WO2007141833A1

WO2007141833A1 - Hydrate post treatment apparatus and hydrate particle diameter control method

Info

Publication number: WO2007141833A1
Application number: PCT/JP2006/311100
Authority: WO
Inventors: Shinji Takahashi; Masahiro Takahashi; Takashi Arai; Kazuyoshi Matsuo
Original assignee: Mitsui Engineering & Shipbuilding Co., Ltd.
Priority date: 2006-06-02
Filing date: 2006-06-02
Publication date: 2007-12-13

Abstract

A dispersing plate is provided in a fluidized bed reactor in which hydrate particles are kept in a fluid state by a hydrate forming gas introduced from below. The upper part in the dispersing plate functions as a fluidized bed part, and the lower part in the dispersing plate functions as a fluidizing gas introducing part. Further, a hydrate particle discharge port is provided in the dispersing plate, and a takeout conveyor is provided below the hydrate particle discharge port. Differential pressure detection means for detecting the differential pressure between the fluidized bed part and the fluidized gas introduction part is provided in the fluidized bed reactor. When the pressure in the fluidized bed part has become higher than the pressure in the fluidized gas introduction part, the rotation speed of the takeout conveyor is increased. On the other hand, when the pressure in the fluidized bed part has become lower than the pressure in the fluidized gas introducing part, the rotation speed of the takeout conveyor is lowered.

Description

Specification

Hydrate post-processing apparatus and noid rate particle size control method

Technical field

TECHNICAL FIELD [0001] 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.

Background art

[0002] As an idrate production line, water and a hydrate-forming gas such as methane gas are brought into contact with each other under a predetermined temperature and pressure to generate a hydrate, and a primary generator generates no hydrate. A secondary generator (hydration dehydrator) that further increases the purity of the hydrate by bringing the hydrate into contact with the hydrate is under investigation (for example, Japan Special 2003- 041273). Gazette, and Japanese Unexamined Patent Publication No. 2003-105362; In view of the fact that hydrate particles having a high degree of dryness as well as purity can be easily obtained, the use of a fluidized bed reactor as a secondary generator has been studied.

[0003] Since 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.

[0004] On the other hand, 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.

[0005] In addition, when a fluidized bed reactor is used as the secondary generator, 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

[0006] 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.

[0007] 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.

[0008] 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 In addition, 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 fluidizing gas introduction section; a hydrate particle discharge opening provided in the dispersion plate; a takeout conveyor provided below the hydrate particle discharge opening; and the fluidized bed reactor including the fluidized bed section 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.

In this hydrate post-treatment device, when the pressure in the fluidized bed section becomes higher than the pressure in the fluidized gas introduction section, the rotational speed of the take-out conveyor is increased, and the pressure in the fluidized bed section is increased by the fluidized gas. When the pressure is lower than the pressure in the introduction section, the rotational speed of the take-out conveyor is lowered. This stabilizes the flow of hydrate particles in the fluidized bed, so that hydrate particles with strong adhesion and binding can be quantitatively and stably obtained from the fluidized bed reactor using the take-out conveyor. It can be taken out.

[0010] 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. In addition, 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. Furthermore, when a cylindrical shutter having the same axial center as that of the take-out conveyor is rotatably provided in the take-out conveyor, and the pressure in the fluidized bed is higher than the pressure in the fluidizing gas inlet When the opening of the hydrate particle discharge port is widened by the shutter and the pressure of the fluidized bed portion becomes lower than the pressure of the fluidized gas introduction portion, the hydrate particle discharge by the shutter. About hydrate aftertreatment apparatus characterized by narrowing the opening width of the mouth.

[0011] In this hydrate post-treatment device, when the pressure in the fluidized bed portion becomes higher than the pressure in the fluidized gas introduction portion, the opening width of the hydrate particle discharge port is widened by the shutter, and the fluidized bed When the pressure of the section becomes lower than the pressure of the fluidizing gas introduction section, the opening width of the hydrate particle discharge port is narrowed by the shutter, so that hydrate particles having strong adhesion and binding properties are removed from the conveyor. Can be quantitatively and stably removed from the fluidized bed reactor.

[0012] 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.

In this hydrate post-processing apparatus, 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.

[0014] 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. And 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.

[0015] 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. In the fluidized bed reactor, if the temperature inside the reactor is increased or the temperature of the hydrate forming gas to be introduced is increased, the particle size of the hydrate particles to be produced becomes smaller. In addition, if 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.

[0016] In the above-mentioned no-id post-treatment device, when the particle size of the hydrate in the fluidized bed reactor is smaller than a predetermined range, at least one of the no-, idlate-forming gas and the inside of the fluidized bed reactor. The temperature is increased to increase the particle size of the hydrate particles. When the particle size of the hydrate in the fluidized bed reactor is larger than the predetermined range, 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. Let

[0017] As a result, 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. In addition, as described above, 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.

[0018] In the hydrate post-treatment device, 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. Here, examples of 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.

[0019] 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.

[0020] In this hydrate post-treatment device, the hydrate forming gas to be introduced and the above-mentioned hydrate forming gas so that the average particle size of the hydrate particles calculated by the average particle size calculating means is within a predetermined range. Control the temperature inside the fluidized bed reactor. Since 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.

[0021] 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. In the processing apparatus, 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. In the hydrate particle size control process, 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.

[0022] In the above-mentioned method for controlling the particle size of the hydrate, 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. When the particle size of the hydrate in the fluidized bed reactor is larger than a predetermined range, 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.

[0023] As a result, particles and id particles having a predetermined uniform particle diameter are formed in the fluidized bed reactor, and the fluid state of the hydrate particles in the fluidized bed reactor is stabilized. Hydrate particle size Since the hydrate particle size is controlled based on the particle size of the nodulate particles obtained in the measurement process, the operator visually determines the particle size in the fluidized bed reactor, which is a high-pressure vessel. This improves the operability of the hydrate after-treatment device that does not require control of reaction conditions while monitoring.

[0024] As described above, according to the present invention, 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.

Brief Description of Drawings

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.

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.

BEST MODE FOR CARRYING OUT THE INVENTION

Hereinafter, 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.

As shown in FIG. 1, 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.

[0028] 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, and 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.

[0029] 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. In addition, 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. Further, 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. 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. Outside the dewatering screen 204, a water recovery jacket 206 for recovering water separated from the hydrate particles by the dehydration screen 204 is provided! /. Between the water recovery jacket 206 and the reaction tank 102, a water return line 118 for returning the water accumulated in the water recovery jacket 206 to the reaction tank 102 is provided.

[0031] At the top of the hydrate dewatering tower 200, there 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! /

[0032] 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 And 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. In the middle of the slurry circulation line 308, a cyclone 310 for separating the slurry into natural gas and hydrate particles is provided.

From the cyclone 310, 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. In addition, a CCD camera 314C for imaging the flowing hydrate particles is installed inside the fluidized bed reactor 3.

[0034] 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. Further, 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. In FIG. 1, reference numeral 10 is a natural gas storage tank, and 20 is a water storage tank. If desired, the natural gas supply line 106 may be provided with a compressor 12 for boosting pressure.

Hereinafter, the operation of the hydrate production line 1000 will be described.

In the primary generator 100, 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. In contact with the reaction tank 102 held, 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.

[0037] 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.

On the other hand, 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.

Accordingly, since 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.

[0040] In this way, 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. Product P. Here, 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.

[0041] In the secondary generator 350, the image data of the hydrate particles is also generated by the CCD camera 314 force. When input, the number of pixels corresponding to each of the hydrate particle images captured by the CCD camera 314 is obtained, and the image area S of each hydrate particle is obtained from the number of pixels. Then, assuming that the image is circular, the diameter d that gives an image area S = π (12 −4) is defined as the particle size of the hydrate particles.

[0042] Next, 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.

(a) Number average diameter Dl = ∑ (nd) / Σ η

(b) Length average diameter D2 = ∑ (nd ² ) / ∑nd

(c) Area average diameter D3 = ∑ (nd ³ ) / ∑ nd ²

(d) Sedimentation average diameter D4 = ∑ (nd ⁴ ) / ∑nd ³

Of these formulas, the area average diameter D3 is most preferred.

[0043] When the average diameter D force thus obtained is smaller than a predetermined range, 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. At the same time, 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.

On the other hand, when the average diameter D is larger than the predetermined range, 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 制御 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.

On the other hand, when the average diameter D is within the predetermined range, 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.

In the hydrate production line 1000 according to this embodiment, since the hydrate particles in the fluidized bed reactor 302 are continuously photographed by the CCD camera 314, the particles in the fluidized bed reactor 302 are real-time. The average diameter D is obtained. Based on the average diameter D thus obtained in real time, 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. As described above, a laser irradiation type particle size measuring device can also be used as the particle size measuring means.

Next, another embodiment of the hydrate particle dispensing means in the hydrate post-processing apparatus according to the present invention will be described.

As shown in FIG. 3, 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.

[0049] 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.

[0050] As shown in Fig. 4, 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. In addition, 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.

[0051] Here, if the diameter of the screw blade 334 is D "and the width of the dispersion plate 320, the idle particle discharge port 330 and the opening 336 of the casing 332 is W, W <D".

Furthermore, the screw conveyor 316A has a cylindrical shutter 340 between the casing 332 and the screw blades 334. As shown in FIG. 6, the shutter 340 has a notch 344 in the body 342 thereof. As shown in FIG. 6, 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. [0053] Since the shutter 340 has the same axis as the screw blade 334, 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 ,.

Further, as shown in FIG. 6, 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.

Further, 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.

[0056] Next, the quantitative dispensing of hydrate particles will be described.

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. Let 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.

[0057] The flow state of the hydrate particles is monitored by the first and second pressure sensors 362 and 364. When the amount of hydrate particles in the fluidized bed 322 increases, 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.

[0058] However, when the differential pressure between the first and second pressure sensors 362, 364 becomes larger than the set value, the rotational speed of the first motor 358 is increased by the controller 366 command, and the screw co Increases the amount of hydrate particles dispensed by NVEA 316A. On the other hand, when the differential pressure between the first and second pressure sensors 362 and 364 becomes smaller than the set value, the rotation speed of the first motor 358 is suppressed by the control device 366 command, and the hydrate by the screw conveyor 316A is suppressed. The amount of discharged particles is reduced. Accordingly, hydrate particles are quantitatively discharged from the fluidized bed reactor 302.

In this case, 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.

Claims

The scope of the claims

[1] An idling post-treatment apparatus for post-treating hydrate particles obtained by bringing water into contact with hydrate-forming gas, wherein the hydrate particles are formed by introducing a downward force. A fluidized bed reactor that is maintained in a fluidized state by a gas is provided with a dispersion plate having a large number of vent holes. Furthermore, a hydrate particle discharge port is provided in the dispersion plate, a take-out conveyor is provided below the hydrate particle discharge port, and the fluidized bed reactor and the fluidized gas are provided in the fluidized bed reactor. A differential pressure detection means for detecting the differential pressure with the introduction part is provided, and when the pressure in the fluidized bed part becomes higher than the pressure in the fluidized gas introduction part, the rotational speed of the take-out conveyor is increased, Pressure is fluidized gas Roh time has fallen lower than the pressure of the inlet portion, characterized in that the lower the rotational speed of the take-out conveyor, Idore over preparative post-processing apparatus.

[2] A post-treatment device for post-treatment of hydrate particles obtained by bringing water into contact with a hydrate-forming gas, wherein the hydrate particles are formed by introducing downward force. A fluidized bed reactor that is maintained in a fluidized state by a gas is provided with a dispersion plate having a large number of vent holes. Furthermore, a hydrate particle discharge port is provided in the dispersion plate, a take-out conveyor is provided below the hydrate particle discharge port, and the fluidized bed reactor and the fluidized gas are provided in the fluidized bed reactor. A differential pressure detection means for detecting the differential pressure with the introduction section is provided, and a cylindrical shutter having the same axis as that of the take-out conveyor is rotatably provided in the take-out conveyor so that the pressure in the fluidized bed section is reduced. Fluidization When the pressure in the fluid inlet is higher than the pressure in the fluidized gas inlet, the shutter is used to widen the opening width of the hydrate particle outlet, and when the pressure in the fluidized bed is lower than the pressure in the fluidized gas inlet. A hydrate post-processing apparatus characterized in that the opening width of the hydrate particle discharge port is narrowed by a cutter.

[3] The hydrate post-processing apparatus according to claim 1 or 2, wherein an opening width of the idle particle discharge port and a rotation speed of the take-out conveyor are controlled independently or simultaneously.

[4] A post-treatment device for post-treatment of hydrate particles obtained by bringing water into contact with a hydrate-forming gas, wherein the hydrate particles are hydrate-formation in which downward force is also introduced. A fluidized bed reactor that is maintained in a fluidized state by a gas, a hydrate particle size measuring means for determining the particle size of hydrate particles flowing in the fluidized bed reactor, and a hydrate determined by the hydrate particle size measuring means. The hydrate particle size is controlled by 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 rate particles. Control means, wherein the hydrate particle size control means is configured to control the temperature of at least one of the hydrate forming gas and the fluidized bed reactor in advance. Hydrate characterized in that it is increased when the particle size of the hydrate particles obtained by the hydrate particle size control means is smaller than a predetermined range, and is lowered when the particle size of the hydrate particles is larger than the predetermined range. Post-processing device.

[5] The hydrate particle size measuring means includes an imaging means for imaging hydrate particles flowing in a fluidized bed reactor, and the hydrate particles based on image data of hydrate particles imaged by the imaging means. The hydrate post-processing apparatus according to claim 4, further comprising an average particle diameter calculating means for determining an average particle diameter of the hydrate.

[6] A hydrate post-treatment device in which hydrate particles produced by contacting water and a hydrate-forming gas are caused to flow in the fluidized bed reactor by the hydrate-forming gas, and then the hydrate A hydrate particle size control method for controlling the particle size of the hydrate to a predetermined average particle size, the hydrate particle size measurement step for obtaining the particle size of the hydrate particles flowing in the reactor, and the hydrate particle size Based on the particle size of the hydrate particles obtained in the measurement process, the temperature of the hydrate forming gas introduced into the fluidized bed reactor and the temperature inside the fluidized bed reactor are controlled to control the particle size of the hydrate particles. A hydrate particle size control step for controlling the hydrate particle size control step. In either case, the temperature 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 is decreased when the particle size of the hydrate particles is larger than the predetermined range. A hydrate particle size control method characterized by this.