CN115591373A - Method for adjusting concentration of sulfur dioxide in acid preparation by using smelting flue gas - Google Patents

Method for adjusting concentration of sulfur dioxide in acid preparation by using smelting flue gas Download PDF

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CN115591373A
CN115591373A CN202211317249.6A CN202211317249A CN115591373A CN 115591373 A CN115591373 A CN 115591373A CN 202211317249 A CN202211317249 A CN 202211317249A CN 115591373 A CN115591373 A CN 115591373A
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rich
rich liquid
flue gas
solution
concentration
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赵丹
黄咏峰
王博
丁腾
耿云峰
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Beijing Beida Pioneer Technology Co ltd
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Beijing Beida Pioneer Technology Co ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1412—Controlling the absorption process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1431—Pretreatment by other processes
    • B01D53/145—Pretreatment by separation of solid or liquid material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1481—Removing sulfur dioxide or sulfur trioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)

Abstract

The invention discloses a method for adjusting sulfur dioxide concentration when smelting flue gas is used for preparing acid. For SO 2 On the basis of the existing organic amine desulfurization process, a plurality of pregnant solution storage tanks and a pregnant solution balancing tank are arranged between an absorption tower and a regeneration tower, and meanwhile, the smelting flue gas with larger concentration fluctuation passes through the flue gas SO 2 On-line analyzer for monitoring SO in flue gas 2 Concentration and control of the opening of regulating valves at the inlets of a plurality of rich liquid storage tanks, and passing of product SO 2 Online flowmeter for detecting SO output by regeneration tower 2 The product gas is associated with and controls a plurality of rich liquid storage tank outlet regulating valves, SO that the SO with relatively stable output flow and concentration to the acid production device continuously is realized 2 And (5) producing gas. The method is used for measuring the flow and SO 2 The flue gas with large concentration change has good adaptability, and the SO in the flue gas is effectively reduced 2 The influence of large concentration fluctuation on the subsequent acid making process; simple process flowThe automatic control can be realized, the upgrading and the reconstruction are easy to be carried out on the operated device, the investment is less, and the operation cost is low.

Description

Method for adjusting concentration of sulfur dioxide in acid preparation by using smelting flue gas
Technical Field
The invention relates to the technical field of acid preparation by smelting flue gas, in particular to SO 2 The smelting flue gas with larger concentration fluctuation is used for the adjustment technology of the sulfur dioxide concentration during acid making.
Background
During the smelting process, a large amount of SO is usually generated 2 Flue gas with large gas volume and SO 2 Wide concentration fluctuation range and the like. For SO 2 The flue gas with higher concentration (more than 4.5 percent) can directly enter an acid making device after being cooled and purified; for SO 2 Flue gases with lower concentration and greater fluctuation (typically 0.01% -4.5%) due to lower SO 2 The concentration can not maintain the heat balance of the acid making system under the self-heating condition, SO the SO in the flue gas needs to be removed 2 The concentrated solution can enter an acid making device after being concentrated to a certain concentration (more than 4.5 percent). However, the difficulty of the technology is how to obtain SO in the smelting flue gas 2 Providing stable SO to acid making device under condition of large concentration fluctuation 2 A gas.
In the existing desulfurization technology, the organic amine desulfurization method is capable of removing SO in flue gas 2 The process for recycling has high desulfurization efficiency, recyclable absorbent and recycled SO 2 Can be used for preparing acid and the like, and is widely applied to the fields of nonferrous smelting, petroleum refining and the like. The process is suitable for low-concentration flue gas desulfurization, and has stronger applicability to higher-concentration flue gas. However, conventional organic amine desulfurization processes enrich SO 2 The gas yield is the SO in the flue gas entering the desulfurization system 2 The concentration of the SO in the flue gas entering the acid making system changes due to fluctuation of concentration 2 The concentration is unstable, and the problems that the heat balance of an acid making system is damaged and the concentration of the product acid does not reach the standard in serious cases can be caused.
In the Chinese patent publication CN105289215A flue gas circulating desulfurization method and system, a first-stage absorption section and a second-stage absorption section are arranged in an absorption tower, and a two-stage absorption mode is adopted to reduce the amount of rich liquid in a regeneration tower, thereby reducing the energy consumption of the system, realizing high-efficiency treatment and low-costConcentration SO 2 The purpose of the flue gas. However, the process only takes low concentrations of SO into account 2 Method for improving amine liquid loading capacity under conditions without considering flue gas SO 2 How to adjust the SO of the product under the condition of large concentration fluctuation 2 And (4) flow so as to enable the flow to be stable and output to a downstream section.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides a method for adjusting the concentration of sulfur dioxide in smelting flue gas for preparing acid, which is used for solving the problem that SO is contained in the smelting flue gas 2 When the concentration fluctuation is large, the product gas SO 2 The effect of flow fluctuations on the acid plant.
The invention provides a method for adjusting the concentration of sulfur dioxide in the process of using smelting flue gas to prepare acid, which adopts an organic amine desulfurizer to remove SO in the flue gas in an absorption tower 2 Absorbing the tail gas into the solution to form rich liquid, and discharging the purified tail gas through a chimney; the rich solution firstly enters rich solution storage tanks with different concentrations for storage, then enters a rich solution balance tank for realizing the stability of the solution concentration, and finally is conveyed into a regeneration tower through a rich solution feeding pump for realizing the SO 2 And (4) regenerating. The key of the technology is that the design of a plurality of rich liquid storage tanks, the directional transportation of rich liquids with different concentrations and the design of a rich liquid balance tank capable of realizing the stable concentration of the rich liquid are adopted in the process flow. Passing through flue gas SO on inlet pipeline of absorption tower 2 The online analyzer controls the opening of the inlet regulating valves of the different rich liquid storage tanks, so that the rich liquids corresponding to different flue gas concentrations enter the different rich liquid storage tanks, and the rich liquids with different concentrations are separately stored; product SO after passing through regeneration tower 2 The online flowmeter controls the opening of the outlet regulating valve of each concentration rich liquid storage tank, SO that the concentration of the rich liquid entering the rich liquid balance tank is stable, and finally the regeneration tower is used for conveying SO 2 The total amount is kept stable. The scheme is convenient to operate, can realize automatic control, is easy to transform the existing device, and can continuously output SO with relatively stable flow and concentration to the acid making device 2 And (5) producing gas.
The technical scheme provided by the invention is as follows:
adjustment of sulfur dioxide concentration when smelting flue gas is used for preparing acidThe method is based on the existing organic amine desulfurization process, and comprises arranging multiple rich liquid storage tanks and a rich liquid balance tank between an absorption tower and a regeneration tower, and passing through flue gas SO 2 On-line analyzer for monitoring SO in flue gas 2 Concentration and control of the opening of regulating valves at the inlets of a plurality of rich liquid storage tanks, and passing of product SO 2 Online flowmeter for detecting SO output by regeneration tower 2 The product gas is associated with and controls a plurality of rich solution storage tank outlet regulating valves, SO that the stable output of SO to the downstream of the organic amine desulfurization device is realized 2 The purpose of (1). The specific operation steps are as follows:
1) Containing SO from smelting furnaces 2 The flue gas enters an organic amine absorption tower after the steps of dust removal, temperature reduction, humidification and the like, and is in countercurrent contact with an organic amine desulfurizer solution in the absorption tower, SO 2 After being absorbed, rich liquid is formed at the bottom of the tower;
2) The rich liquid at the bottom of the absorption tower enters each rich liquid storage tank capable of containing rich liquid with different concentrations through a rich liquid delivery pump, the flow direction and the flow of the rich liquid are controlled by an inlet regulating valve of the rich liquid storage tank, and the opening degree of the regulating valve is controlled by the flue gas SO on an inlet pipeline of the absorption tower 2 Controlling an online analyzer;
3) The rich liquid with different concentrations is conveyed to a rich liquid balancing tank to be mixed, the mixed rich liquid is kept stable within a certain concentration range, the flow of the rich liquid with different concentrations entering the rich liquid balancing tank is controlled by an outlet regulating valve of a rich liquid storage tank, and the opening degree of the outlet regulating valve of the rich liquid storage tank is controlled by an outlet product SO of a regeneration tower 2 Controlling an online flowmeter;
4) The solution in the pregnant solution balancing tank is conveyed to the regeneration tower through a pregnant solution feeding pump to realize regeneration, and stable SO is output from the tower top 2 And (4) conveying the product gas to an acid making device, and returning the barren solution at the bottom of the tower to the absorption tower for recycling.
SO in the smelting flue gas 2 The concentration fluctuation range is 0.01-4.5%.
The organic amine desulfurizer in the step 1) comprises one or more of N, N-dimethylolpiperazine, N-dihydroxyethylpiperazine, N-dihydroxypropylpiperazine, N-dimethylolpiperazinone, N-dihydroxyethylpiperazine and N, N-dihydroxypropylpiperazinone.
The number of the rich liquid storage tanks in the step 2) is at least 2, and the number of the rich liquid balancing tanks is 1. Passing through flue gas SO on inlet pipeline of absorption tower 2 The on-line analyzer controls the opening of the inlet regulating valve of each rich liquid storage tank to enable rich liquids with different concentrations to enter the corresponding rich liquid storage tanks.
The outlet flow of the rich liquid feeding pump in the step 4) is received by the product SO 2 And (4) performing combined control on an online flowmeter and a regeneration tower liquid level meter. When the product SO 2 When the flow rate is smaller than the set value, the motor frequency of the rich liquid feeding pump is increased, and when the product SO is produced 2 And when the flow rate is larger than the set value, reducing the motor frequency of the rich liquid feeding pump.
In the step 4), a pipeline for conveying the solution in the rich solution balancing tank to the regeneration tower and a pipeline for returning the barren solution at the bottom of the regeneration tower to the absorption tower realize cross connection and barren and rich solution heat exchange through a barren and rich solution heat exchanger; and the lean solution at the bottom of the regeneration tower is cooled by a lean solution heat exchanger and a lean solution cooler through a lean solution delivery pump, enters a lean solution tank, and is delivered to the absorption tower through a lean solution delivery pump.
The barren solution delivery pump, the barren solution feed pump, the rich solution delivery pump and the rich solution feed pump related in the steps 1) to 4) adopt variable frequency motors, and the load adjustment range is 0-100%.
Compared with the prior art, the invention has the beneficial effects that:
1. the method disclosed by the invention can realize SO reaction on the product 2 The concentration and the flow are stably adjusted, SO that the SO in the flue gas can be effectively reduced 2 The influence of the large concentration fluctuation on the subsequent acid making process.
2. The invention has simple process flow, can realize automatic control, is easy to upgrade and reform on the operated device, and has less investment and low operation cost.
Drawings
FIG. 1 is a schematic process flow diagram of example 1 of the present invention;
FIG. 2 is a schematic diagram of the logic association of the main valves, pumps and meters related to the process flow of embodiment 1 of the present invention;
in the figure: 1. an absorption tower; 2. barren liquor feeding pump(ii) a 3. A lean liquor tank; 4. a lean liquid cooler; 5. a rich liquid delivery pump; 6. 1# rich liquid storage tank inlet adjusting valve; 7. 2# rich liquid storage tank inlet adjusting valve; 8. a 1# rich liquid storage tank; 9. a 2# rich liquid storage tank; 10. an outlet regulating valve of the 1# rich liquid storage tank; 11. an outlet regulating valve of the 2# rich liquid storage tank; 12. a pregnant solution balancing tank inlet pump; 13. a pregnant solution balancing tank; 14. a rich liquid feeding pump; 15. a lean-rich liquid heat exchanger; 16. a lean liquid delivery pump; 17. a regeneration tower; 18. a reboiler; 19. a regeneration tower condenser; 20. a gas-liquid separator; 21. absorption tower inlet flue gas SO 2 An on-line analyzer; 22. an absorption tower on-line liquid level meter; 23. product SO 2 An online flow meter; 24. a pregnant solution balance tank liquid level meter; 25. a regeneration tower liquid level meter.
Detailed Description
In order to explain the technical contents, the objects and effects achieved by the present invention in detail, the present invention will be further explained by embodiments with reference to the accompanying drawings. Obviously, the drawings in the description are only part of the embodiments of the present invention, and the specific implementation flows may be appropriately increased or decreased or adjusted according to different gas sources, technical conditions, and the like, so as to obtain other embodiments of the drawings.
The invention provides a technology for adjusting the concentration of sulfur dioxide in smelting flue gas with larger volatility, which has simple process flow and can adjust SO in the flue gas 2 The SO of the product gas is realized under the condition of great fluctuation of the concentration 2 Can effectively reduce SO in the flue gas 2 The influence of the large concentration fluctuation on the subsequent acid making process can realize automatic control, and the process has the advantages of low investment and low operation cost.
Example 1
SO (SO) 2 The technology for adjusting the concentration of sulfur dioxide when smelting flue gas with larger concentration fluctuation is used for preparing acid is shown in figure 1, comprises an absorption tower 1, a barren liquor feeding pump 2, a barren liquor tank 3, a barren liquor cooler 4, a rich liquor delivery pump 5, a 1# rich liquor storage tank inlet regulating valve 6, a 2# rich liquor storage tank inlet regulating valve 7 a # 1 rich liquid storage tank 8, a # 2 rich liquid storage tank 9, a # 1 rich liquid storage tank outlet regulating valve 10, a # 2 rich liquid storage tank outlet regulating valve 11, a rich liquid balance tank inlet pump 12, a rich liquid balance tank 13,A rich liquid feeding pump 14, a lean rich liquid heat exchanger 15, a lean liquid delivery pump 16, a regeneration tower 17, a reboiler 18, a regeneration tower condenser 19, a gas-liquid separator 20 and absorption tower inlet flue gas SO 2 On-line analyzer 21, absorption tower on-line liquid level meter 22 and product SO 2 An online flowmeter 23, a pregnant solution balance tank liquid level meter 24 and a regeneration tower liquid level meter 25; wherein, the 1# rich solution storage tank 8 and the 2# rich solution storage tank 9 are parallel, the inlets of the two tanks are connected with the rich solution outlet at the bottom of the absorption tower 1, and the outlet is connected with the inlet of the rich solution balance tank 13; referring to the figure 2,1# rich liquid storage tank inlet regulating valve 6 and 2# rich liquid storage tank inlet regulating valve 7 and the absorption tower inlet flue gas SO 2 The on-line analyzer 21 is electrically connected with and controlled by the opening degree; the outlet regulating valves 10 and 11 of the 1# and 2# rich liquid storage tanks and the product SO simultaneously 2 The online flowmeter 23 is electrically connected with and controlled by the opening degree; the rich liquid delivery pump 5 is arranged on an outlet pipeline at the bottom of the absorption tower 1, and delivers rich liquid into each rich liquid storage tank, the rich liquid delivery pump 5 is electrically connected with the absorption tower online liquid level meter 22, and the absorption tower online liquid level meter 22 controls the working frequency of the rich liquid delivery pump 5; a rich liquid balance tank inlet pump 12 is arranged on an inlet pipeline of the rich liquid balance tank 13, a rich liquid balance tank liquid level meter 24 is arranged in the rich liquid balance tank 13, the rich liquid balance tank inlet pump 12 is electrically connected with the rich liquid balance tank liquid level meter 24, and the working frequency of the rich liquid balance tank inlet pump 12 is regulated and controlled by the rich liquid balance tank liquid level meter 24; a rich liquid feeding pump 14 is arranged on an outlet pipeline of the rich liquid balancing tank 13, and the rich liquid feeding pump 14 and the product SO are simultaneously arranged 2 The on-line flowmeter 23 is electrically connected with the regeneration tower liquid level meter 25 and is connected with the product SO 2 The online flowmeter 23 and the regeneration tower liquid level meter 25 jointly control the working frequency of the rich liquor feeding pump 14; a barren liquor delivery pump 16, a barren liquor heat exchanger 15, a barren liquor cooler 4, a barren liquor tank 3 and a barren liquor feeding pump 2 are sequentially arranged on a barren liquor inlet passage from a barren liquor outlet at the bottom of the regeneration tower 17 to the absorption tower 1, wherein the barren liquor heat exchanger 15 is simultaneously connected with a pipeline for sending the solution in the rich liquor balancing tank 13 to the regeneration tower 17, so that the barren liquor from the regeneration tower 17 and the rich liquor sent to the regeneration tower 17 realize heat exchange of the barren liquor and the rich liquor; the barren solution after heat exchange with the rich solution is further cooled by a barren solution cooler 4 and then enters a barren solution tank 3, and then is conveyed to the absorption tower by a barren solution feeding pump 21; SO output from the regeneration tower 17 2 The product gas is cooled by a regeneration tower condenser 19, liquid water in the gas is separated by a gas-liquid separator 20, and SO containing only gas phase saturated water is output 2 Producing gas; the reboiler 18 heats the lean liquid in the regeneration tower 17.
The tail gas treated by the embodiment is the single-furnace smelting smoke of the secondary lead oxygen-enriched side-blown furnace, the operation system of the furnace type smelting process is 4 hours and one furnace batch, wherein the first 3 hours are an oxidation period, and the last 1 hour is a reduction period and a slag discharging period. The composition, the component content and the flue gas amount of smelting flue gas in different periods are different, and the flue gas conditions are shown in the following table 1.
TABLE 1
Figure BDA0003909902650000051
SO of the system acid device in the process of making acid from smelting flue gas of the secondary lead oxygen-enriched side-blown converter 2 The concentration adjusting method specifically comprises the following steps:
1) The smelting smoke of the oxygen-enriched side-blown converter enters the absorption tower 1 after being cooled, dedusted and acid mist removed, and SO in the smoke in the absorption tower 1 2 SO absorbed by organic amine in oxidation period 2 The content reaches 3.21%, and the formed rich solution is concentrated rich solution. Absorption tower inlet flue gas SO 2 The online analyzer 21 controls the opening of the inlet regulating valve 6 of the 1# rich liquid storage tank to be opened to 70% -75%, controls the opening of the inlet regulating valve 7 of the 2# rich liquid storage tank to be opened to 25% -30%, and enables the high-concentration rich liquid to enter the 1# rich liquid storage tank 8 and the 2# rich liquid storage tank 9 simultaneously. At the same time, the product SO 2 The online flowmeter 23 controls the opening of the outlet regulating valve 10 of the 1# rich liquid storage tank to 100%, and controls the opening of the outlet regulating valve 11 of the 2# rich liquid storage tank to 0. The rich solution is conveyed into a rich solution balance groove 13 through a rich solution balance groove inlet pump 12, then is heated to 90-100 ℃ through a rich solution feeding pump 14 and a lean and rich solution heat exchanger 15, and then enters a regeneration tower 17 for desorption, and the product SO 2 Passes through a regeneration tower condenser 19 and a gas-liquid separator 20 and then enters a downstream acid making process. The barren solution obtained at the bottom of the regeneration tower 17 enters the barren solution cooler 4 after passing through a barren solution delivery pump 16 and a barren and rich solution heat exchanger 15,further cooling to 30-50 ℃, then entering a barren liquor tank 3, and returning to the absorption tower 1 through a barren liquor feeding pump 2 for recycling. After the oxidation period lasts 3 hours, the smelting furnace enters a reduction period, and the 2# rich solution storage tank 9 stores a solution containing about 1145Nm 3 A high-concentration rich solution of sulfur dioxide.
2) SO in flue gas in reduction period 2 The concentration is only 11% of the oxidation period, the smoke amount is 84% of the oxidation period, and the formed rich solution is the dilute rich solution. Absorption tower inlet flue gas SO 2 The online analyzer 21 controls the opening of the inlet regulating valve 6 of the 1# rich liquid storage tank to 100%, controls the opening of the inlet regulating valve 7 of the 2# rich liquid storage tank to 0, and controls the dilute rich liquid to enter the 1# rich liquid storage tank 9. Product SO 2 The opening degree of the outlet regulating valve 10 of the 1# rich solution storage tank is controlled to be 100% by the online flowmeter 23, the opening degree of the outlet regulating valve 11 of the 2# rich solution storage tank is controlled to be 80% -90%, the two rich solutions are conveyed into the rich solution balancing tank 13 by the rich solution balancing tank inlet pump 12 to be mixed, and the mixed rich solution is heated by the rich solution feeding pump 14 and the lean rich solution heat exchanger 15 and then enters the regeneration tower 17 for regeneration. Product SO 2 Passes through a regeneration tower condenser 19 and a gas-liquid separator 20 and then enters a downstream acid making process. The barren solution obtained at the bottom of the regeneration tower 17 enters a barren solution cooler 4 after passing through a barren solution delivery pump 16 and a barren and rich solution heat exchanger 15, is further cooled to 30-50 ℃, then enters a barren solution tank 3, and returns to the absorption tower 1 through a barren solution feed pump 2 for recycling. After the reduction period lasts 0.67 hours, the smelting furnace enters a slag-off period, and the rich liquid in the 2# rich liquid storage tank is still stored with about 410Nm 3 SO of (A) 2 。
3) SO in flue gas in slag discharge period 2 The concentration is only 2.5% of the oxidation period, the smoke amount is 72% of the oxidation period, and the formed rich solution is a dilute rich solution. Absorption tower inlet flue gas SO 2 The online analyzer 21 controls the opening of the inlet regulating valve 6 of the 1# rich solution storage tank to be 100%, controls the opening of the inlet regulating valve 7 of the 2# rich solution storage tank to be 0, and controls the dilute rich solution to enter the 1# rich solution storage tank 9. Product SO 2 The opening degree of the outlet regulating valve 10 of the 1# rich liquid storage tank is controlled to be 75-90% by the online flowmeter 23, the opening degree of the outlet regulating valve 11 of the 2# rich liquid storage tank is controlled to be 90-100%, the two rich liquids are conveyed into the rich liquid balancing tank 13 by the inlet pump 12 of the rich liquid balancing tank to be mixed, and the mixed rich liquid is conveyed into the rich liquid balancing tank 13 by the inlet pump 12 of the rich liquid balancing tank to be mixedThe rich solution feed pump 14 and the lean-rich solution heat exchanger 15 are heated and then enter the regeneration tower 17 for regeneration. The smelting furnace enters an oxidation period after the slag discharging period lasts for 0.33 hour.
The above steps are repeated in a cycle.
The following Table 2 shows the SO products obtained with and without the process 2 And (4) comparing the flow rates.
TABLE 2
Figure BDA0003909902650000061
Obviously, the stable product SO can be obtained by adopting the process 2 And (4) the flow rate.
In conclusion, the technology for adjusting the concentration of sulfur dioxide when smelting flue gas with high volatility is used for preparing acid provided by the invention has the following advantages:
1) Convection and SO 2 The flue gas with large concentration change has good adaptability, and can be applied to the fields of non-ferrous smelting flue gas, circular collecting flue gas, sintering flue gas, secondary lead smelting furnace flue gas and the like.
2) Can realize the SO of the product gas 2 The concentration and the flow are stably adjusted, and the SO in the flue gas is effectively reduced 2 The influence of the large concentration fluctuation on the subsequent acid making process.
3) The process flow is simple, automatic control can be realized, upgrading and reconstruction can be easily carried out on the operated device, the investment is low, and the operation cost is low.
It is noted that the disclosed embodiments are intended to facilitate a further understanding of the invention. The above description is only a partial embodiment of the present invention, but those skilled in the art will understand that: based on the basic principle of the present invention, suitable modifications and adjustments can be made, and these should also be considered as the protection scope of the present invention. Therefore, the invention should not be limited by the disclosure of the embodiments, but should be defined by the scope of the appended claims.

Claims (10)

1. Second time when smelting flue gas is used for preparing acidThe method for regulating sulfur oxide concentration is characterized by that on the basis of organic amine desulfurization process, between absorption tower and regeneration tower several rich liquor storage tanks and a rich liquor equilibrium tank are set, and the flue gas SO is passed through 2 On-line analyzer for monitoring SO in flue gas 2 Concentration by product SO 2 Online flowmeter for detecting SO output by regeneration tower 2 Producing gas; firstly, SO in the flue gas is removed by adopting an organic amine desulfurizer through an absorption tower 2 Absorbing the solution to form a pregnant solution; then passing through the flue gas SO 2 The online analyzer controls the opening degree of the inlet regulating valves of the plurality of rich liquid storage tanks to convey rich liquids with different concentrations to each rich liquid storage tank for storage; then passing through the product SO 2 The online flowmeter performs correlation control on the outlet regulating valves of the rich liquid storage tanks, so that the rich liquid enters the rich liquid balance tank to realize the stability of the solution concentration; finally, conveying the rich liquor in the rich liquor balancing tank into a regeneration tower to realize SO 2 Regeneration, continuous output of SO with relatively stable flow and concentration to acid production device 2 And (5) producing gas.
2. A method of conditioning as claimed in claim 1, characterized in that the method comprises the following steps:
1) The smelting flue gas enters an absorption tower after being dedusted, cooled and humidified, and is in countercurrent contact with an organic amine desulfurizer solution in the absorption tower, SO in the flue gas 2 After being absorbed, rich liquid is formed at the bottom of the tower;
2) The rich liquid at the bottom of the absorption tower enters each rich liquid storage tank capable of containing rich liquid with different concentrations through a rich liquid delivery pump, the flow direction and the flow rate of the rich liquid are controlled by an inlet regulating valve of the rich liquid storage tank, and the opening degree of the inlet regulating valve of the rich liquid storage tank is controlled by the flue gas SO 2 Controlling an online analyzer;
3) The rich liquid with different concentrations is conveyed to the rich liquid balancing tank to be mixed, the flow of the rich liquid with different concentrations entering the rich liquid balancing tank is controlled by the outlet regulating valve of the rich liquid storage tank, and the opening degree of the outlet regulating valve of the rich liquid storage tank is controlled by the product SO 2 The online flowmeter is used for controlling to ensure that the rich liquor mixed in the rich liquor balancing tank is kept stable within a certain concentration range;
4) Solution in the pregnant solution balancing tank is led toThe rich liquor is fed to the regeneration tower by a liquor feeding pump to realize regeneration, and stable SO is output from the tower top 2 And (4) conveying the product gas to an acid making device, and returning the barren solution at the bottom of the tower to the absorption tower for recycling.
3. The conditioning method according to claim 1 or 2, characterized in that SO in the smelting flue gas 2 The concentration fluctuation range is 0.01-4.5%.
4. The conditioning method of claim 2, wherein the organic amine desulfurization agent in step 1) is selected from one or more of N, N-dimethylol piperazine, N-dihydroxyethyl piperazine, N-dihydroxypropyl piperazine, N-dihydroxymethyl piperazinone, N-dihydroxyethyl piperazinone, N-dihydroxypropyl piperazinone.
5. The conditioning method according to claim 2, characterized in that the number of the rich liquid storage tanks in step 2) is at least 2, and the flue gas SO is 2 The on-line analyzer is arranged on an inlet pipeline of the absorption tower.
6. The method of claim 2, wherein the outlet flow rate of the rich liquid feed pump in step 4) is controlled by product SO 2 On-line flow meter and regeneration tower liquid level meter combined control, when product SO 2 When the flow rate is smaller than the set value, the motor frequency of the rich liquid feeding pump is increased, and when the product SO is produced 2 And when the flow rate is larger than the set value, reducing the motor frequency of the rich liquid feeding pump.
7. The process of claim 2, wherein the line for feeding the solution from the pregnant solution equalization tank to the regenerator and the line for returning the lean solution from the bottom of the regenerator to the absorber are cross-connected and heat exchanged with the lean and rich solution by a lean and rich solution heat exchanger.
8. The conditioning method of claim 7, wherein the lean solution at the bottom of the regeneration tower in the step 4) is cooled by a lean solution delivery pump through a lean solution heat exchanger and a lean solution cooler and then enters a lean solution tank, and is delivered to the absorption tower through a lean solution delivery pump.
9. The adjusting method according to claim 8, characterized in that the lean liquid delivery pump, the lean liquid feed pump, the rich liquid delivery pump and the rich liquid feed pump all adopt variable frequency motors, and the load adjusting range is 0-100%.
10. The process of claim 2, wherein step 4) is carried out by feeding SO from the regenerator 2 Cooling the product gas by a condenser of a regeneration tower, separating liquid water in the gas by a gas-liquid separator, and outputting SO only containing gas phase saturated water 2 And sending the product gas to an acid making device.
CN202211317249.6A 2022-10-26 2022-10-26 Method for adjusting concentration of sulfur dioxide in acid preparation by using smelting flue gas Pending CN115591373A (en)

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