CN212843103U - System for improving heat recovery steam production rate of sulfuric acid production dry-suction workshop section - Google Patents

System for improving heat recovery steam production rate of sulfuric acid production dry-suction workshop section Download PDF

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CN212843103U
CN212843103U CN202021226588.XU CN202021226588U CN212843103U CN 212843103 U CN212843103 U CN 212843103U CN 202021226588 U CN202021226588 U CN 202021226588U CN 212843103 U CN212843103 U CN 212843103U
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acid
temperature
heat recovery
evaporator
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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
    • 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 provides a system for improve sulphuric acid production dry-suction workshop section heat recovery steam production rate belongs to the chemical industry field. The system connects the lower tower acid of the low-temperature absorption section of the heat recovery tower with the inlet of the heat exchange equipment, and the lower tower acid is not mixed with the lower tower acid of the high-temperature absorption section, so that the lower tower acid temperature of the high-temperature absorption section is increased, the heat brought out by sulfuric acid sent out by the heat recovery system to the outside is reduced, and the steam production rate of the heat recovery system is increased by about 10-25%.

Description

System for improving heat recovery steam production rate of sulfuric acid production dry-suction workshop section
Technical Field
The utility model relates to a chemical industry field, concretely relates to improve system of sulphuric acid production dry-suction workshop section heat recovery steam production rate.
Background
The modern sulfuric acid production mostly adopts a 2-to-2-absorption production process, and S0 is contained in the sulfuric acid produced by an upstream device2The process gas (or the air participating in the conversion reaction) firstly enters a drying system, concentrated sulfuric acid is used for removing moisture, and then the process gas enters a conversion working sectionConvert at once most S02And O2Reacting to form SO3. Containing SO after one conversion3The process gas is sent into a heat recovery system of a dry absorption section for primary absorption, and high-temperature sulfuric acid is used for absorbing SO in the process gas3And recovering heat of the absorption reaction to produce low pressure steam. SO in process gas after primary absorption3The concentration is reduced, the process gas after the primary absorption is sent to a conversion section for secondary conversion, and the rest S0 is2Continued oxidation to produce SO3The process gas after the secondary conversion is sent into a secondary absorption system of a dry absorption working section to absorb SO in the process gas by using sulfuric acid3And more than 99 percent of S0 in the process gas after 2-to-2-conversion absorption2Are all converted into SO3And sulfuric acid is produced after absorption.
Acid mixing pipelines are arranged among the drying system, the heat recovery system and the secondary absorption system, and the acid concentration and the liquid level stability of the systems are maintained by mutually mixing sulfuric acid.
SO after primary conversion3The reaction heat and dilution heat for absorbing and generating the sulfuric acid account for more than 70% of the process generated heat in the whole dry absorption section, a heat recovery system in the dry absorption section adopts a high-temperature absorption process, high-temperature sulfuric acid is used for heating low-pressure feedwater to generate low-pressure steam, a drying and secondary absorption system adopts a low-temperature absorption process, the acid temperature after absorption is low, the absorption heat cannot be utilized, and the absorption reaction heat is carried out of a process system through circulating water.
The main process flow of the heat recovery system of the dry absorption section is as follows: containing SO3The process gas enters a heat recovery tower which is generally divided into two stages, and a high-temperature absorption section (lower stage) absorbs most of SO in the process gas by using high-temperature (180 ℃) and high-concentration (99%) sulfuric acid3The process gas absorbed by the high-temperature absorption section enters the low-temperature absorption section (the upper stage) again to be absorbed again by sulfuric acid with lower temperature (60 ℃) and lower concentration (-98.5%) from the drying or secondary absorption system. The sulfuric acid absorbed by the low-temperature absorption section enters the high-temperature absorption section to be mixed with high-temperature concentrated sulfuric acid, is pumped and pressurized by a high-temperature circulating pump and is sent into an evaporator to generate low-pressure steam, the acid temperature is reduced, then the low-pressure steam enters a mixer to be added with water to reduce the acid concentration, and then the low-pressure steam is sent into a heat recovery tower to circularly absorb SO3(ii) a The acid side outlet of the evaporator is provided withThe heat recovery system is used for sending acid to the drying or secondary absorption system, and because the acid temperature at the outlet of the evaporator is still higher (180 +/-15 ℃), an evaporator feed water heater is arranged on the external acid sending pipeline and used for preheating feed water entering the evaporator, the acid temperature is reduced to 160 +/-15 ℃, other heat exchangers can be arranged, the process material is heated by externally sent sulfuric acid, and the sulfuric acid is sent to the drying or secondary absorption system after being cooled so as to maintain the acid concentration and the liquid level stability of the system. In a sulfuric acid device using sulfur as a raw material, the steam production rate of a heat recovery system in a dry absorption section is generally 0.45 ton of steam per ton of acid; the steam production rate of a sulfuric acid device taking pyrite as a raw material is generally 0.25-0.35 ton of steam per ton of acid.
SUMMERY OF THE UTILITY MODEL
The utility model provides a system for improve sulphuric acid production dry-suction workshop section heat recovery steam production rate to the technical problem that prior art exists.
The purpose of the utility model can be realized by the following technical scheme:
a system for improving the heat recovery steam production rate of a dry absorption section in sulfuric acid production comprises a heat recovery tower, wherein the heat recovery tower comprises a high-temperature absorption section, a gas-liquid separation section and a low-temperature absorption section, and the high-temperature absorption section is connected with the upper part of the high-temperature absorption section sequentially through a high-temperature circulation tank, a high-temperature circulation pump, an evaporator and a mixer;
and a branch is further arranged on an acid pipeline connected with the evaporator and the mixer, the branch is connected with the drying or secondary absorption system sequentially through at least one heat exchange device, and the liquid output end of the gas-liquid separation section is connected with an inlet of the heat exchange device.
The utility model discloses among the technical scheme: the heat exchange equipment at least comprises an evaporator feed water heater.
The utility model discloses among the technical scheme: the branch is connected with the upper parts of the acid circulating tank, the acid circulating pump, the acid cooler and the drying tower or the secondary absorption tower in turn through the evaporator water supply heater.
The utility model discloses among the technical scheme: the acid side of the acid cooler is also provided with an output end which is connected with the upper part of the low-temperature absorption section.
The utility model discloses among the technical scheme: the output end of the evaporator feed water heater is connected with the evaporator.
Method for improving heat recovery steam production rate of dry absorption section in sulfuric acid production by using system, containing SO3The process gas enters a high-temperature absorption section of the heat recovery tower, and SO is contained in the process gas3Part of the sulfuric acid is absorbed by high-temperature sulfuric acid with the concentration of 99 percent, the acid temperature of a tower under the high-temperature absorption section is raised to 205 +/-15 ℃, high-temperature concentrated acid is boosted by a high-temperature circulating pump and then sent to an evaporator to be heated by low-pressure feed water to generate low-pressure steam, the acid temperature is reduced to 190 +/-15 ℃ after being discharged from the evaporator, part of sulfuric acid discharged from the evaporator is sent to a mixer to adjust the concentration of the sulfuric acid to 99 percent, and then the sulfuric acid is sent to the high-temperature absorption section to circularly3Preheating the rest (10-40%) of sulfuric acid out of the evaporator by an evaporator feed water heater, feeding the sulfuric acid into feed water of the evaporator, reducing the acid temperature to 170 +/-15 ℃, and cooling the rest of sulfuric acid by equipment and then sending the cooled sulfuric acid to a drying or secondary absorption system;
the process gas enters a low-temperature absorption section after being absorbed by a high-temperature absorption section of a heat recovery tower, and is used for spraying and absorbing the residual S0 in the process gas from a sulfuric acid spray system with the drying or secondary absorption system temperature of 60 ℃ and the concentration of 98.5 percent3The acid temperature rises to 150 +/-15 ℃, a gas-liquid separation section is arranged at the lower part of the low-temperature absorption section, the separation section separates the process gas at the outlet of the high-temperature absorption section from the lower tower acid at the low-temperature absorption section, the separated lower tower acid at the low-temperature absorption section is sent to a branch of the outlet of the evaporator through a pipeline, a plurality of heat exchangers can be connected to the pipeline, the lower tower acid at the low-temperature absorption section of the heat recovery tower can be merged into the acid side inlet of any heat exchanger in the pipeline, and the acid is finally sent to a drying or secondary absorption system after being cooled by the heat exchangers.
The utility model has the advantages that:
the low-temperature absorption section of the existing heat recovery tower adopts sulfuric acid with the temperature of about 60 ℃ and the concentration of about 98.5% for absorption, and the purpose is to ensure a heat absorption system S03The absorption rate of the lower tower acid is increased to 150 ℃ after the lower tower acid is absorbed by the low-temperature section, the lower tower acid at the low-temperature section in the heat recovery tower directly enters the high-temperature absorption section, the sulfuric acid after two-stage absorption is mixed and then is sent into the evaporator through the high-temperature circulating pump, but the temperature of the lower tower acid at the low-temperature absorption section is lower than that of the lower tower acid at the outlet of the evaporatorThe temperature of the acid at the mouth is 190 +/-15 ℃ and is lower than the temperature of the acid at the outlet of the water heater of the evaporator (170 +/-15 ℃), and the acid does not contribute to steam production, but the lower tower acid of the low-temperature absorption section is heated by the absorption reaction heat of the high-temperature absorption section, namely the lower tower acid of the low-temperature absorption section is heated to the temperature of the outlet of the water heater of the evaporator (170 +/-15 ℃) from 150 +/-15 ℃, and then is sent to a drying or secondary absorption system, so that the steam production rate of a heat recovery system is reduced. According to the invention, the lower acid of the low-temperature absorption section of the heat recovery tower or the lower acid of the low-temperature absorption tower is independently sent to the drying or secondary absorption system or the acid serial pipeline of the evaporator to reduce the heat brought out by the sulfuric acid sent from the heat recovery system to the drying or secondary absorption system, so that the steam production rate of the heat recovery system at the dry absorption section is improved by about 10-25%.
Drawings
FIG. 1 is a schematic view of a first apparatus of the present invention.
Wherein: 1 is a heat recovery tower, 2 is a high-temperature circulating tank, 3 is a mixer, 4 is an evaporator feed water heater, 5 is a high-temperature circulating pump, 6 is an evaporator, 7 is a drying tower or a secondary absorption tower, 8 is an acid circulating tank, 9 is an acid circulating pump, and 10 is an acid cooler.
Detailed Description
The present invention will be further explained with reference to the following embodiments, but the scope of the present invention is not limited thereto:
referring to fig. 1, a system for increasing the heat recovery steam production rate in the dry absorption section of sulfuric acid production, which comprises a heat recovery tower 1 and a drying tower or a secondary absorption tower 7, wherein the heat recovery tower 1 comprises a high-temperature absorption section, a gas-liquid separation section and a low-temperature absorption section, and the high-temperature absorption section is connected with the upper part of the high-temperature absorption section through a high-temperature circulation tank 2, a high-temperature circulation pump 5, an evaporator 6 and a mixer 3 in sequence;
and a branch is further arranged on an acid pipeline connected with the evaporator 6 and the mixer 3, the branch is sequentially connected with the drying or secondary absorption system through at least one heat exchange device, and the liquid output end of the gas-liquid separation section is connected with an inlet of the heat exchange device.
The heat exchange equipment at least comprises an evaporator feed water heater 4. The branch is connected with the upper parts of an acid circulating tank 8, an acid circulating pump 9, an acid cooler 10 and a drying tower or a secondary absorption tower 7 in sequence through an evaporator feed water heater 4. The acid side of the acid cooler 10 also has an output connected to the upper portion of the low temperature absorption section. The output end of the evaporator feed water heater 4 is connected with the evaporator 6.
A method for increasing steam production using the system of figure 1, the method comprising:
containing SO3The process gas enters a high-temperature absorption section of a heat recovery tower 1, and SO in the process gas3Is absorbed by high-temperature sulfuric acid with the concentration of 99 percent, the acid temperature of the tower under the high-temperature absorption section is raised to 205 +/-15 ℃, high-temperature concentrated acid is boosted by a high-temperature circulating pump 5 and then sent to an evaporator 6 to be heated by low-pressure water supply to generate low-pressure steam, the acid temperature is reduced to 190 +/-15 ℃ after being discharged from the evaporator 6, part of sulfuric acid discharged from the evaporator 6 is sent to a mixer 3 to adjust the concentration of the sulfuric acid to 99 percent and then sent to the high-temperature absorption section to circularly absorb SO in the process gas3Cooling the rest (10-40%) of the sulfuric acid out of the evaporator 6 by heat exchange equipment until the acid temperature is reduced to 170 +/-15 ℃, and cooling the rest of the sulfuric acid by the equipment and then sending the cooled sulfuric acid to a drying or secondary absorption system;
the process gas enters a low-temperature absorption section after being absorbed by a high-temperature absorption section of a heat recovery tower 1, and is used for spraying and absorbing the residual S0 in the process gas from a sulfuric acid spray system with the drying or secondary absorption system temperature of 60 ℃ and the concentration of 98.5 percent3And when the acid temperature reaches 150 +/-15 ℃, a gas-liquid separation section is arranged at the lower part of the low-temperature absorption section, the separation section separates the process gas at the outlet of the high-temperature absorption section from the lower tower acid of the low-temperature absorption section, the separated lower tower acid of the low-temperature absorption section is sent to a branch of an output pipeline of the evaporator 6 through a pipeline, and the acid in the branch is also sent to heat exchange equipment for cooling.
The heat exchange equipment is an evaporator water supply heater 4, the residual part of sulfuric acid discharged from the evaporator and the sulfuric acid output from the bottom of the low-temperature absorption section are cooled by the evaporator water supply heater 4, the acid temperature is reduced to 170 +/-15 ℃, the cooled sulfuric acid is conveyed to an acid circulation tank 8, the sulfuric acid in the acid circulation tank 8 is conveyed to an acid cooler 10 through an acid circulation pump 9 for cooling, the cooled acid is conveyed to the upper part of a drying tower or a secondary absorption tower 7, and the acid at the bottom of the drying tower or the secondary absorption tower 7 is conveyed to the acid circulation tank 8 for circular absorption.
According to the technical scheme shown in figure 1, the flow rate of acid in the lower tower of a low-temperature absorption section is about 135000kg/h, the temperature of acid in the upper tower of the low-temperature absorption section is 60 ℃, the temperature of the acid after absorption is increased to 145 ℃, and when the prior art is adopted, the temperature of sulfuric acid from an outlet of an evaporator feed water heater to a drying or secondary absorption system is about 175 ℃, namely, the heat recovery system is equivalent to heating 135000kg/h of sulfuric acid in the lower tower of the low-temperature absorption section from 145 ℃ to 175 ℃ and then delivering the sulfuric acid out of the system. By adopting the technology, the temperature of the lower tower acid of the low-temperature absorption section is 145 ℃, and the lower tower acid is independently sent to the drying or secondary absorption system, so that the temperature of the lower tower acid of the high-temperature absorption section is increased, the heat output of the heat recovery system to the drying or secondary absorption system is reduced, and the output heat is reduced to be about Q = cm delta t =1.6x135000x (175-6kj/h, according to the heat balance, the part of heat can produce 0.6MPag low-pressure saturated steam about 2785kg/h, so that the steam production rate is improved by 15 percent.

Claims (5)

1. The utility model provides a system for improve sulphuric acid production dry-suction workshop section heat recovery steam yield which characterized in that: the system comprises a heat recovery tower (1), a drying tower or a secondary absorption tower (7), wherein the heat recovery tower (1) comprises a high-temperature absorption section, a gas-liquid separation section and a low-temperature absorption section, and the high-temperature absorption section is connected with the upper part of the high-temperature absorption section sequentially through a high-temperature circulation tank (2), a high-temperature circulation pump (5), an evaporator (6) and a mixer (3);
and a branch is further arranged on an acid pipeline connected with the evaporator (6) and the mixer (3), the branch is sequentially connected with the drying or secondary absorption system through at least one heat exchange device, and the liquid output end of the gas-liquid separation section is connected with the inlet of the heat exchange device.
2. The system of claim 1, wherein: the heat exchange equipment at least comprises an evaporator feed water heater (4).
3. The system of claim 2, wherein: the branch is connected with the upper parts of an acid circulating tank (8), an acid circulating pump (9), an acid cooler (10) and a drying tower or a secondary absorption tower (7) in sequence through an evaporator water supply heater (4).
4. The system of claim 1, wherein: the acid side of the acid cooler (10) is also provided with an output end which is connected with the upper part of the low-temperature absorption section.
5. The system of claim 3, wherein: the output end of the evaporator feed water heater (4) is connected with the evaporator (6).
CN202021226588.XU 2020-06-29 2020-06-29 System for improving heat recovery steam production rate of sulfuric acid production dry-suction workshop section Active CN212843103U (en)

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CN202021226588.XU CN212843103U (en) 2020-06-29 2020-06-29 System for improving heat recovery steam production rate of sulfuric acid production dry-suction workshop section

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CN202021226588.XU CN212843103U (en) 2020-06-29 2020-06-29 System for improving heat recovery steam production rate of sulfuric acid production dry-suction workshop section

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