CN114348973A - Sulfuric acid process conversion tower adopting contact method - Google Patents
Sulfuric acid process conversion tower adopting contact method Download PDFInfo
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- CN114348973A CN114348973A CN202011085598.0A CN202011085598A CN114348973A CN 114348973 A CN114348973 A CN 114348973A CN 202011085598 A CN202011085598 A CN 202011085598A CN 114348973 A CN114348973 A CN 114348973A
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Abstract
The invention provides a conversion tower for a sulfuric acid process by a contact method, which comprises a conversion tower body, a molten salt evaporator and a molten salt pump, wherein the molten salt evaporator is arranged on the conversion tower body; a plurality of conversion reaction zones and 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 conversion reaction zone; a heat exchange pipeline is arranged in the fused salt 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 fused salt evaporator; the heat exchange tube of the conversion tower body, the heat exchange pipeline of the molten salt evaporator and the molten salt pump are connected into a ring. The conversion tower of the sulfuric acid process by the contact method has a simple structure, is convenient to manage, can finish all conversion reactions and heat transmission in the conversion tower, does not need to be led out to enter a heat exchanger for cooling and then to be led into the conversion tower for continuous reaction when the temperature of gas rises to 550 ℃ in the reaction process like the existing conversion tower, and saves a plurality of gas flow conveying pipelines and conveying power.
Description
Technical Field
The invention provides a sulfuric acid process conversion tower adopting 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 sulfuric acid process by the contact method, whether the sulfuric acid is prepared by pyrite or sulfur, or prepared by smelting 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 gas is heated again, the residual gas is converted for the second time through the following catalyst layer 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 conversion tower for a sulfuric acid process by a contact method.
The technical scheme is as follows: the invention provides a conversion tower for a sulfuric acid process by a contact method, which comprises a conversion tower body, a molten salt evaporator and a molten salt pump, wherein the molten salt evaporator is arranged on the conversion tower body; a plurality of conversion reaction zones and 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 conversion reaction zone; a heat exchange pipeline is arranged in the fused salt 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 fused salt evaporator; the heat exchange tube of the conversion tower body, the heat exchange pipeline of the molten salt evaporator and the molten salt pump are connected into a ring.
As an improvement, fused salt is filled in an annular pipeline formed by a heat exchange pipe of the conversion tower body, a heat exchange pipeline of the fused salt evaporator and a fused salt pump to serve 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 fused salt evaporator in parallel, the temperature detector is arranged at the outlet end of the fused salt pump, and the temperature detector sends a temperature signal to the control valve.
As another improvement, the side wall of the cavity of the molten salt 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 system also comprises an inlet header and an outlet header, wherein all heat exchange tubes in the conversion reaction zone are connected with the molten salt pump through the inlet header and are connected with the heat exchange pipeline of the molten salt 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 conversion reaction zone, and each heat exchange layer consists 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 expansion surfaces of the fins are square.
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 and the conversion reaction zone.
Has the advantages that: the conversion tower of the sulfuric acid process by the contact method has simple structure and convenient management, all conversion reactions and heat transmission can be completed in the conversion tower, and the gas temperature is not required to be led out to enter a heat exchanger when the gas temperature rises to 550 ℃ in the reaction process of the existing conversion tower.
Drawings
FIG. 1 is a schematic structural diagram of a conversion tower of a sulfuric acid process by a contact method.
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.
The conversion tower for the sulfuric acid process by the contact method is shown in figures 1 to 4 and comprises a conversion tower body 1, a molten salt evaporator 2, a molten salt pump 3, a control valve 4 and a temperature detector 5.
A plurality of conversion reaction zones 11 and buffer zones 12 filled with catalysts 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 conversion reaction zone 11; the system also comprises an inlet header 17 and an outlet header 18, wherein all heat exchange tubes 15 in the conversion reaction zone 11 are connected with the molten salt pump 3 through the inlet header 17 and connected with a heat exchange pipeline 21 of the molten salt 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; an outlet header 18 is connected to the outlet end of each heat exchange tube 15 through a balancer 10; the balancer 10 is a throttle orifice, and functions to balance the flow rate of the heating medium. 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 and the conversion reaction zone 11.
The heat exchange tubes 15 form a plurality of heat exchange layers in the conversion reaction zone 11, 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 expansion surfaces of the fins are square.
A heat exchange pipeline 21 is arranged in the fused salt 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 fused salt evaporator 2; the side wall of the cavity of the fused salt 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 molten salt evaporator 2 and the molten salt pump 3 are connected into a ring; fused salt 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 fused salt evaporator 2 and the fused salt pump 3 to serve as a heat exchange medium.
The control valve 4 is connected with the fused salt evaporator 2 in parallel, the temperature detector 5 is arranged at the outlet end of the fused salt 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 molten salt in the heat exchange tube 15, so that the temperature of the conversion reaction zone 11 of the conversion tower body 1 is ensured to be basically constant; the endothermic molten salt exchanges heat with media such as water in the molten salt evaporator 2, and then enters the conversion reaction zone 11 again to absorb heat.
The heat exchange tubes with square fins are buried in the catalyst of each layer, and can transfer away the generated heat in the reaction process in time, so as to ensure that the reaction gas and the production gas in the catalyst layer and the layer are at the same equal temperature, and realize isothermal conversion. Because the temperature of the catalyst during the conversion reaction must be higher than 370 ℃ and lower than 650 ℃, and the proper working temperature of the molten salt is more than 250 ℃ and less than t and less than 500 ℃, the molten salt is selected as a heat exchange carrier and flows through the heat exchange tubes.
The heat exchange tubes at each height can be set into a plurality of groups of snakelike tube bundles which are adaptive to the torus, the inner side curvature radius is smaller, the outer side curvature radius is larger, the space between the square fins is ensured not to clamp catalyst particles, and the fins of the adjacent finned tubes (between the left and the right and between the upper and the lower) are preferably lapped to ensure that the temperature in the catalyst is uniform without local overheating. The value of small temperature difference of the inlet and the outlet of the fused salt in each layer of heat exchange pipe in the conversion tower can be set so as to ensure that the temperature in the whole catalyst layer is uniform and equal.
The heat exchange tubes can also be grouped, for example, the reaction temperature of each layer can be adjusted according to the gas concentration requirement.
The buffer layer is an automatic diffusion adjustment area inside the conversion reaction gas, and concentration balance is met.
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 a person skilled in the art, several variations and modifications can be made without departing from the inventive concept, which falls within the scope of the present invention. Therefore, the protection scope of the present patent shall be subject to the appended claims.
Claims (9)
1. A sulfuric acid process conversion tower by a contact method is characterized in that: comprises a conversion tower body (1), a molten salt evaporator (2) and a molten salt pump (3); a plurality of conversion reaction zones (11) and buffer zones (12) filled with catalysts are arranged in the conversion tower body (1) in a staggered manner from bottom to top, 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 conversion reaction zone (11); a heat exchange pipeline (21) is arranged in the fused salt 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 fused salt evaporator (2); the heat exchange tube (15) of the conversion tower body (1), the heat exchange pipeline (21) of the molten salt evaporator (2) and the molten salt pump (3) are connected into a ring; fused salt 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 fused salt evaporator (2) and the fused salt pump (3) to serve as a heat exchange medium.
2. The conversion tower of 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 molten salt evaporator (2) in parallel, the temperature detector (5) is arranged at the outlet end of the molten salt pump (3), and the temperature detector (5) sends a temperature signal to the control valve (4).
3. The conversion tower of the contact sulfuric acid process according to claim 2, characterized in that: the side wall of the cavity of the fused salt 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 conversion tower of the contact sulfuric acid process according to claim 1, characterized in that: the system also comprises an inlet header (17) and an outlet header (18), wherein all heat exchange tubes (15) in the conversion reaction zone (11) are connected with the molten salt pump (3) through the inlet header (17) and are connected with a heat exchange pipeline (21) of the molten salt evaporator (2) through the outlet header (18).
5. The conversion tower of 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 conversion tower of 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 conversion reaction zone (11), and each heat exchange layer is composed of more than one heat exchange tube (15).
7. The conversion tower of 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 conversion tower of 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 expansion surfaces of the fins are square.
9. The conversion tower of the contact sulfuric acid process according to claim 1, characterized in that: the device also comprises a center pillar (19), wherein the center pillar (19) is arranged in the conversion tower body (1) and is used for supporting the conversion tower (1) and the conversion reaction zone (11).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202011085598.0A CN114348973A (en) | 2020-10-12 | 2020-10-12 | Sulfuric acid process conversion tower adopting contact method |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202011085598.0A CN114348973A (en) | 2020-10-12 | 2020-10-12 | Sulfuric acid process conversion tower adopting contact method |
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| CN114348973A true CN114348973A (en) | 2022-04-15 |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101698470A (en) * | 2009-11-05 | 2010-04-28 | 四川大学 | Method and device for preparing sulfuric acid |
| CN104236132A (en) * | 2014-10-13 | 2014-12-24 | 南京工业大学 | Medium-high temperature solar energy storage device based on efficient heat storage and release unit |
| CN105605956A (en) * | 2016-02-26 | 2016-05-25 | 北京工业大学 | High-temperature air and fused salt efficient heat storage system |
| CN106225043A (en) * | 2016-07-20 | 2016-12-14 | 国网北京市电力公司 | Heat pump and heating system |
| CN206754644U (en) * | 2017-05-19 | 2017-12-15 | 青海盐湖工业股份有限公司 | Fused salt feeding line and potassium hydroxide production system |
| CN108584991A (en) * | 2018-05-04 | 2018-09-28 | 中国成达工程有限公司 | A kind of low chlorine photo-thermal fused salt production technology and process units |
| CN214270225U (en) * | 2020-10-12 | 2021-09-24 | 南京华电节能环保股份有限公司 | Conversion tower is used in low energy consumption sulphuric acid production |
-
2020
- 2020-10-12 CN CN202011085598.0A patent/CN114348973A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101698470A (en) * | 2009-11-05 | 2010-04-28 | 四川大学 | Method and device for preparing sulfuric acid |
| CN104236132A (en) * | 2014-10-13 | 2014-12-24 | 南京工业大学 | Medium-high temperature solar energy storage device based on efficient heat storage and release unit |
| CN105605956A (en) * | 2016-02-26 | 2016-05-25 | 北京工业大学 | High-temperature air and fused salt efficient heat storage system |
| CN106225043A (en) * | 2016-07-20 | 2016-12-14 | 国网北京市电力公司 | Heat pump and heating system |
| CN206754644U (en) * | 2017-05-19 | 2017-12-15 | 青海盐湖工业股份有限公司 | Fused salt feeding line and potassium hydroxide production system |
| CN108584991A (en) * | 2018-05-04 | 2018-09-28 | 中国成达工程有限公司 | A kind of low chlorine photo-thermal fused salt production technology and process units |
| CN214270225U (en) * | 2020-10-12 | 2021-09-24 | 南京华电节能环保股份有限公司 | Conversion tower is used in low energy consumption sulphuric acid production |
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