Chemical chain reaction device and use method thereof

Abstract

The invention discloses a chemical chain reaction device and a use method thereof, and belongs to the technical field of energy and chemical engineering. The chemical looping reaction device comprises an air reactor and a fuel reactor, the air reactor and the fuel reactor both adopt a bubbling fluidized bed form, the air reactor surrounds three sides of the fuel reactor, and the chemical looping reaction device further comprises a bed material circulating flow channel I and a bed material circulating flow channel II which are arranged between the air reactor and the fuel reactor, the upper end of the bed material circulating flow channel I is communicated with the fuel reactor, the lower end of the bed material circulating flow channel I is communicated with the air reactor, the upper end of the bed material circulating flow channel II is communicated with the air reactor, and the lower end of the bed material circulating flow channel II is communicated with the fuel reactor. According to the chemical looping reaction device, high-flux circular flowing of bed materials is achieved, heat transfer is enhanced, bed material abrasion and heat loss are reduced, the heat utilization efficiency is improved, the residence time of the reaction materials is conveniently adjusted so as to regulate the reaction process, and the chemical looping reaction device is simple in structure, convenient to operate and low in cost.

Description

Technical Field

[0001] The present invention relates to the field of energy and chemical technology, and in particular to a chemical chain reaction device and a method for using the same. Background Art

[0002] In the reaction process of chemical chain technology, the fuel does not come into direct contact with the air, but the combustion, gasification or reforming reaction of the fuel is achieved through the cyclic alternating reaction of the oxygen carrier between the two reactors; the oxygen carrier undergoes an oxidation reaction in the air reactor to obtain lattice oxygen, which is then transported to the fuel reactor for lattice oxygen and fuel to undergo reduction reactions such as combustion, gasification or reforming. The oxygen carrier that has lost lattice oxygen is recycled back to the air reactor, and relatively pure CO2 and water vapor or CO and H2 products can be obtained by avoiding the dilution of the gas phase products of the fuel reactor by N2. Based on the characteristics of the chemical chain reaction process that pure CO2 or CO and H2 (synthesis gas) can be obtained without additional air separation oxygen production, the technical development of the chemical chain reaction process is a hot topic of current research.

[0003] Chemical chaining technology can be used to convert gas, liquid, and solid fuels. How to design the reactor of chemical chaining technology to efficiently realize the technical advantages has become one of the key factors in whether chemical chaining technology can be promoted and applied. In order to achieve the smooth transportation and circulation of oxygen carrier bed materials, the main body of the device currently designed for chemical chain reaction adopts the form of two fluidized bed reactors in series, mainly including serial fluidized bed reactors and dual circulating fluidized bed reactors. The serial fluidized bed reactor is composed of a fast bed air reactor and a low-speed bubbling bed / turbulent bed fuel reactor. The air reactor and fuel reactor of the dual circulating fluidized bed reactor are composed of two circulating fluidized beds connected in series. Both forms, whether using a riser fast bed or a circulating fluidized bed, use high-speed air to carry the oxygen carrier particles out of the air reactor, and then return the oxygen carrier to the fuel reactor through a flow sealing valve after gas-solid separation through a cyclone separator. A large amount of gas is required to achieve the high gas velocity required for carrying out the oxygen carrier particles, which brings great difficulties to the device system design, solid particle residence time and operation and control of high circulation flux of the oxygen carrier bed material. At the same time, the high gas velocity will also aggravate the pulverization and wear of the oxygen carrier bed material and increase the loss of oxygen carrier. In addition, metal oxides (such as Fe2O3, NiO and Mn3O4, etc.) that usually act as oxygen carriers undergo an endothermic reaction with hydrocarbon fuels in the fuel reactor, relying on the heat carried by the hot oxygen carrier bed of the air reactor to maintain the reaction temperature of the fuel reactor. The atmospheric volume required for the high gas velocity of the air reactor takes away a large amount of sensible heat, resulting in heat loss, which increases the difficulty of thermal balance management of the entire reaction device.

[0004] Therefore, the prior art still needs to be improved and developed. Summary of the invention

[0005] In view of the above-mentioned deficiencies in the prior art, the object of the present invention is to provide a chemical chain reaction device and a method of using the same, aiming to solve the problem that a large amount of gas is required to achieve the high gas velocity required for carrying out the oxygen carrier particles, resulting in great difficulties in the device system design, the residence time of the reaction materials and the operation and control of the high circulation flux of the oxygen carrier bed material. At the same time, the high gas velocity will also aggravate the pulverization and wear of the oxygen carrier bed material and increase the loss of the oxygen carrier.

[0006] The technical solution of the present invention is as follows:

[0007] In a first aspect of the present invention, a chemical chain reaction device is provided, which includes an air reactor and a fuel reactor, wherein the air reactor and the fuel reactor are both in the form of a bubbling fluidized bed, and the air reactor surrounds the fuel reactor on three sides.

[0008] It also includes a bed material circulation flow channel I and a bed material circulation flow channel II arranged between the air reactor and the fuel reactor, the upper end of the bed material circulation flow channel I is communicated with the fuel reactor, the lower end of the bed material circulation flow channel I is communicated with the air reactor, the upper end of the bed material circulation flow channel II is communicated with the air reactor, and the lower end of the bed material circulation flow channel II is communicated with the fuel reactor.

[0009] Optionally, the air reactor comprises a lower air reactor dense phase zone and an upper air reactor dilute phase zone, the lower end of the air reactor dense phase zone is connected to the gas distribution plate I and the gas distribution chamber I in sequence, and the upper end of the air reactor dilute phase zone is connected to the cyclone separator I.

[0010] Optionally, the fuel reactor comprises a lower fuel reactor dense phase zone and an upper fuel reactor dilute phase zone, the lower end of the fuel reactor dense phase zone is connected to the gas distribution plate II and the gas distribution chamber II in sequence, and the upper end of the fuel reactor dilute phase zone is connected to the cyclone separator II.

[0011] Optionally, the lower end of the bed material circulation flow channel I is provided with horizontal openings and vertical openings. A gas distribution plate III is provided, and a gas distribution chamber III is provided at the lower end of the gas distribution plate III.

[0012] Optionally, the lower end of the bed material circulation flow channel II is provided with horizontal openings and vertical openings. A gas distribution plate IV is provided, and a gas distribution chamber IV is provided at the lower end of the gas distribution plate IV.

[0013] Optionally, the bed material circulation flow channel I and the bed material circulation flow channel II are respectively arranged on two opposite sides of the fuel reactor.

[0014] Optionally, a screw feeder is provided on the fuel reactor.

[0015] The second aspect of the present invention provides a method for using the chemical chain reaction device described in the present invention, wherein, in a fuel reactor, a high-valent oxidation state oxygen carrier bed material reacts with fuel to produce gas products (CO2 and water vapor or CO and H2), the gas products enter a cyclone separator II for dust removal to obtain a gas product, the high-valent oxidation state oxygen carrier bed material is reduced to a low-valent reduction state oxygen carrier bed material, and the low-valent reduction state oxygen carrier bed material enters an air reactor through a bed material circulation flow channel I; in the air reactor, the low-valent reduction state oxygen carrier bed material undergoes an oxidation reaction with air to generate a high-valent oxidation state oxygen carrier bed material, while releasing heat to increase the temperature of the high-valent oxidation state oxygen carrier bed material, the oxygen-depleted air is discharged after dust removal by the cyclone separator I, and the hot high-valent oxidation state oxygen carrier bed material returns to the fuel reactor through the bed material circulation flow channel II for recycling.

[0016] Optionally, air is passed through the gas distribution chamber I of the air reactor as a fluidizing medium and a reaction gas;

[0017] When solid fuel is used, it is added into the fuel reactor by a screw feeder, and water vapor and / or CO2 and / or part of the product gas of the fuel reactor is introduced into the gas distribution chamber II of the fuel reactor as fluidizing gas and / or gasifying agent; when gaseous or liquid fuel is used, it is directly introduced into the gas distribution chamber II and enters the fuel reactor, and it is both a reaction raw material and a fluidizing medium;

[0018] Water vapor and / or CO2 and / or part of the product gas of the fuel reactor are introduced into the gas distribution chamber III of the bed material circulation flow channel I and the gas distribution chamber IV of the bed material circulation flow channel II as fluidizing medium. The bed material delivery amount is controlled by adjusting the steam flow rate and cross-gas between the air reactor and the fuel reactor is prevented.

[0019] Optionally, the fuel includes one or more of gaseous fuel, liquid fuel and solid fuel.

[0020] Beneficial effect: The present invention adopts a bubbling fluidized bed for both the fuel reactor and the air reactor involved in the chemical chain reaction technology. The two reactors are connected by a surrounding combination and two bed material circulation flow channels are used to connect the two reactors. In this way, the air reactor for exothermic reaction surrounds the fuel reactor for endothermic reaction on three sides, which reduces the heat dissipation surface and heat loss. At the same time, the air reactor also provides radiation heat transfer, which is beneficial to increase and maintain the temperature of the fuel reactor. The two bed material circulation flow channels and the horizontal openings and vertical openings at their lower ends are arranged The invention discloses a type of gas distribution plate. By adjusting the gas velocity of the gas distribution plate to be higher than the minimum fluidization velocity of the bed material particles, the bed material circulation flux can be regulated. This avoids the requirement that the air reactor (fast bed or circulating fluidized bed) in the two-reactor series mode needs to be higher than the bed material particle carry-out velocity to regulate the bed material circulation flux (the bed material particle carry-out velocity is usually more than 20 times higher than the minimum fluidization velocity). The high-flux circulation flow of the oxygen-carrying bed material can be achieved without the high gas velocity of the bed material particle carry-out velocity of the fast bed / circulating fluidized bed, which greatly reduces the mutual collision of the bed material particles due to high-speed movement and the friction impact between the bed material particles and the vessel wall, reduces the wear and sensible heat loss of the oxygen-carrying bed material, improves the heat utilization efficiency, and at the same time facilitates the adjustment of the reaction material residence time to regulate the reaction process, thereby ensuring the reciprocating circulation of the oxygen-carrying bed material required for the chemical chain reaction between the two reactors and avoiding the technical requirements of contact between the fuel and the air. In addition, the device of the invention has a simple structure, is easy to operate, and has a low cost. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] Figure 1 A schematic diagram of a chemical chain reaction device provided by the present invention;

[0022] Figure 2 This is a schematic top view along the AA line of a chemical chain reaction device provided by the present invention.

[0023] In the figure, 1-air reactor; 1-1-dense phase zone of air reactor; 1-2-dilute phase zone of air reactor; 1-3-distributor plate of air reactor; 1-4-gas distribution chamber I; 1-5-cyclone separator I; 2-fuel reactor; 2-1-dense phase zone of fuel reactor; 2-2-dilute phase zone of fuel reactor; 2-3-distributor plate of fuel reactor; 2-4-gas distribution chamber II; 2-5-cyclone separator II; 3-bed material circulation flow channel I; 3-1-gas distribution plate III; 3-2-gas distribution chamber III; 4-bed material circulation flow channel II; 4-1-gas distribution plate IV; 4-2-gas distribution chamber IV; 5-screw feeder. DETAILED DESCRIPTION

[0024] The present invention provides a chemical chain reaction device and a method for using the same. To make the purpose, technical solution and effect of the present invention clearer and more specific, the present invention is further described in detail below. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not intended to limit the present invention.

[0025] Combination Figure 1-Figure 2As shown, an embodiment of the present invention provides a chemical chain reaction device, which includes an air reactor 1 and a fuel reactor 2. The air reactor 1 and the fuel reactor 2 both adopt a bubbling fluidized bed form. The air reactor 1 surrounds the fuel reactor 2 on three sides, and also includes a bed material circulation flow channel I 3 and a bed material circulation flow channel II 4 arranged between the air reactor 1 and the fuel reactor 2. The upper end of the bed material circulation flow channel I 3 is communicated with the fuel reactor 2, and the lower end of the bed material circulation flow channel I 3 is communicated with the air reactor 1. The upper end of the bed material circulation flow channel II 4 is communicated with the air reactor 1, and the lower end of the bed material circulation flow channel II 4 is communicated with the fuel reactor 2.

[0026] The embodiment of the present invention provides a chemical chain reaction device for chemical chain combustion, gasification and reforming reaction of gaseous, liquid and solid fuels. The device includes an air reactor, a fuel reactor, a bed material circulation flow channel I and a bed material circulation flow channel II. The air reactor surrounds the fuel reactor on three sides, and the bed material is circulated between the two reactors through two bed material circulation flow channels. The method of using the device includes inputting the fuel into the fuel reactor to carry out oxidation or partial oxidation / catalytic reforming reaction of the fuel with the high-valent oxidation state oxygen carrier bed material to obtain CO2, water vapor or synthesis gas, and the low-valent reduction state oxygen carrier bed material after deoxygenation enters the air reactor through the bed material circulation flow channel I to undergo oxidation reaction with air to obtain the high-valent oxidation state oxygen carrier bed material, while releasing heat, and the high-valent oxidation state oxygen carrier bed material returns to the fuel reactor through the bed material circulation flow channel II, and the heat required to maintain the reaction temperature of the fuel reactor is provided by the high-temperature oxygen carrier bed material and the radiant heat of the air reactor. The device of the embodiment of the present invention can realize high-throughput circulation flow of oxygen carrier bed material at low gas velocity, and can enhance heat transfer, reduce wear and heat loss of oxygen carrier bed material, improve heat utilization efficiency, and conveniently adjust the residence time of reaction materials to regulate the reaction process. It has a simple structure, is easy to operate, and has low cost.

[0027] Specifically, the air reactor 1 includes a lower air reactor dense phase zone 1-1 and an upper air reactor dilute phase zone 1-2. The lower end of the air reactor dense phase zone 1-1 is connected to the gas distribution plate I1-3 and the gas distribution chamber I1-4 in sequence, and the upper end of the air reactor dilute phase zone 1-2 is connected to the cyclone separator I1-5.

[0028] Specifically, the fuel reactor 2 includes a lower fuel reactor dense phase zone 2-1 and an upper fuel reactor dilute phase zone 2-2. The lower end of the fuel reactor dense phase zone 2-1 is connected to the gas distribution plate II 2-3 and the gas distribution chamber II 2-4 in sequence, and the upper end of the fuel reactor dilute phase zone 2-2 is connected to the cyclone separator II 2-5.

[0029] Specifically, the upper end of the bed material circulation flow channel I 3 is connected to the fuel reactor 2, and the lower end is connected to the air reactor 1. The lower end of the bed material circulation flow channel I 3 is provided with horizontal openings and vertical openings. Type gas distribution plate III 3-1, a gas distribution chamber III 3-2 is provided at the lower end of the gas distribution plate III 3-1.

[0030] More specifically, the upper end of the bed material circulation flow channel 13 is connected to the fuel reactor dense phase zone 2-1, and the lower end is connected to the air reactor dense phase zone 1-1. The lower end of the bed material circulation flow channel 13 is provided with horizontal openings and vertical openings. Type gas distribution plate III 3-1 (fluidizing gas enters in horizontal and vertical jets respectively, which is convenient for improving and regulating the circulating flow flux of the bed material), and a gas distribution chamber III 3-2 is provided at the lower end of the gas distribution plate III 3-1.

[0031] Specifically, the upper end of the bed material circulation flow channel II 4 is connected to the air reactor 1, and the lower end is connected to the fuel reactor 2. The lower end of the bed material circulation flow channel II 4 is provided with horizontal openings and vertical openings. Type gas distribution plate IV 4-1 (fluidizing gas enters in horizontal and vertical jets respectively, which is convenient for improving and regulating the circulating flow flux of the bed material), and a gas distribution chamber IV 4-2 is provided at the lower end of the gas distribution plate IV 4-1.

[0032] More specifically, the upper end of the bed material circulation flow channel II 4 is connected to the air reactor dense phase zone 1-1, and the lower end is connected to the fuel reactor dense phase zone 2-1. The lower end of the bed material circulation flow channel II 4 is provided with horizontal openings and vertical openings. Type gas distribution plate IV 4-1, a gas distribution chamber IV 4-2 is provided at the lower end of the gas distribution plate IV 4-1.

[0033] Specifically, the bed material circulation flow channel I 3 and the bed material circulation flow channel II 4 are respectively arranged on opposite sides of the fuel reactor 2 to achieve the circulation flow of the oxygen carrier bed between the two reactors.

[0034] Specifically, the fuel reactor 2 is provided with a screw feeder 5. The fuel is added into the fuel reactor by the screw feeder.

[0035] Combination Figure 1-Figure 2As shown, a method for using the chemical chain reaction device provided by an embodiment of the present invention, wherein, in the fuel reactor 2, a high-valent oxidation state oxygen carrier bed material reacts with the fuel to generate a gas product (CO2 and water vapor or CO and H2), the gas product enters the cyclone separator II 2-5 for dust removal to obtain a gas product, the high-valent oxidation state oxygen carrier bed material is reduced to a low-valent reduction state oxygen carrier bed material, and the low-valent reduction state oxygen carrier bed material enters the air reactor 1 through the bed material circulation flow channel I 3; in the air reactor 1, the low-valent reduction state oxygen carrier bed material undergoes an oxidation reaction with the air to generate a high-valent oxidation state oxygen carrier bed material, while releasing heat to increase the temperature of the high-valent oxidation state oxygen carrier bed material, the oxygen-depleted air is discharged after dust removal by the cyclone separator I1-5, and the hot high-valent oxidation state oxygen carrier bed material returns to the fuel reactor 2 through the bed material circulation flow channel II 4 for recycling.

[0036] The embodiment of the present invention adopts the above-mentioned method of use, which can achieve high-throughput circulation of oxygen carrier bed material at low gas velocity, enhance heat transfer, reduce oxygen carrier bed material wear and heat loss, improve heat utilization efficiency, and facilitate adjustment of the reaction material residence time to control the reaction process, and is easy to operate.

[0037] Specifically, the gas distribution chambers I1-4 of the air reactor 1 are supplied with air as a fluidizing medium and a reaction gas;

[0038] When solid fuel is used, it is added into the fuel reactor 2 by the screw feeder 5, and water vapor and / or CO2 and / or part of the product gas of the fuel reactor is introduced into the gas distribution chamber II 2-4 of the fuel reactor 2 as the fluidizing gas for fluidizing the bed material and / or the gasifying agent required for the gasification reaction; when gaseous or liquid fuel is used, it is directly introduced into the gas distribution chamber II 2-4 and enters the fuel reactor 2, and it is both the reaction raw material and the fluidizing medium;

[0039] Water vapor and / or CO2 and / or part of the product gas of the fuel reactor are introduced into the gas distribution chamber III 3-2 of the bed material circulation flow channel I 3 and the gas distribution chamber IV 4-2 of the bed material circulation flow channel II 4 as fluidizing media. The bed material delivery amount is controlled by adjusting the steam flow rate and cross-gas between the air reactor 1 and the fuel reactor 2 is prevented.

[0040] Specifically, the fuel includes one or more of gaseous fuel, liquid fuel and solid fuel.

[0041] The present invention is described in detail below through specific embodiments.

[0042] Embodiment 1: Provide a chemical chain reaction device

[0043] Combination Figure 1-Figure 2As shown, a chemical chain reaction device of this embodiment includes an air reactor 1 and a fuel reactor 2, wherein the air reactor 1 is a bubbling fluidized bed, and the fuel reactor 2 is a bubbling fluidized bed. The air reactor 1 surrounds the fuel reactor 2 on three sides, and also includes a bed material circulation flow channel I 3 and a bed material circulation flow channel II 4 arranged between the air reactor 1 and the fuel reactor 2, wherein the upper end of the bed material circulation flow channel I 3 is communicated with the fuel reactor 2, and the lower end of the bed material circulation flow channel I 3 is communicated with the air reactor 1, and the upper end of the bed material circulation flow channel II 4 is communicated with the air reactor 1, and the lower end of the bed material circulation flow channel II 4 is communicated with the fuel reactor 2. A screw feeder 5 is provided on the fuel reactor 2.

[0044] Among them, the air reactor 1 includes a lower air reactor dense phase zone 1-1 and an upper air reactor dilute phase zone 1-2. The lower end of the air reactor dense phase zone 1-1 is connected to the gas distribution plate I1-3 and the gas distribution chamber I1-4 in sequence, and the upper end of the air reactor dilute phase zone 1-2 is connected to the cyclone separator I1-5.

[0045] Among them, the fuel reactor 2 includes a lower fuel reactor dense phase zone 2-1 and an upper fuel reactor dilute phase zone 2-2. The lower end of the fuel reactor dense phase zone 2-1 is connected to the gas distribution plate II 2-3 and the gas distribution chamber II 2-4 in sequence, and the upper end of the fuel reactor dilute phase zone 2-2 is connected to the cyclone separator II 2-5.

[0046] The upper end of the bed material circulation flow channel I 3 is connected to the dense phase zone 2-1 of the fuel reactor, and the lower end is connected to the dense phase zone 1-1 of the air reactor. The lower end of the bed material circulation flow channel I 3 is provided with horizontal openings and vertical openings. Type gas distribution plate III 3-1, a gas distribution chamber III 3-2 is provided at the lower end of the gas distribution plate III 3-1.

[0047] The upper end of the bed material circulation flow channel II 4 is connected to the air reactor dense phase zone 1-1, and the lower end is connected to the fuel reactor dense phase zone 2-1. The lower end of the bed material circulation flow channel II 4 is provided with horizontal openings and vertical openings. Type gas distribution plate IV 4-1, a gas distribution chamber IV 4-2 is provided at the lower end of the gas distribution plate IV 4-1.

[0048] The bed material circulation flow channel I 3 and the bed material circulation flow channel II 4 are respectively arranged on two opposite sides of the fuel reactor 2 .

[0049] Example 2: The method of using the chemical chain reaction device of Example 1 is as follows:

[0050] The pine wood powder pellets are uniformly added into the fuel reactor 2 by the screw feeder 5. The NiO and Fe2O3 oxygen carrier bed material particles undergo gasification / partial oxidation and catalytic reforming reaction with the volatile matter and fixed carbon of the pine wood powder pellet fuel at 860°C. The pine wood powder particles are converted into synthesis gas with CO and H2 as the main components. The NiO and Fe2O3 oxygen carriers are reduced to low-valent Ni and Fe / FeO oxygen carrier bed materials. The synthesis gas product enters the cyclone separator II 2-5 for dust removal to obtain the product synthesis gas. The reduced Ni and Fe / FeO oxygen carrier bed materials enter the air reactor 1 through the bed material circulation flow channel I 3. In the air reactor 1, the Ni and Fe / FeO oxygen carrier bed materials undergo oxidation reaction with oxygen in the air at 950°C to generate NiO and Fe2O3 oxygen carrier bed materials, while releasing heat to increase and maintain the temperature of the oxygen carrier bed materials. The hot NiO and Fe2O3 oxygen carrier bed materials return to the fuel reactor 2 through the bed material circulation flow channel II 4 to form a circulation flow to realize the recycling of the oxygen carrier. The oxygen-depleted air enters the cyclone separator I1-5 for dust removal and then is discharged.

[0051] The gas distribution chambers I1-4 of the air reactor 1 are supplied with air as a fluidizing medium and a reaction gas;

[0052] The gas distribution chamber II 2-4 of the fuel reactor 2 is fed with water vapor and part of the synthesis gas produced by the fuel reactor as fluidizing gas and gasifying agent;

[0053] Water vapor is introduced into the gas distribution chamber III 3-2 of the bed material circulation flow channel I 3 and the gas distribution chamber IV 4-2 of the bed material circulation flow channel II 4 as the fluidizing medium. The oxygen carrier bed material delivery amount is controlled by adjusting the steam flow rate and the cross-gas between the air reactor 1 and the fuel reactor 2 is prevented.

[0054] Example 3: The method of using the chemical chain reaction device of Example 1 is as follows:

[0055] Methane is used as reaction fuel and as fluidizing gas and is introduced into the fuel reactor 2 through the gas distribution chamber II 2-4 and the gas distribution plate II 2-3. The lattice oxygen of the NiO and Fe2O3 oxygen carrier bed particles undergoes a complete oxidation combustion reaction with methane at 850°C. Methane is converted into CO2 and water vapor. The NiO and Fe2O3 oxygen carrier bed materials are reduced to low-valent Ni and Fe / FeO oxygen carrier bed materials. The CO2 and water vapor products enter the cyclone separator II 2-5 for dust removal to obtain CO2 and water vapor gas products. The reduced Ni and Fe / FeO oxygen carrier bed materials enter the air reactor 1 through the bed material circulation flow channel I 3. In the air reactor 1, the Ni and Fe / FeO oxygen carrier bed materials undergo oxidation reaction with oxygen in the air at 900°C to generate NiO and Fe2O3 oxygen carrier bed materials, while releasing heat to increase and maintain the temperature of the oxygen carrier bed materials. The hot NiO and Fe2O3 oxygen carrier bed materials return to the fuel reactor 2 through the bed material circulation flow channel II 4 to form a circulation flow to realize the recycling of the oxygen carrier. The oxygen-depleted air enters the cyclone separator I1-5 for dust removal and then is discharged.

[0056] The gas distribution chambers I1-4 of the air reactor 1 are supplied with air as a fluidizing medium and a reaction gas;

[0057] A portion of the CO2 and water vapor product gas introduced into the fuel reactor 2 through the gas distribution chamber III 3-2 of the bed material circulation flow channel I 3 and the gas distribution chamber IV 4-2 of the bed material circulation flow channel II 4 is used as the fluidizing medium. The oxygen carrier bed material delivery amount is controlled by adjusting the flow rate and mutual gas cross-talk between the air reactor 1 and the fuel reactor 2 is prevented.

[0058] In summary, the present invention provides a chemical chain reaction device and a method of using the same. The present invention adopts a bubbling fluidized bed form for the fuel reactor and the air reactor involved in the chemical chain reaction technology. The two reactors are connected by a three-sided surround combination and two bed material circulation flow channels. A high-throughput circulation flow of the oxygen carrier bed material can be achieved without the need for a fast bed to carry the bed material at a high gas velocity, thereby enhancing heat transfer, reducing oxygen carrier bed material wear and heat loss, and improving heat utilization efficiency. At the same time, it is convenient to adjust the residence time of the reaction materials to regulate the reaction process, thereby ensuring the reciprocating circulation of the oxygen carrier required for the chemical chain reaction between the two reactors and avoiding the technical requirements of contact between the fuel and the air. In addition, the device of the present invention has a simple structure, is easy to operate, and has low cost.

[0059] It should be understood that the application of the present invention is not limited to the above examples. For ordinary technicians in this field, improvements or changes can be made based on the above description. All these improvements and changes should fall within the scope of protection of the claims attached to the present invention.

Claims

1. A chemical chain reaction device, characterized in that: The invention comprises an air reactor (1) and a fuel reactor (2). Both the air reactor (1) and the fuel reactor (2) adopt a bubbling fluidized bed form. The air reactor (1) surrounds the fuel reactor (2) on three sides. It also includes a bed material circulation flow channel I (3) and a bed material circulation flow channel II (4) arranged between the air reactor (1) and the fuel reactor (2); the upper end of the bed material circulation flow channel I (3) is communicated with the fuel reactor (2), the lower end of the bed material circulation flow channel I (3) is communicated with the air reactor (1), the upper end of the bed material circulation flow channel II (4) is communicated with the air reactor (1), and the lower end of the bed material circulation flow channel II (4) is communicated with the fuel reactor (2).

2. The chemical chain reaction device according to claim 1, characterized in that: The air reactor (1) comprises a lower air reactor dense phase zone (1-1) and an upper air reactor dilute phase zone (1-2), wherein the lower end of the air reactor dense phase zone (1-1) is connected to a gas distribution plate I (1-3) and a gas distribution chamber I (1-4) in sequence, and the upper end of the air reactor dilute phase zone (1-2) is connected to a cyclone separator I (1-5).

3. The chemical chain reaction device according to claim 1, characterized in that: The fuel reactor (2) comprises a lower fuel reactor dense phase zone (2-1) and an upper fuel reactor dilute phase zone (2-2); the lower end of the fuel reactor dense phase zone (2-1) is connected to a gas distribution plate II (2-3) and a gas distribution chamber II (2-4) in sequence, and the upper end of the fuel reactor dilute phase zone (2-2) is connected to a cyclone separator II (2-5).

4. The chemical chain reaction device according to claim 1, characterized in that: The lower end of the bed material circulation flow channel I (3) is provided with horizontal openings and vertical openings. A gas distribution plate III (3-1) is provided at the lower end of the gas distribution plate III (3-1).

5. The chemical chain reaction device according to claim 1, characterized in that: The lower end of the bed material circulation flow channel II (4) is provided with horizontal openings and vertical openings. A gas distribution plate IV (4-1) is provided at the lower end of the gas distribution plate IV (4-1). A gas distribution chamber IV (4-2) is provided at the lower end of the gas distribution plate IV (4-1).

6. The chemical chain reaction device according to claim 1, characterized in that: The bed material circulation flow channel I (3) and the bed material circulation flow channel II (4) are respectively arranged on two opposite sides of the fuel reactor (2).

7. The chemical chain reaction device according to claim 1, characterized in that: The fuel reactor (2) is provided with a screw feeder (5).

8. A method for using the chemical chain reaction device according to any one of claims 1 to 7, characterized in that: In the fuel reactor (2), the high-valent oxidized oxygen carrier bed material reacts with the fuel to generate a gas product, which enters the cyclone separator II (2-5) for dust removal to obtain a gas product, and the high-valent oxidized oxygen carrier bed material is reduced to a low-valent reduced oxygen carrier bed material, which enters the air reactor (1) through the bed material circulation flow channel I (3); in the air reactor (1), the low-valent reduced oxygen carrier bed material undergoes an oxidation reaction with the air to generate a high-valent oxidized oxygen carrier bed material, while releasing heat to increase the temperature of the high-valent oxidized oxygen carrier bed material, and the oxygen-depleted air is discharged after dust removal by the cyclone separator I (1-5), and the hot high-valent oxidized oxygen carrier bed material returns to the fuel reactor (2) through the bed material circulation flow channel II (4) for recycling.

9. The method for using the chemical chain reaction device according to claim 8, characterized in that: The gas distribution chamber I (1-4) of the air reactor (1) is passed with air as a fluidizing medium and a reaction gas; When solid fuel is used, it is added into the fuel reactor (2) through a screw feeder (5), and water vapor and / or CO2 and / or part of the product gas of the fuel reactor is introduced into the gas distribution chamber II (2-4) of the fuel reactor (2) as fluidizing gas and / or gasifying agent; when gaseous or liquid fuel is used, it is directly introduced into the gas distribution chamber II (2-4) and enters the fuel reactor (2), and serves as both a reaction raw material and a fluidizing medium; Water vapor and / or CO2 and / or part of the product gas of the fuel reactor are introduced as fluidizing medium into the gas distribution chamber III (3-2) of the bed material circulation flow channel I (3) and the gas distribution chamber IV (4-2) of the bed material circulation flow channel II (4). The bed material delivery amount is controlled by adjusting the steam flow rate and cross-gas between the air reactor (1) and the fuel reactor (2) is prevented.

10. The method for using the chemical chain reaction device according to claim 8, characterized in that: The fuel includes one or more of gaseous fuel, liquid fuel and solid fuel.

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