined and returned to the front EO absorption section;
the refined EO product 20 is taken off at the side of the EO product tower 22 and sent to the finished product tank by gravity flow;
the EO product tower 22 is provided with an EO aldehyde discharging extraction line connected with the EO aldehyde discharging tower 23, the gas phase pipeline at the top of the EO aldehyde discharging tower 23 is connected with the EO product tower 22, and the outlet pipeline of the EO aldehyde discharging tower kettle pump 34 is sent to the ethylene glycol production working section;
an EO-rich absorption water refining cavity 25 and an EO-poor absorption water flash evaporation cavity 26 which are mutually independent are sequentially arranged in the EO product tower 22 from top to bottom;
the EO-rich absorption water refining cavity 25 is sequentially divided into an EO refining section 27, an EO concentrating section 28 and an EO stripping section 29 from top to bottom, and steam lifting trays are arranged among the sections to communicate a vapor phase; a liquid phase extraction line is also arranged on the steam raising tray so as to lead the liquid phase from the upper section to the lower section and enable the liquid phases of all the sections to be communicated.
Wherein, a lean EO absorption water flash evaporation tank 30 is arranged in the lean EO absorption water flash evaporation cavity 26, and the bottom of the lean EO absorption water flash evaporation tank 30 is connected with the bottom of the rich EO absorption water refining cavity 25 through a lean EO absorption water discharge line; the upper portion of the EO-lean absorption water flash tank 30 is connected by a line to the steam ejector 24, and the outlet line of the steam ejector 24 is connected to the lower portion of the EO-rich absorption water polishing chamber 25.
EO-rich absorption water 14(EO concentration 3 wt%) from the front EO absorption section enters the upper part of an EO stripping section 29 of an EO product tower 22, and after EO stripping, EO concentration and EO refining in the tower, a refined EO product 20 is extracted at the side line of the tower and is sent to a finished product tank area through gravity flow under the action of a head difference. Wherein process condensate or desalted water 16 is added above the feed point to EO product column 22. EO product column reboiler 31 provides heat for the process described above. A lean EO absorption water flash drum 30 is provided in the lower part of the body of the EO product column 22 and is depressurised by the steam ejector 24 to flash process steam which, together with motive steam from the steam ejector 24, is used as stripping steam for the EO stripping section in the EO product column 22. The flash evaporated lean EO absorption water 17 is boosted by an EO product tower kettle pump 32, part of the water is used as a heat source of an EO aldehyde-discharging tower reboiler 33, and then the water is combined and returned to the front EO absorption section.
The EO product overhead is partially condensed in condenser 8 and collected in reflux drum 9 and returned to the top of EO product column 22 via EO reflux pump 10. In which the light components (including CO) are not condensed2Ethylene, etc.) is returned to the front section recovery process through a light component noncondensable gas discharge line 21 provided on the process side of the condenser 8.
An aldehyde-containing EO is withdrawn from the riser tray between the EO concentration section 28 and the EO polishing section 27 of the EO product column 22 and fed to an EO aldehyde rejection column 23 where aldehyde impurities, such as acetaldehyde, are removed. The gas phase after aldehyde removal returns to the EO product tower 22 from the top of the EO aldehyde discharging tower 23; the liquid phase containing aldehyde EO discharge 19 is sent to the rear glycol production section at the bottom of the EO aldehyde discharging tower 23 through an EO aldehyde discharging tower kettle pump 32. The EO rejection column reboiler 33 provides heat for the process described above.
Wherein:
the pressure of an EO-rich absorption water refining cavity of the EO product tower is 0.28MPaG, and the temperature is 100 ℃;
the pressure of a flash chamber of the lean EO absorption water of the EO product tower is 0.23MPaG, and the temperature is 138 ℃;
the EO aldehyde rejection column was at a pressure of 0.29MPaG and a temperature of 50 ℃.
The extracted refined EO product meets the superior product requirements of the industrial ethylene oxide (GB/T13098-2006).
Claims (5)
1. An apparatus for producing refined ethylene oxide, comprising: an EO product tower, an EO aldehyde discharging tower, a condenser, a reflux tank and an EO reflux pump; the EO product tower is provided with an EO product tower reboiler, and the EO aldehyde-discharging tower is provided with an EO aldehyde-discharging tower reboiler; the top of the EO product tower is sequentially connected with a condenser, a reflux tank and an EO reflux pump, and an outlet pipeline of the EO reflux pump is connected with the top of the EO product tower; an EO aldehyde discharging line is arranged on the side line of the EO product tower and connected with the EO aldehyde discharging tower, and an EO aldehyde discharging tower top gas phase line is connected with the EO product tower;
wherein, an EO-rich absorption water refining cavity is arranged in the EO product tower body; the EO-rich absorption water refining cavity sequentially comprises an EO refining section, an EO concentration section and an EO stripping section from top to bottom, wherein the EO refining section, the EO concentration section and the EO stripping section are communicated with each other through a vapor phase and a liquid phase; a vapor lifting tray is respectively arranged between the EO refining section and the EO concentrating section and between the EO concentrating section and the EO stripping section, a liquid phase extraction line is arranged on the vapor lifting tray, and the liquid phase extraction line guides a liquid phase from the upper section to the lower section; the EO aldehyde discharge line is arranged on a lift-off tray between the EO refining section and the EO concentrating section; a refined EO product extraction line is arranged on the side line of the EO product tower, and an EO-poor absorption water discharge line is arranged at the bottom of the EO-rich absorption water refining cavity; water from the front EO-rich absorption enters the upper part of the EO stripping section; the inlet of the process condensate or the desalted water is arranged at the EO concentration section;
the apparatus further comprises a lean EO absorption water flash tank disposed within the EO product column body within a lean EO absorption water flash chamber located below the EO rich absorption water refining chamber, or the lean EO absorption water flash tank is disposed independently of the EO product column; the lean EO absorption water discharge line is connected to the bottom of the lean EO absorption water flash tank;
the device is also provided with a steam ejector, an inlet pipeline of the steam ejector is connected with the top of the EO-poor absorption water flash tank, and an outlet pipeline of the steam ejector is connected with the lower part of the EO-rich absorption water refining cavity.
2. The apparatus of claim 1 wherein the process side of the condenser is provided with a light component non-condensable gas discharge line.
3. A process for producing purified ethylene oxide using the apparatus according to claim 1 or 2, characterized by comprising:
(1) the EO-rich absorption water from the front EO absorption section enters the upper part of an EO stripping section of an EO product tower, EO stripping, EO concentration and EO refining are sequentially carried out in the EO product tower, and a refined EO product is extracted from a lateral line of the EO product tower; adding process condensate or desalted water into the EO concentration section; the pressure of the EO-rich absorption water refining cavity is 0.26-0.3 MPaG, and the temperature is 47-145 ℃;
(2) the EO product overhead material flow is collected in a reflux tank after being partially condensed by a condenser, and returns to the top of the EO product through an EO reflux pump;
(3) extracting aldehyde-containing EO from an EO aldehyde discharging line, sending the EO into an EO aldehyde discharging tower, removing aldehyde-containing impurities, and returning the gas phase to the EO product tower;
the apparatus further comprises a lean EO absorption water flash tank disposed within the EO product column body within a lean EO absorption water flash chamber located below the EO rich absorption water refining chamber, or the lean EO absorption water flash tank is disposed independently of the EO product column; the lean EO absorption water discharge line is connected to the bottom of the lean EO absorption water flash tank; the pressure of the lean EO absorption water flash tank is 0.22-0.24 MPaG, and the temperature is 135-140 ℃;
the device is also provided with a steam ejector, an inlet pipeline of the steam ejector is connected with the top of the EO-poor absorption water flash tank, and an outlet pipeline of the steam ejector is connected with the lower part of the EO-rich absorption water refining cavity;
the process steam is flashed by depressurization by a steam injector, which steam is used as stripping steam for the EO stripping section together with motive steam from the steam injector.
4. The process of claim 3, wherein the flashed lean EO absorption water is pumped up for use at least in part as a heat source for an EO aldehyde rejection column reboiler.
5. The process as claimed in claim 3 or 4, wherein the EO aldehyde rejection column has a pressure of 0.285 to 0.29MPaG and a temperature of 49 to 51 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610104471.6A CN107118181B (en) | 2016-02-25 | 2016-02-25 | Device and method for producing refined ethylene oxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610104471.6A CN107118181B (en) | 2016-02-25 | 2016-02-25 | Device and method for producing refined ethylene oxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107118181A CN107118181A (en) | 2017-09-01 |
| CN107118181B true CN107118181B (en) | 2020-05-08 |
Family
ID=59717791
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610104471.6A Active CN107118181B (en) | 2016-02-25 | 2016-02-25 | Device and method for producing refined ethylene oxide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107118181B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113845494A (en) * | 2021-10-27 | 2021-12-28 | 连云港石化有限公司 | Ethylene oxide refining system |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102137700A (en) * | 2008-07-31 | 2011-07-27 | 陶氏技术投资有限公司 | Processes and systems for purifying ethylene oxide |
-
2016
- 2016-02-25 CN CN201610104471.6A patent/CN107118181B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102137700A (en) * | 2008-07-31 | 2011-07-27 | 陶氏技术投资有限公司 | Processes and systems for purifying ethylene oxide |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107118181A (en) | 2017-09-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102190559B (en) | Method and device for refining methanol by using divided wall distillation column | |
| CN105218315B (en) | A kind of method and device of the refined methyl alcohol of use divided-wall distillation column combination heat pump | |
| CN104788289B (en) | A kind of pump coupled heat technique of ethylene glycol rectifying | |
| CN101492391A (en) | Process for separating ethane nitrile wastewater with combination of abstraction and distillation | |
| CN109761751A (en) | A kind of methanol thermal coupling multi-effect distillation method and device | |
| CN103788026A (en) | Method of purifying propylene epoxide | |
| CN106946654A (en) | A kind of separation method of biomass ethylene glycol | |
| CN107987038A (en) | Epoxidation technique feed separation system and epoxidation technique feed separation method | |
| CN100564335C (en) | A kind of preparation method of formic acid | |
| CN107118181B (en) | Device and method for producing refined ethylene oxide | |
| CN209759413U (en) | Rose extract product extraction element | |
| CN106496069B (en) | Energy-saving device and energy-saving method of acetonitrile refining system | |
| CN105061133B (en) | The recovery method of acetylene and retracting device during a kind of vinyl acetate production | |
| CN107011172A (en) | A kind of utilization partition tower refines the method and device of vinyl acetate | |
| CN102408349B (en) | System for removing formic acid generated during dimethylformamide recovering process | |
| CN101870529A (en) | Method for treating phenolic wastewater in smashed coal pressure gasification | |
| CN214913506U (en) | Carbon dioxide stripping regeneration system in ethylene oxide production | |
| CN212560051U (en) | Methyl methacrylate crude product's splitter | |
| CN216677028U (en) | Furfural refining device | |
| CN106187959A (en) | A kind of furfural treatment method | |
| RU2532808C1 (en) | Method of regenerating solvent in dewaxing and deoiling processes | |
| CN102807476B (en) | Method and device for continuous purification production of polyhydric alcohols | |
| CN102559372B (en) | Ethanol replacement oil preparation method and equipment | |
| CN207793117U (en) | A kind of improved refining of crude phenol system | |
| CN101028999B (en) | Method for extracting cottonseed protein and recovering methanol |
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 |