CN205115045U - Improve ore deposit or smelt device of sour low temperature heat recovery of flue gas sulfur production - Google Patents
Improve ore deposit or smelt device of sour low temperature heat recovery of flue gas sulfur production Download PDFInfo
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- CN205115045U CN205115045U CN201520917546.3U CN201520917546U CN205115045U CN 205115045 U CN205115045 U CN 205115045U CN 201520917546 U CN201520917546 U CN 201520917546U CN 205115045 U CN205115045 U CN 205115045U
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- acid
- tower
- absorption tower
- moisture absorption
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The utility model discloses an improve ore deposit or smelt device of sour low temperature heat recovery of flue gas sulfur production, set up the moisture absorption system in the sulphuric acid device, pass through the tube coupling between moisture absorption system and low temperature heat recovery system and the drying system to the cluster of regarding the sulphuric acid in the moisture absorption system as low temperature heat recovery system blender is sour, and adopt this kind of method can make the ore deposit or to smelt the sour device low temperature heat recovery system's of flue gas sulfur production the rate of steaming sour by 0.3-0.35 ton of common vapour / ton, brings up to 0.46-0.53 ton of vapour / ton acid, and the improvement rate of steaming is more than 50%.
Description
Technical field
The utility model belongs to waste heat or waste heat recovery field, is specifically related to a kind of device improving ore deposit or the recovery of flue gas during smelting Sulphuric acid Low Temperature Thermal.
Background technology
Ore deposit or smelting gas relieving haperacidity industry are equipped with the waste heat that middle pressure waste heat boiler reclaims high-temperature flue gas after fluidizing furnace (or smelting furnace) both at home and abroad at present, the heat that economizer reclaims the middle temperature flue gas of conversion reaction (Sulphur Dioxide is sulphur trioxide) is equipped with at conversion section, in dry absorption section, more existing devices are provided with low-temperature heat recovery system, low-temperature heat recovery system can see patent " a kind of device and method improving ore deposit or smelt gas acid preparing heat organic efficiency ", application number: 201410127399.X.The dry absorption section of ore deposit or flue gas during smelting Sulphuric acid device generally comprises dry recycle system, low-temperature heat recovery system, two inhales the recycle system.Dry recycle system is the dry flue gas from purification section mainly, absorbs the moisture content in flue gas and dry recycle acid concentration is reduced, and two inhale the recycle systems and low-temperature heat recovery system because recycle acid absorbs and contains SO from conversion section
3flue gas and the concentration of recycle acid is raised, therefore, in order to keep the recycle acid concentration of each system of dry absorption section constant and solve isorrheic problem, between each system, need string acid.
Existing low-temperature heat recovery system string enter acid be from dry recycle system string go out about 94% the vitriol oil, in order to keep the material balance of low-temperature heat recovery system, low-temperature heat recovery system must again by this part sulfuric acid string to dry absorption section other system.And the factor that impact seals in low-temperature heat recovery system sulfuric acid amount to mainly contain three: first be temperature from purification section flue gas, because the flue gas entering dry recycle system is saturated flue gas substantially, temperature is about 30 ~ 45 DEG C, flue-gas temperature is higher, the moisture content bringing dry recycle system into is more, and string acid amount is larger; Second is the product acid concentration of dry absorption section, and it is higher to produce acid concentration, and the moisture content taking whole dry absorption section out of is fewer, and string acid is measured larger; 3rd is the concentration of the sulfuric acid sealing in low-temperature heat recovery system, and the concentration sealing in sulfuric acid is lower, and string acid amount is fewer.When therefore raising or produce along with sulfuric acid apparatus the concentration rising of acid when the temperature from purification section flue gas, the acid amount that dehumidification system seals in low-temperature heat recovery system is larger, and the sulfuric acid temperature of low-temperature heat recovery system of going here and there out is higher about 60 ~ 100 DEG C than what seal in, namely the heat taking low-temperature heat recovery system out of increases greatly, therefore just reduces the effect that Low Temperature Thermal reclaims.
Utility model content
The utility model arranges moisture sorbing system before the dehumidification system in ore deposit or flue gas during smelting Sulphuric acid device, moisture sorbing system and dehumidification system and low-temperature heat recovery system three are combined, while guarantee drying efficiency, can the sulfuric acid of about 94% of original dehumidification system be replaced to seal in low-temperature heat recovery system the sulfuric acid of 30 ~ 70% concentration of moisture sorbing system again, the method that this string is sour is only original about 5 ~ 20%, by reducing string acid amount, improve the steam generating capacity of low-temperature heat recovery system.
The purpose of this utility model can be achieved through the following technical solutions:
Improve a method for ore deposit or the recovery of flue gas during smelting Sulphuric acid Low Temperature Thermal, the method comprises the following steps:
(1) the some or all of flue gas of self-purification workshop section is delivered to the bottom of moisture absorption tower in the future, the sulfuric acid being 30 ~ 70% from moisture absorption tower acid circulation groove concentration is delivered to moisture absorption tower top, and the flue gas that moisture absorption tower bottom is up and concentration are the sulfuric acid counter current contact moisture absorption of 30 ~ 70%; Flue gas after moisture absorption and the remaining bottom entering drying tower from purification section flue gas, the absorption liquid after moisture absorption is back to the recycle of moisture absorption tower acid circulation groove;
(2) sulfuric acid being 92 ~ 98.5% by concentration in dry tower acid circulation groove is delivered to the top of drying tower, and contact with the back flow of gas entered and carry out drying, dried flue gas removes a conversion system, and dry liquid is back to the recycle of dry tower acid circulation groove;
(3) gas of 140 ~ 300 DEG C after a conversion system transforms enters the bottom on high temperature absorption tower, gas bottom this successively with high temperature absorption tower in the middle part of from the first order concentration of mixing tank to be the vitriol oil of 99% and the two-stage concentration on top be 98.5% vitriol oil counter current contact react, react the system acid that the concentration terminating rear generation 190 ± 30 DEG C is 99.5 ± 0.5%, the water passed to by heat in vaporizer is delivered in vaporizer by after this system acid pressurization, thus produce the low-pressure steam of 0.6 ± 0.4MPa, the system acid part exported from vaporizer enters mixing tank, pass into from concentration in moisture absorption tower acid circulation groove in mixing tank is the sulfuric acid concentration to 99% in the sulfuric acid adjusting mixer of 30 ~ 70% simultaneously.
In the method that Low Temperature Thermal described in technical solutions of the utility model reclaims: be delivered in moisture absorption tower acid circulation groove or by low-temperature heat recovery system being exported acid by the sulfuric acid that is 92 ~ 98.5% by the concentration in dry tower acid circulation groove and be delivered in moisture absorption tower acid circulation groove, thus the sulfuric acid concentration in adjustment moisture absorption tower acid circulation groove is 30 ~ 70%.
In the method that Low Temperature Thermal described in technical solutions of the utility model reclaims: by system acid to be delivered in dry tower acid circulation groove thus to regulate the concentration of sulfuric acid in dry tower acid circulation groove to be 92 ~ 98.5%.
In the method that Low Temperature Thermal described in technical solutions of the utility model reclaims: in moisture absorption tower acid circulation groove, the temperature of acid is less than 70 DEG C.
In the method that Low Temperature Thermal described in technical solutions of the utility model reclaims: a part for system acid enters mixing tank, this part is 5 ~ 15% of system acid total amount.
Passing into from concentration in moisture absorption tower acid circulation groove in technical solutions of the utility model in mixing tank is the sulfuric acid concentration to 99% in the sulfuric acid adjusting mixer of 30 ~ 70%, in other embodiments, if the sulfuric acid of 30 ~ 70% can not make the sulfuric acid concentration to 99% in mixing tank, now can add appropriate process water in a mixer and regulate.
A kind of device improving ore deposit or the recovery of flue gas during smelting Sulphuric acid Low Temperature Thermal, described device comprises moisture absorption tower, drying tower and high temperature absorption tower, the output terminal of described moisture absorption top of tower is connected with drying tower bottom, the output terminal of described moisture absorption tower bottom is connected with moisture absorption tower acid circulation groove, and the output terminal of moisture absorption tower acid circulation groove is connected with the top of moisture absorption tower by moisture absorption tower acid recycle pump; The output terminal on the top of described drying tower is connected with a conversion system, and the output terminal of described drying tower bottom is connected with dry tower acid circulation groove, and the output terminal of dry tower acid circulation groove is connected with the top of drying tower by drying tower acid circulating pump; The output terminal of a described conversion system is connected with the bottom on high temperature absorption tower, and the output terminal at top, high temperature absorption tower is connected with twice converted system, and the output terminal bottom high temperature absorption tower is connected with vaporizer with high-temperature acid circulation groove, high-temperature acid recycle pump successively; An output terminal of described vaporizer is connected with mixing tank, and the output channel of moisture absorption tower acid recycle pump is provided with a branch road, and this branch road is also connected with mixing tank; The output terminal of described mixing tank is connected with the middle and upper part on high temperature absorption tower.
In the device that raising ore deposit described in the utility model or flue gas during smelting Sulphuric acid Low Temperature Thermal reclaim, another output terminal of vaporizer is connected with de-salted water well heater with evaporator feedwater well heater successively, described de-salted water well heater output terminal be provided with two pipelines, a pipeline is connected with dry tower acid circulation groove, and another pipeline is connected with two desorption systems.
In the device that raising ore deposit described in the utility model or flue gas during smelting Sulphuric acid Low Temperature Thermal reclaim, between the pipeline that moisture absorption tower acid water cooler is connected with moisture absorption tower acid circulation groove at the output terminal of moisture absorption tower bottom or between the pipeline that is connected of the input terminus of described moisture absorption tower acid water cooler on the top of moisture absorption tower and moisture absorption tower acid recycle pump.
In the device that raising ore deposit described in the utility model or flue gas during smelting Sulphuric acid Low Temperature Thermal reclaim, between the pipeline that drying tower acid cooler is connected at bottom output terminal and the dry tower acid circulation groove of drying tower or between the pipeline that is connected of the input terminus of described drying tower acid cooler on drying tower top and drying tower acid circulating pump.
In the device that raising ore deposit described in the utility model or flue gas during smelting Sulphuric acid Low Temperature Thermal reclaim, moisture absorption tower is packing tower, foam column, void tower, dynamic wave or Venturi.
In the device that raising ore deposit described in the utility model or flue gas during smelting Sulphuric acid Low Temperature Thermal reclaim, moisture absorption tower and drying tower are integrated.
The beneficial effects of the utility model: adopt prior art (application number: 201410127399.X), the sulfuric acid sealing in low-temperature heat recovery system mixing tank be from dehumidification system about 94% sulfuric acid, the low-temperature heat recovery system steam generating capacity of this technology is about 0.3 ~ 0.35 ton of vapour/ton acid; After adopting the utility model, the sulfuric acid sealing in low-temperature heat recovery system mixing tank is the sulfuric acid of 30 ~ 70% concentration from moisture sorbing system, the method that this string is sour is only original about 5 ~ 20%, by reducing string acid amount, low-temperature heat recovery system steam generating capacity can bring up to 0.46 ~ 0.53 ton of vapour/ton acid, improves steam generating capacity more than 50%.
Accompanying drawing explanation
Fig. 1,2,3 is process flow diagram of the present utility model.
1-moisture absorption tower, 2-moisture absorption tower acid circulation groove, 3-moisture absorption tower acid recycle pump, 4-moisture absorption tower acid water cooler, 5-drying tower, the dry tower acid circulation groove of 6-, 7-drying tower acid circulating pump, 8-drying tower acid cooler, 9-high temperature absorption tower, 10-high-temperature acid circulation groove, 11-high-temperature acid recycle pump, 12-vaporizer, 13-mixing tank, 14-evaporator feedwater well heater, 15-de-salted water well heater.
Embodiment
Below in conjunction with embodiment, the utility model is described further, but protection domain of the present utility model is not limited thereto:
As Fig. 1,2 and 3, a kind of device improving ore deposit or the recovery of flue gas during smelting Sulphuric acid Low Temperature Thermal, described device comprises moisture absorption tower (1), drying tower (5) and high temperature absorption tower (9), the output terminal at described moisture absorption tower (1) top is connected with drying tower (5) bottom, the output terminal of described moisture absorption tower (1) bottom is connected with moisture absorption tower acid circulation groove (2), and the output terminal of moisture absorption tower acid circulation groove (2) is connected with the top of moisture absorption tower (1) by moisture absorption tower acid recycle pump (3); The output terminal on the top of described drying tower (5) is connected with a conversion system, the output terminal of described drying tower (5) bottom is connected with dry tower acid circulation groove (6), and the output terminal of dry tower acid circulation groove (6) is connected with the top of drying tower (5) by drying tower acid circulating pump (7); The output terminal of a described conversion system is connected with the bottom of high temperature absorption tower (9), the output terminal at high temperature absorption tower (9) top is connected with twice converted system, and the output terminal of high temperature absorption tower (9) bottom is connected with vaporizer (12) with high-temperature acid circulation groove (10), high-temperature acid recycle pump (11) successively; An output terminal of described vaporizer (12) is connected with mixing tank (13), and the output channel of moisture absorption tower acid recycle pump (3) is provided with a branch road, and this branch road is also connected with mixing tank (13); The output terminal of described mixing tank (13) is connected with the middle and upper part of high temperature absorption tower (9).Another output terminal of vaporizer (12) is connected with de-salted water well heater (15) with evaporator feedwater well heater (14) successively, described de-salted water well heater (15) output terminal be provided with two pipelines, a pipeline is connected with dry tower acid circulation groove (6), and another pipeline is connected with two desorption systems.Between the pipeline that is connected with moisture absorption tower acid circulation groove (2) of output terminal that moisture absorption tower acid water cooler (4) is positioned at moisture absorption tower (1) bottom or described moisture absorption tower acid water cooler (4) be positioned between the input terminus on the top of moisture absorption tower (1) and the connected pipeline of moisture absorption tower acid recycle pump (3).Drying tower acid cooler (8) is positioned between pipeline that the bottom output terminal of drying tower (5) and dry tower acid circulation groove (6) be connected or described drying tower acid cooler (8) is positioned between the pipeline that the input terminus on drying tower (5) top and drying tower acid circulating pump (7) be connected.Described moisture absorption tower is packing tower, foam column, void tower, dynamic wave or Venturi.
A kind of method improving ore deposit or the recovery of flue gas during smelting Sulphuric acid Low Temperature Thermal, for 660t/d ore deposit sulphuric acid plant, the method is that the flue gas of about 38 DEG C, self-purification workshop section in the future enters moisture absorption tower, the temperature of moisture absorption tower top spray is 55 ~ 65 DEG C, concentration is after the portion of water in 50 ~ 70% sulfuric acid absorption flue gases, the flue gas after absorption is sent into the bottom of drying tower, the absorption liquid after moisture absorption is back to moisture absorption tower acid circulation groove for recycle again; The sulfuric acid being 92 ~ 98.5% by concentration in dry tower acid circulation groove is delivered to the top of drying tower, and contact with the back flow of gas entered and carry out drying, dried flue gas removes a conversion system, and dry liquid is back to dry tower acid circulation groove for recycle; Send into a conversion system and carry out SO
2conversion after, carry out the SO to once transforming 140 ~ 300 DEG C
3process gas enters the high temperature absorption tower of low-temperature heat recovery system, the concentration spraying middle part successively with high temperature absorption tower one-level to be concentration that the vitriol oil of 99% and the secondary on top spray be 98.5% vitriol oil counter current contact react, to generate temperature be the concentration of 190 ± 30 DEG C be 99.5 ± 0.5% system acid, this system acid also enters high-temperature acid circulation groove, and sending into vaporizer generation pressure through the pressurization of high-temperature acid recycle pump is the low-pressure steam of 0.6 ± 0.4MPa; 10% of this system acid enters in mixing tank, pass into from moisture absorption tower acid circulation groove temperature in mixing tank is 55 ~ 65 DEG C simultaneously, concentration is the sulfuric acid of 50 ~ 70%, thus the concentration of sulfuric acid in maintenance mixing tank is 99%, is that the sulfuric acid of 99% is delivered to the middle part on high temperature absorption tower and carries out counter current contact reaction with the gas of bottom by the concentration in mixing tank.Another part system is produced acid and is sent into evaporator feedwater well heater and de-salted water well heater respectively successively, and the acid amount gone out from de-salted water well heater string is about 101200kg/h, and sour temperature is about 60 ~ 100 DEG C, and steam generating capacity is 0.46 ~ 0.53 ton of vapour/ton acid.This temperature is that the acid of 60 ~ 100 DEG C is divided into two parts, and a part is delivered in dry tower acid circulation groove, thus regulates the sulfuric acid concentration in dry tower acid circulation groove to be 92 ~ 98.5%; Another part is delivered to two desorption systems.
Be delivered in moisture absorption tower acid circulation groove or by low-temperature heat recovery system being exported acid by the sulfuric acid that is 92 ~ 98.5% by the concentration in dry tower acid circulation groove in this embodiment and be delivered in moisture absorption tower acid circulation groove, thus regulate the sulfuric acid concentration in moisture absorption tower acid circulation groove to be 50 ~ 70%.
By system acid to be delivered in dry tower acid circulation groove thus to regulate the concentration of sulfuric acid in dry tower acid circulation groove to be 92 ~ 98.5% in this embodiment.
For 660t/d ore deposit sulphuric acid plant, when adopting the method for patent (201410127399.X), the acid amount sealing in about 94% of mixing tank in low-temperature heat recovery system is about 51000kg/h, acid temperature is about 60 DEG C, the acid amount that low-temperature heat recovery system goes out from de-salted water well heater string is about 145000kg/h, acid temperature is about 120 ~ 150 DEG C, and steam generating capacity is 0.3 ~ 0.35 ton of vapour/ton acid, and when adopting the utility model, the acid amount sealing in about 50 ~ 70% of mixing tank in low-temperature heat recovery system is about 7200kg/h, acid temperature is about 55 ~ 65 DEG C, the acid amount that low-temperature heat recovery system is gone here and there out from de-salted water well heater 15 is about 101200kg/h, acid temperature is about 60 ~ 100 DEG C, only from the string acid amount of two kinds of methods, the acid amount adopting the acid amount of taking out of from low-temperature heat recovery system during the utility model and acid temperature comparatively to adopt the method for patent (201410127399.X) to take out of from low-temperature heat recovery system and acid temperature reduce all greatly, when namely adopting the utility model, the recoverable heat of low-temperature heat recovery system improves greatly, steam generating capacity is 0.46 ~ 0.53 ton of vapour/ton acid, improve steam generating capacity more than 50%.
Claims (6)
1. one kind is improved the device of ore deposit or the recovery of flue gas during smelting Sulphuric acid Low Temperature Thermal, it is characterized in that: described device comprises moisture absorption tower (1), drying tower (5) and high temperature absorption tower (9), the output terminal at described moisture absorption tower (1) top is connected with drying tower (5) bottom, the output terminal of described moisture absorption tower (1) bottom is connected with moisture absorption tower acid circulation groove (2), and the output terminal of moisture absorption tower acid circulation groove (2) is connected with the top of moisture absorption tower (1) by moisture absorption tower acid recycle pump (3); The output terminal on the top of described drying tower (5) is connected with a conversion system, the output terminal of described drying tower (5) bottom is connected with dry tower acid circulation groove (6), and the output terminal of dry tower acid circulation groove (6) is connected with the top of drying tower (5) by drying tower acid circulating pump (7); The output terminal of a described conversion system is connected with the bottom of high temperature absorption tower (9), the output terminal at high temperature absorption tower (9) top is connected with twice converted system, and the output terminal of high temperature absorption tower (9) bottom is connected with vaporizer (12) with high-temperature acid circulation groove (10), high-temperature acid recycle pump (11) successively; An output terminal of described vaporizer (12) is connected with mixing tank (13), and the output channel of moisture absorption tower acid recycle pump (3) is provided with a branch road, and this branch road is also connected with mixing tank (13); The output terminal of described mixing tank (13) is connected with the middle and upper part of high temperature absorption tower (9).
2. the device of raising ore deposit according to claim 1 or the recovery of flue gas during smelting Sulphuric acid Low Temperature Thermal, it is characterized in that: another output terminal of vaporizer (12) is connected with de-salted water well heater (15) with evaporator feedwater well heater (14) successively, described de-salted water well heater (15) output terminal be provided with two pipelines, a pipeline is connected with dry tower acid circulation groove (6), and another pipeline is connected with two desorption systems.
3. the device that reclaims of raising ore deposit according to claim 1 or flue gas during smelting Sulphuric acid Low Temperature Thermal, is characterized in that: between the pipeline that the output terminal that moisture absorption tower acid water cooler (4) is positioned at moisture absorption tower (1) bottom is connected with moisture absorption tower acid circulation groove (2) or described moisture absorption tower acid water cooler (4) be positioned between the input terminus on the top of moisture absorption tower (1) and the connected pipeline of moisture absorption tower acid recycle pump (3).
4. the device that reclaims of raising ore deposit according to claim 1 or flue gas during smelting Sulphuric acid Low Temperature Thermal, is characterized in that: drying tower acid cooler (8) is positioned between pipeline that the bottom output terminal of drying tower (5) and dry tower acid circulation groove (6) be connected or described drying tower acid cooler (8) is positioned between the pipeline that the input terminus on drying tower (5) top and drying tower acid circulating pump (7) be connected.
5. the device of raising ore deposit according to claim 1 or the recovery of flue gas during smelting Sulphuric acid Low Temperature Thermal, is characterized in that: moisture absorption tower is packing tower, foam column, void tower, dynamic wave or Venturi.
6. the device of raising ore deposit according to claim 4 or the recovery of flue gas during smelting Sulphuric acid Low Temperature Thermal, is characterized in that: moisture absorption tower and drying tower are integrated.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520917546.3U CN205115045U (en) | 2015-11-17 | 2015-11-17 | Improve ore deposit or smelt device of sour low temperature heat recovery of flue gas sulfur production |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201520917546.3U CN205115045U (en) | 2015-11-17 | 2015-11-17 | Improve ore deposit or smelt device of sour low temperature heat recovery of flue gas sulfur production |
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| CN205115045U true CN205115045U (en) | 2016-03-30 |
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| CN201520917546.3U Withdrawn - After Issue CN205115045U (en) | 2015-11-17 | 2015-11-17 | Improve ore deposit or smelt device of sour low temperature heat recovery of flue gas sulfur production |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115350569A (en) * | 2022-08-31 | 2022-11-18 | 江西洪安化工有限公司 | Air purification system |
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2015
- 2015-11-17 CN CN201520917546.3U patent/CN205115045U/en not_active Withdrawn - After Issue
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115350569A (en) * | 2022-08-31 | 2022-11-18 | 江西洪安化工有限公司 | Air purification system |
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Granted publication date: 20160330 Effective date of abandoning: 20160817 |
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