CN1006219B - Process and equipment for prodn. of sulfuric acid by chlorine method form waste gas of sulfur dioxide - Google Patents
Process and equipment for prodn. of sulfuric acid by chlorine method form waste gas of sulfur dioxide Download PDFInfo
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- CN1006219B CN1006219B CN86107266.9A CN86107266A CN1006219B CN 1006219 B CN1006219 B CN 1006219B CN 86107266 A CN86107266 A CN 86107266A CN 1006219 B CN1006219 B CN 1006219B
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- tower
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- sulfuric acid
- acid
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Abstract
The present invention belongs to an inorganic chemical industry technology and equipment for sulfur dioxide waste gas recovery. The technology and the equipment of the present invention for preparing sulphuric acid and hydrochloric acid through oxidizing sulfur dioxide waste gas by chlorine or chloride waste gas have the advantages of simplicity and high efficiency. A reaction tower has various efficacies such as reaction, absorption, concentration, separation, etc.; absorption liquid is not circulated, so no acid pump is needed, and the absorption liquid is absorbed through reaction in the reaction tower; 70% sulphuric acid and sulfosalt mixed acid can be directly obtained. The sulfur dioxide clearance rate in the waste gas reaches more than 98%, the chlorine utilization ratio reaches more than 99%, the sulfur dioxide content in tail gas is lower than 0.02%, and the total amount of chlorine and chlorate is about 0.005%.
Description
The invention belongs to inorganic chemical technology and equipment that form waste gas of sulfur dioxide reclaims.
At present, the method that reclaims form waste gas of sulfur dioxide both at home and abroad is more, as soda solution grouting, lime method, the ammonia stripping method, the alkaline earth absorption process, tens kinds of catalytic oxidation-reduction methods etc., but wherein some method produces a large amount of waste residues (as calcium sulfite, calcium sulfate, lime carbonate etc.), waste water, thereby cause secondary pollution, the byproduct using value that some method obtains is little, and some method need consume a large amount of industrial chemicals in short supply, and some method elimination efficiency is not high, and most method technologies are complicated, equipment is huge, and investment is many, the process cost height.
The objective of the invention is to simplify and reclaim the form waste gas of sulfur dioxide Processes and apparatus, and utilize chlorine or chlorine contained exhaust gas superfluous in the present chlorine industry, reach and efficiently and economically recycle form waste gas of sulfur dioxide, make it to generate useful sulfuric acid and hydrochloric acid.
The present invention is that the form waste gas of sulfur dioxide that utilizes chlorine or chlorine contained exhaust gas to handle 0.1% above concentration is produced sulfuric acid and hydrochloric acid, its technological process as shown in drawings, respectively with form waste gas of sulfur dioxide from inlet pipe [1], chlorine or chlorine contained exhaust gas are pressed equivalent or sulfurous gas from inlet pipe [2] and are fed after mixing tank [3] mixes than chlorine excessive 0.1%, feed reaction tower [6], bubble cap formula reaction tower in this way, control air-flow superficial linear velocity 0.03～0.2 meter per second, improved in this way sieve-board type reaction tower, then controlling the air-flow superficial linear velocity is 0.1～0.5 meter per second, add water from water inlet pipe [4] to reaction tower, control reaction tower temperature of reaction is below 250 ℃, only pass through this reaction tower effect, just can reach rapid reaction, absorb, concentrate, isolating effect.The control amount of water makes to feed in the tower behind the sulfurous gas and chlorine reaction, can directly obtain 70% sulfuric acid from discharge port at the bottom of the tower [11], is lower than 70% sulfuric acid, the then corresponding increase of amount of water as making.Obtaining 70% vitriolic simultaneously, from reaction tower, can get the mixing acid of whole hydrochloric acid and part of sulfuric acid, i.e. sulfosalt mixing acid, allow sulfosalt mixing acid flow out from outlet [7], feed distillation tower [8] air distillation, emit hydrochloric acid, can obtain sulfuric acid from sulfuric acid outlet [10] from hydrochloric acid outlet [9].With the mixing acid air distillation, 110 ℃ steam whole hydrochloric acid, and concentration can reach 20%, and remaining sulfuric acid concentration is 70%, and tail gas is emitted from tail gas outlet [5] in the reaction tower.
The total reaction equation is in the reaction tower:
SO
2+CL
2+2H
2O＝H
2SO
4+2HCL
This technology can be used the gas-liquid bubbling style reaction tower of multiple structure type, and for example bubble cap formula reaction absorption tower, improved sieve-board type react the absorption tower, and column plate just can reach the requirements that this technological reaction absorbs for 4～8 layers.Each of every kind of tower layer tower wall all is equipped with visor, liquidometer, thermometer, weather gauge, liquid discharging tube, so that red-tape operati condition and the acid solution of emitting reaction absorption generation.Common sieve-board type reaction tower liquid discharging tube places in the tower, is that liquid discharging tube is placed outside the tower outside our improvement, and valve is housed on the liquid discharging tube, by valve control tapping amount and height of liquid layer, thereby makes reaction reach best effect, can control the concentration of acid solution simultaneously.
The material of reaction tower will be selected corrosion resistant glass reinforced plastic, polyvinyl chloride, polypropylene or acid-proof ceramics for use.
Equipment and technical process that the present invention adopts are simply efficient, and its reaction tower has multiple usefulness such as reaction, absorption, concentrated, separation concurrently, and absorption liquid needn't circulate, thereby does not need acid proof pump.Absorb through the reaction tower reaction, can directly make 70% sulfuric acid and sulfosalt mixing acid, sulfosalt mixing acid can get 20% hydrochloric acid and 70% sulfuric acid through normal pressure distillation, the sulfur dioxide recovery rate is that the sulfurous gas clearance rate can reach more than 98% in the waste gas, the chlorine utilization ratio reaches more than 99%, content of sulfur dioxide is lower than 0.02% in the tail gas, and chlorine and chlorine root total content are about 0.005%.
Having carried out content of sulfur dioxide according to Processes and apparatus of the present invention is 0.1～0.8% to wait the expanding test more than 60 time of several waste gas, the accumulative total expanding test time is about 800 hours, adopt bubble cap formula reaction tower and improved sieve-board type reaction tower to test respectively, made the sulfuric acid of hundreds of kilograms 65～70%, sulfosalt mixing acid and 20% hydrochloric acid are produced research for maximizing and have been released this technical process and equipment.
Embodiment 1: certain adopts bubble cap formula reaction tower, the waste gas that contains sulfurous gas about 0.49% be equivalent to the excessive 0.1%(volume of sulfurous gas) respective amount chlorine respectively from accompanying drawing inlet pipe [1] [2] feed mixing tank [3] and mix the back and feed reaction tower [6] and react, control air-flow superficial linear velocity is 0.1 meter per second, the required water of sulfuric acid that adds generation 65% from water inlet pipe [4], the reaction tower temperature is controlled at below 210 ℃, by reaction, absorb, separate, obtain 65% sulfuric acid from discharge port [11], its sulfurous gas elimination factor is 99.1%, and cl content is 0.005% in the tail gas outlet [5].
Embodiment 2: certain adopts improved sieve-board type reaction tower, the chlorine contained exhaust gas of the waste gas that contains sulfurous gas 0.5% and equivalent respectively from accompanying drawing inlet pipe [1] [2] feed after mixing tank [3] mixes, control air-flow superficial linear velocity is that 0.3 meter per second feeds reaction tower [6], make the required water of generation 70% sulfuric acid from water inlet pipe [4] adding, the reaction tower top temperature is controlled at below 210 ℃, absorb, separate by reaction, from discharge port [11] 70% sulfuric acid, the sulfurous gas elimination factor is 99.0%, and cl content is 0.004% in the tail gas outlet [5].
Embodiment 3: the sulfosalt mixing acid of emitting from reaction tower [6] among the embodiment 2 is fed distillation tower [8] from mixing acid outlet [7], adopt air distillation, separation, temperature is controlled at 110 ℃, gets 20% hydrochloric acid from hydrochloric acid outlet [9], and sulfuric acid outlet [10] gets 70% sulfuric acid.
Claims (2)
1, a kind of recovery form waste gas of sulfur dioxide process for preparing sulfuric acid, and comprise the mixing of reaction gas, reaction tower adds the water reaction, gas velocity control, the reaction tower temperature of reaction, distillation tower distillation temperature and pressure-controlling, it is characterized in that with oxychlorination sulfurous gas system sulfuric acid and hydrochloric acid, with sulfurous gas and chlorine or chlorine contained exhaust gas is pressed equivalent or sulfurous gas mixes than chlorine excessive 0.1%, adding makes the sulfuric acid of sulfurous gas generation 70% and 20% the required water of hydrochloric acid in reaction tower, or the corresponding water of required sulfuric acid that is lower than this concentration and hydrochloric acid, the air-flow superficial linear velocity that gas mixture enters bubble tower is the 0.03-0.2 meter per second, the air-flow superficial linear velocity that enters improved sieve-tray tower is the 0.1-0.5 meter per second, the reaction tower temperature is controlled at below 250 ℃, and mixing acid is 110 ℃ of air distillations in distillation tower.
2, a kind of oxychlorination sulfurous gas system sulfuric acid of claim 1 and sieve-tray tower of hydrochloric acid of being used for is characterized in that the liquid discharging tube of sieve-tray tower is placed outside the tower, and the valve of control height of liquid layer is housed on the liquid discharging tube.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN86107266.9A CN1006219B (en) | 1986-10-14 | 1986-10-14 | Process and equipment for prodn. of sulfuric acid by chlorine method form waste gas of sulfur dioxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN86107266.9A CN1006219B (en) | 1986-10-14 | 1986-10-14 | Process and equipment for prodn. of sulfuric acid by chlorine method form waste gas of sulfur dioxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN86107266A CN86107266A (en) | 1988-05-04 |
| CN1006219B true CN1006219B (en) | 1989-12-27 |
Family
ID=4803541
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN86107266.9A Expired CN1006219B (en) | 1986-10-14 | 1986-10-14 | Process and equipment for prodn. of sulfuric acid by chlorine method form waste gas of sulfur dioxide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1006219B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101823694B (en) * | 2010-05-06 | 2012-04-25 | 杭州四面体科技有限公司 | Processing method for purifying sulfur-containing chlorine hydride |
-
1986
- 1986-10-14 CN CN86107266.9A patent/CN1006219B/en not_active Expired
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| Publication number | Publication date |
|---|---|
| CN86107266A (en) | 1988-05-04 |
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