CN1603229A - Humid gas conversion and heat reclamation acid preparation technique - Google Patents
Humid gas conversion and heat reclamation acid preparation technique Download PDFInfo
- Publication number
- CN1603229A CN1603229A CN 200410064923 CN200410064923A CN1603229A CN 1603229 A CN1603229 A CN 1603229A CN 200410064923 CN200410064923 CN 200410064923 CN 200410064923 A CN200410064923 A CN 200410064923A CN 1603229 A CN1603229 A CN 1603229A
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- Prior art keywords
- gas
- heat
- interchanger
- acid
- transforms
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- 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.)
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- 238000000034 method Methods 0.000 title claims abstract description 35
- 239000002253 acid Substances 0.000 title claims abstract description 19
- 238000006243 chemical reaction Methods 0.000 title claims description 27
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 31
- 230000008569 process Effects 0.000 claims abstract description 31
- 238000009833 condensation Methods 0.000 claims abstract description 22
- 230000005494 condensation Effects 0.000 claims abstract description 22
- 238000001035 drying Methods 0.000 claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 12
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 8
- 238000010438 heat treatment Methods 0.000 claims abstract description 8
- 238000010521 absorption reaction Methods 0.000 claims description 25
- 238000011084 recovery Methods 0.000 claims description 10
- 238000004519 manufacturing process Methods 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 8
- 238000004140 cleaning Methods 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 4
- 238000002407 reforming Methods 0.000 claims description 3
- 229910000831 Steel Inorganic materials 0.000 claims description 2
- 239000005388 borosilicate glass Substances 0.000 claims description 2
- 230000006872 improvement Effects 0.000 claims description 2
- 239000010959 steel Substances 0.000 claims description 2
- 239000000498 cooling water Substances 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 11
- 230000009466 transformation Effects 0.000 abstract description 7
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 abstract 4
- 230000007423 decrease Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 77
- 239000003595 mist Substances 0.000 description 7
- 238000005260 corrosion Methods 0.000 description 5
- 230000007797 corrosion Effects 0.000 description 5
- 238000005406 washing Methods 0.000 description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- 239000007769 metal material Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- MTJGVAJYTOXFJH-UHFFFAOYSA-N 3-aminonaphthalene-1,5-disulfonic acid Chemical compound C1=CC=C(S(O)(=O)=O)C2=CC(N)=CC(S(O)(=O)=O)=C21 MTJGVAJYTOXFJH-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000009885 systemic effect Effects 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
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- Treating Waste Gases (AREA)
- Drying Of Gases (AREA)
Abstract
The invention relates to humid gas transformation and heat reclamation acid making process, which belongs to sulfuric acid industrial technology field. The invention adopts humid gas transformation technology, heating up the purified humid gas, hydrous sulfur dioxide gas directly being sent to transformer, then, sulfuric acid would be compounded by sulfur trioxide that comes from the transformer and water, acid would be available after sulfuric acid gas condensation in the condensation absorbing tower. Meanwhile, the heat produced during the transformation process of sulfur dioxide to sulfur trioxide would be reclaimed by heat reclamation device. Its feature is that: first, humid gas directly being sent into transformer, drying tower and a drying circulatory system including concentrated acid pump is canceled, thus, the power consumption during producing process would decline; second, the heat produced in the technology process would be fully used.
Description
Technical field: the invention belongs to the gas washing in SA production technical field, be used for gas washing in SA production.
Background technology: the gas washing in SA production flow process has comprised the several master operations of raw material crushing, fluidized bed roasting, flue gas cleaning, drying, conversion and absorption now, and technical process is longer.From current gas washing in SA production state of the art, can omit drying process wherein, the furnace gas after be about to purifying directly goes conversion procedure to transform after heating up, like this can shortened process, reduce the power consumption of production system simultaneously.
In existing technology, the furnace gas that enters convertor will carry out drying through the drying tower furnace gas that will wet earlier, and dry back furnace gas will heat up, and furnace gas goes convertor once to transform then, through the SO that once transforms
3Furnace gas goes one to inhale tower, inhales SO in the tower one
3The vitriol oil that is recycled absorbs, owing to absorb SO
3Be thermopositive reaction, so recycle acid also needs to use water quench.Going out one inhales in the furnace gas of tower the unconverted SO that is is still arranged
3SO
2, this part gas will go convertor to carry out twice transformation, and gas goes to second absorption tower, the SO in the gas through behind the twice transformation in convertor
3Be recycled acid and absorb, remaining gas externally discharges.
For existing technology, at SO
2Furnace gas advances before the conversion procedure, and gas must carry out drying.Because under the service temperature that transforms, though the water vapour in the furnace gas can not work the mischief the SO after water vapour and the conversion to catalyzer
3In absorption process, can form acid mist together.Because acid mist is difficult to be absorbed in the absorption tower, causes tail gas to emit white cigarette.Simultaneously, under the comprehensive action of acid mist and moisture, can cause the corrosion of doing pipeline, equipment in suction and the conversion procedure, even catalyst agglomeration, active reduction, resistance increasing etc.The drying of furnace gas is that the sulfuric acid with high density sprays in drying tower, and moisture content in the furnace gas is controlled at≤0.1g/Nm
3, reach the purpose that the control acid mist generates.
Drying process has comprised drying tower, and concentrated acid recycle pump and groove also have a jacket water recycle system (furnace-heated is thermopositive reaction) in addition.Simultaneously, because the drying of furnace gas is carried out (～100 ℃) at a lower temperature, make that heat energy is difficult to obtain utilize.
In another kind of acid-making process, as hydrogen sulfide relieving haperacidity,, adopt this technology of humid gas relieving haperacidity usually because sulfureted hydrogen burning generates a large amount of water, the characteristics of this technology are aqueous SO
2Furnace gas directly enters convertor, transforms the back through convertor and generates SO
3, go out the SO of convertor
3With with a part of H wherein
2O is combined into H
2SO
4Steam goes condenser condenses to become the vitriol oil then, and redundant moisture is taken out of with discharge tail gas, and this technology also is a sophisticated technology.Condenser is tubular(surface)condenser or condensing tower.This technology only is applicable to certain conditions, because the furnace gas excess moisture contains a large amount of moisture in the furnace gas that goes out to transform, so can only once transform, transformation efficiency is difficult to improve SO in the tail gas
2Content can exceed standard, and need do further processing and could discharge.
Summary of the invention: the present invention is the improvement of sulfuric acid production process, has been characterized in cancelling the drying process in original technological process of production, has simplified flow process, has reduced the power consumption in producing, and can maximally utilise the heat that produces in the technological process.
Humid gas of the present invention transforms and the recovery of heat acid-making process, adopts the corrosive of anti-sulfur dioxide gas interchanger, the moisture wet furnace gas after purifying is heated to more than the dew point, and then enters steel heat exchanger and continue to be heated to more than 400 ℃, reaches SO
2The temperature that conversion process requires.
Concrete technological process is: furnace gas is through entering the interchanger heating behind the cleaning section, the characteristics of this interchanger are to adopt anti-SO
2Sour gas corrosive material (as interchanger plumbous, glass material), furnace gas temperature is heated on the dew point, enter the next stage interchanger then, because furnace gas temperature is more than dew point, gas alleviates greatly to Corrosion of Metallic Materials, interchanger can adopt the plain carbon stool material, after this continues the hot furnace gas (SO that utilizes a section and three sections to come out
2Change into SO
3Be thermopositive reaction), furnace gas temperature is heated to more than 400 ℃, enter convertor and transform.
The advanced convertor of furnace gas transforms for one section, the gas that goes out one section of conversion is used for the heat exchange of interchanger, through going two sections conversions again after the interchanger cooling, the reforming gas that goes out two sections removes interchanger, this part heat is used to heat by the next gas in condensation absorption tower, the gas that goes out interchanger goes three sections conversions again, and the gas that goes out three sections is through the warm of moving of interchanger and economizer, the SO in this moment furnace gas
3Generate sulfuric acid with the water vapour reaction, and discharge heat, this heat can reclaim by the form of economizer with steam.The sulfuric acid vapor that goes out economizer absorbs by the condensation in the condensation absorption tower and obtains the vitriol oil, has finished so once to transform and become sour process.
In the gas that goes out the condensation absorption tower, since equilibrium conversion, SO
2Once conversion be incomplete, still have some unconverted for SO in this part gas
3SO
2, therefore after absorbing, need to transform once more, to put forward the doctor positive utilization ratio and to reduce SO through condensation
2Discharging.Like this, the gas that goes out the condensation absorption tower goes four sections of convertor to carry out twice transformation after through the interchanger heat exchange, and the gas reusing vitriol oil that goes out convertor absorbs, and absorbs SO with the vitriol oil in the absorption tower
3, tail gas discharges after going out final absorption tower.
In this flow process, wherein one of key equipment is the cryogenic heat exchanger that is used for the humid gas heating, and this equipment claimed adopts the anti-SO that contains moisture
2The corrosion of sour gas, and can not adopt general metallic substance, equipment material can be the borosilicate glass of antimonial lead and heatproof, by this interchanger furnace gas temperature is heated to more than the dew point, reaches to alleviate furnace gas to back metallic recuperator corrosive purpose.
The another one key equipment is the condensation absorption tower, contains moisture owing to transforming in the furnace gas of back, if adopt the absorption tower this moment, goes out the water vapour of convertor and the SO after the conversion
3Can form acid mist in cooling and absorption process, acid mist is difficult to be absorbed in the absorption tower, therefore adopts the condensation absorption tower to replace traditional absorption tower, and sulfuric acid vapor is condensed into acid in the condensation absorption tower.The service temperature on condensation absorption tower is 200～300 ℃, and sulfuric acid vapor is under condensation under this temperature, and can reduce the generation of acid mist this moment by control of process parameters.
The characteristics of this flow process are: a, adopt acid resistance furnace gas corrosive interchanger, bring up to more than the dew point of water by this interchanger furnace gas temperature that will wet, avoid the corrosion of wet furnace gas to follow-up equipment.B, because the furnace gas that advances convertor has been heated to more than 400 ℃, the moisture in the furnace gas can be to SO
2Conversion have a negative impact.Moisture in c, the furnace gas depends on the water-content in the saturated furnace gas, and by the furnace gas temperature decision that goes out cleaning section, this part moisture is after furnace gas transforms and SO
3In conjunction with generating sulfuric acid.D, because SO
3Hydration reaction is carried out under comparatively high temps, and the heat that produces in the technological process can be fully used, and is used to produce medium-pressure or high pressure steam.E, cancel drying and acid circulation system, comprised equipment such as drying tower, recycle pump and groove, concentrated acid interchanger, reduced systemic resistance simultaneously, reduced power consumption.F, owing to adopt heat recovery equipment such as economizer, do not need the water coolant and the recycle system thereof.
Description of drawings: accompanying drawing 1 transforms and recovery of heat acid-making process general flow chart for humid gas of the present invention.In the accompanying drawing, the 1-cryogenic heat exchanger; The 2-III interchanger; The 3-I interchanger; The 4-convertor; The 5-II interchanger; The 6-IV interchanger; 7-II economizes coal gas; 8-IV condensation absorption tower.
Embodiment:
Embodiment:, the embodiment of the invention is described in detail below in conjunction with accompanying drawing 1.
Furnace gas is through entering cryogenic heat exchanger (1) heating behind the cleaning section, the characteristics of this interchanger are to adopt anti-SO
2Sour gas corrosive material is (as lead, the interchanger of glass material), furnace gas temperature is heated on the dew point, enter next stage interchanger (2 then,) since furnace gas temperature more than dew point, gas alleviates greatly to Corrosion of Metallic Materials, interchanger can adopt the plain carbon stool material, after this advanced convertor of furnace gas transforms for 4 one sections, the gas that goes out one section of conversion is used for the heat exchange of interchanger 3, through going two sections conversions again after interchanger 3 coolings, the reforming gas that goes out two sections removes interchanger 5, this part heat is used to heat the gas by condensation absorption tower 8, the gas that goes out interchanger 5 goes three sections conversions again, and the gas that goes out three sections is through the warm of moving of interchanger 2 and economizer 7, the SO in this moment furnace gas
3Generate sulfuric acid with the water vapour reaction, and discharge heat, this heat can reclaim by the form of economizer 7 with steam.The sulfuric acid vapor that goes out economizer 7 absorbs by the condensation in condensation absorption tower 8 and obtains the vitriol oil, has finished so once to transform and become sour process.
Claims (5)
1. a humid gas transforms and the recovery of heat acid-making process, it is the improvement of sulfuric acid production process, it is characterized in that having cancelled drying tower and corresponding dry acid circulation system and cooling water recirculation system, adopt the corrosive of anti-sulfur dioxide gas interchanger, moisture wet furnace gas after purifying is heated to more than the dew point, and then enter steel heat exchanger and continue to be heated to more than 400 ℃, reach SO
2The temperature that conversion process requires.
2. a humid gas as claimed in claim 1 transforms and the recovery of heat acid-making process, it is characterized in that the corrosive of anti-sulfur dioxide gas interchanger that adopts is the cryogenic heat exchanger that is used for the humid gas heating.
3. a humid gas as claimed in claim 1 or 2 transforms and the recovery of heat acid-making process, it is characterized in that the equipment material of the corrosive of anti-sulfur dioxide gas interchanger that adopts is the borosilicate glass of antimonial lead or heatproof.
4. a humid gas as claimed in claim 1 transforms and the recovery of heat acid-making process, it is characterized in that furnace gas through entering cryogenic heat exchanger (1) heating behind the cleaning section, is heated to furnace gas temperature on the dew point, enters next stage interchanger (2) then; After this advanced convertor of furnace gas transforms for (4) one sections, the gas that goes out one section of conversion is used for the heat exchange of interchanger (3), through going two sections conversions again after interchanger (3) cooling, the reforming gas that goes out two sections removes interchanger (5), this part heat is used for the gas that heating is come by condensation absorption tower (8), the gas that goes out interchanger (5) goes three sections conversions again, and the gas that goes out three sections is through the heat of moving of interchanger (2) and economizer (7), the SO in the furnace gas at this moment
3Generate sulfuric acid with the water vapour reaction, and discharge heat, this heat can pass through the form recovery of economizer (7) with steam.The sulfuric acid vapor that goes out economizer (7) absorbs by the condensation in condensation absorption tower (8) and obtains the vitriol oil, has finished so once to transform and become sour process.
5. one kind transforms and the recovery of heat acid-making process as claim 1 or 4 described humid gas, it is characterized in that having adopted the condensation absorption tower, and the service temperature on condensation absorption tower is 200～300 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200410064923XA CN1313361C (en) | 2004-10-12 | 2004-10-12 | Humid gas conversion and heat reclamation acid preparation technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200410064923XA CN1313361C (en) | 2004-10-12 | 2004-10-12 | Humid gas conversion and heat reclamation acid preparation technique |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1603229A true CN1603229A (en) | 2005-04-06 |
| CN1313361C CN1313361C (en) | 2007-05-02 |
Family
ID=34666430
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB200410064923XA Expired - Lifetime CN1313361C (en) | 2004-10-12 | 2004-10-12 | Humid gas conversion and heat reclamation acid preparation technique |
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| Country | Link |
|---|---|
| CN (1) | CN1313361C (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101706095B (en) * | 2009-09-02 | 2011-07-20 | 陈祥明 | Method for recovering acid making waste heat |
| CN103030115A (en) * | 2011-09-29 | 2013-04-10 | 中国石油化工股份有限公司 | United acid manufacturing method by utilizing sulfuretted hydrogen and sulphur |
| CN103723691A (en) * | 2013-12-12 | 2014-04-16 | 丁华 | Device for preparing sulfuric acid by adopting semi-dry method |
| CN104528661A (en) * | 2015-01-14 | 2015-04-22 | 南丹县南方有色金属有限责任公司 | Heat exchange system for acid making conversion of sulfuric acid secondary system |
| CN108167844A (en) * | 2018-01-05 | 2018-06-15 | 江苏科瑞工程设计有限公司 | A kind of method of the air preheat of spent acid cracking technology |
| CN111302314A (en) * | 2020-02-28 | 2020-06-19 | 中化重庆涪陵化工有限公司 | Sulfur acid making system and method for recovering drying heat |
| CN114307868A (en) * | 2020-10-12 | 2022-04-12 | 南京华电节能环保股份有限公司 | Multistage conversion tower for sulfuric acid process by contact method |
| CN114956009A (en) * | 2022-07-07 | 2022-08-30 | 山东鲁北企业集团总公司 | Production system and method for preparing sulfuric acid and co-producing cement clinker by using gypsum |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5118490A (en) * | 1989-06-21 | 1992-06-02 | Monsanto Company | Absorption of wet conversion gas |
| ES2066432T3 (en) * | 1990-03-23 | 1995-03-01 | Monsanto Co | PROCEDURE TO RECOVER HIGH QUALITY PROCESSING ENERGY FROM A CONTACT SULFURIC ACID PROCEDURE. |
| CN1076215C (en) * | 1999-08-13 | 2001-12-19 | 丁华 | Complementary heat-exchanging process of two conversions of sulfuric acid apparatus |
| CN1258841A (en) * | 1999-09-16 | 2000-07-05 | 束润涛 | Heat exchanger capable of resisting the corrosion of sulfuric acid at dew point |
| CN1238246C (en) * | 2002-12-02 | 2006-01-25 | 南昌有色冶金设计研究院 | Adjustable sulfuric acid conversion heat-exchange process |
-
2004
- 2004-10-12 CN CNB200410064923XA patent/CN1313361C/en not_active Expired - Lifetime
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101706095B (en) * | 2009-09-02 | 2011-07-20 | 陈祥明 | Method for recovering acid making waste heat |
| CN103030115A (en) * | 2011-09-29 | 2013-04-10 | 中国石油化工股份有限公司 | United acid manufacturing method by utilizing sulfuretted hydrogen and sulphur |
| CN103030115B (en) * | 2011-09-29 | 2014-11-26 | 中国石油化工股份有限公司 | United acid manufacturing method by utilizing sulfuretted hydrogen and sulphur |
| CN103723691A (en) * | 2013-12-12 | 2014-04-16 | 丁华 | Device for preparing sulfuric acid by adopting semi-dry method |
| CN103723691B (en) * | 2013-12-12 | 2016-02-03 | 丁华 | Semidrying Sulphuric acid device |
| CN104528661A (en) * | 2015-01-14 | 2015-04-22 | 南丹县南方有色金属有限责任公司 | Heat exchange system for acid making conversion of sulfuric acid secondary system |
| CN108167844A (en) * | 2018-01-05 | 2018-06-15 | 江苏科瑞工程设计有限公司 | A kind of method of the air preheat of spent acid cracking technology |
| CN111302314A (en) * | 2020-02-28 | 2020-06-19 | 中化重庆涪陵化工有限公司 | Sulfur acid making system and method for recovering drying heat |
| CN114307868A (en) * | 2020-10-12 | 2022-04-12 | 南京华电节能环保股份有限公司 | Multistage conversion tower for sulfuric acid process by contact method |
| CN114956009A (en) * | 2022-07-07 | 2022-08-30 | 山东鲁北企业集团总公司 | Production system and method for preparing sulfuric acid and co-producing cement clinker by using gypsum |
| CN114956009B (en) * | 2022-07-07 | 2024-06-21 | 山东鲁北企业集团总公司 | Production system and method for preparing sulfuric acid and co-producing cement clinker by using gypsum |
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| Publication number | Publication date |
|---|---|
| CN1313361C (en) | 2007-05-02 |
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Address after: Liuhe District of Nanjing City, Jiangsu province 210048 geguan Road No. 699 Patentee after: SINOPEC NANJING CHEMICAL RESEARCH INSTITUTE Co.,Ltd. Address before: Liuhe District of Nanjing City, Jiangsu province 210048 geguan Road No. 699 Patentee before: RESEARCH INSTITUTE OF NANJING CHEMICAL INDUSTRIAL Group |
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Granted publication date: 20070502 |