CN112374459B - System and method for improving hydrogen recovery rate in styrene dehydrogenation tail gas of oil refinery - Google Patents
System and method for improving hydrogen recovery rate in styrene dehydrogenation tail gas of oil refinery Download PDFInfo
- Publication number
- CN112374459B CN112374459B CN202011346168.XA CN202011346168A CN112374459B CN 112374459 B CN112374459 B CN 112374459B CN 202011346168 A CN202011346168 A CN 202011346168A CN 112374459 B CN112374459 B CN 112374459B
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- swing adsorption
- pressure swing
- adsorption unit
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
- C01B2203/066—Integration with other chemical processes with fuel cells
Abstract
The invention discloses a system and a method for improving the recovery rate of hydrogen in styrene dehydrogenation tail gas of an oil refinery, and belongs to the technical field of hydrogen recovery of oil refineries. The technical scheme is as follows: the system comprises a hydrogen production pressure swing adsorption unit and a high-purity hydrogen pressure swing adsorption unit which are used in an oil refinery, wherein the hydrogen production pressure swing adsorption unit is provided with a hydrogen production shifted gas inlet, a styrene dehydrogenation tail gas inlet, a desorbed gas outlet and an industrial hydrogen outlet; the high-purity hydrogen pressure swing adsorption unit is provided with an air inlet, a desorption gas outlet and a high-purity hydrogen outlet, the air inlet of the high-purity hydrogen pressure swing adsorption unit is connected with an industrial hydrogen transmission pipe, and the desorption gas outlet of the high-purity hydrogen pressure swing adsorption unit is connected with the air inlet of the compressor. The invention realizes the coupling step recovery, achieves the aim of double high and produces the high-quality hydrogen for the hydrogen fuel cell required by the hydrogen energy industry.
Description
Technical Field
The invention relates to the technical field of hydrogen recovery in an oil refinery, in particular to a system and a method for improving the recovery rate of hydrogen in styrene dehydrogenation tail gas in the oil refinery.
Background
According to the development law of the hydrogen energy industry, industrial by-product hydrogen must be fully recovered and utilized at the present stage, and the hydrogen energy industry starts to enter the orbit, which is an objective requirement of the development of the hydrogen energy industry in China and is a specific requirement provided by numerous local governments such as Shandong, Guangdong and the like when the hydrogen energy industry is developed and planned.
1. Hydrogen production characteristics of oil refinery
Under the influence of upgrading of the quality of refined oil products, crude oil deterioration and other factors, a hydrogen production device is generally adopted by an oil refinery as an important source of hydrogen. The hydrogen production device of the oil refinery is generally provided with a PSA (pressure swing adsorption) unit for purifying hydrogen production conversion gas to produce industrial hydrogen used by the hydrogenation device of the oil refinery. Even if a non-PSA mode is used in the initial construction, the PSA purification production of industrial hydrogen is realized through the later-stage modification.
The hydrogen production device of the oil refinery is large in scale and generally reaches tens of thousands of standard cubic meters per hour, for example, by ten million tons of Qingdao oil refinery companies, the industrial hydrogen output capacities of 2 sets of PSA units of the hydrogen production device are respectively 3 ten thousand standard cubic meters per hour and 4 ten thousand standard cubic meters per hour, and the total amount reaches 7 ten thousand standard cubic meters per hour.
The refinery is generally provided with a hydrogen production device or a PSA unit, has large hydrogen production scale, and is characterized by hydrogen production in the refinery.
2. Ethylbenzene dehydrogenation and styrene production in oil refinery
The ethylbenzene and styrene unit in oil refinery uses catalytic cracking dry gas and benzene as raw material and is divided into ethylbenzene unit and styrene unit. The ethylbenzene unit is mainly used for carrying out alkylation reaction on a dilute ethylene component in catalytic cracking dry gas and liquid phase benzene in a reactor filled with a catalyst to generate ethylbenzene. The styrene unit mainly comprises ethylbenzene and generates the target product styrene through dehydrogenation reaction in a reactor.
In the reaction process of ethylbenzene dehydrogenation to produce styrene, the styrene dehydrogenation tail gas as a by-product contains about 85% (volume content, the same below) of hydrogen. Table 1 shows typical refinery celand refinery styrene unit styrene dehydrogenation tail gas composition (7 month average data 2020).
TABLE 1 styrene dehydrogenation tail gas composition
| Components | Composition, v% | Composition, w% |
| CH4 | 0.485 | 1.18 |
| C2H6 | 0.035 | 0.16 |
| C2H4 | 0.2724 | 1.16 |
| C3H6 | 0.02 | 0.13 |
| C3H8 | 0 | 0 |
| H2 | 85.41 | 26 |
| CO2 | 2.4 | 16.01 |
| O2 | 0.0775 | 0.38 |
| N2 | 10.33 | 44 |
| CO | 0.07 | 0.3 |
| C6 + | 0.9 | 10.68 |
| Total up to | 100 | 100 |
One million-ton oil refinery uses the reaction of dilute ethylene in catalytic dry gas and benzene to prepare ethylbenzene and then uses dehydrogenation to prepare styrene, and the flow rate of dehydrogenation tail gas can be up to 2000Nm3And h, the hydrogen is mostly used as a fuel of a heating furnace or recovered to be used in the oil refining hydrogenation process. For example, the average flow rate of the styrene dehydrogenation tail gas in the styrene device of Qingdao refining company is 2000Nm3At about 600kg/h, the hydrogen-containing tail gas is currently used as a fuel for the heating furnace.
The styrene dehydrogenation tail gas has the following characteristics: the pressure of the styrene dehydrogenation tail gas is extremely low, and is generally 0.04-0.05 MPaG. The industrial hydrogen is produced by the purification modes such as PSA after the tail gas is pressurized by a compressor with large compression ratio, but the impurities such as oxygen, nitrogen, heavy hydrocarbon and the like are high in content, so that no precedent for directly purifying and producing hydrogen for the hydrogen fuel cell with strict requirements on the impurity content exists, and research and development breakthrough in the aspect of technical economy is needed.
Therefore, in the catalytic cracking dry gas styrene production apparatus constructed in many refineries, the hydrogen-containing tail gas generated by ethylbenzene dehydrogenation is mostly recovered and used as fuel gas, and cannot be used with high value. Even if some refineries recover hydrogen by means of Pressure Swing Adsorption (PSA) and the like, the hydrogen recovery method is influenced by adverse factors such as low tail gas pressure, complex impurity composition, small scale and the like, and the high recovery rate, high quality and high yield cannot be realized in the aspects of recovery rate, recovery purity and the like.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: the system and the method overcome the defects of the prior art, and the system and the method for improving the recovery rate of hydrogen in the styrene dehydrogenation tail gas of an oil refinery are provided.
The technical scheme of the invention is as follows:
on one hand, the invention provides a system for improving the recovery rate of hydrogen in styrene dehydrogenation tail gas of an oil refinery, which comprises a hydrogen production pressure swing adsorption unit and a high-purity hydrogen pressure swing adsorption unit, wherein the hydrogen production pressure swing adsorption unit is provided with a hydrogen production conversion gas inlet, a styrene dehydrogenation tail gas inlet, a desorption gas outlet and an industrial hydrogen outlet; the high-purity hydrogen pressure swing adsorption unit is provided with an air inlet, a desorption gas outlet and a high-purity hydrogen outlet, the air inlet of the high-purity hydrogen pressure swing adsorption unit is connected with an industrial hydrogen transmission pipe, and the desorption gas outlet of the high-purity hydrogen pressure swing adsorption unit is connected with the air inlet of the compressor.
Preferably, the air inlet of the compressor is connected with a buffer tank, a styrene dehydrogenation tail gas inlet and a desorption gas inlet are arranged on the buffer tank, and a desorption gas outlet of the high-purity hydrogen pressure swing adsorption unit is connected with a desorption gas inlet of the buffer tank.
On the other hand, the invention also provides a method for improving the recovery rate of hydrogen in the styrene dehydrogenation tail gas of the oil refinery by using the system, wherein the hydrogen production conversion gas of the oil refinery is introduced into the hydrogen production pressure swing adsorption unit from the hydrogen production conversion gas inlet, and meanwhile, the styrene dehydrogenation tail gas is added into the compressor for pressurization and is pressed into the hydrogen production pressure swing adsorption unit from the styrene dehydrogenation tail gas inlet; desorbed gas generated by the hydrogen production pressure swing adsorption unit is discharged into a fuel gas pipe network through a desorbed gas outlet, one part of generated industrial hydrogen enters an industrial hydrogen outlet pipe, and the other part of generated industrial hydrogen is transmitted into the high-purity hydrogen pressure swing adsorption unit through an industrial hydrogen transmission pipe; the desorbed gas generated by the high-purity hydrogen pressure swing adsorption unit is recycled to the compressor from the desorbed gas outlet for pressurization and is pressed into the hydrogen production pressure swing adsorption unit, and the generated high-purity hydrogen is discharged from the high-purity hydrogen outlet.
Compared with the prior art, the invention has the following beneficial effects:
1. the invention connects the high-purity hydrogen pressure swing adsorption unit with the same scale as the styrene dehydrogenation tail gas in series behind the existing hydrocarbon steam conversion hydrogen production pressure swing adsorption unit of the oil refinery, and through the coupling of the high-purity hydrogen pressure swing adsorption unit and the hydrogen production pressure swing adsorption unit, on one hand, the content of hydrogen in the inlet gas of the high-purity hydrogen pressure swing adsorption unit can be firstly improved through the hydrogen production pressure swing adsorption unit, and the hydrogen recovery rate, namely the outlet hydrogen yield, is improved under the same condition by utilizing the characteristic that the hydrogen content in the hydrogen-containing gas in the inlet gas of the pressure swing adsorption unit is higher, so that the hydrogen recovery rate of the styrene dehydrogenation tail gas is improved; on the other hand, the hydrogen production pressure swing adsorption unit with the scale far larger than that of the high-purity hydrogen pressure swing adsorption unit is introduced, and the hydrogen production pressure swing adsorption unit and the high-purity hydrogen pressure swing adsorption unit are purified twice to produce the high-quality hydrogen for the hydrogen fuel cell with extremely strict impurity content requirements, so that the contradiction that the recovery rate needs to be sacrificed when the purity is improved and the purity needs to be sacrificed when the recovery rate is improved in the pressure swing adsorption technology is solved.
2. The invention realizes 'dual purposes' by using the compressor as a desorption gas compressor of the high-purity hydrogen pressure swing adsorption unit and a styrene dehydrogenation tail gas compressor of the hydrogen production pressure swing adsorption unit, can reduce the power consumption of the device, reduce the number of equipment, facilitate the management and simultaneously solve the problem that the scale of the high-purity hydrogen pressure swing adsorption unit is small and is not enough to independently arrange the desorption gas compressor.
3. Generally, when the desorbed gas is separately subjected to cyclic adsorption in the hydrogen-making pressure swing adsorption unit or the high-purity hydrogen pressure swing adsorption unit, the concentration of hydrogen in the inlet gas of the pressure swing adsorption unit is reduced, and the hydrogen yield is further reduced. The invention returns the desorbed gas generated by the high-purity hydrogen pressure swing adsorption unit to the inlet of the hydrogen production pressure swing adsorption unit for 'cyclic adsorption', realizes the coupling of the two pressure swing adsorption units, thereby realizing the 'double high' recovery of low-pressure styrene dehydrogenation tail gas with high quality and high yield, and solving the problems of higher impurity content in the inlet gas and lower yield and lower purity caused by the common cyclic adsorption.
4. The buffer tank with reasonable volume is arranged, so that the problems of low air suction flow, unstable pressure, discontinuous air flow and the like are solved, and the normal operation of the compressor is met.
Drawings
FIG. 1 is a schematic diagram of the present invention.
Fig. 2 is a schematic structural view of comparative example 1.
Fig. 3 is a schematic structural view of comparative example 2.
Fig. 4 is a schematic structural view of comparative example 3.
Detailed Description
Comparative example 1
As shown in fig. 2, the oil refining byproduct hydrogen-producing shifted gas is directly introduced into the hydrogen-producing pressure swing adsorption unit, and the industrial hydrogen separated by the hydrogen-producing pressure swing adsorption unit enters the recycling process. The desorbed gas generated by the hydrogen production pressure swing adsorption unit directly enters a fuel gas pipe network of an oil refinery to be used as fuel of a heating furnace.
Flow Q of inlet converted gas of hydrogen production pressure swing adsorption unit1Hydrogen content alpha1Flow rate Q of styrene dehydrogenation tail gas2Hydrogen content alpha2(volume percentage, the same below), the hydrogen enters a hydrogen production pressure swing adsorption unit to carry out hydrogen purification to produce industrial hydrogen, and the hydrogen recovery rate of the hydrogen production pressure swing adsorption unit is beta1The flow rate of the industrial hydrogen generated by the hydrogen production pressure swing adsorption unit is Q1α1β1The flow rate of hydrogen in the generated desorption gas is Q1α1(1-β1)。
Taking a certain hydrogen production device of Qingdao refining company as an example, the flow Q1Is 60000 Nm3/h，α175%, beta1About 91%, with a recovery of industrial hydrogen flow of 40950 Nm3/h。
Comparative example 2
As shown in fig. 3, different from comparative example 1, a high purity hydrogen pressure swing adsorption unit using industrial hydrogen as a raw material gas is constructed in a suitable scale and connected in series with a hydrogen production pressure swing adsorption unit, and then the industrial hydrogen is purified by the high purity hydrogen pressure swing adsorption unit to produce high purity hydrogen. Because the desorption gas quantity of the high-purity hydrogen pressure swing adsorption unit is too small, the large-scale recovery is difficult to realize, and therefore the desorption gas generated by the two sets of pressure swing adsorption units is merged into a low-pressure desorption gas pipe network to be used as fuel of the hydrogen production converter.
The flow of the inlet styrene dehydrogenation tail gas of the hydrogen production pressure swing adsorption unit is Q2Hydrogen content alpha2The hydrogen recovery rate of the hydrogen production pressure swing adsorption unit is still beta 1, and the industrial hydrogen flow rate generated by the hydrogen production pressure swing adsorption unit and used for producing high-quality hydrogen is Q2α2β1(ii) a The hydrogen recovery rate of the high-purity hydrogen pressure swing adsorption unit is beta2The flow rate of high quality hydrogen is Q2α2β1β2The maximum total yield of hydrogen is beta based on the hydrogen amount in the styrene dehydrogenation tail gas entering from the gas inlet of the hydrogen production pressure swing adsorption unit1β2。
The high quality hydrogen production flow required by polypropylene plant of Qingdao refinery company is the cascade flow of comparative example 2, which is taken as an example and expressed as beta1=91%、β2In the case of =90%, the yield of high-quality hydrogen is 81.9%, and the flow rate of industrial hydrogen produced in the hydrogen production pressure swing adsorption unit is 1547 Nm3H, the flow rate of high-quality hydrogen produced by the high-purity hydrogen pressure swing adsorption unit is 1392.3 Nm3/h。
Comparative example 3
As shown in fig. 4, the low-pressure styrene dehydrogenation tail gas is pressurized by a large-compression-ratio compressor and directly enters a high-purity hydrogen pressure swing adsorption unit to produce high-quality hydrogen. If the pressure of the styrene dehydrogenation tail gas is sufficient, the compressor may not be used.
The flow rate of the low-pressure styrene dehydrogenation tail gas of comparative example 3 was Q2Hydrogen content alpha2The hydrogen recovery rate of the high-purity hydrogen pressure swing adsorption unit is beta2Then the flow of the high-quality hydrogen generated by the high-purity hydrogen pressure swing adsorption unit is Q2α2β2´。
According to the characteristics of the high-purity hydrogen pressure swing adsorption unit, the higher the content of hydrogen in the inlet gas is, the higher the hydrogen recovery rate, i.e., the hydrogen yield, under the same conditions is. For example, Qingdao refining styrene dehydrogenation tail gas pressure swing adsorption single-stage production of high-quality hydrogen, the hydrogen content in dehydrogenation tail gas is 85%, and the received gas contains trace oxygen and C4 +The yield of high-quality hydrogen produced by the pressure swing adsorption method can only reach 80-85 percent generally due to the influence of heavy hydrocarbon and other adverse factors.
Take ethylene dehydrogenation tail gas from Qingdao refinery as an example, Q2Is 2000Nm3/h，α285%, beta280-85% and recovering 1360-1445 Nm high-quality hydrogen flow3/h。
Example 1
As shown in fig. 1, the embodiment provides a system for increasing the recovery rate of hydrogen in styrene dehydrogenation tail gas of an oil refinery, which includes a hydrogen production pressure swing adsorption unit and a high-purity hydrogen pressure swing adsorption unit for the oil refinery, where the hydrogen production pressure swing adsorption unit is provided with a hydrogen production shifted gas inlet, a styrene dehydrogenation tail gas inlet, a desorbed gas outlet and an industrial hydrogen outlet, the styrene dehydrogenation tail gas inlet is connected with a compressor, the desorbed gas outlet is connected with a fuel gas pipe network, and the industrial hydrogen outlet is connected with an industrial hydrogen outlet pipe and an industrial hydrogen transmission pipe; the high-purity hydrogen pressure swing adsorption unit is provided with an air inlet, a desorption gas outlet and a high-purity hydrogen outlet, the air inlet of the high-purity hydrogen pressure swing adsorption unit is connected with an industrial hydrogen transmission pipe, and the desorption gas outlet of the high-purity hydrogen pressure swing adsorption unit is connected with the air inlet of the compressor.
Wherein, the hydrogen production pressure swing adsorption unit and the high-purity hydrogen pressure swing adsorption unit are existing process equipment, and the specific structures are not repeated.
The method for improving the hydrogen recovery rate in the styrene dehydrogenation tail gas of the oil refinery by using the system comprises the following steps: introducing hydrogen production conversion gas of an oil refinery into the hydrogen production pressure swing adsorption unit from a hydrogen production conversion gas inlet, adding styrene dehydrogenation tail gas into a compressor for pressurization, and pressing the styrene dehydrogenation tail gas into the hydrogen production pressure swing adsorption unit from a styrene dehydrogenation tail gas inlet; desorbed gas generated by the hydrogen production pressure swing adsorption unit is discharged into a fuel gas pipe network through a desorbed gas outlet, one part of generated industrial hydrogen enters an industrial hydrogen outlet pipe, and the other part of generated industrial hydrogen is transmitted into the high-purity hydrogen pressure swing adsorption unit through an industrial hydrogen transmission pipe; the desorbed gas generated by the high-purity hydrogen pressure swing adsorption unit is recycled to the compressor from the desorbed gas outlet for pressurization and is pressed into the hydrogen production pressure swing adsorption unit, and the generated high-purity hydrogen is discharged from the high-purity hydrogen outlet.
Hydrogen purity alpha of styrene dehydrogenation tail gas285 percent higher than the purity alpha of hydrogen in the shift gas175% of styrene dehydrogenation tail gas flow rate Q2Is 2000Nm3H, flow rate of the converted gas Q1Is 60000 Nm3/h。
Before styrene dehydrogenation tail gas is not mixed in the inlet gas of the hydrogen production pressure swing adsorption unit, the hydrogen recovery rate beta of the hydrogen production pressure swing adsorption unit191% by weight, mixed with styrene dehydrogenation tail gas, and then produced into hydrogen pressure swing adsorption unitHydrogen recovery is set to beta1And'. Because the hydrogen content of the styrene dehydrogenation tail gas is higher than that of the conversion gas, after the styrene dehydrogenation tail gas is mixed, the hydrogen recovery rate, namely the hydrogen yield of the outlet under the same condition is higher by utilizing the characteristic that the hydrogen content of the hydrogen-containing gas in the inlet gas of the pressure swing adsorption unit is higher after the styrene dehydrogenation tail gas is mixed, and the hydrogen recovery rate beta of the hydrogen production pressure swing adsorption unit1´＞β1。
Similarly, the content of hydrogen in the desorbed gas generated by the high-purity hydrogen pressure swing adsorption unit is 99 percent, the desorbed gas is introduced into the air inlet of the compressor and is mixed with the styrene dehydrogenation tail gas with the hydrogen purity of 85 percent, the hydrogen concentration of the air inlet of the compressor and the styrene dehydrogenation tail gas inlet of the hydrogen production pressure swing adsorption unit is improved, the hydrogen recovery rate of the hydrogen production pressure swing adsorption unit is further improved, and the beta value is increased1´＞β1Degree of the disease. But due to Q1≫Q2Or the flow Q of the desorption gas generated by the high-purity hydrogen pressure swing adsorption unit3Thus, in combination, β1´≈β1。
The inlet gas of the high-purity hydrogen pressure swing adsorption unit is industrial hydrogen with the hydrogen purity of 99.9 percent, and the calculated hydrogen recovery rate beta of the high-purity hydrogen pressure swing adsorption unit290 percent, the content of hydrogen in the desorbed gas generated by the high-purity hydrogen pressure swing adsorption unit is alpha3About 99%.
Taking Qingdao refinery as an example, the yield of dehydrogenation tail gas of high-quality hydrogen to styrene when the dehydrogenation tail gas is not circularly adsorbed is 81.9 percent, and the calculation formula of the total yield of hydrogen after circular adsorption is beta1β2+（1-β2）β1β2+ … … =0.91 × 0.9+ (1-0.9) × 0.91 × 0.9=90%, high purity hydrogen flow 1530Nm3/h。
Compared with the process for producing high-quality hydrogen in the comparative example 3, the yield of the process is 5-10% higher than that of the process for producing high-quality hydrogen in the comparative example 3; the yield of high-quality hydrogen (and the total yield of hydrogen) is the same as 81.9% in the flow for producing high-quality hydrogen in comparative example 2, but the total yield of hydrogen is higher by about 8 percentage points, which is the highest in all the flows.
In this example, the flow of comparative example 3 was conducted to recover 85-170Nm more high-quality hydrogen3H; compared with the flow of the comparative example 2, the industrial hydrogen 153 is recoveredNm3The/h is reduced to 135 tons/year. Meanwhile, the investment and operation cost or hydrogen loss of gas treatment steps or links such as deoxidation, dehydration, heavy hydrocarbon removal and the like are saved, and the cost reduction and the efficiency improvement effects are obvious.
The flow rate of industrial hydrogen generated by the hydrogen production pressure swing adsorption unit is 1700 Nm correspondingly by taking the styrene dehydrogenation tail gas as the raw material3H, depending on the amount of high quality hydrogen product required, when the industrial hydrogen flow required for the high purity hydrogen pressure swing adsorption unit is above 1700 Nm3During the reaction, industrial hydrogen can be supplemented into the gas inlet of the high-purity hydrogen pressure swing adsorption unit so as to ensure the amount of the produced high-quality hydrogen; when the flow of industrial hydrogen needed by the high-purity hydrogen pressure swing adsorption unit is lower than 1700 Nm3At/h, a portion of the industrial hydrogen can be diverted for other uses.
Flow Q of desorbed gas generated by high-purity hydrogen pressure swing adsorption unit3About 170Nm3A compressor is independently added for pressurization and is discharged to a hydrogen pipe network, and the shaft power of the compressor is about 32 kW; low pressure styrene dehydrogenation off-gas flow Q2Is 2000Nm3The shaft power of the low-pressure styrene dehydrogenation tail gas compressor is about 299 kW; coupling the low-pressure styrene dehydrogenation tail gas with desorption gas generated by a high-purity hydrogen pressure swing adsorption unit, wherein the flow rate is 2170Nm3The desorbed gas reabsorption compressor shaft power was about 327 kW. Therefore, the compressor is combined into one and has two functions, the power consumption of the device can be reduced, the number of equipment is reduced, and the management is convenient.
Example 2
On the basis of embodiment 1, the air inlet of the compressor is connected with a buffer tank, a styrene dehydrogenation tail gas inlet and a desorption gas inlet are arranged on the buffer tank, and a desorption gas outlet of the high-purity hydrogen pressure swing adsorption unit is connected with a desorption gas inlet of the buffer tank. Through setting up reasonable volumetric buffer tank, overcome and know the flow of breathing in low and unstable, the discontinuous scheduling problem of tolerance of pressure, satisfy the normal operating of compressor.
Although the present invention has been described in detail by referring to the drawings in connection with the preferred embodiments, the present invention is not limited thereto. Various equivalent modifications or substitutions can be made on the embodiments of the present invention by those skilled in the art without departing from the spirit and scope of the present invention, and these modifications or substitutions are within the scope of the present invention/any person skilled in the art can easily conceive of the changes or substitutions within the technical scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (3)
1. A system for improving the recovery rate of hydrogen in the styrene dehydrogenation tail gas of an oil refinery is characterized in that,
the device comprises a hydrogen production pressure swing adsorption unit and a high-purity hydrogen pressure swing adsorption unit which are used in an oil refinery, wherein the hydrogen production pressure swing adsorption unit is provided with a hydrogen production conversion gas inlet, a styrene dehydrogenation tail gas inlet, a desorption gas outlet and an industrial hydrogen outlet;
the high-purity hydrogen pressure swing adsorption unit is provided with an air inlet, a desorption gas outlet and a high-purity hydrogen outlet, the air inlet of the high-purity hydrogen pressure swing adsorption unit is connected with an industrial hydrogen transmission pipe, and the desorption gas outlet of the high-purity hydrogen pressure swing adsorption unit is connected with the air inlet of the compressor.
2. The system for improving hydrogen recovery rate in styrene dehydrogenation tail gas in an oil refinery according to claim 1, wherein the air inlet of the compressor is connected with a buffer tank, the buffer tank is provided with a styrene dehydrogenation tail gas inlet and a desorption gas inlet, and a desorption gas outlet of the high-purity hydrogen pressure swing adsorption unit is connected with a desorption gas inlet of the buffer tank.
3. The method for improving the recovery rate of hydrogen in the styrene dehydrogenation tail gas of the oil refinery by using the system as claimed in claim 1 or 2, characterized in that the hydrogen production conversion gas of the oil refinery is introduced into the hydrogen production pressure swing adsorption unit from a hydrogen production conversion gas inlet, and simultaneously the styrene dehydrogenation tail gas is added into a compressor for pressurization and is pressed into the hydrogen production pressure swing adsorption unit from a styrene dehydrogenation tail gas inlet; desorbed gas generated by the hydrogen production pressure swing adsorption unit is discharged into a fuel gas pipe network through a desorbed gas outlet, one part of generated industrial hydrogen enters an industrial hydrogen outlet pipe, and the other part of generated industrial hydrogen is transmitted into the high-purity hydrogen pressure swing adsorption unit through an industrial hydrogen transmission pipe; the desorbed gas generated by the high-purity hydrogen pressure swing adsorption unit is recycled to the compressor from the desorbed gas outlet for pressurization and is pressed into the hydrogen production pressure swing adsorption unit, and the generated high-purity hydrogen is discharged from the high-purity hydrogen outlet.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011346168.XA CN112374459B (en) | 2020-11-26 | 2020-11-26 | System and method for improving hydrogen recovery rate in styrene dehydrogenation tail gas of oil refinery |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011346168.XA CN112374459B (en) | 2020-11-26 | 2020-11-26 | System and method for improving hydrogen recovery rate in styrene dehydrogenation tail gas of oil refinery |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112374459A CN112374459A (en) | 2021-02-19 |
| CN112374459B true CN112374459B (en) | 2022-06-03 |
Family
ID=74587849
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011346168.XA Active CN112374459B (en) | 2020-11-26 | 2020-11-26 | System and method for improving hydrogen recovery rate in styrene dehydrogenation tail gas of oil refinery |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112374459B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115253595A (en) * | 2022-08-16 | 2022-11-01 | 瑞必科净化设备（上海）有限公司 | System for purifying hydrogen with backflow through two-stage pressure swing adsorption, method for purifying hydrogen and application |
| CN115321484A (en) * | 2022-08-16 | 2022-11-11 | 瑞必科净化设备（上海）有限公司 | System for purifying hydrogen by two-stage compression and adsorption, method for purifying hydrogen and application |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1832901A (en) * | 2003-07-25 | 2006-09-13 | 沙特阿拉伯石油公司 | Hydrogen purification system |
| CN101260017A (en) * | 2008-04-01 | 2008-09-10 | 新疆新峰股份有限公司 | Pressure-change absorption separation method for ethylene and hydrogen from refining plant dry gas |
| CN101371966A (en) * | 2007-08-23 | 2009-02-25 | 四川省达科特化工科技有限公司 | Pressure-swing adsorption novel art for recovering ethylene and hydrogen from dry gas of oil-extraction plant |
| CN210332179U (en) * | 2019-06-26 | 2020-04-17 | 山东齐旺达石油化工有限公司 | System for obtaining by-product hydrogen by pressure swing adsorption method in ethylene preparation process |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8303930B2 (en) * | 2009-05-18 | 2012-11-06 | American Air Liquide, Inc. | Processes for the recovery of high purity hydrogen and high purity carbon dioxide |
-
2020
- 2020-11-26 CN CN202011346168.XA patent/CN112374459B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1832901A (en) * | 2003-07-25 | 2006-09-13 | 沙特阿拉伯石油公司 | Hydrogen purification system |
| CN101371966A (en) * | 2007-08-23 | 2009-02-25 | 四川省达科特化工科技有限公司 | Pressure-swing adsorption novel art for recovering ethylene and hydrogen from dry gas of oil-extraction plant |
| CN101260017A (en) * | 2008-04-01 | 2008-09-10 | 新疆新峰股份有限公司 | Pressure-change absorption separation method for ethylene and hydrogen from refining plant dry gas |
| CN210332179U (en) * | 2019-06-26 | 2020-04-17 | 山东齐旺达石油化工有限公司 | System for obtaining by-product hydrogen by pressure swing adsorption method in ethylene preparation process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN112374459A (en) | 2021-02-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100453447C (en) | Technological method of purifying hydrogen of hydrogen enriched gas source | |
| CN105948046B (en) | A kind of method for being recycled without stripping gas and producing pure hydrogen and pure carbon monoxide simultaneously that gasifies | |
| CN112374459B (en) | System and method for improving hydrogen recovery rate in styrene dehydrogenation tail gas of oil refinery | |
| CN110563538B (en) | Propylene gas catalytic deoxidation reaction device and deoxidation method | |
| CN101239702B (en) | High temperature coke oven crude gas hydrogen generating system device and technique | |
| CN113501496A (en) | Method and system for comprehensively recycling hydrogen-rich gas of iron and steel plant | |
| CN113200518A (en) | Method for recovering and purifying hydrogen from semi-coke tail gas | |
| CN213172233U (en) | Natural gas hydrogen production desulfurization system | |
| CN101033183A (en) | Process for producing sodium formate from carbonic oxide in synthesis ammonia raw material gas | |
| CN209854029U (en) | Device for preparing methanol from synthesis gas without conversion system | |
| CN104164263B (en) | A kind of coke(oven)gas methanation in presence of sulfur prepares the method for natural gas liquids | |
| CN101704714A (en) | Method for preparing synthesis gas after pure oxygen catalytic partial oxidation of purge gas in methanol synthesis loop to increase yield of methanol and device | |
| CN108046986B (en) | Recycling system and recycling method for effective gas in coal-to-ethylene glycol process | |
| CN111689469A (en) | Process for preparing high-purity hydrogen by adopting palladium alloy membrane purification | |
| CN216377479U (en) | Plasma reforming distributed natural gas hydrogen production device | |
| CN103992198B (en) | A kind of take coke-oven gas as the technique of raw material production benzene | |
| CN109847555B (en) | Device and method for recovering multiple gases in catalytic dry gas based on hydrate method | |
| CN213231512U (en) | Natural gas hydrogen production medium temperature shift system | |
| CN213326721U (en) | Natural gas hydrogen production product purification system | |
| CN211921378U (en) | System for steel mill tail gas comprehensive utilization system ethanol | |
| CN116478012A (en) | Method for preparing methanol by efficiently recycling carbon dioxide with low carbon emission | |
| CN109422243B (en) | Method for recovering tail hydrogen of disproportionation and transalkylation device | |
| CN216303284U (en) | Coke oven gas synthetic ammonia system | |
| CN1508064A (en) | Method for preparing high-purity nitrogen gas | |
| CN220642594U (en) | Novel methanol hydrogen production device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information | ||
| CB02 | Change of applicant information |
Address after: 100020 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Applicant after: CHINA PETROLEUM & CHEMICAL Corp. Applicant after: SINOPEC QINGDAO REFINING CHEMICAL Corp.,Ltd. Applicant after: Shandong Sanwei Chemical Group Co.,Ltd. Address before: 100020 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Applicant before: CHINA PETROLEUM & CHEMICAL Corp. Applicant before: SINOPEC QINGDAO REFINING CHEMICAL Corp.,Ltd. Applicant before: SHANDONG SUNWAY PETROCHEMICAL ENGINEERING Co.,Ltd. |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant |