WO2011090229A1 - 신속한 가스 수화물 제조 방법 - Google Patents
신속한 가스 수화물 제조 방법 Download PDFInfo
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- WO2011090229A1 WO2011090229A1 PCT/KR2010/000448 KR2010000448W WO2011090229A1 WO 2011090229 A1 WO2011090229 A1 WO 2011090229A1 KR 2010000448 W KR2010000448 W KR 2010000448W WO 2011090229 A1 WO2011090229 A1 WO 2011090229A1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
- B01J10/002—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor carried out in foam, aerosol or bubbles
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/108—Production of gas hydrates
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
- B01J2219/00027—Process aspects
- B01J2219/00029—Batch processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00054—Controlling or regulating the heat exchange system
- B01J2219/00056—Controlling or regulating the heat exchange system involving measured parameters
- B01J2219/00069—Flow rate measurement
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
- B01J2219/00081—Tubes
Definitions
- the present invention relates to a rapid gas hydrate manufacturing method. More specifically, the present invention relates to a process comprising i) a first step of injecting an aqueous fresh solution containing a potential feed hydrate into a reactor, and ii) a potential seed hydrate of said first step. A second step of pressurizing a gas into the reactor into which the pure aqueous solution is injected, and iii) a third step of injecting a surfactant solution into the reactor into which the gas of the second step is injected; (Fed-batch type) gas hydrate manufacturing method and a batch type gas hydrate manufacturing method in which the order of the first step and the third step is changed.
- Natural gas is a fuel with cleanliness, stability, and convenience, and has been spotlighted as an alternative energy for solid fuels such as petroleum and coal, and its use in many fields such as home, commerce, transportation, and industry has been increasing. As an energy source that supplies a quarter, it forms the basis of the global energy industry along with solid fuels such as petroleum and coal.
- Liquefied Natural Gas A method of storing and transporting in a dedicated tank installed on the back has been mainly used.
- Liquefied natural gas usually contains 600 times the volume of natural gas per unit volume.
- methane gas which is a major component of liquefied natural gas (LNG)
- LNG liquefied natural gas
- Compressed gas is used as another natural gas storage and transportation method, but it is also difficult to manufacture a large container due to high storage pressure, which is technically difficult and expensive, and has a problem of safety due to high pressure explosion. .
- natural gas hydrates are produced at relatively moderate pressure and temperature (40 bar at 3 ° C) while providing 170 times the volume of gas per unit volume. Is done. These temperature and pressure conditions are much milder than those of liquefied natural gas and compressed gas.
- natural gas hydrate is advantageous because it is unlikely to explode even when exposed to room temperature and atmospheric pressure, thereby ensuring sufficient time to replace the leakage and breakage of the system. That is, natural gas hydrates are safer and economical to store and transport than LNG (liquefied natural gas) or CNG (compressed natural gas).
- Natural gas hydrate is a compound produced by the physical combination of gas and water at low temperature and high pressure, rather than chemical bonding, like dry ice.
- the calorific value of 1 m3 of gas hydrate is about 180m3 It is similar to the calorific value of gas.
- water and gas are buried in low temperature and high pressure undersea or frozen earth, which are easily decomposed into water and gas under dissociation conditions.
- Natural gas hydrates are classified into type I, type II, type ⁇ , etc. according to their molecular structure, and are similar in appearance to ice but have a different structure from ice. Ice has a two-dimensional planar structure at low temperatures near 0 ° C, whereas water molecules form a three-dimensional cavity structure when natural gas hydrate is given the appropriate pressure (20-40 bar).
- the size of a single pupil is about 1 nanometer and the unit cell size is about 2 nanometers, and natural gas enters the inside of the pupil.
- water molecules connected by hydrogen bonds become 'hosts' and gas molecules become 'guests'.
- the general formula of the gas hydrate is Gas (H 2 O) n where n is a hydration number, which has a value of about 5 to 8 depending on the size of the gas molecules. Van der Waals forces act between the nonpolar gas molecules and the water molecules.
- a general method for producing natural gas hydrate is to generate natural gas hydrate by contacting water injected through a high pressure cooled natural gas supplied through a gas nozzle installed at the top of the reactor or a porous plate installed at the bottom of the reactor. Bubbling is the most common method, and since the entire reaction is exothermic, a cooling system is installed in the reactor or a system for lowering the temperature of the reactor from the outside to remove heat generated during the reaction.
- this method has the disadvantage that the generated natural gas hydrate can cause plugging in the raw water or the natural gas injection nozzle, and when the spray plate is used, the mass transfer resistance is large due to the large diameter of the generated raw water particles. It is difficult to separate the generated natural gas hydrate and the unreacted water, and due to the low conversion rate, the amount of unreacted is high, which requires a lot of energy for the separation and reuse process.
- the existing natural gas hydrate production method has a problem in industrialization due to long hydrate induction time and low hydrate crystal growth rate.
- the hydrate induction period may be defined as a period of time maintained in a meta-stable liquid state before the formation of solid gas hydrate crystal grains, and methane hydrate induction time is usually several days.
- nucleation derivation of hydrate crystals
- rapid derivation does not occur consistently and repeatedly even with the same experimental conditions and surfactant concentrations, and affects various factors such as impurities in aqueous solution, external vibration, and cooling method. Will receive.
- the present invention utilizes a small amount of potential seed hydrate solution capable of forming seed hydrate particles to produce gas hydrates at high crystallization rate without induction period in a reactor with a single external cooling device. It aims to manufacture.
- fed-batch type comprising a second step of injecting a surfactant solution into a reactor into which a pressurize and an aqueous fresh solution containing a seed feed hydrate are simultaneously injected ) Is achieved by providing a method for producing a gas hydrate.
- an object of the present invention is i) a first step of injecting a surfactant solution into the reactor, ii) a second step of pressurizing a gas into the reactor into which the surfactant solution of the first step is injected; And iii) a batch type gas hydrate comprising a third step of injecting an aqueous fresh solution containing potential seed hydrate into the reactor into which the gas of the second step is injected.
- an object of the present invention is i) a first step of injecting gas into the reactor (ii) a second step of injecting a surfactant solution into the reactor into which the gas of the first step is pressurized And iii) a third step of injecting an aqueous fresh solution containing a potential seed hydrate into the reactor into which the surfactant solution of the second step is injected. (batch type) is achieved by providing a method for producing a gas hydrate.
- the present invention is a novel method for rapidly forming gas hydrates from a pure aqueous solution without using the memory effect of water or gas hydrate particles already formed, and using a small amount of potential seed hydrate aqueous solution under relatively mild conditions of pressure and temperature in the reactor. It creates hydrates and simultaneously forms natural gas hydrates on them, allowing for rapid reactions.
- Seed hydrate formation in the reactor takes place at atmospheric pressure or at relatively low pressures below 10 bar at temperatures above the freezing point of water.
- the seed hydrate can form gas hydrates immediately without hydrate induction time with an aqueous solution containing a small amount of surfactant, and the hydrate quickly forms a porous structure along the reactor wall.
- This rapid hydrate manufacturing method can be applied to both batch type and fed-batch type processes.
- Figure 1 shows the structure of the gas hydrate molecules of the si, sII type.
- FIG. 2 is a detailed view of a gas hydrate manufacturing apparatus using the gas hydrate manufacturing method of the present invention.
- the method for producing a fed-batch type gas hydrate of the present invention comprises the following steps: i) a first step of injecting an aqueous fresh solution containing a potential feed hydrate into the reactor, ii) the first A second step of pressurizing the reactor into which the pure aqueous solution containing the potential seed hydrate of the step is injected, and iii) injecting a surfactant solution into the reactor into which the gas of the second step is injected; The third step is made.
- the fed-batch type gas hydrate manufacturing method of the present invention comprises: i) a first step of pressurizing a gas into the reactor, ii) a potential seed hydrate into the reactor into which the gas of the first step is injected ( a second step of injecting an aqueous fresh solution containing a potential feed hydrate, and iii) adding a surfactant solution to a reactor into which a pure aqueous solution containing a potential seed hydrate of said second step is injected.
- the third step is to inject.
- the method for producing a fed-batch type gas hydrate of the present invention includes: i) a first injecting an aqueous fresh solution containing pressurize and seed hydrate into a reactor at the same time; Step ii) injecting a surfactant solution into the reactor into which the first step of pressurize and aqueous fresh solution containing a potential feed hydrate are simultaneously injected; Consists of steps.
- a potential feed hydrate is a compound that can be a seed that forms a hydrate, and a salt that forms sI, sII, sH hydrate formers or semi-clathrate compounds is seed hydrate. This can be
- sI, sII and sH hydrates are classified according to the molecular structure of hydrates, especially type H, which was artificially produced only in laboratories, but has recently been found in a seabed of 200-500 m depth on the west coast of Canada (see FIG.
- a semi-clathrate compound refers to a compound containing a structure in which one molecule creates a three-dimensional network structure and another molecule enters a gap when two molecules are determined together under suitable conditions.
- the seed hydrate solution is tetrahydrofuran (THF), 1,3-dioxolane (1,3-dioxolane), tetrahydropyran, cyclopentane, acetone, difluoro Difluoromethane (HFC-32), isobutane, isobutylene, n-butane, propane, LPG (C3 + C4), methyl Methylcyclohexane, methylcyclopentane, neohexane, methyltertbutyl ether, adamantine, tetra n-butyl ammonium bromide ), Tetra-n-butylammonium fluoride and tetra-nbutylammonium chloride.
- THF tetrahydrofuran
- 1,3-dioxolane 1,3-dioxolane
- tetrahydropyran cyclopentane
- acetone difluor
- sodium dodecyl sulfate SDS
- diisoctyl sodium sulfosuccinate DSS
- sodium tetradecyl sulfate sodium hexadecyl sulfate sodium hexadecyl sulfate
- sodium dodecylbenzene sulfonate xylenesulfonate
- sodium oleate 4-n-decylbenzenesulfonate
- 4-n-decylbenzenesulfonate Sodium laurate
- 4-dodecylbenzenesulfonic acid dodecylamine hydrochloride
- dodecyltrimethylammonium chloride 4-n-octylbenzenesulfonate (4-n-Octylbenzene sulfonate), ethoxylated sulfonate
- the amount of the potential seed hydrate aqueous solution mentioned above is sufficient in a small amount, such as within 5% of the total volume of the surfactant solution.
- the potential seed hydrate solution forms seed hydrate directly with the gas injected in the cooled reactor (eg methane gas 35-100 bar).
- the gas may be introduced before or after the potential aqueous seed hydrate solution is injected into the reactor, or may be injected simultaneously.
- Cooling of the reactor may occur before gas enters the reactor, before the potential seed hydrate aqueous solution enters the reactor, or before the surfactant solution enters the reactor.
- the cooling temperature of the reactor is preferably -5 ° C to 5 ° C, and the pressurized pressure of the injected gas is preferably 10 to 50 bar or more than the equilibrium pressure of the gas hydrate. That is, the reaction is performed at relatively mild temperature and pressure conditions.
- the injected gas may be any gas capable of forming a hydrate such as methane, ethane, propane, carbone dioxide or a mixture thereof.
- the gas hydrate is formed immediately without any induction time.
- the surfactant solution forms a porous gas hydrate that rises along the reactor wall when in contact with the gas, which not only makes the gas easily accessible to the unreacted aqueous solution, but also dissipates the heat of reaction by easily dispersing the gas. This results in an increase in gas storage density and conversion yield.
- the aqueous surfactant solution used at this time is sodium dodecyl sulfate (SDS), diisoctyl sodium sulfosuccinate (DSS), sodium tetradecyl sulfate, sodium hexadecyl sulfate (sodium hexadecyl sulfate, sodium dodecylbenzene sulfonate, xylenesulfonate, sodium oleate, 4-n-decylbenzenesulfonate, sodium lauric Sodium laurate, 4-dodecylbenzenesulfonic acid, dodecylamine hydrochloride, dodecyltrimethylammonium chloride, 4-n-octylbenzenesulfonate (4 -n-Octylbenzene sulfonate, Ethoxylated sulfonate, Decylbenzenesulfonate, Pot
- the gas hydrate manufacturing method of the present invention may be applied to a batch type manufacturing method, and in this case, the batch type gas hydrate manufacturing method of the present invention is i) injecting a surfactant solution into a reactor.
- the batch type gas hydrate manufacturing method of the present invention comprises: i) a first step of injecting a surfactant solution into a reactor, ii) a potential seed in a reactor into which the first step of surfactant solution is injected; A second step of injecting an aqueous fresh solution containing a potential feed hydrate, and iii) pressurizing a gas into a reactor into which a pure aqueous solution containing a potential seed hydrate of said second step is injected; The third step is made.
- the batch type gas hydrate manufacturing method of the present invention comprises: i) a first step of injecting a surfactant solution into a reactor, and ii) a gas into a reactor into which the surfactant solution of the first step is injected.
- the second step is to simultaneously inject a fresh aqueous solution containing pressurize and potential feed hydrate.
- the batch type gas hydrate manufacturing method of the present invention comprises: i) a first step of pressurizing a gas into a reactor, and ii) a surfactant solution in a reactor into which the gas of the first step is pressurized. a second step of injecting a surfactant solution, and iii) injecting an aqueous fresh solution containing a potential feed hydrate into the reactor into which the second solution of the surfactant solution is injected. This is done in a third step.
- the surfactant solution and potential seed hydrate aqueous solution which can be used in the batch gas hydrate manufacturing method are the same as those used in the semibatch production method mentioned above.
- seed hydrate is formed on the first injected surfactant solution.
- a potential aqueous seed hydrate solution entering the reactor forms a seed hydrate with the gas injected in the cooled reactor (eg methane gas 35-100 bar), the seed hydrate is already injected into the reactor.
- the gas hydrate is formed immediately without any induction time with the surfactant present.
- the gas may be introduced before, after, or at the same time as a potential seed hydrate solution is injected into the reactor, and the cooling of the reactor may occur before the gas enters the reactor, before the potential seed hydrate solution enters the reactor, or with a surfactant.
- the solution may be made before entering the reactor.
- the cooling temperature of the reactor is -5 °C to 5 °C
- the pressurized pressure of the injected gas is 10 to 50 bar or more than the equilibrium pressure of the gas hydrate like the semi-batch production method.
- the 2 is an experimental apparatus using the manufacturing method of the present invention, in which gas is supplied from a gas tank 1 through a pipe 3 and a mass flow meter 2 is installed therein so that a gas injection amount according to gas hydrate formation is measured.
- the surfactant solution is supplied to the reactor via the liquid injection line 4 to the high pressure liquid pump 5.
- a gas discharge line 6 hangs on the top of the reactor 9.
- the coolant lines 10 connect the reactor with the cooler 11 to which the temperature controller is attached to lower the temperature of the reactor.
- Table 1 below is an experimental result of using a pure THF solution as the seed hydrate forming solution.
- 0.02 liters of 500 ppm SDS and 4 wt% THF solution are fed to the reactor.
- the reactor temperature is then lowered via an external cooler near 0 ° C. and methane gas is charged to the reactor at 50 bar.
- One liter of 500 ppm SDS aqueous solution is then injected into the reactor to produce a gas hydrate.
- methane gas was stored at a temperature of 173 times at a pressure of 0 ° C and 1 atmosphere per unit volume of methane hydrate.
- methane hydrate was formed on the reaction wall.
- Table 2 shows the results of using a pure CP solution as a seed hydrate forming solution.
- the storage density of methane is somewhat lower than the above experiments, but optimizing the reaction temperature, pressure, liquid injection rate, etc. can maximize gas storage.
- the seed hydrate was formed during the pressurization and cooling process before the SDS aqueous solution was injected, and the gas hydrate was immediately formed while the SDS aqueous solution was injected.
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Abstract
Description
반응기 부피(Reactor Volume) | 5 L |
순수 종자 THF 용액(Fresh Seed THF Solution) | 0.02 L (THF 4wt% + SDS 500ppm) |
메탄 가스 소비(Nm3)(Methane Gas Consumption) | 193 |
액체상 SDS 용액(L)(Aqueous SDS Solution) | 1.0 |
액체상 SDS 용액 주입 시간(min)(Aqueous SDS Solution Injection Time) | 100 |
최초 반응 온도/압력(Initial Reaction Temperature/Pressure) | 0.1℃/50bar |
단위 수화물 당 가스 저장 부피(v/v)(Volumetric Gas Storage Per Hydrate) | 173 |
메탄 수화물 유도 시간(min)(Induction time (min) for methane hydrates) | 0 |
반응기 부피(Reactor Volume) | 5 L |
순수 종자 CP 용액(Fresh Seed CP Solution) | 0.02 L (CP 4wt% + SDS 500ppm) |
메탄 가스 소비(Nm3)(Methane Gas Consumption) | 181 |
액체상 SDS 용액(L)(Aqueous SDS Solution) | 1.0 |
액체상 SDS 용액 주입 시간(min)(Aqueous SDS Solution Injection Time) | 100 |
최초 반응 온도/압력(Initial Reaction Temperature/Pressure) | 0.3℃/50bar |
단위 수화물 당 가스 저장 부피(v/v)(Volumetric Gas Storage Per Hydrate) | 163 |
메탄 수화물 유도 시간(min)(Induction time (min) for methane hydrates) | 0 |
Claims (35)
- i) 잠재적 종자 수화물(potential feed hydrate)을 함유한 순수 수용액(aqueous fresh solution)을 반응기에 주입하는 제 1 단계;ii) 상기 제 1 단계의 잠재적 종자 수화물을 함유한 순수 수용액이 주입된 반응기에 가스를 주입하는(pressurize) 제 2 단계; 및iii) 상기 제 2 단계의 가스가 주입된 반응기에 계면활성제 용액(surfactant solution)을 주입하는 제 3 단계;를 포함하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- i) 반응기에 가스를 주입하는(pressurize) 제 1 단계;ii) 상기 제 1 단계의 가스가 주입된 반응기에 잠재적 종자 수화물(potential feed hydrate)을 함유한 순수 수용액(aqueous fresh solution)을 주입하는 제 2 단계; 및iii) 상기 제 2 단계의 잠재적 종자 수화물을 함유한 순수 수용액이 주입된 반응기에 계면활성제 용액(surfactant solution)을 주입하는 제 3 단계;를 포함하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- i) 반응기에 가스 (pressurize) 와 종자 수화물(potential feed hydrate)을 함유한 순수 수용액(aqueous fresh solution)을 동시에 주입하는 제 1 단계; 및ii) 상기 제 1 단계의 가스 (pressurize) 와 종자 수화물(potential feed hydrate)을 함유한 순수 수용액(aqueous fresh solution)이 동시에 주입된 반응기에 계면활성제 용액(surfactant solution)을 주입하는 제 2 단계;를 포함하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- 청구항 제 1 항 또는 제 3 항에 있어서, 반응기에 상기 가스를 주입하기 전에 반응기를 냉각하는(cool down) 단계를 추가로 포함하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- 청구항 제 4 항에 있어서, 상기 반응기의 냉각 온도가 ―5℃ 내지 5℃인 것을 특징으로 하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- 청구항 제 1 항 또는 제 3 항에 있어서, 반응기에 잠재적 종자 수화물(potential feed hydrate)을 함유한 순수 수용액(aqueous fresh solution)을 주입하기 전에 반응기를 냉각하는(cool down) 단계를 추가로 포함하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- 청구항 제 6 항에 있어서, 상기 반응기의 냉각 온도가 ―5℃ 내지 5℃인 것을 특징으로 하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- 청구항 제 1 항 또는 제 3 항에 있어서, 반응기에 계면활성제 용액을 주입하기 전에 반응기를 냉각하는(cool down) 단계를 추가로 포함하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- 청구항 제 8 항에 있어서, 상기 반응기의 냉각 온도가 ―5℃ 내지 5℃인 것을 특징으로 하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- 청구항 제 1 항 또는 제 3 항에 있어서, 반응기에 주입되는 가스는 메탄(methane), 에탄(ethane), 프로판(propane), 이산화탄소(carbone dioxide) 또는 이들의 혼합물인 것을 특징으로 하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- 청구항 제 10 항에 있어서, 상기 주입 가스의 가압 압력이 가스 수화물의 평형 압력보다 10 내지 50 bar 이상인 것을 특징으로 하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- 청구항 제 1 항 또는 제 3 항에 있어서, 상기 잠재적 종자 수화물이 sI, sII, sH 수화물 형성체(hydrate former) 또는 세미-클래스레이트(semi-clathrate) 화합물을 형성하는 염인 것을 특징으로 하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- 청구항 제 12 항에 있어서, 상기 sI, sII, sH 수화물 형성체(hydrate former) 또는 세미-클래스레이트(semi-clathrate) 화합물을 형성하는 염이 테트라하이드로퓨란(tetrahydrofuran, THF), 1,3-다이옥소레인(1,3-dioxolane), 테트라하이드로파이란(tetrahydropyran), 사이클로펜테인(cyclopentane), 아세톤(acetone), 다이플루오로메탄(Difluoromethane, HFC-32), 아이소부테인(isobutane), 아이소부틸렌(iso-butylene), n-부테인(n-butane), 프로페인(propane), LPG(C3+C4), 메틸사이클로헥세인(methylcyclohexane), 메틸사이클로펜테인(methylcyclopetane), 네오헥세인(neohexane), 메틸 tert-부틸 에테르(methyltertbutyl ether), 아다만틴(adamantine), 테트라 n-부틸 암모늄 브로마이드(tetra-nbutylammonium bromide), 테트라 n-부틸 암모늄 플로라이드(tetra-n-butylammonium fluoride) 및 테트라 n-부틸 암모늄 클로라이드(tetra-nbutylammonium chloride)로부터 선택되는 어느 하나 이상의 화합물인 것을 특징으로 하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- 청구항 제 1 항 또는 제 3 항에 있어서, 상기 잠재적 종자 수화물이 소듐 도데실 황산염(sodium dodecyl sulfate, SDS), 다이아이소옥틸 소듐 설포숙신산염(diisooctyl sodium sulfosuccinate, DSS), 소듐 테트라데실 황산염(sodium tetradecyl sulfate), 소듐 헥사데실 설페이트(sodium hexadecyl sulfate), 소듐 도데실벤젠 설폰산염(sodium dodecylbenzene sulfonate), 크실렌설폰산염(Xylenesulfonate), 소듐 올레산염(Sodium oleate), 4-n-데실벤젠술폰산염(4-n-Decylbenzenesulfonate), 소듐 라우르산염(sodium laurate), 4-도데실벤젠설폰산(4-dodecylbenzenesulfonic acid), 도데실아민 하이드로클로라이드(dodecylamine hydrochloride), 도데실트리메틸암모늄 클로라이드(dodecyltrimethylammonium chloride), 4-n-옥틸벤젠설폰산염(4-n-Octylbenzenesulfonate), 에톡시레이티드 설폰산염(Ethoxylated sulfonate), 데실벤젠설폰산염(Decylbenzenesulfonate), 포타슘 올레산염(Potassium oleate), n-데실벤젠 설폰산염(n-Decylbenzene sulfonate), 알킬트리메틸암모늄 브로마이드(Alkyltrimethylammonium bromide, C10-C16 chains), 도데실 아민(Dodecyl amine), 테트라데실트리메틸암모늄 클로라이드(Tetradecyltrimethylammonium chloride), 도데실 폴리사카라이드 글리코시드(dodecyl polysaccharide glycoside), 사이클로덱스트린(Cyclodextrins), 글리코리피드(glycolipids), 리포프로테인-리포펩타이드(lipoprotein―ipopeptides), 포스포리피드(phospholipides), para-톨루엔 설폰산(para-toluene sulfonic acid), 트리실옥세인(trisiloxane), 트리톤(triton) X-100 로부터 선택되는 어느 하나 이상의 화합물의 얼음 입자(ice slurry)인 것을 특징으로 하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- 청구항 제 1 항 또는 제 3 항에 있어서, 상기 잠재적 종자 수화물을 함유한 순수 수용액의 부피가 상기 계면활성제 용액 전체 부피의 5 % 이내인 것을 특징으로 하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- 청구항 제 1 항 또는 제 3 항에 있어서, 상기 계면활성제가 소듐 도데실 황산염(sodium dodecyl sulfate, SDS), 다이아이소옥틸 소듐 설포숙신산염(diisooctyl sodium sulfosuccinate, DSS), 소듐 테트라데실 황산염(sodium tetradecyl sulfate), 소듐 헥사데실 설페이트(sodium hexadecyl sulfate), 소듐 도데실벤젠 설폰산염(sodium dodecylbenzene sulfonate), 크실렌설폰산염(Xylenesulfonate), 소듐 올레산염(Sodium oleate), 4-n-데실벤젠술폰산염(4-n-Decylbenzenesulfonate), 소듐 라우르산염(sodium laurate), 4-도데실벤젠설폰산(4-dodecylbenzenesulfonic acid), 도데실아민 하이드로클로라이드(dodecylamine hydrochloride), 도데실트리메틸암모늄 클로라이드(dodecyltrimethylammonium chloride), 4-n-옥틸벤젠설폰산염(4-n-Octylbenzenesulfonate), 에톡시레이티드 설폰산염(Ethoxylated sulfonate), 데실벤젠설폰산염(Decylbenzenesulfonate), 포타슘 올레산염(Potassium oleate), n-데실벤젠 설폰산염(n-Decylbenzene sulfonate), 알킬트리메틸암모늄 브로마이드(Alkyltrimethylammonium bromide, C10-C16 chains), 도데실 아민(Dodecyl amine), 테트라데실트리메틸암모늄 클로라이드(Tetradecyltrimethylammonium chloride), 도데실 폴리사카라이드 글리코시드(dodecyl polysaccharide glycoside), 사이클로덱스트린(Cyclodextrins), 글리코리피드(glycolipids), 리포프로테인-리포펩타이드(lipoprotein―ipopeptides),포스포리피드(phospholipides), para-톨루엔 설폰산(para-toluene sulfonic acid), 트리실옥세인(trisiloxane), 트리톤(triton) X-100 로부터 선택되는 어느 하나 이상의 화합물인 것을 특징으로 하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- 청구항 제 1 항 또는 제 3 항에 있어서, 상기 계면활성제 용액의 농도가 50 내지 2000 ppm인 것을 특징으로 하는 반회분식(fed-batch type) 가스 수화물 제조 방법.
- i) 계면활성제 용액(surfactant solution)을 반응기에 주입하는 제 1 단계;ii) 상기 제 1 단계의 계면활성제 용액이 주입된 반응기에 가스를 주입하는(pressurize) 제 2 단계; 및iii) 상기 제 2 단계의 가스가 주입된 반응기에 잠재적 종자 수화물(potential feed hydrate)을 함유한 순수 수용액(aqueous fresh solution)을 주입하는 제 3 단계;를 포함하는 회분식(batch type) 가스 수화물 제조 방법.
- i) 계면활성제 용액(surfactant solution)을 반응기에 주입하는 제 1 단계;ii) 상기 제 1 단계의 계면활성제 용액이 주입된 반응기에 잠재적 종자 수화물(potential feed hydrate)을 함유한 순수 수용액(aqueous fresh solution)을 주입하는 제 2 단계; 및iii) 상기 제 2 단계의 잠재적 종자 수화물을 함유한 순수 수용액이 주입된 반응기에 가스를 주입하는(pressurize) 제 3 단계;를 포함하는 회분식(batch type) 가스 수화물 제조 방법.
- i) 계면활성제 용액(surfactant solution)을 반응기에 주입하는 제 1 단계; 및ii) 상기 제 1 단계의 계면활성제 용액이 주입된 반응기에 가스 (pressurize) 및 잠재적 종자 수화물(potential feed hydrate)을 함유한 순수 수용액(aqueous fresh solution)을 동시 주입하는 제 2 단계;를 포함하는 회분식(batch type) 가스 수화물 제조 방법.
- i) 반응기에 가스를 주입하는 (pressurize) 제 1 단계;ii) 상기 제 1 단계의 가스가 주입(pressurize)된 반응기에 계면활성제 용액(surfactant solution)을 주입하는 제 2 단계; 및iii) 상기 제 2 단계의 계면활성제 용액(surfactant solution)이 주입된 반응기에 잠재적 종자 수화물(potential feed hydrate)을 함유한 순수 수용액(aqueous fresh solution)을 주입하는 제 3 단계;를 포함하는 회분식(batch type) 가스 수화물 제조 방법.
- 청구항 제 18 항 또는 제 21 항에 있어서, 반응기에 가스를 주입하기 전에 반응기를 냉각하는(cool down) 단계를 추가로 포함하는 회분식(batch type) 가스 수화물 제조 방법.
- 청구항 제 22 항에 있어서, 상기 반응기의 냉각 온도가 ―5℃ 내지 5℃인 것을 특징으로 하는 회분식(batch type) 가스 수화물 제조 방법.
- 청구항 제 18 항 또는 제 21 항에 있어서, 반응기에 잠재적 종자 수화물을 함유한 순수 수용액를 주입하기 전에 반응기를 냉각하는(cool down) 단계를 추가로 포함하는 회분식(batch type) 가스 수화물 제조 방법.
- 청구항 제 24 항에 있어서, 상기 반응기의 냉각 온도가 ―5℃ 내지 5℃인 것을 특징으로 하는 회분식(batch type) 가스 수화물 제조 방법.
- 청구항 제 18 항 또는 제 21 항에 있어서, 반응기에 계면활성제 용액을 주입하기 전에 반응기를 냉각하는(cool down) 단계를 추가로 포함하는 회분식(batch type) 가스 수화물 제조 방법.
- 청구항 제 26 항에 있어서, 상기 반응기의 냉각 온도가 ―5℃ 내지 5℃인 것을 특징으로 하는 회분식(batch type) 가스 수화물 제조 방법.
- 청구항 제 18 항 또는 제 21 항에 있어서, 반응기에 주입되는 가스는 메탄(methane), 에탄(ethane), 프로판(propane), 이산화탄소(carbone dioxide) 또는 이들의 혼합물인 것을 특징으로 하는 회분식(batch type) 가스 수화물 제조 방법.
- 청구항 제 28 항에 있어서, 상기 주입 가스의 가압 압력이 가스 수화물의 평형 압력보다 10 내지 50 bar 이상인 것을 특징으로 하는 회분식(batch type) 가스 수화물 제조 방법.
- 청구항 제 18 항 또는 제 21 항에 있어서, 상기 잠재적 종자 수화물이 sI, sII, sH 수화물 형성체(hydrate former) 또는 세미-클래스레이트(semi-clathrate) 화합물을 형성하는 염인 것을 특징으로 하는 회분식(batch type) 가스 수화물 제조 방법.
- 청구항 제 30 항에 있어서, 상기 sI, sII, sH 수화물 형성체(hydrate former) 또는 세미-클래스레이트(semi-clathrate) 화합물을 형성하는 염이 테트라하이드로퓨란(tetrahydrofuran, THF), 1,3-다이옥소레인(1,3-dioxolane), 테트라하이드로파이란(tetrahydropyran), 사이클로펜테인(cyclopentane), 아세톤(acetone), 다이플루오로메탄(Difluoromethane, HFC-32), 아이소부테인(isobutane), 아이소부틸렌(iso-butylene), n-부테인(n-butane), 프로페인(propane), LPG(C3+C4), 메틸사이클로헥세인(methylcyclohexane), 메틸사이클로펜테인(methylcyclopetane), 네오헥세인(neohexane), 메틸 tert-부틸 에테르(methyltertbutyl ether), 아다만틴(adamantine), 테트라 n-부틸 암모늄 브로마이드(tetra-nbutylammonium bromide), 테트라 n-부틸 암모늄 플로라이드(tetra-n-butylammonium fluoride) 및 테트라 n-부틸 암모늄 클로라이드(tetra-nbutylammonium chloride)로부터 선택되는 어느 하나 이상의 화합물인 것을 특징으로 하는 회분식(batch type) 가스 수화물 제조 방법.
- 청구항 제 18 항 또는 제 21 항에 있어서, 상기 잠재적 종자 수화물이 소듐 도데실 황산염(sodium dodecyl sulfate, SDS), 다이아이소옥틸 소듐 설포숙신산염(diisooctyl sodium sulfosuccinate, DSS), 소듐 테트라데실 황산염(sodium tetradecyl sulfate), 소듐 헥사데실 설페이트(sodium hexadecyl sulfate), 소듐 도데실벤젠 설폰산염(sodium dodecylbenzene sulfonate), 크실렌설폰산염(Xylenesulfonate), 소듐 올레산염(Sodium oleate), 4-n-데실벤젠술폰산염(4-n-Decylbenzenesulfonate), 소듐 라우르산염(sodium laurate), 4-도데실벤젠설폰산(4-dodecylbenzenesulfonic acid), 도데실아민 하이드로클로라이드(dodecylamine hydrochloride), 도데실트리메틸암모늄 클로라이드(dodecyltrimethylammonium chloride), 4-n-옥틸벤젠설폰산염(4-n-Octylbenzenesulfonate), 에톡시레이티드 설폰산염(Ethoxylated sulfonate), 데실벤젠설폰산염(Decylbenzenesulfonate), 포타슘 올레산염(Potassium oleate), n-데실벤젠 설폰산염(n-Decylbenzene sulfonate), 알킬트리메틸암모늄 브로마이드(Alkyltrimethylammonium bromide, C10-C16 chains), 도데실 아민(Dodecyl amine), 테트라데실트리메틸암모늄 클로라이드(Tetradecyltrimethylammonium chloride), 도데실 폴리사카라이드 글리코시드(dodecyl polysaccharide glycoside), 사이클로덱스트린(Cyclodextrins), 글리코리피드(glycolipids), 리포프로테인-리포펩타이드(lipoprotein―ipopeptides), 포스포리피드(phospholipides), para-톨루엔 설폰산(para-toluene sulfonic acid), 트리실옥세인(trisiloxane), 트리톤(triton) X-100 로부터 선택되는 어느 하나 이상의 화합물의 얼음 입자(ice slurry)인 것을 특징으로 하는 회분식(batch type) 가스 수화물 제조 방법.
- 청구항 제 18 항 또는 제 21 항에 있어서, 상기 잠재적 종자 수화물을 함유한 순수 수용액의 부피가 상기 계면활성제 용액 전체 부피의 5 % 이내인 것을 특징으로 하는 회분식(batch type) 가스 수화물 제조 방법.
- 청구항 제 18 항 또는 제 21 항에 있어서, 상기 계면활성제가 소듐 도데실 황산염(sodium dodecyl sulfate, SDS), 다이아이소옥틸 소듐 설포숙신산염(diisooctyl sodium sulfosuccinate, DSS), 소듐 테트라데실 황산염(sodium tetradecyl sulfate), 소듐 헥사데실 설페이트(sodium hexadecyl sulfate), 소듐 도데실벤젠 설폰산염(sodium dodecylbenzene sulfonate), 크실렌설폰산염(Xylenesulfonate), 소듐 올레산염(Sodium oleate), 4-n-데실벤젠술폰산염(4-n-Decylbenzenesulfonate), 소듐 라우르산염(sodium laurate), 4-도데실벤젠설폰산(4-dodecylbenzenesulfonic acid), 도데실아민 하이드로클로라이드(dodecylamine hydrochloride), 도데실트리메틸암모늄 클로라이드(dodecyltrimethylammonium chloride), 4-n-옥틸벤젠설폰산염(4-n-Octylbenzenesulfonate), 에톡시레이티드 설폰산염(Ethoxylated sulfonate), 데실벤젠설폰산염(Decylbenzenesulfonate), 포타슘 올레산염(Potassium oleate), n-데실벤젠 설폰산염(n-Decylbenzene sulfonate), 알킬트리메틸암모늄 브로마이드(Alkyltrimethylammonium bromide, C10-C16 chains), 도데실 아민(Dodecyl amine), 테트라데실트리메틸암모늄 클로라이드(Tetradecyltrimethylammonium chloride), 도데실 폴리사카라이드 글리코시드(dodecyl polysaccharide glycoside), 사이클로덱스트린(Cyclodextrins), 글리코리피드(glycolipids), 리포프로테인-리포펩타이드(lipoprotein―ipopeptides),포스포리피드(phospholipides), para-톨루엔 설폰산(para-toluene sulfonic acid), 트리실옥세인(trisiloxane), 트리톤(triton) X-100 로부터 선택되는 어느 하나 이상의 화합물인 것을 특징으로 하는 회분식(batch type) 가스 수화물 제조 방법.
- 청구항 제 18 항 또는 제 21 항에 있어서, 상기 계면활성제 용액의 농도가 50 내지 2000 ppm인 것을 특징으로 하는 회분식(batch type) 가스 수화물 제조 방법.
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PCT/KR2010/000448 WO2011090229A1 (ko) | 2010-01-25 | 2010-01-25 | 신속한 가스 수화물 제조 방법 |
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JP3276407B2 (ja) * | 1992-07-03 | 2002-04-22 | 東京瓦斯株式会社 | 地下の炭化水素水和物の採取法 |
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GB2347938B (en) * | 1999-03-15 | 2001-07-11 | Mitsubishi Heavy Ind Ltd | Production method for hydrate and device for producing the same |
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DE102004053627A1 (de) * | 2004-11-01 | 2006-05-04 | Bernd Bonso | Verfahren zur Herstellung, Transport und Lagerung von Gashydraten (Gasclathrat) |
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US7781627B2 (en) * | 2006-02-27 | 2010-08-24 | Sungil Co., Ltd. (SIM) | System and method for forming gas hydrates |
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US8119078B2 (en) * | 2007-09-17 | 2012-02-21 | Mississippi State University | System for stabilizing gas hydrates at low pressures |
US8334418B2 (en) * | 2008-11-05 | 2012-12-18 | Water Generating Systems LLC | Accelerated hydrate formation and dissociation |
US8354565B1 (en) * | 2010-06-14 | 2013-01-15 | U.S. Department Of Energy | Rapid gas hydrate formation process |
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Non-Patent Citations (1)
Title |
---|
HUANG, D. ET AL.: "Thermal Conductive of Methane Hydrate Formed from Sodium Dodecyl Sulfate Solution", J. CHEM. ENG. DATA., vol. 49, 2004, pages 1479 - 1482 * |
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