CN118164439A - SF (sulfur hexafluoride) improvement6Method for forming hydrate rate - Google Patents
SF (sulfur hexafluoride) improvement6Method for forming hydrate rate Download PDFInfo
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- CN118164439A CN118164439A CN202410355285.4A CN202410355285A CN118164439A CN 118164439 A CN118164439 A CN 118164439A CN 202410355285 A CN202410355285 A CN 202410355285A CN 118164439 A CN118164439 A CN 118164439A
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- 229910018503 SF6 Inorganic materials 0.000 title description 2
- SFZCNBIFKDRMGX-UHFFFAOYSA-N sulfur hexafluoride Chemical compound FS(F)(F)(F)(F)F SFZCNBIFKDRMGX-UHFFFAOYSA-N 0.000 title description 2
- 229960000909 sulfur hexafluoride Drugs 0.000 title description 2
- DBMJMQXJHONAFJ-UHFFFAOYSA-M Sodium laurylsulphate Chemical compound [Na+].CCCCCCCCCCCCOS([O-])(=O)=O DBMJMQXJHONAFJ-UHFFFAOYSA-M 0.000 claims abstract description 39
- 238000000034 method Methods 0.000 claims abstract description 36
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 32
- 229920005573 silicon-containing polymer Polymers 0.000 claims abstract description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 230000003068 static effect Effects 0.000 claims abstract description 10
- 239000007864 aqueous solution Substances 0.000 claims abstract description 7
- DAJSVUQLFFJUSX-UHFFFAOYSA-M sodium;dodecane-1-sulfonate Chemical compound [Na+].CCCCCCCCCCCCS([O-])(=O)=O DAJSVUQLFFJUSX-UHFFFAOYSA-M 0.000 claims abstract description 3
- 238000010494 dissociation reaction Methods 0.000 claims description 6
- 230000005593 dissociations Effects 0.000 claims description 6
- 239000013530 defoamer Substances 0.000 claims description 5
- 239000012141 concentrate Substances 0.000 claims description 4
- 239000007789 gas Substances 0.000 abstract description 72
- 239000000243 solution Substances 0.000 abstract description 17
- 238000000926 separation method Methods 0.000 abstract description 9
- 238000011084 recovery Methods 0.000 abstract description 6
- 238000010907 mechanical stirring Methods 0.000 abstract description 4
- 238000004134 energy conservation Methods 0.000 abstract description 3
- 239000005431 greenhouse gas Substances 0.000 abstract 1
- 230000002195 synergetic effect Effects 0.000 abstract 1
- 239000006260 foam Substances 0.000 description 12
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- 230000000052 comparative effect Effects 0.000 description 9
- 238000002425 crystallisation Methods 0.000 description 8
- 230000008025 crystallization Effects 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- 150000004677 hydrates Chemical class 0.000 description 6
- 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 6
- 239000000203 mixture Substances 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 5
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- 238000002347 injection Methods 0.000 description 5
- 239000007924 injection Substances 0.000 description 5
- 238000003756 stirring Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 4
- 238000004401 flow injection analysis Methods 0.000 description 4
- 238000005259 measurement Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000000634 powder X-ray diffraction Methods 0.000 description 4
- 238000005057 refrigeration Methods 0.000 description 4
- 238000010792 warming Methods 0.000 description 4
- 239000002518 antifoaming agent Substances 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000002826 coolant Substances 0.000 description 3
- 230000001186 cumulative effect Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000011010 flushing procedure Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- 238000013019 agitation Methods 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
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- 239000000463 material Substances 0.000 description 2
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- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- WSNMPAVSZJSIMT-UHFFFAOYSA-N COc1c(C)c2COC(=O)c2c(O)c1CC(O)C1(C)CCC(=O)O1 Chemical compound COc1c(C)c2COC(=O)c2c(O)c1CC(O)C1(C)CCC(=O)O1 WSNMPAVSZJSIMT-UHFFFAOYSA-N 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 239000004642 Polyimide Substances 0.000 description 1
- 238000002441 X-ray diffraction Methods 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
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- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 230000006698 induction Effects 0.000 description 1
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- 238000009413 insulation Methods 0.000 description 1
- 230000001678 irradiating effect Effects 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
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- 238000010899 nucleation Methods 0.000 description 1
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- 239000002245 particle Substances 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a method for improving the formation rate of SF 6 hydrate, and belongs to the technical field of gas recovery. The invention comprises the following steps: SF 6 gas is injected into an aqueous solution containing sodium dodecyl sulfonate and active silicone polymer at a certain temperature, and forms SF 6 hydrate with water under a static system. The method adopts the aqueous solution containing sodium dodecyl sulfate and active silicone polymer, obviously accelerates the formation rate of SF 6 hydrate through the synergistic effect of the sodium dodecyl sulfate and the active silicone polymer, simultaneously does not generate bubbles, and has no structural influence on the formation of SF 6 hydrate; the process can be performed under a static system without additional mechanical stirring, has the advantages of energy conservation and high efficiency, provides a feasible solution for the high-efficiency separation and recovery of SF 6, and has important significance for protecting the global environment and reducing the emission of greenhouse gases.
Description
Technical Field
The invention relates to the technical field of gas recovery, in particular to a method for improving the formation rate of SF 6 hydrate.
Background
SF 6 gas is widely used in gas insulated switchgear, particle accelerators in medical and industrial fields, etc., and has excellent insulation properties. However, since SF 6 is a global warming gas whose global warming coefficient is 23900 times greater than that of carbon dioxide, reducing the emission of SF 6 has an important meaning for improving the global warming problem.
Various gases with lower global warming coefficients have been proposed to replace SF 6, the most effective alternative being a mixture of SF 6-N2 containing 50% to 60% SF 6, with a mixture of SF 6-N2 being the most economical. And for the recovery of the mixture SF 6 after use. Compared with the traditional liquefaction, adsorption and membrane separation methods, the separation of sulfur hexafluoride (SF 6) based on hydrate from the gas mixture is a novel SF 6 separation and recovery method, has the advantages of low operating pressure, low cost for recovering target gas, low energy consumption and the like, and is one of the most promising means for recovering and separating SF 6. Gas hydrates are often formed by magnetic or mechanical agitation to maximize the surface area between the gas and water, but this method consumes a lot of energy and takes a very long time.
Chinese patent application publication No. CN102711962a discloses accelerated hydrate formation and dissociation, using gas hydrates to separate a specific gas from a gas mixture. Hydrates of the compounds are formed from the mixed gas feed to concentrate one or more desired gas species in the hydrate phase and the remainder in the gas phase. Next, the hydrates are separated from the gas phase and dissociated to produce a gas stream enriched in the desired material. Additives to accelerate the growth of the hydrates and defoamers are added to alter the reaction rate and eliminate the difficultly ruptured foam caused by the catalyst to increase the overall throughput of the process. The addition of some materials can result in a change in hydrate product density, which can be used to optimize separation of the hydrate from unreacted liquid and/or discarded gas. The application states that the addition of a specific class of defoamer maintains the activity of the catalyst while greatly reducing the impact of the foam. At the same time, the combination of a suitable catalyst and a suitable defoamer increases the rate of hydrate formation and its controllable dissociation and makes the gas production flow suitable for industrial processes.
The invention points out that methane, ethane, propane, carbon dioxide, hydrogen sulfide and nitrogen can be used as hydrate forming gas, and the implementation of methane, ethane and propane gas is verified. Based on the above principle, it seems to be a theoretically possible solution to use the above process for increasing the rate of formation of SF 6 hydrate. However, the inventors have found in practice that the formation of SF 6 hydrate in a stirred reactor (as in the case of the above-mentioned application in which the hydrocarbons are present in the gas mixture reacted in the stirred reactor are present in the presence of 300ppm of accelerator) does not meet the commercial application requirements. This depends mainly on two points, firstly the gas and the type of surfactant, defoamer; secondly, the SF 6 hydrate has the problems of difficult processing and low production rate under the prior art process conditions, which are not consistent with the expected results.
In summary, a new energy-saving and efficient process is sought to increase the formation rate of SF 6 hydrate to meet the commercialization requirements, which is of great importance in reducing the emission and recycling of SF 6.
Disclosure of Invention
In view of the foregoing drawbacks of the prior art, in a first aspect of the present invention, there is provided an energy-saving and efficient method for increasing the rate of formation of SF 6 hydrate, comprising the steps of:
SF 6 gas is injected into an aqueous solution containing sodium dodecyl sulfonate and active silicone polymer at a certain temperature, and forms SF 6 hydrate with water under a static system.
The static system refers to a form that the aqueous solution is not stirred by external force or can achieve similar effect in the process of forming the hydrate.
Preferably, the temperature is 276.9-279.9K.
Preferably, the concentration of the sodium dodecyl sulfate is 100-500 ppm.
Further preferably, the concentration of the sodium dodecyl sulfate is 250ppm.
Preferably, the reactive silicone polymer is Sigma a5633 Antifoam A Concentrate defoamer a 100G.
Preferably, the concentration of the reactive silicone polymer is 1000 to 10000ppm.
It is further preferred when the concentration of the reactive silicone polymer is 1500ppm.
The gas injection is preferably carried out under a suitable gas pressure, which is favorable for balancing the increase of the hydrate generation rate and the energy consumption required for maintaining the gas pressure; at the same time, the constant pressure injection helps to prevent fluctuation caused by pressure change, so that the reaction proceeds to the direction of hydrate generation.
Preferably, the SF 6 gas is injected at a constant pressure, and the gas pressure is 0.9-1.1 MPa.
Preferably, the temperature is raised to 291-297K to dissociate the SF 6 hydrate.
The formation and dissociation of SF 6 hydrate, as demonstrated in one or more embodiments of the present invention, is performed using gas hydrate generation equipment commonly used in the art. Injecting gas by a micro-flow injection pump under the control of temperature and air pressure, and generating hydrate in a crystallization tank; and then the temperature is regulated by a refrigeration cycle controller to dissociate the gas hydrate, so that the separation and recovery of SF 6 are completed.
The inventors found that the reason why the prior art is not suitable for commercial application when applied to SF 6 is that the process maintains a dynamic mass transfer process of the gas-liquid two phases by continuously updating the gas-liquid interface through mechanical stirring, enabling continuous growth of the hydrates and obtaining a considerable gas consumption. However, as SF 6 hydrate slurry is formed, the energy consumption required to maintain a certain stirring rate increases, and the amount of static water contained in the hydrate formed by stirring increases, resulting in low hydrate gas storage density and increased hydrate storage and transportation costs. The high energy consumption and low rate render these methods non-commercial.
The structural characteristics of the hydrate are that water molecules are connected through hydrogen bonds to form polyhedral cage holes with specific structures and sizes, the cage holes can contain gas molecules with equivalent sizes, molecules with too large sizes cannot enter, and molecules with too small sizes cannot exist in the polyhedral cage holes stably, namely the hydrate has certain selectivity to different types of molecules. In addition, under a static system, the generation of SF 6 hydrate is difficult because the hydrate film generated at the gas-liquid interface obstructs the dynamic mass transfer process of the gas-liquid two phases. The idea of the present invention is therefore to select sodium dodecyl sulfate as kinetic hydrate promoter, in combination with active silicone polymer, to allow SF 6 hydrate to grow at high speed without any mechanical agitation.
The principle of the invention is that SF 6 is selected to be combined with sodium dodecyl sulfate and active silicone polymer, so that the induction time is shortened, the nucleation is accelerated, and the phase equilibrium rate and the final conversion rate are improved. The formed hydrate grows into a porous structure on the wall of the reactor, and liquid is absorbed from the body to the crystallization front due to capillary force, and is updated at the gas-liquid interface to form SF 6 hydrate. The process is carried out under a static system, does not depend on mechanical stirring, solves the problems of high energy consumption and low gas storage density of the hydrate required by stirring, and realizes the efficient generation of the SF 6 hydrate.
Compared with the prior art, the invention has the following advantages and beneficial effects:
The invention provides a method for improving the formation rate of SF 6 hydrate, which adopts an aqueous solution containing sodium dodecyl sulfate and an active silicone polymer, can be performed under a static system without additional mechanical stirring, and has the advantages of energy conservation and high efficiency.
Drawings
FIG. 1 is a graph showing the cumulative amounts of SF 6 gas consumed over time for example 1, example 3, and comparative group 1;
Fig. 2 is a PXRD diffractogram of SF 6 hydrate from example 3 and comparative group 2.
Detailed Description
The invention is further illustrated by means of the following examples, which are not intended to limit the scope of the invention. The experimental methods, in which specific conditions are not noted in the following examples, were selected according to conventional methods and conditions, or according to the commercial specifications.
In the following examples:
the reactive silicone polymer was antifoam A100G using Sigma A5633 Antifoam A Concentrate.
Example 1
In order to effectively utilize the kinetic promotion effect of Sodium Dodecyl Sulfate (SDS), the influence of the concentration of SDS on the process was investigated in this example, and the steps are as follows:
(1) Adding SDS solution with set concentration into a crystallization tank;
(2) The temperature control unit is opened, so that the coolant liquid is kept at a constant experimental temperature of 279.7K, and the temperature in the crystallizer tank is ensured;
(3) The vacuum pump is opened, the vacuum pumping operation is carried out on the crystallization tank, and then SF 6 gas is used for flushing for at least 3 times, so that the interference of residual gas in the device on experiments is prevented;
(4) Opening an air inlet valve, introducing raw material gas, namely SF 6 gas, into the hydrate gas separation device, and maintaining an isobaric condition by using a constant pressure mode of a micro-flow injection pump, wherein the gas pressure is 1Mpa;
(5) The volume of gas consumed during formation of SF 6 hydrate was measured using a microfluidic injection pump and then converted to moles of gas consumed per mole of water charged to the high pressure cell; measuring the gas absorption of the SDS solution with set concentration in the SF 6 hydrate formation process;
(6) After the gas is no longer absorbed, the residual gas is removed by a vacuum pump and the refrigeration cycle controller is set to 293K to decompose SF 6 gas hydrate in the vessel.
The set concentrations of SDS solutions selected in this example were 100, 250, 500ppm, respectively.
For comparison, SF 6 gas hydrate was prepared with pure water (i.e., SDS concentration of 0 ppm) as comparative group 1, as follows:
(1) Adding SDS solution with set concentration into a crystallization tank;
(2) The temperature control unit is opened, so that the coolant liquid is kept at a constant experimental temperature of 279.7K, and the temperature in the crystallizer tank is ensured;
(3) The vacuum pump is opened, the vacuum pumping operation is carried out on the crystallization tank, and then SF 6 gas is used for flushing for at least 3 times, so that the interference of residual gas in the device on experiments is prevented;
(4) For pure water, the stirrer is turned on to run at 500rpm to increase the driving force for hydrate formation while avoiding icing;
(5) Opening an air inlet valve, introducing raw material gas, namely SF 6, into the hydrate gas separation device, and maintaining an isobaric condition by using a constant pressure mode of a micro-flow injection pump, wherein the gas pressure is 1Mpa;
(6) The volume of gas consumed during formation of SF 6 hydrate was measured using a microfluidic injection pump and then converted to moles of gas consumed per mole of water charged to the high pressure cell; measuring the gas absorption of the SDS solution with set concentration in the SF 6 hydrate formation process;
(7) After the gas is no longer absorbed, the residual gas is removed by a vacuum pump and the refrigeration cycle controller is set to 293K to decompose SF 6 gas hydrate in the vessel.
FIG. 1 shows the cumulative amount of SF 6 gas consumed during hydrate formation in SDS solutions of different concentrations (0, 100, 250, 500 ppm) over time. As shown in fig. 1, the addition of SDS significantly accelerates the rate of formation of SF 6 hydrate. For pure water, the rate of formation of SF 6 hydrate was very slow at the initial stage, suddenly increased at about 300min, and then smoothed at 400min, whereas for SDS solution, gas consumption was severe even at the initial stage, and then completed at about 120 min. Finally, the final gas absorption of pure water and SDS solution was almost the same. The hydrate promotion effect of SDS250ppm is better than that of SDS100ppm, which is equivalent to SDS 500 ppm. In addition, the amount of foam generated during the dissociation of the hydrate is proportional to the SDS concentration. Considering that the kinetic promoting effect and the foam generating amount depend on the SDS concentration, 250ppm was suitably selected as the optimal SDS concentration of SF 6 hydrate.
Example 2
This example investigated the effect of the concentration of active silicone polymer (AAC) at the preferred SDS concentration on the process, as follows:
(1) Preparing the desired AAC sum and sealable vials;
(2) Adding an appropriate amount of AAC reagent, SDS reagent and water to a container, and preparing a vial containing SDS (250 ppm) and AAC (0, 1000, 1500, 2000, 2500, 5000 and 10000 ppm) solutions;
(3) The same shaking or stirring is carried out on each mixed solution bottle, and the foam amount generated after each mixed solution is shaken is observed;
(4) The foam generation at each AAC concentration was recorded, and the foam generation inhibitory effect of the AAC concentration was determined.
Through the above steps, it was found that the SDS solution produced the most amount of foam without AAC (0 ppm), while the addition of AAC greatly reduced foam formation. The amount of foam generally decreases with increasing AAC concentration, with AAC exceeding 1500ppm almost suppressing foam formation. In view of the minimum requirements of AAC for the same performance, a 250ppm SDS solution is suitable to incorporate AAC at a concentration of 1500 ppm.
Example 3
A method for increasing the rate of formation of SF 6 hydrate comprising the steps of:
(1) Adding 250ppm SDS and 1500ppm ACC water solution into a crystallization tank;
(2) The temperature control unit is opened, so that the coolant liquid is kept at a constant experimental temperature of 279.7K, and the temperature in the crystallizer tank is ensured;
(3) The vacuum pump is opened, the vacuum pumping operation is carried out on the crystallization tank, and then SF 6 gas is used for flushing for at least 3 times, so that the interference of residual gas in the device on experiments is prevented;
(4) Opening an air inlet valve, introducing raw material gas, namely SF 6, into the hydrate gas separation device, and maintaining an isobaric condition by using a constant pressure mode of a micro-flow injection pump, wherein the gas pressure is 1Mpa;
(5) The volume of gas consumed during formation of SF 6 hydrate was measured using a microfluidic injection pump and then converted to moles of gas consumed per mole of water charged to the high pressure cell; measuring the gas absorption of the SDS solution with set concentration in the SF 6 hydrate formation process;
(6) After the gas is no longer absorbed, the residual gas is removed by a vacuum pump and the refrigeration cycle controller is set to 293K to decompose SF 6 gas hydrate in the vessel.
The cumulative amounts of SF 6 gas consumed in the hydrate formation process at 250ppm SDS and 1500ppm ACC over time are shown in FIG. 1. The combination of SDS and ACC accelerates the formation rate of SF 6 hydrate, and the foam amount produced under a static water system is not affected.
Comparative group 2 was prepared by the same procedure without SDS and ACC. The crystal structure of the hydrate of SF 6 formed in this example and comparative example 2 was measured using PXRD to determine whether SDS and AAC would have an effect on the structure of SF 6 hydrate formation. The specific experimental steps are as follows:
S1, acquiring SF 6 hydrate samples, including a pure hydrate sample (comparative group 2) and a hydrate sample added with SDS and AAC;
S2, placing the hydrate sample into a liquid nitrogen container, and finely grinding the sample by using a 50 mu m screen to prevent hydrate dissociation; loading the finely ground hydrate sample into a precooled polyimide tube to maintain the stability of the sample;
S3, performing X-ray diffraction analysis measurement at low temperature (133K), and using X-rays (12.658 keV with a wavelength of 0.9795) with specific energy ) Irradiating the sample; the measurement is carried out by using a 2D CCD detector, the measurement time of a comparative group 2 sample is 60s, and the measurement time of an SF 6 hydrate sample formed in the embodiment is 100s;
S4, converting the acquired two-dimensional PXRD diagram into a one-dimensional diffraction diagram, and analyzing the one-dimensional diffraction diagram to determine the crystal structure of the hydrate.
Fig. 2 is a PXRD diffractogram of SF 6 hydrate of example 3 versus comparative group 2. FIG. 2 shows that the SF 6 hydrate structure formed by the comparative group (pure water) and the present example (SDS 250ppm+AAC 1500ppm solution) is of cubic structure II and the lattice parameter is 17.09. This indicates that neither SDS nor AAC is embedded in the hydrate cage and has no effect on the structure of the hydrate.
The results of the above examples show that the method adopts the aqueous solution containing sodium dodecyl sulfate and active silicone polymer, greatly increases the formation speed of SF 6 hydrate without stirring, has no influence on the formation structure of SF 6 hydrate, and has the advantages of energy conservation and high efficiency.
The foregoing describes in detail preferred embodiments of the present invention. It should be understood that numerous modifications and variations can be made in accordance with the concepts of the invention by one of ordinary skill in the art without undue burden. Therefore, all technical solutions which can be obtained by logic analysis, reasoning or limited experiments based on the prior art by the person skilled in the art according to the inventive concept shall be within the scope of protection defined by the claims.
Claims (8)
1. A method for increasing the rate of formation of SF 6 hydrate comprising the steps of:
SF 6 gas is injected into an aqueous solution containing sodium dodecyl sulfonate and active silicone polymer at a certain temperature, and forms SF 6 hydrate with water under a static system.
2. The method according to claim 1, characterized in that: the temperature is 276.9-279.9K.
3. The method according to claim 1, characterized in that: the concentration of the sodium dodecyl sulfate is 100-500 ppm.
4. The method according to claim 1, characterized in that: the reactive silicone polymer was Sigma a5633Antifoam A Concentrate defoamer a 100G.
5. The method according to claim 1, characterized in that: the concentration of the active silicone polymer is 1000-10000 ppm.
6. The method according to claim 1, wherein: the concentration of sodium dodecyl sulfate was 250ppm and the concentration of the active silicone polymer was 1500ppm.
7. The method according to claim 1, wherein: and injecting SF 6 gas at constant pressure, wherein the gas pressure is 0.9-1.1 MPa.
8. The method according to claim 1, wherein: raising the temperature to 291-297K causes dissociation of the SF 6 hydrate.
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