CN212559465U - Wet process sulfuric acid producing apparatus with high hydrocarbon content acid gas - Google Patents
Wet process sulfuric acid producing apparatus with high hydrocarbon content acid gas Download PDFInfo
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Abstract
A device for preparing sulfuric acid by high-hydrocarbon-content acid gas wet method comprises an incinerator, a heat exchange unit, a conversion reactor, an acid condenser and a washing unit which are sequentially connected through a process gas pipeline, wherein the incinerator is provided with a gas inlet pipe which is simultaneously communicated with the hydrocarbon-content acid gas pipeline and a combustion-supporting gas pipeline, a gas outlet pipe of the incinerator is divided into two paths after passing through the heat exchange unit, and one path is divided into two pathsIs connected to the conversion reactor, and the other path is connected to the combustion-supporting gas pipeline to form circulation. The utility model discloses a SO that will produce in the incinerator2The part of the gas after heat exchange and temperature reduction by the heat exchange unit returns to the incinerator, thereby avoiding the rapid increase of the generation rate of nitrogen oxide caused by overhigh temperature in the incinerator when the air inlet amount is low or the SO in the process gas caused by increasing the air inlet amount to control the temperature in the incinerator2The content is too low and the exhaust emission is increased.
Description
Technical Field
The utility model relates to a device for preparing sulfuric acid, in particular to a device for preparing sulfuric acid by a wet method by using high-hydrocarbon-content acid gas.
Background
The prewashed flash steam and dimethyl ether Claus gas in coal chemical industry enterprises contain hydrocarbon substances with about 5 to 30 mol percent and H with 10 to 50 mol percent2S, the hydrocarbon composition has higher contents of C5 and C6. When the sulfur recovery process is used for treatment, because the incinerator is in anoxic combustion, the hydrocarbon is insufficiently combusted, carbon particles generated by hydrocarbon combustion can block a catalyst bed layer, and meanwhile, the carbon particles can be brought into a sulfur product, so that the quality of the sulfur product is unqualified. In the general wet-process sulfuric acid production process, because the hydrocarbon content is high, a large amount of air needs to be supplemented for controlling the temperature of an incinerator, SO is caused in the process gas2The molar content is lower and is below 2 percent. Because of the addition of a large amount of air, the process gas flow after the incinerator is increased, the sizes of a subsequent conversion reactor, a condenser and tail gas treatment equipment are increased, the manufacturing cost of the device is increased, and the operation cost is increased. The increase of the process gas amount also leads to the increase of the exhaust emission, the heat taken away by the exhaust is increased, the steam production of the device is reduced, the benefit of the device is influenced, and the increase of the exhausted exhaust also leads to the emission of SO2And the total amount of sulfuric acid mist is increased. If the supplement of the dilution air is reduced, the temperature of the incinerator is increased, so that the generation rate of nitrogen oxides is increased rapidly.
For example, the utility model patent with the application number of CN201920128663.X, entitled "wet sulfuric acid process system for producing concentrated sulfuric acid by secondary pressurization", the invention patent application with the application number of CN201911413284.6, entitled "method for producing sulfuric acid", and the invention patent application with the application number of CN201911346398.3, entitled "apparatus and method for preparing sulfuric acid by cracking and regenerating waste sulfuric acid and/or sulfur-containing waste liquid" all produce sulfuric acid by burning, converting and absorbing firstly, but do not solve the problem of overhigh temperature in the incinerator.
Foreign patent technologists inject SiO-containing gas into the process gas through an acid mist control unit2The particle of (2) increases the condensation effect of sulfuric acid, and the acid mist control unit is expensive and is limited by foreign technical monopoly.
Therefore, a new process capable of increasing the concentration of sulfur dioxide in the process gas, reducing the equipment investment and simultaneously not causing the increase of the furnace temperature to cause the discharge of nitrogen oxides to be not up to the standard is needed.
SUMMERY OF THE UTILITY MODEL
The utility model discloses to the device that makes sulphuric acid at present the too high or sulfur dioxide concentration problem that crosses low of stove internal temperature when utilizing high hydrocarbon-containing acid gas to prepare sulphuric acid, provided a high hydrocarbon-containing acid gas wet process sulphuric acid device, can reduce the interpolation of dilution air, SO improves among the process gas2The process gas amount and the size of treatment equipment are reduced so as to achieve the aim of reducing the engineering investment.
The utility model discloses a solve the technical means that above-mentioned problem adopted and do: the utility model provides a high sour wet legal system sulphuric acid device that contains hydrocarbon, includes the burning furnace, heat exchange unit, conversion reactor, acid condenser and the washing unit that connect gradually through the technology gas pipeline, burns the burning furnace and is equipped with the intake pipe, and its intake pipe simultaneously with contain hydrocarbon sour gas pipeline and combustion-supporting gas pipeline intercommunication, and burns the outlet duct of burning furnace and divide into two the tunnel behind the heat exchange unit, be connected to conversion reactor, another way and be connected to combustion-supporting gas pipeline and form the circulation.
Furthermore, an air mixing unit is arranged on the combustion-supporting gas pipeline, and the combustion-supporting gas and the SO are arranged2The gas is mixed into mixed gas through the air mixing unit.
Furthermore, the heat exchange unit comprises a waste heat boiler and a steam superheater which are communicated through a process gas pipeline, the waste heat boiler and the steam superheater are respectively communicated with the steam drum through heat exchange pipelines, and the heat exchange pipeline connected with the steam superheater passes through the conversion reactor.
Furthermore, the conversion reactor comprises a first catalyst bed layer, a second catalyst bed layer and a third catalyst bed layer which are communicated, a process gas pipeline inlet of the conversion reactor is arranged at the first catalyst bed layer, a first-stage intercooler is arranged between the first catalyst bed layer and the second catalyst bed layer, a second-stage intercooler is arranged between the second catalyst bed layer and the third catalyst bed layer, and a process gas cooler is arranged between the third catalyst bed layer and the process gas pipeline outlet of the conversion reactor.
Furthermore, the inlet and outlet of the process gas cooler are communicated with the steam drum through heat exchange pipelines, the inlet end of the second-stage intercooler is connected with the steam drum through the heat exchange pipelines, the outlet end of the second-stage intercooler is connected with the inlet end of the first-stage intercooler through the heat exchange pipelines, and the outlet end of the first-stage intercooler is a high-temperature steam outlet.
Further, ceramic acid-resistant filler and a cyclone demister are arranged in the acid condenser, wherein the ceramic acid-resistant filler is arranged at an inlet of the process gas pipeline, the cyclone demister is arranged at an outlet of the process gas pipeline, and a sulfuric acid outlet is arranged below the acid condenser.
Further, the cone angle of the cyclone demister is 1.5 o -20o。
Furthermore, a sulfuric acid outlet of the acid condenser is connected to a concentrated acid circulating unit, the concentrated acid circulating unit comprises a concentrated acid circulating tank, a concentrated acid circulating pump and a concentrated acid cooler, an outlet pipeline of the concentrated acid cooler is divided into two paths, one path of the outlet pipeline returns to the acid circulating tank to form circulation, and the other path of the outlet pipeline outputs finished sulfuric acid for the concentrated acid outlet.
Furthermore, the heat exchange unit also comprises a water supply preheater, a cooling air fan is connected at a heat exchange gas inlet of the acid condenser, an outlet is communicated with the water supply preheater through a heat exchange pipeline, and the steam drum is also communicated with the water supply preheater through a heat exchange pipeline.
Furthermore, the washing unit comprises a quenching washing tower and an electrostatic demister which are communicated, an inlet of the quenching washing tower is communicated with an outlet of the acid condenser through a process gas pipeline, and an outlet of the electrostatic demister is a tail gas outlet.
Furthermore, the quenching washing tower is divided into a quenching section and a washing section, a sulfuric acid outlet is arranged below the quenching section, a sulfuric acid outlet pipeline is divided into three paths, one path returns to the quenching section to form circulation, the other path returns to the washing section to form circulation, and the other path outputs finished sulfuric acid.
Furthermore, the quenching washing tower is also provided with a softened water inlet which is respectively communicated with the quenching section and the washing section, and the washing section is also provided with a hydrogen peroxide inlet.
Furthermore, a wire mesh demister is arranged at a position close to the electrostatic demister in the quenching washing tower.
The utility model has the advantages that:
1. the utility model discloses a SO that will produce in the incinerator2The part of the gas after heat exchange and temperature reduction by the heat exchange unit returns to the incinerator, thereby avoiding the rapid increase of the generation rate of nitrogen oxide caused by overhigh temperature in the incinerator when the air inlet amount is low or the SO in the process gas caused by increasing the air inlet amount to control the temperature in the incinerator2The content is too low and the exhaust emission is increased.
2. The utility model discloses a set up the whirl defroster in sour condenser, utilize the centrifugal action of whirl defroster to the liquid drop for liquid drop in the gas can be separated and finally flow out from sour condenser bottom, avoids the sulphuric acid gathering on the defroster that evaporates.
Drawings
FIG. 1 is a schematic structural view of an embodiment;
in the figure: 1. the system comprises an incinerator 11, hydrocarbon-containing acid gas, a heat exchange unit 2, a waste heat boiler 21, a waste heat boiler 22, a steam superheater 23, a steam drum 24, a feed water preheater 3, an air mixing unit 31, a combustion-supporting gas fan 32, an air preheater 33, a sulfur dioxide fan 34, mixed gas, a conversion reactor 4, a first catalyst bed 41, a first inter-stage cooler 42, a first inter-stage cooler 43, a second catalyst bed 44, a second inter-stage cooler 45, a third catalyst bed 46, a process cooler 5, an acid condenser 51, a cyclone demister 52, ceramic acid-resistant filler 53, a cooling air fan 53, a washing unit 6, a quenching washing tower 7, a quenching washing tower 71, random or regular filler 72, a wire mesh demister 73, a spiral nozzle 74, a washing liquid circulating pump 75, softened water 76, hydrogen peroxide, 8, an electrostatic demister, 81. the system comprises a clean air fan, a chimney 82, a concentrated sulfuric acid circulating unit 9, an acid circulating tank 91, an acid circulating pump 92 and an acid cooler 93.
Detailed Description
The present invention will be further explained with reference to the accompanying drawings.
Example one
As shown in figure 1, the wet process sulfuric acid producing apparatus with high hydrocarbon content acid gas has hydrocarbon content in acid gas 11 of 5-30 mol%, H2The mol content of S is 10-50%, the wet-process sulfuric acid preparation device from the inlet of the hydrocarbon-containing acid gas 11 sequentially comprises a process gas pipeline communicated with: the process gas containing sulfur trioxide enters the acid condenser 5, the sulfur trioxide forms sulfuric acid in the acid condenser 5 and flows out from an outlet, the unreacted process gas enters the washing unit 6 to continue to react and then is discharged as tail gas, and the sulfur is converted into liquid sulfuric acid and flows out.
The heat exchange unit 2 comprises a waste heat boiler 21 and a steam superheater 22 which are sequentially communicated, the process gas is firstly cooled by the lung heat boiler 21 after coming out of the incinerator 1, and the temperature of the process gas after being cooled for the first time is reduced to 440-oC, then carrying out secondary temperature reduction through the steam superheater 22, and cooling the process gas after the secondary temperature reduction to 410-430-oC。
An air mixing unit 3 is arranged between the steam superheater 22 and the incinerator 1, and the air mixing unit 3 comprises a combustion-supporting air fan 31, an air preheater 32 and a sulfur dioxide fan 33. The process gas pipeline after the second temperature reduction by the steam superheater 22 is divided into two paths, one path is communicated to the subsequent conversion reactor 4, and the other path enters the air mixing unit 3. The air inlet of the incinerator 1 is simultaneously connected with the hydrocarbon-containing acidThe gas inlet pipe of the gas 11 is connected with the gas outlet of the air mixing unit 3, the hydrocarbon-containing acid gas is cooled twice after being combusted in the incinerator 1, part of the cooled process gas enters the air mixing unit 3 and is mixed with combustion-supporting cold air and then enters the incinerator again, and the temperature in the incinerator 1 is controlled to be 950-1000-oAnd C, the input amount of oxygen-containing cold air in the incinerator 1 is reduced through the circulation of the process gas, so that the content of sulfur dioxide in the process gas is improved, and the problem of overhigh temperature in the incinerator 1 when the input amount of the cold air in a non-circulating structure is low is solved.
The cold air passes through the air preheater 32 after being boosted by the combustion-supporting air fan 31, part of the process gas after being cooled for the second time also passes through the air preheater 32 along the process gas pipeline, the cold air and the process gas exchange heat at the air preheater 32, the process gas and the process gas are mixed to form mixed gas 34 after the temperature of the process gas is reduced and the temperature of the cold air is increased, and SO in the mixed gas 342The molar content of the organic silicon compound is 2 to 6 percent, and the temperature is controlled to be 220 ℃ CoAnd C, arranging a sulfur dioxide fan 33 on a process air pipeline before or after the process gas passes through the air preheater 32 to ensure that the process gas smoothly moves forward, wherein in the embodiment, the sulfur dioxide fan 33 is arranged on the process air pipeline after the process gas passes through the air preheater 32. The cold air and the process gas are subjected to heat exchange and then mixed, the temperature difference between the cold air and the process gas is reduced firstly, sulfuric acid dew point corrosion caused by sudden cooling of the high-temperature process gas during direct mixing is avoided, meanwhile, the cold air and the process gas with the closer temperature can be mixed more uniformly, and when the formed mixed gas 34 and the hydrocarbon-containing acid gas 11 enter the incinerator 1 together, the distribution of oxygen in the gas is more uniform, so that the hydrocarbon-containing acid gas 11 can be fully combusted.
The heat exchange unit 2 further comprises a steam drum 23, the steam drum 23 is connected with the waste heat boiler 21 and the steam superheater 22 through heat exchange pipelines, and the heat exchange pipelines between the steam drum 23 and the waste heat boiler 21 form a circulating connection.
The conversion reactor 4 adopts a three-stage catalytic reaction structure and sequentially comprises a first catalyst bed layer 41, a first-stage intercooler 42, a second catalyst bed layer 43 and a second-stage cooler according to the flow direction of the process gasA cooler 44, a third catalyst bed 45 and a process cooler 46. The process gas after the two heat exchanges enters the conversion reactor 4 along the process gas pipeline, the sulfur dioxide gas in the process gas is converted into sulfur trioxide through a plurality of catalytic reactions, heat exchange is carried out after each conversion reaction, and the inlet temperature of the first catalyst bed layer 42 is 405-420- oC, the inlet temperature of the second catalyst bed is 400-440- oC, the inlet temperature of the third catalyst bed layer is 390- oC, avoiding the over-high temperature of the process gas, and finally cooling to 280-300 ℃ by the process gas cooler 46 oC then flows out into the subsequent acid condenser 5.
The first inter-stage cooler 42, the second inter-stage cooler 44 and the process cooler 46 are connected with the steam pocket through heat exchange pipelines for heat exchange, the heat exchange pipelines between the steam pocket 23 and the process cooler 46 form a circulating connection, another heat exchange pipeline passes through the steam superheater 33 after coming out of the steam pocket 23, enters the second inter-stage cooler 44 after heat exchange and temperature rise, enters the first inter-stage cooler 42 after heat exchange and temperature rise again, and forms high-temperature steam after heat exchange and temperature rise. The process gas in the conversion reactor 4 is gradually cooled through multiple heat exchange, SO that the influence of the overhigh temperature of the process gas on SO is avoided2The depth of conversion of (a).
After the process gas rich in sulfur trioxide enters the acid condenser 5, the temperature at the top of the acid condenser is 85-100 DEG oC, SO due to temperature decrease3And H2O hydration produces gaseous sulfuric acid, and then cooling forms liquid sulfuric acid, is provided with a section of ceramic acid-resistant filler 52 at the bottom of acid condenser 5, provides the mass and heat transfer space of hot process gas and sulfuric acid, can improve the mass fraction of the condensed sulfuric acid from 97% to 98.5%. A plurality of cyclone demisters 51 are arranged at the top of the acid condenser 5, sulfuric acid droplets with small particle size which cannot drop are separated from the process gas by the cyclone demisters 51 and then fall onto the top plate of the acid condenser 5, and flow into the bottom of the acid condenser 5 under the action of gravity, and the cone angle of the cyclone demisters 51 is 1.5 o -20oAnd the removal efficiency of 3um droplets of sulfuric acid mist in the process gas passing through the cyclone demister 51 is more than 95%, and the pressure drop is lower than 3 KPa. The acid condenser 5 has a sulfuric acid outlet at the bottom, and the liquid formed in the acid condenser 5The state concentrated sulfuric acid flows out along a sulfuric acid outlet and enters a concentrated sulfuric acid circulating unit 9, and the residual process gas enters a subsequent washing unit 6.
The acid condenser 5 is also connected with a cooling air fan 53, and air in the environment enters the acid condenser 5 after being boosted by the cooling air fan 53 to provide a low condensation temperature for sulfuric acid in the acid condenser 5.
The heat exchange unit 2 further comprises a water supply preheater 24, ambient air after heat exchange is carried out in the acid condenser 5 is connected to the water supply preheater 24 through a pipeline and then is discharged to the air, the water supply preheater 24 is connected with the steam pocket 23 through a heat exchange pipeline, the other end of the heat exchange pipeline, which is located at the water supply preheater 24, is an inlet of deoxygenated water 25, the external deoxygenated water 25 and the ambient temperature after heat exchange in the acid condenser 5 are subjected to heat exchange in the water supply preheater 24 and then enter the steam pocket 23.
The concentrated sulfuric acid circulating unit 9 comprises a concentrated acid circulating tank 91, a concentrated acid circulating pump 92 and a concentrated acid cooler 93, an outlet pipeline of the concentrated acid cooler 93 is divided into two paths, one path is returned to the concentrated acid circulating tank 91 to form circulation, the other path is a concentrated acid outlet, the hot concentrated sulfuric acid flowing out from the acid condenser 5 enters the concentrated sulfuric acid circulating unit 9 to be cooled, part of the hot concentrated sulfuric acid flows out as finished sulfuric acid, and the other part of the hot concentrated sulfuric acid returns to the concentrated acid circulating tank 91 to form circulation to cool the hot sulfuric acid flowing out from the acid condenser 5. The concentrated sulfuric acid is driven to move forward by the concentrated sulfuric acid circulating pump 92, and the concentrated sulfuric acid cooler 93 is further provided with a water cooling pipeline for exchanging heat with the concentrated sulfuric acid through cold water.
The washing unit 6 comprises a quenching washing tower 7 and an electrostatic demister 8 which are communicated from bottom to top, the lower section of the quenching washing tower 7 is a quenching section, the upper section of the quenching section is a washing section, spiral nozzles 73 are arranged above the quenching section and the washing section, a random or structured packing 71 is arranged in the washing section, the bottom of the quenching section is a sulfuric acid outlet, a pipeline of the sulfuric acid outlet is divided into three paths, one path of the sulfuric acid outlet is connected to the spiral nozzles 73 of the quenching section to form circulation, the other path of the sulfuric acid outlet is connected to the spiral nozzles 73 of the washing section to form circulation, the other path of the sulfuric acid outlet is a finished sulfuric acid outlet, the pipeline of the outlet can extend to the finished sulfuric acid outlet of the concentrated sulfuric acid, the concentrated sulfuric acid is diluted and then outputs sulfuric acid with one concentration, and. And the spiral nozzles 73 of the quenching section and the washing section are connected with softened water 75 pipelines, the spiral nozzles 73 of the washing section are also connected with hydrogen peroxide 76 pipelines, and a washing liquid circulating pump 74 is also arranged on a sulfuric acid outlet pipeline. The process gas from the acid condenser 5 enters the quenching section of the quenching washing tower 7, the dilute sulfuric acid mixed with the softened water 75 is circulated and returned to the spiral nozzle 73 above the quenching section, at the moment, the process gas is in countercurrent contact with the dilute sulfuric acid, the process gas is rapidly cooled through the evaporation of water in the dilute sulfuric acid, the dilute sulfuric acid liquid flows out from the bottom of the quenching section, the process gas rises to the washing section, the contact area of the reaction between sulfur dioxide in the process gas and hydrogen peroxide is enlarged by random or structured packing 71 in the washing section, the rapid removal of the sulfur dioxide is facilitated, the residual sulfur dioxide in the process gas and the hydrogen peroxide sprayed from the spiral nozzle 73 above the washing section are rapidly reacted to generate sulfuric acid, and the desulfurization of the process gas is realized.
A wire mesh demister 72 is arranged in the quenching washing tower 7 and close to the electrostatic demister 8, and a small amount of sulfuric acid mist droplets carried in the reacted gas are effectively removed through the wire mesh demister 72 and the electrostatic demister 8 in sequence to obtain clean gas.
The air outlet of the electrostatic demister 8 is connected with a clean air blower 81, and clean air is discharged after being sent into a chimney 82 through the clean air blower 81.
The above embodiments are provided only for the purpose of illustration, not for the limitation of the present invention, and those skilled in the relevant art can make various changes or modifications without departing from the spirit and scope of the present invention, so all equivalent technical solutions should also belong to the protection scope of the present invention, and the protection scope of the present invention should be defined by the claims.
Claims (10)
1. A device for preparing sulfuric acid by a wet method with high-hydrocarbon-content acid gas is characterized in that: comprises an incinerator, a heat exchange unit, a conversion reactor, an acid condenser and a washing unit which are sequentially connected through a process gas pipeline, wherein the incinerator is provided with a gas inlet pipe which is simultaneously communicated with a hydrocarbon-containing acid gas pipeline and a combustion-supporting gas pipeline, and the incineratorThe gas outlet pipe is divided into two paths after passing through the heat exchange unit, one path is connected to the conversion reactor, and the other path is connected to the combustion-supporting gas pipeline to form circulation; the combustion-supporting gas pipeline is provided with an air mixing unit, combustion-supporting gas and SO2The gas is mixed into mixed gas through the air mixing unit.
2. The apparatus for preparing sulfuric acid by wet process of high hydrocarbon-containing acid gas according to claim 1, wherein: the heat exchange unit comprises a waste heat boiler and a steam superheater which are communicated through a process gas pipeline, the waste heat boiler and the steam superheater are respectively communicated with the steam drum through heat exchange pipelines, and the heat exchange pipeline connected with the steam superheater passes through the conversion reactor.
3. The apparatus for preparing sulfuric acid by wet process of high hydrocarbon-containing acid gas according to claim 2, wherein: the conversion reactor comprises a first catalyst bed layer, a second catalyst bed layer and a third catalyst bed layer which are communicated, a process gas pipeline inlet of the conversion reactor is arranged at the first catalyst bed layer, a first-stage intercooler is arranged between the first catalyst bed layer and the second catalyst bed layer, a second-stage intercooler is arranged between the second catalyst bed layer and the third catalyst bed layer, and a process gas cooler is arranged between the third catalyst bed layer and the process gas pipeline outlet of the conversion reactor;
the inlet and outlet of the process gas cooler are communicated with the steam drum through heat exchange pipelines, the inlet end of the second inter-stage cooler is connected with the steam drum through the heat exchange pipelines, the outlet end of the second inter-stage cooler is connected with the inlet end of the first inter-stage cooler through the heat exchange pipelines, and the outlet end of the first inter-stage cooler is a high-temperature steam outlet.
4. The apparatus for preparing sulfuric acid by wet process of high hydrocarbon-containing acid gas according to claim 3, wherein: the acid condenser is internally provided with ceramic acid-resistant filler and a cyclone demister, wherein the ceramic acid-resistant filler is arranged at the inlet of the process gas pipeline, the cyclone demister is arranged at the outlet of the process gas pipeline, and the cone angle of the cyclone demister is 1.5 o -20oAnd a sulfuric acid outlet is arranged below the acid condenser.
5. The apparatus for preparing sulfuric acid by wet process of high hydrocarbon-containing acid gas according to claim 4, wherein: the sulfuric acid outlet of the acid condenser is connected to a concentrated acid circulating unit, the concentrated acid circulating unit comprises a concentrated acid circulating tank, a concentrated acid circulating pump and a concentrated acid cooler, the outlet pipeline of the concentrated acid cooler is divided into two paths, one path of the outlet pipeline returns to the acid circulating tank to form circulation, and the other path of the outlet pipeline outputs finished sulfuric acid for the concentrated acid outlet.
6. The apparatus for preparing sulfuric acid by wet process of high hydrocarbon-containing acid gas according to claim 4, wherein: the heat exchange unit also comprises a water supply preheater, a cooling air fan is connected at the heat exchange gas inlet of the acid condenser, the outlet is communicated with the water supply preheater through a heat exchange pipeline, and the steam drum is also communicated with the water supply preheater through a heat exchange pipeline.
7. The apparatus for preparing sulfuric acid by wet process of high hydrocarbon-containing acid gas according to claim 1, wherein: the washing unit comprises a quenching washing tower and an electrostatic demister which are communicated, an inlet of the quenching washing tower is communicated with an outlet of the acid condenser through a process gas pipeline, and an outlet of the electrostatic demister is a tail gas outlet.
8. The apparatus for preparing sulfuric acid by wet process of high hydrocarbon-containing acid gas according to claim 7, wherein: the quenching washing tower is divided into a quenching section and a washing section, a sulfuric acid outlet is arranged below the quenching section, a sulfuric acid outlet pipeline is divided into three paths, one path returns to the quenching section to form circulation, the other path returns to the washing section to form circulation, and the other path outputs finished sulfuric acid.
9. The apparatus for preparing sulfuric acid by wet process of high hydrocarbon-containing acid gas according to claim 8, wherein: the quenching washing tower is also provided with a softened water inlet which is respectively communicated with the quenching section and the washing section, and the washing section is also provided with a hydrogen peroxide inlet.
10. The apparatus for preparing sulfuric acid by wet process of high hydrocarbon-containing acid gas according to claim 7, wherein: and a wire mesh demister is also arranged at the position close to the electrostatic demister in the quenching washing tower.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111689477A (en) * | 2020-07-21 | 2020-09-22 | 株洲宏大高分子材料有限公司 | Wet process and apparatus for preparing sulfuric acid from high-hydrocarbon-content acidic gas |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111689477A (en) * | 2020-07-21 | 2020-09-22 | 株洲宏大高分子材料有限公司 | Wet process and apparatus for preparing sulfuric acid from high-hydrocarbon-content acidic gas |
| CN111689477B (en) * | 2020-07-21 | 2024-04-26 | 株洲宏大高分子材料有限公司 | Wet process and apparatus for preparing sulfuric acid from acid gas with high hydrocarbon content |
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