CN220531226U - Dehydrogenation system based on BOG gas helium extraction device - Google Patents
Dehydrogenation system based on BOG gas helium extraction device Download PDFInfo
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- CN220531226U CN220531226U CN202322048114.0U CN202322048114U CN220531226U CN 220531226 U CN220531226 U CN 220531226U CN 202322048114 U CN202322048114 U CN 202322048114U CN 220531226 U CN220531226 U CN 220531226U
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- 239000007789 gas Substances 0.000 title claims abstract description 82
- 239000001307 helium Substances 0.000 title claims abstract description 33
- 229910052734 helium Inorganic materials 0.000 title claims abstract description 33
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 title claims abstract description 33
- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 17
- 238000000605 extraction Methods 0.000 title claims abstract description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 48
- 239000001257 hydrogen Substances 0.000 claims abstract description 48
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 48
- 230000001502 supplementing effect Effects 0.000 claims abstract description 42
- 238000006243 chemical reaction Methods 0.000 claims abstract description 35
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 33
- 239000001301 oxygen Substances 0.000 claims abstract description 33
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 33
- 238000002156 mixing Methods 0.000 claims abstract description 24
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 24
- 230000003197 catalytic effect Effects 0.000 claims abstract description 23
- 238000000034 method Methods 0.000 claims abstract description 20
- 230000003647 oxidation Effects 0.000 claims abstract description 17
- 239000002994 raw material Substances 0.000 claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 12
- 230000008569 process Effects 0.000 claims abstract description 10
- 230000001105 regulatory effect Effects 0.000 claims description 8
- 238000004880 explosion Methods 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 description 13
- 230000009471 action Effects 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 238000000746 purification Methods 0.000 description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 230000003068 static effect Effects 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000002360 explosive Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000012544 monitoring process Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
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- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
The utility model discloses a dehydrogenation system based on a BOG gas helium extraction device, which comprises: a hydrogen-containing BOG branch, a make-up branch, a mixing branch and a reaction branch; one end of the hydrogen-containing BOG branch is connected with the raw material gas buffer tank, and the other end of the hydrogen-containing BOG branch is sequentially connected with the heat exchanger and the electric heater and then is communicated with the mixing branch; one end of the air supplementing branch is connected with an air supplementing source, and the other end of the air supplementing branch is indirectly contacted with the electric heater and then connected with an air supplementing port arranged on the mixing branch; the mixing branch is connected with the mixer and then connected with the catalytic oxidation reactor; one end of the reaction branch is connected with the catalytic oxidation reactor, and the other end of the reaction branch is connected with the heat exchanger, the cooler and the gas-liquid separator in sequence and then connected with a subsequent process component; the utility model has reasonable design, realizes oxygen supplementing by arranging the supplementing branch, and simultaneously is provided with the hydrogen analyzer and the oxygen analyzer, so that the oxygen content can be reasonably monitored, and the risk of explosion of hydrogen after air supplementing is reduced.
Description
Technical Field
The utility model relates to a helium purification system, in particular to a helium purification system based on BOG gas.
Background
Helium purification mainly comprises membrane separation, adsorption, cryogenic technology and the like, and hydrogen and helium are symbiotic and are not easy to separate because of similar molecular weight, the separation of hydrogen and helium cannot be realized by the technology, and the existing helium purification method is mainly used for removing hydrogen in BOG gas by a catalytic oxidation method.
The catalytic oxidation reaction needs oxygen, the proportion of supplementary oxygen and hydrogen are adopted to generate water through catalytic oxidation reaction under the action of a special catalyst, so that hydrogen in helium-containing BOG gas is removed, the hydrogen is inflammable and explosive gas, the explosion limit in air is 4% -74.2%, the supplementary air has potential safety hazards, and the stable supplementary air participates in the reaction and ensures the production safety of the subsequent process.
Disclosure of Invention
Therefore, in order to solve the defects, the utility model provides the dehydrogenation system based on the BOG gas helium extracting device, which has reasonable design and simple structure, realizes oxygen supplementing by arranging the supplementing branch, and simultaneously, the hydrogen analyzer and the oxygen analyzer are arranged, so that the oxygen content can be reasonably monitored, and the risk of explosion of hydrogen after air supplementing is reduced.
Specifically, a dehydrogenation system based on BOG gas helium extraction device includes: a hydrogen-containing BOG branch, a make-up branch, a mixing branch and a reaction branch;
one end of the hydrogen-containing BOG branch is connected with the raw material gas buffer tank, and the other end of the hydrogen-containing BOG branch is sequentially connected with the heat exchanger and the electric heater and then is communicated with the mixing branch;
one end of the air supplementing branch is connected with an air supplementing source, and the other end of the air supplementing branch is connected with an air supplementing port arranged on the mixing branch after being acted by the electric heater;
the mixing branch is connected with the mixer and then connected with the catalytic oxidation reactor;
one end of the reaction branch is connected with the catalytic oxidation reactor, and the other end of the reaction branch is connected with the heat exchanger, the cooler and the gas-liquid separator in sequence and then connected with the subsequent process components.
Optionally, a regulating valve, a temperature sensor, a pressure sensor, a flowmeter and an emergency cut-off valve are sequentially installed on the air supplementing branch from an inlet to an outlet.
Optionally, a flowmeter and a hydrogen analyzer are sequentially installed on the hydrogen-containing BOG branch from the raw gas buffer tank to the heat exchanger.
Optionally, a reaction thermometer and an oxygen analyzer are installed on the reaction branch, wherein the reaction thermometer is located between the catalytic oxidation reactor and the heat exchanger, and the oxygen analyzer is located at the rear end of the outlet of the gas-liquid separator.
Optionally, a thermometer is mounted on the mixing branch between the make-up port and the mixer.
Optionally, the raw material gas buffer tank is connected with a BOG gas source and a subsequent procedure return gas source;
optionally, the oxygen supply adopts instrument air.
The utility model has the following advantages:
the utility model has reasonable design and simple structure, is a dehydrogenation system based on a BOG gas helium extracting device, adopts a catalytic oxidation method to remove hydrogen in BOG gas, and reserves helium and other impurity gases to enter a post-process for purifying helium; and the air (mainly oxygen in the air) is supplemented by adopting a supplementing branch to catalyze the oxidation reaction.
In order to overcome the potential safety hazard of the hydrogen generation in the supplemented oxygen and the BOG, a hydrogen analyzer is arranged on the hydrogen-containing BOG branch, an emergency cut-off valve is arranged on the hole supplementing branch, an oxygen analyzer is arranged on the reaction branch, and the content of the supplemented oxygen is jointly monitored by combining a plurality of temperature sensors, so that the potential safety hazard is reduced.
Meanwhile, the utility model adopts instrument air as an oxygen supplementing source, the instrument air is used as an indispensable public and auxiliary engineering for factory production, the air is inexhaustible, the oxygen in the air is utilized to participate in the successful application of the catalytic oxidation reaction control system by the supplementing air in the helium extracting device, the public resources of the factory are reasonably utilized, the high investment and the later long-term operation cost and the depreciation cost of the pure oxygen supplementing are reduced, and the occupied area of the pure oxygen device and the potential safety hazard caused by the pure oxygen device are saved.
Drawings
FIG. 1 is a block diagram of a dehydrogenation system based on a BOG gas helium extraction unit according to the present utility model;
in the figure: 100. a make-up branch; 101. a make-up regulating valve; 102. a make-up temperature sensor; 103. supplementing the air pressure sensor; 104. a make-up flow meter; 105. filling the emergency cut-off valve; 200. a mixing branch; 201. a mixer; 202. a catalytic oxidation reactor; 203. a mixture thermometer; 204. a supplementing port; 205. a check valve; 206. an outlet end thermometer; 300. a hydrogen-containing BOG branch; 301. a raw material gas buffer tank; 302. a hydrogen-containing BOG flowmeter; 303. a hydrogen analyzer; 304. a BOG gas flow meter; 400. a reaction branch; 401. a cooler; 402. a gas-liquid separator; 403. a reaction thermometer; 404. an oxygen analyzer; 500. a heat exchanger; 600. an electric heater.
Detailed Description
Embodiments of the present application are described in detail below, examples of which are illustrated in the accompanying drawings, wherein the same or similar reference numerals refer to the same or similar elements or elements having the same or similar functions throughout. The embodiments described below by referring to the drawings are exemplary and intended for the purpose of explaining the present application and are not to be construed as limiting the present application.
In this document, relational terms such as first and second, and the like may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Moreover, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus.
As described in the background art, oxygen is needed for catalytic oxidation reaction, and proportional supplementary oxygen and hydrogen are adopted to generate water for catalytic oxidation reaction under the action of a special catalyst so as to remove hydrogen in helium-containing BOG gas, wherein the hydrogen is inflammable and explosive gas, the explosion limit in air is 4% -74.2%, the supplementary air has potential safety hazards, and the stable supplementary air participates in the reaction and ensures the production safety of the subsequent procedures. Thus, in order to purify helium in BOG gas, the present embodiment provides a dehydrogenation system based on a BOG gas helium extracting device, as shown in fig. 1, including: a hydrogen-containing BOG circuit 300, a make-up circuit 100, a mixing circuit 200, and a reaction circuit 400;
one end of the hydrogen-containing BOG branch 300 is connected with the raw material gas buffer tank 301, and the other end is sequentially connected with the heat exchanger 500 and the electric heater 600 and then communicated with the mixing branch 200;
one end of the air compensating branch 100 is connected with an air compensating source, and the other end of the air compensating branch is connected with an air compensating port 204 arranged on the mixing branch after being acted by the electric heater;
the mixing branch 200 is connected with the mixer 201 and then connected with the catalytic oxidation reactor 202;
one end of the reaction branch 400 is connected with the catalytic oxidation reactor 202, and the other end is connected with the heat exchanger 500, the cooler 401 and the gas-liquid separator 402 in sequence and then connected with subsequent process components.
An outlet end thermometer 206 and a check valve 205 are also arranged at the outlet end of the electric heater, and the supplementing inlet 204 is positioned at the outlet rear end of the check valve 205; the oxygen supply source adopts instrument air.
Through the technical characteristics, hydrogen can be removed from the BOG gas to purify helium, and when the BOG gas is used, the BOG gas enters a hydrogen-containing BOG branch through a raw material gas buffer tank, exchanges heat through a heat exchanger (adopting gas-gas heat exchange), enters a heater (adopting electric heating), and then enters a mixing branch; the air to be supplemented enters from the supplementing branch, and enters into the mixing branch from the supplementing inlet after being heated by the electric heater, the gas enters into the catalytic oxidation reactor after being mixed in the mixer (adopting the static mixer) of the mixing branch, the gas after the reaction is subjected to heat exchange by the heat exchanger, the gas after the reaction is subjected to heat exchange is subjected to a cold area of the cooler, and the gas and the liquid are separated by the gas-liquid separator, so that the BOG gas after dehydrogenation is obtained.
The electric heater is arranged at the outlet of the cold end of the heat exchanger, the electric heater is used as a reaction heat source when the production is started, certain electric energy is consumed at the moment, after the dehydrogenation reaction is normal, heat energy generated by the reaction is recovered through cold-heat exchange of the gas-gas heat exchanger, the heat energy is reasonably utilized, when the temperature of cold air exceeds the temperature of the outlet of the electric heater, the electric heater stops working and enters a hot standby state to consume no electric energy, otherwise, the electric heater timely heats and supplements the heat energy to constantly enter the reactor to ensure that the catalytic oxidation reaction is stably carried out, and the electric heater supplements the heat energy by adopting accurate PID automatic regulation, so that the energy consumption is extremely low.
The air supplementing inlet is arranged between the outlet of the electric heater and the catalytic oxidation reactor, and the supplemented air is effectively and uniformly mixed with the heated BOG raw material gas through the static mixer and then enters the reactor to react with the oxygen in the air to generate water under the action of the catalyst coal medium, so that the purpose of removing the hydrogen is achieved.
In order to ensure stable supplementary air to participate in the reaction and ensure the production safety of the subsequent process when the hydrogen is removed from the BOG gas, a flowmeter is arranged at the front inlet pipe of a raw material gas buffer tank of the BOG gas, and a hydrogen analyzer and a flowmeter are arranged on a cold end pipe, which is close to a gas-gas heat exchanger, behind the raw material buffer tank; illustratively, a hydrogen-containing BOG flowmeter 302 and a hydrogen analyzer 303 are installed on the hydrogen-containing BOG branch 300 in order from a raw gas buffer tank 301 to a heat exchanger; the raw material gas buffer tank 301 is connected to a hydrogen-containing BOG gas branch on which a BOG gas flowmeter 304 is provided and a post-process return gas branch. The flow meter in front of the buffer tank measures the gas quantity of raw materials, the raw material gas behind the buffer tank is the mixed gas of BOG gas from an LNG storage tank and low helium tail gas returned in the middle of production, the flow meter measures the total gas quantity after mixing, the hydrogen analyzer is arranged in the buffer tank and measures the actual hydrogen content value entering the reactor, and the hydrogen analysis data and the flow data are adopted to participate in the control more accurately;
the low helium tail gas returned from the middle production link before the buffer tank has two benefits, namely, the high hydrogen BOG gas from the LNG storage tank can be diluted to be within a safety control value; secondly, the pressure of the low helium tail gas returned from the middle production link is higher, the pressure is effectively balanced after the low helium tail gas passes through a buffer tank, a gas-gas heat exchanger, a reactor, a cooler and a gas-liquid separator, and the fluctuation of helium content in BOG gas is greatly influenced by the unstable LNG production amount and loading amount, so that the unstable production raw material gas in other working procedures after dehydrogenation is caused, the low helium tail gas returned from the middle production link is unstable, and the effect of peak regulation control is also effectively realized by entering the low helium tail gas from the front of the buffer tank.
The air supplementing branch is provided with a regulating valve, a temperature instrument, a pressure instrument, a flow instrument and an emergency cut-off valve, and the air supplementing branch is provided with an air supplementing regulating valve 101, an air supplementing temperature sensor 102, an air supplementing pressure sensor 103, an air supplementing flowmeter 104 and an air supplementing emergency cut-off valve 105 from an inlet to an outlet in sequence. And when the air is normally supplemented, the supplementing quantity is automatically regulated by the regulating valve, the related data detected by each instrument is uploaded to the background monitoring system to be displayed in real time and participate in interlocking, and when the oxygen in the supplementing air is excessive, the emergency cut-off valve acts to close and isolate the air from entering the reactor so as to ensure the safety of subsequent production.
When the air pipeline enters the dehydrogenation area, the coiled pipe is closely attached to the outer wall of the electric heater and is laid and then connected with the BOG raw material gas pipeline at a pipeline position with a certain distance in front of the static mixer, and at the moment, the pipeline for conveying air is heated by heat energy radiated by the electric heater, so that the problem that the reaction efficiency is affected due to insufficient reaction temperature caused by pulling down reaction temperature when cold air and hot BOG raw material gas are mixed is solved, the product quality is affected, and the heat energy radiated by the electric heater is well recycled.
The check valve is arranged between the air supplementing port and the electric heater, so that the problem that the supplemented air cannot flow back into the electric heater is effectively solved, and the surface temperature of the heating pipe inside the electric heater is far higher than the heated gas temperature, so that mixed gas is formed with BOG gas after the air flows back, and certain safety is realized when the mixed gas meets a high-temperature heating pipe.
The mixed gas thermometer 203 positioned between the supplementing port 204 and the mixer is arranged on the mixing branch, so that the real temperature value entering the reactor can be accurately measured, and the temperature of the electric heater and the temperature of the gas heat exchanger can be conveniently and timely adjusted in production.
A reaction thermometer 403 and an oxygen analyzer 404 are installed on the reaction branch 400, wherein the reaction thermometer 403 is positioned between the catalytic oxidation reactor 202 and the heat exchanger 500, and the oxygen analyzer 404 is positioned at the rear end of the outlet of the gas-liquid separator 402; an oxygen analyzer is arranged at the rear outlet pipe of the catalytic oxidation reactor through gas-gas heat exchange, water cooling and a gas-liquid separator, the opening and closing of an air supplementing regulating valve are controlled by monitoring an oxygen data value, the oxygen content value entering a subsequent process is ensured not to exceed a safety upper limit, and the oxygen analyzer is arranged at the position, so that the high heat generated after reaction and the gas containing saturated water after reaction are effectively avoided from causing burden to an analyzer pretreatment device, and the oxygen analyzer is effectively protected.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present utility model. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the utility model. Thus, the present utility model is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (7)
1. A dehydrogenation system based on BOG gas helium extraction unit, comprising: a hydrogen-containing BOG branch, a make-up branch, a mixing branch and a reaction branch;
one end of the hydrogen-containing BOG branch is connected with the raw material gas buffer tank, and the other end of the hydrogen-containing BOG branch is sequentially connected with the heat exchanger and the electric heater and then is communicated with the mixing branch;
one end of the air supplementing branch is connected with an air supplementing source, and the other end of the air supplementing branch is connected with an air supplementing port arranged on the mixing branch after being acted by the electric heater;
the mixing branch is connected with the mixer and then connected with the catalytic oxidation reactor;
one end of the reaction branch is connected with the catalytic oxidation reactor, and the other end of the reaction branch is connected with the heat exchanger, the cooler and the gas-liquid separator in sequence and then connected with the subsequent process components.
2. The dehydrogenation system based on the BOG gas helium extraction device according to claim 1, wherein a regulating valve, a temperature sensor, a pressure sensor, a flowmeter and an emergency shut-off valve are sequentially arranged on the make-up branch from an inlet to an outlet.
3. A BOG gas helium extraction unit based dehydrogenation system according to claim 1, wherein a flow meter and a hydrogen analyzer are installed in this order on the hydrogen-containing BOG branch from a raw gas buffer tank to a heat exchanger.
4. The system of claim 1, wherein a reaction thermometer and an oxygen analyzer are installed on the reaction branch, wherein the reaction thermometer is located between the catalytic oxidation reactor and the heat exchanger, and the oxygen analyzer is located at the rear end of the outlet of the gas-liquid separator.
5. A dehydrogenation system based on BOG gas helium extraction unit according to claim 1, characterized in that a thermometer is mounted on the mixing branch between the make-up inlet and the mixer.
6. The dehydrogenation system based on a BOG gas helium extraction device according to claim 1, wherein the raw material gas buffer tank is connected with a BOG gas source and a subsequent process return gas source.
7. The system of claim 1, wherein the oxygen supply is instrument air.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322048114.0U CN220531226U (en) | 2023-08-01 | 2023-08-01 | Dehydrogenation system based on BOG gas helium extraction device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322048114.0U CN220531226U (en) | 2023-08-01 | 2023-08-01 | Dehydrogenation system based on BOG gas helium extraction device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220531226U true CN220531226U (en) | 2024-02-27 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322048114.0U Active CN220531226U (en) | 2023-08-01 | 2023-08-01 | Dehydrogenation system based on BOG gas helium extraction device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220531226U (en) |
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2023
- 2023-08-01 CN CN202322048114.0U patent/CN220531226U/en active Active
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