Temperature swing adsorption device for coke oven gas hydrogen extraction process

Abstract

The utility model belongs to the technical field of temperature swing adsorption equipment, and particularly relates to a temperature swing adsorption device for a coke oven gas hydrogen extraction process. Comprising a gas-liquid separator, the gas-liquid separator is respectively connected with a first adsorber and a second adsorber which are arranged in parallel, and the first adsorber and the second adsorber are respectively connected with an unadsorbed gas output pipeline; a hot blowing pipeline and a cold blowing pipeline which are connected to the first adsorption tower and the second adsorption tower are branched from the outlet end of the PSA desorption gas buffer tank, and a debenzolization regeneration heater is arranged on the hot blowing pipeline; the bottoms of the first adsorber and the second adsorber are respectively connected with a depressurization exhaust pipeline and a regeneration exhaust pipeline; and a debenzolization regeneration cooler is arranged on the regeneration exhaust pipeline. According to the device, by accurately controlling the opening and closing of each valve, the adsorption process and the regeneration process are alternately carried out, so that the hydrogen in the coke oven gas can be continuously and efficiently extracted.

Description

TECHNICAL FIELD

[0001] The utility model belongs to the technical field of temperature swing adsorption equipment, and particularly relates to a temperature swing adsorption device for a coke oven gas hydrogen extraction process. BACKGROUND

[0002] With the adjustment of energy structure and the increasing environmental protection requirements, the demand for hydrogen as a clean and efficient energy carrier is growing. Coke oven gas, as a byproduct of the steel industry, contains abundant hydrogen. Extracting hydrogen from coke oven gas not only realizes effective utilization of resources, but also reduces environmental pollution.

[0003] At present, in the coke oven gas hydrogen extraction process, the traditional adsorption device has some shortcomings. On the one hand, some devices cannot efficiently separate hydrogen from coke oven gas, resulting in low hydrogen extraction rate and failing to meet the growing industrial demand. On the other hand, the regeneration process of the adsorbent is complex and inefficient, resulting in high operating cost of the device. In addition, the traditional adsorption device can only operate singly in the adsorption and regeneration processes, i.e. one adsorber is adsorbing while the other is idle, which cannot realize continuous and efficient hydrogen extraction. This not only reduces the utilization rate of the device, but also limits the hydrogen extraction capacity.

[0004] Therefore, it is of great practical significance to develop an energy-saving temperature swing adsorption device that can realize continuous and stable hydrogen extraction. UTILITY MODEL CONTENTS

[0005] In view of the above shortcomings of the prior art, the utility model aims to provide a temperature swing adsorption device for a coke oven gas hydrogen extraction process, which realizes the alternation of adsorption and regeneration processes, thereby continuously and efficiently extracting hydrogen from coke oven gas. At the same time, by accurately controlling the opening and closing of each valve, the smooth progress of the adsorption and regeneration processes can be ensured, and the hydrogen extraction efficiency is improved.

[0006] The utility model is implemented by adopting the following technical solutions:

[0007] The temperature swing adsorption device for the coke oven gas hydrogen extraction process comprises a gas-liquid separator, a coke oven gas pipeline and a purge gas pipeline are connected to the gas inlet end of the gas-liquid separator, the gas outlet end of the gas-liquid separator is connected to the bottom of a first adsorber and a second adsorber through pipelines respectively, the first adsorption tower and the second adsorption tower are arranged in a parallel configuration, the top of the first adsorber and the second adsorber are connected to each other through pipelines, the top of the first adsorber and the second adsorber is connected to an unadsorbed gas external pipeline through pipelines respectively, and the output end of the unadsorbed gas external pipeline is connected to a PSA process;

[0008] The PSA desorption gas buffer tank is branched with a hot blow pipeline and a cold blow pipeline at its outlet end, the output ends of the hot blow pipeline and the cold blow pipeline are respectively connected to the top of the first adsorption tower and the second adsorption tower, and a benzene removal regeneration heater is arranged on the hot blow pipeline;

[0009] The bottoms of the first adsorber and the second adsorber are respectively connected with a pressure reduction exhaust pipeline and a regeneration exhaust pipeline, the output ends of the pressure reduction exhaust pipeline and the regeneration exhaust pipeline are connected with a PSA desorption gas mixing tank, and a benzene removal regeneration cooler is arranged on the regeneration exhaust pipeline.

[0010] 101A / B valves are respectively arranged on the pipelines connected with the bottoms of the first adsorber and the second adsorber and the gas-liquid separator.

[0011] 102A / B valves are respectively arranged on the pipelines leading to the unadsorbed gas export pipeline at the top of the first adsorber and the second adsorber;

[0012] 106A / B valves are arranged on the pipelines connected with the tops of the first adsorber and the second adsorber.

[0013] A 107 valve is arranged on the hot blow pipeline before the inlet of the benzene removal regeneration heater, and a 108 valve is arranged on the cold blow pipeline.

[0014] 104A / B valves are respectively arranged on the pipelines connecting the output ends of the hot blow pipeline and the cold blow pipeline to the tops of the first adsorber and the second adsorber.

[0015] 103A / B valves are respectively arranged on the pipelines leading to the pressure reduction exhaust pipeline at the bottoms of the first adsorber and the second adsorber.

[0016] 105A / B valves are respectively arranged on the pipelines leading to the regeneration exhaust pipeline at the bottoms of the first adsorber and the second adsorber.

[0017] A control system is further included, and the control system is electrically connected with each valve.

[0018] The temperature swing adsorption device for the hydrogen extraction process of coke oven gas mainly includes initial pressure increase, adsorption, pressure reduction, hot blow regeneration, cold blow regeneration and secondary pressure increase stages, realizes effective extraction of hydrogen in the coke oven gas, and realizes regeneration of the adsorbent through the temperature swing adsorption technology, and the working principle is as follows:

[0019] 1) Initial pressure increase: the 101A / B valves are opened through the control system, the purge gas enters the first adsorber or the second adsorber through the gas-liquid separator from the purge gas pipeline for initial pressure increase;

[0020] 2) Adsorption: after the pressure is raised, the coke oven gas from the coke oven gas pipeline enters the first adsorber or the second adsorber for adsorption through a gas-liquid separator, and the unadsorbed gas is discharged to an unadsorbed gas external delivery pipeline through 102A / B valves and finally enters a PSA process;

[0021] 3) Pressure reduction: when the first adsorber or the second adsorber is saturated after adsorption, the regeneration stage needs to be entered, at this time, 102A / B valves are closed, 103A / B valves are opened, and the gas in the adsorber is discharged to a PSA desorption gas mixing tank through a pressure reduction exhaust pipeline;

[0022] 4) Hot blow regeneration: after the pressure reduction is completed, 107 valves on a hot blow pipeline branched out from the outlet end of the PSA desorption gas buffer tank and 104A / B valves connecting the hot blow pipeline to the top of the first adsorber or the second adsorber are opened, the desorption gas in the hot blow pipeline is heated after passing through a benzene removal regeneration heater, enters the first adsorber or the second adsorber for hot blow regeneration, and the hot blown gas is discharged through 105A / B valves on a regeneration exhaust pipeline and is discharged into the PSA desorption gas mixing tank after being cooled by a benzene removal regeneration cooler;

[0023] 5) Cold blow regeneration: after the hot blow regeneration is completed, 107 valves are closed, 108 valves on a cold blow pipeline are opened, the desorption gas in the PSA desorption gas buffer tank enters the first adsorber or the second adsorber for cold blow through the cold blow pipeline, and the cold blown gas is also discharged through 105A / B valves on the regeneration exhaust pipeline and is discharged into the PSA desorption gas mixing tank after being cooled by the benzene removal regeneration cooler;

[0024] 6) Re-pressurization: after the cold blow regeneration is completed, all valves related to regeneration are closed, and the operation of the initial pressure raising stage is repeated to enter the next cycle.

[0025] In the whole process, the first adsorber and the second adsorber alternately perform adsorption and regeneration operations to realize continuous extraction of hydrogen in the coke oven gas, when one of the adsorbers is in an adsorption state and the other adsorber needs to be pressurized to prepare for the next round of adsorption, 106A / B valves on pipelines intercommunicating the top of the first adsorber and the top of the second adsorber are opened to discharge the unadsorbed gas from the top of the first adsorber into the other adsorber, and the pressurization operation is completed, realizing the alternation of the adsorption and regeneration processes.

[0026] Compared with the prior art, the beneficial effects of the utility model are as follows:

[0027] (1) The temperature swing adsorption device for the hydrogen extraction process of coke oven gas, through the parallel configuration of the first adsorber and the second adsorber, and the accurate control of the opening and closing states of each valve, the stable alternation of the adsorption and regeneration processes is realized, so that the hydrogen in the coke oven gas can be continuously and efficiently extracted, the hydrogen extraction efficiency is greatly improved, and the stability and continuity of the device operation are ensured.

[0028] (2) The temperature swing adsorption device for the hydrogen extraction process of coke oven gas, through the control system, the initial pressure increase, adsorption, pressure reduction, hot blowing regeneration, cold blowing regeneration and secondary pressure increase and other stages are accurately controlled, the device is strictly operated according to the predetermined process requirements, not only the reliability and stability of the device operation are improved, but also the fault risk caused by improper operation is significantly reduced, and the overall production efficiency and safety are improved. BRIEF DESCRIPTION OF DRAWINGS

[0029] Figure 1 It is a structure schematic view of the temperature swing adsorption device for the hydrogen extraction process of coke oven gas.

[0030] In the figure: 1, gas-liquid separator; 2, coke oven gas pipeline; 3, purge gas pipeline; 4, first adsorber; 5, second adsorber; 6, unadsorbed gas external pipeline; 7, PSA desorption gas buffer tank; 8, hot blowing pipeline; 9, cold blowing pipeline; 10, benzene removal regeneration heater; 11, pressure reduction exhaust pipeline; 12, regeneration exhaust pipeline; 13, PSA desorption gas mixing tank; 14, benzene removal regeneration cooler; 15, 101A / B valve; 16, 102A / B valve; 17, 106A / B valve; 18, 107 valve; 19, 108 valve; 20, 104A / B valve; 21, 103A / B valve; 22, 105A / B valve. DETAILED DESCRIPTION

[0031] In order to make the purpose, technical scheme of the utility model more clearly, in the following, to the utility model, make further detailed description with the aid of the drawings.

[0032] Example 1

[0033] As Figure 1 shown, the temperature swing adsorption device for the hydrogen extraction process of coke oven gas includes a gas-liquid separator 1, the gas-liquid separator 1 is connected with a coke oven gas pipeline 2 and a purge gas pipeline 3 at the gas inlet end, the gas outlet end of the gas-liquid separator 1 is connected with the bottom of the first adsorber 4 and the second adsorber 5 through pipelines respectively, the first adsorption tower and the second adsorption tower are arranged in a parallel configuration, the top of the first adsorber 4 and the second adsorber 5 is connected with each other through pipelines, the top of the first adsorber 4 and the second adsorber 5 is connected with the unadsorbed gas external pipeline 6 through pipelines respectively, and the output end of the unadsorbed gas external pipeline 6 is connected to the PSA process.

[0034] Further comprising a PSA desorption gas buffer tank 7, the outlet end of the PSA desorption gas buffer tank 7 branches out a hot blow pipeline 8 and a cold blow pipeline 9, the output ends of the hot blow pipeline 8 and the cold blow pipeline 9 are respectively connected to the top of the first adsorber and the second adsorber, and a benzene removal regeneration heater 10 is arranged on the hot blow pipeline 8.

[0035] The bottom of the first adsorber 4 and the second adsorber 5 is respectively connected to a pressure reduction exhaust pipeline 11 and a regeneration exhaust pipeline 12, the output ends of the pressure reduction exhaust pipeline 11 and the regeneration exhaust pipeline 12 are respectively connected to a PSA desorption gas mixing tank 13, and a benzene removal regeneration cooler 14 is arranged on the regeneration exhaust pipeline 12.

[0036] The pipeline connecting the exhaust end of the gas-liquid separator 1 with the bottom of the first adsorber 4 and the second adsorber 5 is respectively provided with a 101A / B valve 15. The A valve corresponds to the first adsorber 4, and the B valve corresponds to the second adsorber 5.

[0037] The pipeline leading to the unadsorbed gas export pipeline 6 at the top of the first adsorber 4 and the second adsorber 5 is respectively provided with a 102A / B valve 16.

[0038] The pipeline connecting the top of the first adsorber 4 and the second adsorber 5 is provided with a 106A / B valve 17.

[0039] The 107 valve 18 is arranged on the hot blow pipeline 8 before the inlet of the benzene removal regeneration heater 10, and the 108 valve 19 is arranged on the cold blow pipeline 9.

[0040] The output ends of the hot blow pipeline 8 and the cold blow pipeline 9 are respectively connected to the pipeline leading to the top of the first adsorber 4 and the second adsorber 5, and a 104A / B valve 20 is arranged thereon.

[0041] The pipeline leading to the pressure reduction exhaust pipeline 11 at the bottom of the first adsorber 4 and the second adsorber 5 is respectively provided with a 103A / B valve 21.

[0042] The pipeline leading to the regeneration exhaust pipeline 12 at the bottom of the first adsorber 4 and the second adsorber 5 is respectively provided with a 105A / B valve 22.

[0043] Further comprising a control system, the control system is electrically connected to each valve.

[0044] When working, the specific steps are as follows:

[0045] 1) Initial pressure rise: the control system opens the 101A / B valve 15, the purge gas enters the gas-liquid separator 1 from the purge gas pipeline 3, and then enters the first adsorber 4 and the second adsorber 5 for initial pressure rise;

[0046] 2) Adsorption: After the pressure is raised, the valve on the purge gas line 3 is closed, the coke oven gas from the coke oven gas line 2 enters the gas-liquid separator 1, and then enters the first adsorber 4 and the second adsorber 5 for adsorption. The unadsorbed gas is discharged to the unadsorbed gas external delivery line 6 through the 102A / B valve 16 and finally enters the PSA process.

[0047] 3) Pressure reduction: After the first adsorber 4 is saturated, the control system closes the 101A valve and the 102A valve, and opens the 103A valve, and the gas in the first adsorber 4 is discharged to the PSA desorption gas mixing tank 13 through the pressure reduction exhaust gas line 11.

[0048] 4) Hot blow regeneration: After the pressure reduction is completed, the control system opens the 107 valve 18 on the hot blow line 8 branched out from the outlet end of the PSA desorption gas buffer tank 7, and the 104A valve connecting the hot blow line 8 to the top of the first adsorber 4. The desorption gas in the PSA desorption gas buffer tank 7 is heated by the benzole removal regeneration heater 10 and then enters the first adsorber 4 for hot blow regeneration. The hot blown gas is discharged through the 105A valve on the regeneration exhaust gas line 12 and cooled by the benzole removal regeneration cooler 14 and then discharged into the PSA desorption gas mixing tank 13.

[0049] 5) Cold blow regeneration: After the hot blow regeneration is completed, the control system closes the 107 valve 18 and opens the 108 valve 19 on the cold blow line 9. The desorption gas in the PSA desorption gas buffer tank 7 enters the first adsorber 4 for cold blow through the cold blow line 9. The cold blown gas is also discharged through the 105A valve on the regeneration exhaust gas line 12 and cooled by the benzole removal regeneration cooler 14 and then discharged into the PSA desorption gas mixing tank 13.

[0050] 6) Re-pressurization: After the cold blow regeneration is completed, the control system closes all valves related to the regeneration of the first adsorber 4, and closes the 102B valve and opens the 106A / B valve 17. The unadsorbed gas generated by the second adsorber 5 is discharged into the first adsorber 4 through the pipeline connecting the top of the first adsorber 4 and the top of the second adsorber 5. After the first adsorber 4 is re-pressurized, the 106A / B valve 17 is closed, the 101A valve and the 102A / B valve 16 are opened, and the next round of adsorption is continued.

[0051] During the entire process, the first adsorber 4 sequentially performs adsorption, pressure reduction, hot blow regeneration, cold blow regeneration, and re-pressurization, while the second adsorber 5 continuously performs adsorption. When the second adsorber 5 is saturated, the regeneration process of the second adsorber 5 is completed by controlling the corresponding valves through the control system, thereby realizing the alternating performance of the adsorption and regeneration processes.

Claims

1. A temperature swing adsorption apparatus for a coke oven gas hydrogen upgrading process, characterized by, The coke oven gas pipeline (2) and the purge gas pipeline (3) are connected to the gas inlet end of the gas-liquid separator (1), the gas outlet end of the gas-liquid separator (1) is connected to the bottom of the first adsorber (4) and the second adsorber (5) through pipelines, the first adsorber and the second adsorber are arranged in parallel, the top of the first adsorber (4) and the second adsorber (5) are connected to the unadsorbed gas outlet pipeline (6) through pipelines, and the output end of the unadsorbed gas outlet pipeline (6) is connected to the PSA process. The PSA desorption gas buffer tank (7) is further included, the outlet end of the PSA desorption gas buffer tank (7) branches out the hot blow pipeline (8) and the cold blow pipeline (9), the output ends of the hot blow pipeline (8) and the cold blow pipeline (9) are respectively connected to the top of the first adsorber and the second adsorber, and the hot blow pipeline (8) is provided with a benzene removal regeneration heater (10). The bottom of the first adsorber (4) and the second adsorber (5) is respectively connected to the pressure reduction exhaust pipeline (11) and the regeneration exhaust pipeline (12), and the output ends of the pressure reduction exhaust pipeline (11) and the regeneration exhaust pipeline (12) are connected to the PSA desorption gas mixing tank (13), and the regeneration exhaust pipeline (12) is provided with a benzene removal regeneration cooler (14).

2. The pressure swing adsorption apparatus for a coke oven gas hydrogen extraction process according to claim 1, characterized in that, The pipeline connecting the gas outlet end of the gas-liquid separator (1) to the bottom of the first adsorber (4) and the second adsorber (5) is respectively provided with a 101A / B valve (15).

3. The pressure swing adsorption apparatus for a coke oven gas hydrogen extraction process according to claim 1, characterized in that, The pipeline connecting the top of the first adsorber (4) and the second adsorber (5) to the unadsorbed gas outlet pipeline (6) is respectively provided with a 102A / B valve (16).

4. The pressure swing adsorption apparatus for hydrogen extraction from coke oven gas process according to claim 1, wherein, The pipeline connecting the top of the first adsorber (4) and the second adsorber (5) is provided with a 106A / B valve (17).

5. The pressure swing adsorption apparatus for hydrogen extraction from a coke oven gas process according to claim 1, characterized in that, The 107 valve (18) is arranged on the hot blow pipeline (8) before the inlet of the benzene removal regeneration heater (10), and the 108 valve (19) is arranged on the cold blow pipeline (9).

6. The pressure swing adsorption apparatus for hydrogen extraction from a coke oven gas process according to claim 1, characterized in that, The pipeline connecting the output ends of the hot blow pipeline (8) and the cold blow pipeline (9) to the top of the first adsorber (4) and the second adsorber (5) is respectively provided with a 104A / B valve (20).

7. The pressure swing adsorption apparatus for hydrogen extraction from a coke oven gas process according to claim 1, characterized in that, The pipeline connecting the bottom of the first adsorber (4) and the second adsorber (5) to the pressure reduction exhaust pipeline (11) is respectively provided with a 103A / B valve (21).

8. The pressure swing adsorption apparatus for hydrogen extraction from a coke oven gas process according to claim 1, characterized in that, The pipeline connecting the bottom of the first adsorber (4) and the second adsorber (5) to the regeneration exhaust pipeline (12) is respectively provided with a 105A / B valve (22).

9. The pressure swing adsorption apparatus for hydrogen extraction from a coke oven gas process according to claim 1, characterized in that, The control system is further included.

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