CN210278704U - Refinery plant industrial tail gas comprehensive utilization system - Google Patents
Refinery plant industrial tail gas comprehensive utilization system Download PDFInfo
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- CN210278704U CN210278704U CN201920740122.2U CN201920740122U CN210278704U CN 210278704 U CN210278704 U CN 210278704U CN 201920740122 U CN201920740122 U CN 201920740122U CN 210278704 U CN210278704 U CN 210278704U
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- 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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The utility model belongs to the environmental protection field especially relates to a refinery plant industrial tail gas comprehensive utilization system, and this system includes: a first pressure swing adsorption apparatus; a carbon dioxide conveying pipeline connected with a desorbed gas outlet of the first pressure swing adsorption equipment; a desulfurization unit; the second pressure swing adsorption equipment is connected with a desulfurization gas outlet of the desulfurization equipment; a low heating value fuel gas conveying pipeline connected with a desorption gas outlet of the second pressure swing adsorption equipment; the third pressure swing adsorption equipment is respectively connected with the unadsorbed gas outlet of the first pressure swing adsorption equipment and the unadsorbed gas outlet of the second pressure swing adsorption equipment; a fuel gas conveying pipeline for the reformer, which is connected with a desorption gas outlet of the third pressure swing adsorption equipment; the fourth pressure swing adsorption equipment is connected with the unadsorbed gas outlet of the third pressure swing adsorption equipment; and the hydrogen conveying pipeline is connected with the unadsorbed gas outlet of the fourth pressure swing adsorption equipment. The system provided by the utility model can turn into the product gas of high added value with refinery plant industry tail gas.
Description
Technical Field
The utility model belongs to the environmental protection field especially relates to a refinery plant industrial tail gas comprehensive utilization system.
Background
At present, the social economy of China is rapidly developing, and the industry of China is gradually getting stronger. In the production and manufacturing process of each industry, a large amount of organic waste gas is discharged, and the organic waste gas discharge of industries such as petrochemical industry, printing and dyeing and the like is particularly serious. Therefore, advanced new technology must be adopted to treat the organic waste gas well so as to relieve the pressure in the aspect of environmental protection and realize the real solution of the air pollution problem.
Along with the rapid development of the petrochemical industry, the problem of treating the industrial tail gas of the refinery plant becomes very severe, and how to treat the industrial tail gas of the refinery plant in an economic and environment-friendly way becomes a new research hotspot in the field of the petrochemical industry.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model aims at providing a refinery industrial tail gas integrated utilization system, the utility model provides a system can turn into the product gas of high added value with refinery industrial tail gas.
The utility model provides a refinery industrial tail gas comprehensive utilization system, include:
the first pressure swing adsorption equipment is connected with the gas outlet end of the hydrogen production PSA desorption gas conveying pipeline;
a carbon dioxide conveying pipeline connected with a desorbed gas outlet of the first pressure swing adsorption equipment;
the desulfurization equipment is respectively connected with the gas outlet end of the styrene alkylation tail gas conveying pipeline, the gas outlet end of the gas cabinet recycling dry gas conveying pipeline and the gas outlet end of the RDS tail gas conveying pipeline;
the second pressure swing adsorption equipment is connected with a desulfurization gas outlet of the desulfurization equipment;
a low heating value fuel gas conveying pipeline connected with a desorbed gas outlet of the second pressure swing adsorption equipment;
the third pressure swing adsorption equipment is respectively connected with the unadsorbed gas outlet of the first pressure swing adsorption equipment and the unadsorbed gas outlet of the second pressure swing adsorption equipment;
a fuel gas conveying pipeline for the reformer, which is connected with a desorbed gas outlet of the third pressure swing adsorption equipment;
the fourth pressure swing adsorption equipment is connected with the unadsorbed gas outlet of the third pressure swing adsorption equipment;
and the hydrogen conveying pipeline is connected with the unadsorbed gas outlet of the fourth pressure swing adsorption equipment.
Preferably, the forward gas outlet of the first pressure swing adsorption equipment is connected with a fuel gas conveying pipeline for the reformer.
Preferably, the system further comprises a first gas-liquid separation device arranged between the gas outlet end of the hydrogen production PSA desorption gas conveying pipeline and the first pressure swing adsorption device, the inlet of the first gas-liquid separation device is connected with the gas outlet end of the hydrogen production PSA desorption gas conveying pipeline, and the gas phase outlet of the first gas-liquid separation device is connected with the inlet of the first pressure swing adsorption device.
Preferably, the system further comprises a raw material gas compression device arranged between the gas outlet end of the hydrogen production PSA desorption gas conveying pipeline and the first gas-liquid separation device, an inlet of the raw material gas compression device is connected with the gas outlet end of the hydrogen production PSA desorption gas conveying pipeline, and an outlet of the raw material gas compression device is connected with an inlet of the first gas-liquid separation device.
Preferably, the system further comprises a second gas-liquid separation device arranged between the desulfurization device and the second pressure swing adsorption device, an inlet of the second gas-liquid separation device is connected with a desulfurization gas outlet of the desulfurization device, and a gas phase outlet of the second gas-liquid separation device is connected with an inlet of the second pressure swing adsorption device.
Preferably, the system further comprises a hydrogen compression device arranged between the fourth pressure swing adsorption device and the hydrogen conveying pipeline, an inlet of the hydrogen compression device is connected with an unadsorbed gas outlet of the fourth pressure swing adsorption device, and an outlet of the hydrogen compression device is connected with the hydrogen conveying pipeline.
Compared with the prior art, the utility model provides a refinery plant industrial tail gas comprehensive utilization system. The utility model provides a system includes: the first pressure swing adsorption equipment is connected with the gas outlet end of the hydrogen production PSA desorption gas conveying pipeline; a carbon dioxide conveying pipeline connected with a desorbed gas outlet of the first pressure swing adsorption equipment; the desulfurization equipment is respectively connected with the gas outlet end of the styrene alkylation tail gas conveying pipeline, the gas outlet end of the gas cabinet recycling dry gas conveying pipeline and the gas outlet end of the RDS tail gas conveying pipeline; the second pressure swing adsorption equipment is connected with a desulfurization gas outlet of the desulfurization equipment; a low heating value fuel gas conveying pipeline connected with a desorbed gas outlet of the second pressure swing adsorption equipment; the third pressure swing adsorption equipment is respectively connected with the unadsorbed gas outlet of the first pressure swing adsorption equipment and the unadsorbed gas outlet of the second pressure swing adsorption equipment; a fuel gas conveying pipeline for the reformer, which is connected with a desorbed gas outlet of the third pressure swing adsorption equipment; the fourth pressure swing adsorption equipment is connected with the unadsorbed gas outlet of the third pressure swing adsorption equipment; and the hydrogen conveying pipeline is connected with the unadsorbed gas outlet of the fourth pressure swing adsorption equipment. In the utility model, hydrogen produced by refinery plantsPSA desorption gas is conveyed to a first pressure swing adsorption device through a pipeline to produce most of CO in the PSA desorption gas2Selectively adsorbing with adsorbent filled in the first pressure swing adsorption equipment, desorbing by reverse discharge, evacuating, etc. to obtain high purity CO2The desorbed gas is discharged from a desorbed gas outlet and then enters a carbon dioxide conveying pipeline; the unadsorbed semi-purified gas is discharged through the unadsorbed gas outlet of the first pressure swing adsorption apparatus. The utility model discloses in, styrene hydrocarbylation tail gas, the gas holder that the refinery produced retrieve dry gas and RDS tail gas and pass through desorption H among the pipeline transport sweetener2S, discharging the obtained desulfurization gas from the desulfurization gas outlet, and allowing the obtained desulfurization gas to enter a second pressure swing adsorption device to obtain part of CH in the desulfurization gas4、CO2The components of C2, C3, C4+ and the like are selectively adsorbed by an adsorbent filled in second pressure swing adsorption equipment, desorption is realized through steps of reverse release, evacuation and the like, and desorbed gas obtained by desorption is discharged from a desorbed gas outlet and then enters a low-calorific-value fuel gas conveying pipeline; the unadsorbed semi-purified gas is discharged through the unadsorbed gas outlet of the second pressure swing adsorption apparatus. The utility model discloses in, from first pressure swing adsorption equipment and second pressure swing adsorption equipment's the not absorption gas export exhaust half purification gas gets into third pressure swing adsorption equipment, remaining CO in the half purification gas2Part of nitrogen, methane, CO and the like are selectively adsorbed by an adsorbent filled in third pressure swing adsorption equipment, desorption is realized through the steps of reverse release, evacuation and the like, and desorbed gas obtained by desorption is discharged from a desorbed gas outlet and then enters a fuel gas conveying pipeline for the converter; the unadsorbed semi-purified gas is discharged through an unadsorbed gas outlet of the third pressure swing adsorption equipment and then enters the fourth pressure swing adsorption equipment, various impurities carried in the gas are selectively adsorbed and removed by an adsorbent filled in the fourth pressure swing adsorption equipment, and the unadsorbed purified gas (high-purity hydrogen) is discharged through the unadsorbed gas outlet and enters a hydrogen conveying pipeline. The system provided by the utility model can respectively obtain fuel gas, high-purity hydrogen and high-purity carbon dioxide for low heat value fuel gas, reformer through carrying out substep recovery, separation, purification to refinery industrial tail gas, wherein hydrogen, low heat value fuel gas, reformer fuel gas can be directly for the reformer fuel gasThe carbon dioxide can be transported to the refinery for utilization, and can be transported to the surrounding areas for sale, thereby having good environmental benefit, economic benefit and social benefit.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required to be used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a flow chart of a comprehensive utilization system for industrial tail gas of a refinery plant provided by an embodiment of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
The utility model provides a refinery industrial tail gas comprehensive utilization system, include:
the first pressure swing adsorption equipment is connected with the gas outlet end of the hydrogen production PSA desorption gas conveying pipeline;
a carbon dioxide conveying pipeline connected with a desorbed gas outlet of the first pressure swing adsorption equipment;
the desulfurization equipment is respectively connected with the gas outlet end of the styrene alkylation tail gas conveying pipeline, the gas outlet end of the gas cabinet recycling dry gas conveying pipeline and the gas outlet end of the RDS tail gas conveying pipeline;
the second pressure swing adsorption equipment is connected with a desulfurization gas outlet of the desulfurization equipment;
a low heating value fuel gas conveying pipeline connected with a desorbed gas outlet of the second pressure swing adsorption equipment;
the third pressure swing adsorption equipment is respectively connected with the unadsorbed gas outlet of the first pressure swing adsorption equipment and the unadsorbed gas outlet of the second pressure swing adsorption equipment;
a fuel gas conveying pipeline for the reformer, which is connected with a desorbed gas outlet of the third pressure swing adsorption equipment;
the fourth pressure swing adsorption equipment is connected with the unadsorbed gas outlet of the third pressure swing adsorption equipment;
and the hydrogen conveying pipeline is connected with the unadsorbed gas outlet of the fourth pressure swing adsorption equipment.
Referring to fig. 1, fig. 1 is a flow chart of a comprehensive utilization system for industrial tail gas of a refinery plant provided by an embodiment of the present invention.
The utility model provides a refinery industrial tail gas comprehensive utilization system includes first pressure swing adsorption equipment, second pressure swing adsorption equipment, third pressure swing adsorption equipment, fourth pressure swing adsorption equipment, sweetener, carbon dioxide pipeline, low calorific value fuel gas pipeline, fuel gas pipeline and hydrogen pipeline for the reformer. The first pressure swing adsorption equipment is provided with an inlet, a desorbed gas outlet, an unadsorbed gas outlet and a downstream gas outlet, and the inlet of the first pressure swing adsorption equipment is connected with the gas outlet end of the hydrogen production PSA desorbed gas conveying pipeline and used for performing pressure swing adsorption treatment on the hydrogen production PSA desorbed gas. In the utility model, the hydrogen production PSA desorption gas refers to the low-pressure exhaust tail gas generated by the hydrogen production pressure swing adsorption device in the regeneration process of the adsorbent. When the system is in operation, hydrogen production PSA desorption gas generated by the refinery plant is conveyed to the first pressure swing adsorption equipment through a hydrogen production PSA desorption gas conveying pipeline, and most CO in the hydrogen production PSA desorption gas2Selectively adsorbing with adsorbent filled in the first pressure swing adsorption equipment, desorbing by reverse discharge, evacuating, etc. to obtain high purity CO2Discharging from a stripping gas outlet; the unadsorbed semi-purified gas is discharged through the unadsorbed gas outlet of the first pressure swing adsorption apparatus.
In the utility model, the inlet end of the carbon dioxide conveying pipeline and the first pressure swing adsorption equipment are separatedThe gas suction outlet is connected and used for conveying high-purity CO obtained by desorption of the first pressure swing adsorption equipment2。
In an embodiment of the present invention, the system further comprises a first gas-liquid separation device, the first gas-liquid separation device is provided with an inlet, a gas phase outlet and a liquid phase outlet. The utility model discloses in, first gas-liquid separation equipment sets up hydrogen manufacturing PSA desorption gas pipeline give vent to anger the end with between the first pressure swing adsorption equipment, first gas-liquid separation equipment's import with hydrogen manufacturing PSA desorption gas pipeline gives vent to anger the end and is connected, first gas-liquid separation equipment's gaseous phase export with first pressure swing adsorption equipment's import is connected for get rid of the liquid material that probably carries in the hydrogen manufacturing PSA desorption gas.
In an embodiment of the present invention, the system further comprises a raw material gas compression device, the raw material gas compression device is provided with an inlet and an outlet. The utility model discloses in, feed gas compression equipment is in hydrogen manufacturing PSA desorption gas pipeline give vent to anger the end with between the first gas-liquid separation equipment, feed gas compression equipment's import with hydrogen manufacturing PSA desorption gas pipeline gives vent to anger the end and is connected, feed gas compression equipment's export with first gas-liquid separation equipment's import is connected for the hydrogen manufacturing PSA desorption gas that gets into the system pressurizes, makes it reach the pressure requirement.
The utility model discloses in, sweetener is provided with air inlet and desulfurization gas export, sweetener's import is given vent to anger end and RDS tail gas pipeline and is given vent to anger the end and be connected with styrene hydrocarbylation tail gas pipeline respectively and give vent to anger end, gas holder recovery dry gas pipeline and RDS tail gas pipeline end of giving vent to anger for H among the styrene hydrocarbylation tail gas of desorption, gas holder recovery dry gas and RDS tail gas2And S. In the present invention, the styrene alkylation tail gas refers to the exhaust gas generated in the operation process of the styrene device; the dry gas recovered by the gas holder is the torch gas collected by the torch collecting holder; the RDS tail gas refers to the tail gas discharged in the running process of an atmospheric heavy oil hydrotreatment (RDS) device.
In the utility model, the second pressure swing adsorptionThe equipment is provided with an inlet, a desorption gas outlet and an unadsorbed gas outlet, and the inlet of the second pressure swing adsorption equipment is connected with the desulfurization gas outlet of the desulfurization equipment and is used for carrying out pressure swing adsorption treatment on the desulfurization gas. When the system is in operation, after the desulfurized gas enters the second pressure swing adsorption equipment, part of CH in the desulfurized gas4、CO2C2, C3, C4+ and other components are selectively adsorbed by an adsorbent filled in second pressure swing adsorption equipment, desorption is realized through steps of reverse release, evacuation and the like, and low-calorific-value fuel gas obtained by desorption is discharged from a desorption gas outlet; the unadsorbed semi-purified gas is discharged through the unadsorbed gas outlet of the second pressure swing adsorption apparatus.
In one embodiment of the present invention, the system further comprises a second gas-liquid separation device, the second gas-liquid separation device is provided with an inlet, a gas phase outlet and a liquid phase outlet. The utility model discloses in, second gas-liquid separation sets up sweetener with between the second pressure swing adsorption equipment, the import of second gas-liquid separation equipment with sweetener gas outlet of sweetener is connected, second gas-liquid separation equipment's gaseous phase export with second pressure swing adsorption equipment's import is connected for get rid of the liquid material that probably carries in the sweetener gas.
The utility model discloses in, the inlet end of low heat value fuel gas pipeline with the desorption gas export of second pressure swing adsorption equipment is connected for carry the low heat value fuel gas that second pressure swing adsorption equipment desorption obtained.
The utility model discloses in, third pressure swing adsorption equipment is provided with import, desorption gas export and unadsorbed gas export, third pressure swing adsorption equipment's import respectively with first pressure swing adsorption equipment's unadsorbed gas export and second pressure swing adsorption equipment's unadsorbed gas export is connected for the unadsorbed gas (also called half purified gas) to first pressure swing adsorption equipment and second pressure swing adsorption equipment carries out the pressure swing adsorption and handles. When the system is in operation, after the semi-purified gas discharged from the unadsorbed gas outlets of the first pressure swing adsorption equipment and the second pressure swing adsorption equipment enters the third pressure swing adsorption equipment, the residual CO in the semi-purified gas2Section (1)Selectively adsorbing nitrogen, methane, CO and the like by an adsorbent filled in third pressure swing adsorption equipment, then realizing desorption through steps of reverse discharge, evacuation and the like, and discharging fuel gas for the converter obtained by desorption from a desorption gas outlet; the unadsorbed semi-purified gas is discharged through the unadsorbed gas outlet of the third pressure swing adsorption unit.
The utility model discloses in, reformer fuel gas pipeline's inlet end with the desorption gas export of third pressure swing adsorption equipment is connected for carry the reformer fuel gas that third pressure swing adsorption equipment desorption obtained.
In an embodiment provided by the present invention, the forward-exhaust gas outlet of the first pressure swing adsorption equipment is connected to the fuel gas conveying pipeline for the reformer, i.e. the forward-exhaust gas after the adsorption of the first pressure swing adsorption equipment is finished is also used as the fuel gas for the reformer, and is desorbed by the third pressure swing adsorption equipment and conveyed by the fuel gas mixture for the reformer.
The utility model discloses in, fourth pressure swing adsorption equipment is provided with import, desorption gas export and unadsorbed gas export, fourth pressure swing adsorption equipment's import with third pressure swing adsorption equipment's unadsorbed gas export is connected for carry out the pressure swing adsorption to third pressure swing adsorption equipment's unadsorbed gas (also called half purified gas) and handle. When the system is in operation, after the semi-purified gas discharged from the unadsorbed gas outlet of the third pressure swing adsorption device enters the fourth pressure swing adsorption device, various impurities carried in the gas are selectively adsorbed and removed by the adsorbent filled in the fourth pressure swing adsorption device, and the unadsorbed purified gas (high-purity hydrogen) is discharged from the unadsorbed gas outlet.
The utility model discloses in, hydrogen pipeline's inlet end with fourth pressure swing adsorption equipment's unadsorbed gas export is connected for carry fourth pressure swing adsorption equipment exhaust high-purity hydrogen.
In one embodiment, the system further comprises a hydrogen compression device, wherein the hydrogen compression device is provided with an inlet and an outlet. The utility model discloses in, hydrogen compression equipment sets up fourth pressure swing adsorption device with hydrogen compression equipment between the hydrogen pipeline, hydrogen compression equipment's import with fourth pressure swing adsorption equipment's unadsorbed gas export is connected, hydrogen compression equipment's export with hydrogen pipeline is connected for handle exhaust high-purity hydrogen to fourth pressure swing adsorption equipment and compress, make it reach the pressure requirement.
The utility model provides a system is through carrying out substep to refinery industry tail gas and retrieving, separation, purification, purifying, can obtain low heat value fuel gas, fuel gas for the converter, high-purity hydrogen and high-purity carbon dioxide respectively, and wherein hydrogen, low heat value fuel gas, fuel gas for the converter can directly be carried and return the refinery utilization, and carbon dioxide can be transported to peripheral area and sell, has good environmental benefit, economic benefits and social.
For the sake of clarity, the following examples are given in detail.
Example 1
The comprehensive utilization system for industrial tail gas of a refinery plant provided by the embodiment as shown in fig. 1 comprises: the system comprises a first pressure swing adsorption device (PSA-1), a second pressure swing adsorption device (PSA-2), a third pressure swing adsorption device (PSA-3), a fourth pressure swing adsorption device (PSA-4), a raw material gas compression device, a desulfurization device, a hydrogen compression device, a first gas-liquid separation device, a second gas-liquid separation device, a carbon dioxide conveying pipeline, a low-calorific-value fuel gas conveying pipeline, a fuel gas conveying pipeline for a reformer and a hydrogen conveying pipeline, wherein the connection relation among the devices is introduced in the above, and the description is omitted.
The operation process of the refinery industrial tail gas comprehensive utilization system provided by the embodiment is as follows:
conveying the styrene alkylation tail gas, the dry gas recovered by the gas holder and the RDS tail gas to desulfurization equipment through pipelines to remove H in the gas2S, the desulfurized gas enters a second gas-liquid separation device, liquid substances possibly carried by the desulfurized gas are removed in the second gas-liquid separation device, and then the desulfurized gas enters PSA-2 at the temperature of 40 ℃ and 0.42MPa after being measured by a flow meter, wherein part of CH in the gas4、CO2C2, C3, C4+ and the like are adsorbed by the adsorbentAnd then, the unadsorbed semi-purified gas enters the PSA-3 after the pressure of the unadsorbed gas outlet of the PSA-2 is regulated by a regulating valve, and impurities of the unadsorbed semi-purified gas are further removed. The gas adsorbed by the adsorbent is desorbed through the steps of reverse discharge, evacuation and the like, the desorbed gas obtained by desorption enters a low-heat-value fuel gas conveying pipeline, and meanwhile, the adsorbent is regenerated and enters the next cycle of adsorption circulation.
The hydrogen production PSA desorption gas is input into a raw material gas compression device through a pipeline under normal pressure, the raw material gas is pressurized to about 0.43MPa in the raw material gas compression device, then liquid substances possibly carried in the hydrogen production PSA desorption gas are removed through a first gas-liquid separation device, the liquid substances are metered by a flowmeter and enter PSA-1, and most CO in the gas enters PSA-1 at the moment2Selectively adsorbing by adsorbent loaded in PSA-1, mixing unadsorbed semi-purified gas with semi-purified gas discharged from PSA-2 after pressure regulation at unadsorbed gas outlet of PSA-1 by regulating valve, and introducing into PSA-3. CO adsorbed by the adsorbent2The desorption is realized through the steps of reverse discharge, evacuation and the like, and the high-purity CO obtained by desorption2And (4) entering a carbon dioxide conveying pipeline, simultaneously regenerating the adsorbent, and entering the next period of adsorption circulation. After the adsorption is finished, partial cis-gassing and excessive CO exist2As fuel gas for the converter, the fuel gas is mixed with desorption gas obtained from PSA-3 and enters a fuel gas conveying pipeline for the converter after pressure stabilization.
The semi-purified gases discharged from the non-adsorbed gas outlets of PSA-1 and PSA-2 are mixed and then enter PSA-3, wherein the residual CO in the semi-purified gases2Part of nitrogen, methane, CO and the like are selectively adsorbed by the adsorbent filled in the PSA-3, the unadsorbed gas enters the PSA-4, various impurities carried in the gas are adsorbed and removed in the PSA-4, and high-purity H is obtained at the unadsorbed gas outlet of the PSA-42Said high purity H2Compressed to 2.4MPa by hydrogen compression equipment and then enters a hydrogen conveying pipeline. The gas absorbed by the adsorbent filled in PSA-3 is desorbed through the steps of reverse discharge, evacuation and the like, the desorbed gas obtained by desorption enters a fuel gas conveying pipeline for the converter, and meanwhile, the adsorbent is regenerated and enters the adsorption cycle of the next period.
In this embodiment, each pressure swing adsorption apparatus includes a plurality of adsorbers, each adsorber sequentially undergoes steps of adsorption (a), pressure Equalization (EiD), reverse release (D), evacuation (V), evacuation flushing (VP), pressure Equalization (EiR), final pressure increase (FR) at different times, and the steps of each adsorber are staggered, so as to achieve the purposes of continuous feeding and product obtaining.
In this embodiment, the information of the raw gas and the product gas is shown in tables 1 to 7:
TABLE 1 tail gas (raw gas) of styrene alkylation
TABLE 2 Dry gas recovery from gas holder (raw gas)
TABLE 3 PSA Desorption gas for Hydrogen production (raw gas)
Table 4 RDS tail gas (raw gas)
TABLE 5 Hydrogen (product gas)
| Content (wt.) | 100％(v) |
| Temperature of | 40℃ |
| Pressure of | 2.4MPa |
| Flow rate | 16095Nm3/h |
| Recovery rate | ≥96％ |
TABLE 6 Fuel gas (product gas)
TABLE 7 carbon dioxide (product gas)
| Content (wt.) | ≥98.4％(v) |
| Temperature of | 40℃ |
| Pressure of | ≥0.005MPa |
| Flow rate | 3617Nm3/h |
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (6)
1. The utility model provides a refinery industrial tail gas comprehensive utilization system which characterized in that includes:
the first pressure swing adsorption equipment is connected with the gas outlet end of the hydrogen production PSA desorption gas conveying pipeline;
a carbon dioxide conveying pipeline connected with a desorbed gas outlet of the first pressure swing adsorption equipment;
the desulfurization equipment is respectively connected with the gas outlet end of the styrene alkylation tail gas conveying pipeline, the gas outlet end of the gas cabinet recycling dry gas conveying pipeline and the gas outlet end of the RDS tail gas conveying pipeline;
the second pressure swing adsorption equipment is connected with a desulfurization gas outlet of the desulfurization equipment;
a low heating value fuel gas conveying pipeline connected with a desorbed gas outlet of the second pressure swing adsorption equipment;
the third pressure swing adsorption equipment is respectively connected with the unadsorbed gas outlet of the first pressure swing adsorption equipment and the unadsorbed gas outlet of the second pressure swing adsorption equipment;
a fuel gas conveying pipeline for the reformer, which is connected with a desorbed gas outlet of the third pressure swing adsorption equipment;
the fourth pressure swing adsorption equipment is connected with the unadsorbed gas outlet of the third pressure swing adsorption equipment;
and the hydrogen conveying pipeline is connected with the unadsorbed gas outlet of the fourth pressure swing adsorption equipment.
2. The system of claim 1, wherein the cis gas outlet of the first pressure swing adsorption unit is connected to the fuel gas delivery pipeline for the reformer.
3. The refinery industrial tail gas comprehensive utilization system according to claim 1, further comprising a first gas-liquid separation device arranged between the hydrogen production PSA desorption gas conveying pipeline gas outlet end and the first pressure swing adsorption device, wherein an inlet of the first gas-liquid separation device is connected with the hydrogen production PSA desorption gas conveying pipeline gas outlet end, and a gas phase outlet of the first gas-liquid separation device is connected with an inlet of the first pressure swing adsorption device.
4. The refinery industrial tail gas comprehensive utilization system according to claim 3, further comprising a raw material gas compression device arranged between the hydrogen production PSA desorption gas conveying pipeline gas outlet end and the first gas-liquid separation device, wherein an inlet of the raw material gas compression device is connected with the hydrogen production PSA desorption gas conveying pipeline gas outlet end, and an outlet of the raw material gas compression device is connected with an inlet of the first gas-liquid separation device.
5. The system of claim 1, further comprising a second gas-liquid separation device disposed between the desulfurization device and the second pressure swing adsorption device, wherein an inlet of the second gas-liquid separation device is connected to the desulfurized gas outlet of the desulfurization device, and a gas phase outlet of the second gas-liquid separation device is connected to the inlet of the second pressure swing adsorption device.
6. The system of claim 1, further comprising a hydrogen compression device disposed between the fourth pressure swing adsorption unit and the hydrogen transportation pipeline, wherein an inlet of the hydrogen compression device is connected to an unadsorbed gas outlet of the fourth pressure swing adsorption unit, and an outlet of the hydrogen compression device is connected to the hydrogen transportation pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920740122.2U CN210278704U (en) | 2019-05-22 | 2019-05-22 | Refinery plant industrial tail gas comprehensive utilization system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920740122.2U CN210278704U (en) | 2019-05-22 | 2019-05-22 | Refinery plant industrial tail gas comprehensive utilization system |
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| CN210278704U true CN210278704U (en) | 2020-04-10 |
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