CN214270225U - Conversion tower is used in low energy consumption sulphuric acid production - Google Patents
Conversion tower is used in low energy consumption sulphuric acid production Download PDFInfo
- Publication number
- CN214270225U CN214270225U CN202022265974.6U CN202022265974U CN214270225U CN 214270225 U CN214270225 U CN 214270225U CN 202022265974 U CN202022265974 U CN 202022265974U CN 214270225 U CN214270225 U CN 214270225U
- Authority
- CN
- China
- Prior art keywords
- heat exchange
- conversion
- conversion tower
- energy consumption
- low energy
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model provides a low energy consumption conversion tower for sulfuric acid production, which comprises a conversion tower body, a molten salt evaporator and a molten salt pump; 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 utility model provides a low energy consumption is conversion tower for sulfuric acid production simple structure, management are convenient, and all conversion reactions and heat transmission all can be accomplished in the conversion tower, need not like current conversion tower, must draw when the gas temperature rises to 550 ℃ in the reaction process and introduce the conversion tower again after getting into the heat exchanger cooling and continue the reaction, have saved a lot of air flow conveying pipeline and transport power.
Description
Technical Field
The utility model provides a low energy consumption conversion tower for sulfuric acid production belongs to the chemical industry equipment field.
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 of (a) is an exothermic reaction (the exotherm Q is:at 25 ℃ per 1mol 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 gas3And after being heated again, the residual gas is converted for the second time through a later catalyst layer and then enters an 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.
SUMMERY OF THE UTILITY MODEL
The technical problem is as follows: in order to solve the defects of the prior art, the utility model provides a low-energy-consumption conversion tower for sulfuric acid production.
The technical scheme is as follows: the utility model provides a low energy consumption conversion tower for sulfuric acid production, which comprises a conversion tower body, a molten salt evaporator and a molten salt pump; 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 body and the conversion reaction zone.
Has the advantages that: the utility model provides a low energy consumption is conversion tower for sulfuric acid production simple structure, management are convenient, and all conversion reactions and heat transmission all can be accomplished in the conversion tower, need not like current conversion tower must draw forth when the gas temperature rises to 550 ℃ in the reaction process and get into the heat exchanger.
Drawings
FIG. 1 is a schematic structural diagram of a conversion tower for low-energy consumption sulfuric acid production.
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 will be further explained below.
The low-energy-consumption conversion tower for producing the sulfuric acid is shown in the 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 middle upright post 19, wherein the middle upright post 19 is arranged in the conversion tower body 1 and is used for supporting the conversion tower body 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 represent some embodiments of the present invention, and the description thereof is specific and detailed, but not to be construed as limiting the scope of the present invention. It should be noted that, for those skilled in the art, without departing from the spirit of the present invention, several variations and modifications can be made, which are within the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the appended claims.
Claims (10)
1. A low energy consumption conversion tower for sulfuric acid production 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.
2. The conversion tower for producing sulfuric acid with low energy consumption as claimed in claim 1, wherein: 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.
3. The conversion tower for producing sulfuric acid with low energy consumption as claimed in claim 1, wherein: 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).
4. The conversion tower for producing sulfuric acid with low energy consumption as claimed in claim 1, wherein: 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).
5. The conversion tower for producing sulfuric acid with low energy consumption as claimed in claim 1, wherein: 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).
6. The conversion tower for producing sulfuric acid with low energy consumption as claimed in claim 5, wherein: 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.
7. The conversion tower for producing sulfuric acid with low energy consumption as claimed in claim 1, wherein: 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).
8. The conversion tower for sulfuric acid production with low energy consumption according to claim 7, wherein: 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.
9. The conversion tower for sulfuric acid production with low energy consumption according to claim 7, wherein: 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.
10. The conversion tower for producing sulfuric acid with low energy consumption as claimed in claim 1, wherein: the conversion tower further 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 body (1) and the conversion reaction zone (11).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022265974.6U CN214270225U (en) | 2020-10-12 | 2020-10-12 | Conversion tower is used in low energy consumption sulphuric acid production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022265974.6U CN214270225U (en) | 2020-10-12 | 2020-10-12 | Conversion tower is used in low energy consumption sulphuric acid production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214270225U true CN214270225U (en) | 2021-09-24 |
Family
ID=77806169
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022265974.6U Active CN214270225U (en) | 2020-10-12 | 2020-10-12 | Conversion tower is used in low energy consumption sulphuric acid production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214270225U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114348973A (en) * | 2020-10-12 | 2022-04-15 | 南京华电节能环保股份有限公司 | Sulfuric acid process conversion tower adopting contact method |
-
2020
- 2020-10-12 CN CN202022265974.6U patent/CN214270225U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114348973A (en) * | 2020-10-12 | 2022-04-15 | 南京华电节能环保股份有限公司 | Sulfuric acid process conversion tower adopting contact method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2016119224A1 (en) | Isothermal and low temperature shift converter and shift conversion process thereof | |
| EP3199231A1 (en) | Large reactor and device and process thereof | |
| CN101254442B (en) | Use of gas-solid catalytic reactor in preparing methanol | |
| CN102850183B (en) | Methanol synthesis system and method | |
| CN107224940B (en) | A kind of methanator and methanation process | |
| CN103240036B (en) | A kind of heat transfer reactor of Anti-temperature difference stress and combinations thereof device and application | |
| CN214270225U (en) | Conversion tower is used in low energy consumption sulphuric acid production | |
| CN213493610U (en) | Low-energy-consumption multistage conversion tower for sulfuric acid production | |
| CN108114672A (en) | A kind of soaking type spiral plate fixed bed reactors of gas solid catalytic reaction | |
| CN109382045A (en) | A kind of spiral plate fixed bed reactors of gas-solid contact catalysis reaction | |
| CN105883852B (en) | A kind of ammonia synthesis reaction system and ammonia synthesis reaction method | |
| CN101279227B (en) | Membrane type wall reactor | |
| CN202808648U (en) | Methanol synthetic system | |
| CN114348973A (en) | Sulfuric acid process conversion tower adopting contact method | |
| CN105413592B (en) | A kind of combined type fixed bed reactors and the device formed by it | |
| CN114307868A (en) | Multistage conversion tower for sulfuric acid process by contact method | |
| CN207169658U (en) | Efficient HPPO device reaction devices | |
| CN107159062B (en) | Reactor | |
| CN205965795U (en) | Many beds hang down resistance catalytic converter | |
| CN2280087Y (en) | Reactor for conversion sulfur oxides by use of heat pipe heat-exchange | |
| CN201161185Y (en) | Double-layer heat exchange plate-type reactor in parallel | |
| CN102133512A (en) | Reactor applied to gas-phase exothermic reaction | |
| CN208990778U (en) | The filling structure of shell and tube reactor catalyst | |
| CN201200885Y (en) | Membrane type wall-shell type reactor | |
| CN208075622U (en) | A kind of heat-exchange device for reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |