CN105174230A - Technology for preparing refined sulfuric acid from smelting waste gas by means of direct absorption method - Google Patents
Technology for preparing refined sulfuric acid from smelting waste gas by means of direct absorption method Download PDFInfo
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- CN105174230A CN105174230A CN201510615455.9A CN201510615455A CN105174230A CN 105174230 A CN105174230 A CN 105174230A CN 201510615455 A CN201510615455 A CN 201510615455A CN 105174230 A CN105174230 A CN 105174230A
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- pov
- acid
- flue gas
- tower
- absorption
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Abstract
The invention discloses a technology for preparing refined sulfuric acid from smelting waste gas by means of a direct absorption method, and belongs to the technical field of sulfuric acid preparation. The problem that in the prior art, the refined sulfuric acid cannot be prepared through smelting waste gas is solved. According to the technology for preparing the refined sulfuric acid from the smelting waste gas by means of the direct absorption method, sulfuric acid is refined through the direct absorption method, the steps are simple, and qualified refined sulfuric acid can be effectively prepared; the refined sulfuric acid can enter a degassing tower in a multi-time circulating mode to remove reducing substances till a product is qualified, and the quality of the product is guaranteed.
Description
Technical field
The present invention relates to sulfuric acid preparation technique field, specifically, particularly relate to the technique that the direct absorption process of a kind of flue gas during smelting produces POV.
Background technology
That is discharged by nonferrous smelting contains SO
2flue gas, obtains containing SO after purification and oxidation
3flue gas, can direct production technical grade vitriol oil product.
But because coloured composition of ores is complicated, smelting furnace complex manufacturing, the SO2 flue gas that contains of smelting furnace by-product is difficult to adopt direct absorption process to produce POV product, and indirect method usually can only be adopted to produce POV product.Indirect method technique is for first producing 25% free SO by flue gas
3oleum, then evaporate SO by oleum
3, and then produce POV product.This technical process is long, output is few, energy consumption is high, production cost is high.
Summary of the invention
In order to solve the problem, the invention discloses the technique that the direct absorption process of a kind of flue gas during smelting produces POV, solve flue gas during smelting in prior art and directly cannot produce the problem of POV.Provide the technique of a kind of flue gas during smelting by direct absorption process POV, obtain qualified POV product with simple and effective step.
The present invention is achieved by the following technical solutions:
The direct absorption process of flue gas during smelting produces a technique for POV, comprises the steps:
A, containing SO
3flue gas enter washing tower from gas approach and wash, the flue gas after washing enters smoke filter and filters;
Flue gas after b, filtration enters absorption tower from the upper end of smoke filter, and the POV be used in self-absorption circulation groove sprays, and POV carries out circulation conveying by pump second, and POV absorbs the SO in flue gas
3, go out from the tower bottom flow on absorption tower after absorption and enter in absorption cycle groove after the cooling of concentrated acid water cooler.
C, concentration according to concentrated acid in absorption cycle groove, added water by water inlet pipe and adjust and be maintained to normal concentration, the acid after dilution is pumped to absorbing tower top spray-absorption SO by pump second again
3, qualified POV is pumped to converge to enter in degassing tower to the arm first on circulating line and with the outlet pipe on reactive tank by pump second and is removed SO
2gas;
D, remove SO
2the POV of gas enters condenser from the bottom of degassing tower and cools, and enters in reactive tank after cooling, adds a certain amount of oxygenant remove potassium permanganate reducing substance further according to practical situation;
E, qualified after POV pumped to the arm second on outlet pipe by pump third and cool through finished product water cooler, send into finished acid storage tank first and finished acid storage tank second after cooling;
F, finished acid are pumped to elevated dosing vessel through pump fourth again.
POV in absorption cycle groove in described step b is by mother liquor Cemented filling, and the temperature of POV is about 70 DEG C, and concentration is 98.3%.
In described step b after POV spray-absorption containing SO
3furnace gas enter convertor from the escape pipe first 11 absorption tower and carry out twice transformation manufacture sulfuric acid again.
Degassing tower in described steps d adopts to be sent into and the cleaned air filtered through air filter by blower fan, and in degassing tower, expellant gas discharges after escape pipe second imports sulfuric acid apparatus process.
Oxygenant in described steps d is placed in dosing tank, is delivered in reactive tank by dosing pump.
Washing tower in described step a adopts washing acid to containing SO
3flue gas wash, washing acid adopts pump first to carry out circulation and carries, and washing acid is cooled by washing acid water cooler, and washing acid is the oleum of 106%.
The washing acid water cooler used in described step a ~ e, concentrated acid water cooler, condenser and finished product water cooler are all connected with recirculated cooling water.
The underproof sulfuric acid produced in described step b ~ d can be delivered to sulfuric acid discharge tube by vomit pipe first, vomit pipe second, vomit pipe third and be entered sloptank as industrial sulphuric acid.
Compared with prior art, the invention has the beneficial effects as follows:
The direct absorption process of a kind of flue gas during smelting of the present invention produces the technique of POV, and by direct absorption process POV, step is simple, effectively can obtain qualified POV; POV repeatedly can circulate and enter degassing tower removing reducing substance to product is qualified, ensures quality product.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
In Fig. 1: 1, mother liquor pipeline; 2, sulfuric acid discharge tube; 3, washing tower; 4, smoke filter; 5, washing acid water cooler; 6, pump first; 7, concentrated acid water cooler; 8, absorption cycle groove; 9, pump second; 10, absorption tower; 11, escape pipe first; 12, water inlet pipe; 13, degassing tower; 14, air filter; 15, blower fan; 16, escape pipe second; 17, condenser; 18, reactive tank; 19, pump third; 20, dosing tank; 21, dosing pump; 22, finished product water cooler; 23, finished acid storage tank first; 24, finished acid storage tank second; 25, pump fourth; 26, elevated dosing vessel; 27, circulating line; 28, arm first; 29, outlet pipe; 30, arm second; 31, vomit pipe first; 32, vomit pipe second; 33, vomit pipe third; 34, circulating water inlet; 35, circulating water outlet pipe; 36, gas approach.
Embodiment
Below in conjunction with accompanying drawing, the present invention is further described:
The direct absorption process of flue gas during smelting produces a technique for POV, comprises the steps:
A, containing SO
3flue gas enter washing tower 3 from gas approach 36 and wash, the flue gas after washing enters smoke filter 4 and filters;
Flue gas after b, filtration enters absorption tower 10 from the upper end of smoke filter 4, and the POV be used in self-absorption circulation groove 8 sprays, and POV carries out circulation conveying by pump second 9, and POV absorbs the SO in flue gas
3, go out from the tower bottom flow on absorption tower 10 after absorption and enter in absorption cycle groove 8 after concentrated acid water cooler 7 cools.
C, concentration according to concentrated acid in absorption cycle groove 8, added water by water inlet pipe 12 and adjust and be maintained to normal concentration, the acid after dilution is pumped to absorption tower 10 tower top spray-absorption SO by pump second 9 again
3, qualified POV is pumped to the arm first 28 on circulating line 27 by pump second 9 and is converged to enter in degassing tower 13 with the outlet pipe 29 on reactive tank 18 and removes SO
2gas;
D, remove SO
2the POV of gas enters condenser 17 from the bottom of degassing tower 13 and cools, and enters in reactive tank 18 after cooling, adds a certain amount of oxygenant remove potassium permanganate reducing substance further according to practical situation;
E, qualified after POV pump to the arm second 30 on outlet pipe 29 by pump the third 19 and cool through finished product water cooler 22, send into finished acid storage tank first 23 and finished acid storage tank second 24 after cooling;
F, finished acid are pumped to elevated dosing vessel 26 through pump fourth 25 again.
POV in absorption cycle groove 8 in described step b is carried by mother liquor pipeline 1, and the temperature of POV is about 70 DEG C, and concentration is 98.3%.
In described step b after POV spray-absorption containing SO
3furnace gas enter convertor from the escape pipe first 11 absorption tower 10 and carry out twice transformation manufacture sulfuric acid again.
Degassing tower 13 in described steps d adopts to be sent into and the cleaned air filtered through air filter 14 by blower fan 15, and in degassing tower 13, expellant gas discharges after escape pipe second 16 imports sulfuric acid apparatus process.
Oxygenant in described steps d is placed in dosing tank 20, is delivered in reactive tank 18 by dosing pump 21.
Washing tower 3 in described step a adopts washing acid to containing SO
3flue gas wash, washing acid adopts pump first 6 to carry out circulation and carries, and washing acid is cooled by washing acid water cooler 5, and washing acid is the oleum of 106%.
The washing acid water cooler 5 used in described step a ~ e, concentrated acid water cooler 7, condenser 17 are all connected with recirculated cooling water with finished product water cooler 22.
The underproof sulfuric acid produced in described step b ~ d can be delivered to sulfuric acid discharge tube 2 by vomit pipe first 31, vomit pipe second 32, vomit pipe the third 33 and be entered sloptank as industrial sulphuric acid.
As shown in Figure 1, washing tower 3 is connected with mother liquor pipeline 1, and washing tower 3 side is provided with gas approach 36, and washing tower 3 is provided with smoke filter 4 above, washing tower 3 is by being connected to form circulation loop between washing acid water cooler 5, pump first 6, and washing acid to be circulated conveying by pump first 6; The upper end of smoke filter 4 is connected to the side on absorption tower 10, absorption tower 10 is by being connected to form circulation loop between concentrated acid water cooler 7, absorption cycle groove 8, pump 9, concentrated acid water cooler 7 is connected at the bottom of the tower on absorption tower 10, the bottom of absorption cycle groove 8 is provided with circulating line 27, the other end of circulating line 27 is connected to the tower top on absorption tower 10, absorption tower 10 is provided with escape pipe first 11, and the top of absorption cycle groove 8 is also connected with water inlet pipe 12.
Circulating line 27 is provided with arm first 28, arm first 28 converges with the outlet pipe 29 on reactive tank 18 side being connected to degassing tower 13, the bottom of degassing tower 13 is connected with air filter 14, air filter 14 side is connected with blower fan 15, degassing tower 13 and condenser 17, reactive tank 18, pump the third 19, circulation loop is connected to form between outlet pipe 29, be connected with condenser 17 bottom at the bottom of the tower of degassing tower 13, condenser 17 upper end is connected to reactive tank 18 upper end, pump the third 19 is arranged on outlet pipe 29, POV is by pump the third 19 circulation conveying, degassing tower 13 is also provided with escape pipe second 16, reactive tank 18 is also connected with dosing tank 20, dosing tank 20 is provided with dosing pump 21.
Outlet pipe 29 is provided with arm second 30, arm second 30 is connected with finished product condenser 22, finished acid storage tank first 23, finished acid storage tank second 24, finished product condenser 22, finished acid storage tank first 23, finished acid storage tank second 24 are also connected with elevated dosing vessel 26, between be provided with pump fourth 25.
Washing acid water cooler 5, concentrated acid water cooler 7, condenser 17 are all connected with recirculated cooling water with finished product water cooler 22, and on Fig. 1,34,35 are recirculated water inlet and outlet piping.
Absorption cycle groove 8 bottom is connected with vomit pipe first 31, and condenser 17 bottom is connected with vomit pipe second 32, and reactive tank 18 bottom is connected with vomit pipe the third 33, and vomit pipe first 31, vomit pipe second 32, vomit pipe the third 33 is all connected to sulfuric acid discharge tube 2.
Washing tower 3 is connected with mother liquor pipeline 1, containing SO
3flue gas enter in washing tower 3 from gas approach 36 and wash, washing acid in washing tower 3 is circulated by pump first 6 and carries and cooled by washing acid water cooler 5, mother liquor pipeline 1 provides washing acid, washing acid becomes the oleum of 106% from the vitriol oil of concentration 98.3% and maintains balance after washing for some time, and the flue gas after washing enters smoke filter 4 and filters; Flue gas after filtration enters absorption tower 10 from the upper end of smoke filter 4, POV in absorption cycle groove 8 is carried by mother liquor pipeline 1, the temperature of POV is about 70 DEG C, concentration is 98.3%, POV in absorption cycle groove 8 is delivered to absorption tower 10 by pump second 9 and sprays, and POV absorbs the SO in flue gas
3, go out from the tower bottom flow on absorption tower 10 after absorption and enter in absorption cycle groove 8 after concentrated acid water cooler 7 cools, after POV spray-absorption containing SO
3furnace gas enter convertor from the escape pipe first 11 absorption tower 10 and carry out twice transformation manufacture sulfuric acid again.
According to the concentration of concentrated acid in absorption cycle groove 8, added water adjust and be maintained to normal concentration by water inlet pipe 12, the acid after dilution is pumped to absorption tower 10 tower top spray-absorption SO by pump second 9 again
3, available POV is pumped to the arm first 28 on circulating line 27 by pump second 9 and is converged to enter in degassing tower 13 with the outlet pipe 29 on reactive tank 18 and removes SO
2gas, degassing tower 13 adopts to be sent into and the cleaned air filtered through air filter 14 by blower fan 15, and in degassing tower 13, expellant gas discharges after escape pipe second 16 imports sulfuric acid apparatus process; Remove SO
2the POV of gas enters condenser 17 from the bottom of degassing tower 13 and cools, enter in reactive tank 18 after cooling, add a certain amount of oxygenant according to practical situation and remove potassium permanganate reducing substance further, oxygenant is placed in dosing tank 20, is delivered in reactive tank 18 by dosing pump 21.Also POV repeatedly can be circulated and enter degassing tower 13 and remove reducing substance to qualified.
POV after qualified is pumped to the arm second 30 on outlet pipe 29 by pump the third 19 and is cooled through finished product water cooler 22, send into finished acid storage tank first 23 and finished acid storage tank second 24 after cooling, finished acid is pumped to elevated dosing vessel 26 through pump fourth 25 and is carried out tinning, transport.
Washing acid water cooler 5, concentrated acid water cooler 7, condenser 17 are all connected with recirculated cooling water with finished product water cooler 22.
The underproof sulfuric acid produced in production process can be delivered to sulfuric acid discharge tube 2 by vomit pipe first 31, vomit pipe second 32, vomit pipe the third 33 and be entered sloptank as industrial sulphuric acid.
The direct absorption process of a kind of flue gas during smelting of the present invention produces the technique of POV, and by direct absorption process POV, step is simple, effectively can obtain qualified POV; POV repeatedly can circulate and enter degassing tower removing reducing substance to product is qualified, ensures quality product.
In sum, be only preferred embodiment of the present invention, not be used for limiting scope of the invention process, all equalizations of doing according to shape, structure, feature and the spirit described in the claims in the present invention scope change and modify, and all should be included in right of the present invention.
Claims (8)
1. the direct absorption process of flue gas during smelting produces a technique for POV, it is characterized in that: comprise the steps:
A, containing SO
3flue gas enter washing tower (3) from gas approach (36) and wash, the flue gas after washing enters smoke filter (4) and filters;
Flue gas after b, filtration enters absorption tower (10) from the upper end of smoke filter (4), the POV be used in self-absorption circulation groove (8) sprays, POV carries out circulation conveying by pump second (9), and POV absorbs the SO in flue gas
3, go out from the tower bottom flow of absorption tower (10) after absorption and enter in absorption cycle groove (8) after concentrated acid water cooler (7) cooling.
C, concentration according to absorption cycle groove (8) interior concentrated acid, added water by water inlet pipe (12) and adjust and be maintained to normal concentration, the acid after dilution is pumped to absorption tower (10) tower top spray-absorption SO by pump second (9) again
3, qualified POV is pumped to the arm first (28) on circulating line (27) by pump second (9) and is converged to enter in degassing tower (13) with the outlet pipe (29) on reactive tank (18) and removes SO
2gas;
D, remove SO
2the POV of gas enters condenser (17) from the bottom of degassing tower (13) and cools, enter in reactive tank (18) after cooling, add a certain amount of oxygenant according to practical situation and remove potassium permanganate reducing substance further;
E, qualified after POV pump to the arm second (30) on outlet pipe (29) and cool through finished product water cooler (22) by pump third (19), send into finished acid storage tank first (23) and finished acid storage tank second (24) after cooling;
F, finished acid are pumped to elevated dosing vessel (26) through pump fourth (25) again.
2. the direct absorption process of flue gas during smelting according to claim 1 produces the technique of POV, it is characterized in that: the POV in the absorption cycle groove (8) in described step b is carried by mother liquor pipeline (1), the temperature of POV is about 70 DEG C, and concentration is 98.3%.
3. the direct absorption process of flue gas during smelting according to claim 1 produces the technique of POV, it is characterized in that: in described step b after POV spray-absorption containing SO
3furnace gas enter convertor from the escape pipe first (11) absorption tower (10) and carry out twice transformation manufacture sulfuric acid again.
4. the direct absorption process of flue gas during smelting according to claim 1 produces the technique of POV, it is characterized in that: the degassing tower (13) in described steps d adopts to be sent into and the cleaned air filtered through air filter (14) by blower fan (15), and degassing tower (13) interior expellant gas discharges after escape pipe second (16) imports sulfuric acid apparatus process.
5. the direct absorption process of flue gas during smelting according to claim 1 produces the technique of POV, it is characterized in that: the oxygenant in described steps d is placed in dosing tank (20), is delivered in reactive tank (18) by dosing pump (21).
6. the direct absorption process of flue gas during smelting according to claim 1 produces the technique of POV, it is characterized in that: the washing tower (3) in described step a adopts washing acid to containing SO
3flue gas wash, washing acid adopt pump first (6) carry out circulation conveying, washing acid pass through washing acid water cooler (5) cool, washing acid is the oleum of 106%.
7. the direct absorption process of flue gas during smelting according to claim 1 produces the technique of POV, it is characterized in that: the filter acid water cooler (5) used in described step a ~ e, concentrated acid water cooler (7), condenser (17) and finished product water cooler (22) are all connected with recirculated cooling water.
8. the direct absorption process of flue gas during smelting according to claim 1 produces the technique of POV, it is characterized in that: the underproof sulfuric acid produced in described step b ~ d can be delivered to sulfuric acid discharge tube (2) by vomit pipe first (31), vomit pipe second (32), vomit pipe third (33) and be entered sloptank as industrial sulphuric acid.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510615455.9A CN105174230A (en) | 2015-09-24 | 2015-09-24 | Technology for preparing refined sulfuric acid from smelting waste gas by means of direct absorption method |
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| CN201510615455.9A CN105174230A (en) | 2015-09-24 | 2015-09-24 | Technology for preparing refined sulfuric acid from smelting waste gas by means of direct absorption method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105731394A (en) * | 2015-12-31 | 2016-07-06 | 安阳市岷山有色金属有限责任公司 | Refined sulfuric acid preparation device and preparation method thereof |
| CN108793089A (en) * | 2018-09-03 | 2018-11-13 | 中国瑞林工程技术股份有限公司 | A kind of technique of sulfuric acid plant's production refined sulfuric acid |
| CN110155955A (en) * | 2019-04-01 | 2019-08-23 | 安阳市岷山有色金属有限责任公司 | A kind of production method for producing electronic-grade sulfuric acid using Flue Gas of Nonferrous Smelting |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1689968A (en) * | 2004-04-19 | 2005-11-02 | 上海京藤化工有限公司 | Production method of refined sulfuric acid and production equipment thereof |
| CN102115045A (en) * | 2010-11-30 | 2011-07-06 | 东营方圆有色金属有限公司 | Method for concentrating and purifying dilute acid by using waste heat of smelting flue gas and device thereof |
-
2015
- 2015-09-24 CN CN201510615455.9A patent/CN105174230A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1689968A (en) * | 2004-04-19 | 2005-11-02 | 上海京藤化工有限公司 | Production method of refined sulfuric acid and production equipment thereof |
| CN102115045A (en) * | 2010-11-30 | 2011-07-06 | 东营方圆有色金属有限公司 | Method for concentrating and purifying dilute acid by using waste heat of smelting flue gas and device thereof |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105731394A (en) * | 2015-12-31 | 2016-07-06 | 安阳市岷山有色金属有限责任公司 | Refined sulfuric acid preparation device and preparation method thereof |
| CN108793089A (en) * | 2018-09-03 | 2018-11-13 | 中国瑞林工程技术股份有限公司 | A kind of technique of sulfuric acid plant's production refined sulfuric acid |
| CN108793089B (en) * | 2018-09-03 | 2021-08-20 | 中国瑞林工程技术股份有限公司 | Process for producing refined sulfuric acid in sulfuric acid plant |
| CN110155955A (en) * | 2019-04-01 | 2019-08-23 | 安阳市岷山有色金属有限责任公司 | A kind of production method for producing electronic-grade sulfuric acid using Flue Gas of Nonferrous Smelting |
| 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 |
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Application publication date: 20151223 |