CN113528197B - Method for recovering hydrocarbons and acetonitrile by acetonitrile method butadiene extraction device - Google Patents
Method for recovering hydrocarbons and acetonitrile by acetonitrile method butadiene extraction device Download PDFInfo
- Publication number
- CN113528197B CN113528197B CN202010314938.6A CN202010314938A CN113528197B CN 113528197 B CN113528197 B CN 113528197B CN 202010314938 A CN202010314938 A CN 202010314938A CN 113528197 B CN113528197 B CN 113528197B
- Authority
- CN
- China
- Prior art keywords
- washing
- acetonitrile
- water
- tower
- solvent
- 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
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C253/00—Preparation of carboxylic acid nitriles
- C07C253/32—Separation; Purification; Stabilisation; Use of additives
- C07C253/34—Separation; Purification
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
- C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
- C07C7/08—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds by extractive distillation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to the technical field of ethylene cracking C4 fraction separation, and discloses a method for recovering hydrocarbons and acetonitrile by an acetonitrile method butadiene extraction device, which comprises the following steps: part of the washing tower water is sent to a dimer washing tower to be used as washing water to remove dimers in a regenerated solvent, dimers are discharged to a liquefaction fuel tank from the tower top, washing wastewater in the tower bottom is sent to a buffer tank for flash evaporation, the wastewater after flash evaporation in the buffer tank enters a solvent recovery tower after heat exchange, the buffer tank exhaust gas is converged with the solvent recovery tower top exhaust gas, the mixture is condensed into a liquid phase through a heat exchanger, the liquid phase is sent to the lower part of the dimer washing tower together with the regenerated solvent and liquefied hydrocarbon, after the mixture is in countercurrent contact with the washing water for water washing, hydrocarbons in the condensed liquid phase, dimers in the regenerated solvent and the liquefied hydrocarbon are discharged to the liquefaction fuel tank from the tower top, and the solvent is dissolved in the washing water and then discharged to the buffer tank from the tower bottom. The method can effectively improve the yield of products and byproducts, reduce the loss of the solvent and improve the economic benefit of the device.
Description
Technical Field
The invention relates to the technical field of separation of ethylene cracking C4 fractions, in particular to a method for recovering hydrocarbons and acetonitrile by an acetonitrile method butadiene extraction device.
Background
The process for extracting butadiene by acetonitrile method takes mixed C4 by-product of ethylene cracking device as raw material, acetonitrile as solvent, and produces polymer grade 1, 3-butadiene product by two-stage extractive distillation and two-stage common distillation. The acetonitrile solvent is extracted and rectified into a rich solvent, then is stripped into a poor solvent, and is recycled in the device after being recovered by a series of reboiler heat.
As is well known, because the saturated vapor pressure of acetonitrile solvent is lower and the acetonitrile solvent is more volatile, three water washing towers, namely a raffinate water washing tower, a butadiene water washing tower and a dimer water washing tower, are arranged in the acetonitrile method butadiene extraction device. In the acetonitrile method butadiene extraction device, raffinate extracted from the top of the first extractive distillation tower and crude butadiene extracted from the top of the second extractive distillation tower contain a certain amount of acetonitrile solvent, and acetonitrile in the raffinate and the crude butadiene is removed in a water washing mode by generally using the principle that water is similar to and soluble in acetonitrile in operation, so that the acetonitrile content in the product and the byproduct is ensured to be below a specified range; and part of the washing wastewater discharged from the two water washing tower kettles is sent to a dimer water washing tower to be used as washing water to remove dimer in the circulating solvent, and the dimer is removed from the top of the dimer water washing tower and is sent out of a battery limit as liquefied fuel. Washing wastewater containing the solvent and discharged from the three water washing tower kettles is converged into a buffer tank which is close to normal pressure and normal temperature, hydrocarbons and acetonitrile carried in the wastewater are flashed out in the buffer tank, and the flashed wastewater enters the middle part of the solvent recovery tower after being heated by a feeding heat exchanger through a feeding pump. The hydrocarbon, acetonitrile and water are separated in the solvent recovery tower, the acetonitrile and a small amount of hydrocarbon and water form an azeotrope which is separated from the top of the solvent recovery tower and then recycled, and the tower kettle is a wastewater discharge device.
However, the above method of removing acetonitrile by washing the C4 component with water and recycling acetonitrile in the waste water has a disadvantage. That is, the loss of the C4 hydrocarbons and the solvent in the vent gas from the buffer tank and the solvent recovery column top is large. When three strands of tower cauldron waste water that have the higher pressure join and get into the buffer tank that is close the ordinary pressure, because the reduction of pressure, the flash distillation can be carried out to tower cauldron waste water in the buffer tank. C4 hydrocarbons dissolved in the tower bottom wastewater under the high-pressure condition can be flashed and resolved out in the buffer tank, the quick flashing and resolving of the C4 components can also carry part of acetonitrile and water, and finally the buffer tank exhausts through an exhaust line discharge device of the buffer tank top pressure split system. The vent gas of the buffer tank generally contains high C4 content and a small amount of acetonitrile, which can cause the waste of device products, byproducts and solvents, reduce the hydrocarbon recovery rate of the device, increase the loss rate of the device solvents and further reduce the economic benefit of the device. Similarly, the normal-temperature tower washing wastewater after flash evaporation in the buffer tank enters the middle part of the solvent recovery tower through a feed pump and a feed heat exchanger after temperature rise, and hydrocarbons, acetonitrile and water are separated in the solvent recovery tower. The condition that C4 hydrocarbons are dissolved in normal-temperature wastewater subjected to flash evaporation in the buffer tank still exists, the hydrocarbons are heated by steam in the solvent recovery tower, and the hydrocarbons can be further analyzed from the wastewater due to the fact that the solubility of hydrocarbon gas is reduced along with the increase of the temperature, and finally can pass through an exhaust line discharge device of a tower top reflux tank split-flow system. Similarly, acetonitrile in the wastewater at normal temperature in the buffer tank is treated by the solvent recovery tower to form acetonitrile water to form an azeotrope (regenerated solvent) which is separated from the top of the solvent recovery tower, but the temperature of the regenerated solvent at the top of the solvent recovery tower is generally higher than the normal temperature of the buffer tank, the higher temperature can cause higher saturated vapor pressure of the acetonitrile, and part of the acetonitrile changes from liquid phase to gas phase in order to reach the saturated vapor pressure and finally is discharged out of the device along with the secondarily resolved hydrocarbons through an exhaust line of a tower top reflux tank split-pass system. The tower top exhaust of the solvent recovery tower generally contains higher C4 content and part of acetonitrile, which can cause the waste of device products, byproducts and solvents, reduce the hydrocarbon recovery rate of the device, increase the loss rate of the device solvents and further reduce the economic benefit of the device.
Therefore, the technology for reasonably recovering the hydrocarbons and the solvent of the acetonitrile method butadiene extraction device becomes a key technology for improving the yield of products and byproducts, reducing the solvent loss and improving the economic benefit of the device of the acetonitrile method butadiene extraction device.
Disclosure of Invention
In order to solve the problem of loss of hydrocarbons and solvents of an acetonitrile butadiene extraction device, the invention aims to provide a method for recovering hydrocarbons and solvents of the acetonitrile butadiene extraction device.
The invention provides a method for recovering hydrocarbons and acetonitrile by an acetonitrile method butadiene extraction device, which comprises the following steps: the method comprises the following steps that washing tower water parts of three washing towers in an acetonitrile butadiene extraction device are sent to a dimer washing tower to serve as washing water to remove dimers in a regeneration solvent, the dimers are discharged from the top of the dimer washing tower and serve as liquefied fuel to be sent to a liquefied fuel tank, washing wastewater in a dimer washing tower kettle and other washing tower water are sent to a buffer tank to be flashed, the wastewater flashed in the buffer tank enters a solvent recovery tower after heat exchange through a feed and discharge heat exchanger, the wastewater in the solvent recovery tower kettle is discharged as regeneration water after heat exchange through the feed and discharge heat exchanger, gas at the top of the solvent recovery tower enters a solvent recovery tower reflux tank after being condensed through a solvent recovery tower condenser, and liquid in the solvent recovery tower reflux tank reflows to the solvent recovery tower or serves as the regeneration solvent to be extracted; the method comprises the steps of merging the buffer tank exhaust gas with the solvent recovery tower top exhaust gas, condensing the liquid phase through a heat exchanger, then feeding the liquid phase, the regenerated solvent and the liquefied hydrocarbon into the lower part of a dimer water washing tower, carrying out countercurrent contact with washing water, washing, discharging the hydrocarbons in the condensed liquid phase, the dimers in the regenerated solvent and the liquefied hydrocarbon from the top of the dimer water washing tower together to serve as liquefied fuel, sending the liquefied fuel to a liquefied fuel tank, dissolving the solvent in the washing water, and then discharging the liquefied fuel from the bottom of the dimer water washing tower to a buffer tank.
The traditional acetonitrile method butadiene extraction device adopts a method of removing acetonitrile by washing C4 components and recycling acetonitrile in waste water, but the process of removing acetonitrile by washing C4 components and recycling acetonitrile can cause a great amount of loss of C4 and acetonitrile. The method comprises the steps of converging the buffer tank exhaust gas and the solvent recovery tower top exhaust gas, condensing the mixture into a liquid phase through a heat exchanger, feeding the liquid phase into the lower part of a dimer water washing tower, and discharging hydrocarbons in the liquid phase from the top of the dimer water washing tower after washing the liquid phase to be used as a liquefied fuel product. The method effectively improves the yield of products and byproducts, reduces the loss of solvent and improves the economic benefit of the device.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention without limiting the invention.
FIG. 1 is a schematic diagram of a process flow for recovering hydrocarbons and solvents in an extraction plant for butadiene by acetonitrile method according to an embodiment of the present invention.
Description of the reference numerals
1-buffer tank, 2-buffer tank discharge gas, 3-wastewater after flash evaporation in the buffer tank, 4-feed and discharge heat exchanger, 5-solvent recovery tower, 6-solvent recovery tower condenser, 7-solvent recovery tower reflux tank, 8-solvent recovery tower top discharge gas, 9-heat exchanger, 10-refrigerant, 11-liquid phase after condensation, 12-dimer water washing tower, 13-liquefied fuel tank, 14-liquefied fuel extraction pump, 15-liquefied fuel, 16-buffer tank feed, 17-regenerated water, 18-regenerated solvent, 19-liquefied hydrocarbon and 20-washing tower water.
Detailed Description
In order that the present invention may be more readily understood, the following detailed description of the invention is given with reference to the accompanying drawings and embodiments, which are given by way of illustration only and are not intended to limit the invention.
The invention provides a method for recovering hydrocarbons and acetonitrile by an acetonitrile method butadiene extraction device, which comprises the following steps: the washing tower water parts of three washing towers in the acetonitrile method butadiene extraction device are distributed to a dimer washing tower to be used as washing water to remove dimers in a regeneration solvent, the dimers are discharged from the top of the dimer washing tower to be used as liquefied fuel to be sent to a liquefied fuel tank, washing wastewater of a dimer washing tower kettle and other washing tower water are sent to a buffer tank to be flashed, the wastewater flashed in the buffer tank enters a solvent recovery tower after heat exchange through a material inlet and outlet heat exchanger, the wastewater of the solvent recovery tower kettle is discharged as regeneration water after heat exchange through a material inlet and outlet heat exchanger, gas at the top of the solvent recovery tower enters a solvent recovery tower reflux tank after being condensed through a solvent recovery tower condenser, the liquid in the solvent recovery tower reflux tank flows back to the solvent recovery tower or is discharged as the regeneration solvent, the buffer tank discharge gas and the solvent recovery tower top discharge gas are converged, condensed into a liquid phase through the heat exchanger, the liquid phase is sent to the lower part of the dimer washing tower together with the regeneration solvent and liquefied hydrocarbon to be in contact with the washing water, the condensed liquid phase, the dimers and the hydrocarbons in the regeneration solvent and the dimer are discharged from the top of the washing tower together as the liquefied fuel tank, and sent to the washing tower to be used as the liquefied fuel tank, and then the dimer washing water is sent to be discharged from the buffer tank after being reversely contacted with the dimer dissolving solvent.
In the invention, the buffer tank is used for collecting wastewater discharged from each washing tower kettle of the acetonitrile method butadiene device. Preferably, the buffer tank vent gas operating pressure: 10-100kPaG, operating temperature: 30-50 ℃, hydrocarbon content in buffer tank exhaust gas: 10-99.9wt%, and the balance of acetonitrile, water and nitrogen.
In the invention, the solvent recovery tower is used for refining the butadiene regeneration solvent by the acetonitrile method. Preferably, the solvent recovery overhead gas operating pressure is: 5-500kPaG, operating temperature: 60-150 ℃, hydrocarbon content in the vent gas at the top of the solvent recovery tower: 0.1-60wt%, and the balance of acetonitrile, water and nitrogen. In addition, the vent gas at the top of the solvent recovery tower is discharged from the top of the reflux tank of the solvent recovery tower.
According to the invention, the heat exchanger condenses the buffer tank discharge gas and the solvent recovery tower top discharge gas into a liquid phase by using a refrigerant, wherein the refrigerant can use hydrocarbons such as propylene and the like, and the condensation temperature of the hydrocarbons is 0.1-20 ℃. Preferably, the process side operating pressure of the heat exchanger is: 5-100kPaG, operating temperature: 0.1-20 ℃.
Preferably, the dimer water washes are from 30 to 50 plates, at an operating pressure of from 0.2 to 0.4MPaG and at an operating temperature of from 30 to 45 ℃.
Preferably, the upper part of the dimer water-washing column is introduced into the solvent recovery column with the discharged regeneration water or fresh water as washing water together with the washing water. The washing water can better recover the hydrocarbons and the solvent in the condensed liquid phase, the addition amount of the regeneration water or the fresh water and the washing water is that the solvent in the condensed liquid phase and the regeneration solvent is completely dissolved, the hydrocarbons, the dimers and the liquefied hydrocarbons are discharged, and the specific amount is determined according to the requirement and belongs to the conventional selection.
The process parameters which are not limited in the invention can be selected conventionally according to the prior art.
The present invention will be described in detail by way of examples.
Examples
This example illustrates the recovery of hydrocarbons and acetonitrile in an acetonitrile butadiene extraction unit of the present invention.
As shown in fig. 1, taking the data of a butadiene extraction apparatus by 12 ten thousand ton/year acetonitrile method as an example:
buffer tank vent gas 2, operating pressure: 70kPaG, operating temperature: 38.5 ℃, wherein the hydrocarbon content: 93.4% (by weight); acetonitrile content: 5.1 percent (weight ratio), and the balance of nitrogen and water; the flow rate is as follows: 120kg/h;
solvent recovery overhead vent gas 8, operating pressure: 70kPaG, operating temperature: 82.8 ℃, wherein the hydrocarbon content: 39.7% (weight ratio); acetonitrile content: 48.8 percent (weight ratio), and the balance of nitrogen and water; the flow rate is as follows: 30kg/h;
the two exhaust gases are converged and then enter a heat exchanger 9 for condensation, and the process side operating pressure of the heat exchanger 9 is as follows: 60kPaG, operating temperature: 2 ℃, and the refrigerant 10 is propylene;
the liquid phase 11 after condensation enters a dimer water washing column 12, the number of the trays of the dimer water washing column 12 is 40, and the operation pressure at the top of the column is as follows: 0.31MPaG, operating temperature: at 40 ℃.
The specific process comprises the following steps:
The buffer tank exhaust gas 2 and the solvent recovery tower top exhaust gas 8 are converged and then sent to a heat exchanger 9, and the heat exchanger 9 uses propylene as a refrigerant 10 to condense the two exhaust gases to a liquid phase. The condensed liquid phase 11 is introduced into the lower part of the dimer water-washing column 12 together with the liquefied hydrocarbon 19 and the regenerated solvent 18.
In the dimer water-washing column 12, the condensed liquid phase 11, the regenerated solvent 18 and the liquefied hydrocarbon 19 are brought into countercurrent contact with the washing water, the hydrocarbons in the condensed liquid phase 11, the dimer in the regenerated solvent 18 and the liquefied hydrocarbon 19 are discharged from the top of the dimer water-washing column 12 together as the liquefied fuel 15 and sent to the liquefied fuel tank 13, and the solvent is dissolved in the washing water and then discharged from the bottom of the dimer water-washing column 12 and sent to the buffer tank 1.
The effects are as follows:
according to the data, the operation time of the 12 ten thousand tons/year acetonitrile method butadiene extraction device is 8000 hours per year, compared with the traditional acetonitrile method butadiene extraction device, the method can recover about 992 tons of liquefied fuel per year, reduce the loss of acetonitrile by about 166 tons, effectively improve the yield of products and byproducts, reduce the loss of solvent and improve the economic benefit of the device.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the disclosed embodiments. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the illustrated embodiments.
Claims (5)
1. A method for recovering hydrocarbons and acetonitrile by an acetonitrile method butadiene extraction device comprises the following steps: the method comprises the following steps that washing tower water parts of three washing towers in an acetonitrile method butadiene extraction device are sent to a dimer washing tower to be used as washing water to remove dimers in a regeneration solvent, the dimers are discharged from the top of the dimer washing tower and are sent to a liquefaction fuel tank as liquefaction fuel, washing wastewater of a dimer washing tower kettle and other washing tower water are sent to a buffer tank for flash evaporation, the wastewater subjected to flash evaporation in the buffer tank enters a solvent recovery tower after heat exchange through a material inlet and outlet heat exchanger, the wastewater of the solvent recovery tower kettle is discharged as regeneration water after heat exchange through a material inlet and outlet heat exchanger, gas at the top of the solvent recovery tower enters a solvent recovery tower reflux tank after condensation through a solvent recovery tower condenser, and liquid in the solvent recovery tower reflux tank flows back to the solvent recovery tower or is extracted as the regeneration solvent; characterized in that the method further comprises: merging the buffer tank exhaust gas with the solvent recovery tower top exhaust gas, condensing the liquid phase through a heat exchanger, then entering the lower part of a dimer water washing tower together with a regenerated solvent and liquefied hydrocarbon, after the liquid phase is in countercurrent contact with washing water and washed, discharging the hydrocarbons in the condensed liquid phase, the dimer in the regenerated solvent and the liquefied hydrocarbon from the top of the dimer water washing tower as liquefied fuel and sending the liquefied fuel to a liquefied fuel tank, and after the solvent is dissolved in the washing water, discharging the liquefied fuel from the bottom of the dimer water washing tower and sending the liquefied fuel to the buffer tank;
wherein, the process side operating pressure of the heat exchanger is as follows: 5-100kPaG, operating temperature: 0.1-20 ℃.
2. The method for recovering hydrocarbons and acetonitrile by an acetonitrile butadiene extraction unit according to claim 1, wherein the operating pressure of the buffer tank vent gas is as follows: 10-100kPaG, operating temperature: 30-50 ℃, hydrocarbon content in buffer tank exhaust gas: 10-99.9wt%, and the balance of acetonitrile, water and nitrogen.
3. The method for recovering hydrocarbons and acetonitrile by an acetonitrile butadiene extraction unit according to claim 1, wherein the operating pressure of the solvent recovery overhead gas is as follows: 5-500kPaG, operating temperature: 60-150 ℃, hydrocarbon content in the vent gas at the top of the solvent recovery tower: 0.1-60wt%, and the balance of acetonitrile, water and nitrogen.
4. The method for recovering hydrocarbons and acetonitrile by an acetonitrile butadiene extraction apparatus according to claim 1, wherein the dimer washing stage number is 30 to 50 plates, the operation pressure is 0.2 to 0.4MPaG, and the operation temperature is 30 to 45 ℃.
5. The method for recovering hydrocarbons and acetonitrile by an acetonitrile butadiene extraction apparatus according to claim 1, wherein the upper part of the dimer water washing column is introduced into the regenerated water or fresh water discharged from the bottom of the solvent recovery column as washing water together with the washing water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010314938.6A CN113528197B (en) | 2020-04-20 | 2020-04-20 | Method for recovering hydrocarbons and acetonitrile by acetonitrile method butadiene extraction device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010314938.6A CN113528197B (en) | 2020-04-20 | 2020-04-20 | Method for recovering hydrocarbons and acetonitrile by acetonitrile method butadiene extraction device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113528197A CN113528197A (en) | 2021-10-22 |
| CN113528197B true CN113528197B (en) | 2023-03-28 |
Family
ID=78123768
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010314938.6A Active CN113528197B (en) | 2020-04-20 | 2020-04-20 | Method for recovering hydrocarbons and acetonitrile by acetonitrile method butadiene extraction device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113528197B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113956126A (en) * | 2021-10-26 | 2022-01-21 | 中国石油化工股份有限公司 | Butadiene separation method by recycling acetonitrile |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103864551A (en) * | 2012-12-10 | 2014-06-18 | 中国石油化工集团公司 | Method for increasing acetonitrile method 1,3-butadiene extraction equipment raffinate product specification |
| CN108727150B (en) * | 2017-04-25 | 2021-02-02 | 中国石化工程建设有限公司 | Method for controlling content of dimer in system circulating solvent of acetonitrile method butadiene extraction device |
| CN108218657B (en) * | 2018-01-08 | 2021-04-30 | 惠生工程（中国）有限公司 | Tail gas recovery method in acetonitrile method butadiene extraction process |
-
2020
- 2020-04-20 CN CN202010314938.6A patent/CN113528197B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN113528197A (en) | 2021-10-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100484894C (en) | Method for treating coal gasification wastewater by single-tower pressurization stripping and device therefor | |
| US3165539A (en) | Recovery of ethylene oxide from a liquid mixture thereof with normally gaseous impurities | |
| CN111954654B (en) | Method for separating aromatic hydrocarbon by extractive distillation | |
| EP2257353A1 (en) | Improved extractive distillation processes using water-soluble extractive solvents | |
| CN101798255A (en) | Method for separating diolefin from petroleum cracking C5 fraction by acetonitrile | |
| CN102781891A (en) | Process for removing oxygenated contaminants from a hydrocarbon stream | |
| US20140350319A1 (en) | Process for removing oxygenated contaminants from an hydrocarbonstream | |
| CN113528197B (en) | Method for recovering hydrocarbons and acetonitrile by acetonitrile method butadiene extraction device | |
| CN101092570B (en) | Method of catalytic cracking reaction for separating oil and gas rich in light hydrocarbon | |
| CN102485708B (en) | C5 fraction separation method employing hypergravity extractive distillation apparatus | |
| CN108727150B (en) | Method for controlling content of dimer in system circulating solvent of acetonitrile method butadiene extraction device | |
| CN1083819C (en) | Method for separating arene by using extraction and rectification | |
| CN108218657B (en) | Tail gas recovery method in acetonitrile method butadiene extraction process | |
| US4306945A (en) | Extracting aromatic hydrocarbons from mixtures containing same | |
| CN112760130B (en) | Oil-gas separation and recovery device and method | |
| CN112760129B (en) | Oil-gas separation and recovery device and method | |
| CN112760127B (en) | Oil-gas separation and recovery device and method | |
| CN112760134B (en) | Oil gas recovery method and device | |
| KR102070422B1 (en) | Propene separation method using extractive distillation | |
| CN112760126B (en) | Oil-gas separation and recovery device and method | |
| CN211871870U (en) | System for recovering carbon second fraction in refinery dry gas | |
| CN115055132B (en) | Production process and device for preparing ethylene by ethanol dehydration | |
| CN112760131B (en) | Oil gas recovery method and device | |
| CN117004430A (en) | Method and device for producing low-aromatic diesel oil and aromatic hydrocarbon | |
| CN106397090B (en) | Producing ethylene with acetylene hydrogenation crude product air lift is dense with separation method and equipment |
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 |