Conversion device for improving sulfur dioxide acid production
By adding a preheating catalytic section for pre-absorption and temperature optimization in the converter, the problem of low sulfur dioxide conversion efficiency in flue gas was solved, achieving efficient sulfur dioxide-to-acid conversion and energy utilization.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- SHIFANG XINSHIDAI ENVIRONMENTAL PROTECTION TECH CO LTD
- Filing Date
- 2025-06-04
- Publication Date
- 2026-05-08
AI Technical Summary
The low conversion efficiency of sulfur dioxide in flue gas limits production capacity and efficiency, mainly because the oxygen-to-sulfur ratio is less than 1:1 when entering the first stage of the converter.
Based on the original converter, the outlet of the preheating catalytic section is led to an additional absorption tower for connection, adding a pre-absorption stage. The flue gas temperature is optimized through multiple heat exchangers and electric heating devices, forming a five-stage three-stage conversion and three-stage absorption process.
The conversion rate of sulfur dioxide in flue gas was increased to 99.84%. By making rational use of energy, the overall energy consumption was reduced, and the oxygen-sulfur ratio was increased to 1.3:1, which is conducive to improving the efficiency of secondary and tertiary absorption.
Smart Images
Figure CN224212411U_ABST
Abstract
Description
Technical Field
[0001] This utility model relates to the field of flue gas acid production technology, and more specifically, to a conversion device for improving sulfur dioxide acid production. Background Technology
[0002] Currently, the raw material used for flue gas acid production is copper smelting flue gas, which contains about 15% sulfur dioxide. Therefore, when the flue gas enters the catalyst inlet of the first stage of the converter, the sulfur dioxide content is still as high as 14%, while the oxygen content in the flue gas is only about 13%. As a result, the oxygen-sulfur ratio is low, only 1:1, which leads to low conversion efficiency of sulfur dioxide in the subsequent process, thus affecting production capacity and efficiency.
[0003] In view of the above, this application is hereby submitted. Utility Model Content
[0004] The technical problem this invention aims to solve is that the sulfur dioxide content in the flue gas entering the first stage of the converter is as high as 14%, resulting in a low oxygen-to-sulfur ratio of only 1:1. This leads to low sulfur dioxide conversion efficiency, affecting production capacity and efficiency. The purpose is to provide a conversion device that improves sulfur dioxide-to-acid conversion. By connecting the outlet of the preheating catalytic section to an additional absorption tower, the SO3 converted in the preheating catalytic section is pre-absorbed, reducing the SO2 concentration in the flue gas entering the first catalytic section to 8.5%. This reduces the oxygen-to-sulfur ratio to 1.3:1, which is beneficial for improving the secondary conversion rate and thus the overall conversion rate.
[0005] This utility model is achieved through the following technical solution:
[0006] A conversion device for improving sulfur dioxide to acid production includes a conversion tower, wherein a preheating catalytic section, a catalytic section I, a catalytic section II, a catalytic section III, and a catalytic section IV are arranged sequentially from top to bottom within the conversion tower.
[0007] The outlet of the preheating catalytic section is connected to the inlet of the preheating absorption tower via a pipeline.
[0008] The outlet of the preheating absorption tower is connected to the air inlet of the I catalytic section via a pipeline;
[0009] The outlet of the catalytic section III is connected to the inlet of an absorption tower via a pipeline;
[0010] The outlet of the first absorption tower is connected to the inlet of the IV catalytic section via a pipeline;
[0011] The outlet of the IV catalytic section is connected to the second absorption tower via a pipeline.
[0012] This invention connects the outlet of the preheating catalytic section to an additional absorption tower on the basis of the original converter, so that the SO3 converted in the preheating catalytic section is pre-absorbed. This reduces the SO2 concentration in the flue gas entering the first catalytic section to 8.5%, thereby achieving an oxygen-sulfur ratio of 1.3:1, which is beneficial to improving the secondary conversion rate and thus improving the overall conversion rate.
[0013] The existing converters only perform two absorptions. That is, the flue gas passes through the preheating catalytic section, catalytic section I, catalytic section II, and catalytic section III in sequence before going to the first absorption tower. After absorption, it returns to catalytic section IV, and after conversion, it goes to the second absorption tower. That is, the converter adopts a 4+1 process of five stages, two conversions, and two absorptions. As a result, the SO2 concentration in the flue gas entering catalytic section I is high, so the conversion efficiency is low.
[0014] This invention adds a pre-absorption step after the flue gas passes through the preheating catalytic section. The flue gas from the pre-absorption step is then converted through catalytic sections I, II, and III before entering the secondary absorption step. The gas from the secondary absorption step is then converted through catalytic section IV before entering the third absorption step, thus forming a five-stage, three-transformation, three-absorption 1+3+1 process. This significantly increases the oxygen-sulfur ratio in the flue gas entering catalytic section I, which is beneficial for the subsequent secondary and tertiary absorption steps.
[0015] In one specific embodiment, a preheating heat exchanger is provided between the preheating catalytic section and the preheating absorption tower to cool the gas discharged from the outlet of the preheating catalytic section after primary conversion to the absorption temperature of the preheating absorption tower.
[0016] In one specific embodiment, the gas discharged from the outlet of the preheating absorption tower after primary absorption is heated to the required conversion temperature of the I catalytic section by a preheating heat exchanger.
[0017] This invention incorporates a preheating heat exchanger, which can utilize the low-temperature flue gas after primary absorption to cool the high-temperature flue gas discharged from the preheating catalytic section after primary conversion, and can also utilize the high-temperature flue gas to heat the low-temperature flue gas, thereby achieving rational energy utilization and reducing overall energy efficiency. Specifically, the high-temperature flue gas after primary conversion flows through the tube side of the preheating heat exchanger, while the low-temperature flue gas after primary absorption flows through the shell side.
[0018] In one specific embodiment, the outlet of catalytic section I is connected to the inlet of catalytic section II via heat exchanger I.
[0019] In one specific embodiment, the outlet of catalytic section II is connected to the inlet of catalytic section III via heat exchanger II.
[0020] Since the temperature of the flue gas at the outlet of the catalytic section is higher than that at the inlet, this invention is equipped with heat exchanger I and heat exchanger II to appropriately reduce the temperature of the flue gas from catalytic sections I and II, so that the flue gas can meet the conversion temperature of the next catalytic section.
[0021] In one specific embodiment, a heat exchanger is provided between the outlet of the catalytic section III and an absorption tower III, which is used to cool the gas discharged from the outlet of the catalytic section III after secondary conversion to the absorption temperature of the absorption tower III.
[0022] In one specific embodiment, a heat exchanger is provided between the outlet of the IV catalytic section and the second absorption tower to cool the gas discharged from the outlet of the IV catalytic section after three conversions to the absorption temperature of the second absorption tower.
[0023] In one specific embodiment, the gas discharged from the outlet of an absorption tower after secondary absorption is sequentially heated to the required conversion temperature of the IV catalytic section by passing through heat exchanger IV and heat exchanger II.
[0024] This invention can utilize the low-temperature flue gas after secondary absorption to cool the high-temperature flue gas discharged from the IV catalytic stage (after three conversions) and the high-temperature flue gas from the II catalytic stage. It can also utilize the high-temperature flue gas to heat the low-temperature flue gas, thereby achieving rational energy utilization and reducing overall energy efficiency. Specifically, the high-temperature flue gas flows through the tube side, and the low-temperature flue gas flows through the shell side.
[0025] In one specific embodiment, the gas discharged from the outlet of the absorption tower after secondary absorption is further heated to the conversion temperature required by the IV catalytic stage by an electric heating device. In order to ensure that the gas after secondary absorption can be heated to the temperature required for catalyst conversion, an additional electric heating device is provided so that if the low temperature gas does not reach the required temperature after heat exchange in the exchanger, it can be further heated by the electric heating device.
[0026] In one specific implementation, the air inlet at the top of the conversion tower is connected to the drying tower via a pipeline.
[0027] Compared with the prior art, this utility model has the following advantages and beneficial effects:
[0028] 1. This utility model provides an improved sulfur dioxide-to-acid conversion device. By connecting the outlet of the preheating catalytic section to an additional absorption tower on the basis of the original converter, the SO3 converted in the preheating catalytic section is pre-absorbed, which reduces the SO2 concentration in the flue gas entering the first catalytic section to 8.5%, thereby achieving an oxygen-to-sulfur ratio of 1.3:1 in the flue gas. This is beneficial to improving the secondary conversion rate, thus enabling the overall conversion rate to reach 99.84%.
[0029] 2. The present invention provides a conversion device for improving sulfur dioxide to acid production. By drawing out the flue gas after the preheating catalytic section, an additional pre-absorption is added. The flue gas from the pre-absorption is converted through catalytic sections I, II, and III and then enters the secondary absorption. The gas from the secondary absorption is converted through catalytic section IV and then enters the third absorption, thus forming a five-stage, three-stage conversion, and three-stage absorption 1+3+1 process. In this way, the oxygen-sulfur ratio in the flue gas entering catalytic section I is greatly increased, which is beneficial to the subsequent secondary and tertiary absorption.
[0030] 3. The present invention provides a conversion device for improving sulfur dioxide to acid production, which is equipped with multiple heat exchangers and uses the high-temperature flue gas after conversion and the low-temperature flue gas after absorption as the fluids for heat exchange, thereby achieving rational use of energy and reducing overall energy efficiency. Attached Figure Description
[0031] To more clearly illustrate the technical solutions of the exemplary embodiments of this utility model, the drawings used in the embodiments will be briefly introduced below. It should be understood that the following drawings only show some embodiments of this utility model and should not be regarded as a limitation of the scope. For those skilled in the art, other related drawings can be obtained based on these drawings without creative effort.
[0032] Figure 1 A schematic diagram of the conversion tower structure provided in an embodiment of this utility model;
[0033] Figure 2 A sulfur dioxide-to-acid conversion device provided in this embodiment of the utility model.
[0034] The attached diagram shows the markings and corresponding component names:
[0035] 1-Preheating catalytic section, 2-Catalytic section I, 3-Catalytic section II, 4-Catalytic section III, 5-Catalytic section IV, 6-Preheating absorption tower, 7-Absorption tower I, 8-Absorption tower II, 9-Preheating heat exchanger, 10-Heat exchanger I, 11-Heat exchanger II, 12-Heat exchanger III, 13-Heat exchanger IV. Detailed Implementation
[0036] To make the objectives, technical solutions, and advantages of this utility model clearer, the present utility model will be further described in detail below with reference to the embodiments and accompanying drawings. The illustrative embodiments and descriptions of this utility model are only used to explain this utility model and are not intended to limit this utility model.
[0037] In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention. However, it will be apparent to those skilled in the art that these specific details are not necessary to implement the present invention. In other embodiments, well-known structures are not specifically described in order to avoid obscuring the present invention.
[0038] Throughout this specification, references to "an embodiment," "an example," or "an example" mean that a particular feature, structure, or characteristic described in connection with that embodiment or example is included in at least one embodiment of the present invention. Therefore, the phrases "an embodiment," "an example," "an example," or "an example" appearing in various places throughout the specification do not necessarily refer to the same embodiment or example. Furthermore, specific features, structures, or characteristics can be combined in one or more embodiments or examples in any suitable combination and / or sub-combination. Moreover, those skilled in the art will understand that the illustrations provided herein are for illustrative purposes and are not necessarily drawn to scale. The term "and / or" as used herein includes any and all combinations of one or more of the associated listed items.
[0039] In the description of this utility model, the terms "front", "rear", "left", "right", "up", "down", "vertical", "horizontal", "high", "low", "inner", and "outer" indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limiting the scope of protection of this utility model.
[0040] Example 1
[0041] like Figure 1 and Figure 2 As shown in the figure, an embodiment of this utility model provides a conversion device for improving sulfur dioxide to acid production, including a conversion tower. The conversion tower contains, from top to bottom, a preheating catalytic section 1, a catalytic section I 2, a catalytic section II 3, a catalytic section III 4, and a catalytic section IV 5.
[0042] The outlet of the preheating catalytic section 1 is connected to the inlet of the preheating absorption tower 6 via a pipeline.
[0043] The outlet of the preheating absorption tower 6 is connected to the air inlet of the I catalytic section 2 via a pipeline;
[0044] The outlet of the catalytic section 4 is connected to the inlet of an absorption tower 7 via a pipeline;
[0045] The outlet of the first absorption tower 7 is connected to the inlet of the fourth catalytic section 5 via a pipeline;
[0046] The outlet of the catalytic section 5 is connected to the second absorption tower 8 via a pipeline.
[0047] This invention connects the outlet of the preheating catalytic section to an additional absorption tower on the basis of the original converter, so that the SO3 converted in the preheating catalytic section is pre-absorbed. This reduces the SO2 concentration in the flue gas entering the first catalytic section to 8.5%, thereby achieving an oxygen-sulfur ratio of 1.3:1, which is beneficial to improving the secondary conversion rate and thus improving the overall conversion rate.
[0048] The existing converters only perform two absorptions. That is, the flue gas passes through the preheating catalytic section, catalytic section I, catalytic section II, and catalytic section III in sequence before going to the first absorption tower. After absorption, it returns to catalytic section IV, and after conversion, it goes to the second absorption tower. That is, the converter adopts a 4+1 process of five stages, two conversions, and two absorptions. As a result, the SO2 concentration in the flue gas entering catalytic section I is high, so the conversion efficiency is low.
[0049] This invention adds a pre-absorption step after the flue gas passes through the preheating catalytic section. The flue gas from the pre-absorption step is then converted through catalytic sections I, II, and III before entering the secondary absorption step. The gas from the secondary absorption step is then converted through catalytic section IV before entering the third absorption step, thus forming a five-stage, three-transformation, three-absorption 1+3+1 process. This significantly increases the oxygen-sulfur ratio in the flue gas entering catalytic section I, which is beneficial for the subsequent secondary and tertiary absorption steps.
[0050] In one specific embodiment, a preheating heat exchanger 9 is provided between the preheating catalytic section 1 and the preheating absorption tower 6 to cool the gas discharged from the outlet of the preheating catalytic section 1 after primary conversion to the absorption temperature of the preheating absorption tower 6.
[0051] In one specific embodiment, the gas discharged from the outlet of the preheating absorption tower 6 after primary absorption is heated to the required conversion temperature of the I catalytic section 2 by the preheating heat exchanger 9.
[0052] This invention incorporates a preheating heat exchanger, which can utilize the low-temperature flue gas after primary absorption to cool the high-temperature flue gas discharged from the preheating catalytic section after primary conversion, and can also utilize the high-temperature flue gas to heat the low-temperature flue gas, thereby achieving rational energy utilization and reducing overall energy efficiency. Specifically, the high-temperature flue gas after primary conversion flows through the tube side of the preheating heat exchanger, while the low-temperature flue gas after primary absorption flows through the shell side.
[0053] In one specific embodiment, the outlet of catalytic section I 2 is connected to the inlet of catalytic section II 3 via heat exchanger I 10.
[0054] In one specific embodiment, the outlet of the II catalytic section 3 is connected to the inlet of the III catalytic section 4 via the II heat exchanger 11.
[0055] Since the temperature of the flue gas at the outlet of the catalytic section is higher than that at the inlet, this invention is equipped with heat exchanger I and heat exchanger II to appropriately reduce the temperature of the flue gas from catalytic sections I and II, so that the flue gas can meet the conversion temperature of the next catalytic section.
[0056] In one specific embodiment, a heat exchanger 12 is provided between the outlet of the catalytic section III 4 and an absorption tower 7 to cool the gas discharged from the outlet of the catalytic section III 4 after secondary conversion to the absorption temperature of the absorption tower 7.
[0057] In one specific embodiment, a heat exchanger 13 is provided between the outlet of the IV catalytic section 5 and the second absorption tower 8 to cool the gas discharged from the outlet of the IV catalytic section 5 after three conversions to the absorption temperature of the second absorption tower 8.
[0058] In one specific embodiment, the gas discharged from the outlet of an absorption tower 7 after secondary absorption is successively heated to the required conversion temperature of the IV catalytic section 5 by passing through the IV heat exchanger 13 and the II heat exchanger 11.
[0059] This invention can utilize the low-temperature flue gas after secondary absorption to cool the high-temperature flue gas discharged from the IV catalytic stage (after three conversions) and the high-temperature flue gas from the II catalytic stage. It can also utilize the high-temperature flue gas to heat the low-temperature flue gas, thereby achieving rational energy utilization and reducing overall energy efficiency. Specifically, the high-temperature flue gas flows through the tube side, and the low-temperature flue gas flows through the shell side.
[0060] In one specific embodiment, the gas discharged from the outlet of the absorption tower 7 after secondary absorption is further heated to the conversion temperature required by the catalytic stage 5 by an electric heating device. In order to ensure that the gas after secondary absorption can be heated to the temperature required for catalyst conversion, an additional electric heating device is provided so that if the low temperature gas does not reach the required temperature after heat exchange in the heat exchanger, it can be further heated by the electric heating device.
[0061] In one specific implementation, the air inlet at the top of the conversion tower is connected to the drying tower via a pipeline.
[0062] The specific embodiments described above further illustrate the purpose, technical solution, and beneficial effects of this utility model. It should be understood that the above description is only a specific embodiment of this utility model and is not intended to limit the scope of protection of this utility model. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of this utility model should be included within the scope of protection of this utility model.
Claims
1. A conversion device for improving sulfur dioxide to acid production, comprising a conversion tower, wherein the conversion tower is provided with a preheating catalytic section (1), a first catalytic section (2), a second catalytic section (3), a third catalytic section (4), and a fourth catalytic section (5) arranged sequentially from top to bottom, characterized in that, The outlet of the preheating catalytic section (1) is connected to the inlet of the preheating absorption tower (6) via a pipeline; The outlet of the preheating absorption tower (6) is connected to the inlet of the I catalytic section (2) via a pipeline; The outlet of the catalytic section (4) is connected to the inlet of an absorption tower (7) via a pipeline; The outlet of the first absorption tower (7) is connected to the inlet of the IV catalytic section (5) via a pipeline; The outlet of the IV catalytic section (5) is connected to the second absorption tower (8) via a pipeline.
2. The device for improving the conversion of sulfur dioxide to acid according to claim 1, characterized in that, A preheating heat exchanger (9) is provided between the preheating catalytic section (1) and the preheating absorption tower (6) to cool the gas discharged from the outlet of the preheating catalytic section (1) after one conversion to the absorption temperature of the preheating absorption tower (6).
3. The device for improving the conversion of sulfur dioxide to acid according to claim 2, characterized in that, The gas discharged from the outlet of the preheating absorption tower (6) after primary absorption is heated to the required conversion temperature of the I catalytic section (2) by the preheating heat exchanger (9).
4. The conversion device for improving sulfur dioxide to acid production according to claim 1, characterized in that, The outlet of the Ⅰ catalytic section (2) is connected to the inlet of the Ⅱ catalytic section (3) through the Ⅰ heat exchanger (10).
5. The device for improving the conversion of sulfur dioxide to acid according to claim 1, characterized in that, The outlet of the catalytic section II (3) is connected to the inlet of the catalytic section III (4) through the heat exchanger II (11).
6. The device for improving the conversion of sulfur dioxide to acid according to claim 1, characterized in that, A heat exchanger (12) is installed between the outlet of the catalytic section (4) and the absorption tower (7) to cool the gas discharged from the outlet of the catalytic section (4) after secondary conversion to the absorption temperature of the absorption tower (7).
7. The device for improving the conversion of sulfur dioxide to acid according to claim 5, characterized in that, A heat exchanger (13) is installed between the outlet of the IV catalytic section (5) and the second absorption tower (8) to cool the gas discharged from the outlet of the IV catalytic section (5) after three conversions to the absorption temperature of the second absorption tower (8).
8. The device for improving the conversion of sulfur dioxide to acid according to claim 7, characterized in that, The gas discharged from the outlet of the first absorption tower (7) after secondary absorption passes through the IV heat exchanger (13) and the II heat exchanger (11) to be heated to the conversion temperature required by the IV catalytic section (5).
9. The device for improving the conversion of sulfur dioxide to acid according to claim 8, characterized in that, The gas discharged from the outlet of the first absorption tower (7) after secondary absorption is further heated to the conversion temperature required by the IV catalytic section (5) by an electric heating device.
10. The device for improving the conversion of sulfur dioxide to acid according to claim 7, characterized in that, The air inlet at the top of the conversion tower is connected to the drying tower via a pipeline.