Complexing agent recovery device and catalyst impregnation system

Abstract

The application provides a complexing agent recovery device and a catalyst impregnation system, which comprises a calcination furnace, a separation device, a buffer device, an absorption device and a complexing agent storage tank; a feeding port of the calcination furnace is used for introducing catalyst materials impregnated by using a complexing method, the calcination furnace is used for calcining the introduced catalyst materials containing a complexing agent to generate calcination tail gas; a gas inlet of the separation device is communicated with a gas outlet of the calcination furnace and is used for introducing the calcination tail gas, the separation device is used for dedusting the calcination tail gas; a gas inlet of the buffer device is communicated with a gas outlet of the separation device, the buffer device is used for removing solid particles in the calcination tail gas; a gas inlet of the absorption device is communicated with a gas outlet of the buffer device, the absorption device is used for absorbing the complexing agent in the calcination tail gas to form a complexing agent solution and discharging gas through a gas outlet; a liquid inlet of the complexing agent storage tank is communicated with a liquid outlet of the absorption device and is used for introducing the complexing agent solution, and a liquid outlet of the complexing agent storage tank is used for leading out the complexing agent solution.

Description

Technical Field

[0001] This invention relates to the field of catalyst preparation equipment technology, and in particular to a complexing agent recovery device and a catalyst impregnation system. Background Technology

[0002] In current industrial production processes, metal-supported catalysts are primarily prepared through impregnation, with the introduction of metal mainly achieved via impregnation with saturated nitrate solutions. Saturated nitrate solutions are the most commonly used metal salt solutions in industry, offering advantages such as high solubility, no residue after calcination, and non-corrosiveness to industrial equipment. However, with increasingly stringent national environmental regulations, the NOx emissions from these solutions have become a concern. X Gas emissions are putting increasing pressure on environmental protection; during the roasting process of nitrate solutions, a large amount of NO is produced. X Gas, which gives rise to subsequent NO X The absorption and treatment unit has placed enormous operational pressure on the system. Current national environmental protection standards require NO... X Emissions below 100 mg / m³ 3 It may decrease further in the future.

[0003] A type that does not produce NO X The emission method involves complexation impregnation, where an impregnation solution containing a complexing agent and a metal salt is used. This causes the metal ions to form a highly soluble complex with the complexing agent. After impregnation, the complexing agent volatilizes through calcination, while the metal remains in the catalyst. The volatilized complexing agent is discharged from the calcination furnace with the exhaust gas and can be recycled. However, there is a lack of recovery devices in this field capable of stably recovering the complexing agent. Summary of the Invention

[0004] A primary objective of this invention is to overcome at least one of the deficiencies of the prior art and to provide a complexing agent recovery device capable of stably recovering complexing agents from roasting exhaust gas.

[0005] To achieve the above objectives, the present invention adopts the following technical solution:

[0006] According to one aspect of the present invention, a complexing agent recovery device is provided, comprising a roasting furnace, a separation device, a buffer device, an absorption device, and a complexing liquid storage tank; the inlet of the roasting furnace is used to introduce catalyst material impregnated by a complexation method, and the roasting furnace is used to roast the introduced catalyst material containing the complexing agent to generate roasting tail gas; the inlet of the separation device is connected to the outlet of the roasting furnace for introducing the roasting tail gas, and the separation device is used to remove dust from the roasting tail gas; the inlet of the buffer device is connected to the outlet of the separation device, and the buffer device is used to remove solid particles from the roasting tail gas; the inlet of the absorption device is connected to the outlet of the buffer device, and the absorption device is used to absorb the complexing agent in the roasting tail gas to form a complexing agent solution, and discharge the gas through an exhaust port; the inlet of the complexing liquid storage tank is connected to the outlet of the absorption device for introducing the complexing agent solution, and the outlet of the complexing liquid storage tank is used to drain the complexing agent solution.

[0007] According to one embodiment of the present invention, the roasting furnace includes a furnace cylinder and a sealed feeding device; the furnace cylinder is used to roast catalyst materials therein, the gas outlet of the furnace cylinder serves as the gas outlet of the roasting furnace, and the furnace cylinder has a first sealed gas inlet for introducing sealed gas; the sealed feeding device includes a first sealed isolation chamber, a first conveying device, and a second conveying device, the first sealed isolation chamber has a second sealed gas inlet for introducing sealed gas, the inlet of the first sealed isolation chamber serves as the inlet of the roasting furnace, the outlet of the first sealed isolation chamber is connected to the inlet of the furnace cylinder, the first conveying device is disposed at the inlet of the first sealed isolation chamber, and the second conveying device is disposed between the outlet of the first sealed isolation chamber and the inlet of the furnace cylinder.

[0008] According to one embodiment of the present invention, the furnace cylinder has a double-layer structure to form a sealed protective cavity, and the furnace cylinder has a third sealing gas inlet communicating with the sealed protective cavity for introducing sealing gas into the sealed protective cavity.

[0009] According to one embodiment of the present invention, the furnace cylinder is arranged in a rotatable manner, and the connection between the connected moving and stationary parts is sealed by a mechanical seal or a double-layer packing seal device.

[0010] According to one embodiment of the present invention, the roasting furnace further includes a sealed discharge device; the sealed discharge device includes a second sealed isolation chamber, a third conveying device and a fourth conveying device, the second sealed isolation chamber has a fourth sealing gas inlet for introducing sealing gas, the inlet of the second sealed isolation chamber is connected to the outlet of the furnace cylinder, the outlet of the second sealed isolation chamber serves as a discharge end, the third conveying device is disposed between the inlet of the second sealed isolation chamber and the outlet of the furnace cylinder, and the fourth conveying device is disposed at the outlet of the second sealed isolation chamber.

[0011] According to one embodiment of the present invention, the separation device is a cyclone separator.

[0012] According to one embodiment of the present invention, the buffer device is a dust removal buffer tank, which includes a tank body and multiple gas distribution plates; the air inlet of the tank body is connected to the air outlet of the separation device, and the air outlet is connected to the air inlet of the absorption device; the height of the air inlet of the tank body is lower than the height of the air outlet; and a discharge port is provided at the bottom of the tank body; the multiple gas distribution plates are arranged vertically and horizontally in the tank body, and are located between the air inlet and the air outlet of the tank body.

[0013] According to one embodiment of the present invention, the absorption device comprises a plurality of absorption towers; each absorption tower comprises a tower body and a draining device, the tower body having an inlet and an outlet, the height of the inlet being lower than the height of the outlet, the bottom of the tower body containing absorbent liquid, and one end of the draining device connected to the bottom of the tower body. The absorption tower is used to absorb a complexing agent in the roasting tail gas through the absorbent liquid to form a complexing agent solution, and to discharge the complexing agent solution through the draining device; wherein the plurality of absorption towers are arranged in series, the inlet of the first absorption tower is connected to the outlet of the buffer device, the outlet of each absorption tower is connected to the inlet of the next absorption tower, and the outlet of the last absorption tower serves as the discharge end; wherein the other end of the draining device of each absorption tower is connected to the bottom of the tower body of the previous absorption tower, and the other end of the draining device of the first absorption tower is connected to the inlet of the complexing liquid storage tank.

[0014] According to one embodiment of the present invention, each of the absorption towers further includes a circulation system and / or a cooling system; the circulation system includes a circulation pipeline and a circulation drive device, the circulation pipeline being connected between the bottom and top of the tower body, the circulation drive device being used to provide circulation power for the pipeline, and the circulation direction being from the bottom to the top of the tower body; the cooling system is disposed in the tower body for cooling the solution at the bottom of the tower body.

[0015] According to one embodiment of the present invention, the draining device includes a draining pipeline, a control valve, and a cooling device; one end of the draining pipeline is connected to the bottom of the tower body; the control valve is disposed on the draining pipeline for controlling the pipeline status; and the cooling device is disposed on the draining pipeline for cooling the solution in the draining pipeline.

[0016] According to one embodiment of the present invention, the absorption device further includes an acid washing tower; the inlet of the acid washing tower is connected to the outlet of the last absorption tower.

[0017] According to one embodiment of the present invention, the feed inlet of the calcining furnace is directly connected to the discharge outlet of the drying device of the catalyst impregnation system to introduce catalyst material impregnated by the complexation method into the calcining furnace; and / or, the feed inlet of the calcining furnace is connected to at least one feed storage tank for storing catalyst material impregnated by the complexation method.

[0018] As can be seen from the above technical solution, the advantages and positive effects of the complexing agent recovery device proposed in this invention are as follows:

[0019] The complexing agent recovery device proposed in this invention includes a roasting furnace, a separation device, a buffer device, an absorption device, and a complexing liquid storage tank. It can be used for tail gas treatment in industrial processes that generate gas containing complexing agents through roasting. It can achieve stable recovery of complexing agents, obtain high-concentration complexing agent solutions, and ensure the safety and economy of the process.

[0020] Another major objective of the present invention is to overcome at least one of the defects of the prior art described above and to provide a catalyst impregnation apparatus having the complexing agent recovery device described above.

[0021] To achieve the above objectives, the present invention adopts the following technical solution:

[0022] According to another aspect of the present invention, a catalyst impregnation system is provided, comprising the complexing agent recovery device proposed in the present invention and described in the above embodiments, wherein the feed inlet of the calcining furnace is connected to the discharge outlet of the drying device of the catalyst impregnation system, and the discharge outlet of the complexing liquid storage tank is connected to the inlet of the impregnation liquid blending device of the catalyst impregnation system.

[0023] As can be seen from the above technical solution, the advantages and positive effects of the catalyst impregnation system proposed in this invention are as follows:

[0024] The catalyst impregnation system proposed in this invention can be used to impregnate metal components by complexation, and the complexing agent solution can be recovered by using a complexing agent recovery device, thereby achieving a stable and continuous production mode. Attached Figure Description

[0025] Various objects, features, and advantages of the invention will become more apparent from the following detailed description of preferred embodiments of the invention, taken in conjunction with the accompanying drawings. The drawings are merely illustrative of the invention and are not necessarily drawn to scale. In the drawings, the same reference numerals always denote the same or similar parts. Wherein:

[0026] Figure 1 This is a process schematic diagram of a complexing agent recovery device according to an exemplary embodiment;

[0027] Figure 2 yes Figure 1 A schematic diagram of the roasting furnace process is shown;

[0028] Figure 3 yes Figure 2 The diagram shows the structure of the sealing feeder.

[0029] Figure 4 yes Figure 1 The diagram shows the structure of the buffer device;

[0030] Figure 5 This is a process schematic diagram of a catalyst impregnation system according to an exemplary embodiment.

[0031] The annotations in the attached figures are explained as follows:

[0032] 100. Complexing agent recovery device; 1162. Discharge port; 154. Second circulation system;

[0033] 110. Calcination furnace; 1163. Fourth sealing gas inlet; 155. Second cooling system;

[0034] 111. Furnace drum; 117. Third conveying device; 160. Third absorption tower;

[0035] 1111. Feed inlet; 118. Fourth conveying device; 161. Third tower body;

[0036] 1112. Discharge port; 120. Separation device; 163. Third drainage device;

[0037] 1113. Air outlet; 130. Buffer device; 164. Third circulation system;

[0038] 1114. First sealing gas inlet; 131. Tank body; 165. Third cooling system;

[0039] 1115. Sealed protective cavity; 1311. Air inlet; 170. Complexing liquid storage tank;

[0040] 1116. Third sealing gas inlet; 1312. Gas outlet; 180. Pickling tower;

[0041] 112. First sealed isolation chamber; 1313. Discharge port; 181. Fourth tower body;

[0042] 1121. Feed inlet; 132. Gas distribution plate; 182. Gas exhaust end;

[0043] 1122. Discharge port; 140. First absorption tower; 183. Liquid discharge end;

[0044] 1123. Second sealing gas inlet; 141. First tower body; 184. Fourth circulation system;

[0045] 1126. Connection port for moving and stationary equipment; 143. First drainage device; 185. Fourth cooling system;

[0046] 1127. Sealing packing; 144. First circulation system; 200. Impregnating solution mixing equipment

[0047] 1128. Sealing packing; 145. First cooling system; Placement;

[0048] 114. First conveying device; 150. Second absorption tower; 300. Impregnation device;

[0049] 115. Second conveying device; 151. Second tower body; 400. Carrier supply device;

[0050] 116. Second sealed isolation chamber; 153. Second drainage device; 500. Drying device.

[0051] 1161. Feed inlet; Detailed Implementation

[0052] Typical embodiments embodying the features and advantages of the present invention will be described in detail in the following description. It should be understood that the present invention can have various variations in different embodiments without departing from the scope of the present invention, and the description and drawings therein are for illustrative purposes only and not intended to limit the present invention.

[0053] In the following description of different exemplary embodiments of the invention, reference is made to the accompanying drawings, which form part of the invention, and in which different exemplary structures, systems, and steps that can implement various aspects of the invention are shown by way of example. It should be understood that other specific embodiments of the components, structures, exemplary devices, systems, and steps may be used, and structural and functional modifications may be made without departing from the scope of the invention. Furthermore, although the terms “above,” “between,” “within,” etc., may be used in this specification to describe different exemplary features and elements of the invention, these terms are used herein only for convenience, such as the orientation according to the examples shown in the drawings. Nothing in this specification should be construed as requiring a specific three-dimensional orientation of the structure to fall within the scope of the invention.

[0054] See Figure 1 This illustration represents a process schematic of the complexing agent recovery device 100 proposed in this invention. In this exemplary embodiment, the complexing agent recovery device 100 is described as being applied to a catalyst impregnation system. It will be readily understood by those skilled in the art that various modifications, additions, substitutions, deletions, or other changes may be made to the specific embodiments described below to apply the relevant designs of this invention to other types of catalyst preparation equipment; these changes remain within the scope of the principles of the complexing agent recovery device 100 proposed in this invention.

[0055] like Figure 1 As shown, in this embodiment, the complexing agent recovery device 100 proposed by the present invention includes a calcination furnace 110, a separation device 120, a buffer device 130, an absorption device, and a complexing liquid storage tank 170. (See also...) Figures 2 to 4 , Figure 2 A schematic diagram of the process of the roasting furnace 110 is shown in the figure. Figure 3 The diagram shows a representative structural schematic of the sealed feeding device; Figure 4 The diagram above shows a representative structural schematic of the buffer device 130. The structure, connection method, and functional relationship of the main components of the complexing agent recovery device 100 proposed in this invention will be described in detail below with reference to the above-mentioned figures.

[0056] like Figure 1As shown, in this embodiment, the feed inlet of the calcining furnace 110 (e.g., the feed inlet 1121 of the first sealed isolation chamber 112) is used to introduce the catalyst material impregnated using the complexation method. During the calcination process, the complexing agent volatilizes and enters the atmosphere of the calcining furnace 110 in gaseous form, forming exhaust gas containing the complexing agent. The remaining solids can be extracted by the processing of the calcining furnace 110 and used as the finished catalyst product. The inlet of the separation device 120 is connected to the outlet of the calcining furnace 110 (e.g., the outlet 1113 of the furnace cylinder 111) and is used to introduce the calcination exhaust gas. The separation device 120 is used to remove dust from the calcination exhaust gas. The inlet 1311 of the buffer device 130 is connected to the outlet of the separation device 120, and the buffer device 130 is used to remove solid particles from the calcination exhaust gas. The inlet of the absorption device (e.g., the inlet of the first absorption tower 140) is connected to the outlet 1312 of the buffer device 130. The absorption device is used to absorb the complexing agent in the roasting tail gas to form a complexing agent solution, and discharges the gas through the exhaust port (e.g., the exhaust port of the third absorption tower 160). The inlet of the complexing liquid storage tank 170 is connected to the outlet of the absorption device (e.g., the first drain device 143 of the first absorption tower 140), and is used to introduce the complexing agent solution. The outlet of the complexing liquid storage tank 170 is used to drain the complexing agent solution. With the above design, the complexing agent recovery device 100 proposed in this invention can be used for tail gas treatment in industrial processes that generate gas containing complexing agents through roasting. It can achieve stable recovery of complexing agents, obtain a high-concentration complexing agent solution, and ensure the safety and economy of the process. In addition, the complexing agent recovery device 100 proposed in this invention, by setting a buffer device 130 after the separation device 120, can make the roasting process and subsequent washing and recovery more stable, and smoothly realize the recovery and utilization of complexing agent, which is conducive to achieving multi-stage stable absorption.

[0057] Optionally, such as Figure 2As shown, in this embodiment, the roasting furnace 110 may include a furnace cylinder 111 and a sealed feeding device. Specifically, the furnace cylinder 111 is used to roast the catalyst material therein, and the gas outlet 1113 of the furnace cylinder 111 serves as the gas outlet of the roasting furnace 110. The furnace cylinder 111 has a first sealed gas inlet 1114 communicating with its cylinder cavity for introducing a sealed gas (e.g., but not limited to nitrogen). The sealed feeding device includes a first sealed isolation chamber 112, a first conveying device 114, and a second conveying device 115. The feed inlet 1121 of the first sealed isolation chamber 112 serves as the feed inlet of the roasting furnace 110, and the discharge outlet 1122 of the first sealed isolation chamber 112 is connected to the feed inlet 1111 of the furnace cylinder 111. The first sealed isolation chamber 112 has a second sealed gas inlet 1123 communicating with its chamber body for introducing a sealed gas (e.g., but not limited to nitrogen). A first conveying device 114 is disposed in the feed inlet 1121 to convey the catalyst material from the feed inlet 1121 to the first sealed isolation chamber 112. A second conveying device 115 is disposed in the discharge outlet 1122 to convey the catalyst material in the first sealed isolation chamber 112 to the furnace cylinder 111 via the discharge outlet 1122. Through the above design, the present invention can further ensure that the feeding and roasting processes of the roasting furnace 110 are carried out in an oxygen-free atmosphere, for example, the oxygen concentration in the oxygen-free atmosphere does not exceed 0.5% of the total volume, thereby preventing the complexing agent from reacting with air and causing oxidation loss or explosion. The present invention can introduce the catalyst material into the furnace cylinder in an air-isolated manner through a sealed feeding device, and generate roasting exhaust gas by roasting the catalyst material through the furnace cylinder. Through the above structural design, the present invention can use a sealed feeding device to ensure that air does not enter the feed inlet of the roasting furnace cylinder, giving the roasting furnace reliable sealing performance and stable operation.

[0058] Furthermore, in this embodiment, the internal volume of the first sealed isolation chamber 112 can be greater than or equal to 0.25m³. 3 For example, 0.25m 3 0.5m 3 1m 3 1.3m 3 And preferably 0.25m 3 ~1 m 3 Furthermore, such as Figure 3 As shown, in this embodiment, the wall of the furnace cylinder 111 can be a double-layer structure to form a sealed protective cavity 1115. Furthermore, the furnace cylinder 111 can also have a third sealing gas inlet 1116, which is connected to the sealed protective cavity 1115 and is used to introduce sealing gas into the sealed protective cavity 1115, thereby ensuring that air does not enter the furnace cylinder.

[0059] Furthermore, such as Figure 2As shown, in this embodiment, the roasting furnace 110 may further include a sealed discharge device. Specifically, the sealed discharge device includes a second sealed isolation chamber 116, a third conveying device 117, and a fourth conveying device 118. The inlet 1161 of the second sealed isolation chamber 116 is connected to the outlet 1112 of the furnace cylinder 111, and the outlet 1162 of the second sealed isolation chamber 116 serves as a discharge end. The second sealed isolation chamber 116 has a fourth sealing gas inlet 1163 connected to its chamber body for introducing sealing gas (e.g., but not limited to nitrogen). The third conveying device 117 is disposed between the inlet 1161 of the second sealed isolation chamber 116 and the outlet 1112 of the furnace cylinder 111 for conveying the roasted material from the furnace cylinder 111 to the furnace cylinder 111. The fourth conveying device 118 is disposed at the outlet 1162 for discharging the material from the second sealed isolation chamber 116 through the outlet 1162. Through the above design, the present invention can further realize that the discharge process of the roasting furnace 110 is carried out in an oxygen-free atmosphere, for example, the oxygen concentration in the oxygen-free atmosphere does not exceed 0.5% by volume, thereby preventing the residual complexing agent in the discharged material from reacting with the air and causing oxidation loss or explosion of the complexing agent.

[0060] Furthermore, in this embodiment, the internal volume of the second sealed isolation chamber 116 can be greater than or equal to 0.25m³. 3 For example, 0.25m 3 0.5m 3 1m 3 1.3m 3 And preferably 0.25m 3 ~1 m 3 .

[0061] Furthermore, in this embodiment, the aforementioned conveying devices can each be selected as screw conveyors, which are particularly suitable for the calcination of powder materials. Taking the second conveying device 115 and the third conveying device 117 as examples, the material conveying device of a screw conveyor typically includes a bearing, a drive device, and a feeding mechanism. The drive device and bearing are located outside the furnace cylinder 111, while the feeding mechanism is located inside the furnace cylinder 111, allowing the material to move within the furnace cylinder 111. It should be noted that, as... Figure 2As shown, in actual operation, taking screw conveyors as an example, the rotation of the screw conveyor is relatively slow to ensure that it contains sufficient solid material. Gas cannot pass through the screw conveyor; only solids can pass through. In fact, the screw conveyor plays a sealing role, similar to the water seal or oil seal used on some containers. The sealing gas enters from the second sealing gas inlet 1123, forming a certain positive pressure in the first sealing isolation chamber 112. The sealing gas cannot be discharged from the feed inlet 1121 through the first conveying device 114, nor can it enter the second conveying device 115 and the cylinder cavity of the furnace 111 from the discharge outlet 1122. The sealing gas enters from the second sealing gas inlet 1163, forming a certain positive pressure in the second sealing isolation chamber 116. The sealing gas cannot enter the cylinder cavity of the furnace 111 from the feed inlet 1161 through the third conveying device 117, nor can it enter the fourth conveying device 118 from the discharge outlet 116. As described above, in this embodiment, the furnace cylinder 111 can function as a moving device, rotating relative to stationary devices such as the sealing feeding device and the sealing discharging device to ensure uniform heating of the material. To further prevent air from entering the roasting furnace 110 via the screw conveyor, a seal is provided at the contact point between the stationary and moving equipment connection port 1126 and the furnace cylinder 111. Furthermore, when the furnace cylinder 111 employs a double-layer structure, the aforementioned sealing structure can be a double-layer packing seal structure. Accordingly, the sealing structure is located at the connection between the moving and moving equipment connection port 1126 and the furnace cylinder 111. The sealing gas within the sealed protection chamber is under a slight positive pressure, creating a pressure difference with the negative pressure within the furnace cylinder 111 of the roasting furnace 110, thus preventing external air from entering the furnace cylinder 111. Since the gas pressure inside the furnace cylinder 111 of the roasting furnace 110 is lower than that within the sealed protection chamber, even with minor leaks at the seal, only sealed gas enters the furnace cylinder 111, preventing the introduction of air or other gases, thus ensuring the safety of the roasting process.

[0062] Furthermore, the amount of sealing gas entering the furnace cylinder 111 can be adjusted by the slight negative pressure within the furnace cylinder 111. For example, the pressure inside the furnace cylinder 111 of the roasting furnace 110 can be controlled at 0.95 to 0.97 atmospheres, and the pressure of the sealing gas in the sealing isolation chamber can be controlled at 1.01 to 1.03 atmospheres. By setting up the aforementioned sealing isolation chamber, the pressure control of the roasting furnace 110 can be made more stable.

[0063] Furthermore, such as Figure 3As shown, in this embodiment, the connection between the moving and stationary devices is on the wall of the furnace cylinder 111. The rotating moving device is connected to the wall of the furnace cylinder 111, forming the moving-stationary device connection port 1126. When the wall of the furnace cylinder 111 has a double-layer structure, and a sealed protective cavity 1115 is formed between the two layers, sealing gas is introduced into the sealed protective cavity 1115 through the second sealing gas inlet 1116, and sealing gas is introduced into the furnace cylinder 111 through the first sealing gas inlet 1114. A sealing packing 1127 is provided between the moving-stationary device connection port 1126 and the outer wall of the furnace cylinder 111 to achieve a sealed isolation between it and the atmosphere. At the same time, a sealing packing 1128 is provided between the moving-stationary device connection port 1126 and the inner wall of the furnace cylinder 111 to achieve a sealed isolation between it and the space inside the furnace cylinder 111. Accordingly, the sealing packing 1127 and the sealing packing 1128 can form a separate double-layer packing sealing device.

[0064] Furthermore, in this embodiment, the roasting furnace 110 can adopt a continuous feeding method, which allows the material to be roasted to be continuously introduced into the furnace cylinder 111 of the roasting furnace 110 for roasting, and reduces the amount of air introduced.

[0065] Furthermore, in this embodiment, the sealing gas can be nitrogen (N2). Additionally, nitrogen can be provided by a PSA nitrogen generation system. In some embodiments, other gases may also be used as the sealing gas, and the sealing gases in the furnace cylinder 111, the sealing protection chamber 1115, the first sealing isolation chamber 112, and the second sealing isolation chamber 116 may be, but are not limited to, the same.

[0066] Furthermore, in this embodiment, the furnace cylinder 111 can have one or more exhaust ports, for example, two respectively located at the head and tail ends of the furnace cylinder 111. These exhaust ports can be connected to an extraction device. Accordingly, the roasting furnace 110 can discharge the gas generated inside the furnace 110 through the exhaust ports. This extraction method allows the exhaust gas generated during the roasting process inside the furnace 110 to be extracted simultaneously at the furnace head and tail. The adverse effect of the difference in exhaust volume between the furnace head and tail can be reduced, lowering the gas velocity inside the furnace cylinder 111 to the minimum value required for roasting. This ensures the roasting effect while reducing dust emissions and decreasing the possibility of air entering the furnace cylinder 111. The gas volume and pressure head of the extraction system can be adjusted by the pressure at the furnace head and tail.

[0067] Furthermore, in this embodiment, the sealing feeding device and the double-layer packing sealing device connected to the furnace cylinder 111 of the roasting furnace 110 can be designed as an integral unit. The sealing feeding device is connected to the furnace cylinder 111 of the roasting furnace 110 by using the wall of the sealing feeding device, and the double-layer sealing isolation chamber wall is used to achieve sealing gas sealing.

[0068] Optionally, in this embodiment, the feed inlet of the calcining furnace 110 (e.g., the feed inlet 1121 of the first sealed isolation chamber 112) can be directly connected to the discharge outlet of the drying device 500 of the catalyst impregnation system to introduce the catalyst material impregnated using the complexation method into the calcining furnace 110. In some embodiments, the feed inlet of the calcining furnace 110 may also be connected to a solid material feeding system. The solid material feeding system includes at least one feed tank capable of storing the catalyst material impregnated using the complexation method. Furthermore, when there are multiple feed tanks, they can be connected in parallel to the feed inlet of the calcining furnace 110, thereby alternating their use for feeding the material to be calcined into the calcining furnace 110.

[0069] As described above, the optimized design of the calcining furnace 110 of the present invention has made comprehensive improvements in the feeding and discharging of the calcining furnace 110, the air extraction system of the calcining furnace 110, and the air protection system, thereby ensuring the safety and stability of the catalyst calcination process.

[0070] Optionally, in some embodiments, the inlet and outlet of the roasting furnace 110 can be connected to a feed tank and an outlet tank, respectively. Solid feeding and discharging can both be done in parallel using two or more tanks (containers for storing solid materials). The feed tank and outlet tank can be detachably and switchably connected to the roasting furnace 110, for example, using flange connections or valve control to maintain communication between the tanks and the roasting furnace 110. The feeding rate can be controlled by a feed rotary valve. When the feed tank is emptied or the outlet tank is full, the process switches to another parallel feed tank or outlet tank to continue operation. This switching process can be controlled manually or automatically by a shut-off valve. In use, the material to be roasted (e.g., a dried composition containing a complexing agent) enters the feed tank, then enters the roasting furnace 110 through the feed inlet, and is roasted. The roasted material is discharged from the roasting furnace 110 into the outlet tank for subsequent processing, such as packaging or further processing. Meanwhile, the exhaust gas generated during the roasting process is drawn downstream by the exhaust device through the gas outlet for recycling.

[0071] Furthermore, in some embodiments, the feed inlet of the feed tank is sealable, thereby preventing air from entering the feed tank during use and facilitating pressure adjustment within the tank. Preferably, a gas balance hole is provided at the top of the discharge tank, and the pressure inside the feed tank is adjusted by a valve. This is particularly suitable for multiple tanks connected in parallel. In the case of multiple tanks connected in parallel, the discharge port of the feed tank used to supply material to the roasting furnace 110 is connected to the feed inlet of the roasting furnace 110, and the feed inlet of the feed tank is sealed, with the material entering the roasting furnace 110 for roasting. The pressure inside the feed tank and the amount of sealing gas entering from the sealed isolation chamber are controlled by the gas balance hole. The feed tank used to receive the material to be roasted is disconnected from the roasting furnace 110. After the material is full, the feed inlet can be sealed, and sealing gas is introduced through the air inlet provided at the bottom, while the exhaust gas containing the complexing agent is discharged through the gas balance hole at the top, thereby achieving gas replacement within the tank and reducing the oxygen brought into the roasting furnace 110 by the material to be roasted.

[0072] Optionally, in this embodiment, the material to be roasted introduced into the roasting furnace 110 is a solid material, which can be a powder, granular solid, shaped solid, etc., and is preferably a powder, such as a microsphere catalyst.

[0073] In some embodiments, the average particle size of the microspherical catalyst described above can be 65 μm to 85 μm, and its particle size is preferably greater than 0 and less than or equal to 149 μm. Furthermore, the microspherical catalyst particles account for 90% to 100% by volume. Preferably, the proportion of particles with a particle size greater than 0 and less than or equal to 20 μm does not exceed 10% by volume, for example, 0% to 3% by volume. The proportion of particles with a particle size greater than 0 and less than or equal to 40 μm does not exceed 20% by volume, for example, 5% to 10% by volume. The particle size of the microspherical catalyst can be measured using Q / SH 3360-210-2020. In addition, this specification uses the example of a complexing agent containing, for example, NH3 in the above-mentioned solid material for illustration.

[0074] Alternatively, in this embodiment, the separation device 120 can be a cyclone separator.

[0075] Optionally, in this embodiment, an induced draft fan may be provided between the roasting furnace 110 and the separation device 120. The induced draft fan is used to draw out the exhaust gas generated by roasting in the roasting furnace 110 and transport it to the separation device 120.

[0076] Optionally, such as Figure 4As shown, in this embodiment, the buffer device 130 can be a dust removal buffer tank, which may include a tank body 131 and three gas distribution plates 132. Specifically, the air inlet 1311 of the tank body 131 is connected to the air outlet of the separation device 120, and the air outlet 1312 is connected to the air inlet of the absorption device (e.g., the air inlet of the first absorption tower 140). The height of the air inlet 1311 of the tank body 131 is lower than the height of the air outlet 1312, and a discharge port 1313 is provided at the bottom of the tank body 131. The three gas distribution plates 132 are arranged vertically and spaced apart in the tank body 131, and are located between the air inlet 1311 and the air outlet 1312 of the tank body 131. In addition, the gas distribution plates 132 can be grid plates or perforated plates. Accordingly, the gas enters the tank 131 through the inlet 1311 and mixes thoroughly with the solution in the tank 131. The solid particles contained therein remain in the solution and can be discharged through the discharge port 1313, while the gas further enters the subsequent absorption process through the outlet 1312.

[0077] In some embodiments, the gas distribution plate 132 may be one, two, four or more, and is not limited thereto. In addition, when there are multiple gas distribution plates 132, the dust removal buffering function of the dust removal buffer tank can be made more stable.

[0078] Furthermore, such as Figure 4 As shown, in this embodiment, the air inlet 1311 of the dust removal buffer tank can be located at the lower part of the tank body 131, and the height of the air outlet 1312 is higher than the height of the air inlet 1311, for example, it can be located at the upper part or top of the tank body 131. Furthermore, the discharge port 1313 can be located at the bottom of the tank body 131.

[0079] Furthermore, in this embodiment, the distance between the air inlet 1311 of the dust removal buffer tank and the bottom of the tank body 131 can be less than or equal to 1 / 4 of the height of the tank body 131, such as 1 / 10, 1 / 8, 1 / 5, 1 / 4, etc., and is preferably 1 / 5 to 1 / 3. In some embodiments, the distance between the air inlet 1311 of the dust removal buffer tank and the bottom of the tank body 131 can also be greater than 1 / 4 of the height of the tank body 131, such as 3 / 10, etc., and is not limited thereto.

[0080] Furthermore, in this embodiment, the installation position of the gas distribution plate 132, that is, the distance between the lowest gas distribution plate 132 and the bottom of the tank body 131 of the dust removal buffer tank, can be 1 / 3 to 2 / 3 of the height of the tank body 131, such as 1 / 3, 1 / 2, 5 / 9, 2 / 3, etc., and is preferably 2 / 5 to 3 / 5. In some embodiments, the distance between the lowest gas distribution plate 132 and the bottom of the tank body 131 can be less than 1 / 3 or greater than 2 / 3 of the height of the tank body 131, such as 2 / 9, 7 / 9, etc., and is not limited thereto.

[0081] Optionally, such as Figure 1 As shown, in this embodiment, the absorption device may include three absorption towers. Specifically, each absorption tower may include a tower body and a draining device. The tower body has an inlet and an outlet, with the inlet height lower than the outlet height, and absorbent liquid at the bottom of the tower body. Accordingly, the absorbent liquid and gas can come into countercurrent contact within the tower body; that is, gas (the exhaust gas generated during roasting) enters the tower body from the bottom and comes into countercurrent contact with the absorbent liquid to complete the absorption. One end of the draining device is connected to the bottom of the tower body. The absorption tower is used to absorb the complexing agent in the roasting exhaust gas through the absorbent liquid to form a complexing agent solution, and the complexing agent solution is discharged through the draining device. In some embodiments, the absorption device may also include one, two, four, or more absorption towers, and preferably multiple absorption towers. Of course, the absorption device may also include other types of absorption equipment, and is not limited thereto.

[0082] In this specification, for ease of understanding and explanation, the three absorption towers are defined as the first absorption tower 140, the second absorption tower 150, and the third absorption tower 160, respectively. Specifically, the first absorption tower 140 includes a first tower body 141 and a first drainage device 143; the second absorption tower 150 includes a first tower body 141 and a second drainage device 153; and the third absorption tower 160 includes a third tower body 161 and a third drainage device 163. Based on this, multiple absorption towers are arranged in series. The inlet of the first absorption tower 140 is connected to the outlet 1312 of the buffer device 130. The outlet of the first absorption tower 140 is connected to the inlet of the second absorption tower 150, and the outlet of the second absorption tower 150 is connected to the inlet of the third absorption tower 160. That is, the outlet of each absorption tower is connected to the inlet of the next absorption tower, and the outlet of the third absorption tower 160 (i.e., the last absorption tower) serves as the discharge end. In this configuration, the other end of the third drain device 163 of the third absorption tower 160 is connected to the bottom of the second tower body 151 of the second absorption tower 150, and the other end of the second drain device 153 of the second absorption tower 150 is connected to the bottom of the first tower body 141 of the first absorption tower 140. That is, the other end of the drain device of each absorption tower is connected to the bottom of the tower body of the preceding absorption tower, and the other end of the first drain device 143 of the first absorption tower 140 (i.e., the first absorption tower) is connected to the inlet of the complexing liquid storage tank 170. Accordingly, multiple absorption towers are arranged in series in the above manner, allowing the absorbent from the downstream absorption tower to enter the upstream absorption tower. This enables stable recovery of the complexing agent in the washing liquid and maximizes the recovery of the complexing agent in the gas phase. It also increases the concentration of the complexing solution obtained by the absorption unit, eliminating the need for concentration and meeting the requirements for reuse of the complexing agent.

[0083] Furthermore, in this embodiment, the material of the absorption tower body can be stainless steel, polypropylene, or other similar materials.

[0084] Furthermore, in this embodiment, the absorption tower can be a packed tower, that is, packing material can be installed in the tower body. The packing material can be Raschig rings, Pall rings, rectangular saddle packing, etc. In some embodiments, the absorption tower can also be a sieve plate tower or a condenser tower, that is, sieve plates or condensers, such as tubular condensers, can be installed in the tower body, with the coolant flowing inside the tubes and the absorbent flowing outside the tubes.

[0085] Furthermore, such as Figure 1As shown, in this embodiment, each absorption tower may further include a circulation system, through which the absorbent at the bottom of the tower can be circulated to the top. That is, the first absorption tower 140 includes a first circulation system 144, the second absorption tower 150 includes a second circulation system 154, and the third absorption tower 160 includes a third circulation system 164. Specifically, for an absorption tower, its circulation system may include a circulation pipeline and a circulation drive device. The circulation pipeline connects the bottom and top of the tower body, and the circulation drive device provides power for the pipeline circulation, with the circulation direction from the bottom to the top of the tower body.

[0086] Furthermore, such as Figure 1 As shown, in this embodiment, each absorption tower may also include a cooling system; that is, the first absorption tower 140 includes a first cooling system 145, the second absorption tower 150 includes a second cooling system 155, and the third absorption tower 160 includes a third cooling system 165. Specifically, for an absorption tower, its cooling system may be installed in the tower body to cool the solution at the bottom of the tower body, so as to ensure that the temperature of the absorbent is low and improve the absorption efficiency.

[0087] Furthermore, in this embodiment, for an absorption tower, its drainage device may include a drainage pipeline, a control valve, and a cooling device. Specifically, one end of the drainage pipeline is connected to the bottom of the tower body. The control valve is installed on the drainage pipeline to control the pipeline status, such as open / closed state and flow rate. The cooling device is installed on the drainage pipeline to cool the solution within the drainage pipeline.

[0088] Furthermore, in this embodiment, for an absorption tower, a water inlet can be provided on its tower body for replenishing water into the tower body as needed. In addition, when the absorption device includes multiple absorption towers, each absorption tower can be provided with a water inlet, or at least one absorption tower (e.g., the last absorption tower) can be provided with a water inlet.

[0089] Furthermore, such as Figure 1 As shown, in this embodiment, the absorption device may further include an acid washing tower 180. Specifically, the inlet of the acid washing tower 180 may be connected to the outlet of the third absorption tower 160 (i.e., the last absorption tower). Through the above design, by setting the acid washing tower 180, the present invention can better absorb the alkaline complexing agent, so that the exhaust gas emitted into the air meets the emission requirements. The solution in the acid washing tower 180 is ultimately a salt solution, which can be further recovered to obtain, for example, ammonium salts.

[0090] Furthermore, in this embodiment, the pickling tower 180 can be a packed tower, and the packing material can be stainless steel or polypropylene. The acid solution can be a dilute sulfuric acid solution. In the pickling tower 180, the exhaust gas enters from the bottom and comes into countercurrent contact with the acid solution to complete the absorption. The absorbed gas is then discharged into the atmosphere.

[0091] Furthermore, such as Figure 1 As shown, in this embodiment, the pickling tower 180 includes a fourth tower body 181 and a fourth draining device. The fourth tower body 181 has an inlet and an outlet. The inlet is connected to the outlet of the absorption device (e.g., the outlet of the third absorption tower 160), and the outlet can serve as a gas discharge end 182-182, directly discharging or connecting to a gas purification system. The fourth draining device is connected to the bottom of the fourth tower body 181 and can serve as a liquid discharge end 183-183, directly discharging or connecting to a liquid recovery system. Additionally, the pickling tower 180 may also be equipped with a fourth circulation system 184 and a fourth cooling system 185. The fourth circulation system 184 is used to transport the liquid at the bottom of the pickling tower 180 to the top for circulation, and the fourth cooling system 185 is used to cool the liquid at the bottom of the pickling tower 180.

[0092] Furthermore, in this embodiment, the pickling tower 180 may be provided with a washing liquid replenishment port for replenishing the pickling tower 180 with washing liquid, such as, but not limited to, dilute sulfuric acid.

[0093] In summary, the complexing agent recovery device 100 proposed in this invention includes a calcination furnace 110, a separation device 120, a buffer device 130, an absorption device, and a complexing liquid storage tank 170. It can be used for tail gas treatment in industrial processes that generate gas containing complexing agents through calcination, and can achieve stable recovery of complexing agents, obtain high-concentration complexing agent solutions, and ensure the safety and economy of the process.

[0094] It should be noted that the complexing agent recovery device 100 shown in the accompanying drawings and described in this specification is merely a few examples among many complexing agent recovery devices 100 capable of employing the principles of the present invention. It should be clearly understood that the principles of the present invention are by no means limited to any detail or component of the complexing agent recovery device 100 shown in the accompanying drawings or described in this specification.

[0095] Based on the detailed description of an exemplary embodiment of the complexing agent recovery device 100 proposed by the present invention above, an exemplary embodiment of the catalyst impregnation system proposed by the present invention will be described below.

[0096] See Figure 5This diagram illustrates, in a representative manner, the process schematic of the catalyst impregnation system proposed in this invention. In this embodiment, the catalyst impregnation system proposed in this invention includes the complexing agent recovery device 100, which is described in detail in the above embodiments. The feed inlet of the calcining furnace 110 is connected to the discharge outlet of the drying device 500 of the catalyst impregnation system, and the discharge outlet of the complexing liquid storage tank 170 is connected to the inlet of the impregnation liquid blending device 200 of the catalyst impregnation system. Accordingly, the impregnation solution mixing device 200 can supply impregnation solution to the impregnation device 300, the carrier supply device 400 can supply carrier to the impregnation device 300, the impregnation product generated by the impregnation device 300 can enter the drying device 500 for drying, and the material dried by the drying device 500 can be provided to the complexing agent recovery device 100 (e.g., calcining furnace 110). The outlet of the complexing agent recovery device 100's complexing agent storage tank 170 is connected to the impregnation solution mixing device 200, so that the synthetic liquid recovered to the complexing agent storage tank 170 can enter the impregnation solution mixing device 200 again to participate in the preparation of impregnation solution. Among them, the recovered complexing agent solution can be used to prepare impregnation solution containing metal salt and complexing agent.

[0097] Specifically, in this embodiment, the catalyst impregnation system proposed in this invention can be used to prepare catalysts by impregnation. When the system is working, an impregnation liquid including metal, complexing agent and water is prepared in the impregnation liquid mixing device 200. The complexing agent can be the complexing agent recovered by the complexing agent recovery device 100 proposed in this invention, or new complexing agent can be added. Then it is introduced into the impregnation device 300 and impregnated by contacting the carrier supplied by the carrier supply device 400. After impregnation, the carrier containing metal and complexing agent is dried in the drying device 500 and then introduced into the calcination furnace 110 of the complexing agent recovery device 100 for calcination. The gas is led out of the calcination furnace 110 and the complexing agent is recovered. The solid is used as the finished catalyst product.

[0098] It should be noted that the catalyst impregnation systems shown in the accompanying drawings and described in this specification are merely a few examples of many catalyst impregnation systems capable of employing the principles of the present invention. It should be clearly understood that the principles of the present invention are by no means limited to any detail or component of the catalyst impregnation systems shown in the accompanying drawings or described in this specification.

[0099] In summary, the catalyst impregnation system proposed in this invention can be used to impregnate metal components by complexation, and the complexing agent solution can be recovered by using the complexing agent recovery device 100, thereby achieving a stable and continuous production mode.

[0100] Based on the detailed description of several exemplary embodiments of the complexing agent recovery device 100 and catalyst impregnation system proposed in this invention, several specific embodiments based on the design concept of this invention will be described below. Specific Implementation Example 1

[0102] A small-scale experimental setup was used, in which the first-stage receiving tower was 2m high and had a volume of 2m³. 3 The second absorption tower is 150 cubic meters high and has a volume of 1 cubic meter per cubic meter. 3 The third absorption tower is 160 cubic meters high, 1.5 meters long, and has a volume of 1 cubic meter per cubic meter. 3 The packing material is all stainless steel Raschig ring packing, and the dust collector buffer tank has a volume of 0.25m³. 3 It contains a saturated sodium hydroxide solution.

[0103] An impregnation solution was prepared using ammonia, nickel acetate, and water, with an NH3 content of 12.5 wt% and a nickel salt content (calculated as Ni) of 7 wt%. The carrier A was impregnated three times with this solution, dried after each impregnation. The weight ratios of the impregnation solution to carrier A for the first, second, and third impregnations were 1:1, 1:1, and 1:1.5, respectively. The mixture was then calcined at 500°C. After three stages of ammonia absorption, water was added to the third-stage absorbent, which was then introduced into the second stage. The second-stage absorbent was introduced into the first stage, and the first-stage absorbent was discharged into the complexing liquid storage tank 170. Multiple measurements showed that the concentration of the recovered ammonia was 26–28 wt%, indicating high stability. The temperatures of the first, second, and third-stage absorbents were 5°C, 3°C, and 2°C, respectively. The gas-to-absorbent ratios in the first absorption tower 140, second absorption tower 150, and third absorption tower 160 were 50:1, 40:1, and 35:1 Nm³, respectively. 3 Gas / m 3 Absorbent solution.

[0104] The specific composition of support A is: 28 wt% Al₂O₃, 20 wt% SiO₂, 50 wt% ZnO, and 2 wt% CeO₂; particles with a diameter greater than 0–20 μm account for 3% by volume, particles with a diameter greater than 0–40 μm account for 10% by volume, and particles with a diameter greater than 0–149 μm account for 96% by volume; the average particle size is 75 μm. The bulk density of the support is 0.85 g / cm³. 3 ). Specific Implementation Example 2

[0106] The impregnation solution contained 13.3% by weight ammonia, prepared with nickel acetate, and impregnated three times with a nickel content of 7% by weight. The weight ratio of the impregnation solution to carrier B in each impregnation was 6:5, 16:515, and 11:515, respectively. The drying temperature was 150°C, and the calcination temperature was 500°C. The ammonia was recovered using the method described in Example 1 above, and the concentration of the recovered ammonia solution was measured to be 26-28% by weight multiple times. The carrier B had the following formulation: 28% by weight Al₂O₃, 35% by weight SiO₂, 35% by weight molecular sieve, and 2% by weight La₂O₃; particles with a diameter greater than 0-20 μm accounted for 3% by volume, particles with a diameter greater than 0-40 μm accounted for 5% by volume, and particles with a diameter greater than 0-149 μm accounted for 97% by volume; the average particle size was 80 μm. The bulk density of carrier B was 1.10 g / cm³. 3 ). Specific Implementation Example 3

[0108] The method of impregnation and recovery was followed according to Specific Example 1. Impregnation was performed using carrier C, with an ammonia content of 10% by weight in the impregnation solution and nickel citrate as the metal, containing 5.5% by weight. Impregnation was performed four times, with the weight ratio of impregnation solution to carrier C being 16:15, 12:15, 12:15, and 10:15, respectively. The concentration of the recovered ammonia water (calculated as ammonium monohydrate) was 26–28% by weight (range of multiple results).

[0109] Support C has the following formulation: comprising 25 wt% Al₂O₃, 35 wt% SiO₂, 45 wt% Fe₂O₃, and 5 wt% La₂O₃; particles with a diameter greater than 0–20 μm account for 3% by volume, particles with a diameter greater than 0–40 μm account for 10% by volume, and particles with a diameter greater than 0–149 μm account for 95% by volume; the average particle size is 78 μm. The bulk density of the support is 1.10 g / cm³. 3 ).

[0110] In summary, in the above three specific embodiments, the concentration of ammonia water recovered by the complexing agent recovery device 100 is 26-28% by weight, indicating that it has high stability.

[0111] The foregoing has described and / or illustrated exemplary embodiments of the complexing agent recovery device and catalyst impregnation system proposed in this invention. However, the embodiments of this invention are not limited to the specific embodiments described herein; rather, components and / or steps of each embodiment may be used independently and separately from other components and / or steps described herein. Each component and / or step of one embodiment may also be used in combination with other components and / or steps of other embodiments. In describing the elements / components / etc. described and / or illustrated herein, the terms “a,” “an,” and “the above” are used to indicate the presence of one or more elements / components / etc. The terms “comprising,” “including,” and “having” are used to indicate an open-ended inclusion and mean that additional elements / components / etc. may exist in addition to those listed. Furthermore, the terms “first” and “second” in the claims and specification are used only as illustrative marks and are not intended to limit the numerical scope of the subject matter.

[0112] Although the complexing agent recovery device and catalyst impregnation system proposed in this invention have been described according to different specific embodiments, those skilled in the art will recognize that modifications can be made to the implementation of this invention within the spirit and scope of the claims.

Claims

1. A complexing agent recovery device, comprising: A roasting furnace, the feed inlet of which is used to introduce catalyst material impregnated by complexation, the roasting furnace being used to roast the introduced catalyst material containing complexing agent to generate roasting exhaust gas. A separation device, the air inlet of which is connected to the air outlet of the roasting furnace, is used to introduce roasting exhaust gas, and the separation device is used to remove dust from the roasting exhaust gas. A buffer device, the air inlet of which is connected to the air outlet of the separation device, is used to remove solid particles from the roasting exhaust gas. An absorption device, the air inlet of which is connected to the air outlet of the buffer device, is used to absorb the complexing agent in the roasting tail gas to form a complexing agent solution, and the gas is discharged through the exhaust port. as well as The complexing liquid storage tank has its inlet connected to the outlet of the absorption device for introducing the complexing agent solution, and its outlet for discharging the complexing agent solution.

2. The complexing agent recovery device according to claim 1, wherein, The roasting furnace includes: A furnace cylinder is used for roasting catalyst materials. The furnace cylinder has gas outlets at its head and tail ends, which serve as the gas outlets of the roasting furnace. The furnace cylinder also has a first sealing gas inlet for introducing sealing gas. as well as A sealed feeding device includes a first sealed isolation chamber, a first conveying device, and a second conveying device. The first sealed isolation chamber has a second sealing gas inlet for introducing sealing gas. The inlet of the first sealed isolation chamber serves as the inlet of the roasting furnace. The outlet of the first sealed isolation chamber is connected to the inlet of the furnace cylinder. The first conveying device is located at the inlet of the first sealed isolation chamber, and the second conveying device is located between the outlet of the first sealed isolation chamber and the inlet of the furnace cylinder.

3. The complexing agent recovery device according to claim 2, wherein, The furnace cylinder has a double-layer structure to form a sealed protective cavity. The furnace cylinder has a third sealing gas inlet connected to the sealed protective cavity for introducing sealing gas into the sealed protective cavity.

4. The complexing agent recovery device according to claim 3, wherein, The furnace cylinder is arranged in a rotatable manner, and the connection between the moving and stationary parts is sealed by a mechanical seal or a double-layer packing seal device.

5. The complexing agent recovery device according to claim 2, wherein, The roasting furnace also includes: A sealed discharge device includes a second sealed isolation chamber, a third conveying device, and a fourth conveying device. The second sealed isolation chamber has a fourth sealing gas inlet for introducing sealing gas. The inlet of the second sealed isolation chamber is connected to the outlet of the furnace cylinder, and the outlet of the second sealed isolation chamber serves as a discharge end. The third conveying device is located between the inlet of the second sealed isolation chamber and the outlet of the furnace cylinder, and the fourth conveying device is located at the outlet of the second sealed isolation chamber.

6. The complexing agent recovery device according to claim 1, wherein, The separation device is a cyclone separator.

7. The complexing agent recovery device according to claim 1, wherein, The buffer device is a dust removal buffer tank, which includes: The tank body has an air inlet connected to the air outlet of the separation device, and an air outlet connected to the air inlet of the absorption device. The height of the air inlet of the tank body is lower than the height of the air outlet, and a discharge port is provided at the bottom of the tank body; and Multiple gas distribution plates are arranged vertically and intermittently within the tank, positioned between the tank's air inlet and outlet.

8. The complexing agent recovery device according to claim 1, wherein, The absorption device comprises: Multiple absorption towers, each of the absorption towers comprising a tower body and a draining device, the tower body having an inlet and an outlet, the height of the inlet being lower than the height of the outlet, an absorbent liquid at the bottom of the tower body, and one end of the draining device connected to the bottom of the tower body, the absorption towers being used to absorb the complexing agent in the roasting tail gas through the absorbent liquid to form a complexing agent solution, and to discharge the complexing agent solution through the draining device; The multiple absorption towers are arranged in series, with the air inlet of the first absorption tower connected to the air outlet of the buffer device, the air outlet of each absorption tower connected to the air inlet of the next absorption tower, and the air outlet of the last absorption tower serving as the discharge end. The other end of the draining device of each absorption tower is connected to the bottom of the tower body of the previous absorption tower, and the other end of the draining device of the first absorption tower is connected to the inlet of the complex liquid storage tank. The absorption tower is a packed tower, a sieve plate tower, or a condenser tower.

9. The complexing agent recovery device according to claim 8, wherein, Each of the absorption towers further comprises: A circulation system, comprising circulation piping and a circulation drive device, wherein the circulation piping connects the bottom and top of the tower body, and the circulation drive device provides circulation power to the piping, and the circulation direction is from the bottom to the top of the tower body; and / or A cooling system is provided in the tower body for cooling the solution at the bottom of the tower body.

10. The complexing agent recovery device according to claim 8, wherein, The draining device includes: The drain pipe is connected at one end to the bottom of the tower body; A control valve, installed on the drain pipe, is used to control the pipe's status; and A cooling device is installed on the drain pipe to cool the solution in the drain pipe.

11. The complexing agent recovery device according to claim 8, wherein, The absorption device further includes: The pickling tower has its inlet connected to the outlet of the last absorption tower.

12. The complexing agent recovery device according to claim 1, wherein, The feed inlet of the calcining furnace is used to directly connect to the discharge outlet of the drying device of the catalyst impregnation system, so as to introduce the catalyst material impregnated by the complexation method into the calcining furnace. and / or The feed inlet of the roasting furnace is connected to at least one feed tank, which is used to store catalyst material impregnated using the complexation method.

13. A catalyst impregnation system comprising the complexing agent recovery device according to any one of claims 1 to 12, wherein, The feed inlet of the calcining furnace is connected to the discharge outlet of the drying device of the catalyst impregnation system, and the discharge outlet of the complexing liquid storage tank is connected to the inlet of the impregnation liquid blending device of the catalyst impregnation system.

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