CN112479802A - Generating system and generating method of propane hydrate - Google Patents
Generating system and generating method of propane hydrate Download PDFInfo
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- CN112479802A CN112479802A CN202011277542.5A CN202011277542A CN112479802A CN 112479802 A CN112479802 A CN 112479802A CN 202011277542 A CN202011277542 A CN 202011277542A CN 112479802 A CN112479802 A CN 112479802A
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- propane
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- RFXDGUUKGNRBCH-UHFFFAOYSA-N propane;hydrate Chemical compound O.CCC RFXDGUUKGNRBCH-UHFFFAOYSA-N 0.000 title claims abstract description 43
- 238000000034 method Methods 0.000 title claims abstract description 19
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 188
- RGSFGYAAUTVSQA-UHFFFAOYSA-N Cyclopentane Chemical compound C1CCCC1 RGSFGYAAUTVSQA-UHFFFAOYSA-N 0.000 claims abstract description 88
- 238000006243 chemical reaction Methods 0.000 claims abstract description 65
- 239000004576 sand Substances 0.000 claims abstract description 64
- 239000000377 silicon dioxide Substances 0.000 claims abstract description 62
- 238000005057 refrigeration Methods 0.000 claims abstract description 45
- DMEGYFMYUHOHGS-UHFFFAOYSA-N heptamethylene Natural products C1CCCCCC1 DMEGYFMYUHOHGS-UHFFFAOYSA-N 0.000 claims abstract description 44
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 36
- 239000011259 mixed solution Substances 0.000 claims abstract description 24
- 239000001294 propane Substances 0.000 claims abstract description 18
- 238000011084 recovery Methods 0.000 claims abstract description 14
- 238000004519 manufacturing process Methods 0.000 claims abstract description 9
- 238000003860 storage Methods 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 44
- 239000002245 particle Substances 0.000 claims description 19
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 18
- 239000003345 natural gas Substances 0.000 claims description 9
- 238000012806 monitoring device Methods 0.000 claims description 7
- 238000002156 mixing Methods 0.000 claims description 6
- 239000012266 salt solution Substances 0.000 claims description 4
- 238000012544 monitoring process Methods 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 2
- 230000006698 induction Effects 0.000 abstract description 13
- 238000010521 absorption reaction Methods 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 15
- 230000015572 biosynthetic process Effects 0.000 description 13
- 238000010899 nucleation Methods 0.000 description 9
- 230000006911 nucleation Effects 0.000 description 9
- 230000000694 effects Effects 0.000 description 8
- 230000008569 process Effects 0.000 description 7
- 239000012071 phase Substances 0.000 description 6
- 239000013078 crystal Substances 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- 239000006200 vaporizer Substances 0.000 description 4
- 239000007788 liquid Substances 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 230000001737 promoting effect Effects 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000014509 gene expression Effects 0.000 description 1
- 150000004677 hydrates Chemical class 0.000 description 1
- 230000000887 hydrating effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 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 description 1
- 238000013508 migration Methods 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/14—Purification; Separation; Use of additives by crystallisation; Purification or separation of the crystals
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
本发明公开了一种丙烷水合物的生成系统，包括生成装置以及制冷装置，所述生成装置包括反应釜与丙烷气罐，所述丙烷气罐通过输送泵连通至所述反应釜，所述丙烷气罐与输送泵之间设置有减压阀以及气体流量计，所述输送泵连通至所述反应釜顶部，所述反应釜底部铺设有硅砂层，所述硅砂层浸没至环戊烷混合溶液中；所述制冷装置包括依次连接的LNG储罐、LNG泵、热交换器以及回收瓶，所述热交换器与所述反应釜连通进行热交换。使用本生成系统或生成方法，能够大大缩短丙烷水合物的诱导时间，提高气体吸收率，在一定时间内增加水合物的生成量；采用LNG冷能作为冷源对反应釜提供制冷量，对比于传统的制冷方式，能够大大降低能耗，降低丙烷水合物的生成成本。
The invention discloses a propane hydrate generation system, comprising a generation device and a refrigeration device, wherein the generation device comprises a reaction kettle and a propane gas tank, the propane gas tank is communicated with the reaction kettle through a conveying pump, and the propane gas tank is connected to the reaction kettle. A pressure reducing valve and a gas flow meter are arranged between the gas tank and the delivery pump, the delivery pump is connected to the top of the reactor, and the bottom of the reactor is laid with a silica sand layer, which is immersed in the cyclopentane mixed solution The refrigeration device includes an LNG storage tank, an LNG pump, a heat exchanger and a recovery bottle connected in sequence, and the heat exchanger communicates with the reaction kettle for heat exchange. Using the generation system or generation method can greatly shorten the induction time of propane hydrate, improve the gas absorption rate, and increase the generation amount of hydrate within a certain period of time; LNG cold energy is used as a cold source to provide refrigeration capacity to the reactor, compared to The traditional refrigeration method can greatly reduce energy consumption and reduce the production cost of propane hydrate.
Description
Technical Field
The invention relates to the field of hydrate generation, in particular to a generation system and a generation method of propane hydrate.
Background
The hydrate is mainly generated into hydrate crystals by using gas molecules or liquid which is easy to generate the hydrate and pure water in seawater at a certain temperature and pressure. The formation of propane hydrate is mild, and in recent years, the research on the mechanism of propane hydrate is more and more focused. Propane can extract water from the porous medium, sand, and produce propane hydrate on top of the sand.
However, there are many factors that affect the generation of hydrate, and at present, it is a common practice of researchers at home and abroad to promote the generation of hydrate by adding hydrating agent or adding porous medium. However, the gas hydrate in a natural state is generated under harsh conditions at a slow rate, no corresponding production device or system is provided in real life, and the hydrate generation process is a heat release process and requires external cold supply to reduce the temperature and maintain the generation of the hydrate, so that the energy consumption of the hydrate artificial synthesis is very large.
Therefore, a new system or method for producing propane hydrate is required, which can solve the above problems.
Disclosure of Invention
An object of the present invention is to provide a new solution for the formation of propane hydrate.
According to a first aspect of the invention, a propane hydrate generation system is provided, which comprises a generation device and a refrigeration device, wherein the generation device comprises a reaction kettle and a propane gas tank, the propane gas tank is communicated to the reaction kettle through a delivery pump, a pressure reducing valve and a gas flowmeter are arranged between the propane gas tank and the delivery pump, the delivery pump is communicated to the top of the reaction kettle, a silica sand layer is laid at the bottom of the reaction kettle, and the silica sand layer is immersed in a cyclopentane mixed solution; refrigerating plant is including the LNG storage tank, LNG pump, heat exchanger and the recovery bottle that connect gradually, heat exchanger is arranged in gasifying LNG and becomes the natural gas and retrieves in the recovery bottle.
Through this scheme, utilize the cold energy of LNG itself to provide the refrigerating output to reation kettle, greatly reduced the energy consumption in the traditional refrigeration process, reduced propane hydrate's formation cost, be fit for industrial production and use.
Preferably, the top of the reaction kettle is communicated with a gas collecting bottle, and a gas flowmeter is arranged between the gas collecting bottle and the reaction kettle.
Through this scheme, the gas collection bottle can retrieve unnecessary propane gas in the reation kettle, keeps the pressure balance among the reation kettle.
Preferably, the bottom of the inner wall of the reaction kettle is provided with a micro-rib structure, and the height of the micro-rib structure is not less than the thickness of the silica sand layer.
Through this scheme, the contact area of little rib structure can double increase and silica sand layer, increases the double-phase contact area of gas-liquid, increases heat transfer and mass transfer between gas and the silica sand layer, forms favorable nucleation structure, accelerates hydrate nucleation, shortens induction time.
Preferably, the heat exchanger includes a refrigeration box, an output pipe of the LNG pump is communicated to a refrigeration pipe of the refrigeration box, the refrigeration pipe is coiled into the refrigeration box, the refrigeration pipe is communicated to the recovery bottle, and the reaction kettle is located in the refrigeration box.
Through this scheme, utilize a large amount of cold energy of LNG self to provide the refrigeration volume to the refrigeration case to reach and carry out refrigerated effect to reation kettle, let in after the refrigeration and retrieve in the recovery bottle.
Preferably, a monitoring device is arranged on the reaction kettle, and the monitoring device at least comprises a pressure sensor and a temperature sensor.
According to a second aspect of the present invention, there is provided a method for producing a propane hydrate using the above-described system for producing a propane hydrate, comprising the steps of:
the method comprises the following steps: mixing cyclopentane with a salt solution to form a cyclopentane mixed solution, wherein the mole mass percentage of cyclopentane in the cyclopentane mixed solution is 1.0-5.0 mol%;
step two: injecting the cyclopentane mixed solution into a reaction kettle and enabling the cyclopentane mixed solution to immerse a silica sand layer of the reaction kettle, wherein the thickness of the silica sand layer is 1.5-5.0cm, and the particle size of silica sand in the silica sand layer is 100-500 mu m;
step three: opening a pressure reducing valve and a delivery pump to inject the propane gas into the reaction kettle until the pressure in the reaction kettle reaches a set pressure, wherein the set pressure is 0.5-2 MPa;
step four: and opening the LNG pump to enable the LNG to provide refrigerating capacity for the reaction kettle through the refrigerating box, and monitoring the temperature and the pressure in the reaction kettle in real time until the temperature and the pressure in the reaction kettle are within a stable range.
Preferably, after the cyclopentane mixed solution is prepared, the molar mass percentage of cyclopentane is 3.0 mol%.
Preferably, the filling thickness of the silica sand layer is 1.5cm, and the particle size of the silica sand used in the silica sand layer is 100 μm.
According to one embodiment of the disclosure, the generation system or the generation method of the propane hydrate can greatly shorten the induction time of the propane hydrate, improve the gas absorption rate and increase the generation amount of the hydrate within a certain time;
the invention adopts LNG cold energy as a cold source to provide refrigerating capacity for the reaction kettle, and compared with the traditional refrigerating mode, the invention can greatly reduce energy consumption and reduce the generation cost of the propane hydrate.
Other features of the present invention and advantages thereof will become apparent from the following detailed description of exemplary embodiments thereof, which proceeds with reference to the accompanying drawings.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description, serve to explain the principles of the invention.
Fig. 1 is a schematic structural view of a propane hydrate formation system according to a first embodiment of the present invention.
Fig. 2 is a schematic view showing the position of a micro-rib structure in a reaction vessel of the propane hydrate formation system of fig. 1.
Detailed Description
Various exemplary embodiments of the present invention will now be described in detail with reference to the accompanying drawings. It should be noted that: the relative arrangement of the components and steps, the numerical expressions and numerical values set forth in these embodiments do not limit the scope of the present invention unless specifically stated otherwise.
The following description of at least one exemplary embodiment is merely illustrative in nature and is in no way intended to limit the invention, its application, or uses.
Techniques, methods, and apparatus known to those of ordinary skill in the relevant art may not be discussed in detail but are intended to be part of the specification where appropriate.
In all examples shown and discussed herein, any particular value should be construed as merely illustrative, and not limiting. Thus, other examples of the exemplary embodiments may have different values.
It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, further discussion thereof is not required in subsequent figures.
Example one
As shown in fig. 1 to fig. 2, the generation system of propane hydrate in the present embodiment includes a generation device and a refrigeration device, the generation device includes a reaction kettle 1 and a propane gas tank 111, the propane gas tank 111 is communicated to the reaction kettle 1 through a delivery pump 114, a pressure reducing valve 112 and a gas flow meter 113 are disposed between the propane gas tank 111 and the delivery pump 114, the delivery pump 114 is communicated to the top of the reaction kettle 1, a silica sand layer 12 is laid at the bottom of the reaction kettle 1, and the silica sand layer 12 is immersed in a cyclopentane mixed solution; the refrigeration device comprises an LNG storage tank 131, an LNG pump 132, a heat exchanger 133 and a recovery bottle 134 which are connected in sequence, wherein the heat exchanger 133 is used for gasifying LNG to change the LNG into natural gas and recovering the natural gas into the recovery bottle 134.
According to the scheme of the embodiment, the LNG self cold energy is used as the cold source to provide the refrigerating capacity for the reaction kettle, so that the energy consumption in the traditional refrigerating process is greatly reduced, the generation cost of the propane hydrate is reduced, and the method is suitable for industrial production.
In this embodiment or other embodiments, a gas collecting bottle 121 is communicated with the top of the reaction kettle 1, and a gas flowmeter 122 is disposed between the gas collecting bottle 121 and the reaction kettle 1. The gas collecting bottle 121 can recover redundant propane gas in the reaction kettle 1, and the pressure balance in the reaction kettle 1 is kept.
In this embodiment or other embodiments, the bottom of the inner wall of the reaction kettle 1 is provided with a micro-rib structure 11, and the height of the micro-rib structure 11 is not less than the thickness of the silica sand layer 12. The micro-rib structure 11 can multiply increase the contact area with the silica sand layer 12, increase the contact area of gas-liquid two phases, increase the heat transfer and mass transfer between the gas and the silica sand layer, form a favorable nucleation structure, accelerate the nucleation of the hydrate and shorten the induction time.
The micro-rib structure 11 in this embodiment surrounds the inner wall of the reaction kettle 1 and is distributed over the inner wall of the reaction kettle 1, the cross section of the micro-rib structure 11 is in a wave shape, that is, a plurality of annular protrusions and grooves are uniformly and alternately distributed on the inner wall of the reaction kettle 1, wherein the widths of the protrusions and the grooves are both larger than the particle size of silica sand in the silica sand layer 12.
In this or other embodiments, the heat exchanger 133 includes a refrigeration box 135, the output pipe of the LNG pump 132 is connected to a refrigeration pipe (not shown) of the refrigeration box 135, the refrigeration pipe is coiled into the refrigeration box 135, the refrigeration pipe is connected to the recovery bottle 134, and the reaction kettle 1 is located in the refrigeration box 135. Utilize a large amount of cold energy of LNG self to provide the refrigeration volume to refrigeration case 135 to reach and carry out refrigerated effect to reation kettle 1, let in after the refrigeration and retrieve in retrieving bottle 134 and retrieve. This refrigeration case 135 is, for example, a water bath case or a water bath jacket, and performs refrigeration using water as a medium, and since the specific heat capacity of water is large, the utilization rate of cold energy can be greatly improved, and it is helpful to keep the temperature constant.
In other embodiments, the heat exchanger 133 includes a vaporizer and a refrigeration box, two ends of the vaporizer are respectively connected to the LNG pump 132 and the recovery bottle 134, the vaporizer is connected to the refrigeration box, LNG is vaporized by the vaporizer to become natural gas, and the natural gas is recovered to the recovery bottle, and the reaction kettle 1 is placed in the refrigeration box, so as to achieve the effect of refrigerating the reaction kettle. LNG is introduced to release a large amount of cold energy, so that a better refrigeration effect is achieved.
In other embodiments, this refrigeration case can also be water bath and press from both sides the cover, and the water bath is pressed from both sides the cover in reation kettle 1 periphery, lets in LNG through the LNG pump, utilizes the LNG cold energy to provide the refrigerating output to reation kettle to reach the effect of carrying out the refrigeration to reation kettle 1.
The recovery bottle 134 in this embodiment is used to collect the gasified natural gas, and may also be used to directly connect the gasified natural gas to a domestic natural gas pipeline.
In this embodiment or other embodiments, the reaction kettle 1 is provided with a monitoring device 151, and the monitoring device 151 at least includes a pressure sensor and a temperature sensor (both shown in the figure).
The monitoring device 151 in this case also comprises a data processing device (not shown in the figures) which processes the data collected by the pressure sensor and the temperature sensor, converts them into readable data and displays them. The data processing device is a device having data processing capability, such as a microcomputer, a mobile phone, or an industrial personal computer.
According to the present embodiment, the system and the method for producing propane hydrate can greatly shorten the induction time of propane hydrate, improve the gas absorption rate, and increase the amount of hydrate produced in a certain period of time.
Example two
According to a second aspect of the present invention, there is provided a method for producing a propane hydrate using the above-described system for producing a propane hydrate, comprising the steps of:
the method comprises the following steps: mixing cyclopentane with a salt solution to form a cyclopentane mixed solution, wherein the mole mass percentage of cyclopentane in the cyclopentane mixed solution is 1.0-5.0 mol%;
step two: injecting the cyclopentane mixed solution into a reaction kettle and enabling the cyclopentane mixed solution to just submerge a silica sand layer of the reaction kettle, wherein the height of the cyclopentane mixed solution is consistent with the thickness of the silica sand layer, the thickness of the silica sand layer is 1.5-5.0cm, and the particle size of silica sand in the silica sand layer is 100-500 μm;
in the step, the reaction kettle needs to be evacuated in advance, and then the cyclopentane mixed solution is injected into the reaction kettle, so that the formation of the hydrate is prevented from being influenced by the existence of other gas impurities in the reaction kettle.
Step three: opening a pressure reducing valve and a delivery pump to inject the propane gas into the reaction kettle until the pressure in the reaction kettle reaches a set pressure, wherein the set pressure is 0.5-2 MPa;
step four: and opening the LNG pump to enable the LNG to refrigerate the reaction kettle through the refrigeration box, monitoring the temperature and the pressure in the reaction kettle in real time, keeping the temperature range between 2 ℃ and 5 ℃ until the temperature and the pressure in the reaction kettle are stabilized to be within the generation range, and completing the generation of the propane hydrate.
And B, adding cyclopentane into a 3 wt% salt solution for sufficient mixing in a blending process to obtain a cyclopentane mixed solution with the mole mass percent of cyclopentane being 1.0mol-5.0 mol%.
In the embodiment, cyclopentane is a good hydrate accelerant, is insoluble in water, can generate a hydrate under the atmospheric pressure above the freezing point, the required generation condition is easy to reach, and the cyclopentane is added in the generation process of the propane hydrate to make the phase equilibrium condition of the hydrate move towards the low pressure and high temperature direction. The existence of silica sand increases the contact between gas and water molecules, and the water molecules are dispersed among silica sand particle pores during the generation of the hydrate, thereby promoting the migration and capillary movement of water in the silica sand and accelerating the nucleation of the hydrate. Because the pore diameter of the silica sand particles is smaller, the smaller particles have larger edges and surfaces, and therefore more sites are provided to further promote hydrate nucleation and shorten the induction time.
EXAMPLE III
In the embodiment, the filling thickness of the silica sand layer is 1.5cm, and the particle size of the silica sand used in the silica sand layer is 100 μm. After the cyclopentane mixed solution is prepared, the molar mass percentage of cyclopentane is 1.0 mol%, 3.0 mol% and 5.0 mol%, and through experimental comparison, the influence of the molar mass percentage of cyclopentane on the formation of propane hydrate is shown in the following table:
table 1: influence of the molar mass percentage of cyclopentane on the formation of propane hydrate
As can be seen from table 1: under the condition of keeping other parameters unchanged, when the mole mass percent of cyclopentane is 3.0 mol%, the induction time is shortest and the gas absorption rate is best. When the molar mass of cyclopentane is 1 mol%, the hydrate induction time is long, the gas absorption rate is low, hydrate crystals suitable for experiments cannot be obtained, and the generated hydrate crystals are not enough. When the molar mass of the cyclopentane is 5 mol%, hydrate crystals aggregate to form slurry similar to a solid phase, further generation of the hydrate is hindered, and the generation amount of the hydrate is reduced.
Example four
In this embodiment, after the cyclopentane mixed solution is prepared, the molar mass percentage of cyclopentane is 3.0 mol%, and the particle size of silica sand used in the silica sand layer is 6 μm. The effects on the formation of propane hydrate when the packing thickness of the silica sand layer was 1.5cm, 3.5cm and 5cm, respectively, are shown in the following table:
table 2: effect of silica sand pack thickness on propane hydrate formation
As can be seen from table 2: under the condition of keeping other parameters unchanged, when the thickness of the silica sand layer is 1.5cm, the induction time is shortest, the gas absorption rate is optimal, water dispersed among the silica sand is absorbed into a gas phase to a hydrate growth area, the hydrate nucleation can be accelerated, the hydrate growth is accelerated, and a large amount of hydrates are generated. When the filling thickness is 3.0cm and 5.0cm, water molecules dispersed in the silica sand with lower depth do not participate in the generation of hydrate, and the generation amount of the hydrate is not greatly increased; when the thickness of the silica sand layer is less than 1.5cm, the hydrate generation amount is less because the water dispersed among the silica sand is less, and the requirement of large-scale production cannot be met.
EXAMPLE five
In this embodiment, after the blending of the cyclopentane mixed solution, the molar mass percentage of cyclopentane is 3.0 mol%, the filling thickness of the silica sand layer is 1.5cm, and when the particle size of the silica sand used in the silica sand layer is 50 μm, 100 μm, 300 μm, 500 μm, the effect on the formation of propane hydrate is shown in the following table:
table 3: influence of particle size of silica sand used for silica sand layer on formation of propane hydrate
As can be seen from table 3: when the particle size of the silica sand used in the silica sand layer is 100 μm, the induction time is shortest, the gas absorption rate is optimal, the pore diameter of the silica sand particles is smaller, the smaller particles have larger edges and surfaces, the surface contact area of the gas phase and the liquid phase is further increased, and therefore more positions are provided for further promoting hydrate nucleation and shortening the induction time.
As the silica sand particle size increases, the surface contact area of the gas phase and the liquid phase decreases, the sites required for hydrate nucleation decrease, and thus the induction time becomes longer. And with the particle size less than 100 μm, gas and solution cannot effectively and completely permeate into the silica sand layer due to the undersized gaps among the silica sand particles, so that the induction time and the gas absorption rate are influenced.
Although some specific embodiments of the present invention have been described in detail by way of examples, it should be understood by those skilled in the art that the above examples are for illustrative purposes only and are not intended to limit the scope of the present invention. It will be appreciated by those skilled in the art that modifications may be made to the above embodiments without departing from the scope and spirit of the invention. The scope of the invention is defined by the appended claims.
Claims (8)
1. A generation system of propane hydrate comprises a generation device and a refrigeration device, and is characterized in that the generation device comprises a reaction kettle and a propane gas tank, the propane gas tank is communicated to the reaction kettle through a delivery pump, a pressure reducing valve and a gas flowmeter are arranged between the propane gas tank and the delivery pump, the delivery pump is communicated to the top of the reaction kettle, a silica sand layer is laid at the bottom of the reaction kettle, and the silica sand layer is immersed into a cyclopentane mixed solution; refrigerating plant is including the LNG storage tank, LNG pump, heat exchanger and the recovery bottle that connect gradually, heat exchanger is arranged in gasifying LNG and becomes the natural gas and retrieves in the recovery bottle.
2. The propane hydrate generation system of claim 1, wherein a gas collection bottle is communicated with the top of the reaction kettle, and a gas flow meter is arranged between the gas collection bottle and the reaction kettle.
3. The propane hydrate generation system according to claim 2, wherein the bottom of the inner wall of the reaction kettle is provided with a micro-rib structure, and the height of the micro-rib structure is not lower than the thickness of the silica sand layer.
4. A propane hydrate generation system as claimed in claim 3, wherein the heat exchanger comprises a refrigeration tank, the output pipe of the LNG pump communicates into refrigeration pipes of the refrigeration tank, the refrigeration pipes are coiled into the refrigeration tank, the refrigeration pipes communicate to the recovery bottle, and the reaction vessel is located in the refrigeration tank.
5. The propane hydrate generation system of claim 1, wherein the reaction kettle is provided with a monitoring device, and the monitoring device at least comprises a pressure sensor and a temperature sensor.
6. A method for producing a propane hydrate using the system for producing a propane hydrate according to any one of claims 1 to 5, comprising the steps of:
the method comprises the following steps: mixing cyclopentane with a salt solution to form a cyclopentane mixed solution, wherein the mole mass percentage of cyclopentane in the cyclopentane mixed solution is 1.0-5.0 mol%;
step two: injecting the cyclopentane mixed solution into a reaction kettle and enabling the cyclopentane mixed solution to be just immersed on a silica sand layer of the reaction kettle, wherein the thickness of the silica sand layer is 1.5-5.0cm, and the particle size of silica sand in the silica sand layer is 100-500 mu m;
step three: opening a pressure reducing valve and a delivery pump to inject the propane gas into the reaction kettle until the pressure in the reaction kettle reaches a set pressure, wherein the set pressure is 0.5-2 MPa;
step four: and opening the LNG pump to enable the LNG to provide refrigerating capacity for the reaction kettle through the refrigerating box, and monitoring the temperature and the pressure in the reaction kettle in real time until the temperature and the pressure in the reaction kettle are within a stable range.
7. The method for producing a propane hydrate according to claim 5, wherein the molar mass percentage of cyclopentane in the mixed solution of cyclopentane is 3.0 mol%.
8. The method for producing propane hydrate according to claim 5, wherein the silica sand layer has a packing thickness of 1.5cm, and the silica sand used for the silica sand layer has a particle size of 100 μm.
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