CN111004082A - System and method for removing carbon dioxide from C2 fraction - Google Patents
System and method for removing carbon dioxide from C2 fraction Download PDFInfo
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- CN111004082A CN111004082A CN201811165881.7A CN201811165881A CN111004082A CN 111004082 A CN111004082 A CN 111004082A CN 201811165881 A CN201811165881 A CN 201811165881A CN 111004082 A CN111004082 A CN 111004082A
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- C07C7/005—Processes comprising at least two steps in series
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- 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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
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Abstract
The invention discloses a system and a method for removing carbon dioxide from a C2 fraction. The method comprises the following steps: compressing and cooling the C2 fraction, then feeding the C2 fraction into the middle part of an absorption separation tower, taking methanol as a solvent in the absorption tower under a shallow cooling condition, and obtaining a hydrocarbon-rich gas with the purity of over 90 mol% at the top of the absorption tower and a carbon dioxide-rich gas at the top of a desorption tower by a method of introducing a circulating gas through decompression flash evaporation and compression of the absorption tower bottoms. The method can effectively remove carbon dioxide in the C2 fraction, simultaneously avoids the condition that components such as ethane, ethylene and the like are absorbed in the absorption process, has the hydrocarbon recovery rate of over 86 percent, and realizes better economic benefit. The physical absorption separation method is adopted, the solvent is easy to regenerate, the process flow is simple, and the investment cost is reduced.
Description
Technical Field
The invention relates to the technical field of C2 fraction separation, in particular to a system and a method for removing carbon dioxide from a C2 fraction.
Background
The energy structure of China presents the current situation of rich coal, poor oil and less gas, and the vigorous development of the coal chemical technology is one of the main directions of energy development of China due to the adjustment of the energy structure and strategy. The coal gasification technology provides an effective path for clean utilization of coal resources and solving the problem of energy structure. In the process of preparing the gas from the coal, a corresponding gas purification process such as low-temperature methanol washing is required to be matched to remove carbon dioxide and sulfide in the synthesis gas, and methanol can simultaneously absorb partial components such as C2 and the like in the purification process, so that the purge gas of the low-temperature methanol washing contains a certain amount of gases such as hydrocarbons such as ethane, ethylene and the like, and does not meet the emission standard, and meanwhile, the hydrocarbon components have a certain recovery value and need to be recovered.
CN 105435580 a discloses a method for recovering hydrocarbon components from purge gas of coal gasification low-temperature methanol washing, wherein the purge gas is subjected to two-stage pressure swing adsorption and membrane separation to obtain C2 fraction with a hydrocarbon concentration of about 36%, and methanol is used as an absorbent to further absorb carbon dioxide in the C2 fraction. In the methanol absorption process, components such as ethane and ethylene are absorbed simultaneously, so that the recovery rate of the C2 component is low; meanwhile, the gas operation load of the absorption tower is greatly changed due to the large content of the carbon dioxide.
Therefore, how to effectively separate carbon dioxide from the C2 fraction is a technical problem to be solved.
Disclosure of Invention
In order to realize the removal of carbon dioxide and the recovery of hydrocarbons in the C2 fraction and improve the recovery rate of hydrocarbons in the C2 fraction, the invention provides a system and a method for removing carbon dioxide from a C2 fraction. The invention uses methanol as solvent to remove carbon dioxide from C2 fraction under light cooling condition. Methanol is used as an absorption solvent, a decompression flash evaporation and compression circulating device is arranged at the bottom of an absorption tower, hydrocarbon-rich gas is obtained at the top of the absorption tower, carbon dioxide gas is obtained at the top of a desorption tower, the recovery rate of hydrocarbons reaches over 86 percent, the removal rate of carbon dioxide reaches over 95 percent, and the method has important industrial application value.
It is an object of the present invention to provide a system for removing carbon dioxide from a C2 fraction.
The system comprises:
an absorption tower, a reduced-pressure flash tank and a desorption tower;
the C2 fraction feed pipeline is connected with the compressor and the cooler in sequence and then connected with the middle part of the absorption tower; an outlet pipeline at the bottom of the absorption tower is connected with a reduced-pressure flash tank; an outlet pipeline at the top of the reduced-pressure flash tank is connected with a compressor and then is connected with the lower part of the absorption tower, and an outlet pipeline at the bottom of the reduced-pressure flash tank is connected with the middle part of the desorption tower after passing through a heat exchanger; an outlet pipeline at the bottom of the desorption tower passes through the heat exchanger and then is connected with the upper part of the absorption tower; the top of the desorption tower is connected with a product line;
among them, it is preferable that,
and the upper section of the absorption tower is provided with an intermediate condenser.
It is another object of the present invention to provide a process for removing carbon dioxide from a C2 fraction.
The method comprises the following steps:
and after the C2 fraction is compressed and cooled, methanol is adopted as an absorbent, and a hydrocarbon-rich gas product is obtained at the top of the absorption tower through absorption, reduced pressure flash evaporation, compression circulation and desorption, and a carbon dioxide-rich gas is obtained at the top of the desorption tower.
The method comprises the following steps:
(1) compressing and cooling the C2 fraction, then feeding the C2 fraction into the middle part of an absorption tower, adding an absorbent methanol from the top of the absorption tower, absorbing carbon dioxide in the C2 fraction, obtaining hydrocarbon-rich gas at the top of the tower, and sending the liquid phase at the bottom of the tower to a reduced-pressure flash tank;
(2) the liquid phase in the tower kettle is subjected to reduced pressure flash evaporation, hydrocarbons and part of carbon dioxide are flashed out and sent to a compressor as circulating gas, and the circulating gas is compressed and then returns to the lower part of the absorption tower;
(3) and (3) transferring the liquid phase at the bottom of the flash tank to a desorption tower after heat exchange, obtaining carbon dioxide-rich gas at the top of the tower, obtaining regenerated methanol at the bottom of the tower, cooling and returning to the absorption tower for recycling.
Among them, preferred are:
in the step (1), C2 fraction is compressed to 1.8 MPa-3.2 MPa, cooled to 5-20 ℃ and enters the middle part of the absorption tower.
In the step (2), the recycle gas after decompression flash evaporation is compressed to the pressure of 1.8-3.2 MPa and returns to the bottom of the absorption tower.
In the step (3), the regenerated methanol is obtained at the tower kettle of the desorption tower, the temperature is reduced to 5-20 ℃ after the methanol is cooled by a heat exchanger and a cooler, and the methanol returns to the absorption tower for recycling;
in step (3), preferably, a fresh stream of methanol is introduced into the bottom of the desorption tower as a make-up solvent, because the methanol absorbent will have a certain loss at the top of the absorption tower.
The number of the preferable theoretical plates of the absorption tower is 18-55, the operating pressure is 1.8-3.2 MPa, and the tower top temperature is 5-30 ℃;
the preferable operating pressure of the reduced-pressure flash tank is 0.6MPa to 1.2 MPa;
the preferable outlet pressure of the compressor is 1.8MPa to 3.2 MPa;
the number of the theoretical plates of the desorption tower is preferably 10-30, the operating pressure is 0.1-0.4 MPa, and the temperature of the tower kettle is 70-110 ℃.
The invention specifically adopts the technical scheme as follows:
(1) c2 fraction compression: the pressure of the C2 fraction is increased to 1.8MPa to 3.2MPa by a compressor;
(2) cooling of C2 fraction: cooling the compressed C2 fraction obtained in the step 1) to 5-20 ℃;
(3) absorption: the C2 fraction after compression and cooling enters the middle part of an absorption tower, methanol as an absorbent is sprayed from the top of the tower at the temperature of 5-20 ℃, heat is released in the absorption process, the temperature is reduced to 5-20 ℃ through an intercooler and then the methanol flows downwards, carbon dioxide is continuously absorbed from top to bottom and hydrocarbon components are released, and hydrocarbon-rich gas is obtained at the top of the absorption tower;
(4) decompression flash evaporation: the tower bottom liquid of the absorption tower enters a flash tank for decompression flash evaporation, the pressure drop is 0.6 MPa-1.2 MPa, hydrocarbon and carbon dioxide which are flashed out are taken as circulating gas, and the liquid phase enters a desorption tower after heat exchange;
(5) and (3) circulating gas compression: compressing the recycle gas obtained in the step 4) to 1.8-3.2 MPa by a compressor;
(6) desorbing: and (3) transferring the solvent subjected to pressure reduction flash evaporation to the middle part of a desorption tower after heat exchange, obtaining carbon dioxide-rich gas at the top of the desorption tower, obtaining a regenerated methanol solvent at the tower bottom, and returning the regenerated methanol solvent to the absorption tower for recycling after heat exchange of a heat exchanger and temperature reduction of a cooler.
In the method, the hydrocarbon-rich gas obtained in the step 3) mainly contains 75-94 mol% of hydrocarbon components such as methane, ethane and ethylene and 6-25 mol% of carbon dioxide.
In the method, the carbon dioxide-rich gas obtained in the step 6) mainly contains 86-95 mol% of carbon dioxide and 5-14 mol% of hydrocarbons such as ethane and ethylene.
In the method, because the circulating gas is introduced into the bottom of the absorption tower, components such as ethane, ethylene and the like are prevented from being absorbed simultaneously, the recovery rate of hydrocarbons reaches more than 85 percent, and the removal rate of carbon dioxide reaches more than 95 percent.
The C2 fraction is a concentrated gas obtained by removing most of carbon dioxide from purge gas of low-temperature methanol washing through pressure swing adsorption and membrane separation, the content of hydrocarbon components is 28-40 mol%, and the hydrocarbon components mainly comprise ethane, ethylene and a small amount of methane.
In the method, the C2 fraction is preferably fed at a temperature of 5-20 ℃, and a propylene refrigeration system can be selected, a lithium bromide refrigeration system can be selected to provide a refrigerant, and the lithium bromide refrigeration system is preferably selected.
In the method, the preferable feeding temperature of the methanol solvent is 5-20 ℃, a propylene refrigeration system can be selected, a lithium bromide refrigeration system can also be selected to provide a refrigerant, and the lithium bromide refrigeration system is preferable.
Preferably, the stripper overhead gas is sent to a concentration system or a fuel system.
The system of the invention is schematically illustrated in fig. 1, and the process of the invention is further explained below with reference to the drawing.
In the figure 1, C2 fraction 1 is pressurized to 1.8 MPa-3.2 MPa by a compressor 2, cooled to 5-20 ℃ by a cooler 4 and enters an absorption tower 6;
in the absorption tower 6, methanol is used as an absorption solvent, the methanol solvent 3 is sprayed from the top of the tower at the temperature of 5-20 ℃, a large amount of gas is absorbed at the top of the tower, and an intercooler is arranged at the upper section of the absorption tower to reduce the operation temperature in the absorption tower; completing the absorption and separation process in the absorption tower 6, and obtaining hydrocarbon-rich gas 7 at the top of the absorption tower; the tower liquid of the absorption tower enters a reduced pressure flash tank 8;
the tower bottom liquid from the absorption tower is decompressed to 0.6 MPa-1.2 MPa in a decompression flash tank 8 for flash evaporation, the flash evaporation gas is sent to a circulating gas compressor 9 as a circulating material flow for compression, and the liquid is sent to a desorption tower 12 after heat exchange through a heat exchanger 11;
the recycle gas from the reduced-pressure flash tank 8 is compressed to 1.8MPa to 3.2MPa by a recycle gas compressor 9 and returns to the bottom of the absorption tower 6 as recycle gas 5;
the carbon dioxide-rich solution after heat exchange by the heat exchanger 11 enters the middle part of the desorption tower 12, carbon dioxide-rich gas 13 is obtained at the top of the tower, regenerated solvent methanol is obtained at the bottom of the tower, and the regenerated solvent methanol returns to the absorption tower 6 for recycling after heat exchange and cooling.
The amount of absorbent used in the absorption column in the process of the present invention is not particularly limited, and can be determined by those skilled in the art depending on the degree of separation and the operating conditions.
In the method, the hydrocarbon-rich gas obtained at the top of the absorption tower can be sent to an ethylene cracking device to produce ethylene; if necessary, chemical absorption and other methods can be used to completely remove a small amount of carbon dioxide in the hydrocarbon-rich gas.
The method for removing the carbon dioxide in the C2 fraction by using the methanol as the absorption solvent has the following advantages:
(1) in the method, the carbon dioxide in the C2 fraction can be removed by adopting a decompression flash evaporation circulation mode; meanwhile, the components such as ethane and ethylene can be prevented from being absorbed, and the recovery rate of the C2 component is greatly improved;
(2) by adopting the modes of reduced pressure flash evaporation and compression circulation, the tower kettle of the absorption tower is not provided with a reboiler, so that the energy consumption can be saved by 35-45% compared with the mode of arranging the reboiler at the tower kettle of the absorption tower, the effective comprehensive utilization of energy is realized through a heat exchanger, and the method has important significance for energy conservation and environmental protection.
(3) In the method, the gas operation pressure is slightly medium, the absorption tower operation temperature is slightly shallow and cold (0-20 ℃), the requirements on operation conditions are not high, the investment is low, the operation cost is low, and the operation is simple;
(4) in the method, the carbon dioxide in the C2 fraction is removed by adopting a physical absorption method, the solvent is easy to regenerate, the process flow is simple, and the methanol has better chemical stability, no corrosivity, easily available raw materials and little pollution;
(5) in the method, the boiling point of the absorbent methanol is lower, the temperature requirement of the tower bottom of the desorption tower is not high, waste heat steam can be used as a heat source, and the energy consumption in the solvent recovery process is lower.
Drawings
FIG. 1 is a schematic diagram of a system for removing carbon dioxide from a C2 fraction according to the present invention;
description of reference numerals:
Detailed Description
The present invention will be further described with reference to the following examples.
Example 1
A system for removing carbon dioxide from a C2 fraction, as shown in fig. 1, the system comprising:
an absorption tower 6, a reduced-pressure flash tank 8 and a desorption tower 12;
a C2 fraction feeding pipeline is connected with a C2 fraction compressor 2 and a C2 fraction cooler 4 in sequence and then connected with the middle part of an absorption tower 6; an outlet pipeline at the bottom of the absorption tower 6 is connected with a reduced-pressure flash tank 8; an outlet pipeline at the top of the reduced-pressure flash tank 8 is connected with a circulating gas compressor 9 and then is connected with the lower part of the absorption tower 6, and an outlet pipeline at the bottom of the reduced-pressure flash tank 8 is connected with the middle part of the desorption tower 12 after passing through a heat exchanger 11; an outlet pipeline at the bottom of the desorption tower 12 passes through the heat exchanger 11 and the cooler 10 and then is connected with the upper part of the absorption tower 6; the top of the desorber 12 is connected to a carbon dioxide rich product line.
And an intermediate condenser is arranged at the upper section of the absorption tower 6.
The composition of the C2 fraction obtained from the low temperature methanol wash tail gas is shown in table 1.
TABLE 1
The C2 fraction is separated by adopting the method for removing the carbon dioxide in the C2 fraction by using the methanol as an absorption solvent.
The specific process comprises the following steps:
(1) the C2 fraction enters a compressor 2, the pressure is increased to 2.4MPa through compression, the C2 fraction enters a fraction cooler 4 to be cooled to 14 ℃, and the C2 fraction enters an absorption tower 6.
(2) Methanol is used as an absorption solvent in the absorption tower, the methanol solvent is sprayed from the top of the tower at the temperature of 8 ℃, the solvent absorbs a large amount of gas at the top of the tower, the temperature rises, the gas is cooled to 5 ℃ through an intercooler and flows downwards, carbon dioxide is gradually absorbed in the absorption tower and hydrocarbon components are released, and hydrocarbon-rich gas is obtained at the top of the absorption tower. The number of theoretical plates of the absorption column is preferably 25, the operating pressure is 2.4MPa, and the column top temperature is 10 ℃. The material liquid in the tower bottom enters a reduced pressure flash tank 8, and the hydrocarbon-rich gas at the tower top can be sent to an ethylene device.
(3) The bottom liquid from the absorption tower is flashed in a reduced-pressure flash tank 8 to 0.8MPa under reduced pressure. The flash evaporation gas as the recycle gas enters a recycle gas compressor 9, the pressure is increased to 2.5MPa through compression, and the flash evaporation gas as the recycle gas returns to the bottom of the absorption tower 6. Carbon dioxide and a small amount of ethane are mainly dissolved in the solution after the decompression flash evaporation, the solution enters a heat exchanger 11, exchanges heat with the bottom liquid of the desorption tower, and then enters the middle part of the desorption tower 12.
(4) The heat-exchange solution from the heat exchanger 11 enters the middle part of the desorption tower 12 for desorption. The theoretical plate number of the desorption tower is 10, the operation pressure is 0.25MPa, and the tower kettle temperature is 89 ℃. Obtaining carbon dioxide-rich gas at the top of the desorption tower, obtaining regenerated solvent methanol at the bottom of the desorption tower, cooling the solvent methanol to 8 ℃ by a heat exchanger 11 and an absorbent cooler, and returning the solvent methanol to the absorption tower 6 for recycling.
The composition of the isolated product is shown in Table 2
TABLE 2
In this example, the carbon dioxide removal rate was 95.14%, and the recovery rate of hydrocarbons in the fraction reached 88.6%.
Claims (9)
1. A system for removing carbon dioxide from a C2 fraction, the system comprising:
an absorption tower, a reduced-pressure flash tank and a desorption tower;
the C2 fraction feed pipeline is connected with the compressor and the cooler in sequence and then connected with the middle part of the absorption tower; an outlet pipeline at the bottom of the absorption tower is connected with a reduced-pressure flash tank; an outlet pipeline at the top of the reduced-pressure flash tank is connected with a compressor and then is connected with the lower part of the absorption tower, and an outlet pipeline at the bottom of the reduced-pressure flash tank is connected with the middle part of the desorption tower after passing through a heat exchanger; an outlet pipeline at the bottom of the desorption tower passes through the heat exchanger and then is connected with the upper part of the absorption tower; the top of the desorption tower is connected with a product extraction line.
2. A system for removing carbon dioxide from a C2 fraction, characterized by:
and the upper section of the absorption tower is provided with an intermediate condenser.
3. A method for removing carbon dioxide from a C2 fraction using the system of claim 1 or 2, wherein the method comprises:
and after the C2 fraction is compressed and cooled, methanol is adopted as an absorbent, and a hydrocarbon-rich gas product is obtained at the top of the absorption tower through absorption, reduced pressure flash evaporation, compression circulation and desorption, and a carbon dioxide-rich gas is obtained at the top of the desorption tower.
4. A method for removing carbon dioxide from a C2 fraction as claimed in claim 3, wherein:
the method comprises the following steps:
(1) compressing and cooling the C2 fraction, then feeding the C2 fraction into the middle part of an absorption tower, adding an absorbent methanol from the top of the absorption tower, absorbing carbon dioxide in the C2 fraction, obtaining hydrocarbon-rich gas at the tower top, and feeding tower bottom liquid to a reduced-pressure flash tank;
(2) carrying out reduced pressure flash evaporation on the tower bottom liquid, flashing hydrocarbon and part of carbon dioxide, sending the hydrocarbon and part of carbon dioxide to a compressor as circulating gas, and sending the circulating gas to the lower part of an absorption tower after boosting pressure;
(3) and (3) transferring the liquid phase at the bottom of the flash tank to a desorption tower after heat exchange, obtaining carbon dioxide-rich gas at the top of the tower, obtaining regenerated methanol at the bottom of the tower, cooling and returning to the absorption tower for recycling.
5. The method for removing carbon dioxide from a C2 fraction as set forth in claim 4, wherein:
in the step (1), C2 fraction is compressed to 1.8 MPa-3.2 MPa, cooled to 5-20 ℃ and enters the middle part of the absorption tower.
6. The method for removing carbon dioxide from a C2 fraction as set forth in claim 4, wherein:
in the step (2), the recycle gas after decompression flash evaporation is compressed to the pressure of 1.8-3.2 MPa and returns to the bottom of the absorption tower.
7. The method for removing carbon dioxide from a C2 fraction as set forth in claim 4, wherein:
in the step (3), the regenerated methanol is obtained at the tower kettle of the desorption tower, the temperature is reduced to 5-20 ℃ after the methanol is cooled by a heat exchanger and a cooler, and the methanol returns to the absorption tower for recycling.
8. The method for removing carbon dioxide from the fraction C2 according to claim 7, wherein:
in the step (3), a strand of fresh methanol is introduced into the tower bottom of the desorption tower to be used as a supplementary solvent.
9. The method for removing carbon dioxide from a C2 fraction as set forth in claim 4, wherein:
the number of theoretical plates of the absorption tower is 18-55, the operating pressure is 1.8-3.2 MPa, and the temperature at the top of the tower is 5-30 ℃;
the operating pressure of the reduced-pressure flash tank is 0.6MPa to 1.2 MPa;
the outlet pressure of the compressor is 1.8MPa to 3.2 MPa;
the number of theoretical plates of the desorption tower is 10-30, the operating pressure is 0.1-0.4 MPa, and the temperature of the tower kettle is 70-110 ℃.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114685236A (en) * | 2020-12-28 | 2022-07-01 | 中国石油化工股份有限公司 | Method and device for removing carbon dioxide and methanol from crude propylene gas |
| CN114853591A (en) * | 2022-06-13 | 2022-08-05 | 扬州大学 | Resource utilization method of acetone and carbon dioxide in sodium phenolate carboxylation reaction |
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| CN114853591A (en) * | 2022-06-13 | 2022-08-05 | 扬州大学 | Resource utilization method of acetone and carbon dioxide in sodium phenolate carboxylation reaction |
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