CN103588179A - Device and method for improving steam generating rate of low-temperature waste heat recovery system for sulfuric acid - Google Patents
Device and method for improving steam generating rate of low-temperature waste heat recovery system for sulfuric acid Download PDFInfo
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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
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Abstract
The invention discloses a device for improving a steam generating rate of a low-temperature waste heat recovery system for sulfuric acid, and provides a method for improving the steam generating rate of the low-temperature waste heat recovery system for sulfuric acid. According to the invention, high-temperature acid production heat of the low-temperature waste heat recovery system is used for generating secondary steam with lower pressure, the secondary steam is sent into a high-temperature absorption tower and serves as part of make-up water, latent heat of the secondary steam is brought back to the low-temperature waste heat recovery system to generate low-pressure steam with higher pressure, and the steam generating rate for low pressure steam production of the system can be increased from 0.45 t to about 0.57 t each time 1 ton of sulfuric acid is produced.
Description
Technical field
The present invention relates to a kind of device and method that improves sulfuric acid low temperature residual neat recovering system steam generating capacity.
Background technology
Gas washing in SA production industry, has been provided with Low Temperature Thermal retrieving arrangement at dry absorption section at present, and its technical process is: containing SO
3process gas enter high temperature absorption tower, by spray acid in tower, absorbed releases heat, acid temperature rise, high temperature concentrated acid is pumped pressurization by high temperature circulation pump and is sent into vaporizer and produce low-pressure steam, enters mixing tank and add water to reduce acid dense after sour temperature drop is low, then sends into the circulation of high temperature absorption tower again and absorbs SO
3; Device produces acid and picks out from the circulation acid tube of evaporator outlet, after feedwater heating apparatus and the cooling of de-salted water well heater outside confession, the sour temperature of outer confession is generally 90 ℃ ~ 130 ℃, still has part heat to fail efficient recovery.In this class Low Temperature Thermal retrieving arrangement, the steam generating capacity of low-pressure steam is generally 1 ton of sulphuric acid production low-pressure steam 0.45t left and right of every production.
Therefore, need a kind of method that improves sulfuric acid low temperature residual neat recovering system steam generating capacity to address the above problem.
Summary of the invention
For solving above-mentioned deficiency of the prior art, the object of the present invention is to provide a kind of device that improves sulfuric acid low temperature residual neat recovering system steam generating capacity.
For solving the problems of the technologies described above, the technical scheme that the device of raising sulfuric acid low temperature residual neat recovering system steam generating capacity of the present invention adopts is as follows:
A kind of device that improves sulfuric acid low temperature residual neat recovering system steam generating capacity, comprise high temperature absorption tower, high temperature circulation groove, high temperature circulation pump, vaporizer, mixing tank, service pump, jet pump, the second vaporizer and de-salted water well heater, described high temperature circulation groove connects the bottom on described high temperature absorption tower, described high temperature circulation pump connects the import of described high temperature circulation groove and vaporizer, the outlet of described vaporizer connects described mixing tank, and described mixing tank connects the top on described high temperature absorption tower; The outlet of described vaporizer also connects described the second vaporizer, and the import of described service pump connects described de-salted water well heater, and described feedwater pump outlet connects described vaporizer; The import of described jet pump connects described de-salted water well heater, and described injection water pump outlet connects described mixing tank and the second vaporizer; Described the second vaporizer connects described de-salted water well heater;
On described the second vaporizer, be provided with secondary steam outlet, be provided with de-salted water import and sulfuric acid outlet on described de-salted water well heater, be provided with low-pressure steam outlet on described vaporizer, the top on described high temperature absorption tower is provided with process gas outlet.
Further, also comprise feedwater heating apparatus, the outlet of described vaporizer also connects described the second vaporizer by described feedwater heating apparatus, and described feedwater pump outlet connects described vaporizer by described feedwater heating apparatus.
Further, also comprise deoxygenator, between described de-salted water well heater and described service pump and jet pump, be provided with described deoxygenator.
Further, described the second vaporizer is flash tank (12).
Beneficial effect: the invention provides a kind of device that improves sulfuric acid low temperature residual neat recovering system steam generating capacity, the heat of low-grade secondary steam is injected to the high temperature absorption tower of sulfuric acid low temperature heat reclamation device, produce whereby more high-grade low-pressure steam, thereby the steam generating capacity of 1 ton of sulfuric acid low-pressure steam of every production of low-temperature heat recovery system is brought up to 0.57t left and right by 0.48t.
The invention also discloses a kind of method that improves sulfuric acid low temperature residual neat recovering system steam generating capacity, adopt following technical scheme:
Improve a method for sulfuric acid low temperature residual neat recovering system steam generating capacity, adopt the device of raising sulfuric acid low temperature residual neat recovering system steam generating capacity as above, comprise the following steps:
1) entrance of the secondary steam, the process gas containing SO3 being produced with described the second vaporizer or flash tank (12) on described high temperature absorption tower mixes;
2), in described high temperature absorption tower, the SO3 in process gas is recycled acid and absorbs, release of heat produces the vitriol oil, low-grade heat in secondary steam is converted into the heat of the vitriol oil;
3), step 2) vitriol oil that obtains enters high temperature circulation groove, sends into vaporizer produce low-pressure steam through the pressurization of high temperature circulation pump, obtains the product acid of system;
4), the product acid of a part of system sends into mixing tank and regulates and produce sour concentration, regulates the later product acid of concentration to return to high temperature absorption tower again, continues the SO3 in absorption technique gas;
5), the product acid of another part system sends to the second vaporizer from the outlet of vaporizer, produces acid heating water in the second vaporizer and produces secondary steam, produces acid cooling;
6), in de-salted water well heater, add de-salted water, the product acid of step 5) is sent in de-salted water well heater and is heated de-salted water, produces acid cooling, produces subsequently acid and sends outside;
7), the de-salted water that obtains of step 6) sends into thermal de-aeration in deoxygenator, a part of deaerated water is sent into vaporizer through service pump, produces low-pressure steam; Part deaerated water is sent into the second vaporizer after jet pump pressurization, produces secondary steam; Some deaerated water sends into through jet pump pressurization the concentration that mixing tank regulates the vitriol oil.
Further, in step 5), the feedwater of feedwater heating apparatus preheating evaporator is first sent in the product acid of system, then sends into the second vaporizer heated feed water generation secondary steam.
Further, described the second vaporizer is flash tank.
Further, the pressure of the low-pressure steam producing in described vaporizer is 0.8 ± 0.2MPa, and the pressure of the secondary steam that described the second vaporizer produces is 0.25 ± 0.2MPa.
Further, step 2) in, the temperature of the vitriol oil is 205 ± 20 ℃, and in step 3), to produce sour temperature be 190 ± 20 ℃ to system, produces sour temperature and be reduced to 130 ± 20 ℃ in step 5), produces sour temperature and be reduced to 70 ± 20 ℃ in step 6).
Beneficial effect: the invention provides a kind of method that improves sulfuric acid low temperature residual neat recovering system steam generating capacity, the heat of low-grade secondary steam is injected to the high temperature absorption tower of sulfuric acid low temperature heat reclamation device, produce whereby more high-grade low-pressure steam, thereby the steam generating capacity of 1 ton of sulfuric acid low-pressure steam of every production of low-temperature heat recovery system is brought up to 0.57t left and right by 0.48t.
Accompanying drawing explanation
Fig. 1 is the principle schematic of embodiment 1;
Fig. 2 is the principle schematic of embodiment 2;
Fig. 3 is the principle schematic of embodiment 3.
Embodiment
Below in conjunction with accompanying drawing, the present invention is further described.
Process gas containing SO3 mixes near 1 entrance of high temperature absorption tower with secondary steam, mixed gas enters high temperature heat recovery tower 1, the lower liquid sulfuric acid of tower top spray, packing layer SO3 at tower is absorbed to generate the high vitriol oil, release reaction heat, acid temperature rises, now the latent heat of secondary steam is converted into the heat of high-temperature sulfuric acid simultaneously, high-temperature sulfuric acid flows into high temperature circulation groove 2 after tower bottom collects, through 3 pressurizations of high temperature circulation pump, send into the low-pressure steam that vaporizer 4 produces 0.8 ± 0.2MPa pressure, after the vitriol oil goes out vaporizer, the low mixing tank 5 of sending into again of temperature drop regulates acid dense, then return to again high temperature absorption tower 1, SO3 in circulation absorption technique gas, the product acid of heat recovery system picks out after upstream device cooling and sends outside from the circulation acid tube of evaporator outlet.Accompanying drawing 1 ~ 3 provides respectively the technical process that produces secondary steam on 3 kinds of product acid tube roads, existing explanation respectively:
1, as shown in Figure 1, the second vaporizer 9 is first sent in the product acid of heat recovery system, and heating injection water produces secondary steam, and desalination well heater 10 preheating de-salted waters are sent in the product acid after cooling again, after sour temperature drop is low, send outside.Extraneous de-salted water is first sent into 10 preheatings of de-salted water well heater, then send into thermal de-aeration in deoxygenator 8, part deaerated water sends into through service pump 6 low-pressure steam that vaporizer 4 produces 0.8 ± 0.2MPa, it is (0.25 ± 0.2MPa) secondary steam that another part deaerated water is sent into the second vaporizer generation pressure through jet pump 7 pressurizations, and some deaerated water send mixing tank 5 to regulate the concentration of recycle acids too after jet pump 7 pressurizations.
2, as shown in Figure 2, feedwater heating apparatus 11 preheating feedwater are first sent in the product acid of heat recovery system, then send into the second vaporizer 9, and heating injection water produces secondary steam, and desalination well heater 10 preheating de-salted waters are sent in the product acid after cooling again, after sour temperature drop is low, send outside.Extraneous de-salted water is first sent into 10 preheatings of de-salted water well heater, then send into thermal de-aeration in deoxygenator 8, part deaerated water is first sent into feedwater heating apparatus 11 pre-heating temperature elevations through service pump 6 pressurizations, after send into again and in vaporizer 4, produce 0.8 ± 0.2MPa low-pressure steam, it is (0.25 ± 0.2MPa) secondary steam that another part deaerated water is sent into the second vaporizer generation pressure through jet pump 7 pressurizations, and some deaerated water send mixing tank 5 to regulate the concentration of recycle acids too after jet pump 7 pressurizations.
3, as shown in Figure 3, feedwater heating apparatus 11 preheating feedwater are first sent in the product acid of heat recovery system, then send into desalination well heater 10 heating de-salted waters, after sour temperature drop is low, send outside.Extraneous de-salted water is first sent in de-salted water well heater 10 and is produced the high-temperature-hot-water of 150 ± 30 ℃, and it is (0.25 ± 0.2MPa) secondary steam that high-temperature-hot-water flash distillation in flash tank 12 produces pressure; A hot water part after flash distillation is first sent into preheating in feedwater heating apparatus 11 through service pump 6 pressurization, after send into again in vaporizer 4 and produce 0.8 ± 0.2MPa low-pressure steam, another part hot water send mixing tank 5 to regulate the concentration of recycle acids after jet pump 7 pressurizations.
The present invention utilizes low-temperature heat recovery system high temperature to produce the secondary steam that sour heat generation pressure is lower (pressure is 0.25 ± 0.2MPa), these secondary steams are sent into a high temperature absorption tower water part as a supplement, the latent heat of secondary steam is taken back to low-temperature heat recovery system, produce the higher low-pressure steam of pressure, reclaiming and producing low-pressure steam vapor pressure is 0.8 ± 0.2MPa, and the steam generating capacity of system can be brought up to the highest 0.58t left and right from 1 ton of sulphuric acid production low-pressure steam 0.45t of every production.
embodiment 1
Refer to shown in Fig. 1,
Process gas containing SO3 mixes at high temperature absorption tower 1 entrance with the secondary steam (pressure is 0.25 ± 0.2MPa) that the second vaporizer 9 produces, SO3 in process gas is recycled acid and absorbs in high temperature absorption tower 1, release of heat produces the high-temperature concentrated sulfuric acid of 205 ± 20 ℃, now in secondary steam, low-grade heat is converted into the heat of high-temperature concentrated sulfuric acid, high-temperature concentrated sulfuric acid enters high temperature circulation groove 2 in confluxing of tower bottom, through 3 pressurizations of high temperature circulation pump, send into vaporizer 4 and produce (0.8 ± 0.2MPa) low-pressure steam, the vitriol oil goes out the rear sour temperature drop of vaporizer 4 and is low to moderate 190 ± 20 ℃, obtain the product acid of system, the product acid of a part of system is sent into mixing tank 5 regulates acid dense, the sulfuric acid reducing after concentration returns to high temperature absorption tower 1 again, SO3 in circulation absorption technique gas, the product acid (temperature is 190 ± 20 ℃) of part system picks out from the branch of the circulation acid tube of vaporizer 4 outlets, send into the second vaporizer 9 heated feed waters and produce the secondary steam that pressure is 0.25 ± 0.2MPa, acid temperature drop is low to moderate 130 ± 20 ℃, send into again de-salted water well heater 10 heating de-salted waters, acid temperature drop is low to moderate 70 ± 20 ℃, produces acid and send outside after cooling.The de-salted water that the external world sends into is heated to 85 ± 20 ℃ in de-salted water well heater 10, then sends into thermal de-aeration in deoxygenator 8, and the deaerated water part of 104 ℃ is sent into vaporizer 4 after service pump 6 pressurizations, produces the low-pressure steam of 0.8 ± 0.2MPa; Another deaerated water is sent into the second vaporizer 9 after jet pump 7 pressurizations, produce the secondary steam of 0.25 ± 0.2MPa, also have another deaerated water to send into through jet pump 7 pressurizations the concentration that mixing tank regulates recycle acid, adopt the heat recovery system of this technical process, the low-pressure steam steam generating capacity of 1 ton of sulfuric acid of the every production of its system can be brought up to 0.58t by 0.45t.
embodiment 2
Refer to shown in Fig. 2,
Process gas containing SO3 mixes at high temperature absorption tower 1 entrance with the secondary steam (pressure is 0.25 ± 0.2MPa) that the second vaporizer 9 produces, SO3 in process gas is recycled acid and absorbs in high temperature absorption tower 1, release of heat produces the high vitriol oil of 205 ± 20 ℃ of left and right, now in secondary steam, low-grade heat is converted into the heat of high temperature concentrated acid, high temperature concentrated acid enters high temperature circulation groove 2 in confluxing of tower bottom, through 3 pressurizations of high temperature circulation pump, send into vaporizer 4 and produce (0.8 ± 0.2MPa) low-pressure steam, after the vitriol oil goes out vaporizer, sour temperature drop is low to moderate 190 ± 20 ℃, obtain the product acid of system, the product acid of part system is sent into mixing tank 5 and is regulated acid dense, the sulfuric acid reducing after concentration returns to high temperature absorption tower 1 again, SO3 in circulation absorption technique gas, the product acid (temperature is 190 ± 20 ℃) of part system picks out from the branch of the circulation acid tube of evaporator outlet, first send into the feedwater of feedwater heating apparatus 11 preheating evaporators 4, acid temperature drop to 165 ± 20 ℃, then send into again the second vaporizer 9 heated feed waters and produce the secondary steam that pressure is 0.25 ± 0.2MPa, acid temperature drop is low to moderate 125 ± 20 ℃, send into de-salted water well heater 10 heating de-salted waters, sour temperature drop is low to moderate 70 ± 20 ℃, produces acid and send outside after cooling again.The de-salted water that the external world sends into is heated to 85 ± 20 ℃ in de-salted water well heater 10, send into again thermal de-aeration in deoxygenator 8, the deaerated water part of 104 ℃ is first sent into preheating in feedwater heating apparatus 11 after service pump 6 pressurizations, then sends into the low-pressure steam that vaporizer 4 produces 0.8 ± 0.2MPa; Another deaerated water is sent into the second vaporizer 9 after jet pump 7 pressurizations, produce the secondary steam of 0.25 ± 0.2MPa, also have another deaerated water to send into through jet pump 7 pressurizations the concentration that mixing tank regulates recycle acid, adopt the heat recovery system of this technical process, the low-pressure steam steam generating capacity of 1 ton of sulfuric acid of the every production of its system can be brought up to 0.55t by 0.45t.
Refer to shown in Fig. 3,
Process gas containing SO3 mixes at high temperature absorption tower 1 entrance with the secondary steam (pressure is 0.25 ± 0.2MPa) that flash tank 12 produces, SO3 in process gas is recycled acid and absorbs in high temperature absorption tower 1, release of heat produces the high vitriol oil of 205 ± 20 ℃ of left and right, now in secondary steam, low-grade heat is converted into the heat of high temperature concentrated acid, high temperature concentrated acid enters high temperature circulation groove 2 in confluxing of tower bottom, through 3 pressurizations of high temperature circulation pump, send into vaporizer 4 and produce (0.8 ± 0.2MPa) low-pressure steam, after the vitriol oil goes out vaporizer, sour temperature drop is low to moderate 190 ± 20 ℃, obtain the product acid of system.The acid of part product is sent into mixing tank 5 again and is regulated acid dense, and the sulfuric acid reducing after concentration returns to high temperature absorption tower 1, the SO3 in circulation absorption technique gas again; The product acid (temperature is 190 ± 20 ℃) of part system picks out from the branch of the circulation acid tube of evaporator outlet, first send into the feedwater of feedwater heating apparatus 11 preheating evaporators 4, acid temperature drop to 165 ± 20 ℃, send into again de-salted water well heater 10 heating de-salted waters, acid temperature drop is low to moderate 70 ± 20 ℃, produces acid and send outside after cooling.The de-salted water that the external world sends into is heated to 150 ± 30 ℃ in de-salted water well heater 10, send into again the secondary steam of flash distillation generation 0.25 ± 0.2MPa in flash tank 12, a hot water part after flash distillation is first sent into preheating in feedwater heating apparatus 11 after service pump 6 pressurizations, then sends into the low-pressure steam that vaporizer 4 produces 0.8 ± 0.2MPa; Another hot water is sent into the concentration that mixing tank 5 regulates recycle acid after jet pump 7 pressurizations, adopts the heat recovery system of this technical process, and the low-pressure steam steam generating capacity of 1 ton of sulfuric acid of the every production of its system can be brought up to 0.55t by 0.45t.
The above is only the preferred embodiment of the present invention; be noted that for those skilled in the art; under the premise without departing from the principles of the invention, can also make some improvements and modifications, these improvements and modifications also should be considered as protection scope of the present invention.
Claims (9)
1. a device that improves sulfuric acid low temperature residual neat recovering system steam generating capacity, it is characterized in that, comprise high temperature absorption tower (1), high temperature circulation groove (2), high temperature circulation pump (3), vaporizer (4), mixing tank (5), service pump (6), jet pump (7), the second vaporizer (9) and de-salted water well heater (10), described high temperature circulation groove (2) connects the bottom on described high temperature absorption tower (1), described high temperature circulation pump (3) connects the import of described high temperature circulation groove (2) and vaporizer (4), the outlet of described vaporizer (4) connects described mixing tank (5), described mixing tank (5) connects the top on described high temperature absorption tower (1), the outlet of described vaporizer (4) also connects described the second vaporizer (9), and the import of described service pump (6) connects described de-salted water well heater (10), and the outlet of described service pump (6) connects described vaporizer (4), the import of described jet pump (7) connects described de-salted water well heater (10), and the outlet of described jet pump (7) connects described mixing tank (5) and the second vaporizer (9), described the second vaporizer (9) connects described de-salted water well heater (10),
On described the second vaporizer (9), be provided with secondary steam outlet, on described de-salted water well heater (10), be provided with de-salted water import and sulfuric acid outlet, on described vaporizer (4), be provided with low-pressure steam outlet, the top on described high temperature absorption tower (1) is provided with process gas outlet.
2. a kind of device that improves sulfuric acid low temperature residual neat recovering system steam generating capacity according to claim 1, it is characterized in that, also comprise feedwater heating apparatus (11), the outlet of described vaporizer (4) also connects described the second vaporizer (9) by described feedwater heating apparatus (11), and the outlet of described service pump (6) connects described vaporizer (4) by described feedwater heating apparatus (11).
3. a kind of device that improves sulfuric acid low temperature residual neat recovering system steam generating capacity according to claim 1 and 2, it is characterized in that, also comprise deoxygenator (8), between described de-salted water well heater (10) and described service pump (6) and jet pump (7), be provided with described deoxygenator (8).
4. a kind of device that improves sulfuric acid low temperature residual neat recovering system steam generating capacity according to claim 1 and 2, is characterized in that, described the second vaporizer (9) is flash tank (12).
5. a method that improves sulfuric acid low temperature residual neat recovering system steam generating capacity, is characterized in that, adopts the device of the raising sulfuric acid low temperature residual neat recovering system steam generating capacity of stating as claim 3 office, comprises the following steps:
1) entrance of the secondary steam, the process gas containing SO3 being produced with described the second vaporizer (9) or flash tank (12) on described high temperature absorption tower (1) mixes;
2), in described high temperature absorption tower (1), the SO3 in process gas is recycled acid and absorbs, release of heat produces the vitriol oil, low-grade heat in secondary steam is converted into the heat of the vitriol oil;
3), step 2) vitriol oil that obtains enters high temperature circulation groove (2), sends into vaporizer (4) produce low-pressure steam through high temperature circulation pump (3) pressurization, obtains the product acid of system;
4), the product acid of a part of system sends into mixing tank (5) and regulates and produce sour concentration, regulates the later product acid of concentration to return to high temperature absorption tower (1) again, continues the SO3 in absorption technique gas;
5), the product acid of another part system sends to the second vaporizer (9) from the outlet of vaporizer (4), produces acid heating water in the second vaporizer (9) and produces secondary steam, produce acid and lower the temperature;
6), in de-salted water well heater (10), add de-salted water, heating de-salted water in de-salted water well heater (10) is sent in the product acid of step 5), produces acid cooling, produces subsequently acid and sends outside;
7), the de-salted water that obtains of step 6) sends into thermal de-aeration in deoxygenator (8), a part of deaerated water is sent into vaporizer (4) through service pump (6), produces low-pressure steam; Part deaerated water is sent into the second vaporizer (9) after jet pump (7) pressurization, produces secondary steam; Some deaerated water sends into through jet pump (7) pressurization the concentration that mixing tank (5) regulates the vitriol oil.
6. the method for raising sulfuric acid low temperature residual neat recovering system steam generating capacity as claimed in claim 5, it is characterized in that, in step 5), the feedwater of feedwater heating apparatus (11) preheating evaporator (4) is first sent in the product acid of system, then sends into the second vaporizer (9) heated feed water generation secondary steam.
7. the method for raising sulfuric acid low temperature residual neat recovering system steam generating capacity as claimed in claim 5, is characterized in that, described the second vaporizer (9) is flash tank.
8. the method for raising sulfuric acid low temperature residual neat recovering system steam generating capacity as claimed in claim 5, it is characterized in that, the pressure of the low-pressure steam producing in described vaporizer (4) is 0.8 ± 0.2MPa, and the pressure of the secondary steam that described the second vaporizer (9) produces is 0.25 ± 0.2MPa.
9. the method for raising sulfuric acid low temperature residual neat recovering system steam generating capacity as claimed in claim 5, it is characterized in that, step 2) in, the temperature of the vitriol oil is 205 ± 20 ℃, in step 4), to produce sour temperature be 190 ± 20 ℃ to system, in step 5), produce sour temperature and be reduced to 130 ± 20 ℃, in step 6), produce sour temperature and be reduced to 70 ± 20 ℃.
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| CN104495757B (en) * | 2015-01-06 | 2016-09-28 | 东华工程科技股份有限公司 | SO in sulfuric acid apparatus3absorb low-temperature heat energy recovery system |
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| CN111252743A (en) * | 2020-04-01 | 2020-06-09 | 中化重庆涪陵化工有限公司 | Sulfur acid making system for recovering low-level heat of secondary absorption process |
| CN111252743B (en) * | 2020-04-01 | 2021-05-28 | 中化重庆涪陵化工有限公司 | Sulfur acid making system for recovering low-level heat of secondary absorption process |
| CN111704114A (en) * | 2020-06-29 | 2020-09-25 | 南京海陆化工科技有限公司 | Method for improving steam production rate of heat recovery system in dry absorption section of sulfuric acid production |
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Application publication date: 20140219 |