CN103318850A - Low-temperature waste heat recovery system for pyrite and metallurgical off-gas acid making device - Google Patents
Low-temperature waste heat recovery system for pyrite and metallurgical off-gas acid making device Download PDFInfo
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- CN103318850A CN103318850A CN2013102995908A CN201310299590A CN103318850A CN 103318850 A CN103318850 A CN 103318850A CN 2013102995908 A CN2013102995908 A CN 2013102995908A CN 201310299590 A CN201310299590 A CN 201310299590A CN 103318850 A CN103318850 A CN 103318850A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention relates to a low-temperature waste heat recovery system for a pyrite and metallurgical off-gas acid making device. The low-temperature waste heat recovery system provided by the invention is characterized by comprising a DWHS absorbing tower, an evaporator, a recycle acid pump groove, a deoxygenated water preheater, an acid-acid heat exchanger, a desalted water preheater and a diluter. The connection order is as follows: the bottom of the DWHS absorbing tower is connected with the recycle acid pump groove; output of the recycle acid pump groove is divided into two paths: one path is successively connected with the evaporator, the deoxygenated water preheater, the acid-acid heat exchanger and the desalted water preheater; and the other path is successively connected with the diluter and the acid-acid heat exchanger; an outlet of the diluter is also connected with an input port on the upper portion of the DWHS absorbing tower; The upper portion of the DWHS absorbing tower inputs sulfuric acid from two acid absorption thermoelectric cooler outlets of an acid making device, and the lower portion of the DWHS absorbing tower inputs flue gas from three segments of coal economizer of the acid making device so as to form two segments of absorbing tower. As for the upper portion, low-temperature sulfuric acid from a drying and absorption workshop section is adopted for absorption, and as for the lower portion, high-temperature sulfuric acid is adopted for circulation absorption.
Description
Technical field
The present invention relates to the low temperature exhaust heat recovery system in a kind of sulfuric acid production process flow process, particularly disclose a kind of low temperature exhaust heat recovery system for sulfurous iron ore and metallurgical off-gas acid-making device, be applicable to pyrite-based sulfuric acid production and metallurgical off-gas acid-making device.
Background technology
Gas washing in SA production mainly comprises the burning of sulfur-bearing raw material, the oxidation of sulfurous gas and three processes of absorption of sulphur trioxide, and these processes all discharge with a large amount of chemical energy.Most of sulfuric acid production plant is recycled as much as possible to height, the middle potential temperature heat energy of sulfur-bearing material combusting and oxidizing sulfur dioxide generation, and for the low-temperature heat energy in dry and the absorption system, except minority manufacturing enterprise is used for heat industrial water and domestic water, generally all be to remove and waste with recirculated cooling water for a long time.
Traditional sulphur-burning sulphuric acid plant has only reclaimed 60%～70% of the total heat that produces, has developed at present the method that the low-temperature heat energy of supporting acid production with sulphur reclaims both at home and abroad, and the heat energy recovery rate of sulphur-burning sulphuric acid plant reached more than 90%.And for sulfurous iron ore and metallurgical off-gas acid-making device, only reclaimed at present 50%～60% of the total heat that produces, because the existence of purification system being arranged, enter the sulfur dioxide gas of drying tower by water saturated, the water balance of whole dried desorption system can not bear extra amount of water.Just because of the existence of doing the water balance problem of inhaling operation in pyrite-based sulfuric acid production or the metallurgical off-gas acid-making, the low temperature exhaust heat recovery technology in the acid production with sulphur and device thereof can not directly be used for pyrite-based sulfuric acid production or metallurgical off-gas acid-making.A kind of brand-new low temperature exhaust heat recovery technology that is applicable to pyrite-based sulfuric acid production and metallurgical off-gas acid-making and device thereof have just arisen at the historic moment.
The recycling degree of used heat has become an important indicator weighing the sulfuric acid industry technology in the gas washing in SA production, and the green energy resource factory that sulfuric acid production plant is considered as not discharging carbonic acid gas has become a kind of common recognition.In today of energy growing tension, in the situation that sulfuric acid apparatus generally is recycled utilization at high, middle potential temperature heat energy, how the low temperature exhaust heat recovery technology of rational exploitation and utilization pyrite-based sulfuric acid production and metallurgical off-gas acid-making is of great immediate significance.
Summary of the invention
Purpose of the present invention
The present invention is achieved in that a kind of low temperature exhaust heat recovery system for sulfurous iron ore and metallurgical off-gas acid-making device, it is characterized in that: described low temperature exhaust heat recovery system is an organic whole, equipment comprises the DWHS absorption tower, vaporizer, the cyclic acid pump groove, the deaerated water preheater, sour interchanger, demineralized-water preheater and diluter, the said apparatus order of connection is: connect the cyclic acid pump groove from bottom, DWHS absorption tower, the output of cyclic acid pump groove is divided into two-way, one the tunnel connects vaporizer successively, the deaerated water preheater, sour interchanger and demineralized-water preheater, another road connects diluter and sour interchanger successively, and the delivery port of diluter also is connected with the input aperture of DWHS absorption tower epimere; The sulfuric acid of described DWHS absorption tower epimere input is inhaled the acid cooler outlet from two of sulphuric acid plant, the flue gas of hypomere input is from three sections economizers of sulphuric acid plant, form two sections absorption towers, epimere is the low temperature absorption section, adopt low temperature sulfuric acid absorption dry and that the absorption section string comes, hypomere is the high temperature absorber portion, adopts the high-temperature sulfuric acid circulation to absorb.
The low-pressure steam that makes the extra fecund of sulphuric acid plant give birth to 3.771t/h after having three flow processs to carry out in the described low temperature exhaust heat recovery system, extra factor of created gase is 0.201t/t acid, described three flow processs are as follows:
A) sour flow process, concentration is after to be 99.6% recycle acid by cyclic acid pump pump in the acid circulating pump groove, be divided into two-way: the one tunnel sends into dry and the absorption operation as the string acid of low temperature exhaust heat recovery, for fully reclaiming heat, on the sour loop of string, be provided with successively vaporizer, deaerated water preheater, sour interchanger and demineralized-water preheater; High-temperature concentrated sulfuric acid and steam heat exchange cooling in vaporizer, vaporizer output steam; Diluter is sent on another road, mixes with 93～96% sulfuric acid from drying tower system through peracid acid heat exchange in diluter, adjusts the high temperature absorber portion that sulfuric acid concentration to 99% is sent into the DWHS absorption tower afterwards;
B) carbonated drink flow process, after deaerated water pressurizes via the low pressure feed water pump, send into the deaerated water well heater, send into vaporizer after the sulfuric acid heating by low temperature exhaust heat recovery guest performer, deaerated water vaporization in vaporizer, generate the low-pressure saturated steam of 0.3～0.8MPa, this saturation steam by steam separator in the vaporizer separate with liquid water after send into sulphuric acid plant low-pressure steam pipe network;
C) flue gas is from the flue gas after the conversion first time of sulphuric acid plant conversion procedure, flue gas is introduced the DWHS absorption tower, acid contacts with low temperature absorption with high temperature circulation acid with the low temperature absorption section at the high temperature section absorber portion successively in tower, and contained sulphur trioxide is absorbed and sends the first absorption tower entrance back to by DWHS absorption tower top exit pipeline after acid absorbs in the flue gas.
Also connect the guest performer's acid tube road from the recycle pump of drying tower on the incoming line of the sour interchanger of described acid, the heat that utilizes high-temperature sulfuric acid behind the vaporizer in the future 93%～96% low temperature acid of self-desiccation tower recycle pump is heated to more than 100 ℃, the heat of taking out of with recovery system part guest performer acid, and the temperature of raising recycle acid, the heat energy recovery rate of raising system.
Connect from deoxygenator guest performer acid tube road on the incoming line of described deaerated water preheater, connect the guest performer's acid tube road from desalted water station on the incoming line of described deaerated water preheater, with the heat that recovery system guest performer acid is taken out of, improve the heat energy recovery rate of system.
The invention has the beneficial effects as follows: the present invention increases the low temperature exhaust heat recovery system by the drying at pyrite-based sulfuric acid production and metallurgical off-gas acid-making device with absorbing in the operation, come 93%～96% sulfuric acid to be used for the water that adds of alternative low temperature exhaust heat recovery system with dry and absorption system string, thereby do not affect the water balance of whole sulfate system; In the situation that dry and absorption system water balance permission also can add part water, to improve system's heat energy recovery rate in diluter.Employing the present invention can reclaim pyrite-based sulfuric acid production or metallurgical off-gas acid-making is done most of absorption reaction heat of inhaling operation, produces the low-pressure saturated steam of 0.3～0.8MPa, and the while is the consumption of economized cycle water coolant significantly.Therefore the benefit of the present invention's generation is apparent.。
Description of drawings
Fig. 1 is low temperature exhaust heat recovery system process flow diagram of the present invention.
Among the figure: 1, DWHS absorption tower; 2, diluter; 3, cyclic acid pump groove; 4, sour interchanger; 5, deaerated water preheater; 6, vaporizer; 7, demineralized-water preheater; 8, blowdown system.
Embodiment
With reference to the accompanying drawings, a kind of low temperature exhaust heat recovery system for sulfurous iron ore and metallurgical off-gas acid-making device of the present invention is an organic whole, equipment comprises DWHS absorption tower 1, vaporizer 6, cyclic acid pump groove 3, deaerated water preheater 5, sour interchanger 4, demineralized-water preheater 7 and diluter 2, the said apparatus order of connection is: connect cyclic acid pump groove 3 from 1 bottom, DWHS absorption tower, the output of cyclic acid pump groove 3 is divided into two-way, one the tunnel connects vaporizer 6 successively, deaerated water preheater 5, sour interchanger 4 and demineralized-water preheater 7, another road connects diluter 2 and sour interchanger 4 successively, and the delivery port of diluter 2 also is connected with the input aperture of DWHS absorption tower 1 epimere.The sulfuric acid of DWHS absorption tower 1 epimere input is inhaled the acid cooler outlet from two of sulphuric acid plant, the flue gas of hypomere input is from three sections economizers of sulphuric acid plant, form two sections absorption towers, epimere is the low temperature absorption section, adopt low temperature sulfuric acid absorption dry and that the absorption section string comes, hypomere is the high temperature absorber portion, adopts the high-temperature sulfuric acid circulation to absorb.
The low-pressure steam that makes the extra fecund of sulphuric acid plant give birth to 3.771t/h after having three flow processs to carry out in the low temperature exhaust heat recovery system of the present invention, extra factor of created gase is 0.201t/t acid, three flow processs are as follows:
1) sour flow process:
Concentration is 99.6%(wt% approximately) recycle acid pumped in the acid circulating pump groove 3 by cyclic acid pump after, be divided into two-way:
One the tunnel sends into dry and the absorption operation as the string acid of low temperature exhaust heat recovery, is abundant recovery heat, is provided with successively vaporizer 6, deaerated water preheater 5, sour interchanger 4 and demineralized-water preheater 7 on the sour loop of string.At vaporizer 6 interior high-temperature concentrated sulfuric acids and steam heat exchange cooling, vaporizer 6 output steam; The high-temperature concentrated sulfuric acid of going out from vaporizer 6 and deaerated water will enter the deaerated water heating of vaporizer 6 in the 5 interior heat exchange of deaerated water preheater; The high-temperature concentrated sulfuric acid of going out from deaerated water preheater 7 and 93～96% low temperature sulfuric acid heat exchange the sour interchanger 4 of acid from drying tower system, to seal in the diluter 2 after 93～96% the low temperature acid heating, to improve the heat energy recovery rate of low temperature exhaust heat recovery system, adjusting enters the sour dense of DWHS absorption tower 1 high temperature section and reaches 99%; The sulfuric acid temperature of going out from the sour interchanger 4 of acid is still higher, lowers the temperature with the further heat exchange of the de-mineralized water that comes from the outside in demineralized-water preheater 7 first, sends into afterwards sulphuric acid plant and does the suction circulation groove, will deliver to deoxygenator after the de-mineralized water heating simultaneously.
Diluter 2 is sent on another road, in diluter 2, mix with 93～96% sulfuric acid from drying tower system through peracid acid heat exchange, adjust acid concentration to 99% and send into the high temperature absorber portion on DWHS absorption tower 1 afterwards, sulfuric acid contacts with flue gas in tower, after absorbing the sulphur trioxide in the flue gas, concentration increases, and discharges from the tower bottom outlet and enters acid circulating pump groove 3, finishes once circulation.In addition, from dry and absorb that concentration that operation attracts is 98～98.5%, temperature is about the low temperature absorption section that 60 ℃ sulfuric acid enters 1 top, DWHS absorption tower, sulfuric acid contacts with flue gas, further absorbs the SO in the flue gas
3And effectively control the generation of acid mist, the sulfuric acid after the low temperature absorption section absorbs also falls into the high temperature absorber portion, finally mixes at the bottom of tower with the absorption acid of high temperature absorber portion.
2) carbonated drink flow process:
The de-mineralized water that desalted water station is sent here is sent into demineralized-water preheater 7, sends into thermal deaerator after the sulfuric acid heating by low temperature exhaust heat recovery guest performer, and de-mineralized water becomes deaerated water behind the free oxygen except the middle dissolving of anhydrating in deoxygenator; After deaerated water pressurizes via the low pressure feed water pump, send into deaerated water preheater 5, send into vaporizer 6 after the sulfuric acid heating by low temperature exhaust heat recovery guest performer, in vaporizer 6 interior deaerated water vaporizations, generate the low-pressure saturated steam of 0.3～0.8MPa, this saturation steam by vaporizer 6 interior steam separators separate with liquid water after send into sulphuric acid plant low-pressure steam pipe network.
3) flue gas flow:
Flue gas is from the flue gas after the conversion first time of sulphuric acid plant conversion procedure, flue gas is introduced DWHS absorption tower 1, acid contacts with low temperature absorption with high temperature circulation acid with the low temperature absorption section at the high temperature section absorber portion successively in tower, contained sulphur trioxide is absorbed and sends the first absorption tower entrance back to by DWHS absorption tower 1 top exit pipeline after acid absorbs in the flue gas, and is removed by the mist eliminator at top, the first absorption tower and to enter conversion section behind the acid mist and carry out conversion second time.The DWHS absorption tower of low temperature exhaust heat recovery system of the present invention also can substitute pyrite-based sulfuric acid production and metallurgical off-gas acid-making and do first absorption tower of inhaling in the operation, can also or connect use in parallel with the first absorption tower.
Embodiment:
Certain produces 150000 tons of pyrite-based sulphuric acid plants per year, with 8000 hours years man-hour calculation, calculated after one section (being the high temperature absorber portion) and two sections (being the low temperature absorption section) absorption on DWHS absorption tower, to go out tower flue gas and form the 1(flue gas that sees the following form to advance low temperature exhaust heat recovery tower temperature be 180 ℃ by the flue gas composition that enters the low temperature exhaust heat recovery tower after once transforming).
One section spray concentration is 99% sulfuric acid, the sulfuric acid of two sections sprays 98%, concentration is about 99.6% behind two sections sulphur trioxides that absorb in the flue gas, minute two-way after being pumped in the acid circulating pump groove by cyclic acid pump: the one tunnel passes through vaporizer, deaerated water preheater successively, sour interchanger and demineralized-water preheater heat exchange cooling are sent into afterwards pyrite-based sulphuric acid plant and are done the suction circulation groove; Diluter is sent on another road, mixes with 95% dilute sulphuric acid in diluter, adjusts acid concentration to 99%, sends into afterwards the DWHS absorption tower.
Be set in and be water within each interchanger and walk shell side, tube side is walked in acid.The sulfuric acid temperature of evaporator outlet is 170
oC, deaerated water preheater acid side outlet acid temperature is 164
oC, sour exchanger heat side outlet acid temperature is 137
oC, it is 60 that rare cold acid enters sour heat exchange temperature
OC, it is 103 that demineralized-water preheater exports sour temperature
oC, sulfuric acid stream temperature loss between each equipment is 1
OCBy SO
3Volumetric flow rate and design temperature can calculate that sulfuric acid goes out sour pump and the temperature of flow through diluter and each interchanger, volumetric flow rate.See Table 2-table 4.
Following table 2 is the process stream energy balance sheet.
Following table 3 is process stream energy balance sheet (continued 1).
Following table 4 is process stream energy balance sheet (continued 2).
The demineralized-water preheater inlet water temperature is 20
OC, pressure is 0.4MPa, deaerated water preheater inlet water temperature is 104
OC, pressure is 0.8MPa(G), vaporizer output low-pressure steam pressure is 0.6MP (G), current are 0.1MP through the pressure-losses of shell side in each preheater, can calculate vaporizer producing steam amount by above data based heat balance principle, see the following form 5.
Table 5 is material and energy balance table (continued 3).
Table 6 is material and energy balance table (continued 4).
Draw thus and adopt low temperature exhaust heat recovery system of the present invention, can make the low-pressure steam of the extra voluminous 3.771t/h of this pyrite-based sulphuric acid plant, extra steam generating capacity is 0.201t/t acid.If dry and absorption operation water balance allows to add in right amount water in system of the present invention, can also further improve low-pressure steam output.If this pyrite-based sulphuric acid plant does not increase this low temperature exhaust heat recovery system, the flue gas after once transforming directly enters common the first absorption tower, and absorption system needs a large amount of recirculated water to be cooled off.Therefore adopt low temperature exhaust heat recovery system of the present invention so that sulfuric acid apparatus has greatly reduced the consumption of dry and absorption system recirculated water when producing extra a large amount of steam.
This shows, the low temperature exhaust heat recovery system that the present invention is used for pyrite-based sulfuric acid production and metallurgical off-gas acid-making is greatly improved comprehensive heat utilization rate, has not only reclaimed available energy, and has reduced the pollution of environment.
Claims (4)
1. low temperature exhaust heat recovery system that is used for sulfurous iron ore and metallurgical off-gas acid-making device, it is characterized in that: described low temperature exhaust heat recovery system is an organic whole, equipment comprises the DWHS absorption tower, vaporizer, the cyclic acid pump groove, the deaerated water preheater, sour interchanger, demineralized-water preheater and diluter, the said apparatus order of connection is: connect the cyclic acid pump groove from bottom, DWHS absorption tower, the output of cyclic acid pump groove is divided into two-way, one the tunnel connects vaporizer successively, the deaerated water preheater, sour interchanger and demineralized-water preheater, another road connects diluter and sour interchanger successively, and the delivery port of diluter also is connected with the input aperture of DWHS absorption tower epimere; The sulfuric acid of described DWHS absorption tower epimere input is inhaled the acid cooler outlet from two of sulphuric acid plant, the flue gas of hypomere input is from three sections economizers of sulphuric acid plant, form two sections absorption towers, epimere is the low temperature absorption section, adopt low temperature sulfuric acid absorption dry and that the absorption section string comes, hypomere is the high temperature absorber portion, adopts the high-temperature sulfuric acid circulation to absorb.
2. described low temperature exhaust heat recovery system for sulfurous iron ore and metallurgical off-gas acid-making device according to claim 1, it is characterized in that: the low-pressure steam that makes the extra fecund of sulphuric acid plant give birth to 3.771t/h after having three flow processs to carry out in the described low temperature exhaust heat recovery system, extra factor of created gase is 0.201t/t acid, and described three flow processs are as follows:
A) sour flow process, concentration is after to be 99.6% recycle acid by cyclic acid pump pump in the acid circulating pump groove, be divided into two-way: the one tunnel sends into dry and the absorption operation as the string acid of low temperature exhaust heat recovery, for fully reclaiming heat, on the sour loop of string, be provided with successively vaporizer, deaerated water preheater, sour interchanger and demineralized-water preheater; High-temperature concentrated sulfuric acid and steam heat exchange cooling in vaporizer, vaporizer output steam; Diluter is sent on another road, mixes with 93～96% sulfuric acid from drying tower system through peracid acid heat exchange in diluter, adjusts the high temperature absorber portion that sulfuric acid concentration to 99% is sent into the DWHS absorption tower afterwards;
B) carbonated drink flow process, after deaerated water pressurizes via the low pressure feed water pump, send into the deaerated water well heater, send into vaporizer after the sulfuric acid heating by low temperature exhaust heat recovery guest performer, deaerated water vaporization in vaporizer, generate the low-pressure saturated steam of 0.3～0.8MPa, this saturation steam by steam separator in the vaporizer separate with liquid water after send into sulphuric acid plant low-pressure steam pipe network;
C) flue gas is from the flue gas after the conversion first time of sulphuric acid plant conversion procedure, flue gas is introduced the DWHS absorption tower, acid contacts with low temperature absorption with high temperature circulation acid with the low temperature absorption section at the high temperature section absorber portion successively in tower, and contained sulphur trioxide is absorbed and sends the first absorption tower entrance back to by DWHS absorption tower top exit pipeline after acid absorbs in the flue gas.
3. according to claim 1 or 2 described low temperature exhaust heat recovery systems for sulfurous iron ore and metallurgical off-gas acid-making device, it is characterized in that: also connect the guest performer's acid tube road from the recycle pump of drying tower on the incoming line of the sour interchanger of described acid, the heat that utilizes high-temperature sulfuric acid behind the vaporizer in the future 93%～96% low temperature acid of self-desiccation tower recycle pump is heated to more than 100 ℃, the heat of taking out of with recovery system part guest performer acid, and the temperature of raising recycle acid, the heat energy recovery rate of raising system.
4. the low temperature exhaust heat recovery system for sulfurous iron ore and metallurgical off-gas acid-making device according to claim 1 and 2, it is characterized in that: connect from deoxygenator guest performer acid tube road on the incoming line of described deaerated water preheater, connect the guest performer's acid tube road from desalted water station on the incoming line of described deaerated water preheater, with the heat that recovery system guest performer acid is taken out of, improve the heat energy recovery rate of system.
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Cited By (8)
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| CN103588179A (en) * | 2013-11-13 | 2014-02-19 | 俞向东 | Device and method for improving steam generating rate of low-temperature waste heat recovery system for sulfuric acid |
| CN103723691A (en) * | 2013-12-12 | 2014-04-16 | 丁华 | Device for preparing sulfuric acid by adopting semi-dry method |
| CN104773711A (en) * | 2015-03-27 | 2015-07-15 | 南京梅山冶金发展有限公司 | Recovery equipment and recovery method of pyrite-based sulfuric acid production dry absorption work section waste heat |
| CN105236360A (en) * | 2015-11-17 | 2016-01-13 | 南京海陆化工科技有限公司 | Device and method for improving recycling of low-temperature heat of ore or smelted fume prepared sulfuric acid |
| CN105460904A (en) * | 2014-08-20 | 2016-04-06 | 孟莫克化工成套设备(上海)有限公司 | Sulfuric acid apparatus low temperature thermal recovery system using predrying tower, and acid crossflow method and application thereof |
| CN106335882A (en) * | 2016-08-25 | 2017-01-18 | 长沙有色冶金设计研究院有限公司 | Sulfuric acid drying suction process complete low-temperature position heat recovery system |
| CN107879317A (en) * | 2017-10-30 | 2018-04-06 | 襄阳泽东化工集团有限公司 | A kind of system for improving acid production with sulphur low temperature exhaust heat recovery steam production |
| CN109437239A (en) * | 2018-12-27 | 2019-03-08 | 中冶焦耐(大连)工程技术有限公司 | The low temperature position exhaust heat recovering method and device of process are absorbed in a kind of acid-making process |
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| CN104773711A (en) * | 2015-03-27 | 2015-07-15 | 南京梅山冶金发展有限公司 | Recovery equipment and recovery method of pyrite-based sulfuric acid production dry absorption work section waste heat |
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| CN109437239A (en) * | 2018-12-27 | 2019-03-08 | 中冶焦耐(大连)工程技术有限公司 | The low temperature position exhaust heat recovering method and device of process are absorbed in a kind of acid-making process |
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Application publication date: 20130925 |