CN201501791U - Industrial acid making waste heat recovery system - Google Patents
Industrial acid making waste heat recovery system Download PDFInfo
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- CN201501791U CN201501791U CN2009201946496U CN200920194649U CN201501791U CN 201501791 U CN201501791 U CN 201501791U CN 2009201946496 U CN2009201946496 U CN 2009201946496U CN 200920194649 U CN200920194649 U CN 200920194649U CN 201501791 U CN201501791 U CN 201501791U
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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 utility model discloses an industrial acid making waste heat recovery system, which comprises an air input passage, a water feeding passage, a steam discharge passage, an air pocket on a boiler, a reaction furnace, a converter and a high-temperature dry absorption system. Air enters the reaction furnace through the air input passage, and the water feeding passage and the steam discharge passage are communicated with the air pocket on the boiler. The industrial acid making waste heat recovery system is characterized in that the steam discharge passage is sequentially provided with a low-temperature superheater which can change steam into medium pressure steam and utilize SO3 gas of an outlet of a third section of the converter as a heat source, a low-temperature superheater which utilizes SO3 gas of an outlet of a second section of the converter as a heat source and a high-temperature super heater which utilizes SO3 gas discharged by an outlet of a first section of the converter as a heat source, and the reaction furnace is a sulfur burner for sulfuric acid production from sulfur-burning or a smelting furnace for smelter acid production. Through preheating fed water and air entering the furnace by aid of purifying, converting and dry absorbing low and medium temperature waste heat, the industrial acid making waste heat recovery system greatly increases waste heat recovery rate and utilization, thereby reducing cost and saving energy.
Description
Technical field
The utility model relate to a kind of sulfuric acid industry waste heat recovery, utilize system, refer in particular to the Waste Heat Recovery System (WHRS) of acid production with sulphur or smelting acid making.
Background technology
Modern vitriol works, particularly acid production with sulphur not only as production vitriolic factory, and regard a former factory of energy 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.OMpa is set behind sulfur furnace; Utilize the used heat of conversion process, the superheated vapour with steam heating to 450 ℃ promptly adds low temperature superheater four sections outlets, increases temperature superheater at one section outlet, and the saturation steam that boiler is come out is heated to be 450 ℃ superheated vapour; 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, oiler feed 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) saturation steam.Waste heat utilization technology is greatly improved.This technology domesticizes, but producing steam 0.45t/t (acid) 0.60～1.0Mpa saturation steam.Wherein 0.2t/t acid low-pressure steam is used for the deoxygenator 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 dried the suction low pressure boiler is set; In conversion superheater and economizer are set.Though this method says that from the first law of thermodynamics used heat utilization ratio 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 thermo-efficiency less than 20%; Same heat is as producing middle pressure steam, and generating thermo-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 sulfurous gas now along with the height that does, particularly oxygen-rich smelting The Application of Technology of smelting technology level, and the relieving haperacidity level is reached a new high, common employing 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 smelting technological disparities, the standard that none 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.
The utility model content
In order to overcome above-mentioned deficiency, the utility model purpose is to provide a kind of used heat that utilizes purification, transforms and do the low middle temperature of suction to feed water, go into stove preheating of air and heating steam, thereby improves the industrial relieving haperacidity Waste Heat Recovery System (WHRS) of waste heat recovery rate and utilization ratio.
To achieve these goals, the technical solution adopted in the utility model is: industrial relieving haperacidity Waste Heat Recovery System (WHRS), include air input passage, efflux gas bag, Reaktionsofen, the convertor on passage, the boiler for aquaporin, steam and do suction high temperature absorption system, air enters Reaktionsofen by air input passage, efflux passage for aquaporin, steam and be connected with gas bag on the boiler, it is characterized in that: described steam effluxes and is provided with the SO with three sections outlets of convertor that steam can be become middle pressure steam on the passage successively
3Gas is the low temperature superheater of thermal source, with the SO of convertor second stage exit
3The SO that gas is the low temperature superheater of thermal source, discharged with the convertor one section outlet
3Gas is the high temperature superheater of thermal source.
Describedly be provided with low-temperature pre-heater and high-temperature preheater to aquaporin, low-temperature pre-heater and high-temperature preheater are serially connected in to do to be inhaled in the high temperature absorption system.
The interchanger that to be provided with 150～160 ℃ of sulfur trioxide gas after transforming on the described air input passage successively be the thermal source medium, be the interchanger of thermal source medium with the furnace gas of electric precipitation outlet or whirlwind outlet.
Described to also being provided with economizer on the aquaporin, the SO that described economizer is discharged with low temperature superheater
3Gas is the thermal source medium.
Described Reaktionsofen is the sulfur furnace of acid production with sulphur or the smelting furnace of metallurgical off-gas acid-making.
The beneficial effects of the utility model: owing to be the interchanger of thermal source medium at interchanger that to be provided with 150～160 ℃ of sulfur trioxide gas after transforming on the air input passage successively be the thermal source medium, with the furnace gas of electric precipitation outlet or whirlwind outlet, cryogenic used heat has obtained efficient recovery and has made full use of in making, thereby reduced cost, saved the energy; Owing on to aquaporin, be provided with low-temperature pre-heater and high-temperature preheater successively, and make dry up to suck back and receive thermal device used heat is provided, simultaneously under the effect of two low temperature superheaters and a high temperature superheater, one section of convertor, two sections, three sections exit portion heats are passed to steam, finally 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 ratio.
Description of drawings
The utility model is described in further detail below in conjunction with accompanying drawing.
Fig. 1 is the interface chart of air input channel of the present utility model and vapour passage waste heat recovery;
Fig. 2 is an interface chart of giving the aquaporin waste heat recovery of the present utility model.
Among the figure: 1, Reaktionsofen; 2, air input passage; 3, drum; 4, with the SO of convertor 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 convertor
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 convertor one section outlet
3Gas is the high temperature superheater of thermal source; 15, economizer; 16, boiler; 17, convertor.
Embodiment
As shown in Figure 1, 2, now be that example is illustrated the utility model with the acid production with sulphur, the acid production with sulphur Waste Heat Recovery System (WHRS), include air input passage 2, efflux gas bag 3, Reaktionsofen 1, convertor 17 and the softened water pump 5 on passage 7, the boiler 16, the dried high temperature absorption system 8 of inhaling for aquaporin 11, steam, air enters Reaktionsofen 1 by air input passage 2, and Reaktionsofen 1 is a sulfur furnace; Softened water pump 5 flows to boiler 16 with water by giving aquaporin 11, steam in the gas bag 3 on the boiler 16 effluxes passage 7 by steam and the discharge of heating back formation middle pressure steam is used, and described steam effluxes and is provided with the SO with 17 3 sections outlets of convertor that steam can be become on the passage 7 successively
3Gas is the low temperature superheater 6 of thermal source, with the SO of convertor 17 second stage exits
3The SO that gas is the low temperature superheater 4 of thermal source, discharged with convertor 17 one section outlets
3Gas is the high temperature superheater 14 of thermal source.The described aquaporin 11 of giving is provided with low-temperature pre-heater 12, high-temperature preheater 13 and economizer (15), and low-temperature pre-heater 12 and high-temperature preheater 13 are serially connected in to do inhales in the high temperature absorption system 8 SO that economizer (15) is discharged with low temperature superheater (6)
3Gas is the thermal source medium.
Principle of work
The present invention is exactly that the used heat that will make full use of low middle temperature increases steam production.Increase steam production by following approach.
1, establish the YHRS absorption system do inhaling, the used heat that high temperature is absorbed is used for preheating sulfur furnace outlet oiler feed, 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 service 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 is spissated 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.
2, 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 8O
3Gas drops to 150～160 ℃ and enters the high temperature absorption tower; The sulfur furnace service temperature, because air has carried out preheating, temperature is brought up to about 1100 ℃ from 1000 ℃.
By such flow process, waste heat is: (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 saturation steam 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 vapours from 250 ℃ of saturation steams needs heat 1.57 * 10
7KJ/h
Surplus heat: 1.10 * 10
7KJ/h
Surplus 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 deoxygenator, utilizes heat to be: 1.02 * 10
7KJ/h.Utilize high temperature to absorb water that recycle acid will come from boiler feedpump 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 0.60Mpal saturation steam 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 vapour during this part heat can not become, and can remove molten sulphur by the hot water circulation mode.190 ℃ of hot water past, 160 ℃ of hot water were returned, and had utilized this part heat.
Claims (5)
1. industrial relieving haperacidity Waste Heat Recovery System (WHRS), include air input passage (2), efflux gas bag (3), Reaktionsofen (1), the convertor (17) on passage (7), the boiler (16) for aquaporin (11), steam and do suction high temperature absorption system (8), air enters Reaktionsofen (1) by air input passage (2), efflux passage (7) for aquaporin (11), steam and be connected with gas bag (3) on the boiler (16), it is characterized in that: described steam effluxes and is provided with the SO with (17) three sections outlets of convertor that steam can be become middle pressure steam on the passage (7) successively
3Gas is the low temperature superheater (6) of thermal source, with the SO of convertor (17) second stage exit
3The SO that gas is the low temperature superheater (4) of thermal source, discharged with convertor (17) one section outlet
3Gas is the high temperature superheater (14) of thermal source.
2. industrial relieving haperacidity Waste Heat Recovery System (WHRS) according to claim 1, it is characterized in that: the described aquaporin (11) of giving is provided with low-temperature pre-heater (12) and high-temperature preheater (13), and low-temperature pre-heater (12) and high-temperature preheater (13) are serially connected in to do to be inhaled in the high temperature absorption system (8).
3. industrial relieving haperacidity Waste Heat Recovery System (WHRS) according to claim 1 is characterized in that: the interchanger (9) that to be provided with 150～160 ℃ of sulfur trioxide gas after transforming on the described air input passage (2) successively be the thermal source medium, be the interchanger (10) of thermal source medium with the furnace gas of electric precipitation outlet or whirlwind outlet.
4. industrial relieving haperacidity Waste Heat Recovery System (WHRS) according to claim 1 is characterized in that: described giving on the aquaporin (11) also is provided with economizer (15), the SO that described economizer (15) is discharged with low temperature superheater (6)
3Gas is the thermal source medium.
5. industrial relieving haperacidity Waste Heat Recovery System (WHRS) according to claim 1 is characterized in that: described Reaktionsofen (1) is the smelting furnace of the sulfur furnace of acid production with sulphur or metallurgical off-gas acid-making.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009201946496U CN201501791U (en) | 2009-09-11 | 2009-09-11 | Industrial acid making waste heat recovery system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009201946496U CN201501791U (en) | 2009-09-11 | 2009-09-11 | Industrial acid making waste heat recovery system |
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| Publication Number | Publication Date |
|---|---|
| CN201501791U true CN201501791U (en) | 2010-06-09 |
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| CN2009201946496U Expired - Fee Related CN201501791U (en) | 2009-09-11 | 2009-09-11 | Industrial acid making waste heat recovery system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107289428A (en) * | 2017-07-11 | 2017-10-24 | 贺照刚 | For burning the device and method that sulphur UTILIZATION OF VESIDUAL HEAT IN and steam are produced in bromine water production |
| 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 |
-
2009
- 2009-09-11 CN CN2009201946496U patent/CN201501791U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107289428A (en) * | 2017-07-11 | 2017-10-24 | 贺照刚 | For burning the device and method that sulphur UTILIZATION OF VESIDUAL HEAT IN and steam are produced in bromine water production |
| 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 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20100609 Termination date: 20140911 |
|
| EXPY | Termination of patent right or utility model |