CN211677036U - Device for reducing effective gas content of PSA desorption gas - Google Patents
Device for reducing effective gas content of PSA desorption gas Download PDFInfo
- Publication number
- CN211677036U CN211677036U CN202020166101.7U CN202020166101U CN211677036U CN 211677036 U CN211677036 U CN 211677036U CN 202020166101 U CN202020166101 U CN 202020166101U CN 211677036 U CN211677036 U CN 211677036U
- Authority
- CN
- China
- Prior art keywords
- gas
- adsorption tower
- section
- outlet
- psa
- 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
Abstract
The utility model relates to a PSA device, concretely relates to reduce PSA desorption gas effective gas content's device. The system comprises a raw material gas storage tank, a gas-liquid separator, a first section of adsorption tower, a second section of adsorption tower and a hydrogen production adsorption tower which are sequentially connected through pipelines, wherein a temperature controller is additionally arranged on a pipeline at the bottom inlet of the first section of adsorption tower, and the temperature controller is provided with a shell pass for gas to pass through and a tube pass for desalted water to pass through. The utility model discloses add temperature controller on the pipeline of one section adsorption tower entry, temperature controller is equipped with the shell side that supplies gas to pass through and the pipe side that supplies the demineralized water to pass through. The temperature controller controls the inlet temperature of the first section of the adsorption tower to be 28-32 ℃, thereby prolonging the cycle time and reducing the waste of effective components in the desorption gas.
Description
Technical Field
The utility model relates to a PSA device, concretely relates to reduce PSA desorption gas effective gas content's device.
Background
Matched engineering PSA-CO of ethylene glycol device2/CO/H2The device comprises three sections, wherein the first section is pressure swing adsorption to remove CO2PSA-CO of2A second stage of PSA-CO purification of CO and a third stage of H production2PSA-H of2And (5) working sections. The main source of PSA stripper gas is PSA-CO2Reverse-venting and evacuation of gas and PSA-H2The vacuum is pumped. In general, the effective gas in the analysis gas is CO + H2The content of (B) is between 35 and 50 percent.
In the prior art, due to the influence of various factors, the content of effective gas in the analysis gas after the device is started is higher and can exceed 50 percent sometimes. This portion of the process gas is generally treated as fuel, resulting in a large waste of active ingredients. Therefore, in the PSA process, it has been a research focus of the skilled person to control the effective gas content in the PSA process gas to a low level.
Of course, the stripping gas may also continue to serve as the feed gas for hydrogen production, but this adds an additional process step. The cost is increased compared to reducing the effective gas content of the PSA stripping gas. If the content of effective gas in the PSA gas can be directly reduced, the cost is greatly reduced.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a reduce device of effective gas content in PSA analysis gas, the device has solved the high problem of effective gas content of current PSA analysis gas, reduces the waste of effective constituent in the analysis gas, has reduced manufacturing cost.
Reduce PSA analysis gas effective gas content's device, including looping through feed gas storage jar, vapour and liquid separator, one section adsorption tower, two-stage process adsorption tower, the hydrogen manufacturing adsorption tower that the pipeline links to each other, add temperature controller on the pipeline of one section adsorption tower bottom entry, temperature controller is equipped with the shell side that supplies gas to pass through and supplies the tube side that the desalinized water passes through.
Wherein:
the temperature controller is provided with a desalted water inlet, a desalted water outlet, a gas inlet and a gas outlet, the gas inlet is connected with the top of the gas-liquid separator, and the gas outlet is connected with the bottom of the first section of adsorption tower.
The temperature controller adopts a shell-and-tube heat exchanger, the pressure of a tube side and the pressure of a shell side are both 1-1.5MPa, and the heat exchange area is 300-2。
The bottom of the first section of adsorption tower is connected with a desorption gas tank. Preferably, the bottom of the first section of adsorption tower is connected with a desorption gas tank through a desorption gas buffer tank.
And the top of the first section of adsorption tower is provided with an adsorption gas outlet which is connected with the top of the second section of adsorption tower.
The two-stage adsorption tower top be equipped with crude hydrogen export, crude hydrogen exit linkage hydrogen manufacturing adsorption tower top, two-stage adsorption tower bottom is equipped with the carbon monoxide export, the carbon monoxide export links to each other with carbon monoxide storage jar.
The top of the hydrogen production adsorption tower is provided with a hydrogen outlet which is connected with a hydrogen storage tank, the top of the hydrogen production adsorption tower is also provided with a hydrogen production desorption gas outlet, and the hydrogen production desorption gas outlet is connected with the top of the first section of adsorption tower.
The gas-liquid separator is connected with the liquid collecting tank.
The utility model discloses add temperature controller on the pipeline of one section adsorption tower entry, temperature controller is equipped with the shell side that supplies gas to pass through and the pipe side that supplies the demineralized water to pass through. The temperature controller controls the inlet temperature of the first section of the adsorption tower to be 28-32 ℃, thereby prolonging the cycle time and reducing the waste of effective components in the desorption gas. The temperature at the inlet of the first-stage adsorption tower is generally above 35 ℃ and can reach above 40 ℃ at most.
The working process is as follows:
(1) the raw material gas firstly enters PSA-CO2Section, mainly for CO removal2And small amounts of other impurities. PSA-CO2The working section mainly comprises an adsorption tower and a desorption gas tank. The raw material enters a temperature controller after being separated by a gas-liquid separator from a raw material gas storage tank, the temperature is controlled to be 28-32 ℃ by the temperature controller, then the raw material is introduced from an inlet at the bottom of a first section of adsorption tower, and the desorption of partial impurities is obtained at an outlet of the first section of adsorption towerCarbon gas. And sending the obtained semi-product decarbonized gas to a PSA-CO working section, and sending the desorption gas into a desorption gas tank. PSA-CO2The workshop section can be additionally provided with a desorption gas buffer tank. The analysis gas firstly enters the analysis gas buffer tank, and then enters the analysis gas tank after being buffered.
(2) After the semi-product decarbonization gas enters a PSA-CO working section, H2、N2、O2And part of CH4Discharging the impurities from the top of the two-stage adsorption tower to obtain crude hydrogen as PSA-H2Raw materials of the working section. And CO and a small amount of impurities are sent out from the bottom of the two-section adsorption tower through the steps of reverse discharging and evacuating, and enter a product carbon monoxide storage tank.
(3) Crude hydrogen from PSA-CO section goes to PSA-H2And after impurities are removed from the hydrogen production adsorption tower at the working section, a qualified hydrogen product is obtained at a hydrogen outlet at the top of the hydrogen production adsorption tower. The gas discharged by vacuumizing, namely the desorption gas of the hydrogen production adsorption tower enters the top of the first section of the adsorption tower for recycling.
Compared with the prior art, the utility model discloses following beneficial effect has:
the utility model discloses add temperature controller on the pipeline of one section adsorption tower entry, temperature controller is equipped with the shell side that supplies gas to pass through and the pipe side that supplies the demineralized water to pass through. The utility model discloses an add temperature controller, with the entry temperature control of one section adsorption column bottom at 28-32 ℃, prolonged cycle time, reduce the waste of effective constituent in the desorption gas. The utility model provides a problem that current PSA analytic gas active ingredient content is high, reduced effective gaseous content in the PSA analytic gas, then greatly reduced manufacturing cost.
Drawings
FIG. 1 is a schematic structural view of the present invention;
in the figure: 1. a feed gas storage tank; 2. a gas-liquid separator; 3. a first stage adsorption tower; 4. an adsorbed gas outlet; 5. a crude hydrogen outlet; 6. a hydrogen production desorption gas outlet; 7. a hydrogen outlet; 8. a hydrogen storage tank; 9. a hydrogen production adsorption tower; 10. a second section of adsorption tower; 11. a carbon monoxide outlet; 12. a carbon monoxide storage tank; 13. a desorption gas buffer tank; 14. resolving the gas tank; 15. a desalted water outlet; 16. a temperature controller; 17. a gas outlet; 18. a gas inlet; 19. a desalted water inlet; 20. a liquid collecting tank.
Detailed Description
The present invention will be further described with reference to the following examples.
Example 1
As shown in fig. 1, the device for reducing the effective gas content of PSA desorption gas comprises a raw gas storage tank 1, a gas-liquid separator 2, a first-stage adsorption tower 3, a second-stage adsorption tower 10 and a hydrogen production adsorption tower 9 which are sequentially connected through a pipeline, wherein a temperature controller 16 is additionally arranged on the pipeline at the inlet at the bottom of the first-stage adsorption tower 3, and the temperature controller 16 is provided with a shell side through which gas passes and a tube side through which desalted water passes.
Wherein:
the temperature controller 16 is provided with a desalted water inlet 19, a desalted water outlet 15, a gas inlet 18 and a gas outlet 17, the gas inlet 18 is connected with the top of the gas-liquid separator 2, and the gas outlet 17 is connected with the bottom of the first section of the adsorption tower 3.
The temperature controller 16 adopts a shell-and-tube heat exchanger, the pressure of the tube side and the pressure of the shell side are both 1-1.5MPa, and the heat exchange area is 300-2。
The bottom of the first section of the adsorption tower 3 is connected with a desorption gas tank 14, and preferably, the bottom of the first section of the adsorption tower 3 is connected with the desorption gas tank 14 through a desorption gas buffer tank 13.
The top of the first section of the adsorption tower 3 is provided with an adsorption gas outlet 4, and the adsorption gas outlet 4 is connected with the top of the second section of the adsorption tower 10.
The top of the second-stage adsorption tower 10 is provided with a crude hydrogen outlet 5, the crude hydrogen outlet 5 is connected with the top of the hydrogen production adsorption tower 9, the bottom of the second-stage adsorption tower 10 is provided with a carbon monoxide outlet 11, and the carbon monoxide outlet 11 is connected with a carbon monoxide storage tank 12.
The top of the hydrogen production adsorption tower 9 is provided with a hydrogen outlet 7, the hydrogen outlet 7 is connected with a hydrogen storage tank 8, the top of the hydrogen production adsorption tower 9 is also provided with a hydrogen production desorption gas outlet 6, and the hydrogen production desorption gas outlet 6 is connected with the top of the first section of adsorption tower 3.
The gas-liquid separator 2 is connected to the catch tank 20.
The working process is as follows:
(1) first, the raw material gas is firstInto PSA-CO2Section, mainly for CO removal2And small amounts of other impurities. PSA-CO2The working section mainly comprises an adsorption tower and a desorption gas tank 14. The raw material enters a liquid collecting tank 20 after being separated by a gas-liquid separator 2 from a raw material gas storage tank 1, the raw material gas enters a temperature controller 16 from a gas inlet 18, the temperature is controlled to be 28-32 ℃ by the temperature controller 16, the raw material gas is discharged from a gas outlet 17 and then is introduced from an inlet at the bottom of a first section of adsorption tower 3, and decarbonization gas with partial impurities removed is obtained at an adsorption gas outlet 4 of the first section of adsorption tower 3. The obtained semi-product decarbonization gas is sent to a PSA-CO working section, enters a two-section adsorption tower 10, and the desorption gas enters a desorption gas tank 14. PSA-CO2The workshop section can be additionally provided with a desorption gas buffer tank 13. The desorption gas firstly enters the desorption gas buffer tank 13, and then enters the desorption gas tank 14 after being buffered.
(2) After the semi-product decarbonization gas enters a PSA-CO working section, H2、N2、O2And part of CH4Discharging the impurities from a crude hydrogen outlet 5 at the top of the two-stage adsorption tower 10 to obtain crude hydrogen serving as PSA-H2Raw materials of the working section. CO and a small amount of impurities are sent out from a carbon monoxide outlet 11 at the bottom of the two-section adsorption tower 10 through a reverse discharging and evacuating step and enter a product carbon monoxide storage tank 12.
(3) Crude hydrogen from PSA-CO section goes to PSA-H2After impurities are removed from the hydrogen production adsorption tower 9 at the working section, a qualified hydrogen product is obtained at a hydrogen outlet 7 at the top of the hydrogen production adsorption tower 9 and enters a hydrogen storage tank 8. The gas discharged by vacuumizing, namely the desorption gas of the hydrogen production adsorption tower 9 enters the top of the first section of the adsorption tower 3 for recycling through a pipeline from a hydrogen production desorption gas outlet 6.
The utility model provides a CO + H in raw material gas2The content is 90.25%, the purity of the obtained CO is 98.2-98.5%, and the obtained H2The purity is 99.0-99.9%.
The process data before the implementation of the utility model is shown in the following table 1, and the process data after the implementation is shown in the following table 2.
TABLE 1 data sheet before implementation
| Serial number | Raw material gas flow rate Nm3/h | CO + H in the analysis gas2Content% | First stage inlet temperature | Total adsorption time min |
| 1 | 25012 | 41.2 | 40 | 31 |
| 2 | 24625 | 39.3 | 39 | 32 |
| 3 | 23976 | 50.5 | 37 | 31.5 |
TABLE 2 data sheet after implementation
| Serial number | Raw material gas flow rate Nm3/h | CO + H in the analysis gas2Content% | First stage inlet temperature | Total adsorption time min |
| 1 | 24783 | 23.8 | 32 | 35 |
| 2 | 24498 | 25.1 | 30 | 38 |
| 3 | 24037 | 24.0 | 29 | 36.5 |
As can be seen from the above, the effective component CO + H in the analysis gas of the present invention2The content is obviously reduced.
Claims (9)
1. The utility model provides a reduce device of PSA analysis gas effective gas content, includes feed gas storage jar (1), vapour and liquid separator (2), one section adsorption tower (3), two-stage adsorption tower (10), hydrogen manufacturing adsorption tower (9) that loop through the pipeline links to each other, its characterized in that: a temperature controller (16) is additionally arranged on a pipeline at the inlet at the bottom of the first section of the adsorption tower (3), and the temperature controller (16) is provided with a shell pass through which gas passes and a tube pass through which desalted water passes.
2. The apparatus of claim 1, wherein the effective gas content of the PSA stripping gas is reduced by: the temperature controller (16) is provided with a desalted water inlet (19), a desalted water outlet (15), a gas inlet (18) and a gas outlet (17), the gas inlet (18) is connected with the top of the gas-liquid separator (2), and the gas outlet (17) is connected with the bottom of the first section of adsorption tower (3).
3. The apparatus for reducing the effective gas content of PSA stripping gas according to claim 1 or 2, characterized in that: the temperature controller (16) adopts a shell-and-tube heat exchanger, the pressure of the tube side and the shell side are both 1-1.5MPa, and the heat exchange area is 300-2。
4. The apparatus of claim 1, wherein the effective gas content of the PSA stripping gas is reduced by: the bottom of the first section of the adsorption tower (3) is connected with a desorption gas tank (14).
5. The apparatus of claim 4, wherein the effective gas content of the PSA desorption gas is: the bottom of the first section of the adsorption tower (3) is connected with a desorption gas tank (14) through a desorption gas buffer tank (13).
6. The apparatus of claim 1, wherein the effective gas content of the PSA stripping gas is reduced by: the top of the first section of the adsorption tower (3) is provided with an adsorption gas outlet (4), and the adsorption gas outlet (4) is connected with the top of the second section of the adsorption tower (10).
7. The apparatus of claim 1, wherein the effective gas content of the PSA stripping gas is reduced by: the top of the second-stage adsorption tower (10) is provided with a crude hydrogen outlet (5), the crude hydrogen outlet (5) is connected with the top of the hydrogen production adsorption tower (9), the bottom of the second-stage adsorption tower (10) is provided with a carbon monoxide outlet (11), and the carbon monoxide outlet (11) is connected with a carbon monoxide storage tank (12).
8. The apparatus of claim 1, wherein the effective gas content of the PSA stripping gas is reduced by: the top of the hydrogen production adsorption tower (9) is provided with a hydrogen outlet (7), the hydrogen outlet (7) is connected with a hydrogen storage tank (8), the top of the hydrogen production adsorption tower (9) is also provided with a hydrogen production desorption gas outlet (6), and the hydrogen production desorption gas outlet (6) is connected with the top of the first section of adsorption tower (3).
9. The apparatus of claim 1, wherein the effective gas content of the PSA stripping gas is reduced by: the gas-liquid separator (2) is connected with the liquid collecting tank (20).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020166101.7U CN211677036U (en) | 2020-02-13 | 2020-02-13 | Device for reducing effective gas content of PSA desorption gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020166101.7U CN211677036U (en) | 2020-02-13 | 2020-02-13 | Device for reducing effective gas content of PSA desorption gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211677036U true CN211677036U (en) | 2020-10-16 |
Family
ID=72776930
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202020166101.7U Active CN211677036U (en) | 2020-02-13 | 2020-02-13 | Device for reducing effective gas content of PSA desorption gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211677036U (en) |
-
2020
- 2020-02-13 CN CN202020166101.7U patent/CN211677036U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101549856B (en) | Separation method of comprehensively recycled hydrogen and carbon monooxide from synthesis purge gas | |
| CN109126381B (en) | Method for removing carbon dioxide in industrial gas through pressure swing adsorption | |
| KR880000803B1 (en) | Separation process of mixed gas and apparatus thereof | |
| CN111871149B (en) | Two-stage pressure swing adsorption system for recovering adsorbed components and application method thereof | |
| CN102423601B (en) | Tail gas treatment device for cyclohexane oxidation system and treatment method thereof | |
| CN103521033A (en) | Method for purifying and reclaiming secondary gas in fire flood | |
| CN113350968A (en) | Hydrogen extraction device and process for recovering tail gas components by using synthetic hydrogen | |
| CN113200518A (en) | Method for recovering and purifying hydrogen from semi-coke tail gas | |
| CN114857856A (en) | System and method for synchronously recovering nitrogen and carbon dioxide from boiler flue gas | |
| CN103055660B (en) | Method and system for treating cyclohexane oxidation tail gas | |
| CN211677036U (en) | Device for reducing effective gas content of PSA desorption gas | |
| CN103395744B (en) | Rapid hydrogen extraction driving method for pressure swing adsorption hydrogen production system | |
| CN111174530A (en) | Method and device for separating and purifying krypton and xenon | |
| CN212881746U (en) | Two-stage pressure swing adsorption system for recovering adsorbed components | |
| CN214243809U (en) | System for producing hydrogen and coproducing LNG (liquefied Natural gas) by using raw gas | |
| CN110822924B (en) | Cold rolling bell-type furnace tail gas recycling method and system | |
| CN206033231U (en) | High -purity nitrogen generator of pressure swing adsorption | |
| CN216472232U (en) | Energy-saving process system for purifying hydrogen from raw coke oven gas with low-concentration hydrogen | |
| CN205137496U (en) | System for gas boiler and gas turbine flue gas are used for gas to transfer storage | |
| CN111151097A (en) | Pressure swing adsorption purification recovery device and process for polypropylene SPG process tail gas | |
| CN215208468U (en) | Hydrogen purification system in chlor-alkali tail gas | |
| CN211799850U (en) | Pressure swing adsorption purification recovery device for polypropylene SPG process tail gas | |
| CN210278704U (en) | Refinery plant industrial tail gas comprehensive utilization system | |
| CN220424946U (en) | Carbon dioxide purification device | |
| CN216785724U (en) | Device for recovering hydrogen from acid-making waste gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |