CN207713686U - Device in Gas alkane hydrate purification system - Google Patents
Device in Gas alkane hydrate purification system Download PDFInfo
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- CN207713686U CN207713686U CN201721575924.XU CN201721575924U CN207713686U CN 207713686 U CN207713686 U CN 207713686U CN 201721575924 U CN201721575924 U CN 201721575924U CN 207713686 U CN207713686 U CN 207713686U
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- 150000001335 aliphatic alkanes Chemical class 0.000 title claims abstract description 19
- 238000000746 purification Methods 0.000 title claims abstract description 15
- 239000007789 gas Substances 0.000 claims abstract description 119
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 61
- 238000006243 chemical reaction Methods 0.000 claims abstract description 47
- NMJORVOYSJLJGU-UHFFFAOYSA-N methane clathrate Chemical compound C.C.C.C.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O NMJORVOYSJLJGU-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000000203 mixture Substances 0.000 claims abstract description 10
- 238000003756 stirring Methods 0.000 claims abstract description 10
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 10
- 239000002912 waste gas Substances 0.000 claims abstract description 9
- 239000002351 wastewater Substances 0.000 claims abstract description 8
- 238000009833 condensation Methods 0.000 claims description 17
- 230000005494 condensation Effects 0.000 claims description 17
- 238000005507 spraying Methods 0.000 claims description 10
- 230000005587 bubbling Effects 0.000 claims description 8
- 238000005057 refrigeration Methods 0.000 claims description 7
- 230000006835 compression Effects 0.000 claims description 6
- 238000007906 compression Methods 0.000 claims description 6
- 238000002309 gasification Methods 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 5
- 230000000087 stabilizing effect Effects 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 3
- 239000013078 crystal Substances 0.000 abstract description 4
- 238000000605 extraction Methods 0.000 abstract description 4
- 239000007921 spray Substances 0.000 abstract description 4
- 238000005516 engineering process Methods 0.000 abstract description 2
- 150000004677 hydrates Chemical class 0.000 abstract description 2
- 230000008014 freezing Effects 0.000 abstract 2
- 238000007710 freezing Methods 0.000 abstract 2
- 238000004519 manufacturing process Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 17
- 239000003245 coal Substances 0.000 description 14
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 13
- 238000000034 method Methods 0.000 description 12
- 230000033228 biological regulation Effects 0.000 description 8
- 239000002994 raw material Substances 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 238000006703 hydration reaction Methods 0.000 description 6
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- RGSFGYAAUTVSQA-UHFFFAOYSA-N Cyclopentane Chemical compound C1CCCC1 RGSFGYAAUTVSQA-UHFFFAOYSA-N 0.000 description 2
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 2
- 238000009933 burial Methods 0.000 description 2
- 239000001273 butane Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000005065 mining Methods 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- DMEGYFMYUHOHGS-UHFFFAOYSA-N heptamethylene Natural products C1CCCCCC1 DMEGYFMYUHOHGS-UHFFFAOYSA-N 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000003541 multi-stage reaction Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model is related to device in Gas purification technique fields, more particularly to device in Gas alkane hydrate purification system.Extraction system includes water supply subsystem, device in Gas supply subsystem, reaction subsystem, isolated subsystem and freezing subsystem；Water supplies subsystem water out and is connected with subsystem spray equipment entrance is reacted；The outlet of device in Gas supply subsystem device in Gas is connected with subsystem device in Gas entrance is reacted；Reaction subsystem end mixture outlet is connected with separator matter inlet to be separated；The outlet of gas gas hydrate, wastewater outlet and waste gas outlet is arranged in separator, and the outlet of gas gas hydrate is connected with the entrance of freezing subsystem；Device in Gas bubble structure and/or stirring structure are also set up in reaction subsystem.This technology water spray and under, gas gas bell floats, and the two comes into full contact with, increase hydrate production quantity；The product of upstream reactor becomes the crystal seed in downstream reactor reaction, promotes downstream reactor reaction rapider, generates more gas gas hydrates.
Description
Technical Field
The utility model relates to a gas purification technical field especially relates to gas alkane hydrate purification system.
Background
Coal Bed gas (Coal Bed Methane (CBM) for short) refers to unconventional natural gas adsorbed in Coal beds. Coal Mine Methane (CMM) is low-concentration Coal bed gas, also called oxygen-containing Coal bed gas, which is pumped and discharged during mining and mixed with air, is a very expensive resource although a main disaster of Coal Mine safety, and can be used as a chemical raw material and a fuel required by industry, power generation and resident life. The coal bed gas resource with the global burial depth of 2000 m and shallow depth is about 240 billion cubic meters, and the coal bed gas resource with the Chinese burial depth of 2000 m and shallow depth is about 31.5 billion cubic meters. In order to achieve coal mining safety, the amount of coal bed gas extracted and discharged into the atmosphere in China is hundreds of millions of cubic meters every year, the coal bed gas is the most important world-wide coal bed gas discharge country, the discharge amount accounts for the first place in the world, the greenhouse effect caused by the discharge of the coal bed gas is more than 20 times of that of carbon dioxide, and not only is serious atmospheric pollution caused, but also huge resource waste is caused. At present, most of low-concentration gas (less than 7%) pumped and discharged from a mine is in an emptying state, and how to effectively collect, store and reasonably utilize the gas is a technical problem which needs to be solved urgently.
SUMMERY OF THE UTILITY MODEL
Technical problem to be solved
The utility model aims at providing a gas alkane hydrate purification system to reach the purpose of effectively utilizing the gas.
(II) technical scheme
In order to solve the technical problem, the utility model provides a gas paraffin hydrate purification system, it includes: the system comprises a water supply subsystem, a gas supply subsystem, a reaction subsystem, a separator and a refrigeration subsystem; wherein,
the water outlet of the water supply subsystem is connected with the inlet of the spraying device of the reaction subsystem; the gas outlet of the gas supply subsystem is connected with the gas inlet of the reaction subsystem; the final mixture outlet of the reaction subsystem is connected with the substance inlet to be separated of the separator; the separator is provided with a gas hydrate outlet, a waste water outlet and a waste gas outlet, and the gas hydrate outlet is connected with the inlet of the refrigeration subsystem;
and a gas bubbling structure and/or a stirring structure are/is also arranged in the reaction subsystem.
In some embodiments, preferably, the reaction subsystem comprises: more than one reactor; when the number of the reactors is more than two, all the reactors are connected in series and/or in parallel.
In some embodiments, it is preferred that when two reactors are connected in series, the product of the upstream reactor enters the downstream reactor to continue the reaction; when the two reactors are connected in parallel, the reactors are respectively connected with the water supply subsystem and the gas supply subsystem.
In some embodiments, it is preferable that the transfer channels of the two reactors are provided with a gasification structure and a pressurization structure.
In some embodiments, preferably, the water supply subsystem comprises: the condenser comprises a water supply pipeline and a first condensation structure, wherein the first condensation structure is erected on the water supply pipeline.
In some embodiments, preferably, the gas supply subsystem comprises: the gas-liquid separator comprises a gas supply pipeline, a compression structure, a pressure stabilizing structure, a second condensation structure and a nozzle structure, wherein the compression structure, the pressure stabilizing structure, the second condensation structure and the nozzle structure are sequentially erected on the gas supply pipeline along the gas supply direction.
In some embodiments, it is preferable that a third condensation structure communicated with a cold source is arranged in the reaction subsystem.
(III) advantageous effects
In the technical scheme provided by the utility model, gas is compressed and condensed and then reacts with water to generate hydrate, and based on the principle, the gas is sprayed from top to bottom by virtue of water, bubbles and floats from bottom to top, the gas and the water are opposite to each other, the sprayed water and the gas are fully contacted, and the generation amount of the hydrate is increased; moreover, through a multi-stage (such as two-stage) reactor, the product of the upstream reactor becomes the seed crystal in the reaction of the downstream reactor, so that the reaction of the downstream reactor is more rapid and efficient, and more gas hydrate is generated.
The hydrate can be safely stored and transported at normal temperature and pressure.
Drawings
FIG. 1 is a schematic structural diagram of a gas alkane hydrate purification apparatus with reactors connected in series according to an embodiment of the present invention;
FIG. 2 is a schematic structural diagram of an apparatus for purifying gas alkane hydrate in which reactors are connected in parallel according to an embodiment of the present invention;
fig. 3 is a schematic structural diagram of a gas alkane hydrate purification device with reactors connected in parallel and in series according to an embodiment of the present invention.
The attached drawings are marked as follows:
1 gas flow regulator; 2, a nozzle structure; 3, a pore plate structure; 4 a first reactor; 5 a second reactor; 6, a stirring device; 7, a spraying device; 8, a water pump; and 9, a water flow regulator.
Detailed Description
The following detailed description of the embodiments of the present invention is provided with reference to the accompanying drawings and examples. The following examples are intended to illustrate the invention, but are not intended to limit the scope of the invention.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In order to reduce the waste amount of gas, collect the problem that utilizes as far as possible with gas, the utility model discloses a gas alkane hydrate purification system.
The product will be described in detail below by way of a basic design, an extended design, and an alternative design.
The following provides a system for purifying gas alkane hydrate, as shown in fig. 1, which mainly comprises: the system comprises a water supply subsystem, a gas supply subsystem, a reaction subsystem, a separator and a refrigeration subsystem; wherein, the water outlet of the water supply subsystem is connected with the inlet of the spraying device 7 of the reaction subsystem; a gas outlet of the gas supply subsystem is connected with a gas inlet of the reaction subsystem; the final mixture outlet of the reaction subsystem is connected with the substance inlet to be separated of the separator; the separator is provided with a gas hydrate outlet, a waste water outlet and a waste gas outlet, and the gas hydrate outlet is connected with the inlet of the refrigeration subsystem; and a gas bubbling structure and/or a stirring structure are/is also arranged in the reaction subsystem.
Based on the basic system, the specific structures of several reaction subsystems are given below:
structure one, reaction subsystem include a reactor, set up bubbling structure, stirring structure and spray set 7 in this reactor, and water spouts 7 blowout from the spray set, and the gas is from bubbling structure drum department, and pore plate structure 3 is chooseed for use to the bubbling structure, sets up the through-hole that is covered with whole board on the pore plate structure 3. Stirring means 6 are provided in the liquid for stirring and separating unhydrated gas from the liquid into the atmosphere for contact with the water vapor above the liquid surface. The reaction subsystem is applied to extraction processes that do not include two, three, or more stages of reactors.
And the second structure is that the reaction subsystem comprises a plurality of reactors, and as shown in FIG. 1, two reactors are connected in series and are upstream and downstream of the product. The reactor at the upstream is provided with a spraying structure and a bubbling structure (an orifice plate structure 3), and the reactor at the downstream is provided with a spraying structure and a stirring structure. In this case, the upstream reactor may be provided with exhaust gas discharge holes, typically nitrogen and oxygen.
In addition, in order to facilitate the efficient reaction of the product in the downstream, a gasification structure and a pressurization mechanism are preferably arranged on the product transfer channel, and the product is gasified, pressurized and stabilized and then sent to the downstream reactor.
And the third structure, the reaction subsystem comprises a plurality of reactors, as shown in fig. 3, taking two as an example, the two reactors are connected in parallel and in series, the series connection is used for facilitating the upstream and downstream treatment of the product, the parallel connection is realized because the upstream and downstream reactors are respectively connected with the water supply subsystem and the gas supply subsystem, namely, two raw materials are fed into the downstream reactor (also called as a second reactor 5). In this case, the upstream reactor may be provided with exhaust gas discharge holes, typically nitrogen and oxygen. In order to facilitate the efficient reaction of the products in the downstream, the two reactors connected in series are preferably provided with a gasification structure and a pressurization mechanism on the product transfer channel, so that the products are gasified, pressurized and stabilized, and then sent to the downstream reactor.
The water supply subsystem includes: water supply pipeline and first condensation structure, first condensation structure erect on water supply pipeline, still set up flow regulator and water pump 8 on this pipeline, and water pump 8 can improve water pressure. In some embodiments, a flow regulator, a condenser, and a water pump 8 are provided in the water supply line in this order in the water flow direction.
The gas supply subsystem comprises: gas supply line, compression structure, steady voltage structure, second condensation structure and nozzle structure 2, compression structure, steady voltage structure, second condensation structure, nozzle structure 2 erect in proper order on gas supply line along gas supply direction.
The reaction subsystem is internally provided with a third condensation structure communicated with a cold source, the third condensation structure is used for providing a low-temperature environment in the reactor, and the third condensation structure is fully contacted with reaction raw materials and products as far as possible in order to promote the uniform reaction temperature of all positions of the reactor. The third condensing structure can be in different structural forms such as a coil pipe, a column pipe and the like.
It should be noted that the flow regulation is not required for both the gas supply and the water supply, and it is essential to provide various control valves on the supply lines. For gas, it is necessary to prevent backflow, and therefore, it is also essential to provide a check valve.
Next, the purification method of the purification system is described with reference to fig. 1, and the method mainly includes a gas supply branch, a water supply branch, a hydrate generation process, and a post-generation treatment process. Wherein,
the process flow of the gas supply branch is as follows: introducing gas, controlling the flow rate of the gas by a gas flow regulator 1, compressing the gas according to preset process parameters (such as pressure, temperature, flow rate and the like) until the pressure is slightly higher than the reaction pressure, and then performing pressure stabilization treatment to maintain the pressure stability during the hydration reaction. The gas with stable pressure is condensed and is sent into the reactor to participate in the hydration reaction through the flow regulation of the nozzle structure 2.
The process flow of the water supply branch comprises the following steps: water is introduced through a water source, the flow of the water is controlled by a water flow regulator 9, and after being pressurized by a water pump 8, the water is condensed and then is sent to a spraying device 7 of the reactor.
The hydrate generation process comprises the following steps:
in a low-temperature environment, water is sprayed from the spraying device 7 of the reactor from top to bottom and is in a water-gas state. The gas bubbles from the orifice plate device of the first reactor 4 from bottom to top and is in a micromolecular gaseous state. The gas and the water move relatively and fully contact with each other to produce gas hydrate (mixed with the waste water and the waste gas to form a mixture). For convenience of distinguishing the products may be referred to herein as the first gas hydrate and the mixture may be referred to as the first mixture. The exhaust gas of the first reactor is discharged from the first reactor.
Subsequently, as shown in fig. 1, the first reactor 4 and the second reactor are connected in series, the first mixture of the first reactor 4 is gasified and pressurized and then fed into the second reactor 5, and since the first gas hydrate of the first reactor 4 is used as a seed crystal to promote the hydrate reaction in the second reactor 5, the second gas hydrate is produced with a higher concentration. In the second reactor 5, the second gas hydrate is still mixed with the waste water, the waste gas, which may be referred to as a second mixture. The gas concentration of the second gas hydrate is greater than the gas concentration of the first gas hydrate. The second reactor 5 is used as a secondary reactor, gas is subjected to hydration reaction with water from the bottom through the stirring device 6, unreacted gas escapes from the water surface, and water mist sprayed by the spraying device 7 is rehydrated. After passing through the two reactors, water and alkane gas (such as methane, ethane and the like) in the gas are basically reacted.
Some waste gas is generated in the first reactor and the second reactor and is respectively discharged through respective waste gas outlets.
In some embodiments, the first reactor and the second reactor may have other connection relationships, such as: the two are connected in series, as shown in figure 2, and the corresponding material trend is that after the raw materials are respectively reacted in the two reactors, the obtained products are all sent into a separator. For another example: the two are connected in series and in parallel, as shown in figure 3, after the corresponding materials react in the first reactor, the product of the first reactor is sent to the second reactor after gasification and pressurization, in order to supplement the insufficient raw materials, part of the raw materials are directly supplemented to the second reactor to participate in the reaction together, and then the product of the second reactor is sent to the separator.
The main component of gas is alkanes, of which methane is the majority and small amounts of ethane, propane and butane. Therefore, the first gas hydrate and the second gas hydrate each contain methane, ethane, propane, and/or butane.
Next, the second mixture (containing hydrate, gas, water) is sent to a separation structure (such as a large three-phase separator) to separate gas hydrate, waste water, and waste gas, wherein the separated gas hydrate is frozen, and a small amount of pure water separated flows out from the lower part of the separator, and is recycled into the reactor because the water tends to maintain a crystal structure. The gas which does not enter the hydrate is mainly nitrogen and oxygen and is directly discharged.
The method is a main process flow for purifying the gas alkane hydrate, the raw materials are combined more fully by changing the state of the raw materials during hydration reaction, and the concentration of extracted gas and the purity of a product are gradually improved by utilizing multi-stage reaction, so that the gas is purified efficiently.
In addition, the wastewater can be returned to the condenser for condensation treatment before entering the first reactor 4 and the second reactor 5 during recycling.
The low temperature environment mentioned above can be set with reference to the ambient temperature required in the process of generating hydrates from gas and water by extracting the reaction heat generated in the reaction to reach the normal reaction temperature. In addition, in order to guide the reaction heat as much as possible and distribute the low-temperature environment as uniformly as possible, one skilled in the art can arrange the refrigeration structure to reach the low-temperature environment by various ways as required.
In other preparation processes, a step of condensing the compressed gas and then feeding the condensed gas into the bubbling device of the first reactor 4 (referring to any connection relationship in fig. 1-3) may be added based on the basic process; the condensed compressed gas can be sent into the second reactor 5 and stirred (for the connection relationship between fig. 2 and fig. 3), and the link can supplement the consumption of the gas in the second reactor 5, thereby not only increasing the absorption amount of the gas, but also improving the concentration of the gas hydrate.
In addition, the main purpose of the technology is to increase the extraction amount of the gas, and to further improve the extraction effect of the gas by skillfully utilizing the reaction principle and promoting the hydration reaction by adding an auxiliary agent in consideration of the fact that a certain reaction heat is generated in the hydration reaction of the gas and water. Thus, in various preparation processes it may be preferable to add thermodynamic and kinetic additives to the water before it is fed to the spraying device 7, such as: cyclopentane, tetrahydrofuran, and the like.
The flow regulation, the water flow regulation and the gas flow regulation are carried out in different ways, and in the case of gas, the condensed gas is distributed to the first reactor 4 and/or the second reactor 5 by means of flow regulation; the manner of flow regulation is preferably nozzle regulation.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (6)
1. A system for purifying gas alkane hydrate, comprising: the system comprises a water supply subsystem, a gas supply subsystem, a reaction subsystem, a separator and a refrigeration subsystem; wherein,
the water outlet of the water supply subsystem is connected with the inlet of the spraying device of the reaction subsystem; the gas outlet of the gas supply subsystem is connected with the gas inlet of the reaction subsystem; the final mixture outlet of the reaction subsystem is connected with the substance inlet to be separated of the separator; the separator is provided with a gas hydrate outlet, a waste water outlet and a waste gas outlet, and the gas hydrate outlet is connected with the inlet of the refrigeration subsystem;
and a gas bubbling structure and/or a stirring structure are/is also arranged in the reaction subsystem.
2. The system for gas alkane hydrate purification of claim 1, wherein the reaction subsystem comprises: more than one reactor; when the number of the reactors is more than two, all the reactors are connected in series and/or in parallel.
3. The system for purifying a gas alkane hydrate of claim 2,
when the two reactors are connected in series, the product of the upstream reactor enters the downstream reactor for continuous reaction, and a gasification structure and a pressurization structure are arranged on the transfer channels of the two reactors;
when the two reactors are connected in parallel, the reactors are respectively connected with the water supply subsystem and the gas supply subsystem.
4. The system for purifying a gas alkane hydrate as claimed in any one of claims 1 to 3,
the water supply subsystem includes: the condenser comprises a water supply pipeline and a first condensation structure, wherein the first condensation structure is erected on the water supply pipeline.
5. The system for gas alkane hydrate purification of any one of claims 1-3, wherein the gas supply subsystem comprises: the gas-liquid separator comprises a gas supply pipeline, a compression structure, a pressure stabilizing structure, a second condensation structure and a nozzle structure, wherein the compression structure, the pressure stabilizing structure, the second condensation structure and the nozzle structure are sequentially erected on the gas supply pipeline along the gas supply direction.
6. The system for purifying gas alkane hydrate as claimed in any one of claims 1 to 3, wherein a third condensing structure communicated with a cold source is arranged in the reaction subsystem.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201721575924.XU CN207713686U (en) | 2017-11-22 | 2017-11-22 | Device in Gas alkane hydrate purification system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201721575924.XU CN207713686U (en) | 2017-11-22 | 2017-11-22 | Device in Gas alkane hydrate purification system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107880960A (en) * | 2017-11-22 | 2018-04-06 | 中能冰气能源科技（北京）有限公司 | Device in Gas alkane hydrate method of purification and system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107880960A (en) * | 2017-11-22 | 2018-04-06 | 中能冰气能源科技（北京）有限公司 | Device in Gas alkane hydrate method of purification and system |
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Granted publication date: 20180810 |