CN216604669U - Device for recovering high-purity hydrogen by utilizing styrene dehydrogenation tail gas - Google Patents
Device for recovering high-purity hydrogen by utilizing styrene dehydrogenation tail gas Download PDFInfo
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- CN216604669U CN216604669U CN202220102054.9U CN202220102054U CN216604669U CN 216604669 U CN216604669 U CN 216604669U CN 202220102054 U CN202220102054 U CN 202220102054U CN 216604669 U CN216604669 U CN 216604669U
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- tail gas
- hydrogen
- swing adsorption
- pressure swing
- dehydrogenation tail
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Abstract
The utility model discloses a device for recovering high-purity hydrogen by utilizing styrene dehydrogenation tail gas, in particular to the technical field of hydrogen recovery, which comprises a condenser, wherein the condenser is connected with a dehydrogenation tail gas absorption tower, the dehydrogenation tail gas absorption tower is connected with a hydrogen compressor, the hydrogen compressor is connected with a liquid separation tank, the liquid separation tank is connected with a pressure swing adsorption tower, and the pressure swing adsorption tower is connected with a hydrogen recovery tank. Has good economic benefit.
Description
Technical Field
The utility model relates to the technical field of hydrogen recovery, in particular to a device for recovering high-purity hydrogen by utilizing styrene dehydrogenation tail gas.
Background
In the prior art of a styrene device, dehydrogenation tail gas from a crude styrene exhaust condenser directly enters a tail gas absorption tower, aromatic hydrocarbon is absorbed by directly contacting with an absorbent, after the aromatic hydrocarbon is recovered, the dehydrogenation tail gas leaving the absorption tower is directly sent to a fuel gas tank of a steam superheater as fuel, in the mode, a compressor is adopted to control the pressure of a dehydrogenation reaction system, the dehydrogenation tail gas after compression and absorption enters the fuel gas tank, and natural gas is used as supplementary fuel. When the dehydrogenation reaction system is adjusted and operated, the dehydrogenation tail gas and the steam superheater are high in operation relevance, the influence range is large, once the compressor is abnormally shut down, the fuel gas addition of the steam superheater is directly influenced, accidents such as shutdown of the superheater due to interlocking of low fuel gas pressure and the like can be caused due to failure in timely treatment, and the dehydrogenation reaction system is rich in H2The dehydrogenation tail gas is used as fuel gas, which causes a great deal of resource waste.
SUMMERY OF THE UTILITY MODEL
In order to overcome the defects in the prior art, the utility model provides a device for recovering high-purity hydrogen by utilizing styrene dehydrogenation tail gas, wherein a hydrogen compressor and a pressure swing adsorption tower are arranged, the dehydrogenation tail gas is subjected to pressure boosting and then mixed with crude hydrogen to be subjected to pressure swing adsorption treatment, and a high-purity hydrogen product is separated.
In order to achieve the purpose, the utility model provides the following technical scheme: a device for recovering high-purity hydrogen by utilizing styrene dehydrogenation tail gas comprises a condenser, wherein the condenser is connected with a dehydrogenation tail gas absorption tower, dehydrogenation tail gas from the condenser directly enters the dehydrogenation tail gas absorption tower, and aromatic hydrocarbon is adsorbed by directly contacting with circulating lean oil to recover the aromatic hydrocarbon;
the dehydrogenation tail gas absorption tower is connected with a hydrogen press, and the hydrogen press can pressurize dehydrogenation tail gas which is a byproduct of ethylbenzene dehydrogenation reaction in a styrene device;
the supercharger is connected with the liquid separation tank, and the supercharged tail gas is sent to the liquid separation tank for gas-liquid separation;
the liquid separation tank is connected with a pressure swing adsorption tower, a crude hydrogen inlet is connected on a pipeline at the front end of the pressure swing adsorption tower, gas phase after gas-liquid separation and byproduct crude hydrogen from the mixed carbon dioxide device are mixed and then enter the pressure swing adsorption tower for pressure swing adsorption, and under the sequential selective adsorption of various adsorbents, CO and CO in the gas phase are adsorbed2、CH4After impurities are adsorbed, the unadsorbed hydrogen flows out from the top of the tower and is used as a product to be sent to a hydrogen recovery tank, wherein H2Purity greater than 99.99% and pressure about 3.1 MPaG;
wherein, the pressure swing adsorption process of the pressure swing adsorption tower comprises the following steps: adsorption, five continuous pressure equalizing and reducing, sequential discharge, reverse discharge, flushing, five continuous pressure equalizing and increasing and final product pressure increasing;
ten pressure swing adsorption towers are arranged, and one of the ten adsorption towers is always in a feeding adsorption state;
the pressure swing adsorption tower is connected with a fuel gas tank, the adsorbed impurities are completely desorbed through the pressure swing adsorption tower, and desorbed gas is sent to the fuel gas tank to be further utilized as fuel.
The utility model has the technical effects and advantages that:
1. the device adopts styrene dehydrogenation tail gas and crude hydrogen as gas sources, wherein the content of hydrocarbons difficult to desorb is high and the gas components are complex, and a hydrogen compressor and a pressure swing adsorption tower are arranged to mix the pressurized tail gas and the crude hydrogen and then carry out pressure rise and drop and desorption for many times so as to separate out high-purity hydrogen with the content of more than 99.99 percent;
2. the residual desorption gas is reused as fuel, so that the energy consumption is greatly reduced, and even if the desorption gas is suddenly interrupted, the influence of the device on the operation of the steam superheater is obviously reduced;
3. simple structure, stable and reliable technology, long running period and low production cost.
Drawings
Fig. 1 is an overall schematic view of the present invention.
In the figure: 1. a condenser; 2. a dehydrogenation tail gas absorption tower; 3. a hydrogen press; 4. liquid separating tank; 5. a pressure swing adsorption tower; 6. a crude hydrogen gas inlet; 7. a hydrogen recovery tank; 8. a fuel gas tank.
Detailed Description
The preferred embodiments of the present invention will be described in conjunction with the accompanying drawings, and it will be understood that they are described herein for the purpose of illustration and explanation and not limitation.
Example (b):
the device adopts a 10-1-5PSA flushing process flow, namely, one of ten pressure swing adsorption towers 5 is always in a feeding adsorption state, and the adsorption and regeneration process comprises the steps of adsorption, continuous five-time pressure equalizing and reducing, sequential release, reverse release, flushing, continuous five-time pressure equalizing and increasing, final product pressure increasing and the like;
as shown in fig. 1, dehydrogenation tail gas from a crude styrene tail gas condenser 1 directly enters a dehydrogenation tail gas absorption tower 2, aromatic hydrocarbon is absorbed in the absorption tower through direct contact with circulating lean oil, after the aromatic hydrocarbon is recovered, the tail gas at the top of the dehydrogenation tail gas absorption tower 2 is pressurized to 3.2MPaG by a hydrogen compressor 3 and then sent to a liquid separation tank 4 at a PSA section for gas-liquid separation, and the gas phase and crude hydrogen gas (3.2MPaG) from mixed carbon dioxide are mixed together and enter a pressure swing adsorption tower 5 in an adsorption state for pressure swing adsorption and desorption;
under the sequential selective adsorption of a plurality of adsorbents, wherein CO and CO are contained2、CH4After the impurities are adsorbed, the unadsorbed hydrogen flows out from the top of the pressure swing adsorption tower 5 and is sent to a hydrogen recovery tank 7 as a high-purity hydrogen product, wherein H2Purity greater than 99.99% and pressure about 3.1 MPaG;
after the reverse releasing process of the pressure swing adsorption tower 5 is completely finished, in order to ensure that the adsorbent is completely regenerated, in the process, hydrogen from a forward releasing gas tank is used for flushing the adsorption bed against the adsorption direction so as to ensure that impurities in the adsorbent are completely desorbed, flushing desorption gas enters a desorption gas mixing tank, and the mixed desorption gas is sent to a fuel gas tank 8 to be reused as fuel.
The following is a material balance table in the embodiment of the device:
TABLE 1 Material balance Table
Claims (4)
1. The device for recycling high-purity hydrogen by utilizing the styrene dehydrogenation tail gas comprises a condenser (1) and is characterized in that the condenser (1) is connected with a dehydrogenation tail gas absorption tower (2), the dehydrogenation tail gas absorption tower (2) is connected with a hydrogen compressor (3), the hydrogen compressor (3) is connected with a liquid separation tank (4), the liquid separation tank (4) is connected with a pressure swing adsorption tower (5), and the pressure swing adsorption tower (5) is connected with a hydrogen recovery tank (7).
2. The apparatus for recovering high-purity hydrogen from styrene dehydrogenation tail gas according to claim 1, wherein the front end pipeline of the pressure swing adsorption tower (5) is connected with a crude hydrogen inlet (6).
3. The apparatus for recovering high-purity hydrogen from styrene dehydrogenation tail gas according to claim 1, wherein the pressure swing adsorption tower is further connected with a fuel gas tank (8).
4. The apparatus for recovering high-purity hydrogen gas from styrene dehydrogenation tail gas according to claim 1, wherein the pressure swing adsorption tower (5) is provided with ten.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220102054.9U CN216604669U (en) | 2022-01-16 | 2022-01-16 | Device for recovering high-purity hydrogen by utilizing styrene dehydrogenation tail gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202220102054.9U CN216604669U (en) | 2022-01-16 | 2022-01-16 | Device for recovering high-purity hydrogen by utilizing styrene dehydrogenation tail gas |
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| CN216604669U true CN216604669U (en) | 2022-05-27 |
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| CN202220102054.9U Active CN216604669U (en) | 2022-01-16 | 2022-01-16 | Device for recovering high-purity hydrogen by utilizing styrene dehydrogenation tail gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117018816A (en) * | 2023-05-15 | 2023-11-10 | 北京石油化工学院 | Recovery device for ethylbenzene dehydrogenation tail gas adsorption and desorption styrene and hydrogen |
| CN117018816B (en) * | 2023-05-15 | 2024-04-30 | 北京石油化工学院 | Recovery device for ethylbenzene dehydrogenation tail gas adsorption and desorption styrene and hydrogen |
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2022
- 2022-01-16 CN CN202220102054.9U patent/CN216604669U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117018816A (en) * | 2023-05-15 | 2023-11-10 | 北京石油化工学院 | Recovery device for ethylbenzene dehydrogenation tail gas adsorption and desorption styrene and hydrogen |
| CN117018816B (en) * | 2023-05-15 | 2024-04-30 | 北京石油化工学院 | Recovery device for ethylbenzene dehydrogenation tail gas adsorption and desorption styrene and hydrogen |
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