CN109264674B - Process and system for preparing sulfuric acid by using smelting flue gas - Google Patents
Process and system for preparing sulfuric acid by using smelting flue gas Download PDFInfo
- Publication number
- CN109264674B CN109264674B CN201811509697.XA CN201811509697A CN109264674B CN 109264674 B CN109264674 B CN 109264674B CN 201811509697 A CN201811509697 A CN 201811509697A CN 109264674 B CN109264674 B CN 109264674B
- Authority
- CN
- China
- Prior art keywords
- acid
- flue gas
- refined
- circulating
- sulfuric acid
- 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
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
-
- 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
- C01B17/48—Sulfur dioxide; Sulfurous acid
- C01B17/50—Preparation of sulfur dioxide
- C01B17/56—Separation; Purification
-
- 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
-
- 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
- C01B17/90—Separation; Purification
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to a process and a system for preparing sulfuric acid by using smelting flue gas. The process uses sulfur dioxide-containing flue gas of a smelting plant as a raw material, converts sulfur dioxide into sulfur trioxide after purification, deep cooling impurity removal and drying, and then prepares refined sulfuric acid by an absorption method after filtering and washing the flue gas. The invention can maximize the yield of the refined sulfuric acid produced by the sulfur dioxide-containing flue gas of a smelting plant. Meanwhile, the invention enriches the sulfuric acid products of the smelting plant, can flexibly adjust the specification and the quality of the product sulfuric acid to meet the market demand, improves the economic benefit of enterprises, and is suitable for the reconstruction of newly built sulfuric acid devices and old sulfuric acid devices.
Description
Technical Field
The invention relates to a process and a system for preparing sulfuric acid by using smelting flue gas, belonging to the technical field of chemical industry.
Background
There are two main industrial processes for refining sulfuric acid, one is industrial distillation of sulfuric acid and the other is absorption of gaseous sulfur trioxide. The industrial sulfuric acid distillation method adopts an electric heating type sulfuric acid quartz glass purification device to prepare refined sulfuric acid through atmospheric or reduced pressure distillation. The production process can prepare high-purity refined sulfuric acid, but has the defects of high energy consumption, poor safety performance and small production scale. The method for absorbing gaseous sulfur trioxide is characterized by that it utilizes a series of measures to prepare pure sulfur trioxide gas, and uses refined sulfuric acid to absorb sulfur trioxide gas in a refined acid absorption tower so as to produce refined sulfuric acid. The production process can be stably operated in a large scale, has lower production cost and stable and reliable product quality, and has better economic benefit.
In the process of preparing refined sulfuric acid by using smelting flue gas as a raw material, heavy metals such as arsenic, cadmium, mercury and the like and other impurities are contained in the smelting flue gas to different degrees due to the influence of impurities of the smelting raw material and process conditions. These impurities seriously affect the quality of the produced sulfuric acid, reducing the economic value of the product sulfuric acid. Currently, with the development of economy, especially the development of the electronic industry, the demand of refined sulfuric acid such as sulfuric acid for storage batteries, electronic-grade sulfuric acid and the like is increasing, and the market of the refined sulfuric acid is very promising.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide a process and a system for preparing sulfuric acid by using smelting flue gas, so as to maximize the output of refined sulfuric acid and improve the benefit.
In order to solve the technical problems, the technical scheme of the invention is as follows:
a process for preparing sulfuric acid by using smelting flue gas comprises the following steps:
s1, washing and purifying the smelting flue gas containing sulfur dioxide to obtain first flue gas;
s2, carrying out cryogenic impurity removal treatment on the first flue gas obtained in the S1; removing acid mist in the first flue gas to obtain acid mist with content not higher than 5mg/m3The second flue gas of (2);
s3, drying the second flue gas obtained in the S2 by using concentrated sulfuric acid with the concentration of 93-95wt% to obtain the flue gas with the water content of not more than 0.1g/Nm3(water content under standard conditions) of a third flue gas;
s4, converting sulfur dioxide in the third flue gas obtained in the S3 into sulfur trioxide, and obtaining a fourth flue gas containing sulfur trioxide;
s5, filtering and removing impurities from the fourth flue gas obtained in the S4, and washing and removing impurities from the fourth flue gas by using nicotinic acid as a washing medium to obtain a fifth flue gas;
s6, taking the fifth flue gas obtained in the step S5 as a raw material, and preparing sulfuric acid by a contact method to obtain refined acid and residual gas;
and S7, sequentially carrying out demisting, secondary conversion, acid absorption and tail gas absorption treatment on the residual gas, and then discharging the gas after reaching the standard.
In the present invention, the nicotinic acid is oleum, i.e. concentrated sulfuric acid containing free sulfur trioxide.
The method comprises the steps of firstly washing and purifying the smelting flue gas, primarily removing impurities, and then carrying out cryogenic impurity removal on the smelting flue gas. In the deep cooling process, the temperature of the flue gas is reduced, the contained water vapor and heavy metal impurities loaded by the gas phase are removed, then acid mist and water are further removed, and the flue gas is dried by concentrated sulfuric acid and then sent to a conversion unit. Under catalytic conversion conditions, sulfur dioxide is converted to sulfur trioxide. After the flue gas is subjected to the purification treatment, the cleanliness is high, the flue gas does not have adverse effects on a catalyst contacted with the flue gas during a conversion reaction period, catalyst poisoning does not need to be worried about, good conversion effect and conversion rate are favorably obtained, and the service life of the catalyst is prolonged; the obtained flue gas containing sulfur trioxide is further filtered and washed, and then refined acid is prepared by a contact method. In the process, the medium used for drying treatment is concentrated sulfuric acid, and the concentrated sulfuric acid can be put into use again after being cooled after primary drying treatment is completed; and the washing and impurity removal of the fourth flue gas mainly uses nicotinic acid as a washing medium, and impurities in the flue gas can be adsorbed. In addition, after the nicotinic acid is subjected to primary washing impurity removal treatment, the nicotinic acid can be cooled and then put into the washing impurity removal process again, and redundant nicotinic acid can be sent into a nicotinic acid intermediate acid production tank to be further prepared into industrial-grade sulfuric acid, so that the types of sulfuric acid products are enriched.
Further, during cryogenic impurity removal treatment, the first flue gas and the circulating liquid flow in opposite directions and contact with each other, heat exchange is carried out, and cooling is achieved. Optionally, the circulating liquid is sprayed from top to bottom, and the first flue gas is introduced from the bottom of the device, so that the first flue gas exchanges heat with the circulating liquid in the ascending process, and the cooling is realized.
Further, in S2, when the first flue gas obtained in S1 is subjected to cryogenic impurity removal treatment, the temperature of the first flue gas is reduced to 2-7 ℃.
Further, in S3, the concentrated sulfuric acid is cooled and used again for drying.
Further, in S5, the nicotinic acid is cooled and then used again for washing to remove impurities. Furthermore, the redundant nicotinic acid can be diluted to prepare an industrial-grade sulfuric acid product.
Further, after S6, the method further comprises a step of desorbing the refined acid, namely, hot air after filtering, oil removal, water removal and heating is introduced into the refined acid to remove sulfur dioxide, so as to obtain a refined product acid; preferably, in the desorption step, an oxidizing agent is added to the purified acid to remove the reduced matter.
A system for preparing sulfuric acid by utilizing smelting flue gas comprises a first purification unit, a cryogenic impurity removal unit, a drying unit, a first conversion unit, a second purification unit, a first absorption unit, a second conversion unit, a second absorption unit and a tail gas absorption unit which are sequentially communicated; the deep cooling impurity removal unit comprises a deep cooling tower, a first demister, a first circulating pump and a first circulating liquid cooler which are sequentially communicated, and the deep cooling tower, the first circulating pump and the first circulating liquid cooler are sequentially communicated to form a circulating loop; the drying unit comprises a drying tower, a drying acid circulating tank, a second circulating pump and a second circulating liquid cooler which are sequentially communicated and form a circulating loop; the second purification unit comprises a flue gas filter, a nicotinic acid washing tower, a nicotinic acid circulating tank, a third circulating pump and a third circulating liquid cooler which are sequentially communicated, and the nicotinic acid washing tower, the nicotinic acid circulating tank, the third circulating pump and the third circulating liquid cooler are sequentially communicated to form a circulating loop.
And the smoke gas filter is communicated with the smoke gas filter.
Further, the first absorption unit comprises a refined acid absorption tower, a refined acid circulation tank, a fourth circulation pump and a fourth circulation liquid cooler, wherein the refined acid absorption tower, the refined acid circulation tank, the fourth circulation pump and the fourth circulation liquid cooler are sequentially communicated to form a circulation loop.
Further comprises a refined acid desorption tower communicated with a liquid outlet of the fourth circulating pump, and a liquid outlet of the refined acid desorption tower is communicated with a refined acid intermediate tank.
Optionally, an appropriate amount of an oxidizing agent is metered into the purified acid desorption column as needed to remove reducing impurities.
Further, the device also comprises a second demister, wherein the second demister is communicated between the first absorption unit and the second conversion unit.
Preferably, the pipelines and equipment in the first absorption unit, which are contacted with the acid or the acid gas, are all made by adopting a roller lining or a compact lining made of polytetrafluoroethylene materials or an equal-steel (isostatic) lining forming process.
Compared with the prior art, the invention has the following beneficial effects:
1. the invention can maximize the production of refined sulfuric acid from the smelting flue gas containing sulfur dioxide, thereby improving the economic benefit of enterprises;
2. the invention adopts a flue gas purification mode of deep cooling dehydration and heavy metal removal of flue gas, is simple and effective, and can ensure the maximization of the quality and the yield of the refined sulfuric acid. Meanwhile, the method is beneficial to reducing catalyst poisoning caused by heavy metals, ensuring the conversion rate of sulfur dioxide and prolonging the service life of the catalyst;
3. the present invention belongs to a direct contact method for producing refined sulfuric acid, and the process is reliable, the product quality is stable, and the production cost is low.
4. The invention has the advantages of simple process, short flow, small occupied area of the device, environmental protection, economy and energy saving.
5. The technical scheme of the invention can flexibly adjust the product structure according to the market condition, and is beneficial to improving the enterprise benefit. 6. The invention is suitable for newly-built sulfuric acid devices and the reconstruction of old sulfuric acid devices.
Drawings
FIG. 1 is a schematic configuration diagram of a sulfuric acid production plant using metallurgical off-gas according to a first embodiment of the present invention.
FIG. 2 is a schematic configuration diagram of a refined acid desorption module apparatus according to a first embodiment of the present invention.
Detailed Description
The present invention will be described in detail with reference to examples. It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict. For convenience of description, the words "upper", "lower", "left" and "right" in the following description are used only to indicate the correspondence between the upper, lower, left and right directions of the drawings themselves, and do not limit the structure.
Example 1
As shown in fig. 1 and 2, a system for preparing sulfuric acid by using smelting flue gas comprises a first purification unit, a cryogenic impurity removal unit, a drying unit, a first conversion unit 8, a second purification unit, a first absorption unit, a second conversion unit 13, a second absorption unit 14 and a tail gas absorption unit 15 which are sequentially communicated; the deep cooling impurity removal unit comprises a deep cooling tower 4 and a first demister 5 which are sequentially communicated, the first demister is a two-stage wet-type electric demister, and further comprises a first circulating liquid cooler 17 and a first circulating pump 16, and the deep cooling tower 4, the first circulating pump 16 and the first circulating liquid cooler 17 are sequentially communicated to form a circulating loop; the drying unit comprises a drying tower 6, a drying acid circulating tank 21, a second circulating pump 22 and a second circulating liquid cooler 23 which are sequentially communicated and form a circulating loop; the second purification unit comprises a flue gas filter 9 and a nicotinic acid washing tower 10 which are sequentially communicated, and further comprises a nicotinic acid circulating tank 27, a third circulating pump 28 and a third circulating liquid cooler 29, wherein the nicotinic acid washing tower 10, the nicotinic acid circulating tank 27, the third circulating pump 28 and the third circulating liquid cooler 29 are sequentially communicated to form a circulating loop.
The first purification unit comprises a one-stage dynamic wave purification device 1, a gas cooling device 2 and a two-stage dynamic wave purification device 3 which are sequentially communicated.
The cryogenic impurity removal unit further comprises a refrigerating fluid storage tank 18, a refrigerating fluid circulating pump 19 and a refrigerating unit 20 which are sequentially communicated, an inlet of the refrigerating fluid storage tank is communicated with the first circulating liquid cooler, and a liquid outlet of the refrigerating unit is communicated with the first circulating liquid cooler.
The second purification unit also comprises a nicotinic acid intermediate acid producing tank 24 communicated with a liquid outlet of a third circulating liquid cooler 29, an industrial-grade product acid delivery pump 25 and an industrial-grade product acid cooler 26. The nicotinic acid intermediate acid-producing tank 24, the industrial-grade product acid delivery pump 25 and the industrial-grade product acid cooler 26 are communicated in sequence to form a circulation loop. The nicotinic acid intermediate acid-producing groove 24 is communicated with the smoke filter 9. The outlet of the industrial-grade product acid cooler 26 may produce an industrial-grade product acid.
The first absorption unit comprises a refined acid absorption tower 11, a refined acid circulation tank 30, a fourth circulation pump 31 and a fourth circulation liquid cooler 32, wherein the refined acid absorption tower 11, the refined acid circulation tank 30, the fourth circulation pump 31 and the fourth circulation liquid cooler 32 are communicated in sequence to form a circulation loop. Optionally, ultrapure water is added to the purified acid circulation tank as needed to maintain the concentration of the purified acid in the circulation tank at 98.3% to secure the absorption effect of the purified acid absorption tower.
Further comprises a refined acid desorption tower 33 communicated with a liquid outlet of the fourth circulating pump 31, and a refined acid intermediate tank 34 is communicated with a liquid outlet of the refined acid desorption tower 33. The device also comprises an air filter 41, an air fan 40, an air dryer 39, an air degreaser 38 and an air heater 37 which are communicated in sequence, wherein the air outlet of the air heater is communicated with the refined acid desorption tower. The sulfur dioxide in the refined acid can be removed by clean hot air to the refined acid desorption tower, and the product purity is improved.
The device also comprises a refined finished product acid intermediate tank 34, a refined finished product acid delivery pump 35 and a refined finished product acid cooler 36 which are communicated in sequence, wherein a circulation loop is formed by the refined finished product acid intermediate tank and the refined finished product acid cooler, and the refined finished product acid intermediate tank is communicated with a liquid outlet of the refined acid desorption tower. Optionally, ultrapure water is added into the intermediate tank of the refined finished product acid according to requirements, so that the specification and quality of the product refined sulfuric acid can be flexibly adjusted.
The device also comprises a second demister 12, a second conversion unit 13, a second absorption unit 14 and a tail gas absorption unit 15 which are communicated in sequence. The second mist eliminator 12 is shown as a fiber mist eliminator.
A process for preparing refined sulfuric acid by using smelting flue gas comprises the following process flows: the smelting flue gas containing sulfur dioxide and with the temperature of about 220-330 ℃ enters a first purification unit, and the smoke dust and harmful substances in the flue gas are removed through a first-stage dynamic wave purification device 1, a gas cooling device 2 and a second-stage dynamic wave purification device 3 in sequence.
The smelting flue gas containing sulfur dioxide cooled to about 40 ℃ enters a flue gas deep cooling tower 4. Cooling the circulating liquid of the flue gas cryogenic tower to 3 ℃ by using the refrigerating liquid, pumping the circulating liquid into the top of the flue gas cryogenic tower for spraying, and discharging the flue gasAnd cooling the gas to 5 ℃ to condense and remove water and heavy metal impurities in the flue gas. Then the acid mist in the flue gas is removed by a two-stage electric demister (the acid mist content is less than or equal to 5 mg/m)3) And enters a drying tower 6.
And (3) the smelting flue gas containing sulfur dioxide is in countercurrent contact with sprayed 93-95% concentrated sulfuric acid in a drying tower, and the residual water in the flue gas is removed by utilizing the strong water absorption of the concentrated acid. Water content after drying is less than or equal to 0.1g/Nm3The flue gas is delivered to a first conversion unit 8 by a sulfur dioxide fan 7 for primary conversion after foam is captured by a stainless steel wire mesh foam catcher at the top of the drying tower.
The flue gas containing sulfur trioxide at the temperature of about 160-220 ℃ after the primary conversion is subjected to the flue gas filter 9 to remove acid mist, dust and other impurities carried in the flue gas, so that the pure flue gas containing sulfur trioxide is obtained. The filtered pure flue gas containing sulfur trioxide enters a nicotinic acid washing tower 10 for further washing and purification, the temperature is reduced to 75 ℃, and impurities in the flue gas are washed into nicotinic acid. The nicotinic acid is cooled to 70 ℃ by a third circulating pump 28 through a third circulating liquid cooler 29 and then returns to the nicotinic acid washing tower for circular washing.
Part of the nicotinic acid is sent to a nicotinic acid intermediate acid tank 24, and water is continuously added into the tank through an automatic control system to adjust the acid concentration of the industrial-grade product. The industrial grade product acid is cooled to 40 ℃ by an industrial grade product acid cooler 26 through an industrial grade product acid delivery pump 25, one part of the industrial grade product acid returns to a nicotinic acid intermediate acid producing tank to control the temperature of the product acid in the tank to be less than 90 ℃, and the other part of the industrial grade product acid is used as a product to produce industrial grade sulfuric acid.
The flue gas of high purity sulfur trioxide with the temperature of 75 ℃ below zero obtained after being purified by a flue gas filter 9 and a nicotinic acid washing tower 10 enters a refined acid absorption tower with a tetrafluoro lining. The sulfur trioxide in the flue gas is absorbed by the refined acid which is circularly sprayed from top to bottom in the tower. And the flue gas absorbed by the refined acid absorption tower is subjected to acid mist removal by a fiber demister and then enters a second conversion unit for secondary conversion.
The concentration of the refined acid is increased after the refined acid absorbs the sulfur trioxide in the flue gas, and the refined acid automatically flows into a refined acid circulating groove from the bottom of a refined acid absorbing tower. Ultrapure water is continuously added into the tank through an automatic control system to control the concentration of the refined acid to be 98.3 percent. And adjusting the concentration, pumping the solution to a fourth circulating liquid cooler by a fourth circulating pump, cooling the solution to 70 ℃, and returning the solution to the refined acid absorption tower for circularly absorbing sulfur trioxide.
And sending part of the refined acid to a refined acid desorption tower before the inlet of the fourth circulating liquid cooler. The sulfur dioxide contained in the high-temperature refined sulfuric acid in the tower is removed by introducing clean air which is filtered, deoiled, dewatered and heated into the refined acid desorption tower. The desorption flue gas generated in the refined acid desorption tower returns to the inlet of the drying tower through a pipeline. Meanwhile, a certain amount of oxidant is added into the refined acid desorption tower according to actual conditions to further remove potassium permanganate reducing substances contained in the refined acid.
The high-temperature refined sulfuric acid after desorption enters a refined acid intermediate tank. Ultrapure water is added into the intermediate tank of the refined product acid according to the requirement, so that the specification and the quality of the product refined sulfuric acid can be flexibly adjusted. The refined product acid is cooled to 40 ℃ by a refined product acid cooler through a refined product acid delivery pump, one part of the refined product acid returns to a refined product acid intermediate tank to control the temperature of the refined product acid in the tank to be less than 90 ℃, and the other part of the refined product acid is output as the refined product acid and is sent to a refined product storage tank.
The primary conversion flue gas after sulfur trioxide is absorbed is about 130-200 ℃ after secondary conversion by the second conversion unit, and then is up to standard and discharged after absorption treatment by the second absorption unit and the tail gas absorption unit. The embodiment can produce the refined sulfuric acid meeting the requirement of the analysis and purification product in the chemical reagent sulfuric acid (GB/T625-2007) standard. Meanwhile, the embodiment can also produce industrial-grade sulfuric acid with various product concentrations meeting the requirement of industrial sulfuric acid (GB/T534-2014).
The refined acid product obtained by the system and the process of the embodiment has high purity, can reach the analytical purity level, has high conversion rate of sulfur dioxide in the flue gas, and greatly improves the economic benefit while treating the smelting flue gas.
100000Nm in flue gas amount3/h，SO2The concentration is 6% for example. By adopting the conventional contact acid preparation process (without a deep cooling impurity removal unit), the temperature of the flue gas at the outlet of the first purification unit is about 40 ℃ in summer, at the moment, the acid preparation system cannot produce refined sulfuric acid and can only produce 26.45t/h of industrial-grade 98% sulfuric acid(ii) a In winter, the temperature of the flue gas at the outlet of the first purification unit is about 30 ℃, and at the moment, the acid making system can produce 10.77t/h of refined sulfuric acid and 15.68t/h of industrial-grade 98% sulfuric acid;
by adopting the technical scheme, the acid making system can produce 23.27/h of refined sulfuric acid and 3.18t/h of industrial-grade 98% sulfuric acid all the year round according to the condition that the temperature of the flue gas at the outlet of the deep cooling impurity removal unit is controlled to be 5 ℃. The yield of the refined sulfuric acid is at least increased by 116 percent, and the economic benefit of enterprises is greatly increased.
The foregoing examples are set forth to illustrate the present invention more clearly and are not to be construed as limiting the scope of the invention, which is defined in the appended claims to which the invention pertains, as modified in all equivalent forms, by those skilled in the art after reading the present invention.
Claims (4)
1. A system for preparing sulfuric acid by utilizing smelting flue gas is characterized by comprising a first purification unit, a deep cooling impurity removal unit, a drying unit, a first conversion unit, a second purification unit and a first absorption unit which are sequentially communicated; the deep cooling impurity removal unit comprises a deep cooling tower, a first demister, a first circulating pump and a first circulating liquid cooler which are sequentially communicated, and the deep cooling tower, the first circulating pump and the first circulating liquid cooler are sequentially communicated to form a circulating loop; the drying unit comprises a drying tower, a drying acid circulating tank, a second circulating pump and a second circulating liquid cooler which are sequentially communicated and form a circulating loop; the second purification unit comprises a flue gas filter, a nicotinic acid washing tower, a nicotinic acid circulating tank, a third circulating pump and a third circulating liquid cooler which are sequentially communicated, and the nicotinic acid washing tower, the nicotinic acid circulating tank, the third circulating pump and the third circulating liquid cooler are sequentially communicated to form a circulating loop.
2. The system of claim 1, further comprising a niacin intermediate acid tank in communication with the liquid outlet of the third circulating liquid cooler, the niacin intermediate acid tank being in communication with the flue gas filter.
3. The system of claim 1, wherein the first absorption unit comprises a refined acid absorption tower, a refined acid circulation tank, a fourth circulation pump and a fourth circulation liquid cooler, and the refined acid absorption tower, the refined acid circulation tank, the fourth circulation pump and the fourth circulation liquid cooler are communicated in sequence and form a circulation loop.
4. The system as claimed in claim 3, further comprising a refined acid desorption tower connected to the liquid outlet of the fourth circulation pump, wherein the liquid outlet of the refined acid desorption tower is connected to the refined acid intermediate tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811509697.XA CN109264674B (en) | 2018-12-11 | 2018-12-11 | Process and system for preparing sulfuric acid by using smelting flue gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811509697.XA CN109264674B (en) | 2018-12-11 | 2018-12-11 | Process and system for preparing sulfuric acid by using smelting flue gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109264674A CN109264674A (en) | 2019-01-25 |
| CN109264674B true CN109264674B (en) | 2020-07-03 |
Family
ID=65187575
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811509697.XA Active CN109264674B (en) | 2018-12-11 | 2018-12-11 | Process and system for preparing sulfuric acid by using smelting flue gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109264674B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110155955B (en) * | 2019-04-01 | 2021-07-23 | 岷山环能高科股份公司 | Production method for preparing electronic-grade sulfuric acid by using non-ferrous smelting flue gas |
| CN109879255B (en) * | 2019-04-27 | 2024-11-29 | 招远市招金金合科技有限公司 | System and method for producing refined sulfuric acid by pyrite acid making system |
| CN110354622A (en) * | 2019-07-30 | 2019-10-22 | 易门铜业有限公司 | Flue gas removal of impurities and tail gas cleaning device in a kind of acid manufacturing processes |
| CN111115587B (en) * | 2020-01-19 | 2024-06-21 | 长沙华时捷环保科技发展股份有限公司 | Method and system for preparing analytically pure sulfuric acid from smelting flue gas |
| CN112142013B (en) * | 2020-09-27 | 2023-07-04 | 黑龙江紫金铜业有限公司 | Method for producing food additive sulfuric acid by nonferrous smelting flue gas |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54119396A (en) * | 1978-03-09 | 1979-09-17 | Hitachi Zosen Corp | Manufacture of sulfuric acid |
| CN106430117A (en) * | 2016-10-21 | 2017-02-22 | 河池市生富冶炼有限责任公司 | Method for preparing analytical pure sulfuric acid by using smelting flue gas |
| CN108002352A (en) * | 2017-12-28 | 2018-05-08 | 广西生富锑业科技股份有限公司 | A kind of method of troilite melting flue gas extracting sulfuric acid |
| CN108147373A (en) * | 2017-12-28 | 2018-06-12 | 广西生富锑业科技股份有限公司 | A kind of method that flue gas during smelting prepares sulfuric acid |
| CN108607303A (en) * | 2018-04-23 | 2018-10-02 | 安徽华铂再生资源科技有限公司 | A kind of closing acid-scrubbing cleaning technique of deep dehydration |
-
2018
- 2018-12-11 CN CN201811509697.XA patent/CN109264674B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54119396A (en) * | 1978-03-09 | 1979-09-17 | Hitachi Zosen Corp | Manufacture of sulfuric acid |
| CN106430117A (en) * | 2016-10-21 | 2017-02-22 | 河池市生富冶炼有限责任公司 | Method for preparing analytical pure sulfuric acid by using smelting flue gas |
| CN108002352A (en) * | 2017-12-28 | 2018-05-08 | 广西生富锑业科技股份有限公司 | A kind of method of troilite melting flue gas extracting sulfuric acid |
| CN108147373A (en) * | 2017-12-28 | 2018-06-12 | 广西生富锑业科技股份有限公司 | A kind of method that flue gas during smelting prepares sulfuric acid |
| CN108607303A (en) * | 2018-04-23 | 2018-10-02 | 安徽华铂再生资源科技有限公司 | A kind of closing acid-scrubbing cleaning technique of deep dehydration |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109264674A (en) | 2019-01-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109264674B (en) | Process and system for preparing sulfuric acid by using smelting flue gas | |
| CN104138713A (en) | Method, device and reactor for recovery of sulfur from acidic gas | |
| CN106430117B (en) | A kind of method that melting flue gas produces analytical pure sulfuric acid | |
| CN103318850A (en) | Low-temperature waste heat recovery system for pyrite and metallurgical off-gas acid making device | |
| CN102872695A (en) | Method for sintering and desulfurizing enriched smoke to prepare sulfuric acid | |
| CN211521596U (en) | System for preparing analytically pure sulfuric acid from smelting flue gas | |
| CN109675394B (en) | Low-concentration SO2Method for preparing analytically pure sulfuric acid by one-by-one absorption of smelting flue gas | |
| CN111115587A (en) | Method and system for preparing analytically pure sulfuric acid from smelting flue gas | |
| CN109173598B (en) | Method for recovering CS in viscose waste gas by using composite solvent2Method (2) | |
| CN101979130A (en) | Method for Recycling and Removing Hydrogen Sulfide from Industrial Gas | |
| CN210645731U (en) | Device for realizing solvent recovery and nitrogen recycling by compression condensation membrane separation technology | |
| CN107082407B (en) | A kind of method of purification of anhydrous hydrofluoric acid | |
| CN108793089B (en) | Process for producing refined sulfuric acid in sulfuric acid plant | |
| CN209226584U (en) | Acid-scrubbing cleaning-absorption process reagent of sulfuric acid manufacture production system | |
| CN105502302A (en) | Method and system for preparing smelting flue gas into sulphur | |
| EP2272796B1 (en) | Process for production of concentrated sulphuric acid from off-gas | |
| CN110272027B (en) | Wet process system and process for waste sulfuric acid | |
| CN101428773A (en) | Purifying method for nitric oxide gas with 3N purity | |
| CN204412040U (en) | A kind of combined type Gas Purification Factory low concentration acid gas processing device | |
| CN102952589A (en) | Method for removing acid gas out of raw gas or shifted gas of raw gas | |
| CN216946224U (en) | Device for directly producing electronic-grade sulfuric acid from pyrite | |
| CN216727188U (en) | Methyl chloride synthesis system | |
| CN212327892U (en) | Energy-saving flue gas carbon dioxide recovery system | |
| CN114590782A (en) | Device and method for directly producing electronic-grade sulfuric acid from pyrite | |
| CN113800479A (en) | Process for preparing electronic-grade sulfuric acid by cyclic absorption method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |