CN214536091U - Waste heat recovery system with flash evaporator - Google Patents

Waste heat recovery system with flash evaporator Download PDF

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Publication number
CN214536091U
CN214536091U CN202022922227.5U CN202022922227U CN214536091U CN 214536091 U CN214536091 U CN 214536091U CN 202022922227 U CN202022922227 U CN 202022922227U CN 214536091 U CN214536091 U CN 214536091U
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flash
evaporator
heat recovery
water heater
water
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俞向东
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Nanjing Hailu Chemical Technology Co ltd
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Nanjing Hailu Chemical Technology Co ltd
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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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • 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
    • 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 utility model discloses a waste heat recovery system with flash vessel belongs to the chemical industry field. The method is characterized in that a flash evaporation water heater is arranged on a pipeline for delivering high-temperature sulfuric acid, the flash evaporation water is heated by the heat of the delivered sulfuric acid, and the flash evaporation water is delivered into a flash evaporator to reduce the pressureFlashing to low-pressure exhaust steam, sending the low-pressure exhaust steam into the process gas at the inlet of the high-temperature absorption tower of the dry absorption waste heat recovery device, and mixing with SO in the process gas3And (4) reacting. By adopting the utility model, the steam yield of the ore or the smelting flue gas acid making dry absorption waste heat recovery can be improved to 0.5 +/-0.1 ton steam/ton sulfuric acid from below 0.4 ton steam/ton sulfuric acid in the prior art.

Description

Waste heat recovery system with flash evaporator
Technical Field
The utility model belongs to the chemical industry field, concretely relates to waste heat recovery system with flash vessel.
Background
The prior dry absorption waste heat recovery process for preparing acid by using ore or smelting flue gas converts an acid preparation System (SO) once2Oxidation to SO3) post-SO-containing3The process gas is sent into a high-temperature absorption tower of a waste heat recovery device of a dry absorption working section, and SO in the process gas is circularly absorbed in the high-temperature absorption tower by adopting a high-temperature absorption process3High-temperature concentrated sulfuric acid (about 200 ℃) is generated at the outlet of the tower, the high-temperature concentrated sulfuric acid is pressurized by an acid circulating pump and is sent into an evaporator, the high-temperature concentrated sulfuric acid heats the feed water of the evaporator in the evaporator, low-pressure steam (not higher than 1.2MPa (g)) is generated, the temperature of the circulating acid is reduced (about 190 ℃) after the high-temperature concentrated sulfuric acid is discharged from the evaporator, most of the circulating acid is sent into a mixer, the concentration of the circulating acid is reduced by using dilution water, and the circulating acid returns to a heat recovery tower to circularly absorb SO in the process gas3(ii) a The mass of sulfuric acid in the heat recovery device is increased due to the absorption of circulating acid S03 in the heat recovery tower and the addition of dilution water in the mixer, in order to maintain the material balance of the heat recovery device, a serial acid pipeline for sending out the sulfuric acid to the outside is arranged on a circulating acid pipeline at the outlet of the evaporator, and as the temperature of the sent-out sulfuric acid is higher (about 190 ℃), an evaporator feed water heater for preheating the feed water entering the evaporator is arranged on the serial acid pipeline in the prior art, and other heat exchange equipment such as a desalted water heater and the like are also arranged, so that the heat of the sent-out sulfuric acid is recovered by using a medium with a lower temperature. In the prior art, the evaporator water heater heats the feed water entering the evaporator by the heat of the delivered acid, which directly contributes to improving the low-pressure steam yield of the heat recovery device, while the heat is recovered by heat exchange between other media such as desalted water and the delivered sulfuric acid, the low-pressure steam yield of the heat recovery device cannot be directly improved, and the acid steam yield per ton (the low-pressure steam yield per 1 ton sulfuric acid produced by the acid making device) of the dry absorption waste heat recovery device in the prior art is below 0.4 ton steam per ton sulfuric acid.
SUMMERY OF THE UTILITY MODEL
The utility model provides a to the defect that prior art exists, provide a waste heat recovery system with flash vessel.
The purpose of the utility model can be realized by the following technical scheme:
a waste heat recovery system with flash evaporator is prepared as setting flash water heater on high-temp sulfuric acid pipeline, heating flash water by heat of sulfuric acid, sending flash water to flash evaporator for decompression and flash evaporation to obtain low-pressure steam exhaust, sending said low-pressure steam exhaust to high-temp absorbing tower of dry-sucking waste heat recovery unit for recovering SO in process gas3And (4) reacting.
The utility model discloses among the technical scheme: low pressure exhaust steam and SO in process gas3The sulfuric acid is generated by reaction, the temperature of the process gas at the inlet of the heat recovery tower is raised, and the heat of the process gas is absorbed by the circulating sulfuric acid in the high-temperature absorption tower, so that the temperature of the circulating sulfuric acid at the inlet of the evaporator is raised, the yield of low-pressure steam of the evaporator is increased, and the steam production rate per ton of the dry absorption waste heat recovery device is increased.
The utility model discloses among the technical scheme: the flash water is sent into a flash evaporator to be flashed into low-pressure exhaust steam after passing through a flash water heater, and the residual flash water is pressurized by a flash water circulating pump at the outlet of the flash evaporator and then is continuously sent into the flash water heater to circularly absorb the heat of high-temperature sulfuric acid sent out.
The utility model discloses among the technical scheme: the sulfuric acid delivered by the waste heat recovery device is cooled by a flash evaporation water heater and then is delivered into a desalted water heater, and the heat of the delivered sulfuric acid is further recovered by dehydration at a lower temperature.
The utility model discloses among the technical scheme: after the desalted water delivered outside is heated by a desalted water heater, one part of desalted water is delivered into a flash evaporator, and the balance of materials entering and exiting the flash evaporator is maintained, so that the flash evaporator flash water liquid level is stable.
The system for implementing the method includes, but is not limited to, the following three types, specifically:
the system comprises a heat recovery tower, wherein the output end of process gas is connected with the bottom of the heat recovery tower, the output end of the bottom of the heat recovery tower is connected with an evaporator sequentially through an acid circulating pump tank, an acid circulating pump and the evaporator, the evaporator is provided with two output ends, one of the output ends is connected with the upper part of the heat recovery tower through a mixer, and the other output end is connected with an evaporator feed water heater, a flash evaporation water heater and a desalted water heater sequentially.
In a first system: the flash evaporation water heater also has an output end connected with the exhaust steam flash evaporator, the output end at the top of the exhaust steam flash evaporator is connected with the output end of the process gas, and the output end at the bottom of the exhaust steam flash evaporator is connected with the flash evaporation water heater through the flash evaporation water circulating pump.
In a first system: the desalted water output pipeline is connected with the desalted water heater, one of the output ends of the desalted water heater is connected with the exhaust steam flash evaporator, and the other output end of the desalted water heater is discharged.
In some specific embodiments: the process gas is mixed with low-pressure exhaust steam (steam pressure is 0.2 +/-0.1 MPa) generated by an exhaust steam flash evaporator before entering a heat recovery tower, and part of SO in the process gas3Reacting with low-pressure exhaust steam to generate H2SO4The temperature of the process gas is raised to 260 +/-20 ℃, the process gas continuously reacts with the circulating acid sprayed from the upper part after entering the heat recovery tower, and the circulating acid absorbs SO in the process gas3And sensible heat of the process gas is generated, high-temperature concentrated sulfuric acid with the temperature of 210 +/-10 ℃ is generated at the bottom of the tower, the high-temperature concentrated sulfuric acid enters an acid circulating pump tank and is pressurized by an acid circulating pump and then is sent into an evaporator, the high-temperature concentrated sulfuric acid heats low-pressure feed water in the evaporator to generate low-pressure steam with the pressure of 0.8 +/-0.4 MPa, and the temperature and SO of the process gas are treated by a heat recovery tower3All reduce and send out the dry suction waste heat recovery device. Most of concentrated sulfuric acid is sent into a mixer after being cooled by an evaporator, and is returned to a heat recovery tower to circularly absorb SO in the process gas after being reduced in concentration by using dilution water3(ii) a Heat recovery tower internal circulation acid absorption S03The mass of the sulfuric acid in the heat recovery device is increased by the dilution water added in the mixer, in order to maintain the material balance of the heat recovery device, a serial acid pipeline for sending the sulfuric acid to the outside is arranged on a circulating acid pipeline at the outlet of the evaporator, an evaporator water supply heater is arranged on the serial acid pipeline for preheating low-pressure water supplied outside the battery limits due to the high temperature of the sent sulfuric acid, the sent sulfuric acid enters a flash water heater after being cooled by the evaporator water supply heater, the flash water is heated to the saturation temperature and then enters a desalted water heater, normal-temperature desalted water supplied outside the battery limits is heated, and the temperature of the sent acid is finally reduced to be below 100 DEG CAnd sending out the boundary area of the dry absorption waste heat recovery device.
Normal temperature desalted water fed into the battery compartment is heated to 120 +/-10 ℃ by a desalted water heater and then divided into 2 parts, one part of the normal temperature desalted water is fed into an exhaust steam flash evaporator to supplement flash water, the supplement amount is equal to the evaporation amount of the exhaust steam flash evaporator, and the rest desalted water is fed out of the battery compartment of the dry absorption waste heat recovery device.
And (3) pressurizing flash water in the exhaust steam flash evaporator by a flash water circulating pump, then sending the flash water into a flash water heater, heating the flash water to 150 +/-10 ℃, returning the flash water into the exhaust steam flash evaporator for expansion and pressure reduction, sending a part of flash water into low-pressure exhaust steam (the steam pressure is 0.2 +/-0.1 MPa) for flash evaporation into a process gas pipeline of a heat recovery tower, cooling the rest part of flash water to the saturation temperature, mixing with the water supplement at the outlet of a desalted water heater, pressurizing by the flash water circulating pump, then continuously sending the flash water into the flash water heater, and circularly absorbing the heat of the sulfuric acid which is sent out.
The second system for recovering the waste heat and generating the steam rate comprises a heat recovery tower, wherein the output end of the process gas is connected with the bottom of the heat recovery tower, the output end of the bottom of the heat recovery tower is connected with an evaporator through an acid circulating pump groove and an acid circulating pump in sequence, the evaporator is provided with three output ends, one of the output ends is connected with the upper part of the heat recovery tower through a mixer, and the second output end is connected with an evaporator feed water heater and a desalted water heater in sequence; the third output end is connected with a desalted water heater through a flash evaporation water heater.
In a second system: the flash water heater also has an output end connected with the exhaust steam flash evaporator, the output end at the top of the exhaust steam flash evaporator is connected with the output end of the process gas, and the output at the bottom of the exhaust steam flash evaporator is connected with the flash water heater through the flash water circulating pump end.
In a second system: the desalted water output pipeline is connected with the desalted water heater, one of the output ends of the desalted water heater is connected with the exhaust steam flash evaporator, and the other output end of the desalted water heater is discharged.
In some specific embodiments: the other technical scheme is the same as the first technical scheme, and the technical scheme is characterized in that an evaporator water supply heater and a flash water heater are connected in parallel on an acid delivery pipeline, one part of acid delivered from an outlet of an evaporator enters the evaporator water supply heater to preheat evaporator water supply, the other part of acid delivered from the outlet of the evaporator directly enters the flash water heater to heat flash water to generate low-pressure exhaust steam (steam pressure is 0.2 +/-0.1 MPa), sulfuric acid at an outlet of the evaporator water supply heater and sulfuric acid at an outlet of the flash water heater are combined and then are sent to a desalted water heater, the temperature of the sulfuric acid at an inlet of the dehydration heater is the same as that of the first scheme, and the recovered heat is consistent.
And the third system for recovering the steam yield by waste heat comprises a heat recovery tower, wherein the output end of the process gas is connected with the bottom of the heat recovery tower, the output end of the bottom of the heat recovery tower is connected with an evaporator sequentially through an acid circulating pump groove, an acid circulating pump and an evaporator, the evaporator is provided with two output ends, one of the two output ends is connected with the upper part of the heat recovery tower through a mixer, and the other output end is connected with a flash evaporation water heater, an evaporator feed water heater and a desalted water heater sequentially.
In a third system: the flash evaporation water heater also has an output end connected with the exhaust steam flash evaporator, the output end at the top of the exhaust steam flash evaporator is connected with the output end of the process gas, and the output end at the bottom of the exhaust steam flash evaporator is connected with the flash evaporation water heater through the flash evaporation water circulating pump.
In a third system: the desalted water output pipeline is connected with the desalted water heater, one of the output ends of the desalted water heater is connected with the exhaust steam flash evaporator, and the other output end of the desalted water heater is discharged.
In some specific embodiments: the other technical proposal is the same as the first technical proposal, and is characterized in that sulfuric acid is sent out from the outlet of the evaporator and firstly enters a flash water heater, low-pressure exhaust steam (the steam pressure is 0.2 +/-0.1 MPa) is generated by heating flash water, and the low-pressure exhaust steam is sent into an evaporator water supply heater to be preheated and then enters the evaporator water supply. Under the condition of the same heat exchange area as the previous 2 technical schemes, because the temperature of the sulfuric acid entering the external delivery is increased, the low-pressure steam (the steam pressure is 0.2 +/-0.1 MPa) produced by the technical scheme is the maximum, more low-pressure steam can be provided for the process gas pipeline at the inlet of the heat recovery tower, and the heat recovery tower can adapt to the high SO at the inlet3The working condition of gas concentration causes the temperature of the feed water of the evaporator to be reduced although the temperature of the acid at the inlet of the feed water heater of the evaporator is reduced, but the yield of the dead steam flash evaporator is reducedThe heat quantity sent to the evaporator is unchanged, and the direct steam production of the evaporator is not reduced.
The utility model discloses among the technical scheme: the flash evaporation water heater is arranged on the acid delivery pipeline of the dry absorption waste heat recovery device, the flash evaporation water is heated by using delivered sulfuric acid, the flash evaporation water enters the flash evaporator after flowing out of the flash evaporation water heater and is decompressed, partial flash evaporation water is flashed into low-pressure exhaust steam (with the pressure of 0.2 +/-0.1 MPa (g)) after decompression, and the residual flash evaporation water is pressurized by the flash evaporation water circulating pump at the water side outlet of the flash evaporator and then is delivered into the flash evaporation water heater to circularly absorb the heat of the delivered sulfuric acid.
Sending low-pressure exhaust steam generated by the flash evaporator to a process gas inlet pipeline of a heat recovery tower of a dry absorption waste heat recovery device, sending the process gas to the dry absorption waste heat recovery device at the temperature of about 180 ℃, mixing the process gas with the low-pressure exhaust steam, and then mixing water vapor with SO in the process gas3The temperature of the exothermic reaction process gas is raised to 260 +/-20 ℃, the heat of low-pressure exhaust steam with lower temperature (the saturation temperature of the exhaust steam is about 130 ℃) is converted into the heat of process gas with higher temperature (above 280 ℃) through chemical reaction, the process gas with temperature above 280 ℃ enters a heat recovery tower, and SO is absorbed by circulating acid to generate sulfuric acid3After heat addition, the temperature and SO of the process gas3The concentration is reduced and the steam is sent out of a heat recovery device, the heat of the low-pressure exhaust steam generated by the exhaust steam flash evaporator is transferred to high-temperature (the temperature is 210 +/-10 ℃) concentrated sulfuric acid at the outlet of the tower, the high-temperature concentrated sulfuric acid is pressurized by an acid circulating pump (3) and then sent into an evaporator (4), and the evaporator can produce more low-pressure steam (not higher than 1.2MPa (g)) with the flow basically equal to the low-pressure exhaust steam (the pressure is 0.2 +/-0.1 MPa (g)) sent into an inlet gas pipeline of the heat recovery tower.
The utility model has the advantages that:
by adopting the utility model, the steam yield of the ore or the smelting flue gas acid making dry absorption waste heat recovery can be improved to 0.5 +/-0.1 ton steam/ton sulfuric acid from below 0.4 ton steam/ton sulfuric acid in the prior art.
Drawings
Fig. 1 is a flow chart of a first system for implementing the present invention.
Fig. 2 is a flow chart of a second system for implementing the present invention.
Fig. 3 is a flow chart of a third system for implementing the present invention.
Wherein: 1-a heat recovery tower, 2-an acid circulating pump tank, 3-an acid circulating pump, 4-an evaporator, 5-a mixer, 6-an evaporator water supply heater, 7-a flash evaporation water heater, 8-a desalted water heater, 9-a flash evaporation water circulating pump and 10-an exhaust steam flash evaporator.
Detailed Description
The present invention is further described with reference to the following examples, but the scope of the present invention is not limited thereto: example 1
Referring to fig. 1, a first system for improving the recovery steam production rate of acid-making dry absorption waste heat of ore or smelting flue gas comprises a heat recovery tower 1, wherein an output end of process gas is connected with the bottom of the heat recovery tower 1, an output end of the bottom of the heat recovery tower 1 is connected with an evaporator 4 sequentially through an acid circulating pump groove 2, an acid circulating pump 3 and an evaporator 4, the evaporator 4 is provided with two output ends, one of the two output ends is connected with the upper part of the heat recovery tower 1 through a mixer 5, and the other output end is connected with an evaporator water supply heater 6, a flash evaporation water heater 7 and a desalted water heater 8 sequentially.
In a first system: the flash evaporation water heater 7 is also provided with an output end connected with an exhaust steam flash evaporator 10, the output end at the top of the exhaust steam flash evaporator 10 is connected with the output end of the process gas, and the output end at the bottom of the exhaust steam flash evaporator 10 is connected with the flash evaporation water heater 7 through a flash evaporation water circulating pump 9.
In a first system: the desalted water output pipeline is connected with a desalted water heater 8, one output end of the desalted water heater 8 is connected with a steam exhaust flash evaporator 10, and the other output end is discharged.
The method for improving the recovery steam production rate of the dry absorption waste heat of the acid production from ore or smelting flue gas by using the first system comprises the following steps:
the process gas is mixed with the low-pressure steam-exhaust steam pressure of 0.2 +/-0.1 MPa generated by the steam-exhaust flash evaporator 10 before entering the heat recovery tower 1, and partial SO in the process gas3Reaction with low pressure steam to form H2SO4The temperature of the process gas is raised to 260 +/-20 ℃, and the process gas and the upper part of the process gas are circulated by spraying after entering the heat recovery tower 1The acid continues to react, and the circulating acid absorbs SO in the process gas3And process gas heat is generated, high-temperature concentrated sulfuric acid with the temperature of 210 +/-10 ℃ is generated at the bottom of the tower, enters an acid circulating pump tank 2 and is pressurized by an acid circulating pump 3 and then is sent into an evaporator 4, the high-temperature concentrated sulfuric acid heats low-pressure feed water in the evaporator 4 to generate low-pressure steam with the pressure of 0.8 +/-0.4 MPa, and the temperature of the process gas and SO are processed by a heat recovery tower3All reduce and send out the dry suction waste heat recovery device. Concentrated sulfuric acid is cooled by an evaporator 4, 75 +/-15 percent of the concentrated sulfuric acid is sent into a mixer, the concentration of the concentrated sulfuric acid is reduced to 99 +/-0.1 percent by using dilution water, and the concentrated sulfuric acid returns to a heat recovery tower 1 to circularly absorb SO in the process gas3(ii) a Heat recovery tower internal circulation acid absorption S03And the dilution water added in the mixer causes the mass of the sulfuric acid in the heat recovery device to be increased, in order to maintain the material balance of the heat recovery device, a serial acid pipeline for sending the sulfuric acid to the outside is arranged on an outlet circulating acid pipeline of the evaporator, an evaporator water-feeding heater 6 is arranged on the serial acid pipeline for preheating low-pressure water fed outside the boundary area, the sulfuric acid sent outside is cooled by the evaporator water-feeding heater 6 and then enters a flash water heater, the flash water is heated to the saturation temperature and then enters a desalted water heater 8, normal-temperature desalted water fed outside the boundary area is heated, and the temperature of the acid sent outside the boundary area is finally reduced to be below 100 ℃ and then is sent out of the boundary area of the dry absorption waste heat recovery device.
Normal temperature desalted water fed into a battery compartment is heated to 120 +/-10 ℃ by a desalted water heater 8 and then divided into 2 parts, one part of the normal temperature desalted water is sent to an exhaust steam flash evaporator 10 to supplement flash water, the supplement amount is equal to the evaporation amount of the exhaust steam flash evaporator 10, and the rest desalted water is sent out of the battery compartment of the dry absorption waste heat recovery device.
The flash water in the exhaust steam flash evaporator 10 is pressurized by a flash water circulating pump and then is sent to a flash water heater 7, the flash water is heated to 150 +/-10 ℃, the flash water returns to the exhaust steam flash evaporator 10 for expansion and pressure reduction, a small part of flash water is flashed to have low-pressure exhaust steam pressure of 0.2 +/-0.1 MPa and is sent to a process gas pipeline of a heat recovery tower 1, the rest part of flash water is cooled to saturation temperature and is mixed with the desalted water heater outlet water supplement, and then the flash water is pressurized by the flash water circulating pump and then is continuously sent to the flash water heater 7, so that the heat of the sulfuric acid which is sent outside is circularly absorbed.
The method for improving the recovery steam yield of the dry absorption waste heat of the acid production from the ore or the smelting flue gas by using the second system comprises the following specific steps:
in the technical scheme of figure 1, an evaporator water-feeding heater 6 and a flash water heater 7 on an acid delivery pipeline are connected in series, sulfuric acid delivered from an evaporation outlet firstly enters the evaporator water-feeding heater 6 to preheat water fed into an evaporator, and then enters the flash water heater 7 to generate low-pressure exhaust steam with the pressure of 0.2 +/-0.1 MPa.
The technical scheme of the figure 2 is different from the technical scheme of the figure 1 in that an evaporator feed water heater 6 and a flash evaporation water heater 7 on an external acid supply pipeline are connected in parallel, 40 +/-10% of external acid supply at an outlet of an evaporator 4 enters the evaporator feed water heater 6 to preheat evaporator feed water, the other part of the external acid supply is sent to directly enter the flash evaporation water heater 7, the pressure of low-pressure exhaust steam generated by heating flash evaporation water is 0.2 +/-0.1 MPa, sulfuric acid at the outlet of the evaporator feed water heater 6 is combined with sulfuric acid at the outlet of the flash evaporation water heater 7 and then is sent to a desalted water heater, the temperature of the inlet sulfuric acid of the dehydration heater is the same as that of the first scheme, and the recovered heat is the same.
The method for improving the recovery steam yield of the dry absorption waste heat of the acid production by the ore or the smelting flue gas by using the third system comprises the following steps:
in the technical scheme of figure 1, an evaporator water-feeding heater 6 and a flash water heater 7 on an acid delivery pipeline are connected in series, sulfuric acid delivered from an evaporation outlet firstly enters the evaporator water-feeding heater 6 to preheat water fed into an evaporator, and then enters the flash water heater 7 to generate low-pressure exhaust steam with the pressure of 0.2 +/-0.1 MPa.
The technical scheme of the figure 3 is different from the technical scheme of the figure 1 in that sulfuric acid is sent out from an outlet of an evaporator 4 and firstly enters a flash water heater 7, the pressure of low-pressure exhaust steam generated by heating flash water is 0.2 +/-0.1 MPa, and the low-pressure exhaust steam is sent into an evaporator feed water heater 6 to be preheated and then enters evaporator feed water. Under the condition of the same heat exchange area as the previous 2 technical schemes, as the temperature of the sulfuric acid entering the external delivery is increased, the steam pressure of the low-pressure exhaust steam produced by the technical scheme is maximum at 0.2 +/-0.1 MPa, more low-pressure exhaust steam can be provided for the process gas pipeline at the inlet of the heat recovery tower, and the heat recovery tower can adapt to the high SO at the inlet3Operating conditions of gas concentration, although evaporator feeds water heaterThe temperature of the acid at the mouth is reduced, which causes the temperature of the water supply of the evaporator to be reduced, but the yield of the steam exhaust flash evaporator is increased, the heat sent to the evaporator is unchanged, and the direct steam yield of the evaporator is not reduced.

Claims (3)

1. The utility model provides a waste heat recovery system with flash vessel which characterized in that: the system comprises a heat recovery tower (1), wherein the output end of process gas is connected with the bottom of the heat recovery tower (1), the output end of the bottom of the heat recovery tower (1) is sequentially connected with an acid circulating pump tank (2), an acid circulating pump (3) and an evaporator (4), the evaporator (4) is provided with two output ends, one of the output ends is connected with the upper part of the heat recovery tower (1) through a mixer (5), and the other output end is sequentially connected with a flash evaporation water heater (7), an evaporator water supply heater (6) and a desalted water heater (8).
2. The system of claim 1, wherein: the flash evaporation water heater (7) is also provided with an output end connected with a waste steam flash evaporator (10), the output end at the top of the waste steam flash evaporator (10) is connected with the output end of the process gas, and the output end at the bottom of the waste steam flash evaporator (10) is connected with the flash evaporation water heater (7) through a flash evaporation water circulating pump (9).
3. The system of claim 1, wherein: the output pipeline of the desalted water is connected with a desalted water heater (8), one output end of the desalted water heater (8) is connected with a steam exhaust flash evaporator (10), and the other output end is discharged.
CN202022922227.5U 2020-12-08 2020-12-08 Waste heat recovery system with flash evaporator Active CN214536091U (en)

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Application Number Priority Date Filing Date Title
CN202022922227.5U CN214536091U (en) 2020-12-08 2020-12-08 Waste heat recovery system with flash evaporator

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Application Number Priority Date Filing Date Title
CN202022922227.5U CN214536091U (en) 2020-12-08 2020-12-08 Waste heat recovery system with flash evaporator

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CN214536091U true CN214536091U (en) 2021-10-29

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