CN212335119U - Refinery gas separation and recovery system - Google Patents
Refinery gas separation and recovery system Download PDFInfo
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- CN212335119U CN212335119U CN202021953237.9U CN202021953237U CN212335119U CN 212335119 U CN212335119 U CN 212335119U CN 202021953237 U CN202021953237 U CN 202021953237U CN 212335119 U CN212335119 U CN 212335119U
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Abstract
The utility model discloses a refinery gas separation and recovery system. The system comprises a compressor, a condenser, a separation tank, a heater, a membrane separation unit and an absorption tower; refinery gas is introduced into the inlet end of the compressor, and the outlet end of the compressor is connected with the inlet end of the condenser; the outlet end of the condenser is connected with the inlet end of the separation tank; the outlet end of the top of the separation tank is connected with the inlet end of the heater; the outlet end of the heater is connected with the inlet end of the membrane separation unit; the outlet end of the retentate side of the membrane separation unit is connected with the inlet end of the bottom of the absorption tower; introducing an absorbent barren solution into an inlet end at the top of the absorption tower; and the outlet end at the top of the absorption tower is connected with a fuel gas pipe network. The system can recover hydrogen and light hydrocarbon to the maximum extent, the hydrogen recovery rate reaches over 86 percent, the light hydrocarbon recovery rate can reach over 87 percent, and greater economic benefit can be brought to refineries.
Description
Technical Field
The utility model relates to a refinery gas retrieves technical field, and more specifically says, in particular to refinery gas separation recovery system.
Background
Oil refineries, abbreviated as refineries, use petroleum as raw materials to produce various chemical raw materials, thereby meeting the requirements of national economic development and daily life of people. In order to ensure the stable operation of the plant, the gas is usually discharged into a gas cabinet through a special pipeline, so that the gas is called gas. At present, the scheme of recycling and reusing gas in a refinery plant is as follows: firstly, gas is sent into a desulfurizing device to remove hydrogen sulfide, and then the gas is sent into a fuel gas pipe network to be burnt as fuel gas. Generally, the gas contains a large amount of hydrogen and C3-C6 components, light hydrocarbons for short. The heat value of hydrogen is lower, and the hydrogen is also an important raw material of a hydrogenation device, and light hydrocarbon is an important chemical raw material, and the economic value of the hydrogen is far greater than that of fuel gas, so the current recycling scheme of a refinery is not economical. For example, according to the production data of a certain refinery, the refinery will produce 3.3 ten thousand tons of gas in one year, the hydrogen content in the gas is about 7 wt%, the value is 3895 ten thousand yuan, the light hydrocarbon content is about 34 wt%, the value is 2991 ten thousand yuan, the rest 59 wt% of the gas can be used as fuel gas, the value is 3894 ten thousand yuan, and the total value of the gas is 10780 ten thousand yuan. If only the gas is used as fuel gas, it can only produce 6653 ten thousand yuan of economic value.
SUMMERY OF THE UTILITY MODEL
In view of the above-mentioned deficiencies of the prior art, the present invention is directed to a refinery gas separation and recovery system for solving the problem of uneconomical recycling of refinery gas existing in the prior art.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a refinery gas separation and recovery system comprises a compressor 1, a condenser 2, a separation tank 3, a heater 4, a membrane separation unit 5 and an absorption tower 6;
refinery gas S-1 is introduced into the inlet end of the compressor 1, and the outlet end of the compressor 1 is connected with the inlet end of the condenser 2; the outlet end of the condenser 2 is connected with the inlet end of the separation tank 3; the outlet end of the top of the separation tank 3 is connected with the inlet end of the heater 4; the outlet end of the heater 4 is connected with the inlet end of the membrane separation unit 5; the outlet end of the retentate side of the membrane separation unit 5 is connected with the inlet end at the bottom of the absorption tower 6; an absorbent barren solution S-9 is introduced into the inlet end at the top of the absorption tower 6; and the outlet end at the top of the absorption tower 6 is connected with a fuel gas pipe network.
Optionally, according to the refinery gas separation and recovery system, the outlet end of the bottom of the separation tank 3 is connected with a liquid-phase light hydrocarbon S-5 receiving device outside the system.
Optionally, according to the refinery gas separation and recovery system, the outlet end of the permeation side of the membrane separation unit 5 is connected with a permeation gas S-8 receiving device containing high-purity hydrogen outside the system.
Optionally, according to the refinery gas separation and recovery system, the outlet end at the bottom of the absorption tower 6 is connected with a receiving device of the absorbent rich liquid S-11 outside the system.
Optionally, according to the refinery gas separation and recovery system, the outlet end at the top of the absorption tower 6 is connected with a fuel gas pipe network outside the system.
The utility model has the advantages and beneficial effect: the utility model provides a refinery gas separation recovery system at first utilizes the compressor to step up the gas to adopt the cold medium to liquefy the gas, retrieve some light bodies with the liquid form, then utilize gas membrane separation, let hydrogen survey the enrichment at the membrane infiltration, retrieve most hydrogen with the gas form, utilize the absorbent to retrieve remaining light hydrocarbon in oozing the residual gas at last, the residual gas can regard as the fuel gas to use. The separation and recovery method and the separation and recovery system can recover hydrogen and light hydrocarbon to the maximum extent, the hydrogen recovery rate reaches over 86 percent, the light hydrocarbon recovery rate reaches over 87 percent, and greater economic benefit is brought to refineries.
Drawings
FIG. 1 is a schematic structural view of a refinery gas separation and recovery system according to the present invention;
in the figure: 1. a compressor; 2. a condenser; 3. a separation tank; 4. a preheater; 5. a membrane separation unit; 6-an absorption tower; s-1, gas; s-2, high-temperature and high-pressure gas; s-3, mixing gas with liquid; s-4, gas phase components; s-5, liquid-phase light hydrocarbon; s-6, high-temperature gas phase components; s-7, residual gas is permeated; s-8, permeating gas; s-9, absorbent barren liquor; s-10, hydrogen and fuel gas with low light hydrocarbon content; s-11 and an absorbent rich solution.
Detailed Description
To facilitate an understanding of the present application, the present application will now be described more fully with reference to the accompanying drawings. Preferred embodiments of the present application are given in the accompanying drawings. This application may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. The terminology used herein in the description of the present application is for the purpose of describing particular embodiments only and is not intended to be limiting of the application.
The utility model provides a refinery gas separation recovery design as follows:
firstly, compressing refinery gas S-1, heating and boosting the compressed refinery gas S-1, and then condensing and cooling the high-temperature and high-pressure gas S-2 to change a part of gas-phase light hydrocarbon into a liquid phase so as to obtain gas-liquid mixed gas S-3;
then carrying out gas-liquid separation treatment on the gas-liquid mixed gas S-3 to obtain a gas-phase component S-4 and a liquid-phase light hydrocarbon S-5; wherein the obtained liquid-phase light hydrocarbon S-5 can be sent to other devices for reuse. And heating the gas-phase component S-4 to a temperature higher than the dew point temperature to obtain a high-temperature gas-phase component S-6.
Separating the high-temperature gas-phase component S-6 by using a membrane separation technology to obtain hydrogen-poor permeation residual gas S-7 and permeation gas S-8 containing high-purity hydrogen; wherein the obtained permeation gas S-8 of the high-purity hydrogen can be sent to other devices for reuse.
The membrane is based on a dissolution-diffusion principle, and due to the fact that pressure difference exists between two sides of the membrane, under the pushing of the pressure, all components are dissolved into the upstream side of the membrane firstly and then are diffused to the downstream side of the membrane, and due to the fact that the dissolution-diffusion rates of all components on the membrane are different, a certain component can permeate preferentially, and therefore separation of all components is achieved.
Then the hydrogen-poor retentate gas S-7 is contacted with the absorbent barren solution S-9, further preferably, the hydrogen-poor retentate gas S-7 is in countercurrent contact with the absorbent barren solution S-9, most of light hydrocarbon in the retentate gas S-7 is dissolved in the absorbent barren solution S-9 due to the high solubility of the light hydrocarbon in the absorbent, so that most of the light hydrocarbon is transferred from the retentate gas S-7 to the absorbent barren solution S-9, the retentate gas S-7 is changed into fuel gas S-10 with low content of hydrogen and light hydrocarbon, and the absorbent barren solution S-9 is changed into absorbent rich solution S-11; the absorbent rich liquid S-11 can be sent to other devices for reuse.
Finally, the fuel gas S-10 is sent to a fuel gas pipe network.
Based on above-mentioned refinery gas separation recovery design, the utility model provides a refinery gas separation recovery system, as shown in figure 1, this system includes compressor 1, condenser 2, knockout drum 3, heater 4, membrane separation unit 5 and absorption tower 6. Refinery gas S-1 is introduced into the inlet end of the compressor 1, and the outlet end of the compressor 1 is connected with the inlet end of the condenser 2; the outlet end of the condenser 2 is connected with the inlet end of the separation tank 3; the outlet end of the top of the separation tank 3 is connected with the inlet end of the heater 4; the outlet end of the heater 4 is connected with the inlet end of the membrane separation unit 5; the outlet end of the retentate side of the membrane separation unit 5 is connected with the inlet end at the bottom of the absorption tower 6; an absorbent barren solution S-9 is introduced into the inlet end at the top of the absorption tower 6; and the outlet end at the top of the absorption tower 6 is connected with a fuel gas pipe network.
After entering the compressor 1 from the inlet end of the compressor 1, the refinery gas S-1 is compressed and pressurized by the compressor 1, the compressed refinery gas S-1 is heated and pressurized to obtain high-temperature and high-pressure gas S-2, the high-temperature and high-pressure gas S-2 is cooled by a cooling medium in the condenser 2, and a part of gas-phase light hydrocarbon is changed into a liquid phase after being cooled to obtain gas-liquid mixed gas S-3. The gas-liquid mixed gas S-3 enters a separation tank 3 for gas-liquid separation treatment to obtain liquid-phase light hydrocarbon S-5 and a gas-phase component S-4. The liquid phase is accumulated at the bottom of the tank, and can be connected with a liquid phase light hydrocarbon S-5 receiving device outside the system at the outlet end of the bottom of the separating tank 3, and the liquid phase light hydrocarbon S-5 is recycled from the bottom of the tank to the outside of the boundary area. The gas phase component S-4 is heated up by the heat medium of the heater 4 to be higher than the dew point temperature, so as to obtain the high-temperature gas phase component S-6, and the skilled person in the art can easily know that the heat medium of the heater 4 can be hot water, steam and the like according to the professional knowledge in the field. The high-temperature gas-phase component S-6 enters a membrane separation unit 5, the membrane is based on a dissolution-diffusion principle, because pressure difference exists on two sides of the membrane, under the pushing of pressure, each component is firstly dissolved and enters the upstream side of the membrane and then diffuses to the downstream side of the membrane, because the permeation rate dissolution-diffusion rate of each component on the membrane is inconsistent, a certain component can preferentially permeate, so that the separation of each component is realized, for a glassy organic membrane, the permeation rate of a hydrogen component is far higher than that of other components, a hydrogen-poor permeation residual gas S-7 is obtained on the high-pressure side of the membrane separation unit 5, a permeation gas S-8 containing high-purity hydrogen can be obtained on the low-pressure side of the membrane separation unit 5, and a receiving device of the permeation gas S-8 can be connected to the outlet end of the permeation side of the membrane separation unit 5 to be sent out of a boundary area for reuse. The hydrogen-poor residual gas S-7 enters from the bottom of the absorption tower 6, and the absorbent lean liquid S-9 enters from the top of the absorption tower 6, wherein the absorbent lean liquid S-9 is gasoline, diesel oil and the like. The residual gas S-7 and the absorbent barren solution S-9 are in countercurrent contact in the absorption tower 6, most of light hydrocarbon is transferred from the residual gas S-7 to the absorbent barren solution S-9 due to the high solubility of the light hydrocarbon in the absorbent, the residual gas S-7 is changed into fuel gas S-10 with low content of hydrogen and light hydrocarbon and is sent to a fuel gas pipe network, the absorbent barren solution S-9 is changed into absorbent rich solution S-11, and the outlet end at the bottom of the absorption tower 6 can be connected with a receiving device of the absorbent rich solution to be sent to the outside of a boundary area for reuse.
Examples
Taking a certain oil refinery as an example, the oil refinery generates 3.3 ten thousand tons of gas one year, and the gas separation and recovery method and the system provided by the utility model are adopted to recover hydrogen and light hydrocarbon in the gas. The gas pressure in the plant was 0.4MPaG, the temperature was 30 ℃ and the gas composition is shown in Table 1.
TABLE 1 certain refinery gas composition
| Composition of | H2 | N2 | O2 | C1 | C2 | C3 | C4 | C5+ |
| Vol％ | 54.09 | 20.28 | 0.86 | 9.23 | 5.67 | 4.8 | 3.42 | 1.64 |
In the gas separation and recovery system provided by the utility model, the compressor 1 adopts a reciprocating compressor, and the power is 403. kW; the heat exchange area of the condenser 2 is 32m2(ii) a The separating tank 3 is vertical, and has a diameter of 2.8m and a volume of 28m3(ii) a The heat exchange area of the preheater 4 is 13m2(ii) a The membrane separation unit 5 used was a Prism-II membrane with a membrane area 1503m2(ii) a The diameter of the absorption tower (6) is 1.5m, and the number of the tower plates is 10.
Conditions of the compressor 1: the outlet pressure was 2.06 MPaG.
Condenser conditions: the temperature was 40 ℃.
The operating conditions of the membrane module are as follows: feed pressure 2.00MPaG, temperature 83 ℃; the pressure of the infiltration side is 5KPaG, and the temperature is 84 ℃; the pressure on the retentate side was 1.90MPaG and the temperature was 84 ℃.
Operating conditions of the absorption tower: the pressure at the top of the tower is 0.97MPaG, and the temperature is 43 ℃; the column bottom pressure was 1.00MPaG and the temperature was 51 ℃.
In the embodiment, the recovery rate of the refinery gas hydrogen is 86.46%, the recovery rate of the light hydrocarbon is 87.91%, 2596 ten thousand standard square hydrogen can be recovered one year, 9968 tons of light hydrocarbon can be recovered one year, and the economic benefit can reach 2942 ten thousand yuan per year.
It is to be understood that the invention is not limited to the above-described embodiments, and that modifications and variations may be made by those skilled in the art in light of the above teachings, and all such modifications and variations are intended to be included within the scope of the invention as defined in the appended claims.
Claims (5)
1. A refinery gas separation and recovery system is characterized by comprising a compressor (1), a condenser (2), a separation tank (3), a heater (4), a membrane separation unit (5) and an absorption tower (6);
refinery gas (S-1) is introduced into the inlet end of the compressor (1), and the outlet end of the compressor (1) is connected with the inlet end of the condenser (2); the outlet end of the condenser (2) is connected with the inlet end of the separation tank (3); the outlet end of the top of the separation tank (3) is connected with the inlet end of the heater (4); the outlet end of the heater (4) is connected with the inlet end of the membrane separation unit (5); the outlet end of the retentate side of the membrane separation unit (5) is connected with the inlet end of the bottom of the absorption tower (6); an absorbent barren solution (S-9) is introduced into the inlet end at the top of the absorption tower (6); and the outlet end at the top of the absorption tower (6) is connected with a fuel gas pipe network.
2. The refinery gas separation and recovery system according to claim 1, wherein the outlet end at the bottom of the knockout drum (3) is connected with a liquid-phase light hydrocarbon (S-5) receiving device outside the system.
3. The refinery gas separation and recovery system according to claim 1, wherein the outlet end of the permeation side of the membrane separation unit (5) is connected to a permeation gas (S-8) receiving device containing high-purity hydrogen outside the system.
4. The refinery gas separation and recovery system according to claim 1, wherein the outlet end at the bottom of the absorption tower (6) is connected with an absorbent rich liquid (S-11) receiving device outside the system.
5. The refinery gas separation and recovery system according to claim 1, wherein the top outlet end of the absorption tower (6) is connected to a fuel gas pipe network outside the system.
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| CN112011357A (en) * | 2020-09-09 | 2020-12-01 | 盘锦浩业化工有限公司 | Refinery gas separation and recovery method and system |
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| CN112011357A (en) * | 2020-09-09 | 2020-12-01 | 盘锦浩业化工有限公司 | Refinery gas separation and recovery method and system |
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