CN203754422U - Device for increasing heat recovery efficiency in process for preparing acid from mine or smelting gas - Google Patents
Device for increasing heat recovery efficiency in process for preparing acid from mine or smelting gas Download PDFInfo
- Publication number
- CN203754422U CN203754422U CN201420153638.4U CN201420153638U CN203754422U CN 203754422 U CN203754422 U CN 203754422U CN 201420153638 U CN201420153638 U CN 201420153638U CN 203754422 U CN203754422 U CN 203754422U
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- China
- Prior art keywords
- waste heat
- heat boiler
- feed water
- middle pressure
- well heater
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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 a device for increasing heat recovery efficiency in a process for preparing acid from mine or smelting gas, belonging to the technical field of residual or waste heat recovery. The device is internally provided with a medium-pressure waste heat boiler feed water heater, a desalted water heater and an oxygen extractor, wherein an input end and an output end of the medium-pressure waste heat boiler feed water heater are connected with an evaporator feed water heater and the desalted water heater respectively in sequence; the oxygen extractor is connected with three water pumps which are a low-pressure feed water pump, a jet water pump and a medium-pressure feed water pump respectively, the low-pressure feed water pump is connected with the evaporator feed water heater, the jet water pump is connected with a mixer, and the medium-pressure feed water pump is connected with the other input end of the medium-pressure waste heat boiler feed water heater. According to the device and a method, feed water of a medium-pressure waste heat boiler behind a boiling furnace is heated by virtue of waste heat due to high acid-producing temperature in a low-temperature heat recovery system on a dry absorption section, so that the heat recovery efficiency of a process system for preparing acid from mine or smelting gas is improved.
Description
Technical field
The utility model belongs to waste heat or waste heat recovery technical field, is specifically related to a kind of device that improves ore deposit or smelting gas acid preparing heat organic efficiency.
Background technology
Ore deposit or smelting gas relieving haperacidity industry are equipped with the waste heat that middle pressure waste heat boiler reclaims high-temperature flue gas after fluidizing furnace (or smelting furnace) both at home and abroad at present, at conversion section, be equipped with the heat that economizer reclaims conversion reaction (Sulphur Dioxide is sulphur trioxide), at the more existing devices of dry absorption section, be provided with low-temperature heat recovery system, its technical process is containing S0 by economizer exit
3process gas send into high temperature absorption tower, SO3 in process gas is sprayed sulfuric acid absorption in tower, the heat that absorption reaction heat discharges improves acid temperature, high temperature concentrated acid is pumped into vaporizer by high temperature circulation and produces low-pressure steam, recycle acid temperature enters mixing tank after reducing and mixes to reduce concentration with water or low-concentration sulfuric acid, then sends into the circulation of high temperature absorption tower again and absorbs SO
3; Recycle acid goes out on the pipeline of vaporizer to pick out and produce acid tube road, and system is produced acid through evaporator feedwater well heater preheating low pressure feed water, then passes through de-salted water well heater preheating de-salted water, produces sour temperature and is down to 100 ℃～140 ℃ and sends dry absorption section back to.In such heat recovery system, produce sour temperature higher, still have amount of heat not utilized.
Utility model content
The purpose of this utility model is further to improve for above-mentioned technical problem the heat recovery rate of dry absorption section low-temperature heat recovery system, improves the steam generating capacity of ore deposit or smelting gas sulphuric acid plant.
The purpose of this utility model can be achieved through the following technical solutions:
A kind of device that improves ore deposit or smelting gas acid preparing heat organic efficiency, this device is provided with middle pressure waste heat boiler feedwater heating apparatus, de-salted water well heater and deoxygenator, and an input terminus in described middle pressure waste heat boiler feedwater heating apparatus is connected with de-salted water well heater with evaporator feedwater well heater respectively successively with an output terminal; Described deoxygenator is connected with three water pumps, respectively low pressure feed water pump, jet pump and middle pressure service pump, low pressure feed water pump is connected with evaporator feedwater well heater, and jet pump is connected with mixing tank, and middle pressure service pump is connected with another input terminus of middle pressure waste heat boiler feedwater heating apparatus; Another output terminal of middle pressure waste heat boiler feedwater heating apparatus is connected with waste heat boiler.
This device also comprises economizer, and process gas enters high temperature absorption tower after entering economizer again, and another output terminal of middle pressure waste heat boiler feedwater heating apparatus is connected with waste heat boiler by economizer.
Described de-salted water well heater is provided with 2 passages, is respectively sulfuric acid output passage and de-salted water input channel.
A method that improves ore deposit or smelting gas acid preparing heat organic efficiency, the method adopts above-mentioned raising ore deposit or smelts the device of gas acid preparing heat organic efficiency, and the method comprises the following steps:
1) process gas enters high temperature absorption tower and reacts the high vitriol oil of generation with the recycle acid in high temperature absorption tower, the high vitriol oil generating enters high temperature circulation groove after collecting at the bottom of the tower on high temperature absorption tower, after the pressurization of high temperature circulation pump, send into vaporizer, now obtain respectively low-pressure steam and produce acid, the low-pressure steam obtaining adopts pipeline output;
2) part for product acid step 1) being obtained enters in mixing tank mixes with water or low-concentration sulfuric acid, returns to high temperature absorption tower, the SO3 in circulation absorption technique gas after mixing again; System is produced sour another part and from the circulation acid tube of evaporator outlet, is picked out to be introduced in evaporator feedwater well heater and heat low pressure feed water, and then enter to add in middle pressure waste heat boiler feedwater heating apparatus and hanker pressing feedwater, finally enter in de-salted water well heater and heat de-salted water, the system obtaining from de-salted water well heater is produced acid and is exported from sulfuric acid output passage;
3) de-salted water, step 2) is inputted by de-salted water input channel, after de-salted water heater heats, send into and in deoxygenator, carry out thermal de-aeration to obtain temperature be 104 ℃ of deaerated water, by low pressure feed water pump, will after the low pressure feed water pressurization of 104 ℃, send in evaporator feedwater well heater and heat up, after intensification, send in vaporizer, the low-pressure steam obtaining is exported by pipeline; By jet pump, the dilution water of 104 ℃ is sent in mixing tank, thereby the acid of reduction sulfuric acid is dense; By middle pressure service pump, the feedwater pressurization of 104 ℃ is sent in middle pressure waste heat boiler feedwater heating apparatus and heated up, the feedwater after heating up is sent in waste heat boiler.
In step 1), the temperature of process gas is 220～280 ℃, and producing sour temperature is 170～210 ℃, and the pressure of low-pressure steam is 0.6～1Mpa.
Step 2) part for the product acid described in, for producing 70%～90% of sour total mass, is produced sour another part for producing 10%～30% of sour total mass.
Step 2) in, system is produced sour another part and from the circulation acid tube of evaporator outlet, is picked out to be introduced in evaporator feedwater well heater and heat low pressure feed water, produce sour temperature and be reduced to 160～200 ℃, enter again in middle pressure waste heat boiler feedwater heating apparatus and add and hanker pressing feedwater, produce sour temperature and be reduced to 120～160 ℃, finally enter in de-salted water well heater and heat the de-salted water of 20 ℃, system is produced when sour temperature is down to 50～110 ℃ and is exported from sulfuric acid output passage.
In step 3), de-salted water is through de-salted water heater heats, and the temperature of de-salted water is to send into deoxygenator after 60～100 ℃; Water temperature in evaporator feedwater well heater is to send in vaporizer after 150～190 ℃; Water temperature in middle pressure waste heat boiler feedwater heating apparatus is to send in waste heat boiler after 140～180 ℃.
In some embodiments, in step 1), process gas can also be sent into the temperature to process gas after economizer and enter high temperature absorption tower from 220～280 ℃ are cooled to 150～210 ℃; In step 3), by middle pressure service pump, the feedwater pressurization of 104 ℃ is sent in middle pressure waste heat boiler feedwater heating apparatus and is warming up to 140～180 ℃, the feedwater after heating up is sent in waste heat boiler by economizer.
Process gas described in technical solutions of the utility model is that this area produces the gas containing sulphur trioxide that sulfuric acid is commonly used.
The feedwater that the utility model utilizes dry absorption section low-temperature heat recovery system comparatively high temps to produce medium pressure boiler waste heat boiler after sour waste-heat fluidizing furnace, has improved ore deposit or has smelted the efficiency that gas acid-making process system thermal reclaims.
The beneficial effects of the utility model:
1, in technical solutions of the utility model, utilize dry absorption section low-temperature heat recovery system to send high-temperature sulfuric acid heated feed water in middle pressure waste heat boiler feedwater heating apparatus outside, middle pressure waste heat boiler feed temperature is mentioned to 160 ± 20 ℃ by 104 ℃, enter again economizer heating, then send into and in waste heat boiler, produce steam, make the steam production of waste heat boiler improve 10% left and right, thereby make 1 ton of total steam generating capacity of sulfuric acid of the every production of whole sulphuric acid plant bring up to 1.7t left and right from 1.5t.
2, the medium pressure boiler feedwater of pressing waste heat boiler feedwater heating apparatus to be warming up to 160 ± 20 ℃ in technical solutions of the utility model in process also can directly enter waste heat boiler without economizer, in such cases, the steam production of waste heat boiler is substantially unchanged, but by 180 ℃ of left and right, bring up to 250 ℃ of left and right owing to entering the temperature of absorption section low-temperature heat recovery system process gas, the heat of process gas is recycled acid and absorbs in high temperature absorption tower, recycle acid temperature is further raise, so the steam generating capacity of absorption section low-temperature heat recovery system vaporizer sulfuric acid per ton increases 0.2t left and right.
3, in technical solutions of the utility model, dry absorption section low-temperature heat recovery system is sent high-temperature sulfuric acid outside and also can be heated other medium, and the temperature of sending sulfuric acid outside is further reduced, and reclaims more heats.
Accompanying drawing explanation
Fig. 1 is process flow diagram of the present utility model.
1-high temperature absorption tower, 2-high temperature circulation groove, 3-mixing tank, 4-economizer, 5-high temperature circulation pump, 6-vaporizer, 7-evaporator feedwater well heater, in 8-, press waste heat boiler feedwater heating apparatus, 9-de-salted water well heater, 10-low pressure feed water pump, 11-jet pump, in 12-, press service pump, 13-deoxygenator, 14-waste heat boiler.
Fig. 2 is process flow diagram of the present utility model
1-high temperature absorption tower, 2-high temperature circulation groove, 3-mixing tank, 5-high temperature circulation pump, 6-vaporizer, 7-evaporator feedwater well heater, presses waste heat boiler feedwater heating apparatus in 8-, 9-de-salted water well heater, 10-low pressure feed water pump, 11-jet pump, presses service pump in 12-, 13-deoxygenator, 14-waste heat boiler.
Embodiment
Below in conjunction with embodiment, the utility model is described in further detail, but protection domain of the present utility model is not limited to this:
Embodiment 1
As shown in Figure 1, by temperature, be the SO of 250 ± 30 ℃
3process gas enters economizer 4, described SO
3the temperature of process gas enters high temperature absorption tower 1 after being down to 180 ± 30 ℃, recycle sulfuric acid and the SO of high temperature absorption tower 1 top spray
3it is that 220 ℃ of left and right systems are produced acid that reaction generates temperature, and system is produced acid and after tower bottom collects, flowed into high temperature circulation groove 2, sends into vaporizer 6 produce the low-pressure steam that pressure is 0.8 ± 0.2MPa through 5 pressurizations of high temperature circulation pump, and the low-pressure steam obtaining adopts pipeline output; System is produced acid and is cooled to after 190 ± 20 ℃ through vaporizer 6, thereby the system that massfraction is 90% is produced acid and is sent into the acid of the dilution water sent into squirt pump in mixing tank 3 or lower concentration and mixes and make sour concentration reduction, return to again afterwards high temperature absorption tower 1, the SO in circulation absorption technique gas
3;
Massfraction is that 10% system is produced acid and picked out from the branch of the circulation acid tube of vaporizer 6 outlets, first send into the low pressure boiler feedwater of 104 ℃ of evaporator feedwater well heater 7 heating, system is produced and after sour temperature is down to 180 ± 20 ℃, is entered 104 ℃ of medium pressure boilers feedwater of middle pressure waste heat boiler feedwater heating apparatus 8 heating, system is produced and after sour temperature is down to 140 ± 20 ℃, is entered de-salted water well heater 9 heating normal temperature de-salted waters again, system is produced sour temperature and is down to after 80 ± 30 ℃, adopts the output of sulfuric acid output passage;
Normal temperature de-salted water is introduced into preheating in de-salted water well heater 9, and de-salted water temperature is sent into deoxygenator 13 and carried out thermal de-aeration after being increased to 80 ± 20 ℃, and deoxygenator 13 outlets arrange respectively low pressure feed water pump 10, jet pump 11 and middle pressure service pump 12; After the low pressure feed water pressurization that low pressure feed water pump 10 will 104 ℃, send in evaporator feedwater well heater 7, and send into vaporizer 6 after water is heated to 170 ± 20 ℃ to produce 0.8 ± 0.2MPa low-pressure steam; Middle pressure service pump 12 is sent into the middle pressure feedwater of 104 ℃ in middle pressure waste heat boiler feedwater heating apparatus 8, after being increased to 160 ± 20 ℃, middle pressure feed temperature by entering again in waste heat boiler 14 after economizer 4, use this flow process can make the steam generating capacity of the acid per ton of waste heat boiler improve 13% left and right.
Embodiment 2
As shown in Figure 2, by temperature, be the SO of 250 ± 30 ℃
3process gas directly enters high temperature absorption tower 1, recycle sulfuric acid and the SO of high temperature absorption tower 1 top spray
3it is that 230 ℃ of left and right systems are produced acid that reaction generates temperature, and system is produced acid and after tower bottom collects, flowed into high temperature circulation groove 2, sends into vaporizer 6 produce the low-pressure steam that pressure is 0.8 ± 0.2MPa through 5 pressurizations of high temperature circulation pump, and the low-pressure steam obtaining adopts pipeline output; System is produced sour vaporizer 6 and is cooled to after 190 ± 20 ℃, thereby the system that massfraction is 70% is produced acid and is sent into the acid of the dilution water sent into squirt pump in mixing tank 3 or lower concentration again and mixes and make sour concentration reduction, return to again afterwards high temperature absorption tower 1, the SO in circulation absorption technique gas
3;
Massfraction is that 30% system is produced acid and picked out from the branch of the circulation acid tube of vaporizer 6 outlets, first send into the low pressure boiler feedwater of 104 ℃ of evaporator feedwater well heater 7 heating, system is produced and after sour temperature is down to 180 ± 20 ℃, is entered 104 ℃ of medium pressure boilers feedwater of middle pressure waste heat boiler feedwater heating apparatus 8 heating, system is produced after sour temperature is down to 140 ± 20 ℃ and is entered de-salted water well heater 9 heating normal temperature de-salted waters again, and system is produced sour temperature and is down to 80 ± 30 ℃;
Normal temperature de-salted water is introduced into preheating in de-salted water well heater 9, and de-salted water temperature is sent into deoxygenator 13 and carried out thermal de-aeration after being increased to 80 ± 20 ℃, and deoxygenator 13 outlets arrange respectively low pressure feed water pump 10, jet pump 11 and middle pressure service pump 12; After the low pressure feed water pressurization that low pressure feed water pump 10 will 104 ℃, send in evaporator feedwater well heater 7, and send into vaporizer 6 after water is heated to 170 ± 20 ℃ to produce 0.8 ± 0.2MPa low-pressure steam; Middle pressure service pump 12 is sent into the middle pressure feedwater of 104 ℃ in middle pressure waste heat boiler feedwater heating apparatus 8, after being increased to 160 ± 20 ℃, middle pressure feed temperature directly enters in waste heat boiler 14, now, the steam generating capacity of waste heat boiler is substantially unchanged, but because steamer 6 import recycle acid temperature improve, can make the steam generating capacity of dry absorption section low-temperature heat recovery system acid per ton bring up to 0.5t from 0.3t.
Claims (4)
1. one kind is improved ore deposit or smelts the device of gas acid preparing heat organic efficiency, it is characterized in that: this device is provided with middle pressure waste heat boiler feedwater heating apparatus (8), de-salted water well heater (9) and deoxygenator (13), an input terminus in described middle pressure waste heat boiler feedwater heating apparatus (8) is connected with de-salted water well heater (9) with evaporator feedwater well heater (7) respectively successively with an output terminal; Described deoxygenator (13) is connected with three water pumps, respectively low pressure feed water pump (10), jet pump (11) and middle pressure service pump (12), low pressure feed water pump (10) is connected with evaporator feedwater well heater (7), jet pump (11) is connected with mixing tank (3), and middle pressure service pump (12) is connected with another input terminus of middle pressure waste heat boiler feedwater heating apparatus (8).
2. the device of raising according to claim 1 ore deposit or smelting gas acid preparing heat organic efficiency, is characterized in that: another output terminal of middle pressure waste heat boiler feedwater heating apparatus (8) is connected with waste heat boiler (14).
3. the device of raising according to claim 1 and 2 ore deposit or smelting gas acid preparing heat organic efficiency, is characterized in that: this device also comprises economizer (4), and process gas enters high temperature absorption tower (1) after entering economizer (4) again; Another output terminal of middle pressure waste heat boiler feedwater heating apparatus (8) is connected with waste heat boiler (14) by economizer (4).
4. the device of raising according to claim 1 ore deposit or smelting gas acid preparing heat organic efficiency, is characterized in that: described de-salted water well heater (9) is provided with 2 passages, is respectively sulfuric acid output passage and de-salted water input channel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420153638.4U CN203754422U (en) | 2014-03-31 | 2014-03-31 | Device for increasing heat recovery efficiency in process for preparing acid from mine or smelting gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420153638.4U CN203754422U (en) | 2014-03-31 | 2014-03-31 | Device for increasing heat recovery efficiency in process for preparing acid from mine or smelting gas |
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| Publication Number | Publication Date |
|---|---|
| CN203754422U true CN203754422U (en) | 2014-08-06 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420153638.4U Withdrawn - After Issue CN203754422U (en) | 2014-03-31 | 2014-03-31 | Device for increasing heat recovery efficiency in process for preparing acid from mine or smelting gas |
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| CN (1) | CN203754422U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103896219A (en) * | 2014-03-31 | 2014-07-02 | 南京海陆化工科技有限公司 | Device and method for improving recovery efficiency of ore or smelting gas acid-making heat |
-
2014
- 2014-03-31 CN CN201420153638.4U patent/CN203754422U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103896219A (en) * | 2014-03-31 | 2014-07-02 | 南京海陆化工科技有限公司 | Device and method for improving recovery efficiency of ore or smelting gas acid-making heat |
| CN103896219B (en) * | 2014-03-31 | 2015-12-09 | 南京海陆化工科技有限公司 | A kind of device and method improving ore deposit or smelt gas acid preparing heat organic efficiency |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20140806 Effective date of abandoning: 20151209 |
|
| C25 | Abandonment of patent right or utility model to avoid double patenting |