CN113213434A - Dry absorption conversion system for refined sulfuric acid - Google Patents
Dry absorption conversion system for refined sulfuric acid Download PDFInfo
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- CN113213434A CN113213434A CN202110456537.9A CN202110456537A CN113213434A CN 113213434 A CN113213434 A CN 113213434A CN 202110456537 A CN202110456537 A CN 202110456537A CN 113213434 A CN113213434 A CN 113213434A
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- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 148
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 75
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 69
- 239000007789 gas Substances 0.000 claims abstract description 45
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 25
- 239000003546 flue gas Substances 0.000 claims abstract description 25
- 238000001035 drying Methods 0.000 claims abstract description 23
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 13
- 230000023556 desulfurization Effects 0.000 claims abstract description 13
- 239000002253 acid Substances 0.000 claims description 68
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 51
- 238000001816 cooling Methods 0.000 claims description 12
- 239000006260 foam Substances 0.000 claims description 9
- 229910021642 ultra pure water Inorganic materials 0.000 claims description 8
- 239000012498 ultrapure water Substances 0.000 claims description 8
- 238000007872 degassing Methods 0.000 claims description 6
- 238000007664 blowing Methods 0.000 claims description 4
- 238000010790 dilution Methods 0.000 claims description 4
- 239000012895 dilution Substances 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 4
- 239000002131 composite material Substances 0.000 claims description 3
- 238000007670 refining Methods 0.000 claims description 3
- 230000003584 silencer Effects 0.000 claims description 2
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 abstract description 28
- 238000000034 method Methods 0.000 abstract description 18
- 229910001868 water Inorganic materials 0.000 abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 9
- 230000008569 process Effects 0.000 abstract description 5
- 238000000746 purification Methods 0.000 abstract description 5
- 238000005507 spraying Methods 0.000 abstract description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 13
- 238000004519 manufacturing process Methods 0.000 description 12
- 238000004821 distillation Methods 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- PVNIIMVLHYAWGP-UHFFFAOYSA-N Niacin Chemical compound OC(=O)C1=CC=CN=C1 PVNIIMVLHYAWGP-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- VTVVPPOHYJJIJR-UHFFFAOYSA-N carbon dioxide;hydrate Chemical compound O.O=C=O VTVVPPOHYJJIJR-UHFFFAOYSA-N 0.000 description 2
- 230000008602 contraction Effects 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 229960003512 nicotinic acid Drugs 0.000 description 2
- 235000001968 nicotinic acid Nutrition 0.000 description 2
- 239000011664 nicotinic acid Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 235000011149 sulphuric acid Nutrition 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000030279 gene silencing Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- HIFJUMGIHIZEPX-UHFFFAOYSA-N sulfuric acid;sulfur trioxide Chemical compound O=S(=O)=O.OS(O)(=O)=O HIFJUMGIHIZEPX-UHFFFAOYSA-N 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
- C01B17/76—Preparation by contact processes
- C01B17/80—Apparatus
- C01B17/806—Absorbers; Heat exchangers
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a dry absorption conversion system of refined sulfuric acid, which comprises a dry absorption section and a conversion section, wherein one-to-one absorption process is adopted, SO2 gas after deep purification enters a refined sulfuric acid drying tower, 93-98% sulfuric acid is used for spraying and absorbing water in flue gas to reduce the water content in the flue gas to be below 0.1g/m, the flue gas is delivered to the conversion section by an S02 fan after demisting and defoaming by a demister, the flue gas is filtered by a precision filter after four-stage conversion and then enters the refined sulfuric acid absorption tower, and sulfur trioxide is sprayed and absorbed by 98% sulfuric acid and then enters a desulfurization system, SO that the purpose of preparing the refined sulfuric acid is achieved, and the total conversion rate can reach more than 96.0%.
Description
Technical Field
The invention relates to the technical field of inorganic chemical manufacturing, in particular to a dry absorption conversion system for refined sulfuric acid.
Background
At present, the quality standard of the domestic reagent sulfuric acid executes GB/T625-2007 chemical reagent sulfuric acid, and the production method mainly comprises a distillation method and an absorption method. The distillation method for preparing reagent sulfuric acid by acid cleaning purification-absorption method generally adopts w (H2SO4) 98% industrial sulfuric acid as raw material, and is a post-treatment physical purification process of industrial sulfuric acid after pretreatment and heating distillation purification in a quartz glass device. The heat source used in the distillation method is mainly electric energy, and coal gas are also used. The distillation method has the greatest defect of high energy consumption, and according to the statistics of production practices for many years, the electricity consumption of 400-600 kWh for producing one ton of reagent sulfuric acid is high. In addition, other factors also limit the reduction of production cost. For example, a single device has small processing capacity, the capacity is about 200kg/d, and the yield can be increased only by multiple parallel production, so that the operation and safe production management of the device are not facilitated; the wall of the quartz glass is easy to scale, and the quartz glass needs to be cleaned regularly by hydrofluoric acid, so that equipment corrosion is caused and the production cost is increased.
In order to overcome the defects of the distillation method and reduce the production cost, the production process of the reagent sulfuric acid by the absorption method is produced along with the improvement of the manufacturing technology of materials and equipment. The absorption process uses pure SO3 gas as raw material, w (H2SO4) 98% reagent sulfuric acid as circulating absorbent, and desalted water is added into the system to balance the acid concentration. The production of reagent sulfuric acid by absorption method is characterized by that it uses the control of raw material, auxiliary material and impurity intake in the course of production as main means, and adopts the accurate process control to make the product purity reach the set goal and directly produce reagent sulfuric acid, i.e. the combination reaction of SO3 and H2O.
The clean absorption of SO3 can be divided into two categories: one is that SO3 gas is filtered and purified by a dust removal filter and then directly absorbed by a reagent acid absorption tower (hereinafter referred to as a filtering, purifying and absorbing method), and desalted water is added into the system to balance the acid concentration; the filtering, purifying and absorbing method has the advantages of low cost, and the cost of the produced reagent sulfuric acid product is basically equal to that of the industrial sulfuric acid, but the filtered furnace gas still contains a certain amount of impurities, and the produced reagent sulfuric acid can only reach the GB/T625-2007 chemical purity specification. The other is that fuming sulfuric acid is prepared by absorption, then nicotinic acid is heated to separate out pure SO3 for absorption by a reagent acid absorption tower (hereinafter referred to as nicotinic acid evaporation absorption method), and desalted water is added into the system to balance the acid concentration; the purity of the reagent sulfuric acid produced by the fuming acid evaporation absorption method can reach the GB/T625-2007 analytical purity specification, but the process of distilling the fuming acid to remove the SO3 is still high in energy consumption, and the cost advantage is not obvious.
Accordingly, the prior art is yet to be improved and developed.
Disclosure of Invention
In view of the above-mentioned disadvantages of the prior art, the present invention aims to provide a dry absorption conversion system for highly efficient and highly pure purified sulfuric acid.
In order to solve the technical problems, the invention adopts the following technical scheme:
a dry absorption conversion system for refining sulfuric acid comprises a dry absorption section and a conversion section, wherein the dry absorption section comprises the following steps:
the first step is as follows: the heat of dilution generated by drying the acid, absorbing the heat of reaction generated by the acid, and removing the heat by means of respective acid coolers;
the second step is that: respectively feeding the dry acid and the absorption acid into respective circulating tanks, and controlling the concentration of the circulating acid by mutually crossing the acid and adding ultrapure water;
the third step: producing finished acid to maintain the balance between the concentration of each circulating acid and the liquid level of the circulating tank;
the fourth step: a drying and absorption circulation system; returning acid of the drying and absorbing tower to respective circulating tanks, maintaining stable sulfuric acid concentration through acid mixing and ultrapure water adding, then entering respective circulating pumps and acid coolers of the drying and absorbing tower, cooling and then entering the tower for recycling;
the fifth step: SO2 blowing off
The SO 2-containing gas discharged from the degassing tower and the sulfuric acid tail gas are sent to a desulfurization system;
the conversion section adopts four-section primary conversion, SO2 flue gas from an S02 fan sequentially passes through the tube spaces of heat exchangers IV, III, II and I to exchange heat with high-temperature S03 gas coming out of the first section, the second section, the third section and the fourth section of the converter, the converted gas after heat exchange is converted through a first layer, a second layer, a third layer and a fourth layer, the temperature of the converted gas after heat exchange is reduced to 180 ℃ through a cooler, and then the converted gas enters a precision filter and an absorption tower, and 98% sulfuric acid is used for absorbing the S03; and after the foam of the gas discharged from the absorption tower is removed by the foam remover, the gas is sent to a desulfurization system for tail gas treatment.
The dry absorption conversion system for the refined sulfuric acid is characterized in that a heating electric furnace for heating and preheating the conversion system is arranged at an inlet of one layer of the converter.
The dry absorption conversion system for the refined sulfuric acid is characterized in that the cooling mode of the surplus heat after the conversion section is air cooling.
The dry absorption conversion system for the refined sulfuric acid is characterized in that a secondary line and a valve are further arranged on the converter.
The dry absorption conversion system for the refined sulfuric acid is characterized in that an outlet of the S02 fan is provided with an S02 concentration analyzer.
The dry absorption conversion system for the refined sulfuric acid is characterized in that a temperature-rising circulating air pipe is arranged at the inlet of the fan.
The dry absorption conversion system for the refined sulfuric acid is characterized in that a silencer is arranged at the inlet of the fan.
The dry absorption conversion system for the refined sulfuric acid is characterized in that the sulfur dioxide fan room is provided with an SO2 leakage alarm device.
The dry absorption conversion system for the refined sulfuric acid is characterized in that the conversion fan and the cooling fan are both provided with variable frequency speed regulators.
In the dry absorption conversion system for the refined sulfuric acid, a heat exchanger of the conversion section is a composite flow large-hole plate contraction and expansion pipe high-efficiency heat exchanger.
Compared with the prior art, the invention has the advantages that:
1. the purpose of preparing refined sulfuric acid is achieved, and the total conversion rate can reach over 96.0 percent;
2. the tail gas is sent to a desulfurization system, and no waste residue, waste water and waste gas are discharged.
Drawings
FIG. 1 is a flow chart of a dry absorption conversion system for refined sulfuric acid according to the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
It will be understood that when an element is referred to as being "on," "secured to" or "disposed on" another element, it can be directly on the other element or intervening elements may also be present. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or intervening elements may also be present.
It should be noted that the terms of orientation such as left, right, up and down in the embodiments of the present invention are only relative to each other or are referred to the normal use state of the product, and should not be considered as limiting.
The embodiment of the invention provides a dry absorption conversion system for refining sulfuric acid, which comprises a dry absorption section and a conversion section, and the dry absorption section comprises the following steps:
the first step is as follows: the heat of dilution generated by drying the acid, absorbing the heat of reaction generated by the acid, and removing the heat by means of respective acid coolers;
the second step is that: respectively feeding the dry acid and the absorption acid into respective circulating tanks, and controlling the concentration of the circulating acid by mutually crossing the acid and adding ultrapure water;
the third step: producing finished acid to maintain the balance between the concentration of each circulating acid and the liquid level of the circulating tank;
the fourth step: a drying and absorption circulation system; returning acid of the drying and absorbing tower to respective circulating tanks, maintaining stable sulfuric acid concentration through acid mixing and ultrapure water adding, then entering respective circulating pumps and acid coolers of the drying and absorbing tower, cooling and then entering the tower for recycling;
the fifth step: SO2 blowing off
The SO 2-containing gas discharged from the degassing tower and the sulfuric acid tail gas are sent to a desulfurization system;
the conversion section adopts four-section primary conversion, SO2 flue gas from an S02 fan sequentially passes through the tube spaces of heat exchangers IV, III, II and I to exchange heat with high-temperature S03 gas coming out of the first section, the second section, the third section and the fourth section of the converter, the converted gas after heat exchange is converted through a first layer, a second layer, a third layer and a fourth layer, the temperature of the converted gas after heat exchange is reduced to 180 ℃ through a cooler, and then the converted gas enters a precision filter and an absorption tower, and 98% sulfuric acid is used for absorbing the S03; and after the foam of the gas discharged from the absorption tower is removed by the foam remover, the gas is sent to a desulfurization system for tail gas treatment.
In the embodiment of the invention, a dry absorption conversion system adopts a one-to-one absorption process, SO2 gas after deep purification enters a refined sulfuric acid drying tower, 93-98% sulfuric acid is used for spraying and absorbing water in flue gas, SO that the water in the flue gas is reduced to be below 0.1g/m, and after demisting and defoaming are carried out by a demister, the flue gas is sent to a conversion section by an S02 fan.
Specifically, the flue gas is converted in four stages, filtered by a precision filter, enters a refined sulfuric acid absorption tower, and sprayed by 98% sulfuric acid to absorb sulfur trioxide, and then enters a desulfurization system.
More specifically, the heat of dilution generated by drying the acid absorbs the heat of reaction generated by the acid, and the heat is removed by the respective acid coolers. The dry acid and the absorption acid respectively enter into respective circulating grooves, and the concentration of the circulating acid is controlled by mutually crossing the acid and adding ultrapure water. And producing finished acid to maintain the balance between the concentration of each circulating acid and the liquid level of the circulating tank.
In the invention, the circulation acid flow adopts: tower-tank-pump-acid cooler-tower (i.e. post-pump cooling flow).
Further, a drying and absorption cycle system; returning acid of the drying and absorbing tower to respective circulating tanks, maintaining stable sulfuric acid concentration through acid mixing and ultrapure water adding, then entering respective circulating pumps and acid coolers of the drying and absorbing tower, cooling and then entering the tower for recycling; and demisting the absorbed tail gas and then feeding the tail gas into a desulfurization system.
Further, the fifth step: s02 blowing:
the product acid is 95-98% sulfuric acid. The refined AR-grade sulfuric acid with qualified iron content is led out from a bypass pipe at the outlet of a circulating acid pump, enters the upper section of a degassing tower, is subjected to primary S02 removal, enters the lower section of the degassing tower, is subjected to S02 gas removal together with the refined acid fed by the circulating pump of a reaction tank, is added with a certain amount of oxidant as required to further remove reducing substances, is cooled, and is fed into a finished product storage tank.
The S02-containing gas discharged from the degassing tower and the sulfuric acid tail gas are sent to a desulfurization system.
And conveying the product acid which does not reach the AR level to an underground tank for industrial acid treatment, pumping the product acid from the underground tank to an industrial acid finished product storage tank, and conveying the product acid to a loading elevated tank by a conveying pump when the finished acid is sold out, and then loading and transporting the product acid outside the truck.
Specifically, the amount of the converted flue gas entering the outlet of the drying tower is as follows:
TABLE 3-22 amount of flue gas introduced into the outlet of the drying tower
| Composition of flue gas | SO2 | SO3 | N2 | CO2 | H2O | O2 | Total up to |
| Nm3/h | 1392 | 0 | 8378 | 4972 | 0 | 1570 | 16312 |
| ％ | 8.53 | 0 | 51.36 | 30.48 | 0 | 9.62 | 100 |
Further, the conversion section adopts four-section primary conversion, SO2 flue gas from an SO2 fan sequentially passes through the tube spaces of heat exchangers IV, III, II and I to exchange heat with high-temperature S03 gas coming out of the first section, the second section, the third section and the fourth section of the converter, the conversion is carried out through a first layer, a second layer, a third layer and a fourth layer, the converted gas after heat exchange is cooled to 180 ℃ through a cooler and then enters a precision filter and an absorption tower, and 98% sulfuric acid is used for absorbing the S03; and after the foam of the gas discharged from the absorption tower is removed by the foam remover, the gas is sent to a desulfurization system for tail gas treatment.
Specifically, the total conversion rate of the application can reach more than 96.0%.
Furthermore, a temperature-raising electric furnace is arranged at an inlet of one layer of the converter and is used for raising the temperature and preheating the conversion system.
Furthermore, the surplus heat in the conversion section is cooled by air.
When the system is started, the converter must be heated in advance, a heating electric furnace is arranged at the first section of the converter, and the electric heating furnace is used for heating dry air and heating and preheating the conversion system. The conversion section is provided with the necessary secondary lines and valves for regulating the reaction temperature in the various layers of the converter.
An outlet of the S02 fan is provided with an S02 concentration analyzer, and the concentration of S02 is controlled by purified flue gas distribution. An electric butterfly valve is arranged at the purified flue gas distribution position to automatically distribute the amount of flue gas entering sulfuric acid and desulfurizing; one section of the converter (the other three sections of auxiliary line butterfly valves are manually adjusted) is a DCS system automatic control operation.
Furthermore, 4-20 mA signals of all protection and interlocking devices of the S02 fan enter the DCS system for automatic control operation.
The inlet of the fan is provided with a temperature-rising circulating air pipe, so that mother acid for driving can be greatly saved during temperature rising, and the heat utilization rate is improved. When the circulating air pipe is in low-gas concentration in the smelting furnace, the sulfuric acid drying system maintains low-load self-circulation, and the safe operation of the whole system is ensured.
Furthermore, the heat exchanger of the conversion working section adopts a composite flow large-hole plate contraction and expansion pipe high-efficiency heat exchanger.
And the sulfur dioxide fan room is provided with an SO2 leakage alarm device.
The fan inlet is provided with a silencing device, and necessary secondary line pipes and valves are arranged among the heat exchangers in the conversion working section in order to adjust the reaction temperature of each layer of the converter.
Furthermore, the conversion fan needs to be provided with a variable-frequency speed regulator, and the cooling fan needs to be provided with a variable-frequency speed regulator.
Specifically, the flue gas desulfurized after absorption in the present application is as follows:
TABLE 3-23 amount of flue gas introduced into the outlet of the drying tower
| Composition of flue gas | SO2 | SO3 | N2 | CO2 | H2O | O2 | Total up to |
| Nm3/h | 56 | 0 | 8378 | 4972 | 0 | 902 | 14308 |
| ％ | 0.39 | 0 | 58.55 | 34.75 | 0 | 6.30 | 100 |
In conclusion, the invention discloses a dry absorption conversion system of refined sulfuric acid, which comprises a dry absorption section and a conversion section, wherein a one-to-one absorption process is adopted, S02 gas subjected to deep purification enters a refined sulfuric acid drying tower, 93-98% sulfuric acid is sprayed to absorb water in flue gas, so that the water in the flue gas is reduced to be below 0.1g/m, demisting and foam removal are carried out by a demister, the flue gas is sent to the conversion section by an S02 fan, the flue gas is filtered by a precision filter after four stages of conversion, then enters a refined sulfuric acid absorption tower, and enters a desulfurization system after 98% sulfuric acid is sprayed to absorb sulfur trioxide, so that the purpose of preparing the refined sulfuric acid is achieved, and the total conversion rate can reach more than 96.0%.
While the present invention has been described with reference to the embodiments shown in the drawings, the present invention is not limited to the embodiments, which are illustrative and not restrictive, and it will be apparent to those skilled in the art that various changes and modifications can be made therein without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (10)
1. A dry absorption conversion system for refining sulfuric acid is characterized by comprising a dry absorption section and a conversion section, wherein the dry absorption section comprises the following steps:
the first step is as follows: the heat of dilution generated by drying the acid, absorbing the heat of reaction generated by the acid, and removing the heat by means of respective acid coolers;
the second step is that: respectively feeding the dry acid and the absorption acid into respective circulating tanks, and controlling the concentration of the circulating acid by mutually crossing the acid and adding ultrapure water;
the third step: producing finished acid to maintain the balance between the concentration of each circulating acid and the liquid level of the circulating tank;
the fourth step: a drying and absorption circulation system; returning acid of the drying and absorbing tower to respective circulating tanks, maintaining stable sulfuric acid concentration through acid mixing and ultrapure water adding, then entering respective circulating pumps and acid coolers of the drying and absorbing tower, cooling and then entering the tower for recycling;
the fifth step: SO2 blowing off
The SO 2-containing gas discharged from the degassing tower and the sulfuric acid tail gas are sent to a desulfurization system;
the conversion section adopts four-section primary conversion, SO2 flue gas from an S02 fan sequentially passes through the tube spaces of heat exchangers IV, III, II and I to exchange heat with high-temperature S03 gas coming out of the first section, the second section, the third section and the fourth section of the converter, the converted gas after heat exchange is converted through a first layer, a second layer, a third layer and a fourth layer, the temperature of the converted gas after heat exchange is reduced to 180 ℃ through a cooler, and then the converted gas enters a precision filter and an absorption tower, and 98% sulfuric acid is used for absorbing the S03; and after the foam of the gas discharged from the absorption tower is removed by the foam remover, the gas is sent to a desulfurization system for tail gas treatment.
2. The dry absorption conversion system for refined sulfuric acid as claimed in claim 1, wherein a temperature-raising electric furnace for raising the temperature and preheating the conversion system is provided at an inlet of one layer of said converter.
3. The dry absorption conversion system for refined sulfuric acid as claimed in claim 1, wherein the cooling means of the surplus heat after said conversion section is air cooling.
4. The dry-suction conversion system for refined sulfuric acid according to claim 1 or 2, characterized in that a secondary line and a valve are further provided on the converter.
5. The dry suction conversion system for refined sulfuric acid as claimed in claim 1, wherein the S02 blower outlet is provided with an S02 concentration analyzer.
6. The dry absorption conversion system for refined sulfuric acid as claimed in claim 1, wherein said blower inlet is provided with a temperature-raising circulating air pipe.
7. The dry suction conversion system for refined sulfuric acid as claimed in claim 1, wherein said fan inlet is provided with a silencer.
8. The dry absorption conversion system for refined sulfuric acid as claimed in claim 1, wherein said sulfur dioxide blower room is provided with an SO2 leak alarm device.
9. The dry absorption conversion system for refined sulfuric acid as claimed in claim 1, wherein said conversion blower and said cooling blower are each provided with a variable frequency speed regulator.
10. The dry absorption conversion system for refined sulfuric acid according to claim 1, wherein the heat exchanger of the conversion section is a composite flow large-orifice plate converging-diverging tube high-efficiency heat exchanger.
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| CN211521596U (en) * | 2020-01-19 | 2020-09-18 | 长沙华时捷环保科技发展股份有限公司 | System for preparing analytically pure sulfuric acid from smelting flue gas |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN211521596U (en) * | 2020-01-19 | 2020-09-18 | 长沙华时捷环保科技发展股份有限公司 | System for preparing analytically pure sulfuric acid from smelting flue gas |
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