WO2007141833A1 - Appareil de post-traitement d'hydrate et procédé de régulation du diamètre d'une particule d'hydrate - Google Patents

Appareil de post-traitement d'hydrate et procédé de régulation du diamètre d'une particule d'hydrate Download PDF

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Publication number
WO2007141833A1
WO2007141833A1 PCT/JP2006/311100 JP2006311100W WO2007141833A1 WO 2007141833 A1 WO2007141833 A1 WO 2007141833A1 JP 2006311100 W JP2006311100 W JP 2006311100W WO 2007141833 A1 WO2007141833 A1 WO 2007141833A1
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WO
WIPO (PCT)
Prior art keywords
hydrate
particle size
fluidized bed
bed reactor
particles
Prior art date
Application number
PCT/JP2006/311100
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English (en)
Japanese (ja)
Inventor
Shinji Takahashi
Masahiro Takahashi
Takashi Arai
Kazuyoshi Matsuo
Original Assignee
Mitsui Engineering & Shipbuilding Co., Ltd.
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 Mitsui Engineering & Shipbuilding Co., Ltd. filed Critical Mitsui Engineering & Shipbuilding Co., Ltd.
Priority to PCT/JP2006/311100 priority Critical patent/WO2007141833A1/fr
Publication of WO2007141833A1 publication Critical patent/WO2007141833A1/fr

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Classifications

    • 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
    • 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

Definitions

  • the present invention relates to a hydrate post-treatment device and a hydrate particle size control method, and more particularly, to a hydrate post-treatment device and a hydrate post-treatment device capable of obtaining a uniform and optimum particle size.
  • the present invention relates to a hydrate particle size control method.
  • the hydrate particles in the fluidized bed reactor are sent to a molding machine and granulated and formed into a product, the hydrate particles in the fluidized bed reactor are quantitatively and There is a demand for a stable supply.
  • the particle size of hydrate particles is small! /, And the surface area of hydrate particles increases, so the hydrate formation rate increases, but atmospheric pressure, which has been studied as a hydrate storage condition, — Low stability at 20 ° C. Therefore, in the secondary generator, it is necessary to control the particle size of the hydrate particles so that the generation rate of the hydrate is increased to some extent, and the stability under the above-mentioned storage conditions is an optimal value.
  • the hydrate particles have the same particle size, and the hydrate particles flow inside the fluidized bed reactor. There is a problem that it is not stable. Therefore, in the secondary generator, it is necessary to control the generation conditions so that the uniformity of the hydrate particle size is high. However, since the fluidized bed reactor is a high-pressure vessel, it is difficult to control the particle size visually. Disclosure of the invention
  • the present invention has been made to solve the above problems, and a first object is to quantitatively convert hydrate particles, which are said to have strong adhesion and binding properties, into fluidized bed reactor force. And it is providing the hydrate post-processing apparatus which can be extracted stably.
  • a second object of the present invention is to provide a secondary generator or the like that has high uniformity without visually monitoring the particle size of the hydrate particles and can obtain hydrate particles with an optimum particle size.
  • Another object of the present invention is to provide a hydrate particle size control method for controlling the particle size of hydrate particles in the hydrate aftertreatment device and the hydrate aftertreatment device.
  • the invention described in claim 1 is a hydrate post-treatment device for post-treating hydrate particles obtained by bringing water into contact with a hydrate-forming gas, wherein the hydrate particles
  • a fluidized bed reactor that is maintained in a fluidized state by the introduced hydrate-forming gas is provided with a dispersion plate having a large number of air holes, and the upper part of the dispersion plate is used as a fluidized bed portion and the lower part of the dispersion plate is disposed below.
  • a differential pressure detecting means for detecting a differential pressure with the fluidized gas introduction part is provided, and when the pressure of the fluidized bed part becomes higher than the pressure of the fluidized gas introduction part, the rotational speed of the take-out conveyor is increased, When the pressure of Doso portion has decreased lower than the pressure of the fluidizing gas inlet is directed to hydrate post-processing apparatus, characterized in that lowering the rotational speed of the take-out conveyor.
  • the invention according to claim 2 is a hydrate post-treatment device for post-treating hydrate particles obtained by bringing water and hydrate-forming gas into contact, wherein the hydrate particles are Fluidized bed reaction maintained in a fluidized state by the introduced hydrate-forming gas
  • a dispersion plate having a large number of ventilation holes is provided in the vessel, the fluidized bed portion is provided above the dispersion plate, the fluidized gas introduction portion is provided below the dispersion plate, and a hydrate particle discharge port is provided on the dispersion plate.
  • a take-out conveyor is provided below the hydrate particle discharge port, and a differential pressure detecting means for detecting a differential pressure between the fluidized bed part and the fluidized gas introduction part is provided in the fluidized bed reactor.
  • the invention according to claim 3 is the hydrate post-processing device according to claim 1 or 2, wherein the opening width of the hydrate particle discharge port and the rotational speed of the take-out conveyor are independent or simultaneously.
  • the present invention relates to an idle post-treatment device characterized by control.
  • the opening width of the hydrate particle discharge port and the rotation speed of the take-out conveyor are controlled independently or simultaneously, so that hydrate particles having strong adhesion and binding properties are taken out. It is possible to dispense more quantitatively and stably from the fluidized bed reactor using a conveyor.
  • the invention described in claim 4 is a hydrate post-treatment device for post-treating hydrate particles obtained by bringing water into contact with hydrate-forming gas, wherein the hydrate particles are A fluidized bed reactor that is maintained in a fluidized state by the introduced hydrate forming gas, and a hydrate granule for obtaining a particle size of the hydrate particles flowing in the fluidized bed reactor. Based on the particle size of the hydrate particles obtained by the diameter measuring means and the hydrate particle diameter measuring means, the temperature of the hydrate forming gas introduced into the fluidized bed reactor and the temperature inside the fluidized bed reactor are determined.
  • hydrate particle size control means for controlling the particle size of the hydrate particles, wherein the hydrate particle size control means includes at least one of the hydrate forming gas and the fluidized bed reactor.
  • the temperature of the hydrate particles is increased when the hydrate particle size determined by the hydrate particle size control means is smaller than a predetermined range, and is decreased when the hydrate particle size is larger than the predetermined range. It relates to a hydrate post-processing device.
  • This hydrate post-treatment device is a device for applying various post-treatments such as dehydration and cooling to the nodulate produced by the primary generator to obtain a high purity hydrate.
  • various post-treatments such as dehydration and cooling to the nodulate produced by the primary generator to obtain a high purity hydrate.
  • the particle size of the hydrate particles to be produced becomes smaller.
  • the temperature inside the reactor is lowered, or the temperature of the introduced idolate forming gas is lowered, the particle size of the hydrate particles produced increases.
  • nodulate particles having a predetermined uniform particle diameter are formed in the fluidized bed reactor, so that the fluid state of the hydrate particles in the fluidized bed reactor is stabilized.
  • the hydrate particle size is controlled by the hydrate particle size control unit based on the hydrate particle size obtained by the hydrate particle size measurement unit, so that it is a high pressure vessel. In the fluidized bed reactor, the operator can visually monitor the particle size and improve the operability without having to control the reaction conditions.
  • a dehydrator that performs physical dehydration and hydration dehydration is provided in the previous stage of the fluidized bed reactor, and the hydrate particles generated in the primary generator are preliminarily processed. Therefore, excess water may be removed.
  • the hydrate-forming gas include a gas that forms hydrate with water, such as natural gas, methane, ethane, propane, butane, carbon dioxide, oxygen, nitrogen, and hydrogen.
  • the invention described in claim 5 is the hydrate post-processing device according to claim 4, wherein the hydrate particle size measuring means images the hydrate particles flowing in the fluidized bed reactor.
  • the present invention relates to a hydrate post-processing apparatus comprising: a means; and an average particle diameter calculating means for obtaining an average particle diameter of the hydrate particles based on image data of hydrate particles imaged by the imaging means.
  • the average particle size calculation means calculates the average particle size of the hydrate particles based on the image data of the hydrate particles captured by the imaging means, when the particle size distribution of the hydrate particles changes, The hydrate particle size can be measured in real time.
  • the invention according to claim 6 is a method in which hydrate particles produced by contacting water and a hydrate-forming gas are fluidized by the hydrate-forming gas in a fluidized bed reactor.
  • a hydrate particle size control method for controlling the hydrate particle size to a predetermined average particle size, the hydrate particle size measuring step for obtaining a particle size of the hydrate particles flowing in the reactor And controlling the temperature of the hydrate-forming gas introduced into the fluidized bed reactor and the temperature inside the fluidized bed reactor based on the particle size of the hydrate particles obtained in the hydrate particle size measuring step.
  • a hydrate particle size control step for controlling the particle size of the hydrate particles.
  • the hydrate forming gas and The temperature of at least one of the inside of the fluidized bed reactor is increased when the particle size of the hydrate particles obtained by the hydrate particle size measuring means is smaller than a predetermined range, and the particle size of the particles of the hydrate particles is predetermined.
  • the present invention relates to a method for controlling a hydrate particle size, characterized in that it is lowered when it is larger than the range.
  • the hydrate forming gas and the fluidized bed reactor when the particle size of the hydrate in the fluidized bed reactor is smaller than a predetermined range, the hydrate forming gas and the fluidized bed reactor The temperature of at least one of the parts is increased to increase the particle size of the hydrate particles.
  • the temperature of at least one of the hydrate forming gas and the fluidized bed reactor is lowered to reduce the particle size of the hydrate particles. Decrease.
  • a hydrate post-treatment device and a hydrate granule that can obtain hydrate particles having an optimum particle size with high uniformity without visually monitoring the particle size.
  • a diameter control method is provided. Further, hydrate particles having strong adhesion and binding properties can be discharged quantitatively and stably.
  • FIG. 1 is a schematic configuration diagram of a hydrate post-processing apparatus according to the present invention.
  • FIG. 2 An example of an image of hydrate particles in a fluidized bed reactor, which is a secondary generator, taken with a CCD camera.
  • FIG. 3 is a schematic configuration diagram showing another embodiment of the hydrate post-processing apparatus according to the present invention.
  • FIG. 4 is a cross-sectional view taken along the line XX in FIG.
  • FIG. 5 is a sectional view taken along the line Y—Y in FIG.
  • FIG. 6 is a perspective view of a shutter.
  • a hydrate production line including a secondary generator which is an example of a hydrate post-processing apparatus according to the present invention, will be described.
  • the hydrate production line 1000 includes a primary generator 100 that generates hydrate that also has water and natural gas power, and a hydrate dehydration that dehydrates the hydrate generated by the primary generator 100.
  • Tower 200 and hydrate dehydrated in hydrate dewatering tower 200 And a secondary generator 300 for increasing the purity of hydrate by contacting with natural gas.
  • the primary generator 100 includes a reaction tank 102 for generating water and natural gas by contacting water and natural gas, a water supply line 104 for supplying water to the reaction tank 102, and a natural gas for the reaction tank 102.
  • Natural gas supply line 106 for supplying water
  • a stirrer 108 for stirring water and natural gas in the reaction tank 102
  • the natural gas supplied from the natural gas supply line 106 that has not reacted with water.
  • a gas circulation line 110 for returning the natural gas of the reaction to the reaction tank 102 and a slurry circulation line 112 for extracting and circulating the hydrate slurry generated in the reaction line 102 are provided.
  • One end of the gas circulation line 110 opens near the top of the reaction tank 102, and the other end communicates with a gas outlet pipe 114 disposed near the bottom of the reaction tank 102.
  • the gas circulation line 110 is provided with a compressor 110A and a heat exchange 110B.
  • the slurry circulation line 112 is provided with a pump 112A and a heat exchange ⁇ 112B, and hydrate slurry is drawn out from between the pump 112A and the heat exchange ⁇ 112B. Hydrate extraction line 116 is branched.
  • the primary generator 100 has a gas outlet line 120 for extracting unreacted natural gas from the reaction tank 102 and introducing it into the secondary generator 300.
  • the idrate dehydration tower 200 has a substantially upright cylindrical shape, and a bottom force hydrate slurry is introduced through a hydrate extraction line 116.
  • a dewatering screen section 202 is formed in the upper half of the hydrate dewatering tower 200.
  • a dewatering screen section 202 is formed in the dewatering screen section 202.
  • a dewatering screen 204 in which a large number of holes of, for example, 50 / zm are formed on the entire surface is formed. Is provided.
  • a water recovery jacket 206 for recovering water separated from the hydrate particles by the dehydration screen 204 is provided! /.
  • a water return line 118 for returning the water accumulated in the water recovery jacket 206 to the reaction tank 102 is provided.
  • a dewatering and idrate transporting conveyor 208 which is a screw conveyor for charging the hydrate particles dehydrated in the hydrate dewatering tower 200 into the secondary generator 300. Being! /
  • the secondary generator 300 is provided in the fluidized bed reactor 302 and the bottom of the fluidized bed reactor 302, A gas blow-out pipe 304 for injecting natural gas upward, and a jacket provided on the outer wall of the fluidized bed reactor 302, in which a refrigerant flows to maintain the inside of the fluidized bed reactor 302 at a predetermined temperature 306
  • the top force of the fluidized bed reactor 302 also has a slurry circulation line 308 that draws the mixed slurry of natural gas with the nodulate particles and returns it to the bottom of the fluidized bed reactor 302.
  • a cyclone 310 for separating the slurry into natural gas and hydrate particles is provided.
  • a gas return line 312 for returning the natural gas separated from the slurry to the fluidized bed reactor 302 is branched and communicated with the gas outlet pipe 304.
  • the gas return line 312 is provided with a compressor 312A and a heat exchanger 312B.
  • a CCD camera 314C for imaging the flowing hydrate particles is installed inside the fluidized bed reactor 3.
  • the secondary generator 300 further obtains the average particle diameter of the hydrate particles based on the image force captured by the CDD camera, and the refrigerant flowing through the jacket 306 based on the obtained average particle diameter of the hydrate particles.
  • a secondary generator controller 350 is provided that controls the amount and temperature, and the temperature of the natural gas that returns the gas return line 312 back to the fluidized bed reactor 302.
  • temperature sensors 351 and 352 are provided between the heat exchange 312A of the gas return line 31 2 and the gas outlet pipe 304 and inside the fluidized bed reactor 302, respectively. In the temperature sensors 351 and 352, respectively.
  • the temperature detection result is also input to the secondary generator control unit 350. As a result, the control of the refrigerant flowing through the heat exchanger 312B and the jacket 306 is correct, and feedback is performed along the direction.
  • a screw conveyor 316 for taking out hydrate particles is provided in the vicinity of the bottom of the fluidized bed reactor 302. Downstream of the secondary generator 300, a former 400 is provided for creating and forming the nodulate particles taken out by the take-out conveyor 316.
  • reference numeral 10 is a natural gas storage tank
  • 20 is a water storage tank.
  • the natural gas supply line 106 may be provided with a compressor 12 for boosting pressure.
  • water at a predetermined temperature supplied from the water supply line 104 and natural gas at a predetermined temperature supplied from the natural gas supply line 106 are maintained at a predetermined temperature and pressure.
  • slurry of idrate is produced.
  • Excess natural gas is also blown through the gas circulation line 110 into the slurry layer in the reaction tank 102 with the gas blowing pipe 114 force.
  • the produced slurry of the noidate is returned to the reaction tank 102 through the slurry circulation line 112, while a part of the slurry is withdrawn from the nodule extraction line 116 and is fed into the hydrate dehydration tower 200. Introduced at the bottom. In the hydrate dewatering tower 200, the slurry is separated into water and hydrate particles, and the hydrate particles having a specific gravity smaller than that of the water float up in the hydrate dewatering tower 200 and gather at the top of the hydrate dewatering tower 200. . Then, water between the hydrate particles is pushed out to the water recovery jacket 206 through the dehydration screen 204 in the dehydration screen unit 202. The water pushed out to the water recovery jacket 206 is returned to the reaction tank 102 through the water return line 118.
  • the dehydrated hydrate particles are extracted from the top of the hydrate dewatering tower 200 by the dehydrated hydrate transport conveyor 208 and introduced into the fluidized bed reactor 302 of the secondary generator 300.
  • the inside of the fluidized bed reactor 302 is maintained at a predetermined temperature by the jacket 306, and at the same time, is brought to a predetermined pressure by the natural gas derived from the gas outlet line 120 and the natural gas ejected from the gas outlet pipe 304. Is retained.
  • the hydrate particles introduced into the fluidized bed reactor 302 are maintained in a fluidized state by natural gas blown out from the gas blowing pipe 304.
  • the hydrate particles come into contact with the natural gas again in the fluidized bed reactor 302, the water in the hydrate particles reacts with the natural gas to newly generate hydrate. As a result, the hydrate particles are dried and at the same time the hydrate purity is increased. Furthermore, the particle size increases and the particle size distribution is made uniform.
  • the nodulate particles having a high particle and idrate purity and having a uniform particle size are taken out of the fluidized bed reactor 302 by the take-out conveyor 316, and granulated and formed by the forming unit 400.
  • hydrate particles are continuously imaged inside the fluidized bed reactor 302 by the CCD camera 314.
  • An example of the noid rate particle R image captured by the CCD camera 314 is shown in FIG.
  • the image data of the hydrate particles is also generated by the CCD camera 314 force.
  • the relationship between the particle size d and the number n of hydrate particles is determined. Then, the average diameter D is obtained from the particle diameter d and the number n.
  • the formula for obtaining the average diameter D is as follows.
  • the area average diameter D3 is most preferred.
  • the secondary generator control unit 350 may reduce the flow rate of the refrigerant flowing through the jacket 306, or the temperature of the refrigerant. Or the temperature inside the fluidized bed reactor 302 is increased.
  • the heat exchanger 312B is controlled to increase the temperature of the natural gas ejected from the gas outlet pipe 304. Thereby, the particle size of the hydrate particles in the fluidized bed reactor 302 is increased.
  • the secondary generator control unit 350 reduces the force that increases the flow rate of the refrigerant flowing through the jacket 306 or the temperature of the refrigerant. Then, the temperature inside the fluidized bed reactor 302 is lowered. At the same time, the heat exchange 312 ⁇ ⁇ is controlled to lower the temperature of the natural gas ejected from the gas outlet pipe 304. Thereby, the particle size of the hydrate particles in the fluidized bed reactor 302 is reduced.
  • the flow rate and temperature of the refrigerant flowing through the jacket 306 and the temperature of the natural gas ejected from the gas blowing pipe 304 are maintained as they are.
  • the particles in the fluidized bed reactor 302 are real-time.
  • the average diameter D is obtained.
  • the temperature in the fluidized bed reactor 302 and the gas blowing pipe 3 04 Force Because the temperature of the natural gas to be ejected is controlled, there is no control delay in controlling the particle size of the hydrate particles.
  • a laser irradiation type particle size measuring device can also be used as the particle size measuring means.
  • the fluidized bed reactor 302 is provided with a dispersion plate 320 having a large number of vent holes 318 therein.
  • a fluidized bed portion 322 is formed above the dispersion plate 320, and a fluidized gas introduction portion 324 is formed below the dispersion plate 320.
  • the fluidized bed reactor 302 is provided with a hydrate particle inlet 326 at the top and a fluidized gas inlet 328 at the bottom.
  • Unreacted natural gas in the fluidized bed section 322 is supplied to the fluidized gas introduction section 324 via the cyclone 310, the compressor 312A, and the heat exchanger 312B. Further, the fluidized bed reactor 302 passes through the side surface of the fluidized bed reactor 302 through the lower part of the dispersion plate 320, and is provided with a take-out competitor (hereinafter referred to as a takeout competitor) provided in the radial direction of the fluidized bed reactor 302. This is called a screw conveyor.) 316A is provided.
  • the dispersion plate 320 has a rectangular hydrate particle discharge port 330 directly above the screw conveyor 316A.
  • the screw conveyor 316A is formed of a casing 332 and screw blades 334 as shown in FIG.
  • the casing 332 has an opening 336 that faces the hydrate particle discharge port 330 of the dispersion plate 320.
  • the opening 336 is formed in the same shape as the hydrate particle discharge port 330.
  • the screw conveyor 316A has a cylindrical shutter 340 between the casing 332 and the screw blades 334.
  • the shutter 340 has a notch 344 in the body 342 thereof.
  • the notch 344 is formed by a plurality of, for example, a first plurality of notch parts 344A and a notch part 344B, and the first notch part 344A is more than the first notch part 344A.
  • the notch 344B in 2 has a larger opening width.
  • the opening area of the nodule particle discharge port 330 provided in the dispersion plate 320 can be arbitrarily changed by rotating the shutter 340.
  • the notch 344 may have an opening width that increases in a stepwise manner toward the tip of the shirt 340 as described above !, but the opening width may be continuously increased. Oh ,.
  • the shutter 340 has ring-shaped gears 346 at the tip and side surfaces thereof. Each of these gears 346 is in mesh with the small gear 348. These small gears 348 are provided on a rotating shaft 354 that passes through the fluidized bed reactor 302 and are rotated by a motor 356 with a speed reducer. Further, the screw blades 334 of the screw conveyor 316A are rotated by another motor 358.
  • the present invention has a differential pressure detecting means 360 for detecting the differential pressure between the fluidized bed portion 322 and the fluidized gas introducing portion 324.
  • the differential pressure detecting means 360 includes a first pressure sensor 362 provided at the top of the fluidized bed reactor 3002, a second pressure sensor 364 provided at the bottom of the fluidized bed reactor 302, and first and second pressure sensors.
  • the controller 366 is configured to control either one of the motors 356 and 358 or both at the same time when the differential pressure between the 362 and 364 deviates from a predetermined range force.
  • the natural gas When natural gas is supplied to the fluidized gas introduction section 324 of the fluidized bed reactor 302, the natural gas is jetted from the numerous vent holes 318 provided in the dispersion plate 320 to the fluidized bed section 322 to fluidize the hydrate particles R.
  • the fluidized hydrate particles R flow into the hydrate particle discharge port 330 provided in the dispersion plate 320, and are discharged out of the fluidized bed reactor 3002 by the screw conveyor 316A.
  • the flow state of the hydrate particles is monitored by the first and second pressure sensors 362 and 364.
  • the differential pressure is increased. It is known that the differential pressure decreases as the amount of hydrate particles in the fluidized bed portion 322 decreases as it increases.
  • the same effect can be obtained by rotating the shutter 340 to control the opening area of the hydrate particle discharge port 330 provided on the dispersion plate 320 instead of controlling the rotation speed of the screw conveyor 316A. . Further, the same effect can be obtained by controlling the screw conveyor 316A rotation speed and the rotation position of the shutter 340 simultaneously.

Abstract

La présente invention concerne une plaque de dispersion installée dans un réacteur à lit fluidisé, dans lequel les particules d'hydrate sont conservées à l'état fluide à l'aide d'un gaz, formant de l'hydrate, introduit par en dessous. La partie supérieure de la plaque de dispersion sert de partie lit fluidisé et la partie inférieure de la plaque de dispersion sert de partie introduisant un gaz fluidisant. En outre, un orifice d'évacuation de particules d'hydrate est disposé dans la plaque de dispersion et un transporteur de sortie est installé sous l'orifice d'évacuation de particules d'hydrate. Les moyens de détection de pression différentielle, destinés à détecter la pression différentielle entre la partie lit fluidisé et la partie introduction de gaz fluidisé, sont placés dans le réacteur à lit fluidisé. Lorsque la pression se trouvant dans la partie lit fluidisé dépasse la pression présente dans la partie introduction de gaz fluidisé, la vitesse de rotation du transporteur de sortie augmente. En revanche, lorsque la pression se trouvant dans la partie lit fluidisé descend en dessous de la pression présente dans la partie introduction de gaz fluidisé, la vitesse de rotation du transporteur de sortie baisse.
PCT/JP2006/311100 2006-06-02 2006-06-02 Appareil de post-traitement d'hydrate et procédé de régulation du diamètre d'une particule d'hydrate WO2007141833A1 (fr)

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Application Number Priority Date Filing Date Title
PCT/JP2006/311100 WO2007141833A1 (fr) 2006-06-02 2006-06-02 Appareil de post-traitement d'hydrate et procédé de régulation du diamètre d'une particule d'hydrate

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PCT/JP2006/311100 WO2007141833A1 (fr) 2006-06-02 2006-06-02 Appareil de post-traitement d'hydrate et procédé de régulation du diamètre d'une particule d'hydrate

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108434790A (zh) * 2018-05-09 2018-08-24 常州大学 一种水合物浆液气液固三相分离装置

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2005255945A (ja) * 2004-03-15 2005-09-22 Mitsui Eng & Shipbuild Co Ltd ガスハイドレート製造方法及び装置
JP2006117755A (ja) * 2004-10-20 2006-05-11 Mitsui Eng & Shipbuild Co Ltd 高濃度ガスハイドレート生成装置およびその装置を用いたガスハイドレート製造プラント
JP2006160820A (ja) * 2004-12-03 2006-06-22 Mitsui Eng & Shipbuild Co Ltd ハイドレート後処理装置およびハイドレート粒径制御方法

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2005255945A (ja) * 2004-03-15 2005-09-22 Mitsui Eng & Shipbuild Co Ltd ガスハイドレート製造方法及び装置
JP2006117755A (ja) * 2004-10-20 2006-05-11 Mitsui Eng & Shipbuild Co Ltd 高濃度ガスハイドレート生成装置およびその装置を用いたガスハイドレート製造プラント
JP2006160820A (ja) * 2004-12-03 2006-06-22 Mitsui Eng & Shipbuild Co Ltd ハイドレート後処理装置およびハイドレート粒径制御方法

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108434790A (zh) * 2018-05-09 2018-08-24 常州大学 一种水合物浆液气液固三相分离装置

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