WO2012134077A9 - Dispositif de fabrication continue d'hydrate de gaz - Google Patents

Dispositif de fabrication continue d'hydrate de gaz Download PDF

Info

Publication number
WO2012134077A9
WO2012134077A9 PCT/KR2012/001822 KR2012001822W WO2012134077A9 WO 2012134077 A9 WO2012134077 A9 WO 2012134077A9 KR 2012001822 W KR2012001822 W KR 2012001822W WO 2012134077 A9 WO2012134077 A9 WO 2012134077A9
Authority
WO
WIPO (PCT)
Prior art keywords
pipe
gas
reactor
hydrate
gas hydrate
Prior art date
Application number
PCT/KR2012/001822
Other languages
English (en)
Korean (ko)
Other versions
WO2012134077A3 (fr
WO2012134077A2 (fr
Inventor
김철호
김호경
이재익
정태석
허주호
신재웅
Original Assignee
에스티엑스조선해양 주식회사
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 에스티엑스조선해양 주식회사 filed Critical 에스티엑스조선해양 주식회사
Priority to JP2013558783A priority Critical patent/JP2014523397A/ja
Priority to US14/008,451 priority patent/US20140017141A1/en
Publication of WO2012134077A2 publication Critical patent/WO2012134077A2/fr
Publication of WO2012134077A9 publication Critical patent/WO2012134077A9/fr
Publication of WO2012134077A3 publication Critical patent/WO2012134077A3/fr

Links

Images

Classifications

    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • 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
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0053—Details of the reactor
    • B01J19/0066—Stirrers
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/1812—Tubular reactors
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/20—Use of additives, e.g. for stabilisation
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures

Definitions

  • the present invention relates to a gas hydrate continuous production apparatus using potential hydrate crystals. More specifically, the present invention provides a pipe-type ice machine for injecting a potential hydrate crystal of an aqueous solution containing a surfactant into a pipe-type reactor; A gas pipe hydrate comprising an elongated pipe-shaped reactor, a pipe-type reactor that maximizes the conversion rate while circulating and transporting the injected hydrate crystals and gases to each other to produce gas hydrates, and then circulating them over the entire length section of the reactor. It relates to a manufacturing apparatus.
  • the pipe-type reactor is provided with a pig ball (pig-ball) for circulating the gas hydrate in the pipe-type reactor by the action of circulating the inside of the pipe reactor in a plurality of connected state at regular intervals It is characterized by.
  • 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.
  • LNG liquefied natural gas
  • methane gas which is the main component of liquefied natural gas, requires about -162 °C of cryogenic temperature to be liquefied. Therefore, it is very expensive not only for the production of liquefied natural gas but also for the manufacture of natural gas transportation equipment in the sea and on land. There is a problem.
  • 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 pressures and temperatures while providing 170 times the volume of gas per unit volume. Once formed, hydrates are preserved at -20 ° C and 1 atmosphere. These temperature and pressure conditions are much milder than the temperature and pressure conditions 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 or CNG.
  • 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 H, 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 (see Figure 1).
  • 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 (H2O) 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.
  • the general method for producing natural gas hydrate is to produce a 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. Most of the bubbling method is used, 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.
  • the problem of reducing the long hydrate induction time and the problem of low hydrate crystal growth rate must be solved.
  • the reaction area that can meet the temperature and pressure conditions and react must be wide. Conventional methods such as nozzle spraying, microbubbles, and agitation are used to increase the reaction area, but the conversion rate is limited and the manufacturing cost of the apparatus is high.
  • the heat conductivity is lowered due to the adsorption of the heat exchanger surface and the hydrate after the formation of the hydrate (adhesion of ice in the refrigerating chamber), making the heat exchange in the reactor more difficult and difficult to separate. Will interfere.
  • the hydrates generated in the reactor are discharged in the form of a slurry, followed by a dehydration process, thereby removing the unreacted water in the reactor, thereby increasing the gas filling rate in the hydrate. have.
  • the hydrate slurry is pressurized by mechanical force or centrifugal force for dehydration.
  • an ice membrane is formed in the filter net or filter for filtering the hydrate slurry, and thus the dewatering ability is reduced.
  • the present invention has been proposed to solve the above problems, it is easy to gas diffusion during the production reaction and the contact area of water and gas is maximized, resulting in a high gas capture rate and shortening the overall hydrate formation time, high conversion rate And relatively low gas hydrate formation pressure, and does not require latent heat due to phase change as compared with gas hydrate formation in an aqueous solution, thereby reducing the overall reaction calorific value.
  • the reduction of the process increases the overall reaction efficiency and the reduction of the cooling process required to remove the heat of reaction, which can reduce the production cost.
  • the process of producing the gas hydrate continuously without the dehydration process can be produced without the dehydration process. Gas Hydrate Continuous Manufacturing Sheet To provide an object.
  • An object of the present invention is a pipe-type ice machine for injecting a potential hydrate crystal (potential hydrate crystal) of the aqueous solution containing a surfactant into the pipe-type reactor;
  • a gas pipe hydrate comprising an elongated pipe-shaped reactor, a pipe-type reactor that maximizes the conversion rate while circulating and transporting the injected hydrate crystals and gases to each other to produce gas hydrates, and then circulating them over the entire length section of the reactor.
  • an object of the present invention is characterized in that it comprises a pig ball (pig-ball) for circulating the gas hydrate in the pipe reactor by the action of circulating the inside of the pipe reactor in a plurality of connected state at regular intervals It is achieved by providing a gas hydrate continuous manufacturing apparatus.
  • a pig ball pig-ball
  • Gas hydrate continuous production apparatus of the present invention already has a porous structure, potential hydrate crystals such as ice particles or powder ice particles that do not require a separate hydrate induction time to convert to gas hydrate crystals (potential hydrate)
  • potential hydrate crystals such as ice particles or powder ice particles that do not require a separate hydrate induction time to convert to gas hydrate crystals (potential hydrate)
  • the gas hydrate continuous manufacturing apparatus of the present invention forms gas hydrates from potential hydrate crystals, latent heat due to phase change is lower than that of gas hydrates directly formed in an aqueous solution. Since it is not necessary, the total reaction calorific value may be reduced, thereby reducing the production cost and reducing the process for removing the reaction heat.
  • the gas hydrate continuous manufacturing apparatus of the present invention discards the existing method of producing a gas hydrate slurry after the dehydration process to produce a gas hydrate continuously without such a dehydration process, it is necessary to additionally install a device for cleaning the filter net or filter In the first place, there is no problem that mass production for commercialization is difficult due to the large size of equipment due to the dehydration process in the reactor.
  • FIG. 1 is a view for explaining the structure of a gas hydrate (gas hydrate).
  • FIG. 2 is a conceptual diagram showing the concept of a gas hydrate continuous production apparatus using a potential hydrate crystal of the present invention.
  • Figure 3 is a schematic diagram showing the heat of reaction of the pipe-type reactor using a conventional gas hydrate continuous production apparatus.
  • Figure 4 is a schematic diagram showing the heat of reaction of the pipe-type reactor using an embodiment of the gas hydrate continuous production apparatus of the present invention.
  • FIG. 5 is a schematic view of a gas hydrate continuous production apparatus using an embodiment of the gas hydrate continuous production apparatus of the present invention.
  • FIG. 6 is a schematic diagram showing in detail the pipe-type reactor in FIG.
  • FIG. 7 is a view illustrating a state where the adjacent pig balls are installed at different angles and effects thereof in an embodiment of the apparatus for continuously manufacturing gas hydrates of the present invention.
  • gas tank 2 gas regulator
  • thermocouple 8 second thermocouple
  • pelletizer 20 secondary storage tank
  • the gas hydrate continuous production apparatus of the present invention includes a pipe-type ice maker for injecting a potential hydrate crystal of an aqueous solution containing a surfactant into a pipe-type reactor;
  • An elongated pipe-shaped reactor comprising a pipe-type reactor that maximizes the conversion rate while circulating and transporting the injected potential hydrate crystals and gases to each other to produce gas hydrates, and then circulating them over the entire length section of the reactor.
  • the pipe-type ice maker 15 injects a potential hydrate crystal of an aqueous solution containing a surfactant into the pipe-type reactor 9 (see FIG. 6).
  • the pipe-type reactor 9 means that the reactor is made into an elongated pipe shape as shown in FIG. 6 rather than a normal cylindrical shape (this will be described in more detail later in this section).
  • gas hydrate is a low-molecular-weight gas and water at low temperatures and pressures, which are present as solid crystals like dry ice by physical bonding similar to structural entanglement rather than chemical bonding. Refer to the compound (see FIG. 1).
  • a potential hydrate crystal since a potential hydrate crystal has a porous structure, it is converted into a gas hydrate crystal, and thus a precursor of a gas hydrate crystal without a separate hydrate induction time is required. It is called.
  • Potential hydrate crystals with a porous structure include 1) solid ice particles, or 2) insoluble forms of the surfactant-containing aqueous solution through a preliminary process of pre-cooling and pulverizing the aqueous solution containing the surfactant. Slurry form in the suspension state of the solid particles may be used.
  • the aqueous solution is impregnated with the porous material and then cooled, or 4) the superabsorbent resin is absorbed and cooled, thereby eliminating the pre-crushing process.
  • the aqueous solution may be injected directly into the pipe reactor 9.
  • the porous material or superabsorbent resin artificially separate the aqueous solution particles to maximize the contact area between the aqueous solution and the gas.
  • all materials commercially available may be used as the porous material.
  • activated carbon, silica gel, or zeolite may be used.
  • the superabsorbent polymer may be used all of the commercially available general resin, preferably polyacrylate, polyacrylamide (polyacryl amide), polyacryl acid, polymethacrylic acid, Polyethylene oxide, polyvinyl alcohol, and the like may be used.
  • the gas diffusion in the potential hydrate crystals is easy and the contact area between the water and the gas is maximized, which leads to a high gas collection rate and shorter overall hydrate formation time, as well as a high conversion rate. And relatively low gas hydrate formation pressure.
  • the latent heat according to the phase change is not necessary, and thus the total amount of heat generated from the reaction is reduced, which is an apparatus and a process for removing the reaction heat in the pipe-type reactor 9. This reduces the overall cost savings.
  • FIGS 3 and 4 are schematic diagrams showing the calorific value to be removed from the outside, respectively, when forming a hydrate from an aqueous solution and when forming a hydrate in a crystal of a potential hydrate in an ice particle state, which is an embodiment of the present invention.
  • the emission amount when generating 1 kg of methane hydrate from ice particles is absorbed at the phase change of 1 kg of ice particles from 542.4 KJ / kg That's 106.6 KJ / kg minus 435.8 KJ / kg of calories.
  • the aqueous solution containing the surfactant is in the form of ice particles and has already removed latent heat, the amount of heat to be removed in the pipe reactor 9 is reduced during the reaction, thus removing the heat of reaction in the pipe reactor 9.
  • the capacity and cooling time of the total cooler 21 is to be reduced.
  • the above mentioned potential hydrate crystals will comprise a surfactant, which can be used with all commonly used surfactants, but is preferably sodium dodecyl sulfate (SDS), diisooctyl sodium sulfo Succinate (diisooctyl sodium sulfosuccinate (DSS), sodium tetradecyl sulfate, sodium hexadecyl sulfate, sodium dodecylbenzene sulfonate, xylenesulfonate, sodium Sodium oleate, 4-n-decylbenzenesulfonate, sodium laurate, 4-dodecylbenzenesulfonic acid, dodecylamine hydro Dodecylamine hydrochloride, dodecyltrimethylammonium chloride, 4-n-octylbenzenesulfonate, Ethoxylated sulfonate, Decylbenzenes
  • the amount of the above-mentioned surfactant is sufficient in a small amount of about 0.5% of the total volume of the aqueous solution, and the concentration of the surfactant is preferably in the range of 50 ppm to 1000 ppm.
  • the cooling temperature of the pipe reactor 9 is preferably in the range of -10 °C to 10 °C.
  • the pressure in the pipe reactor 9 is preferably in the range of 10 bar to 100 bar.
  • the gas injected into the pipe reactor 9 may be methane, ethane, propane, carbone dioxide, butane or mixtures thereof.
  • the conversion rate may not reach the required level.
  • the present invention does not make the reactor into a general cylindrical shape but rather an elongated pipe shape as shown in FIG. 6 (the present invention is specifically called a 'pipe type reactor' in order to reflect this feature). ).
  • the reason why the present invention introduces the pipe-type reactor 9 rather than the conventional cylindrical reactor is that the gas hydrate first generated inside the pipe-type reactor 9 is not immediately discharged to the outside, This is to maximize the conversion rate through the process of circulating the entire length of the pipe reactor 9 while staying.
  • the aqueous solution containing the surfactant is cooled and pulverized by the pipe-type ice maker 15 to make ice particles, and then injected into the pipe-type reactor 9, and then the reaction gas is gas cylinder 1 From the nozzle 4 through a mass flow meter 3 capable of measuring the gas injection according to the formation of gas hydrates through the pipe, the outlet portion of the pipe ice maker 15 in the pipe reactor 9 In a) gas hydrate is produced immediately.
  • the pressure is set through the gas regulator 2 to maintain a constant pressure in the pipe-type reactor 9, and the coolant lines 13 and 14 are connected to the pipe-type reactor in the cooler 21 to which the temperature controller is attached. It is connected to (9) to drop the temperature of the pipe reactor (9).
  • the gas hydrate produced at the outlet portion a of the pipe-shaped ice maker 15 in the pipe-shaped reactor 9 is not immediately discharged to the outside, but stays inside the pipe-shaped reactor 9 while the pipe-shaped reactor 9 The conversion rate is maximized as it is circulated through the entire length of.
  • the pipe-type reactor 9 is composed of two long bodies A and B, in order to increase the effect by making the entire length of the pipe-type reactor 9 longer.
  • the gas hydrate is produced at the outlet portion (a) of the pipe ice maker 15 in the pipe reactor 9 and then circulated through the entire length of the pipe reactor 9 before the end of the pipe reactor 9 ( B) is discharged and collected in the primary storage tank 18, and then finally stored in the secondary storage tank 20 via a pelletizer 19 equipped with a decompression device.
  • a pelletizer 19 equipped with a decompression device.
  • the present invention is a device for adopting the screw method by using a pig ball (pig-ball) 16 instead of the conventional screw method as a means for circulating the gas hydrate over the entire length of the pipe-type reactor (9)
  • the aim was to reduce the cost of manufacturing and reduce manufacturing costs.
  • the present invention is characterized in that the gas hydrate is circulated and transported in the pipe-type reactor 9 by the action of the pig ball 16 which circulates inside the pipe-type reactor 9 in a plurality of connected states at regular intervals. .
  • the pig ball 16 is in a state in which a plurality of pig balls 16 are connected at regular intervals by the chain 22 in the pipe-type reactor 9, in which case the diameter of the pig ball 16 is a pipe-type reactor ( It is preferable to bring it into a state almost close to the inner diameter of 9). This is because the pig ball 16 can move effectively inside the pipe-like reactor 9 and effectively scrape off the gas hydrate generated in the ice state on the inner wall of the pipe-like reactor 9.
  • the pig ball 16 circulates in the direction a to b with the chain 22 as the pig ball rotating wheel 17 rotates, and in this process, the pig ball 16 is piped. Since the gas hydrate generated in the state of ice on the inner wall of the reactor 9 is scraped off and continuously pushed in the direction of travel, the gas hydrate is also transferred from a to b according to the action of the pig ball 16. do.
  • the adjacent pig ball 16 of the plurality of pig ball 16 is connected to be different angles. This allows the trailing pig ball 16 to scrape off the gas hydrate that the preceding pig ball 16 could not scrape as shown in FIG. 7, thereby avoiding a loss in the continuous production of gas hydrate. At the same time it is intended to prevent the continuous deposition of gas hydrate on the inner wall of the pipe-type reactor (9).
  • the technical idea of the present invention may still have high utility even when the potential hydrate crystal as described above is not used.
  • the present invention also provides a gas hydrate continuous production apparatus comprising a pipe-type reactor that maximizes the conversion while producing gas hydrate as an elongated pipe-shaped reactor and circulating it over the entire length of the reactor.
  • a gas hydrate continuous production apparatus comprising a pipe-type reactor that maximizes the conversion while producing gas hydrate as an elongated pipe-shaped reactor and circulating it over the entire length of the reactor.
  • the gas hydrate is formed from the potential hydrate crystal, it is possible to reduce the reaction time and maximize the reaction efficiency and to reduce the production cost and the process for removing the heat of reaction. Is a technology that can realize its practical and economic value in the field of resource acquisition and energy production technology.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

La présente invention concerne un dispositif de fabrication continue d'un hydrate de gaz au moyen de cristaux d'hydrates potentiels. Plus spécifiquement, la présente invention concerne un dispositif de fabrication continue d'un hydrate de gaz comprenant: une machine à glace en forme de tuyau destinée à injecter des cristaux d'hydrates potentiels dans une solution aqueuse contenant un tensioactif dans un réacteur en forme de tuyau; et le réacteur en forme de tuyau, un réacteur façonné tel un long tuyau, destiné à produire des cristaux de gaz par induction d'une réaction entre les cristaux d'hydrates potentiels injectés et un gaz, et à transporter les cristaux de gaz produits dans un mouvement circulaire à travers toute la longueur de l'intérieur du réacteur, maximisant ainsi un taux de conversion. Dans la présente invention, le réacteur en forme de tuyau comprend des tournants sphériques, qui sont reliés entre eux à intervalles prédéfinis, et se déplacent selon un mouvement circulaire dans le réacteur en forme de tuyau, transportant ainsi, selon un mouvement circulaire, l'hydrate de gaz dans le réacteur en forme de tuyau. Du fait de l'abandon du procédé classique qui consiste à déshydrater après production d'une boue d'hydrate de gaz, et de l'adoption de la fabrication d'hydrate de gaz sans procédé de déshydratation, le dispositif de fabrication continue d'un hydrate de gaz de la présente invention résout, dès le début, le problème posé par la nécessité d'ajouter un dispositif supplémentaire de lavage d'un tamis ou d'un filtre, ainsi que celui de la difficulté posée pour la production de masse en vue de la commercialisation, qui nécessite une augmentation de la dimension de l'équipement lorsque le procédé de déshydratation s'effectue à l'intérieur du réacteur.
PCT/KR2012/001822 2011-03-29 2012-03-13 Dispositif de fabrication continue d'hydrate de gaz WO2012134077A2 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
JP2013558783A JP2014523397A (ja) 2011-03-29 2012-03-13 ガス水和物連続製造装置
US14/008,451 US20140017141A1 (en) 2011-03-29 2012-03-13 Successive gas hydrate manufacturing device

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
KR1020110028088A KR101274302B1 (ko) 2011-03-29 2011-03-29 가스 수화물 연속 제조 장치
KR10-2011-0028088 2011-03-29

Publications (3)

Publication Number Publication Date
WO2012134077A2 WO2012134077A2 (fr) 2012-10-04
WO2012134077A9 true WO2012134077A9 (fr) 2012-11-29
WO2012134077A3 WO2012134077A3 (fr) 2013-01-17

Family

ID=46932049

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/KR2012/001822 WO2012134077A2 (fr) 2011-03-29 2012-03-13 Dispositif de fabrication continue d'hydrate de gaz

Country Status (4)

Country Link
US (1) US20140017141A1 (fr)
JP (1) JP2014523397A (fr)
KR (1) KR101274302B1 (fr)
WO (1) WO2012134077A2 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3670635A1 (fr) * 2018-12-20 2020-06-24 Fachhochschule Vorarlberg GmbH Procédé et dispositif de fabrication d'hydrate de gaz
CN112473571B (zh) * 2020-10-28 2022-06-14 中石化宁波工程有限公司 一种能加速鼓泡床内气体水合物生成的方法

Family Cites Families (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4199834A (en) * 1978-07-27 1980-04-29 Willis Oil Tool Co. Pig ball transfer unit
JP3957804B2 (ja) * 1997-02-04 2007-08-15 北陸電力株式会社 ガス水和物の製造方法及びガス水和物製造用添加物
JP2004050167A (ja) * 2002-05-27 2004-02-19 Kenichi Suzuki 炭酸ガスの隔離方法及びその装置
JP4575206B2 (ja) * 2005-03-30 2010-11-04 中国電力株式会社 ガスハイドレートの製造方法及び製造装置
JP4559898B2 (ja) * 2005-03-31 2010-10-13 独立行政法人産業技術総合研究所 ガスハイドレート製造装置
JP4998772B2 (ja) * 2006-06-14 2012-08-15 独立行政法人産業技術総合研究所 ハイドレートの製造装置
JP5062527B2 (ja) * 2007-11-09 2012-10-31 東京電力株式会社 高圧用炭酸ガス細泡化装置及びこれを用いた炭酸ガスの地中貯留システム
US20090175774A1 (en) * 2008-01-03 2009-07-09 Baker Hughes Incorporated Hydrate inhibition test loop
JP5589197B2 (ja) * 2008-05-13 2014-09-17 国立大学法人東京工業大学 液体二酸化炭素の超微粒化方法および超微粒化システム
US10392573B2 (en) * 2008-10-17 2019-08-27 Ecolab Usa Inc. Method of controlling gas hydrates in fluid systems
JP2009119463A (ja) * 2008-12-29 2009-06-04 Mitsui Eng & Shipbuild Co Ltd ガスハイドレートの海中生成方法及びガスハイドレート生成装置
KR101034138B1 (ko) * 2009-01-06 2011-05-13 에스티엑스조선해양 주식회사 잠재적 수화물 결정을 이용한 가스 수화물 제조 방법
JP5489150B2 (ja) * 2009-02-26 2014-05-14 学校法人日本大学 クラスレートハイドレートの製造方法
JP5208862B2 (ja) * 2009-06-12 2013-06-12 一般財団法人電力中央研究所 エマルジョンの製造・注入装置及び方法並びにメタンハイドレートの採掘方法
KR101495221B1 (ko) * 2010-08-23 2015-02-24 동국대학교 산학협력단 천연가스 하이드레이트 제조 장치 및 천연가스 하이드레이트 제조 방법

Also Published As

Publication number Publication date
JP2014523397A (ja) 2014-09-11
KR20120110308A (ko) 2012-10-10
KR101274302B1 (ko) 2013-06-13
WO2012134077A3 (fr) 2013-01-17
US20140017141A1 (en) 2014-01-16
WO2012134077A2 (fr) 2012-10-04

Similar Documents

Publication Publication Date Title
WO2012026631A1 (fr) Dispositif et procédé pour la fabrication d'hydrate de gaz naturel
Cheng et al. Quantitative analysis of methane hydrate formation in size-varied porous media for gas storage and transportation application
WO2012134078A2 (fr) Procédé de fabrication continue d'hydrate de gaz
JP2001507742A (ja) 水化物から気体を回収する方法
KR101034138B1 (ko) 잠재적 수화물 결정을 이용한 가스 수화물 제조 방법
WO2012134077A9 (fr) Dispositif de fabrication continue d'hydrate de gaz
JP2003105362A (ja) 天然ガスハイドレートの生成方法および生成システム
CN103818882B (zh) 一种回收含尘热烟气中硫蒸气的方法
WO2011090229A1 (fr) Procédé pour la formation rapide d'un gaz hydraté
CN206692505U (zh) 一种高热量回收效率的煤气化黑水和灰水处理系统
CN102688605A (zh) 黑水处理系统和方法
Zhengzhuo et al. Review of hydrate reactor in natural gas hydrate storage and transportation
CN101693522B (zh) 合成氨废气分离回收系统
CN206176888U (zh) 一种利用液化空气供冷制取lng的系统
CN202430008U (zh) 一种五氧化二磷生产及热能回收装置
CN100430124C (zh) 一种用于气体储运的水合物生产工艺
CN204987651U (zh) 一种套管气降噪防爆液化装置
CN202655001U (zh) 一种大型熔硫釜
CN107987908A (zh) 用于可燃冰试采过程的天然气快速形成及原位存储系统
CN204097414U (zh) 一种超临界处理装置及含碳物质气化系统
WO2012026630A1 (fr) Dispositif de revaporisation de gaz naturel
CN207527285U (zh) Cng加气站利用lng冷能脱水的工艺系统
WO2014027787A2 (fr) Procédé de production d'hydrate de gaz par mise en réaction d'une pluralité de gaz hôtes avec de l'eau
CN220811864U (zh) 一种流化床甲醇重整制氢加氢一体化装置
CN216498481U (zh) 一种新型模块化高纯度二氧化碳液化提纯装置

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 12763257

Country of ref document: EP

Kind code of ref document: A2

ENP Entry into the national phase

Ref document number: 2013558783

Country of ref document: JP

Kind code of ref document: A

WWE Wipo information: entry into national phase

Ref document number: 14008451

Country of ref document: US

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 12763257

Country of ref document: EP

Kind code of ref document: A2