CN102336396B - Continuous heat transfer sulfur dioxide conversion process - Google Patents
Continuous heat transfer sulfur dioxide conversion process Download PDFInfo
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- CN102336396B CN102336396B CN 201110303168 CN201110303168A CN102336396B CN 102336396 B CN102336396 B CN 102336396B CN 201110303168 CN201110303168 CN 201110303168 CN 201110303168 A CN201110303168 A CN 201110303168A CN 102336396 B CN102336396 B CN 102336396B
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Abstract
The invention discloses a continuous heat transfer sulfur dioxide conversion process, which is suitable for the sulfuric acid making industry. The process comprises the following steps of: allowing high-concentration SO2 smoke from a blower to pass through a primary conversion heat exchanger, heating to catalyst ignition temperature, introducing into a first-section reaction layer of a converter, controlling reaction temperature in the converter by adjusting the air quantity of a cooling fan, heating the primarily converted gas by using the primary conversion heat exchanger, and introducing the primarily converted gas into a first absorption tower; and introducing the smoke into a secondary conversion heat exchanger after SO3 is completely absorbed, heating the smoke to the catalyst ignition temperature, introducing the smoke into a second-section reaction layer of the converter, controlling reaction temperature in the converter by adjusting the air quantity of the cooling fan, heating the secondarily converted gas by using the secondary conversion heat exchanger, introducing the secondarily converted gas into a second absorption tower, and exhausting after SO3 is completely absorbed. The process overcomes a temperature control bottleneck in a high-concentration smoke conversion technology, a catalyst and steel for equipment are operated at tolerable lower temperature, and the conversion rate is over 99.85 percent.
Description
Technical field
The present invention relates to a kind of hot Sulphur Dioxide technique that continues to move, mainly be applicable to sulfuric acid and produce industry, especially utilize non-ferrous metal metallurgy to produce high density sulphur dioxide flue gas acid preparing industry.
Background technology
The raw materials such as non-ferrous smelt enterprise pyrometallurgical smelting such as copper, nickel, lead, zinc mostly are sulphide ores, after it is smelted the tail gas traditional treatment method be with behind its purifying and dedusting by the oxidation extracting sulfuric acid.Along with the progress of smelting technology, smelting enterprise has generally adopted the continuous smelting technology of oxygen enrichment or industrial air, has therefore produced the flue gas of high concentration SO 2, and this has higher requirement to the flue gas acid preparing device.As pressing existing acid-making process, needing flue gas during smelting is diluted to SO2 concentration is about 12%, and this will make the size of sulphuric acid plant increase 3～5 times, and construction investment and the working cost of corresponding sulphuric acid plant all can increase considerably.If with the flue gas concentration dilution, the flue gas that contains SO230%～60% does not enter conversion system, and enough oxygen contents need to be arranged, and requires simultaneously reaction carriers (catalyst and convertor) can bear very high temperature.Enough oxygen contents can be realized by filling into air or oxygen, and oxidizing reaction institute liberated heat is uncontrollable, because if so2 concentration in flue gas surpasses 12%, convertor one deck temperature out will be above 640 ℃.Generally speaking, be used for carrying out being limited to 630 ℃ on catalyzer thermally-stabilised of SO2 oxidizing reaction, be used for making the common used material of convertor, carbon steel and 304 stainless steels etc. can not be in long-time running more than 600 ℃, so temperature control also is difficult point and the bottleneck of high-concentration fume transformation technology.
Be the principle of a reversible exothermic reaction based on 2SO2+O2=2SO3, in order to obtain higher transformation efficiency this reaction carried out as far as possible to the positive reaction direction, namely reach by reducing temperature of reaction.Reducing temperature of reaction in the normal sulfate system operation, to implement difficulty larger, is thermopositive reaction mainly due to this reaction, and the transformation efficiency of reaction is higher, and the reaction heat of emitting is also just larger, and this just gives and reduces temperature of reaction and bring difficulty.Present conversion process is to carry out a conversion zone by arranging after interchanger is realized every section reacted temperature is reduced to optimal temperature again, but when SO2 concentration surpasses 12% even when higher, one section temperature is uncontrollable in the lower scope, at this moment will cause one section reaction heat excessive, make the temperature of reactant gases surpass all unaffordable ultimate temperatures of 640 ℃ of these catalyst and steel.
Summary of the invention
The invention solves heat in the high concentration SO 2 smoke conversion process and too much be difficult to the difficult problem that shifts out, what provide that a kind of theory is advanced, simple in structure, difficulty of processing is little, technological operation is simple, engineering construction investment is few continues to move hot Sulphur Dioxide technique.Main innovation is greatly to have simplified the technical process of gas washing in SA production, and whole system only needs two interchanger, a convertor and auxiliary air blower that whole conversion system is normally moved, and control is simple.
Specifically implement like this: continue to move hot Sulphur Dioxide technique, it is characterized in that step is:
1) flue gas from sulphur dioxide blower enters the shell side that once transforms interchanger, be heated to touch coal combustion initiation temperature (420 ± 10 ℃) after, the one section responding layer that enters convertor;
2) flue gas step 1) carries out oxidizing reaction in one section responding layer of convertor, move heat pipe in being provided with in the tactile coal seam of one section responding layer, in move and pass into freezing air or cold water or low-pressure steam in the heat pipe, the heat that oxidizing reaction produces by in move freezing air in the heat pipe or cold water or low-pressure steam and remove, by regulating the flow of cooling blower, the temperature of control convertor is 520 ± 10 ℃;
3) flue gas that contains a large amount of SO3 out enters the tube side that once transforms interchanger from one section responding layer of convertor, and with the flue gas heat exchange from sulphur dioxide blower, the flue-gas temperature of one section responding layer is reduced to 150 ± 10 ℃ and gone out tube side and enter the absorption tower one time;
4) flue gas after SO3 is removed on an absorption tower enters the shell side of twice transformation interchanger, be heated to touch coal combustion initiation temperature (420 ± 10 ℃) after, enter the second-stage reaction layer of convertor;
5) flue gas step 4) carries out oxidizing reaction in the second-stage reaction layer of convertor, move heat pipe in also being provided with in the tactile coal seam of second-stage reaction layer, in move and pass into freezing air or cold water or low-pressure steam in the heat pipe, the heat that oxidizing reaction produces by in move freezing air in the heat pipe or cold water or low-pressure steam and remove, by regulating the flow of cooling blower, the temperature of control convertor is 450 ± 10 ℃, can satisfy system's thermal equilibrium, can guarantee higher transformation efficiency again;
6) flue gas that contains a large amount of SO3 out enters the tube side of twice transformation interchanger from the second-stage reaction layer of convertor, carry out heat exchange with the flue gas from an absorption tower, the flue-gas temperature of second-stage reaction layer is reduced to 150 ± 10 ℃ and is gone out tube side and enter the double absorption tower, absorbed SO3 after, directly emptying;
7) behind freezing air, cold water or the low-pressure steam absorbing heat in one section, two excellent responding layers in the heat transfer tube, reclaim heat by economizer, boiler or superheater.
Technique of the present invention is that a kind of theory is advanced, workable, engineering construction investment is few, the simple high density Sulphur Dioxide of technological operation technique, solved the temperature control bottleneck in the high-concentration fume transformation technology, catalyst and equipment are all moved under a lesser temps that can bear with steel, and transformation efficiency can reach more than 99.85%, the relatively simple method of heat energy utilization in the technique reclaims, and this recovery of heat mode has guaranteed that equipment is not corroded.
Description of drawings
Fig. 1 is the process flow sheet of this invention
Embodiment
Continue to move hot Sulphur Dioxide technique, step is:
1) pipeline 7 of flue gas before transforming from sulphur dioxide blower enters the shell side that once transforms interchanger 1, be heated to touch coal combustion initiation temperature (420 ± 10 ℃) after, the one section responding layer that enters convertor 3;
2) flue gas step 1) carries out oxidizing reaction in one section responding layer of convertor 3, move heat pipe 6 in being provided with in the tactile coal seam of one section responding layer, in move and pass into freezing air or cold water or low-pressure steam in the heat pipe 6, the heat that oxidizing reaction produces by in move freezing air in the heat pipe 6 or cold water or low-pressure steam and remove, by regulating the flow of cooling blower 2, the temperature of control convertor 3 is 520 ± 10 ℃;
3) contain a large amount of SO
3Flue gas out enter the tube side that once transforms interchanger 1 from one section responding layer of convertor 3, with the flue gas heat exchange from sulphur dioxide blower, the flue-gas temperature of one section responding layer is reduced to 150 ± 10 ℃ and is entered the absorption tower one time by transforming rear line 8 after going out tube side;
4) remove SO through an absorption tower
3After flue gas enter the shell side of twice transformation interchanger 5, be heated to touch coal combustion initiation temperature (420 ± 10 ℃) after, enter the second-stage reaction layer of convertor 3;
5) flue gas step 4) carries out oxidizing reaction in the second-stage reaction layer of convertor 3, move heat pipe 6 in also being provided with in the tactile coal seam of second-stage reaction layer, in move and pass into freezing air or cold water or low-pressure steam in the heat pipe 6, the heat that oxidizing reaction produces by in move freezing air in the heat pipe 6 or cold water or low-pressure steam and remove, by regulating the flow of cooling blower 2, the temperature of control convertor is 450 ± 10 ℃;
6) contain a large amount of SO
3Flue gas out enter the tube side of twice transformation interchanger 5 from the second-stage reaction layer of convertor 3, carry out heat exchange with flue gas from an absorption tower, the flue-gas temperature of second-stage reaction layer is reduced to 150 ± 10 ℃ and is gone out tube side and enter the double absorption tower, has absorbed SO
3After, directly emptying;
7) behind freezing air, cold water or the low-pressure steam absorbing heat in one section, two excellent responding layers in the heat transfer tube 6, produce hot water, steam or high-temperature steams by economizer, boiler or superheater 4, reach the effective recycling of heat.
Claims (2)
1. continue to move hot Sulphur Dioxide technique, it is characterized in that step is:
1) flue gas from sulphur dioxide blower enters the shell side that once transforms interchanger, be heated to touch the coal combustion initiation temperature after, the one section responding layer that enters convertor;
2) flue gas step 1) carries out oxidizing reaction in one section responding layer of convertor, move heat pipe in being provided with in the tactile coal seam of one section responding layer, in move and pass into freezing air or cold water or low-pressure steam in the heat pipe, the heat that oxidizing reaction produces by in move freezing air in the heat pipe or cold water or low-pressure steam and remove, by regulating the flow of cooling blower, the temperature of control convertor is 520 ± 10 ℃;
3) contain a large amount of SO
3Flue gas out enter the tube side that once transforms interchanger from one section responding layer of convertor, with the flue gas heat exchange from sulphur dioxide blower, the flue-gas temperature of one section responding layer is reduced to 150 ± 10 ℃ and is gone out tube side and enter the absorption tower one time;
4) remove SO through an absorption tower
3After flue gas enter the shell side of twice transformation interchanger, be heated to touch the coal combustion initiation temperature after, enter the second-stage reaction layer of convertor;
5) flue gas step 4) carries out oxidizing reaction in the second-stage reaction layer of convertor, move heat pipe in also being provided with in the tactile coal seam of second-stage reaction layer, in move and pass into freezing air or cold water or low-pressure steam in the heat pipe, the heat that oxidizing reaction produces by in move freezing air in the heat pipe or cold water or low-pressure steam and remove, by regulating the flow of cooling blower, the temperature of control convertor is 450 ± 10 ℃;
6) contain a large amount of SO
3Flue gas out enter the tube side of twice transformation interchanger from the second-stage reaction layer of convertor, carry out heat exchange with flue gas from an absorption tower, the flue-gas temperature of second-stage reaction layer is reduced to 150 ± 10 ℃ and is gone out tube side and enter the double absorption tower, has absorbed SO
3After, directly emptying;
7) behind freezing air, cold water or the low-pressure steam absorbing heat in one section, second-stage reaction layer in the heat transfer tube, reclaim heat by economizer, boiler or superheater.
2. according to claim 1ly continue to move hot Sulphur Dioxide technique, it is characterized in that touching the coal combustion initiation temperature is 420 ± 10 ℃.
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| CN 201110303168 CN102336396B (en) | 2011-09-27 | 2011-09-27 | Continuous heat transfer sulfur dioxide conversion process |
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| CN 201110303168 CN102336396B (en) | 2011-09-27 | 2011-09-27 | Continuous heat transfer sulfur dioxide conversion process |
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| CN102336396B true CN102336396B (en) | 2013-04-10 |
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Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EA027063B1 (en) | 2012-06-06 | 2017-06-30 | Хальдор Топсёэ А/С | Process for the oxidation of soto so |
| CN106966373A (en) * | 2016-06-28 | 2017-07-21 | 荆门市熊兴化工有限公司 | Description on Production of Sulfaminic Acid line with surplus energy utility system |
| CN106915731B (en) * | 2017-04-14 | 2023-08-08 | 双盾环境科技有限公司 | Adjustable high-concentration SO (SO) treatment by using inert catalyst 2 SO production by flue gas 3 Device for gas |
| CN107021461B (en) * | 2017-04-14 | 2017-12-26 | 双盾环境科技有限公司 | A kind of adjustable application inertia catalyst processing high concentration SO2Flue gas produces SO3The technique of gas |
| CN107381513B (en) * | 2017-09-14 | 2019-09-27 | 长沙有色冶金设计研究院有限公司 | A kind of high concentration SO2Flue gas acid preparing technique |
| CN112441566A (en) * | 2019-08-29 | 2021-03-05 | 中石化南京化工研究院有限公司 | Distributed SO of sulfuric acid device2Transformation method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4138309A (en) * | 1976-06-18 | 1979-02-06 | Hch. Bertrams Aktiengesellschaft | Multi-stage apparatus for concentrating sulphuric acid |
| CN2280087Y (en) * | 1996-12-20 | 1998-04-29 | 南京化工大学 | Reactor for conversion sulfur oxides by use of heat pipe heat-exchange |
| CN101580230A (en) * | 2009-06-03 | 2009-11-18 | 江苏中兴化工设备有限公司 | Method for preparing acid through low-concentration SO2 unstable-state conversion |
| CN201361530Y (en) * | 2009-01-06 | 2009-12-16 | 中国瑞林工程技术有限公司 | Flue gas recirculation loop of high-concentration sulfur dioxide reforming device |
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- 2011-09-27 CN CN 201110303168 patent/CN102336396B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4138309A (en) * | 1976-06-18 | 1979-02-06 | Hch. Bertrams Aktiengesellschaft | Multi-stage apparatus for concentrating sulphuric acid |
| CN2280087Y (en) * | 1996-12-20 | 1998-04-29 | 南京化工大学 | Reactor for conversion sulfur oxides by use of heat pipe heat-exchange |
| CN201361530Y (en) * | 2009-01-06 | 2009-12-16 | 中国瑞林工程技术有限公司 | Flue gas recirculation loop of high-concentration sulfur dioxide reforming device |
| CN101580230A (en) * | 2009-06-03 | 2009-11-18 | 江苏中兴化工设备有限公司 | Method for preparing acid through low-concentration SO2 unstable-state conversion |
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Owner name: SHUANGDUN ENVIRONMENTAL TECHNOLOGY CO., LTD. Free format text: FORMER NAME: YIXING CHEMICAL INDUSTRY COMPLETE-SET EQUIPMENT CO., LTD. |
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Address after: Huankeyuan Garden Road 214205 Jiangsu city of Yixing Province, No. 105 Patentee after: SHUANGDUN ENVIRONMENT TECHNOLOGY CO., LTD. Address before: Huankeyuan Garden Road 214205 Jiangsu city of Yixing Province, No. 105 Patentee before: Yixing City Chemical Industry Complete Equipment Co., Ltd. |