CN114307868A - Multistage conversion tower for sulfuric acid process by contact method - Google Patents
Multistage conversion tower for sulfuric acid process by contact method Download PDFInfo
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- CN114307868A CN114307868A CN202011085584.9A CN202011085584A CN114307868A CN 114307868 A CN114307868 A CN 114307868A CN 202011085584 A CN202011085584 A CN 202011085584A CN 114307868 A CN114307868 A CN 114307868A
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- heat exchange
- heat
- conversion tower
- conversion
- sulfuric acid
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 82
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 52
- 238000000034 method Methods 0.000 title claims abstract description 39
- 230000008569 process Effects 0.000 title claims abstract description 26
- 239000003054 catalyst Substances 0.000 claims abstract description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 230000003044 adaptive effect Effects 0.000 claims description 3
- 239000002893 slag Substances 0.000 claims description 3
- 230000005540 biological transmission Effects 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 13
- 230000006872 improvement Effects 0.000 description 9
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 7
- 239000012495 reaction gas Substances 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulfur dioxide Inorganic materials O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 229910052720 vanadium Inorganic materials 0.000 description 3
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 3
- 238000003723 Smelting Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 230000029087 digestion Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 230000036632 reaction speed Effects 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 229910000272 alkali metal oxide Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052755 nonmetal Inorganic materials 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 description 1
- 229910052683 pyrite Inorganic materials 0.000 description 1
- 239000011028 pyrite Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000006057 reforming reaction Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
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Abstract
The invention provides a multistage conversion tower for a sulfuric acid process by a contact method, which comprises a conversion tower body, a heat conducting oil evaporator and a heat conducting oil pump, wherein the heat conducting oil evaporator is arranged on the conversion tower body; a plurality of conversion reaction zones and heat release buffer zones filled with catalysts are arranged in the conversion tower body in a staggered manner from bottom to top, the bottom of the conversion tower body is provided with an air inlet, and the top of the conversion tower body is provided with an air outlet; a group of heat exchange tubes are arranged in the heat release buffer area; a heat exchange pipeline is arranged in the heat conduction oil evaporator, and two ends of the heat exchange pipeline are respectively connected with a heat exchange pipeline inlet and a heat exchange pipeline outlet which are arranged on the surface of the heat conduction oil evaporator; the heat exchange tube of the conversion tower body, the heat exchange pipeline of the heat conducting oil evaporator and the heat conducting oil pump are connected into a ring. The multistage conversion tower for the sulfuric acid process by the contact method has a simple structure, is convenient to manage, can complete all conversion reactions and heat transmission in the conversion tower, and does not need to be led out to enter a heat exchanger when the gas temperature rises to 550 ℃ in the reaction process of the conventional conversion tower.
Description
Technical Field
The invention provides a multistage conversion tower for a sulfuric acid process by a contact method, belonging to the field of chemical equipment.
Background
Currently, processes for producing sulfuric acid include contact processes and digestion processes. The concentration of the sulfuric acid prepared by the digestion method is low; the contact sulfuric acid process, whether it is a process for preparing acid by pyrite or sulfur, or a process for preparing acid by smelting various other ores, is the most common method, and the concentration of the finally obtained sulfuric acid is more than 98%.
The contact process for preparing sulfuric acid mainly comprises three stages: SO (SO)2Preparation of SO2Conversion to SO3、SO3And (4) absorbing. SO (SO)2Conversion to SO3The reaction of (2) can be completed only under the action of a catalyst. The conversion reaction is exothermic and the catalyst is usually V2O5The vanadium catalyst is a main active component, simultaneously an alkali metal oxide is added as a promoter, and diatomite which is added with a metal or nonmetal oxide to increase the strength and the activity is used as a carrier of the catalyst. The catalyst is prepared into columnar particles with the diameter of 4-6 mm and the length of 5-15 mm, and in recent years, the catalyst is also prepared into spherical or annular particles in order to reduce the resistance of gas flowing through a bed layer of the catalyst and reduce energy consumption.
The light-off temperature of the sulfuric acid process conversion catalyst is typically slightly above 400 ℃. The light-off temperature of the low-temperature active vanadium catalyst can reach about 370 ℃. Raw gas (SO) entering the conversion tower2+O2) The temperature must be greater than the light-off temperature of the catalyst, typically 410-450 ℃. Because the temperature of the raw material gas for preparing acid by ore smelting is reduced to about 40 ℃ after wet purification, the raw material gas must be heated by a heat exchanger, and the raw material gas is indirectly heated to the temperature required by the reaction by hot gas after the conversion reaction and then enters a conversion tower.
Due to SO2Conversion to SO3The reaction(s) is an exothermic reaction (exotherm Q: at 25 ℃ per 1mol of SO formed3The exothermic heat of (2) was 98.4 kJ. The vanadium catalyst has a higher reaction speed and a higher conversion rate at 400 ℃), which can cause the temperature of a catalyst bed to rise, and if the temperature exceeds 650 ℃, the catalyst is damaged. The conversion tower is generally divided into 3-5 layers, and indirect or direct cooling is carried out between layers, so that the catalyst and reaction gas keep proper temperature, high conversion rate and high reaction speed.
In the modern twice conversion process of sulfuric acid production, gas passing through two or three layers of catalysts enters an intermediate absorption tower to absorb SO in the gas3After the residual air is heated again and passes throughAnd the catalyst layer on the surface is converted for the second time and then enters the absorption tower for final absorption. The intermediate absorption removes the reaction product, so that the secondary conversion rate is improved, and the total conversion rate is more than 99.5 percent. However, since the two conversion processes are performed, the production equipment is complicated, and more than two conversion towers and absorption towers are required, which not only increases the cost, but also causes inconvenience in installation and installation.
Disclosure of Invention
The technical problem is as follows: in order to solve the defects of the prior art, the invention provides a multistage conversion tower for a sulfuric acid process by a contact method.
The technical scheme is as follows: the invention provides a multistage conversion tower for a sulfuric acid process by a contact method, which comprises a conversion tower body, a heat conducting oil evaporator and a heat conducting oil pump, wherein the heat conducting oil evaporator is arranged on the conversion tower body; a plurality of conversion reaction zones and heat release buffer zones filled with catalysts are arranged in the conversion tower body in a staggered manner from bottom to top, the bottom of the conversion tower body is provided with an air inlet, and the top of the conversion tower body is provided with an air outlet; a group of heat exchange tubes are arranged in the heat release buffer area; a heat exchange pipeline is arranged in the heat conduction oil evaporator, and two ends of the heat exchange pipeline are respectively connected with a heat exchange pipeline inlet and a heat exchange pipeline outlet which are arranged on the surface of the heat conduction oil evaporator; the heat exchange tube of the conversion tower body, the heat exchange pipeline of the heat conducting oil evaporator and the heat conducting oil pump are connected into a ring.
As an improvement, the annular pipeline formed by the heat exchange pipe of the conversion tower body, the heat exchange pipeline of the heat conduction oil evaporator and the heat conduction oil pump is filled with heat conduction oil as a heat exchange medium.
As another improvement, the device also comprises a control valve and a temperature detector; the control valve is connected with the heat conduction oil evaporator in parallel, the temperature detector is arranged at the outlet end of the heat conduction oil pump, and the temperature detector sends a temperature signal to the control valve.
As another improvement, the side wall of the cavity of the heat-conducting oil evaporator is provided with a water inlet, the top of the cavity is provided with a steam outlet, and the bottom of the cavity is provided with a slag discharge port.
As another improvement, the heat exchanger also comprises an inlet header and an outlet header, wherein all heat exchange tubes in the heat release buffer area are connected with the heat conduction oil pump through the inlet header and are connected with a heat exchange pipeline of the heat conduction oil evaporator through the outlet header.
As a further improvement, the inlet header is connected with the inlet end of each heat exchange tube through a balancer; the outlet header is connected with the outlet end of each heat exchange tube through a balancer; the balancer is a throttle orifice plate.
As another improvement, the heat exchange tubes form a plurality of heat exchange layers in the heat release buffer area, and each heat exchange layer is composed of more than one heat exchange tube.
As a further improvement, the heat exchange tubes in each layer of heat exchange layer are coiled tubes adaptive to the circular ring surface, and the inner curvature radius of the heat exchange tubes is small, and the outer curvature radius of the heat exchange tubes is large.
As a further improvement, each layer of heat exchange layer is provided with a group of fins connected with the heat exchange tube, and the fins can be spiral fins.
As another improvement, the device also comprises a central upright which is arranged in the conversion tower body and used for supporting the conversion tower, the conversion reaction zone and the heat release buffer zone.
Has the advantages that: the multistage conversion tower for the sulfuric acid process by the contact method has a simple structure, is convenient to manage, can complete all conversion reactions and heat transmission in the conversion tower, and does not need to be led out to enter a heat exchanger for cooling when the gas temperature rises to 550 ℃ in the reaction process like the conventional conversion tower, and then is led into the conversion tower for continuous conversion.
Drawings
FIG. 1 is a schematic diagram of the structure of a multistage conversion tower for a sulfuric acid process by a contact method according to the present invention.
FIG. 2 is a cross-sectional view of a reforming tower having heat exchange tubes.
Fig. 3 is a partially enlarged view of the reforming tower body.
Fig. 4 is a schematic structural view of the balancer.
Detailed Description
The present invention is further explained below.
A multistage conversion tower for a sulfuric acid process by a contact method is shown in figures 1 to 4 and comprises a conversion tower body 1, a heat conduction oil evaporator 2, a heat conduction oil pump 3, a control valve 4 and a temperature detector 5.
A plurality of conversion reaction zones 11 filled with catalysts and heat release buffer zones 12 are arranged in the conversion tower body 1 from bottom to top in a staggered manner, the bottom of the conversion tower body 1 is provided with an air inlet 13, and the top of the conversion tower body is provided with an air outlet 14; a group of heat exchange tubes 15 are arranged in the heat release buffer area 12; the heat-transfer oil evaporator also comprises an inlet header 17 and an outlet header 18, wherein all heat exchange tubes 15 in the heat release buffer area 12 are connected with the heat-transfer oil pump 3 through the inlet header 17 and are connected with a heat exchange pipeline 21 of the heat-transfer oil evaporator 2 through the outlet header 18. The inlet header 17 is connected with the inlet end of each heat exchange tube 15 through a balancer 10; the outlet header 18 is connected with the outlet end of each heat exchange pipe 15 through a balancer 10, and is used for balancing the flow of the heating medium; the balancer 10 is a restriction orifice. The device also comprises a central upright post 19, wherein the central upright post 19 is arranged in the conversion tower body 1 and is used for supporting the conversion tower 1, the conversion reaction zone 11 and the heat release buffer zone 12.
The heat exchange tubes 15 form a plurality of heat exchange layers in the heat release buffer area 12, and each heat exchange layer is composed of more than one heat exchange tube 15; the heat exchange tubes 15 in each layer of heat exchange layer are coiled tubes adaptive to the torus, and the inner side curvature radius is small, and the outer side curvature radius is large; each layer of heat exchange layer is provided with a group of fins connected with the heat exchange tube 15, and the fins can be spiral fins.
A heat exchange pipeline 21 is arranged in the heat conduction oil evaporator 2, and two ends of the heat exchange pipeline 21 are respectively connected with a heat exchange pipeline inlet 22 and a heat exchange pipeline outlet 23 which are arranged on the surface of the heat conduction oil evaporator 2; the side wall of the cavity of the heat-conducting oil evaporator 2 is provided with a water inlet 24, the top is provided with a steam outlet 25, and the bottom is provided with a slag discharge port 26.
The heat exchange tube 15 of the conversion tower body 1, the heat exchange pipeline 21 of the heat conducting oil evaporator 2 and the heat conducting oil pump 3 are connected into a ring; the annular pipeline formed by the heat exchange pipe 15 of the conversion tower body 1, the heat exchange pipeline 21 of the heat conduction oil evaporator 2 and the heat conduction oil pump 3 is filled with heat conduction oil as a heat exchange medium.
The control valve 4 is connected with the heat conduction oil evaporator 2 in parallel, the temperature detector 5 is arranged at the outlet end of the heat conduction oil pump 3, and the temperature detector 5 sends a temperature signal to the control valve 4.
The working principle of the device is as follows:
sulfur dioxide and oxygen to be reacted enter the conversion tower body 1 from the gas inlet 13, contact and react with the catalyst in the conversion reaction zone 11, and sulfur trioxide flows out from the gas outlet 14 at the top.
The heat released by the catalytic reaction exchanges heat with the heat conduction oil in the heat exchange tube 15, so that the temperature in the conversion tower body 1 is basically constant; the heat-absorbing heat-conducting oil exchanges heat with media such as water in the heat-conducting oil evaporator 2 and then enters the conversion tower body 1 again to absorb heat.
The heat exchange tubes are disposed between the layers of the reforming reaction zone 11 (catalyst layer). The proper working temperature t of the heat conducting oil is less than 300 ℃, so that the gas which is changed into high temperature due to the heat generated by the reaction in the catalyst layer can be timely cooled to proper temperature and then enters the upper catalyst layer. The heat transfer oil is selected as the heat transfer medium, and the heat transfer oil can flow through the heat exchange pipe without being limited by the temperature of the catalyst which must be higher than 370 ℃ and lower than 650 ℃.
The heat exchange tubes at each height can be set into a plurality of groups of snakelike tube bundles which are suitable for the torus, the inner side curvature radius is smaller, the outer side curvature radius is larger, and the reaction gas is cooled in time. The fins outside the tube can be spiral high-frequency welding fins, and the fin spacing can be set according to the condition of conventional gas. The temperature difference of the inlet and the outlet of the heat transfer oil in the heat exchange pipe in the conversion tower only needs to ensure that the temperature of the reaction gas is uniform and equal when the reaction gas enters the whole catalyst layer. The heat exchange tubes are arranged between catalyst layers, and the local concentration difference of reaction gas is adjusted uniformly after flowing through the heat exchange tube bundle after automatic expansion. The heat exchange tubes can also be grouped according to the temperature required by reactants with different concentrations, so that the requirement is met.
The grouping number of the catalyst layers in the whole conversion tower can be determined according to the temperature difference required by constant temperature. If the temperature difference between the inlet and outlet of the reaction gas entering the catalyst layer is required to be small, the number of groups can be large. This ensures that the conversion reaction is substantially within a constant temperature range.
The above-mentioned embodiments only express several embodiments of the present invention, and the description thereof is more specific and detailed, but not construed as limiting the scope of the invention. It should be noted that, for those skilled in the art, various changes and modifications can be made without departing from the spirit of the invention, and these changes and modifications are within the scope of the invention. Therefore, the protection scope of the present patent shall be subject to the appended claims.
Claims (9)
1. A multistage conversion tower for a sulfuric acid process by a contact method is characterized in that: the device comprises a conversion tower body (1), a heat conducting oil evaporator (2) and a heat conducting oil pump (3); a plurality of conversion reaction zones (11) filled with catalysts and heat release buffer zones (12) are arranged in the conversion tower body (1) from bottom to top in a staggered manner, the bottom of the conversion tower body (1) is provided with an air inlet (13), and the top of the conversion tower body is provided with an air outlet (14); a group of heat exchange tubes (15) are arranged in the heat release buffer area (12); a heat exchange pipeline (21) is arranged in the heat conduction oil evaporator (2), and two ends of the heat exchange pipeline (21) are respectively connected with a heat exchange pipeline inlet (22) and a heat exchange pipeline outlet (23) which are arranged on the surface of the heat conduction oil evaporator (2); the heat exchange tube (15) of the conversion tower body (1), the heat exchange pipeline (21) of the heat conduction oil evaporator (2) and the heat conduction oil pump (3) are connected into a ring; and heat conduction oil is filled in an annular pipeline formed by the heat exchange pipe (15) of the conversion tower body (1), the heat exchange pipeline (21) of the heat conduction oil evaporator (2) and the heat conduction oil pump (3) to serve as a heat exchange medium.
2. The multistage conversion tower for the contact sulfuric acid process according to claim 1, characterized in that: the device also comprises a control valve (4) and a temperature detector (5); the control valve (4) is connected with the heat conduction oil evaporator (2) in parallel, the temperature detector (5) is arranged at the outlet end of the heat conduction oil pump (3), and the temperature detector (5) sends a temperature signal to the control valve (4).
3. The multistage conversion tower for the contact sulfuric acid process according to claim 2, characterized in that: the side wall of the cavity of the heat-conducting oil evaporator (2) is provided with a water inlet (24), the top of the cavity is provided with a steam outlet (25), and the bottom of the cavity is provided with a slag discharge hole (26).
4. The multistage conversion tower for the contact sulfuric acid process according to claim 1, characterized in that: the heat exchange system is characterized by further comprising an inlet header (17) and an outlet header (18), wherein all heat exchange tubes (15) in the heat release buffer area (12) are connected with the heat conduction oil pump (3) through the inlet header (17) and connected with a heat exchange pipeline (21) of the heat conduction oil evaporator (2) through the outlet header (18).
5. The multistage conversion tower for the contact sulfuric acid process according to claim 5, characterized in that: the inlet header (17) is connected with the inlet end of each heat exchange tube (15) through a balancer (10); the outlet header (18) is connected with the outlet end of each heat exchange tube (15) through a balancer (10); the balancer (10) is a throttle orifice plate.
6. The multistage conversion tower for the contact sulfuric acid process according to claim 1, characterized in that: the heat exchange tubes (15) form a plurality of heat exchange layers in the heat release buffer area (12), and each heat exchange layer is composed of more than one heat exchange tube (15).
7. The multistage conversion tower for the contact sulfuric acid process according to claim 7, characterized in that: the heat exchange tubes (15) in each layer of heat exchange layer are coiled tubes adaptive to the torus, and the inner side curvature radius is small, and the outer side curvature radius is large.
8. The multistage conversion tower for the contact sulfuric acid process according to claim 7, characterized in that: each layer of heat exchange layer is provided with a group of fins connected with the heat exchange tube (15), and the fins are spiral fins.
9. The multistage conversion tower for the contact sulfuric acid process according to claim 1, characterized in that: the device is characterized by further comprising a center pillar (19), wherein the center pillar (19) is arranged in the conversion tower body (1) and used for supporting the conversion tower (1), the conversion reaction zone (11) and the heat release buffer zone (12).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011085584.9A CN114307868A (en) | 2020-10-12 | 2020-10-12 | Multistage conversion tower for sulfuric acid process by contact method |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202011085584.9A CN114307868A (en) | 2020-10-12 | 2020-10-12 | Multistage conversion tower for sulfuric acid process by contact method |
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| CN202011085584.9A Pending CN114307868A (en) | 2020-10-12 | 2020-10-12 | Multistage conversion tower for sulfuric acid process by contact method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN118637564A (en) * | 2024-08-15 | 2024-09-13 | 福建天甫电子材料有限公司 | Electronic grade sulfuric acid preparation equipment and preparation method thereof |
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| CN1603229A (en) * | 2004-10-12 | 2005-04-06 | 南化集团研究院 | Humid gas conversion and heat reclamation acid preparation technique |
| CN109476479A (en) * | 2016-07-21 | 2019-03-15 | 托普索公司 | The method that sulfuric acid is produced from sulfur feed stock using quenching of gases |
| CN109987587A (en) * | 2019-04-29 | 2019-07-09 | 哈尔滨博奥环境技术有限公司 | A kind of sulfuric acid Preparation equipment and technique |
| CN213493610U (en) * | 2020-10-12 | 2021-06-22 | 南京华电节能环保股份有限公司 | Low-energy-consumption multistage conversion tower for sulfuric acid production |
-
2020
- 2020-10-12 CN CN202011085584.9A patent/CN114307868A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1603229A (en) * | 2004-10-12 | 2005-04-06 | 南化集团研究院 | Humid gas conversion and heat reclamation acid preparation technique |
| CN109476479A (en) * | 2016-07-21 | 2019-03-15 | 托普索公司 | The method that sulfuric acid is produced from sulfur feed stock using quenching of gases |
| CN109987587A (en) * | 2019-04-29 | 2019-07-09 | 哈尔滨博奥环境技术有限公司 | A kind of sulfuric acid Preparation equipment and technique |
| CN213493610U (en) * | 2020-10-12 | 2021-06-22 | 南京华电节能环保股份有限公司 | Low-energy-consumption multistage conversion tower for sulfuric acid production |
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| Title |
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| Н.Г.拉索欣著: "核电站蒸汽发生器装置", 原子能出版社, pages: 83 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN118637564A (en) * | 2024-08-15 | 2024-09-13 | 福建天甫电子材料有限公司 | Electronic grade sulfuric acid preparation equipment and preparation method thereof |
| CN118637564B (en) * | 2024-08-15 | 2024-10-22 | 福建天甫电子材料有限公司 | Electronic grade sulfuric acid preparation equipment and preparation method thereof |
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Application publication date: 20220412 |