CN101706095B - Method for recovering acid making waste heat - Google Patents
Method for recovering acid making waste heat Download PDFInfo
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- CN101706095B CN101706095B CN2009100423683A CN200910042368A CN101706095B CN 101706095 B CN101706095 B CN 101706095B CN 2009100423683 A CN2009100423683 A CN 2009100423683A CN 200910042368 A CN200910042368 A CN 200910042368A CN 101706095 B CN101706095 B CN 101706095B
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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
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Abstract
The invention discloses a method for recovering acid making waste heat of sulfur acid making or smelting acid making. The method comprises the following steps of: recovering partial heat carried by SO3 gas discharged from a first-section outlet, a second-section outlet and a third-section outlet of a converter in the production process of acid making; recovering heat generated by high temperature absorption of a dry absorption heat recovering system; and transferring partial heat carried by acid of a dry absorption heat recovering system to boiler water feed by using a heat exchanger on a boil water feed channel of an outlet of a reacting furnace. The scheme uses heat absorbed by dry absorption high temperature to preheat the boiler water feed of an outlet of a sulfur burner and converts the partial heat into medium pressure overheat steam. Therefore, the method can save investment, reduces requirements for soft water quality, and improves generating efficiency above all. The method appropriately modifies a heat recovering system of a converting system at the same time. The method saves a coal economizer, increases a superheater and is additionally provided with an air preheater. For smelting fume acid making, the method can provide a high temperature absorption system on the dry absorption part, and the generated heat can preheat the boiler water feed in the smelting part.
Description
Technical field
The present invention relates to the method that a kind of industrial relieving haperacidity Waste Heat Recovery is utilized, specifically be meant the method for a kind of acid production with sulphur or smelting acid making Waste Heat Recovery.
Background technology
Modern sulfuric acid plant, particularly acid production with sulphur not only as the factory that produces sulfuric acid, and regard an energy factory as.It is to utilize sulfur furnace S+O
2→ SO
2Reaction heat, the middle pressure steam that waste heat boiler produces 4.0～6.0Mpa is set behind sulfur furnace; Utilize the used heat of conversion process, the superheated steam with Steam Heating to 450 ℃ promptly adds low temperature superheater four sections outlets, increases temperature superheater at one section outlet, and the saturated vapor that boiler is come out is heated to be 450 ℃ superheated steam; Utilize the conversion low-temperature waste heat to come the preboiler feedwater simultaneously, promptly change SO in low temperature superheater outlet and III
3Economizer is established in outlet, boiler feedwater is heated to 230～250 ℃ from 104 ℃, to improve steam production.Do like this and generally speaking can produce 0.40Mpa, 450 ℃ of steam, 1.15t/t (acid).
U.S. MOSK proposes the HRS technology at dried desorption system in recent years, will absorb sour temperature and bring up to more than 200 ℃, and acid is dense more than 99%, produce the steam of 0.6～1.0Mpa, but producing steam is 0.45～0.50t/t (acid) saturated vapor.Waste heat utilization technology is greatly improved.This technology domesticizes, but producing steam 0.45t/t (acid) 0.60～1.0Mpa saturated vapor.Wherein 0.2t/t (acid) low-pressure steam is used for the oxygen-eliminating device of molten sulphur and sulfur furnace outlet boiler, actual 0.25～0.3/t (acid) low-pressure steam that obtains.Above-mentioned acid production with sulphur used heat utilizes scheme to establish the used heat that two boilers reclaim the relieving haperacidity process, promptly in the sulfur furnace outlet medium-pressure boiler is set, and in conversion superheater and economizer is set.Dried the suction low-pressure boiler is set, though this method says that from the first law of thermodynamics used heat utilization rate is higher.But from the second law of thermodynamics, it is defective promptly utilizing angle to see from available energy, because dried suction product is low-pressure steam, and its generating thermal efficiency less than 20%; Same heat is as producing middle pressure steam, and the generating thermal efficiency can reach more than 30%.Second will be provided with two boilers, has not only increased investment, has also increased burden for production management.The 3rd, be to adopt special stainless steel because do the suction boiler tubes, stainless steel is afraid of chlorion, to water quality requirement chlorion＜0.5PPM, this has increased cost to water treatment.
Metallurgical off-gas acid-making has not only improved the concentration of sulfur dioxide now along with the height that does, particularly oxygen-rich smelting The Application of Technology of smelting technique level, and the relieving haperacidity level is reached a new high, and generally adopts double conversion double absorption relieving haperacidity technology; And also add waste heat boiler in the smelting outlet and come producing steam, quantity of steam is because of various metal smelt technological disparities, the standard that neither one is unified.But up to the present flue gas during smelting transforms and does the used heat of inhaling part and do not obtain utilization basically, and it utilizes method similar to pyrite-based sulfuric acid production.
Summary of the invention
In order to overcome above-mentioned deficiency, the object of the present invention is to provide a kind of method of relieving haperacidity Waste Heat Recovery of the rate of recovery that can improve used heat.
The technical solution adopted in the present invention is:
A. reclaim one section, two sections and the three sections SO that outlet is discharged of the converter in the industrial relieving haperacidity production process
3Gas with a part of heat, concrete scheme is: efflux the SO that is provided with on the passage with three sections outlets of converter at steam
3Gas is the low temperature superheater of thermal source and the SO that swaps out mouthful with converter II
3Gas is the low temperature superheater of thermal source; The SO that is discharged with the converter one section outlet
3Gas is the high temperature superheater of thermal source, and steam becomes 4.0MPa, 450 ℃ steam the most at last.
B. reclaim to do heat absorption recovery system high temperature and absorb the heat that is produced, on the boiler feedwater passage of reacting furnace outlet, utilize heat exchanger will do the heat absorption recovery system acid with the part heat pass to boiler feedwater.
The acid of described step b with the part heat concrete scheme of passing to boiler feedwater be: the heat exchanger that utilizes two series connection, and make the flow direction of boiler feedwater opposite with the flow direction of acid, divide the secondary preheating to boiler feedwater, when first heat exchanger, soft water is preheating to 100～108 ℃, when second heat exchanger, boiler feedwater is preheating to 200～210 ℃ to water again.
High temperature among the described step b absorbs and is meant that absorbing sour tower exit temperature reaches more than 150 ℃.
Described reacting furnace is the sulfur furnace of acid production with sulphur or the smelting furnace of metallurgical off-gas acid-making.For various metallurgical off-gas acid-makings, can utilize the dried high temperature absorption heat of inhaling to come preheating to smelt the outlet boiler feedwater.Other right is identical with " method of pyrite-based sulfuric acid production Waste Heat Recovery " right.(" troilite waste recovery method " patent applied for).As be provided with the middle low-temperature waste heat of electric precipitation in the electric precipitation outlet.
Operation principle: the present invention absorbs heat to reaction heat, the dried high temperature of inhaling in the reacting furnace, presses superheated steam during conversion generation heat all becomes.Establish the YHRS absorption system do inhaling, the used heat that high temperature is absorbed is used for preheating reacting furnace outlet boiler feedwater, divides two sections preheatings, and first section is utilized the high temperature absorption system to efflux sulfuric acid about 190 ℃ will to feed water and be preheating to 104 ℃ from 40 ℃; Second section is utilized about 104 ℃ of water preheats to 205 that recycle acid comes feed pump ℃, to the trans-utilization economizer with water preheat to 240 ℃.Obviously water does not become at the warm chlorine ion concentration, and unlike boiler, the water inlet chlorion is 0.5PPM, and stove water is wanted high one, two order of magnitude, because of chlorion will concentrate in boiler, discharges the balance that chlorion reaches chlorion by blowdown.Therefore, preheating feedwater chlorion is required low one, two order of magnitude of comparable HRS system, can arrive 5～50PPM.Will carry out appropriate reconstruction to conversion system, original conversion process is changed into IV II flow process from III II flow process, and second stage exit also will utilize the part heat to come heating steam, a mouthful SO only may swap out IV
3Temperature reduces, and increases the Waste Heat Recovery amount; At one section outlet high temperature superheater is set; Three sections outlets low temperature superheater is set, economizer and air preheater make SO
3Gas drops to 150～160 ℃ and enters the high temperature absorption tower; The reacting furnace operating temperature, because air has carried out preheating, temperature is brought up to about 1100 ℃ from 1000 ℃.
Beneficial effect of the present invention is: because the middle low-temperature waste heat that utilizes conversion and electric precipitation outlet flue gas during smelting to be provided with electric precipitation comes the air of preheating reacting furnace; Utilize and transform the high low temperature superheater of one section, three sections outlet used heat as steam, utilize a used heat of inhaling the high temperature absorption to come the preboiler feedwater, the used heat of all recovery all can generate 4.0Mpa, 450 ℃ middle pressure steam, and self need not consume steam whole heat recovery system, therefore institute's producing steam can all be used for generating electricity, or low-pressure steam all is defeated by user's use after the back pressure type generating, so greatly improved Waste Heat Recovery rate and utilization rate.
Description of drawings
The present invention is described in further detail below in conjunction with accompanying drawing.
Fig. 1 is that the present invention is to air heat and steam Waste Heat Recovery schematic flow sheet;
Fig. 2 is the Waste Heat Recovery schematic flow sheet of YRHS feedwater heating of the present invention.
Among the figure: 1, sulfur furnace; 2, air input passage; 3, drum; 4, with the SO of converter second stage exit
3Gas is the low temperature superheater of thermal source; 5, softened water pump; 6, with the SO of three sections outlets of converter
3Gas is the low temperature superheater of thermal source; 7, steam effluxes passage; 8, do the heat system that absorbs; 9, air preheater; 10, with the furnace gas be the preheater of thermal source; 11, give aquaporin; 12, low-temperature pre-heater; 13, high-temperature preheater; 14, the SO that is discharged with the converter one section outlet
3Gas is the high temperature superheater of thermal source; 15, economizer; 16, boiler; 17, converter; 18, converter II changes.
Specific embodiments
As shown in Figure 1, 2, the method for acid production with sulphur Waste Heat Recovery, this method may further comprise the steps:
A. one section of the converter 17 in the Recovered sulphur relieving haperacidity production process, two sections and three sections export the SO that discharged
3Gas with a part of heat, concrete scheme is: efflux the SO that is provided with on the passage 7 with three sections outlets of converter at steam
3Gas be thermal source low temperature superheater 6, with converter II change 18 the outlet SO
3The SO that gas is the low temperature superheater 4 of thermal source, discharged with the converter one section outlet
3Gas is the high temperature superheater 14 of thermal source, finally utilizes high temperature superheater 14 with SO
3Gas with a part of heat pass to steam, steam is become 4.0MPa, 450 ℃ steam.
B. reclaim and do the heat that the absorption of heat absorption recovery system 8 high temperature is produced, utilizing the heat exchanger of two series connection on the boiler feedwater passage 11 of sulfur furnace 1 outlet is low-temperature pre-heater 12, high-temperature preheater 13, and make the flow direction of feedwater opposite with the flow direction of acid, divide the secondary preheating to boiler feedwater, for the first time behind low-temperature pre-heater 12, soft water is preheating to 104 ℃, for the second time behind high-temperature preheater 13, water vapour is preheating to 204 ℃, water vapour further heats through economizer 15 then, and last water vapour is transferred in the gas bag 3 that links to each other with boiler 16.
The calculating of Waste Heat Recovery amount of the present invention: (is that the 200kt/a sulphuric acid output calculates with 25t/h).
Sulfur furnace outlet boiler: (comprising the invert atmosphere amounts of preheat) 5.91 * 10
7KJ/h, its heat can produce 32.89t/h, the saturated vapor of 4.0Mpa when 240 ℃ of water inlets.
Transform one section high temperature superheater: 1.36 * 10
7KJ/h
Transform the II mouthful low temperature superheater that swaps out: 1.85 * 10
6KJ/h
Transform three sections outlet low temperature superheaters: 1.13 * 10
7KJ/h
Three totals: 2.67 * 10
7KJ/h
Wherein 32.89t/h steam is heated to 450 ℃ of superheated steams from 250 ℃ of saturated vapors needs heat 1.57 * 10
7KJ/h
After-heat: 1.10 * 10
7KJ/h
After-heat can produce 450 ℃ of steam of 4.0Mpa by the method for 240 ℃ of spray desuperheatings, and injection flow rate is 4.84t/h, promptly increases steam production 4.8t/h, and the total steam production is 37.73t/h.
Doing suction high temperature absorption portion further specifies:
Doing suction high temperature absorption portion and can produce 0.60～1.00Mpa steam, 0.45～0.5t/t (acid), is 1.17 * 10 by calculating that like this high temperature absorption portion reclaims heat (establishing 40 ℃ of water temperatures)
6～1.30 * 10
6KJ/t (acid).For the 25t/h acid system, reclaim heat and should be: 2.93 * 10
7-3.25 * 10
7KJ/h.
With the outer sulfuric acid of discharging 192 ℃ of high temperature absorption portion, with 38m
3The soft water of/h is preheating to 104 ℃ from 40 ℃, advances oxygen-eliminating device, utilizes heat to be: 1.02 * 10
7KJ/h.Utilize high temperature to absorb water that recycle acid will come from boiler feed pump again and be preheating to 205 ℃ from 104 ℃, advance to transform economizer, utilize heat to be: 1.61 * 10
7KJ/h adds up to and utilizes heat: 2.63 * 10
7KJ/h still has 3.00 * 10
6～6.20 * 10
6The kJ/h heat does not use up, quite the heat of 0.60Mpa1 saturated vapor 1.10～2.20t/h steam.It is a small amount of more than needed that this illustrates that the low potential temperature heat of whole acid production with sulphur process comes the preheating feedwater still to have, and presses superheated steam during this part heat can not become.How does this part heat utilize? can remove molten sulphur by the hot water circuit mode.190 ℃ of hot water past, 160 ℃ of hot water were returned, and had utilized this part heat.
Claims (4)
1. the method for a relieving haperacidity Waste Heat Recovery, it is characterized in that: this method may further comprise the steps:
A. reclaim one section, two sections and the three sections SO that outlet is discharged of the converter in the relieving haperacidity production process
3Gas with a part of heat, concrete scheme is: efflux the SO that is provided with on the passage with three sections outlets of converter at steam
3The SO that gas is the low temperature superheater of thermal source, swap out mouthful with converter II
3Gas is the low temperature superheater of thermal source; The SO that is discharged with the converter one section outlet
3Gas is the high temperature superheater of thermal source, and steam becomes 4.0MPa, 450 ℃ steam the most at last;
B. reclaim to do heat absorption recovery system high temperature and absorb the heat that is produced, on the boiler feedwater passage of reacting furnace outlet, utilize heat exchanger will do the heat absorption recovery system acid with the part heat pass to boiler feedwater.
2. the method for relieving haperacidity Waste Heat Recovery according to claim 1, it is characterized in that: the acid of described step b with the part heat concrete scheme of passing to boiler feedwater be: the heat exchanger that utilizes two series connection, and make the flow direction of boiler feedwater opposite with the flow direction of acid, divide the secondary preheating to boiler feedwater, when first heat exchanger, soft water is preheating to 100～108 ℃, and when second heat exchanger, boiler feedwater is preheating to 200～210 ℃ to water again.
3. the method for relieving haperacidity Waste Heat Recovery according to claim 1 is characterized in that: the reacting furnace among the described step b is the incinerator of acid production with sulphur or the smelting furnace of metallurgical off-gas acid-making.
4. the method for relieving haperacidity Waste Heat Recovery according to claim 1 is characterized in that: high temperature among the described step b absorbs and is meant that absorbing the temperature that acid goes out tower reaches more than 150 ℃.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100423683A CN101706095B (en) | 2009-09-02 | 2009-09-02 | Method for recovering acid making waste heat |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100423683A CN101706095B (en) | 2009-09-02 | 2009-09-02 | Method for recovering acid making waste heat |
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| CN101706095A CN101706095A (en) | 2010-05-12 |
| CN101706095B true CN101706095B (en) | 2011-07-20 |
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Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102556982B (en) * | 2011-12-30 | 2015-04-22 | 凯密迪公司 | Low-temperature exhaust heat system for sulfuric acid recovering device and application of low-temperature exhaust heat system |
| CN104728825A (en) * | 2013-12-18 | 2015-06-24 | 招远市招金金合科技有限公司 | Low temperature exhaust heat utilization system and method |
| CN111841310A (en) * | 2020-07-02 | 2020-10-30 | 宁波科新化工工程技术有限公司大连分公司 | Acid making waste heat utilization and tail gas comprehensive treatment process and device |
| CN112696963A (en) * | 2020-12-07 | 2021-04-23 | 中国恩菲工程技术有限公司 | Low-temperature waste heat recovery system of smelting flue gas acid making system |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5130112A (en) * | 1990-03-23 | 1992-07-14 | Monsanto Company | Method for recovering high grade process energy from a contact sulfuric acid process |
| CN1136801A (en) * | 1994-10-13 | 1996-11-27 | 埃德默斯顿公司 | Reactor container, plant and process for production of sulfuric acid |
| DE19522927A1 (en) * | 1995-06-23 | 1997-01-02 | Sued Chemie Ag | Concentrated sulphuric acid is manufactured in a process with two contact stages in the presence of steam |
| US6279514B1 (en) * | 2000-08-07 | 2001-08-28 | Timothy J. Browder | Method of recovering heat in sulfuric acid production plant |
| CN1603229A (en) * | 2004-10-12 | 2005-04-06 | 南化集团研究院 | Humid gas conversion and heat reclamation acid preparation technique |
| CN1740090A (en) * | 2005-06-16 | 2006-03-01 | 洪博志 | Low temperature heat energy recovering method and system for the first absorption section in sulfuric acid production |
| CN1751984A (en) * | 2004-09-20 | 2006-03-29 | 中国石油天然气股份有限公司 | Process for producing sulfuric acid by high-temperature cracking of alkylation waste sulfuric acid |
| CN101481095A (en) * | 2009-02-05 | 2009-07-15 | 中国石化集团南京设计院 | Process for recovering and utilizing sulfuric acid manufacture energy |
-
2009
- 2009-09-02 CN CN2009100423683A patent/CN101706095B/en not_active Expired - Fee Related
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5130112A (en) * | 1990-03-23 | 1992-07-14 | Monsanto Company | Method for recovering high grade process energy from a contact sulfuric acid process |
| CN1136801A (en) * | 1994-10-13 | 1996-11-27 | 埃德默斯顿公司 | Reactor container, plant and process for production of sulfuric acid |
| DE19522927A1 (en) * | 1995-06-23 | 1997-01-02 | Sued Chemie Ag | Concentrated sulphuric acid is manufactured in a process with two contact stages in the presence of steam |
| US6279514B1 (en) * | 2000-08-07 | 2001-08-28 | Timothy J. Browder | Method of recovering heat in sulfuric acid production plant |
| CN1751984A (en) * | 2004-09-20 | 2006-03-29 | 中国石油天然气股份有限公司 | Process for producing sulfuric acid by high-temperature cracking of alkylation waste sulfuric acid |
| CN1603229A (en) * | 2004-10-12 | 2005-04-06 | 南化集团研究院 | Humid gas conversion and heat reclamation acid preparation technique |
| CN1740090A (en) * | 2005-06-16 | 2006-03-01 | 洪博志 | Low temperature heat energy recovering method and system for the first absorption section in sulfuric acid production |
| CN101481095A (en) * | 2009-02-05 | 2009-07-15 | 中国石化集团南京设计院 | Process for recovering and utilizing sulfuric acid manufacture energy |
Non-Patent Citations (4)
| Title |
|---|
| 俞向东.硫磺制酸废热回收及利用.《硫酸工业》.2000,(第03期),第43-46,56页. * |
| 孟福泉等.80kt_a硫磺制酸系统的废热回收利用.《硫酸工业》.2000,(第4期),第34-36页. * |
| 申屠华德等.硫铁矿制酸干吸转化工序的节能和废热利用.《硫酸工业》.2008,(第02期),第26-31页. * |
| 陶波.硫磺制酸废热回收系统蒸汽参数的选择.《硫酸工业》.2007,(第4期),第26-28页. * |
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