Integrated desulfurization and decarbonization device for blast furnace gas
By adopting fluidized bed adsorption towers in blast furnace gas desulfurization and decarbonization technology, synchronous removal of sulfur and carbon and separation of adsorbent materials are achieved, and the problems of long and high costs in the prior art are solved, and the processing process is simplified. Reduces energy consumption and investment costs.
Patent Information
- Application Number
- CN202420442747.1
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-03-07
- Publication Date
- 2024-12-13
- Estimated Expiration
- 2034-03-07
AI Technical Summary
The existing blast furnace gas desulfurization and decarbonization technology has problems such as long overall process, high investment costs, and large energy consumption and material losses, making it difficult to effectively simplify the processing process and reduce costs.
Adsorption towers in the form of fluidized beds, by simultaneously transporting two adsorption materials into the adsorption tower, synchronous removal of sulfur and carbon, and transferring the separation of desorption gas to the separation of adsorption materials, thereby simplifying the processing process and reducing Energy consumption and footprint reduce investment costs.
The treatment process of blast furnace gas reduction and carbon reduction is effectively simplified, the difficulty of separation of desorbed gas H2S and CO2 is reduced, energy consumption and material consumption are reduced, investment costs are reduced, and equipment footprint is reduced.
Smart Images
Figure CN222160087U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to a desulfurization and decarbonization device, in particular to a blast furnace gas integrated desulfurization and decarbonization device, belonging to the field of environmental management. Background Art
[0002] Blast furnace gas is the largest by-product energetic medium in the steel process. In 2012, the national output was nearly 80 billion cubic meters. The calorific value of blast furnace gas is not high, only 3500KJ / m 3 The composition is relatively complex, including N2, CO2, CO, H2, HCl, O2, S, dust, etc. Among them, S contains organic sulfur COS and H2S, which cannot be removed by traditional desulfurization technology, causing equipment corrosion and pollutant emissions in subsequent pipeline transportation and terminal utilization; CO2 content is about 20%, which is the main source of carbon emissions in the steel process. Desulfurization and decarbonization of blast furnace gas at the source is a technical choice that is beneficial to the industry and society. However, for the blast furnaces that have been built, desulfurization and decarbonization require multiple sets of equipment, such as organic sulfur hydrolysis + sulfur adsorption desulfurization equipment, chemical absorption and desorption decarbonization equipment, which have the problems of large land occupation, large investment, high energy consumption and material loss, and long processing process. In actual engineering promotion, it is greatly hindered by the above problems and cost constraints.
[0003] Anhui Weida Environmental Protection Technology Co., Ltd. disclosed a blast furnace gas decarbonization and synergistic desulfurization method, CN116478739A, which adopts the traditional process series mode, that is, the decarbonization + desulfurization treatment method, in which the decarbonization method is amine absorption, and the desulfurization method is hydrolysis + dry adsorption. The overall process flow is long and the investment cost is high. At the same time, the flue gas temperature needs to be repeatedly adjusted to meet the requirements of decarbonization and desulfurization. The system is relatively complex, the operation and maintenance are difficult, and the processing cost is difficult to control. Zhejiang Feida Environmental Protection Technology Co., Ltd. disclosed a CO2 capture and utilization device suitable for blast furnace gas, CN113684068A, which is also similar.
[0004] MCC Southern Metropolis Environmental Protection Engineering Technology Co., Ltd. disclosed a blast furnace gas desulfurization and decarbonization system and process, CN115558529A, which uses an absorbent to remove H2S and CO2 at the same time, and then achieves desulfurization and decarbonization of blast furnace gas through the process of flash evaporation-desorption-sulfur secondary absorption and separation. Although this solution only uses one tower in the absorption stage, the subsequent desorption of the absorbent and the separation of sulfur are still relatively complicated, the overall process is relatively long, and there are multiple operations of heating and cooling and condensation gas-liquid separation, and the energy consumption is inevitably high. Utility Model Content
[0005] In view of the problems of the above-mentioned prior art in desulfurizing and decarbonizing blast furnace gas, such as long overall process flow, high investment cost, high energy consumption and material loss, the utility model proposes a device for integrated desulfurization and decarbonization of blast furnace gas. The utility model adopts a fluidized bed to adsorb and remove sulfur and carbon from blast furnace gas, and realizes the simultaneous removal of sulfur and carbon by simultaneously conveying two adsorption materials into the adsorption tower, thereby transferring the separation of desorbed gas to the separation of adsorption materials, thereby effectively simplifying the treatment process of blast furnace gas pollution reduction and carbon reduction, and greatly reducing the difficulty of separating H2S and CO2 in desorbed gas, reducing energy consumption and floor space, and significantly reducing investment costs.
[0006] According to the implementation scheme of the utility model, a device for integrated desulfurization and decarbonization of blast furnace gas is provided.
[0007] A device for integrated desulfurization and decarbonization of blast furnace gas, the device comprising an adsorption tower, a first cyclone separator, a second cyclone separator, a first silo, and a second silo. The bottom or lower part of the adsorption tower is provided with a blast furnace gas inlet, a first adsorption material inlet, and a second adsorption material inlet. The top or upper part of the adsorption tower is provided with a first outlet and a second outlet. The first outlet is located above the second outlet. The first outlet of the adsorption tower is connected to the inlet of the first cyclone separator. The solid outlet of the first cyclone separator is connected to the first silo. The second outlet of the adsorption tower is connected to the inlet of the second cyclone separator. The solid outlet of the second cyclone separator is connected to the second silo. The tops of the first cyclone separator and the second cyclone separator are both provided with gas outlets.
[0008] In the utility model, the device also includes a desorption tower, a third cyclone separator, and a first gas tank. The bottom or lower part of the desorption tower is provided with a high-temperature carrier gas inlet and a first adsorption particle inlet. The top or upper part of the desorption tower is provided with an outlet. The outlet of the first silo is connected to the first adsorption particle inlet of the desorption tower. The outlet of the desorption tower is connected to the inlet of the third cyclone separator. The gas outlet of the third cyclone separator is connected to the first gas tank.
[0009] In the utility model, the solid outlet of the third cyclone separator is connected to the first adsorption material inlet of the adsorption tower.
[0010] In the utility model, the device further comprises a fresh adsorbent silo arranged upstream of the adsorption tower, wherein the outlet of the fresh adsorbent silo is connected to the second adsorption material inlet of the adsorption tower.
[0011] In the utility model, the device also includes a second gas tank. The bottom or lower part of the desorption tower is also provided with a second adsorption particle inlet. The outlet of the second silo is connected to the second adsorption particle inlet of the desorption tower. The outlet of the desorption tower is connected to the inlet of the third cyclone separator. The gas outlet of the third cyclone separator is connected to the second gas tank.
[0012] Preferably, a three-way valve is provided at the gas outlet of the third cyclone separator. The gas outlet of the third cyclone separator is connected to the inlet of the three-way valve. The first outlet of the three-way valve is connected to the first gas tank. The second outlet of the three-way valve is connected to the second gas tank.
[0013] In the utility model, the solid outlet of the third cyclone separator is connected to the first adsorption material inlet and / or the second adsorption material inlet of the adsorption tower.
[0014] Preferably, a discharge port is further provided at the bottom of the desorption tower, and the discharge port is connected to the first adsorption material inlet and / or the second adsorption material inlet of the adsorption tower.
[0015] Preferably, a first discharge valve is provided at the bottom of the first silo.
[0016] Preferably, a second discharge valve is provided at the bottom of the second silo.
[0017] In the utility model, the device further comprises a hydrolysis tower arranged upstream of the adsorption tower, and the gas outlet of the hydrolysis tower is connected to the blast furnace gas inlet of the adsorption tower.
[0018] In the present invention, the device for integrated desulfurization and decarbonization of blast furnace gas includes two schemes. In the first scheme, Figure 1As shown, the device includes an adsorption tower, a first cyclone separator, a second cyclone separator, a first silo and a second silo. Among them, a blast furnace gas inlet, a first adsorption material inlet and a second adsorption material inlet are provided at the bottom or lower part of the adsorption tower, and an outlet is provided at the top or upper part of the adsorption tower. The first cyclone separator and the second cyclone separator are respectively provided with an inlet, a gas outlet and a solid outlet. After passing through the hydrolysis tower, the organic sulfur COS in the blast furnace gas is hydrolyzed and converted into H2S and CO2. The hydrolyzed blast furnace gas enters the bottom of the adsorption tower from the blast furnace gas inlet, and the two adsorption materials corresponding to the adsorption of H2S and CO2 enter the bottom of the adsorption tower from the first adsorption material inlet and the second adsorption material inlet respectively. The blast furnace gas entering the adsorption tower drives the two adsorption materials to flow in the adsorption tower, and the H2S and CO2 in the blast furnace gas are adsorbed by the two adsorption materials respectively. The two adsorption particles adsorbing H2S and CO2 are separated at different heights on the upper part of the adsorption tower due to differences in particle size, density and mass, and enter the first cyclone separator and the second cyclone separator for discharge respectively. The adsorption particles discharged from the two cyclone separators are transported into their respective silos (i.e., the first silo and the second silo) respectively; the blast furnace gas that has achieved desulfurization and decarbonization is discharged from the gas outlet at the top of the first cyclone separator or the second cyclone separator, and sent to the pipeline for subsequent utilization. This solution realizes the simultaneous desulfurization and decarbonization of blast furnace gas in a single adsorption tower in the form of a fluidized bed, which reduces the equipment footprint and reduces the investment cost. Moreover, two adsorption materials are simultaneously transported into the adsorption tower to achieve the simultaneous removal of sulfur and carbon, and thus the separation of desorbed gas is transferred to the separation of adsorption materials, thereby effectively simplifying the treatment process of blast furnace gas pollution reduction and carbon reduction, and greatly reducing the difficulty of separating H2S and CO2 in the desorbed gas, reducing energy consumption.
[0019] In the above scheme, the device also includes a desorption tower, a third cyclone separator, and a first gas tank. The bottom or lower part of the desorption tower is provided with a high-temperature carrier gas inlet and a first adsorption particle inlet, and the top or upper part of the desorption tower is provided with an outlet. The third cyclone separator is provided with an inlet, a gas outlet, and a solid outlet. After being discharged from the cyclone separator, the first adsorption particles saturated with CO2 adsorption enter the first silo, and the second adsorption particles saturated with H2S adsorption enter the second silo. Among them, the first adsorption particles saturated with CO2 adsorption enter the bottom of the desorption tower from the first adsorption particle inlet, and the high-temperature carrier gas entering the desorption tower from the high-temperature carrier gas inlet drives the first adsorption particles to fluidize and rise in the desorption tower. CO2 is desorbed during the heating process, and the desorbed gas enters the third cyclone separator through the outlet at the top of the desorption tower, and is discharged from the gas outlet of the third cyclone separator to the first gas tank; the adsorption material particles regenerated after desorption are discharged from the solid outlet of the third cyclone separator, and returned to the first adsorption material inlet of the adsorption tower through the conveying device for recycling. At the same time, the second adsorption particles saturated with H2S are directly discarded, and a fresh adsorbent silo is added in front of the adsorption tower to replenish fresh desulfurization adsorbent to the second adsorption material inlet, that is, the desulfurization adsorption material is no longer recycled. This solution recycles the decarbonization adsorption material, effectively reducing energy consumption and material consumption, and saving costs; the desulfurization adsorption material is used once, which reduces costs while ensuring the stability of desulfurization and decarbonization efficiency.
[0020] In the second option, if Figure 2 As shown, the device for integrated desulfurization and decarbonization of blast furnace gas includes an adsorption tower, a first cyclone separator, a second cyclone separator, a first silo, a second silo, a desorption tower, a third cyclone separator, a first gas tank, and a second gas tank, that is, a second gas tank is added on the basis of the first scheme. In this scheme, the desulfurization adsorption material and the decarbonization adsorption material are returned to the adsorption tower for recycling after desorption and regeneration, which further reduces material consumption and reduces costs. At this time, the first adsorption particles saturated with CO2 adsorption in the first silo and the second adsorption particles saturated with H2S adsorption in the second silo are periodically and alternately transported to the desorption tower for desorption and regeneration. When the first silo transports the first adsorption particles into the desorption tower, the generated desorption gas enters the first gas tank via the gas outlet of the third cyclone separator. At this time, the regenerated adsorption material particles are discharged from the solid outlet of the third cyclone separator and returned to the adsorption tower via the first adsorption material inlet for recycling. When the second silo transports the second adsorption particles into the desorption tower, the generated desorption gas enters the second gas tank. At this time, the regenerated adsorption material particles return to the adsorption tower through the second adsorption material inlet for recycling.
[0021] Preferably, the solution further includes a three-way valve disposed at the gas outlet of the third cyclone separator, wherein the valve switching cycle of the three-way valve is consistent with the switching cycle of the first silo and the second silo for alternately conveying adsorbed particles, so that the desorbed gases generated by the two adsorbed particles respectively enter the corresponding gas tanks.
[0022] It is further preferred that a discharge port is provided at the bottom of the desorption tower. If some of the adsorption material particles fall to the bottom of the desorption tower after desorption and regeneration, they are discharged from the discharge port, and returned to the adsorption tower through the first adsorption material inlet or the second adsorption material inlet by the conveying device for recycling. When the first adsorption particles are conveyed into the desorption tower by the first silo, the adsorption material particles that fall to the bottom of the desorption tower after regeneration are discharged from the discharge port and return to the adsorption tower through the first adsorption material inlet. When the second silo conveys the second adsorption particles into the desorption tower, the adsorption material particles that fall to the bottom of the desorption tower after regeneration return to the adsorption tower through the second adsorption material inlet.
[0023] In the present application, a first discharge valve is provided at the bottom of the first silo, a second discharge valve is provided at the bottom of the second silo, and a discharge valve is also provided at the bottom of the fresh adsorbent silo. The setting of the discharge valve controls the discharge time and discharge amount of each silo. Among them, the first discharge valve and the second discharge valve are opened and closed periodically, so that the first adsorbed particles in the first silo and the second adsorbed particles in the second silo alternately enter the desorption tower, and the switching period is preferably 0.5-0.8 times the full silo time of the corresponding silo.
[0024] In the present application, the adsorbent materials entering the adsorption tower include H2S adsorbent material and CO2 adsorbent material. The two adsorbent materials are respectively a micro-mesoporous carbon-based material modified by an alkali metal salt or an alkaline earth metal salt and a molecular sieve material loaded (or unloaded) with amines. Since the adsorption is selective, H2S and CO2 are selectively adsorbed by the two adsorbent materials, respectively, and H2S is mainly chemically adsorbed, while CO2 is mainly physically adsorbed. The adsorption temperatures are both around 40°C. Therefore, the mutual influence of the two adsorbent materials placed in an adsorption tower is small, and the simultaneous removal of sulfur and carbon can be achieved. The two adsorbent materials differ in particle size, density, and quality, and can be separated by controlling the fluidizing gas velocity. Generally speaking, the particle size range of the adsorbent material is 50μm-20mm, and the bulk density of the material is 0.3-0.7g / cm 3 . The present application transfers the separation of desorbed gas to the separation of adsorbent materials on the basis of simultaneous removal of sulfur and carbon, that is, by controlling factors such as fluidizing gas velocity, desorption conditions, and particle size, density, and quality of adsorbent materials, the separation of desorbed gas H2S and CO2 is achieved, and the number of adsorption / desorption tower devices is kept as one group, which simplifies the processing flow and reduces the number of devices. It is a better solution in terms of cost and energy consumption.
[0025] In the present application, the high-temperature carrier gas entering the desorption tower is the crude desorption product gas collected in the product gas tank (i.e., the first gas tank or the second gas tank), so as to avoid the problem that the desorption gas and the carrier gas need to be further separated. Figure 1 There is no decomposition process for the desulfurization adsorption material. It is discarded after reaching saturation after multiple cycles of adsorption of COS and H2S. Fresh desulfurization adsorbent is added to the adsorption tower. At this time, only the decarbonization adsorption material needs to be decomposed, and the carrier gas uses the desorption gas mainly composed of CO2 collected in the first gas tank. Figure 2 In the process, the desorption of the two adsorbent materials is carried out alternately, and the desorbed gas collected in the corresponding gas tank is used as the carrier gas, so the separation of the two desorbed gases can be achieved relatively easily. The temperature of the high-temperature carrier gas in the desorption tower is between 70-150°C, and the gas velocity (relative to the adsorbed particles) is about 0.5-2.0m / s to ensure the fluidization and sufficient desorption of the particles.
[0026] In the present application, "analysis" and "desorption" have the same meaning and can be used interchangeably.
[0027] Compared with the prior art, the utility model has the following beneficial effects:
[0028] 1. The utility model simultaneously transports two adsorption materials into the adsorption tower to achieve the simultaneous removal of sulfur and carbon, and thus transfers the separation of desorbed gas to the separation of adsorption materials, thereby effectively simplifying the treatment process of blast furnace gas pollution reduction and carbon reduction, and greatly reducing the difficulty of separating desorbed gas H2S and CO2, reducing energy consumption.
[0029] 2. Compared with the existing solutions, the desulfurization and decarbonization in the utility model only uses one set of adsorption and desorption towers, which effectively simplifies the treatment process, reduces the equipment footprint, and greatly reduces construction and equipment investment.
[0030] 3. The utility model recycles the decarbonization adsorption material and the desulfurization adsorption material, effectively reducing energy consumption and material consumption and saving costs. Moreover, the utility model adopts a fluidized bed synchronous removal process, which can flexibly adjust the feed amount and feed ratio of the two adsorption materials according to the CO2 and H2S concentrations in the flue gas, thereby reducing material loss and ensuring the stability of the desulfurization and decarbonization efficiency. BRIEF DESCRIPTION OF THE DRAWINGS
[0031] Figure 1 This is a structural schematic diagram of the integrated desulfurization and decarbonization device for blast furnace gas in the utility model;
[0032] Figure 2 This is another structural schematic diagram of the integrated desulfurization and decarbonization device for blast furnace gas in the utility model.
[0033] Reference numerals:
[0034] 1: adsorption tower; 201: first cyclone separator; 202: second cyclone separator; 203: third cyclone separator; 301: first silo; 302: second silo; 4: desorption tower; 501: first gas tank; 502: second gas tank; 6: fresh adsorbent silo; 7: three-way valve; 801: first discharge valve; 802: second discharge valve. DETAILED DESCRIPTION
[0035] The technical solution of the utility model is illustrated below, and the scope of protection requested for the utility model includes but is not limited to the following embodiments.
[0036] According to the implementation scheme of the utility model, a device for integrated desulfurization and decarbonization of blast furnace gas is provided.
[0037] A device for integrated desulfurization and decarbonization of blast furnace gas, the device comprising an adsorption tower 1, a first cyclone separator 201, a second cyclone separator 202, a first silo 301, and a second silo 302. The bottom or lower part of the adsorption tower 1 is provided with a blast furnace gas inlet, a first adsorption material inlet, and a second adsorption material inlet. The top or upper part of the adsorption tower 1 is provided with a first outlet and a second outlet. The first outlet is located above the second outlet. The first outlet of the adsorption tower 1 is connected to the inlet of the first cyclone separator 201. The solid outlet of the first cyclone separator 201 is connected to the first silo 301. The second outlet of the adsorption tower 1 is connected to the inlet of the second cyclone separator 202. The solid outlet of the second cyclone separator 202 is connected to the second silo 302. The tops of the first cyclone separator 201 and the second cyclone separator 202 are both provided with gas outlets.
[0038] In the utility model, the device further comprises a desorption tower 4, a third cyclone separator 203, and a first gas tank 501. The bottom or lower portion of the desorption tower 4 is provided with a high-temperature carrier gas inlet and a first adsorption particle inlet. The top or upper portion of the desorption tower 4 is provided with an outlet. The outlet of the first silo 301 is connected to the first adsorption particle inlet of the desorption tower 4. The outlet of the desorption tower 4 is connected to the inlet of the third cyclone separator 203. The gas outlet of the third cyclone separator 203 is connected to the first gas tank 501.
[0039] In the present invention, the solid outlet of the third cyclone separator 203 is connected to the first adsorption material inlet of the adsorption tower 1 .
[0040] In the present invention, the device further comprises a fresh adsorbent silo 6 arranged upstream of the adsorption tower 1. The outlet of the fresh adsorbent silo 6 is connected to the second adsorption material inlet of the adsorption tower 1.
[0041] In the present invention, the device further comprises a second gas tank 502. A second adsorbed particle inlet is also provided at the bottom or lower portion of the desorption tower 4. The outlet of the second silo 302 is connected to the second adsorbed particle inlet of the desorption tower 4. The outlet of the desorption tower 4 is connected to the inlet of the third cyclone separator 203. The gas outlet of the third cyclone separator 203 is connected to the second gas tank 502.
[0042] Preferably, a three-way valve 7 is provided at the gas outlet of the third cyclone separator 203. The gas outlet of the third cyclone separator 203 is connected to the inlet of the three-way valve 7. The first outlet of the three-way valve 7 is connected to the first gas tank 501. The second outlet of the three-way valve 7 is connected to the second gas tank 502.
[0043] In the present invention, the solid outlet of the third cyclone separator 203 is connected to the first adsorption material inlet and / or the second adsorption material inlet of the adsorption tower 1 .
[0044] Preferably, a discharge port is further provided at the bottom of the desorption tower 4 , and the discharge port is connected to the first adsorption material inlet and / or the second adsorption material inlet of the adsorption tower 1 .
[0045] Preferably, a first discharge valve 801 is provided at the bottom of the first silo 301 .
[0046] Preferably, a second discharge valve 802 is provided at the bottom of the second silo 302 .
[0047] In the present invention, the device further comprises a hydrolysis tower arranged upstream of the adsorption tower 1. The gas outlet of the hydrolysis tower is connected to the blast furnace gas inlet of the adsorption tower 1.
[0048] Example 1
[0049] like Figure 1 As shown, a device for integrated desulfurization and decarbonization of blast furnace gas includes an adsorption tower 1, a first cyclone separator 201, a second cyclone separator 202, a first silo 301, and a second silo 302. The bottom of the adsorption tower 1 is provided with a blast furnace gas inlet, and the lower part is provided with a first adsorption material inlet and a second adsorption material inlet. The upper part of the adsorption tower 1 is provided with a first outlet and a second outlet. The first outlet is located above the second outlet. The first outlet of the adsorption tower 1 is connected to the inlet of the first cyclone separator 201. The solid outlet of the first cyclone separator 201 is connected to the first silo 301. The second outlet of the adsorption tower 1 is connected to the inlet of the second cyclone separator 202. The solid outlet of the second cyclone separator 202 is connected to the second silo 302. The tops of the first cyclone separator 201 and the second cyclone separator 202 are both provided with gas outlets.
[0050] Example 2
[0051] Example 1 is repeated, except that the device further includes a desorption tower 4, a third cyclone separator 203, and a first gas tank 501. The bottom of the desorption tower 4 is provided with a high-temperature carrier gas inlet, and the lower part is provided with a first adsorption particle inlet. The top of the desorption tower 4 is provided with an outlet. The outlet of the first silo 301 is connected to the first adsorption particle inlet of the desorption tower 4. The outlet of the desorption tower 4 is connected to the inlet of the third cyclone separator 203. The gas outlet of the third cyclone separator 203 is connected to the first gas tank 501.
[0052] Example 3
[0053] Example 2 is repeated except that the solid outlet of the third cyclone separator 203 is connected to the first adsorption material inlet of the adsorption tower 1 .
[0054] Example 4
[0055] Example 3 is repeated, except that the device further comprises a fresh adsorbent silo 6 disposed upstream of the adsorption tower 1. The outlet of the fresh adsorbent silo 6 is connected to the second adsorption material inlet of the adsorption tower 1.
[0056] Example 5
[0057] Example 4 is repeated, except that a first discharge valve 801 is provided at the bottom of the first silo 301. A discharge valve is also provided at the bottom of the fresh adsorbent silo 6.
[0058] Example 6
[0059] like Figure 2 As shown, a device for integrated desulfurization and decarbonization of blast furnace gas includes an adsorption tower 1, a first cyclone separator 201, a second cyclone separator 202, a first silo 301, and a second silo 302. The bottom of the adsorption tower 1 is provided with a blast furnace gas inlet, and the lower part is provided with a first adsorption material inlet and a second adsorption material inlet. The upper part of the adsorption tower 1 is provided with a first outlet and a second outlet. The first outlet is located above the second outlet. The first outlet of the adsorption tower 1 is connected to the inlet of the first cyclone separator 201. The solid outlet of the first cyclone separator 201 is connected to the first silo 301. The second outlet of the adsorption tower 1 is connected to the inlet of the second cyclone separator 202. The solid outlet of the second cyclone separator 202 is connected to the second silo 302. The tops of the first cyclone separator 201 and the second cyclone separator 202 are both provided with gas outlets.
[0060] The device also includes a desorption tower 4, a third cyclone separator 203, and a first gas tank 501. The bottom of the desorption tower 4 is provided with a high-temperature carrier gas inlet, and the lower part is provided with a first adsorption particle inlet. The top of the desorption tower 4 is provided with an outlet. The outlet of the first silo 301 is connected to the first adsorption particle inlet of the desorption tower 4. The outlet of the desorption tower 4 is connected to the inlet of the third cyclone separator 203. The gas outlet of the third cyclone separator 203 is connected to the first gas tank 501.
[0061] The device also includes a second gas tank 502. A second adsorbed particle inlet is also provided at the lower portion of the desorption tower 4. The outlet of the second silo 302 is connected to the second adsorbed particle inlet of the desorption tower 4. The outlet of the desorption tower 4 is connected to the inlet of the third cyclone separator 203. The gas outlet of the third cyclone separator 203 is connected to the second gas tank 502.
[0062] In this embodiment, the first silo and the second silo periodically and alternately transport adsorbed particles into the desorption tower. When the first silo transports the first adsorbed particles into the desorption tower, the generated desorbed gas enters the first gas tank via the third cyclone separator. When the second silo transports the second adsorbed particles into the desorption tower, the generated desorbed gas enters the second gas tank.
[0063] Example 7
[0064] Example 6 is repeated, except that a three-way valve 7 is provided at the gas outlet of the third cyclone separator 203. The gas outlet of the third cyclone separator 203 is connected to the inlet of the three-way valve 7. The first outlet of the three-way valve 7 is connected to the first gas tank 501. The second outlet of the three-way valve 7 is connected to the second gas tank 502.
[0065] The valve switching cycle of the three-way valve is consistent with the switching cycle of the first silo and the second silo for alternately conveying the adsorbed particles.
[0066] Example 8
[0067] Example 7 is repeated except that the solid outlet of the third cyclone separator 203 is connected to the first adsorption material inlet and the second adsorption material inlet of the adsorption tower 1 respectively.
[0068] When the first silo delivers the first adsorbent particles into the desorption tower, the regenerated adsorbent material particles are discharged from the solid outlet of the third cyclone separator and return to the adsorption tower through the first adsorbent material inlet for recycling. When the second silo delivers the second adsorbent particles into the desorption tower, the regenerated adsorbent material particles return to the adsorption tower through the second adsorbent material inlet.
[0069] Example 9
[0070] Example 8 was repeated, except that a discharge port was further provided at the bottom of the desorption tower 4. The discharge port was connected to the first adsorption material inlet and the second adsorption material inlet of the adsorption tower 1 respectively.
[0071] When the first silo delivers the first adsorption particles into the desorption tower, the adsorption material particles that have fallen to the bottom of the desorption tower after regeneration are discharged from the discharge port and return to the adsorption tower through the first adsorption material inlet for recycling. When the second silo delivers the second adsorption particles into the desorption tower, the adsorption material particles that have fallen to the bottom of the desorption tower after regeneration return to the adsorption tower through the second adsorption material inlet.
[0072] Example 10
[0073] Example 9 is repeated, except that a first discharge valve 801 is provided at the bottom of the first silo 301. A second discharge valve 802 is provided at the bottom of the second silo 302.
[0074] The first discharge valve and the second discharge valve are opened and closed periodically, so that the first adsorption particles in the first silo and the second adsorption particles in the second silo enter the desorption tower alternately.
[0075] Embodiment 11
[0076] Example 10 was repeated, except that the device further included a hydrolysis tower disposed upstream of the adsorption tower 1. The gas outlet of the hydrolysis tower was connected to the blast furnace gas inlet of the adsorption tower 1.
Claims
1. A device for integrated desulfurization and decarbonization of blast furnace gas, characterized in that: The device comprises an adsorption tower (1), a first cyclone separator (201), a second cyclone separator (202), a first silo (301), and a second silo (302); wherein a blast furnace gas inlet, a first adsorption material inlet, and a second adsorption material inlet are provided at the bottom or lower portion of the adsorption tower (1); a first outlet and a second outlet are provided at the top or upper portion of the adsorption tower (1); the first outlet is located above the second outlet; the first outlet of the adsorption tower (1) is connected to the inlet of the first cyclone separator (201); the solid outlet of the first cyclone separator (201) is connected to the first silo (301); the second outlet of the adsorption tower (1) is connected to the inlet of the second cyclone separator (202); the solid outlet of the second cyclone separator (202) is connected to the second silo (302); and the tops of the first cyclone separator (201) and the second cyclone separator (202) are both provided with gas outlets.
2. The device according to claim 1, characterized in that: The device also includes a desorption tower (4), a third cyclone separator (203), and a first gas tank (501); wherein a high-temperature carrier gas inlet and a first adsorption particle inlet are provided at the bottom or lower portion of the desorption tower (4); an outlet is provided at the top or upper portion of the desorption tower (4); the outlet of the first silo (301) is connected to the first adsorption particle inlet of the desorption tower (4); the outlet of the desorption tower (4) is connected to the inlet of the third cyclone separator (203); and the gas outlet of the third cyclone separator (203) is connected to the first gas tank (501).
3. The device according to claim 2, characterized in that: The solid outlet of the third cyclone separator (203) is connected to the first adsorption material inlet of the adsorption tower (1).
4. The device according to claim 3, characterized in that: The device further comprises a fresh adsorbent silo (6) arranged upstream of the adsorption tower (1); the outlet of the fresh adsorbent silo (6) is connected to the second adsorption material inlet of the adsorption tower (1).
5. The device according to claim 2, characterized in that: The device also includes a second gas tank (502); a second adsorption particle inlet is also provided at the bottom or lower part of the desorption tower (4); the outlet of the second silo (302) is connected to the second adsorption particle inlet of the desorption tower (4); and the gas outlet of the third cyclone separator (203) is connected to the second gas tank (502).
6. The device according to claim 5, characterized in that: A three-way valve (7) is provided at the gas outlet of the third cyclone separator (203); the gas outlet of the third cyclone separator (203) is connected to the inlet of the three-way valve (7); the first outlet of the three-way valve (7) is connected to the first gas tank (501); and the second outlet of the three-way valve (7) is connected to the second gas tank (502).
7. The device according to claim 5 or 6, characterized in that: The solid outlet of the third cyclone separator (203) is connected to the first adsorption material inlet and / or the second adsorption material inlet of the adsorption tower (1).
8. The device according to claim 5 or 6, characterized in that: The bottom of the desorption tower (4) is also provided with a discharge port; the discharge port is connected to the first adsorption material inlet and / or the second adsorption material inlet of the adsorption tower (1).
9. The device according to any one of claims 1 to 6, characterized in that: A first discharge valve (801) is provided at the bottom of the first silo (301); and / or A second discharge valve (802) is provided at the bottom of the second silo (302).
10. The device according to claim 7, characterized in that: A first discharge valve (801) is provided at the bottom of the first silo (301); and / or A second discharge valve (802) is provided at the bottom of the second silo (302).
11. The device according to claim 8, characterized in that: A first discharge valve (801) is provided at the bottom of the first silo (301); and / or A second discharge valve (802) is provided at the bottom of the second silo (302).
12. The device according to any one of claims 1 to 6, characterized in that: The device also comprises a hydrolysis tower arranged upstream of the adsorption tower (1); the gas outlet of the hydrolysis tower is connected to the blast furnace gas inlet of the adsorption tower (1).
13. The device according to claim 7, characterized in that: The device also comprises a hydrolysis tower arranged upstream of the adsorption tower (1); the gas outlet of the hydrolysis tower is connected to the blast furnace gas inlet of the adsorption tower (1).
14. The device according to claim 8, characterized in that: The device also comprises a hydrolysis tower arranged upstream of the adsorption tower (1); the gas outlet of the hydrolysis tower is connected to the blast furnace gas inlet of the adsorption tower (1).
15. The device according to claim 9, characterized in that: The device also comprises a hydrolysis tower arranged upstream of the adsorption tower (1); the gas outlet of the hydrolysis tower is connected to the blast furnace gas inlet of the adsorption tower (1).