CN110156557B - Method for recovering petrochemical produced gas - Google Patents
Method for recovering petrochemical produced gas Download PDFInfo
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- CN110156557B CN110156557B CN201910499476.7A CN201910499476A CN110156557B CN 110156557 B CN110156557 B CN 110156557B CN 201910499476 A CN201910499476 A CN 201910499476A CN 110156557 B CN110156557 B CN 110156557B
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/04—Purification or separation of nitrogen
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/40—Carbon monoxide
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
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- 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0001—Separation or purification processing
- C01B2210/0009—Physical processing
- C01B2210/0025—Physical processing by absorption in liquids
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- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention relates to a method for recovering and treating petrochemical produced gas with strong applicability, low energy consumption and high product purity. The method has good wide applicability, can be suitable for gas byproducts produced in petrochemical processing processes such as catalytic cracking, catalytic reforming, isomerization and the like, realizes the high-efficiency recovery of gases such as hydrogen, carbon monoxide, methane, ethylene, ethane and the like in chemical gases, and has high economic value by recycling the absorbent and the refrigerant.
Description
Technical Field
The invention relates to the field of organic chemical industry, in particular to a method for recovering petrochemical industry produced gas.
Background
In the petroleum processing process, a large amount of light hydrocarbon components can be produced as a byproduct due to the cracking and reforming processes, wherein the yield of dry gas is 3-4%, the dry gas mainly comprises methane, and part of components are rich in C2 +Light hydrocarbon; the yield of liquefied gas is about 5-7%, and the liquefied gas mainly contains C3、C4The components and the byproducts are mostly part of raw materials required in the petrochemical production process, and especially methane, hydrogen, ethane and the like are important cost components in the petrochemical production.
Therefore, the method for separating and recovering the light hydrocarbon from the tail gas produced by the petrochemical industry has great economic and social benefits. The existing technologies for recovering light hydrocarbons mainly comprise a cryogenic separation method, an absorption separation method, a pressure swing adsorption method, a membrane separation method, a metal complex separation method, a hydrate separation method and the like.
Chinese patent CN1160748A discloses a method for recovering and separating catalytic conversion gas rich in propylene and butylene, which comprises feeding cracked products into a fractionating tower, simultaneously extracting a mixture of recycled oil and slurry oil from the bottom of the tower, directly using the heat of the mixture as a heat source of a reboiler of a stabilizer, and using the middle section of the fractionating tower as a heat source of a reboiler of a desorption tower through circulating reflux;
chinese patent CN1640992A proposes a refrigeration oil absorption method for recovering liquefied gas from oil field associated gas or natural gas, which can be used in the situation of using less absorbent to obtain higher light hydrocarbon recovery rate, and has the advantages of simple process, reduced energy consumption and improved economic benefit. However, the method is only suitable for recovering liquefied gas from oilfield associated gas or natural gas, cannot be applied to gas produced by petrochemical technology, and cannot recover C2、C3、C4The fractions were separated.
US5502971A discloses a process for recovering C2And a low-pressure low-temperature process of heavier hydrocarbons, which is suitable for recovering refinery dry gas. The process cancels the traditional high-pressure scheme and adopts a low-pressure technology, so that the recovery temperature can be kept above the temperature of the generated nitric acid resin, the potential possibility of danger is avoided, and simultaneously, the higher olefin yield can be kept. Although the process adopts a low-pressure scheme, the temperature is still as low as-100 ℃, and the process still belongs to a cryogenic separation process, so the investment is large and the energy consumption is high.
Therefore, the above methods have the disadvantages of large investment, high energy consumption, low yield purity, insufficient separation and the like.
Disclosure of Invention
The invention aims to provide a method for recovering and treating petrochemical produced gas with strong applicability, low energy consumption and high product purity. The specific technical scheme is as follows:
a petrochemical gas recovery method specifically comprises the following steps:
after the petrochemical gas is pretreated, free water and impurities are removed, the pressure is increased by a compressor, the petrochemical gas enters a cooler for cooling and drying, the petrochemical gas enters a first absorption tower from the bottom of the first absorption tower after passing through a balance tank, and C in the petrochemical gas is absorbed by a first absorbent in the first absorption tower2And heavier components to obtain rich absorption liquid, the rich absorption liquid is discharged from the bottom of the first absorption tower and enters the balance tank to be contacted with the raw material gas, and the gas discharged from the top of the first absorption towerEntering the bottom of the second absorption tower, and further absorbing a small amount of C in the gas by a second absorbent in the tower2The gas discharged from the second absorption tower is cooled and then enters a gas-liquid separator, and CO and H2The gas is discharged from a gas outlet of the gas-liquid separator, the separated liquid phase is sent to a desorption tower, and the gas discharged from the top of the desorption tower comprises CO and N2，H2The bottom of the desorption tower produces methane; sending the rich absorption liquid flowing out of the balance tank to a deethanizer, and distilling off C from the top of the deethanizer2Cooling the fraction, separating into gas-liquid two phases in a first reflux tank, refluxing one part of the liquid phase to a deethanizer, sending the other part of the liquid phase to a first absorption tower, allowing the gas phase in the reflux tank to enter a third absorption tower to contact with a third absorbent, sending the rich absorption liquid to the deethanizer from the bottom of the third absorption tower, and discharging C from the top of the third absorption tower2Is sent to a first rectifying tower to separate ethylene and ethane; the bottom discharge of the deethanizer enters a depropanizer to C3Separation is carried out, C3Cooling, separating into gas phase and liquid phase in a second reflux tank, refluxing the liquid phase to the depropanizing tower, introducing the gas phase into a fourth absorption tower, delivering rich absorption liquid from the bottom of the fourth absorption tower to the depropanizing tower, and discharging C from the top of the fourth absorption tower3(ii) a The bottom discharge of the depropanizing tower enters a debutanizing tower to be treated with C4Separation is carried out, C4Cooling, separating into gas phase and liquid phase in the third reflux tank, refluxing the liquid phase to the debutanizer, and outputting gas phase C4Fractionating; the bottom discharge of the debutanizer is sent to a second rectifying tower, and C is output from the top of the second rectifying tower5Cut fraction, bottom stable gasoline is produced.
Further, a fourth absorption column top discharge C3Sending the mixture to a third rectifying tower to separate propylene and propane.
Further, methane produced by the desorption tower is used as a refrigerant.
Further, carrying out subsequent rectification treatment on the rich absorption liquid discharged from the bottom of the second absorption tower.
Further, the stable gasoline produced at the bottom of the second rectifying tower is used as an absorbent.
The invention has the beneficial effects that:
1. the method for recovering petrochemical gas has good wide applicability, and can be suitable for gas byproducts produced in petrochemical processing processes such as catalytic cracking, catalytic reforming, isomerization and the like.
2. The recovery method of the invention can effectively separate the gases such as hydrogen, carbon monoxide and the like in the petrochemical gas and can obtain high-purity methane.
3. The recovery method provided by the invention is matched with the fractionating tower to arrange the absorption tower, so that the working energy consumption of the recovery method can be effectively reduced, the purity of the separated product is improved, and partial recycling of the absorbent is realized.
4. The recovery method has the characteristics of simple operation, low energy consumption and high recovery rate, and can separate and extract products such as methane, ethylene, ethane and the like in the petrochemical gas according to requirements.
Drawings
FIG. 1 is a schematic process flow diagram of a petrochemical process gas recovery process according to the present invention;
1. the system comprises a compressor, 2, a cooler, 3, a balance tank, 4, a first absorption tower, 5, a second absorption tower, 6, a gas-liquid separator, 7, a desorption tower, 8, a deethanizer, 9, a cooler, 10, a first reflux tank, 11, a third absorption tower, 12, a first rectifying tower, 13, a depropanizer, 14, a cooler, 15, a second reflux tank, 16, a fourth absorption tower, 17, a third rectifying tower, 18, a debutanizer, 19, a cooler, 20, a third reflux tank and 21, a second rectifying tower.
Detailed Description
Referring to fig. 1, the invention is a petrochemical produced gas recovery method, comprising the following specific operation steps:
the gas produced by petrochemical technology is firstly pretreated to remove free water and impurities, then the pressure is increased by a compressor 1, the gas enters a cooler 2 for cooling and drying, then the gas enters a first absorption tower 4 from the bottom after passing through a balance tank 3, and C in the gas is absorbed by a first absorbent in the first absorption tower 42And heavier components are obtained, rich absorption liquid is obtained, the rich absorption liquid is discharged from the bottom of the first absorption tower 4 and enters the balancing tank 3 to be contacted with the raw material gas, and the rich absorption liquid is discharged from the top of the first absorption tower 4The gas thus discharged is introduced into the bottom 5 of the second absorption column, where a small amount of C in the gas is further absorbed by the second absorbent2The gas discharged from the second absorption tower 5 is cooled and enters a gas-liquid separator 6 for separating CO and H2The gas is discharged from a gas outlet of the gas-liquid separator 6, the separated liquid phase is sent to a desorption tower 7, and the gas discharged from the top of the desorption tower 7 comprises CO and N2，H2The bottom of the desorption tower 7 produces methane; sending the rich absorption liquid flowing out of the balancing tank 3 to a deethanizer 8, and distilling off C from the top of the deethanizer 82The distillate is cooled and then is divided into a gas phase and a liquid phase in a first reflux tank 10, one part of the liquid phase reflows to a deethanizer 8, the other part of the liquid phase is sent to a first absorption tower 4, the gas phase in the reflux tank 3 enters a third absorption tower 11 to be contacted with a third absorbent, rich absorption liquid is sent to the deethanizer 8 from the bottom of the third absorption tower 11, and C discharged from the top of the third absorption tower 112Is sent to a first rectification column 12 to separate ethylene and ethane; the bottom discharge of the deethanizer 8 enters a depropanizer 13 for reaction C3Separation is carried out, C3Cooling, separating into gas phase and liquid phase in the second reflux tank 15, refluxing the liquid phase to the depropanizing tower 13, introducing the gas phase into the fourth absorption tower 16, delivering the rich absorption liquid from the bottom of the fourth absorption tower 16 to the depropanizing tower 13, and discharging C from the top of the fourth absorption tower 163And a top discharge C of the fourth absorption column 163Sending the mixture to a third rectifying tower 17 for separating propylene and propane, discharging the bottom of a depropanizing tower 13, sending the discharged material to a debutanizing tower 18 for removing C4Separation is carried out, C4Cooled and then enters a third reflux tank 20 to be divided into a gas phase and a liquid phase, the liquid phase refluxes to the debutanizer 18, and the output gas phase is C4Fractionating; the bottom discharge of the debutanizer 18 is sent to the second rectifying tower 2, and the top output C of the second rectifying tower 215Cut fraction, bottom stable gasoline is produced.
The catalytic dry gas of a certain chemical plant is taken as a treatment object, and the composition of the catalytic dry gas is shown in table 1:
after the recovery method of the invention is used for processing, the hydrogen recovery rate reaches more than 90 percent, and the methane recovery rateUp to more than 80 percent, C2The recovery rate reaches more than 85 percent.
Although exemplary embodiments of the present invention have been described for illustrative purposes, those skilled in the art will appreciate that various modifications, additions, substitutions and the like can be made in form and detail without departing from the scope and spirit of the invention as disclosed in the accompanying claims, all of which are intended to fall within the scope of the claims, and that various steps in the various sections and methods of the claimed product can be combined together in any combination. Therefore, the description of the embodiments disclosed in the present invention is not intended to limit the scope of the present invention, but to describe the present invention. Accordingly, the scope of the present invention is not limited by the above embodiments, but is defined by the claims or their equivalents.
Claims (1)
1. A petrochemical gas recovery method specifically comprises the following steps:
pretreating petrochemical gas to be recovered to remove free water and impurities, increasing pressure by a compressor, cooling and drying by a cooler, introducing into a first absorption tower from the bottom of the first absorption tower after passing through a balance tank, and absorbing C in the gas by a first absorbent in the first absorption tower2And heavier components are obtained, the rich absorption liquid is discharged from the bottom of the first absorption tower and enters a balance tank to be contacted with the raw material gas, the gas discharged from the top of the first absorption tower enters the bottom of the second absorption tower, and the second absorbent further absorbs a small amount of C in the gas in the tower2The gas discharged from the second absorption tower is cooled and then enters a gas-liquid separator, and CO and H2The gas is discharged from a gas outlet of the gas-liquid separator, the separated liquid phase is sent to a desorption tower, and the gas discharged from the top of the desorption tower comprises CO and N2，H2The bottom of the desorption tower produces methane; sending the rich absorption liquid flowing out of the balance tank to a deethanizer, and distilling off C from the top of the deethanizer2Cooling the distillate, separating into gas phase and liquid phase in the first reflux tank, refluxing one part of the liquid phase to the deethanizer, and sending the other partIntroducing the gas phase in the reflux tank into a third absorption tower to contact with a third absorbent, delivering the rich absorption liquid to a deethanizer from the bottom of the third absorption tower, and discharging C from the top of the third absorption tower2Is sent to a first rectifying tower to separate ethylene and ethane; the bottom discharge of the deethanizer enters a depropanizer to C3Separation is carried out, C3Cooling, separating into gas phase and liquid phase in a second reflux tank, refluxing the liquid phase to the depropanizing tower, introducing the gas phase into a fourth absorption tower, delivering rich absorption liquid from the bottom of the fourth absorption tower to the depropanizing tower, and discharging C from the top of the fourth absorption tower3(ii) a The bottom discharge of the depropanizing tower enters a debutanizing tower to be treated with C4Separation is carried out, C4Cooling, separating into gas phase and liquid phase in the third reflux tank, refluxing the liquid phase to the debutanizer, and outputting gas phase C4Fractionating; the bottom discharge of the debutanizer is sent to a second rectifying tower, and C is output from the top of the second rectifying tower5Fractionating, and producing stable gasoline at the bottom;
a top discharge C of the fourth absorption column3Sending the mixture to a third rectifying tower to separate propylene and propane;
methane produced by the desorption tower is used as a refrigerant;
and carrying out subsequent rectification treatment on the rich absorption liquid discharged from the bottom of the second absorption tower.
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| CN201910499476.7A CN110156557B (en) | 2019-06-11 | 2019-06-11 | Method for recovering petrochemical produced gas |
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| CN201910499476.7A CN110156557B (en) | 2019-06-11 | 2019-06-11 | Method for recovering petrochemical produced gas |
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| CN110156557B true CN110156557B (en) | 2020-06-05 |
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| CN112174766B (en) * | 2020-11-02 | 2023-03-31 | 上海睿碳能源科技有限公司 | Method and apparatus for purifying a low carbon olefin containing stream |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101559320A (en) * | 2009-04-15 | 2009-10-21 | 上海惠生化工工程有限公司 | Separation method of Fischer-Tropsch synthesis gas by combining rectification and solvent absorption |
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Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101559320A (en) * | 2009-04-15 | 2009-10-21 | 上海惠生化工工程有限公司 | Separation method of Fischer-Tropsch synthesis gas by combining rectification and solvent absorption |
Non-Patent Citations (2)
| Title |
|---|
| "发挥炼油化工一体化优势从炼厂干气回收乙烯和轻烃";吴晓云;《当代石油石化》;20030630;第11卷(第6期);18-22 * |
| "回收炼厂干气中高浓度C2工艺开发及经济性评价";王珏;《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》;20170315(第3期);B015-29 * |
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