TWI694863B - Circulating amount controllable fluidized bed reactor and circulating amount controllable dual fluidized bed reactors reaction system - Google Patents

Abstract

A circulating amount controllable fluidized bed reactor and a circulating amount controllable dual fluidized bed reactors reaction system are provided. The circulating amount controllable fluidized bed reactor includes a reaction tube and a flow rate controllable feeding device. The flow rate controllable feeding device includes a top end feeding inlet, a bottom discharging outlet, a bending part disposed between the top end feeding inlet and the bottom discharging outlet, and a bottom fluid inlet disposed adjacent to the bending part. A control fluid flows into the flow rate controllable feeding device via the bottom fluid inlet. The bottom discharging outlet is interconnected with a first unreacted solid feeding inlet. An unreacted solid passes through the top end feeding inlet, the bending part, the bottom discharging outlet, and the first unreacted solid feeding inlet and enters the reaction tube.

Description

Controllable circulation volume fluidized bed reactor and controllable circulation volume dual fluidized bed reactor Application system

The invention relates to a fluidized bed reactor with a controllable circulation amount and a dual fluidized bed reaction system with a controlled circulation amount, in particular to a fluidized bed reactor with a controllable circulation amount for removing acid gas and Controllable circulation volume double fluidized bed reaction system.

Hydrogen sulfide is a toxic gas that is common in chemical processes such as biogas and hydrodesulfurization processes for crude oil refining and must be removed. The conventional method for removing hydrogen sulfide includes the use of a fluidized bed with an absorbent. In order to extend the use time of the absorbent, the regeneration system is increased to use the fluidized bed as the reactor, and the absorbent can be smoothly returned to the deacidification reactor to achieve energy efficiency. Loop effect. However, the circulation volume of the conventional fluidized bed is not easy to control and cannot effectively regenerate the absorbent, resulting in the absorbent being unable to be used for a long time.

In view of this, the object of the present invention is to provide a fluidized bed reactor with a controllable circulation amount, which can overcome the above problems.

Another object of the present invention is to provide a controllable circulation amount dual fluidized bed reaction system using a controllable circulation amount fluidized bed reactor, which can overcome the above problems.

The controllable circulating fluidized bed reactor of the present invention is for the main reaction fluid to react with unreacted solids to generate a main reaction product containing the first reacted fluid and the reacted solids. The controllable circulating fluidized bed reactor includes a reaction tube and a flow-controllable feeding device. The reaction tube includes a main reaction fluid inlet, a first unreacted solids inlet, a second unreacted solids inlet, a reacted solids outlet, and a main reaction product outlet. The main reaction fluid inlet is provided at the bottom end of the reaction tube body for the main reaction fluid to enter the reaction tube body. The first unreacted solid inlet is disposed between the top and bottom of the reaction tube. The second unreacted solids inlet allows unreacted solids to enter the reaction tube. The outlet of the reacted solid is provided at a position adjacent to the bottom end of the reaction tube body for the reacted solid to leave the reaction tube body. The main reaction product outlet is set at the top of the reaction tube body for the main reaction product material to leave the reaction tube body. Flow-controllable feeding device includes a top feed port, a bottom discharge port, a bending part provided between the top feed port and the bottom discharge port, and a bottom fluid inlet provided at a position adjacent to the bending part . Among them, the control fluid enters the flow-controllable feed device from the bottom fluid inlet, the bottom outlet is connected to the first unreacted solid inlet, and the unreacted solid passes through the bending part, the bottom outlet, and the top feed inlet The first unreacted solid inlet enters the reaction tube.

In the embodiment of the present invention, the flow-controllable feeding device is an L-shaped valve.

In the embodiment of the present invention, the fluidized bed reactor with a controllable circulation amount is a gas/solid fluidized bed reactor.

The circulating volume controllable dual fluidized bed reaction system of the present invention comprises a circulating volume controllable fluidized bed reactor, a first separator, a variable diameter fluidized bed reactor, and a second separator. The first separator is in communication with a fluidized bed reactor with a controllable circulation volume to receive the main reaction generated material for separating the first reacted fluid from the reacted solids. Variable-diameter fluidized bed reactor and fluidized bed with controllable circulation The reactor is communicated to receive the reacted solids for the reacted reacted fluid to react with the reacted solids to generate a reacted reacted material including the second reacted fluid and unreacted solids. The variable-diameter fluidized bed reactor includes a first tube and a second tube. The first tube has a first inner diameter and includes a first fluid inlet, a first port, and a first solid inlet. The first fluid inlet is disposed at the bottom end of the first tube. The first interface is disposed on the top of the first tube. The first solid inlet is disposed between the first fluid inlet of the first pipe and the first interface. The second tube has a second inner diameter, and includes a second interface and a first outlet. The second interface is disposed at one end of the second tube, and is connected to the first interface to make the first tube and the second tube communicate with each other. The first outlet is provided at the other end of the second tube. Among them, the first inner diameter is larger than the second inner diameter. The second separator communicates with the variable-diameter fluidized bed reactor and the fluidized-bed reactor with a controllable circulation volume separately for separating the second reacted fluid from the unreacted solids and receiving the regeneration reaction from the variable-diameter fluidized bed reactor It can produce materials and provide unreacted solids. The circulating volume can be controlled fluidized bed reactor.

In an embodiment of the invention, the first separator includes a first separator inlet, a first separator solid outlet, and a first separator fluid outlet. The inlet of the first separator is connected to the outlet of the main reaction product, so that the main reaction product enters the first separator. The solids outlet of the first separator is provided at the bottom of the first separator, and the reacted solids separated by the main reaction product leave the first separator. The first separator fluid outlet is provided at a position other than the first separator inlet and the first separator solid outlet of the first separator, for the first reacted fluid separated by the main reaction product to leave the first separator.

In an embodiment of the present invention, the first solid inlet is in communication with the reacted solid outlet, and the reacted solid is fed into the variable-diameter fluidized bed reactor. The first fluid inlet is for the regeneration reaction fluid to enter the variable-diameter fluidized bed reactor. The first discharge port is used for the material generated by the regeneration reaction to leave the variable-diameter fluidized bed reactor.

In an embodiment of the invention, the second separator includes a second separator inlet, a second separator solid outlet, and a second separator fluid outlet. The inlet of the second separator communicates with the first outlet, The materials for the regeneration reaction enter the second separator. The solids outlet of the second separator is set at the bottom of the second separator and communicates with the top feed port, for the unreacted solids separated by the material generated by the regeneration reaction to leave the second separator and enter the fluidized bed with a controllable circulation for reaction Device. The second separator fluid outlet is provided at a position other than the first separator inlet and the first separator solid outlet of the second separator, for the second reacted fluid separated by the regeneration reaction material to leave the second separator.

In an embodiment of the present invention, the first inner diameter is 2 to 10 times the second inner diameter.

In the embodiment of the present invention, the variable-diameter fluidized bed reactor forms a rapid fluidized bed at a portion where the inner diameter is the second inner diameter.

In an embodiment of the present invention, the main reaction fluid is hydrogen sulfide, the unreacted solid is selected from the group consisting of zinc oxide, iron oxide, ferrous oxide, and mixtures thereof, and the regeneration reaction fluid is oxygen.

100: reaction tube

110: main reaction fluid inlet

121: The first unreacted solids import

122: second unreacted solids import

130: Export of reacted solids

140: main reaction generated material export

150: Flow-controllable feeding device

151: Top feed port

152: bottom discharge port

153: Bending section

154: Bottom fluid inlet

200: first separator

210: the first separator inlet

220: solid outlet of the first separator

230: fluid outlet of the first separator

300: Variable diameter fluidized bed reactor

301: Inner wall

310: The first pipe fitting

311: the first fluid inlet

312: the first interface

313: The first solid import

314: Pressure equalization chamber

315: homogenizing element

316: tapered part

320: Second pipe fitting

321: Second interface

322: the first outlet

333: Pipe fittings

400: second separator

410: second separator inlet

420: solid outlet of the second separator

430: second separator fluid outlet

510: fluid supply unit

520: fluid supply unit

530: fluid supply unit

540: fluid supply unit

550: fluid supply unit

600: solid supply unit

801: Axial

802: Radial

910: Fluidized bed reactor with controllable circulation

920: Controllable circulation volume double fluidized bed reaction system

D ₁ : first inner diameter

D ₂ : second inner diameter

L ₁ : first length

L ₂ : second length

1 is a schematic diagram of an embodiment of a fluidized bed reactor with a controllable circulation volume of the present invention; FIG. 2 is a schematic diagram of an embodiment of a dual fluidized bed reactor system with a controlled circulation volume of the present invention; FIG. 3 is a controllable circulation volume of the present invention 4 is a schematic diagram of an embodiment of a variable-diameter fluidized bed in a double-fluidized bed reaction system; FIG. 4 is a schematic diagram of a different embodiment of a dual-fluidized bed reaction system with a controllable circulation volume of the present invention; FIG. 5 is a dual-fluid with a controlled circulation volume Test results of the bed reaction system.

The fluidized bed reactor with controllable circulation amount of the present invention is preferably a gas/solid fluidized bed reactor used for gas/solid reaction, that is, the fluid is a gas. However, in different embodiments, the fluid may be a liquid, and the fluidized bed reactor with a controllable circulation amount is a liquid/solid fluidized bed reactor applied to a liquid/solid reaction.

As shown in the embodiment shown in FIG. 1, the circulating fluidized bed reactor 910 of the present invention includes a reaction tube 100 and a flow-controllable feeding device 150. The reaction tube body 100 includes a main reaction fluid inlet 110, a first unreacted solids inlet 121, a second unreacted solids inlet 122, a reacted solids outlet 130, and a main reaction product outlet 140. The main reaction fluid inlet 110 is provided at the bottom end of the reaction tube body 100 for the main reaction fluid to enter the reaction tube body 100. The first unreacted solid inlet 121 is disposed between the top and bottom of the reaction tube body 100. The second unreacted solid inlet 122 allows unreacted solid to enter the reaction tube body 100. The reacted solid outlet 130 is disposed adjacent to the bottom end of the reaction tube body 100 for the reacted solid to leave the reaction tube body 100. The main reaction product outlet 140 is provided at the top of the reaction tube body 100 for the main reaction product material to leave the reaction tube body 100.

As shown in the embodiment shown in FIG. 1, the flow-controllable feeding device 150 includes a top inlet 151, a bottom outlet 152, and a bending portion 153 disposed between the top inlet 151 and the bottom outlet 152 And a bottom fluid inlet 154 disposed at a position adjacent to the bent portion 153. Among them, the control fluid enters the flow-controllable feed device 150 from the bottom fluid inlet 154, the bottom outlet 152 communicates with the first unreacted solid inlet 121, and the unreacted solid passes through the bent portion 153 from the top feed inlet 151, The bottom outlet 152 and the first unreacted solid inlet 121 enter the reaction tube 100.

In the embodiment shown in FIG. 1, the flow-controllable feed device 150 is an L-shaped valve, and the bent portion 153 is a bent portion of the L-shaped valve. When the unreacted solid passes through the bent portion 153 through the tip feed port 151, the flow rate is reduced due to the curved path, which causes accumulation. Then, by increasing or decreasing the flow rate of the control fluid, such as an inert gas, which enters from the bottom fluid inlet 154, the unreacted solids can be controlled from entering the circulation volume. Flow of fluidized bed reactor 910. Among them, it is difficult for the general valve to control the flow into the fluidized bed, and the L-shaped valve adjusts the fluid flow at the inlet 154, which can make the absorbent flow more smoothly and achieve effective control of the regenerated absorbent circulation. More specifically, a fluid supply unit 550 equipped with an inert gas may be used to adjust the flow rate of unreacted solids from the bottom fluid inlet 154 into the fluidized bed reactor 910 with a controllable circulation amount. In different embodiments, the bent portion is not limited to a single curved member of 90°, and may be a member bent at different angles or multiple times.

As shown in the embodiment shown in FIG. 2, the circulating volume controllable dual fluidized bed reaction system 920 of the present invention includes a circulating volume controllable fluidized bed reactor 910, a first separator 200, and a variable diameter fluidized bed reactor 300, and second separator 400. The first separator 200 is in communication with a fluidized bed reactor 910 with a controllable circulation amount to receive a main reaction product for separating the first reacted fluid from the reacted solids. The variable-diameter fluidized bed reactor 300 is in communication with a fluidized-bed reactor 910 with a controllable circulation amount to receive the reacted solids for reacting the regenerated reaction fluid with the reacted solids to generate a regeneration reaction including the second reacted fluid and unreacted solids Generate materials. In other words, after the reaction of the variable-diameter fluidized bed, the solid is converted into a regeneration reaction solid.

As shown in the embodiment shown in FIG. 3, the variable-diameter fluidized bed reactor 300 includes a first tube 310 and a second tube 320. The first tube 310 has a first inner diameter D1 and includes a first fluid inlet 311, a first port 312, and a first solid inlet 313. The first fluid inlet 311 is disposed at the bottom end of the first tube 310. Further, the bottom of the variable-diameter fluidized bed reactor 300 may be provided with a pressure equalizing chamber 314 and a homogenizing element 315 such as a diffusion plate, so that the fluid reaction material enters the variable-diameter fluidized bed reactor 300 from the first fluid inlet 311 Later, it can flow to the other end more evenly. The first interface 312 is disposed on the top of the first tube 310. The first tube 310 is preferably tapered inwardly from the tapered portion 316 to form the first interface 312, but it is not limited thereto. The first solid inlet 313 is disposed between the first fluid inlet 311 and the first port 312 of the first pipe member 310 for the solid reaction material to enter the variable-diameter fluidized bed reactor 300. In terms of better implementation, the first solid The body inlet 313 is disposed between the homogenizing element 315 of the first tube 310 and the first interface 312.

As shown in the embodiment shown in FIG. 3, the second tube 320 has a second inner diameter D2 and includes a second interface 321 and a first discharge port 322. The second interface 321 is disposed at one end of the second tube 320 and is connected to the first interface 312 so that the first tube 310 and the second tube 320 communicate with each other. The first discharge port 322 is provided at the other end of the second pipe 320 opposite to the second port 321 for the reacted material to leave the variable-diameter fluidized bed reactor 300.

As shown in the embodiment shown in FIG. 3, viewed from different angles, the variable-diameter fluidized bed reactor 300 includes a pipe member 333, and the inner wall 301 of the pipe member 333 extends a first length L1 along the axial direction 801 with a first inner diameter D1, It shrinks in a radial direction 802 perpendicular to the axial direction 801 to a second inner diameter D2, and extends a second length L2 along the axial direction 801 with the second inner diameter D2. Among them, the tube 333 within the retracted range is a tapered portion 316. One end of the tube 333 having the first inner diameter D1 includes the first fluid inlet 311. The other end of the tube 333 having the second inner diameter D2 includes the first discharge port 322. The portion of the tube 333 having the first inner diameter D1 has a first solid inlet 313 at a position other than the fluid inlet 311.

In some operations using a fluidized bed reactor, the flow rate of the mixture in the fluidized bed reactor to the outlet must exceed a critical speed as the operating condition. For example, if solid materials are required to leave the outlet, the mixture The flow rate of the material to the outlet must exceed this critical speed. For the embodiment shown in FIG. 3, if the amount of solid materials entering from the first solid inlet 313 and exiting from the first outlet 322 is set to be equal, the flow rate of the mixture to the first outlet 322 must exceed At this critical speed, the solid material can reach and leave the first discharge port 322 with the fluid material. Therefore, in the variable-diameter fluidized bed reactor 300 of the present invention, the flow rate of the portion where the inner diameter is the second inner diameter D2 must exceed this critical speed. Since the first inner diameter D1 of the variable-diameter fluidized bed reactor 300 of the present invention is larger than the second inner diameter D2, when the flow rate of the mixed material leaving the variable-diameter fluidized bed reactor 300 is fixed, the mixed material The portion with the inner diameter of the first inner diameter D1 stays longer than the portion with the inner diameter of the second inner diameter D2. Based on the above, compared with the conventional fluidized bed reactor with uniform pipe diameter, if the flow rate of the mixture material to the outlet should also exceed the critical speed, in this variable diameter fluidized bed reactor, the fluid reaction material and the solid reaction material The portion with the inner diameter of the first inner diameter D1 can stay for a longer time, thereby prolonging the time of staying in the variable-diameter fluidized bed reactor, and making the reaction more sufficient.

In the aforementioned fluidized bed reactor, the flow rate of the mixture material to the outlet exceeds the critical speed, while the solid material can follow the fluid material to reach and leave the outlet, the fluidized bed reactor forms a fast fluidized bed. Among them, the fluidized bed reactor has a minimum fluidization speed. When the flow velocity of the fluid in the fluidized bed reactor is 20 to 100 times the minimum fluidization speed, it belongs to a fast fluidized bed. In a preferred embodiment, the variable-diameter fluidized bed reactor 300 forms a rapid fluidized bed at a portion where the inner diameter is the second inner diameter D2. The first inner diameter D1 is 2 to 10 times the second inner diameter D2. In an embodiment, the first inner diameter D1 is 3 times the second inner diameter D2. The variable-diameter fluidized bed reactor 300 forms a bubbling bed at a portion where the inner diameter is the first inner diameter D1. Among them, when the flow velocity of the fluid in the fluidized bed reactor is 3 to 10 times the minimum fluidization speed, it belongs to the bubbling bed.

As shown in the embodiment shown in FIG. 2, the second separator 400 communicates with the variable-diameter fluidized bed reactor 300 and the controllable circulation fluidized bed reactor 910 respectively, for separating the second reacted fluid from the unreacted solids In addition, the variable-diameter fluidized bed reactor 300 receives regenerated reaction products and provides unreacted solids to the circulating fluidized bed reactor 910 with controllable circulation. Among them, the second reacted fluid and the corresponding main reaction and regeneration reaction include but are not limited to the following.

The main reaction is ZnO+H2S=ZnS+H2O, the main reaction fluid is H2S, the unreacted solid is H2S, the first reacted fluid is H2O, the reacted solid is ZnS, the regeneration reaction is ZnS+O2=ZnO+SO2, the regeneration reaction The fluid is O2.

The main reaction is FeO+H2S=FeS+H2O, the main reaction fluid is H2S, the unreacted solid is FeO, the first reacted fluid is H2O, the reacted solid is FeS, the regeneration reaction is FeS+O2=FeO+SO2, the regeneration reaction The fluid is O2.

The main reaction is Fe2O3+3 H2S=Fe2S3+H2O, the main reaction fluid is H2S, the unreacted solid is Fe2O3, the first reacted fluid is H2O, the reacted solid is Fe2S3, the regeneration reaction is Fe2S3+O2=Fe2O3+3S, regeneration The reaction fluid is O2.

The main reaction is MOx+x H2S+(CO,H2O)=MSx+x H2O, the main reaction fluid is H2S+(CO,H2O), the unreacted solid is MOx, the first reacted fluid is H2O, the reacted solid is MSx, regeneration The reaction is MSx+3x/2 O2=MOx+x SO2, and the regeneration reaction fluid is O2.

In the embodiment shown in FIG. 2, the reaction tube body 100 of the fluidized bed reactor 910 with a controllable circulation amount is a tube body with an equal inner diameter. However, in different embodiments, the reaction tube body 100 can also use the aforementioned variable-diameter fluidized bed reactor.

In the embodiment shown in FIG. 2, the first separator 200 includes a first separator inlet 210, a first separator solid outlet 220, and a first separator fluid outlet 230. The first separator inlet 210 communicates with the main reaction product outlet 140 for the main reaction product to enter the first separator 200. The first separator solid outlet 220 is provided at the bottom of the first separator 200 for the reacted solid separated by the main reaction product to leave the first separator 200. The first separator fluid outlet 230 is provided at a position other than the first separator inlet 210 and the first separator solid outlet 220 of the first separator 200, and is preferably at the top of the first separator 200 for generation by the main reaction The first reacted fluid for material separation leaves the first separator 200.

In the embodiment shown in FIG. 2, the second separator 400 includes a second separator inlet 410, a second separator solid outlet 420, and a second separator fluid outlet 430. Second separator inlet 410 is in communication with the first outlet 322 for the material generated by the regeneration reaction to enter the second separator 400. The second separator solid outlet 420 is provided at the bottom of the second separator 400 and communicates with the first unreacted solid inlet 121 for the unreacted solid separated by the regeneration reaction material to leave the second separator 400 and enter the circulation volume. Controlled fluidized bed reactor 910. In the embodiment shown in FIG. 2, the first solid inlet 313 is in communication with the reacted solid outlet 130 for the reacted solid to enter the variable-diameter fluidized bed reactor 300. The first fluid inlet 311 is for the regeneration reaction fluid to enter the variable-diameter fluidized bed reactor 300. The first outlet 322 is used for the regeneration reaction product to leave the variable-diameter fluidized bed reactor 300.

The second separator fluid outlet 430 is provided at a position other than the first separator inlet 410 and the first separator solid outlet 420 of the second separator 400, and is preferably located at the top of the first separator inlet 410 for the regeneration reaction The second reacted fluid separated by the generated material leaves the second separator 400.

In a preferred embodiment, fluid supply units 510, 520, 530, 540, etc. may be used for fluid supply or flow rate adjustment, and solid supply unit 600 may be used for solid supply, for example. More specifically, in one embodiment, a fluid supply unit 510 may be used to supply the main reaction fluid, and a fluid supply unit 520 containing an inert gas may be used to adjust the concentration of the supplied main reaction fluid. The fluid supply unit 530 may be used to supply the regeneration reaction fluid. A fluid supply unit 540 filled with an inert gas may be used to adjust the flow rate of the reacted solids entering the variable-diameter fluidized bed reactor 300. Among them, a communication pipe unit may be further provided between the first solid inlet 313 and the reacted solid outlet 130 to improve the regulation efficiency of the flow rate of unreacted solids. On the other hand, as shown in FIG. 4, according to the design or use requirements, a thermal insulation device such as thermal insulation foam can be provided outside part of the elements of the controllable circulation volume dual fluidized bed reaction system 920.

Fig. 5 is the test result of the controllable circulation volume double fluidized bed reaction system. Among them, the test temperature is room temperature, the flow rate of inert gas from the bottom fluid inlet 154 (see Figure 1) is 0.5~1.5L/min, the length of the reaction tube 100 is 2 meters, and the tube diameter is 5 inches Inch, the material is SUS310. Specifically, the flow rate of the inert gas entering the bottom end fluid inlet is changed, and the relationship between the circulation volume of the solid (absorbent) and the flow rate of the inert gas in this system is observed. As shown in Figure 5, from the experimental results, in the 0.5-1.5L/min inert gas flow rate range, the relationship between the solid circulation volume and the inert gas flow rate is y=21.402x-7.014, which is a linear relationship. According to this, the solid circulation volume can be controlled by changing the flow rate of the inert gas entering the bottom fluid inlet. In other words, the flow rate of the fluidized bed reactor with controllable circulation volume of the present invention can be effectively controlled.

Although the foregoing description and drawings have disclosed preferred embodiments of the present invention, it must be understood that various additions, many modifications and substitutions may be used in the preferred embodiments of the present invention without departing from the scope as defined in the appended patent application The spirit and scope of the principles of the present invention. Those of ordinary skill in the art to which the present invention pertains will appreciate that the present invention can be used in many forms, structures, arrangements, ratios, materials, elements, and component modifications. Therefore, the embodiments disclosed herein should be considered to illustrate the present invention, rather than to limit the present invention. The scope of the present invention should be defined by the scope of the attached patent application and cover its legal equivalents, not limited to the previous description.

100: reaction tube

110: main reaction fluid inlet

121: The first unreacted solids import

122: second unreacted solids import

130: Export of reacted solids

140: main reaction generated material export

150: Flow-controllable feeding device

200: first separator

210: the first separator inlet

220: solid outlet of the first separator

230: fluid outlet of the first separator

300: Variable diameter fluidized bed reactor

311: the first fluid inlet

313: The first solid import

322: the first outlet

400: second separator

410: second separator inlet

420: solid outlet of the second separator

430: second separator fluid outlet

510: fluid supply unit

520: fluid supply unit

530: fluid supply unit

540: fluid supply unit

550: fluid supply unit

600: solid supply unit

910: Fluidized bed reactor with controllable circulation

920: Controllable circulation volume double fluidized bed reaction system

Claims (10)

A controllable circulating fluidized bed reactor for a main reaction fluid to react with an unreacted solid to generate a main reaction product containing a first reacted fluid and a reacted solid The fluidized bed reactor includes: a reaction tube including: a main reaction fluid inlet provided at the bottom end of the reaction tube for the main reaction fluid to enter the reaction tube; a first unreacted solid inlet provided at Between the top and the bottom of the reaction tube; a second unreacted solid inlet for the unreacted solid to enter the reaction tube; a reacted solid outlet, located adjacent to the circulating fluidized bed controllable reaction The position of the bottom end of the reactor for the reacted solids to leave the fluidized bed reactor with controllable circulation volume; and an outlet of the main reaction product, which is provided at the top of the reaction tube body for the main reaction product to leave the Reaction tube; and a flow-controllable feed device, including a top feed port, a bottom feed port, a bent portion provided between the top feed port and the bottom feed port, and a A bottom fluid inlet disposed at a position adjacent to the bent portion, wherein a control fluid enters the flow-controllable feed device from the bottom fluid inlet, the bottom outlet is in communication with the first unreacted solid inlet, the Unreacted solids enter the reaction tube from the top feed port through the bent portion, the bottom discharge port, and the first unreacted solid inlet. The circulating volume controllable fluidized bed reactor as described in item 1 of the patent application scope, wherein the flow controllable feed device is an L-shaped valve. The fluidized bed reactor with controllable circulation volume as described in item 1 of the patent application is a gas/solid fluidized bed reactor. A circulating volume controllable dual-fluid bed reaction system, comprising: a circulating volume controllable fluidized bed reactor as described in any one of patent application items 1 to 3; a first separator, and the circulating volume A controllable fluidized bed reactor communicates to receive the main reaction product to separate the first reacted fluid from the reacted solids; a variable-diameter fluidized bed reactor is fluidized with the controllable circulation The bed reactor communicates to receive the reacted solids for a regenerated reaction fluid to react with the reacted solids to generate a regenerated reaction-forming material including a second reacted fluid and the unreacted solids, including; a first pipe member having A first inner diameter, including: a first fluid inlet, located at the bottom end of the first tube; a first interface, located at the top of the first tube; a first solid inlet, located at the first tube Between the first fluid inlet and the first interface; and a second tube with a second inner diameter, including: a second interface disposed at one end of the second tube and connected to the first interface And make the first tube and the second tube communicate with each other; a first discharge port is provided at the other end of the second tube; wherein, the first inner diameter is greater than the second inner diameter; a second separator , Respectively communicated with the variable-diameter fluidized bed reactor and the controllable circulating volume fluidized-bed reactor for separating the second reacted fluid from the unreacted solid and receiving from the variable-diameter fluidized bed reactor The regeneration reaction generates materials and provides the unreacted generated solids to the fluidized bed reactor with a controllable circulation amount. The circulating volume controllable dual-fluid bed reaction system as described in item 4 of the patent application scope, wherein the first separator comprises: a first separator inlet, which is connected to the outlet of the main reaction product for the generation of the main reaction The material enters the first separator; a first separator solid outlet is provided at the bottom of the first separator for the reacted solid separated by the main reaction product to leave the first separator; and a first The separator fluid outlet is provided at a position other than the first separator inlet and the first separator solid outlet of the first separator, for the first reacted fluid separated by the main reaction product to leave the first Splitter. The circulating volume controllable dual-fluid bed reaction system as described in item 5 of the patent application scope, wherein: the first solid inlet is in communication with the reacted solid outlet for the reacted solid to enter the variable-diameter fluidized bed reactor The first fluid inlet is for the regeneration reaction fluid to enter the variable diameter fluidized bed reactor; the first outlet is for the regeneration reaction product to leave the variable diameter fluidized bed reactor. The circulating volume controllable dual-fluid bed reaction system as described in item 6 of the patent application scope, wherein the second separator includes: a second separator inlet, which communicates with the first discharge port for the regeneration reaction to generate The material enters the second separator; a second separator solid outlet is provided at the bottom of the second separator and communicates with the top feed port for the unreacted solid separated by the regeneration reaction material to leave the first separator Two separators, and enter the fluidized bed reactor with controllable circulation volume; A second separator fluid outlet is provided at a position other than the first separator inlet of the second separator and the solid outlet of the first separator, for the second reacted fluid separated by the material generated by the regeneration reaction to leave The second separator. The circulating volume controllable dual-fluid bed reaction system as described in item 4 of the patent application scope, wherein the first inner diameter is 2 to 10 times the second inner diameter. As described in item 4 of the patent application, the circulating volume controllable dual-fluid bed reaction system, the variable-diameter fluidized bed reactor forms a rapid fluidized bed at a portion where the inner diameter is the second inner diameter. The circulating volume controllable two-fluid bed reaction system as described in item 4 of the patent application scope, wherein the main reaction fluid is hydrogen sulfide, and the unreacted solid is selected from zinc oxide, iron oxide, ferrous oxide and mixtures thereof Group, the regeneration reaction fluid is oxygen.

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