CN217843822U - Device for improving steam production rate of high-temperature and high-pressure steam in acid production by sulfur - Google Patents

Device for improving steam production rate of high-temperature and high-pressure steam in acid production by sulfur Download PDF

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CN217843822U
CN217843822U CN202221794168.0U CN202221794168U CN217843822U CN 217843822 U CN217843822 U CN 217843822U CN 202221794168 U CN202221794168 U CN 202221794168U CN 217843822 U CN217843822 U CN 217843822U
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converter
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sulfur
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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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Abstract

The utility model discloses an improve device of sour high temperature high pressure steam production rate of sulphur system, this method is with the combustion air that the process gas heating of converter III section export sent into the sulfur burning furnace, sends into high-pressure waste heat boiler's high pressure feedwater with the heating of low temperature heat recovery system high temperature concentrated sulfuric acid. Adopt the technical scheme of the utility model, converter III section export economizer changes air heater into, and gas and gaseous heat transfer, heat exchange tube metal wall temperature are the average temperature of cold and hot side, are difficult to appear sulphuric acid dew point corrosion, have improved the reliability of low temperature heat recovery device operation.

Description

Device for improving steam production rate of high-temperature and high-pressure steam in acid production by sulfur
Technical Field
The utility model relates to a chemical industry field, concretely relates to improve device of sour high temperature high pressure steam production rate of sulphur system.
Background
The device for preparing acid by sulfur mainly comprises 2 procedures of sulfur burning conversion and dry absorption. Combustion of sulfur to produce S0 2 And S0 2 To SO by catalytic oxidation 3 The process reaction, the dry absorption process finishes the drying of the sulfuric acid which is sent into the combustion air of the sulfur incinerator and the SO-containing produced in the sulfur incinerator conversion process 3 The process gas absorbs and produces sulfuric acid product.
The temperature of process gas generated by combustion reaction in a sulfur burning conversion process is over 1000 ℃, a high-pressure waste heat boiler is arranged at the outlet of the sulfur burning furnace, the heat quantity of the high-temperature process gas is recovered to produce high-temperature saturated steam, the process gas is cooled by the high-pressure waste heat boiler and then enters a converter, the converter is usually provided with a plurality of sections of catalyst layers, the process gas sequentially enters each section of the converter, and S0 in the process gas 2 To SO by catalytic oxidation 3 The temperature of the post-process air is increased, the post-process air is discharged from each section of the converter to heat the process air with lower temperature, high-pressure feed water and high-pressure steam, the excess heat in the process is recovered to produce high-temperature high-pressure steam, and more than 99.5 percent of SO is added 2 Oxidation to SO 3 . Usually, an economizer is arranged at the III section of the converter to preheat feed water sent into a high-pressure boiler, and the cooled process gas is sent to a low-temperature heat recovery system high-temperature absorption tower in a dry absorption process to absorb SO in the process gas 3 (ii) a The temperature of the process gas is reduced after the process gas enters the Wen Xishou tower for absorption, the process gas with higher temperature is used for heating to the conversion temperature, and the rotary gasifier continues to carry out the remaining SO 2 Oxidation to SO 3 Then the waste slag is discharged out of the converter again for secondary absorption, and finally 99.6 percent of S0 generated by the sulfur incinerator is generated 2 Absorbed and converted into sulfuric acid.
In the dry absorption process, the combustion-supporting air fed into the sulfur incinerator is dried by adopting sulfuric acid at about 60 ℃, and the temperature of the fed combustion-supporting air is below 60 ℃; dry absorption process absorbing converter SO 3 The process for producing sulfuric acid is also exothermic, and in order to recover this part of the reaction heat, SO is introduced at the outlet of the III section of the converter 3 The primary converted gas with higher concentration is sent into a high-temperature absorption tower of a low-temperature heat recovery system, and a high-temperature absorption process is adopted, namelyAbsorbing SO in process gas by sulfuric acid with concentration of 99% and temperature of about 180 DEG C 3 Then sulfuric acid with the concentration of 98.5 percent and the temperature of about 60 ℃ is used for absorbing residual SO in the process gas 3 After the two times of sulfuric acid absorption, high-temperature (205 +/-15 ℃) concentrated sulfuric acid (the concentration is 99.5 +/-0.5%) is generated, and low-pressure saturated steam below 1.0MPa can be generated by adopting the concentrated sulfuric acid.
In the process, the temperature of combustion air fed into the sulfur incinerator is low (below 60 ℃), and about 1 ton of high-temperature high-pressure steam is produced as a byproduct when 1 ton of sulfuric acid is produced by the sulfur acid production device.
SUMMERY OF THE UTILITY MODEL
The purpose of the utility model is that: the high-pressure feed water heater of the low-temperature heat recovery system of the sulfur acid making device replaces a converter III section coal economizer in the prior art, high-temperature concentrated sulfuric acid is used for heating and feeding the high-pressure waste heat boiler feed water, the feed water temperature is increased to be equivalent to the effect of the coal economizer in the prior art, and process gas at the outlet of the converter III section is used for heating and feeding combustion-supporting air into a sulfur incinerator to increase the temperature of the sulfur incinerator. Thereby improving the steam yield of the high-temperature high-pressure steam of the sulfur acid-making device.
The purpose of the utility model can be realized by the following technical proposal:
a device for improving the steam production rate of high-temperature and high-pressure steam in the acid production from sulfur comprises a sulfur incinerator, a high-temperature absorption tower and a converter, wherein the output end of the sulfur incinerator is connected with the converter through a high-pressure waste heat boiler, and the converter is sequentially provided with a section I, a section II, a section III and a section IV from top to bottom;
the process gas outlet of the I section of the converter is connected with the II section of the converter through a high-temperature superheater, the process gas outlet of the II section of the converter is connected with the III section of the converter through a heat-heat exchanger, and the process gas outlet of the III section of the converter is connected with the bottom of the high-temperature absorption tower sequentially through a cold-heat exchanger and an air preheater.
The utility model discloses among the technical scheme: and the output end at the top of the high-temperature absorption tower is connected with the IV section of the converter through a cold-heat exchanger and a hot-heat exchanger in sequence.
The utility model discloses among the technical scheme: the bottom of the high-temperature absorption tower is connected with a high-temperature circulation tank, one output of the high-temperature circulation tank is connected with an evaporator, and the evaporator is connected with the middle part of the high-temperature absorption tower through a mixer; the other output end is connected with the desalted water heater through the high-pressure feed water heater.
In other embodiments: the high-temperature absorption tower is connected with the evaporator through the high-temperature circulating groove, and one output end of the evaporator is connected with the middle part of the high-temperature absorption tower through the mixer; the other output end is connected with the desalted water heater through the high-pressure feed water heater.
The utility model discloses among the technical scheme: an output pipeline of high-pressure water supply is sequentially connected with the high-pressure water supply heater, the IV-section economizer and the high-pressure waste heat boiler, and a gas output end of the high-pressure waste heat boiler is sequentially connected with the low-temperature superheater and the high-temperature superheater.
The utility model discloses among the technical scheme: the output pipe of the combustion-supporting air is connected with the sulfur burner through an air preheater.
The method for improving the steam yield of high-temperature high-pressure steam in the acid production from sulfur by using the device heats combustion-supporting air fed into a sulfur incinerator by using process gas at the outlet of the section III of the converter, and heats high-pressure feed water fed into a high-pressure waste heat boiler by using high-temperature concentrated sulfuric acid of a low-temperature heat recovery system.
The method comprises the following steps: and (3) heating high-pressure feed water fed into the high-pressure waste heat boiler by using high-temperature concentrated sulfuric acid at the outlet of the high-temperature circulating pump of the low-temperature heat recovery system.
The method comprises the following steps: high-pressure feed water fed into a high-pressure waste heat boiler is heated by high-temperature concentrated sulfuric acid at an outlet of an evaporator of a low-temperature heat recovery system.
In the first technical scheme:
the temperature of process gas at the outlet of the section III of the converter is 480 +/-15 ℃, the process gas is firstly sent into a cold-heat exchanger to heat the process gas at the outlet of the high-temperature absorption tower of the low-temperature heat recovery system in the dry absorption process, the temperature is reduced to 280 +/-15 ℃, then the process gas is sent into an air preheater to heat combustion-supporting air at about 60 ℃ to 160 +/-25 ℃, and the process gas is sent into the low-temperature heat recovery system in the dry absorption process after the temperature is reduced to adopt the high-temperature absorption tower. The combustion-supporting air is heated to 160 +/-25 ℃ by an air preheater and then is sent into a sulfur burning furnace, sulfur is burned in the sulfur burning furnace to generate high-temperature (1120 +/-50 ℃) process gas, the high-temperature process gas enters a high-temperature high-pressure waste heat boiler, and high-pressure feed water is heated to generate high-pressure saturated steam.
The process gas from the outlet of the III section of the converter is cooled by a cold-heat exchanger and then enters a high-temperature absorption tower of a low-temperature heat recovery system in a dry absorption process, and S0 in the process gas is absorbed by adopting a high-temperature absorption process 3 The acid temperature at the bottom of the heat recovery tower reaches 205 +/-15 ℃, the concentration reaches 99.5 +/-0.5 percent and becomes high-temperature concentrated sulfuric acid, the high-temperature concentrated sulfuric acid enters a high-temperature circulation tank, a part of concentrated sulfuric acid (20 +/-10 percent) is pressurized by a high-temperature circulation pump, then the high-temperature concentrated sulfuric acid is sent to a high-pressure feed water heater to preheat the high-pressure feed water at the temperature of 104 ℃ to 150 +/-15 ℃, the subsequent flow of the high-pressure feed water is consistent with the prior art, and then the high-pressure feed water enters an IV-section economizer to be preheated and then is sent to a high-pressure waste heat boiler.
In a second technical solution:
the conditions are the same as the first technical scheme, except that the process gas from the outlet of the III section of the converter enters the high-temperature absorption tower of the low-temperature heat recovery system of the dry absorption process after being cooled by the cold-heat exchanger, and the high-temperature absorption process is adopted to absorb S0 in the process gas 3 The acid temperature at the bottom of the heat recovery tower reaches 205 +/-15 ℃, the concentration reaches 99.5 +/-0.5 percent and becomes high-temperature concentrated sulfuric acid, the high-temperature concentrated sulfuric acid enters a high-temperature circulation tank, is pressurized by a high-temperature circulation pump and then completely enters an evaporator, the concentrated sulfuric acid is cooled to 190 +/-15 ℃ after being discharged from the evaporator, a part of the concentrated sulfuric acid (20 +/-10 percent) is sent to a high-pressure feed water heater to preheat high-pressure feed water at 104 ℃ to 135 +/-15 ℃, the subsequent flow of the high-pressure feed water is consistent with the prior art, and then the high-pressure feed water enters an IV economizer to be preheated and then is sent to a high-pressure waste heat boiler.
The utility model has the advantages that:
in the prior art, process gas at an outlet of a section III of a converter enters an economizer, water is fed into a high-pressure boiler in a preheating mode, and the process gas enters a heat recovery tower of a low-temperature heat recovery system after the temperature of the process gas is reduced. In the actual production process, the process gas exchanges heat with the feed water, the heat exchange coefficient of the water side is far larger than that of the process gas side, the temperature of the outer wall of the metal of the heat exchange tube is closer to the temperature of the water side, when the temperature of the feed water is lower, the temperature of the outer wall of the metal of the heat exchange tube of the economizer is lower than the dew point of gaseous sulfuric acid in the process gas, the sulfuric acid is condensed to corrode equipment, once the heat exchange tube bundle corrodes and perforates, high-pressure feed water rapidly leaks in a large amount, if the high-pressure feed water is not discovered in time, the acid concentration of a low-temperature heat recovery system at the downstream of the economizer at the outlet of the section III is rapidly reduced, the acid temperature is rapidly increased, and the corrosion and scrapping of the system equipment can be caused in a short time. Adopt the technical scheme of the utility model, converter III section export economizer changes into air heater, and gaseous heat transfer, heat exchange tube metal wall temperature are the average temperature of cold and hot side, are difficult to appear sulphuric acid dew point corrosion, have improved the reliability of low temperature heat recovery device operation.
Drawings
Fig. 1 is a first schematic diagram of the device of the present invention.
Fig. 2 is a second schematic diagram of the device of the present invention.
Wherein: the system comprises a 1-sulfur burner, a 2-high-pressure waste heat boiler, a 3-air preheater, a 4-cold-heat exchanger, a 5-hot-heat exchanger, a 6-converter, a 7-evaporator, an 8-high-pressure feed water heater, a 9-desalted water heater, a 10-high-temperature circulating pump, an 11-mixer, a 12-high-temperature circulating tank, a 13-high-temperature absorption tower, a 14-IV section economizer, a 15-low-temperature superheater and a 16-high-temperature superheater.
Detailed Description
The present invention will be further described with reference to the following embodiments, but the scope of the present invention is not limited thereto:
referring to fig. 1-2, a device for increasing the steam generation rate of high-temperature high-pressure steam in the acid production from sulfur comprises a sulfur incinerator 1, a high-temperature absorption tower 13 and a converter 6, wherein the output end of the sulfur incinerator 1 is connected with the converter 6 through a high-pressure waste heat boiler 2, and the converter is sequentially provided with a section i, a section ii, a section iii and a section iv from top to bottom;
the process gas outlet of the first section of the converter is connected with the second section of the converter through a high-temperature superheater 16, the process gas outlet of the second section of the converter is connected with the third section of the converter through a hot heat exchanger 5, and the process gas outlet of the third section of the converter is connected with the bottom of a high-temperature absorption tower 13 through a cold heat exchanger 4 and an air preheater 3 in sequence. The output end at the top of the high-temperature absorption tower 13 is connected with the IV section of the converter through the cold-heat exchanger 4 and the hot-heat exchanger 5 in sequence. An output pipeline of high-pressure feed water is sequentially connected with a high-pressure feed water heater 8, an IV-section economizer 14 and the high-pressure waste heat boiler 2, and a gas output end of the high-pressure waste heat boiler 2 is sequentially connected with a low-temperature superheater 15 and a high-temperature superheater 16. The output pipe of the combustion air is connected with the sulfur incinerator 1 through an air preheater 3.
The bottom of the high-temperature absorption tower 13 is connected with a high-temperature circulating tank 12, one output of the high-temperature circulating tank 12 is connected with an evaporator 7, and the evaporator 7 is connected with the middle part of the high-temperature absorption tower 13 through a mixer 11; the other output end is connected with a desalted water heater 9 through a high-pressure feed water heater 8 in sequence.
Or, the high temperature absorption tower 13 is connected with the evaporator 7 through the high temperature circulation tank 12, and one output end of the evaporator is connected with the middle part of the high temperature absorption tower 13 through the mixer 11; the other output end is connected with a desalted water heater 9 through a high-pressure feed water heater 8 in sequence.
As shown in figure 1, the temperature of the process gas at the outlet of the section III of the converter is 480 +/-15 ℃, the process gas is firstly sent into a cold-heat exchanger 4 to heat the process gas at the outlet of a high-temperature heat recovery system 13 in the dry absorption process, the temperature is reduced to 280 +/-15 ℃, then the process gas is sent into an air preheater 3 to heat combustion-supporting air at about 60 ℃ to 160 +/-25 ℃, and the process gas is sent into the low-temperature heat recovery system in the dry absorption process to adopt the high-temperature absorption tower after the temperature of the process gas is reduced. Combustion air is heated to 160 +/-25 ℃ by an air preheater 3 and then sent into a sulfur incinerator 1, sulfur is combusted in the sulfur incinerator to generate high-temperature (1120 +/-50 ℃) process gas, the high-temperature process gas enters a high-temperature high-pressure waste heat boiler 2, high-pressure feed water is heated to generate high-pressure saturated steam, and the high-pressure saturated steam is superheated into high-temperature high-pressure superheated steam by a converter IV outlet low-temperature superheater 15 and a converter I section outlet high-temperature superheater 16.
The process gas from the outlet of the III section of the converter is cooled by a cold-heat exchanger and then enters a high-temperature absorption tower 13 of a low-temperature heat recovery system in a dry absorption process, and S0 in the process gas is absorbed by adopting a high-temperature absorption process 3 The acid temperature at the bottom of the heat recovery tower 13 reaches 205 +/-15 ℃, the concentration reaches 99.5 +/-0.5 percent to become high-temperature concentrated sulfuric acid, the high-temperature concentrated sulfuric acid enters a high-temperature circulating tank 12, then is pressurized by a high-temperature circulating pump 10, and then a part of concentrated sulfuric acid (20 +/-10 percent) is sent to a high-pressure feed water heater to preheat the high-pressure feed water at the temperature of 104 ℃ to 150 +/-15 ℃, and the high-pressure feed water is fed into a high-pressure feed water heaterAnd (3) preheating the waste gas in an economizer 14 at the section IV, then sending the waste gas to a high-pressure waste heat boiler 2, cooling the process gas at the outlet of the sulfur burner at 1120 +/-50 ℃ to produce high-pressure saturated steam, and overheating the saturated steam by a low-temperature superheater 15 and a high-temperature superheater 16 to obtain high-temperature high-pressure superheated steam.
By adopting the process flow, the yield of the high-temperature high-pressure superheated steam of 1 ton of sulfuric acid produced by the acid making device is improved to about 1.07 ton.
As shown in figure 2, the temperature of the process gas at the outlet of the section III of the converter is 480 +/-15 ℃, the process gas is firstly sent into a cold-heat exchanger 4 to heat the process gas at the outlet of a high-temperature heat recovery system 13 in the dry absorption process, the temperature is reduced to 280 +/-15 ℃, then the process gas is sent into an air preheater 3 to heat combustion-supporting air at about 60 ℃ to 160 +/-25 ℃, and the process gas is sent into the low-temperature heat recovery system in the dry absorption process to adopt the high-temperature absorption tower after the temperature of the process gas is reduced. Combustion air is heated to 160 +/-25 ℃ by an air preheater 3 and then sent into a sulfur incinerator 1, sulfur is combusted in the sulfur incinerator to generate high-temperature (1120 +/-50 ℃) process gas, the high-temperature process gas enters a high-temperature high-pressure waste heat boiler 2, high-pressure feed water is heated to generate high-pressure saturated steam, and the high-pressure saturated steam is superheated into high-temperature high-pressure superheated steam by a converter IV outlet low-temperature superheater 15 and a converter I section outlet high-temperature superheater 16.
The process gas from the outlet of the III section of the converter is cooled by a cold-heat exchanger and then enters a high-temperature absorption tower 13 of a low-temperature heat recovery system in a dry absorption process, and S0 in the process gas is absorbed by adopting a high-temperature absorption process 3 The acid temperature at the bottom of the heat recovery tower 13 reaches 205 +/-15 ℃, the concentration reaches 99.5 +/-0.5 percent and becomes high-temperature concentrated sulfuric acid, the high-temperature concentrated sulfuric acid enters a high-temperature circulation tank 12, is pressurized by a high-temperature circulation pump 10 and then completely enters an evaporator 7, the concentrated sulfuric acid is cooled to 190 +/-15 ℃ after being discharged from the evaporator 7, a part of the concentrated sulfuric acid (20 +/-10 percent) is sent to a high-pressure feed water heater to preheat high-pressure feed water at 104 ℃ to 135 +/-15 ℃, the high-pressure feed water enters an IV-section economizer 14 to be preheated and then is sent to a high-pressure waste heat boiler 2, the process gas at the outlet of a sulfur burning furnace at 1120 +/-50 ℃ is cooled, high-pressure saturated steam is produced, and the high-temperature saturated steam is superheated by a low-temperature superheater 15 and a high-temperature superheater 16 to become high-temperature high-pressure superheated steam.
By adopting the process flow, the yield of the high-temperature high-pressure superheated steam of 1 ton of sulfuric acid produced by the acid making device is improved to about 1.06 ton.
The utility model discloses the principle: the high-pressure feed water heater of the low-temperature heat recovery system of the sulfur acid making device replaces a converter III section economizer in the prior art, high-temperature concentrated sulfuric acid is used for heating and feeding feed water into a high-pressure waste heat boiler, the feed water temperature is increased to be equivalent to the effect of the coal economizer in the prior art, and process gas at the outlet of the converter III section is used for heating and feeding combustion-supporting air into a sulfur incinerator, so that the temperature of the sulfur incinerator is increased. Thereby improving the steam yield of high-temperature and high-pressure steam of the sulfur acid production device. The high-temperature and high-pressure steam production rate of the sulfur acid-making device adopting the method is improved by 6 to 7 percent when 1 ton of sulfuric acid is produced.

Claims (6)

1. The utility model provides an improve device of sour high temperature high pressure steam production rate of sulphur system which characterized in that: the device comprises a sulfur incinerator (1), a high-temperature absorption tower (13) and a converter (6), wherein the output end of the sulfur incinerator (1) is connected with the converter (6) through a high-pressure waste heat boiler (2), and the converter is sequentially provided with a section I, a section II, a section III and a section IV from top to bottom;
the process gas outlet of the first section of the converter is connected with the second section of the converter through a high-temperature superheater (16), the process gas outlet of the second section of the converter is connected with the third section of the converter through a hot heat exchanger (5), and the process gas outlet of the third section of the converter is connected with the bottom of a high-temperature absorption tower (13) through a cold heat exchanger (4) and an air preheater (3) in sequence.
2. The device for improving the steam production rate of the high-temperature high-pressure steam of the sulfur acid production according to claim 1, which is characterized in that: the output end of the top of the high-temperature absorption tower (13) is connected with the IV section of the converter through a cold-heat exchanger (4) and a hot-heat exchanger (5) in sequence.
3. The device for improving the steam production rate of the high-temperature high-pressure steam of the sulfur acid production according to claim 1, which is characterized in that: the bottom of the high-temperature absorption tower (13) is connected with a high-temperature circulating tank (12), one output of the high-temperature circulating tank (12) is connected with an evaporator (7), and the evaporator (7) is connected with the middle part of the high-temperature absorption tower (13) through a mixer (11); the other output end is connected with a desalted water heater (9) through a high-pressure feed water heater (8) in sequence.
4. The device for improving the steam production rate of the high-temperature high-pressure steam for preparing acid from sulfur according to claim 1, which is characterized in that: the high-temperature absorption tower (13) is connected with the evaporator (7) through a high-temperature circulating groove (12), and one output end of the evaporator is connected with the middle part of the high-temperature absorption tower (13) through a mixer (11); the other output end is connected with a desalted water heater (9) through a high-pressure feed water heater (8) in sequence.
5. The apparatus for increasing the steam production rate of high-temperature high-pressure steam from sulfur-producing acid according to claim 3, wherein: an output pipeline of high-pressure feed water is sequentially connected with a high-pressure feed water heater (8), an IV-section economizer (14) and a high-pressure waste heat boiler (2), and a gas output end of the high-pressure waste heat boiler (2) is sequentially connected with a low-temperature superheater (15) and a high-temperature superheater (16).
6. The device for improving the steam production rate of the high-temperature high-pressure steam of the sulfur acid production according to claim 1, which is characterized in that: the output pipe of the combustion-supporting air is connected with the sulfur incinerator (1) through an air preheater (3).
CN202221794168.0U 2022-07-12 2022-07-12 Device for improving steam production rate of high-temperature and high-pressure steam in acid production by sulfur Active CN217843822U (en)

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