KR20120000772A - Method for refining sinter flue gas - Google Patents

Method for refining sinter flue gas Download PDF

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Publication number
KR20120000772A
KR20120000772A KR1020100061228A KR20100061228A KR20120000772A KR 20120000772 A KR20120000772 A KR 20120000772A KR 1020100061228 A KR1020100061228 A KR 1020100061228A KR 20100061228 A KR20100061228 A KR 20100061228A KR 20120000772 A KR20120000772 A KR 20120000772A
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KR
South Korea
Prior art keywords
flue gas
bed
sintered
ammonia
exhaust gas
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Application number
KR1020100061228A
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Korean (ko)
Inventor
류성윤
최종철
Original Assignee
현대제철 주식회사
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Priority to KR1020100061228A priority Critical patent/KR20120000772A/en
Publication of KR20120000772A publication Critical patent/KR20120000772A/en

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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
    • B01D53/02—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 adsorption, e.g. preparative gas chromatography
    • B01D53/06—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 adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B01D53/08—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 adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds according to the "moving bed" method
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/54—Nitrogen compounds
    • B01D53/56—Nitrogen oxides
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8637—Simultaneously removing sulfur oxides and nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • 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
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/404—Nitrogen oxides other than dinitrogen oxide
    • 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
    • B01D2258/025—Other waste gases from metallurgy plants

Abstract

PURPOSE: A method for refining sintered flue gas is provided to constantly maintain the eliminating efficiency of nitrogen oxides and to stably manage a facility by adjusting the discharging speed of activated carbon. CONSTITUTION: A method for refining sintered flue gas includes the following: Sintering exhaust gas passes through a sulfur oxides bed(S100). The first ammonia injecting amount required for reacting ammonia and nitrogen oxide contained in the sintering exhaust gas is calculated(S200). The concentration of sulfur dioxide in the sintering exhaust gas through the sulfur oxides bed is measured, a second ammonia injecting amount required for reacting ammonia and sulfur dioxide contained in the sintering gas through the sulfur oxides bed is calculated(S300). Ammonia is sprayed to sintering exhaust gas(S400). The sintering exhaust gas passes through a nitrogen oxides bed(S500).

Description

Method for refining sinter flue gas

It relates to a sintered flue gas purification method that can improve the NOx removal efficiency in the two-stage activated carbon adsorption column of the present invention.

In general, the sintering process is manufactured by using coke, bituminous coal, anthracite coal in a constant proportion as a raw material of fine iron ore, limestone, serpentine, silica sand and the like as fuel.

In the sintering process, sulfur (S) and nitrogen (N) components contained in iron ore react with oxygen in the air drawn into the sintering machine to form sulfur oxides (SOx) and nitrates (NOx).

If it is discharged to the atmosphere as it may cause environmental pollution, the activated carbon having the property of adsorbing impurities to remove the SOx and NOx through the further desulfurization and denitrification process to discharge the exhaust gas into the atmosphere.

An object of the present invention is to provide a sintered flue gas purification method that can improve the NOx removal efficiency in the two-stage activated carbon adsorption column.

The present invention comprises the steps of passing the sintered exhaust gas through the SOx bed; Calculating a first injection amount of ammonia required for reacting with NO contained in the sintered flue gas; Calculating a second injection amount of ammonia required to react with SO 2 contained in the sintered flue gas by measuring the concentration of SO 2 in the sintered flue gas passed through the SOx bed; Injecting an amount of ammonia corresponding to the first injection amount and the second injection amount into the sintered exhaust gas; And passing the sintered exhaust gas through the NOx bed.

In addition, the calculating of the first injection amount may calculate the amount of ammonia required to react with NO contained in the sintered flue gas by measuring the NO concentration of the sintered flue gas passing through the SOx bed.

In the calculating of the first injection amount, ammonia required for reacting with NO contained in the sintered flue gas may be calculated in an equivalent ratio of 1: 1.

In addition, the calculating of the second injection amount may calculate the ammonia required to react with SO 2 contained in the sintered flue gas in a 1: 2 equivalent ratio.

In addition, when there are a plurality of activated carbon adsorption towers and the same sintered flue gas is blown into each of the activated carbon adsorption towers, the concentration value of SO 2 measured by one activated carbon adsorption tower may be used when calculating the second ammonia injection amount of another activated carbon adsorption tower.

According to the sintered flue gas purification method of the present invention, the amount of ammonia can be controlled according to the SO 2 adsorption capacity in the SOx bed, and the activated carbon discharge rate can be controlled to stably operate the equipment, thereby optimizing the use of ammonia. .

In addition, since the SO 2 adsorption capacity changes in the SOx bed over time, it can be detected quickly to reduce operating costs and maintain the NOx removal efficiency consistently.

1 is a cross-sectional view of the sintered exhaust gas purification apparatus used in the sintered exhaust gas purification method according to an embodiment of the present invention.
Figure 2 is a flow chart showing a sintered flue gas purification method according to an embodiment of the present invention.

The present invention improves the method of injecting ammonia in the sintered flue gas purification apparatus using activated carbon for efficient purification of the sintered flue gas discharged during sintering during the steelmaking process to the preferred embodiment of the present invention see Figures 1 and 2 This will be described in detail.

1 is a cross-sectional view of a sintered exhaust gas purification apparatus used in the sintered exhaust gas purification method according to an embodiment of the present invention, Figure 2 is a flow chart showing a sintered exhaust gas purification method according to an embodiment of the present invention.

Referring to FIG. 1, the chamber 10, the ammonia chamber 12, the sintered exhaust gas inlet 13, the sintered exhaust gas outlet 14, the SOx bed 21, the NOx bed 22, the ammonia injector 30, SO 2 The sensor 41 and the NO sensor 42 are shown.

As shown in FIG. 1, the activated carbon adsorption tower used in the present invention has a sintered exhaust gas inlet 13 formed at a lower portion thereof, and a sintered exhaust gas outlet 14 formed at an upper portion thereof. The bed 21 and the NOx bed 22 are interposed. There is an ammonia chamber 12 which sprays ammonia between two stages of activated carbon beds.

The sintered exhaust gas blown into the chamber 10 through the lower sintered exhaust gas inlet 13 passes through the SOx bed 21 and the NOx bed 22 and then exits to the sintered exhaust gas outlet 14.

In SOx bed 21, SO 2 is removed by adsorbing SO 2 on the surface of activated carbon, and in NOx bed 22, NO in the sintered flue gas is removed by reacting ammonia and NO with activated carbon as a catalyst to convert water and nitrogen. do.

The removal reaction of the SOx bed 21 and the NOx bed 22 is as follows.

SOx bed: SO2 + H 2 O + 1 / 2O 2 → H 2 SO 4 (removed by adsorption in the form of sulfuric acid). Formula (1)

NOx bed: 4NO + 4NH 3 + O 2- > 4N 2 + 6H 2 O (reduced removal on activated carbon catalyst). Equation (2)

That is, after the sintered exhaust gas passes through the SOx bed 21 and before passing through the NOx bed 22, the ammonia is injected into the sintered exhaust gas in the ammonia chamber 12 located on the side of the chamber 10 so that the ammonia is NOx like the sintered exhaust gas. Flow into bed (22).

At this time, the injected ammonia must be maintained at an equivalent ratio of 1: 1 with NO contained in the sintered flue gas as shown in Equation (2) to efficiently remove NO. That is, the amount of ammonia (first injection amount) sufficient to react with NO contained in the sintered flue gas blown into the chamber 10 is calculated and injected.

However, when the SOx bed 21 is adsorbed onto the surface of activated carbon over time as SO 2 is deteriorated, the SOx bed 21 may not be completely removed from the SOx bed 21 and moved to the ammonia chamber 12.

At this time, SO 2 reacts with ammonia to form ammonium sulfate. As ammonia to be used for NO removal is consumed, NO removal efficiency decreases, and SO 2 that does not react with ammonia is activated on the activated carbon of the NOx bed 22. The likelihood of occurrence of a problem of deterioration of the efficiency of the NOx bed 22 due to adsorption increases.

Accordingly, the present invention provides a sintered flue gas purification process that can effectively remove SOx and NOx by additionally supplying a sufficient amount of ammonia to react with SOx by sensing the amount of SOx that has not been removed.

First, the sintered exhaust gas is passed through the SOx bed 21 (S100). When the sintered exhaust gas is introduced into the sintered exhaust gas inlet 13 of the chamber 10, the sintered exhaust gas passes through the SOx bed 21 while moving upward. Passing through the SOx bed 21, SO 2 is adsorbed on the surface of the activated carbon to remove SO 2 .

The first injection amount of ammonia required to react with the NO contained in the sintered flue gas is calculated (S200). In order to calculate this, it is necessary to know the amount of NO contained in the sintered flue gas. Since the amount of NO contained in the sintered flue gas blown into the chamber 10 does not change significantly, the amount of ammonia corresponding to the value is first injected. It can be calculated as In the chemical formula, maintaining an equivalent ratio of 1: 1 may remove all NO, but a sufficient amount may be injected therein.

There is no data on the amount of NO contained in the sintered flue gas blown into the chamber 10, or the NO concentration of the sintered flue gas passed through the SOx bed 21 is measured and calculated on the basis of this in order to more accurately calculate the first injection amount. One injection amount can be calculated. As shown in FIG. 1, the NO sensor 42 may be installed on the top of the SOx bed 21 to measure the NO concentration.

In addition, by measuring the SO 2 concentration of the sintered flue gas passed through the SOx bed 21 to calculate a second injection amount of ammonia required to react with SO 2 contained in the sintered flue gas (S300).

As described above, when the efficiency of the SOx bed 21 is lowered, SO 2 may not be removed, and the SOx bed 21 may be exited. SO 2 for measuring these SO 2 concentration The sensor 41 is installed on the SOx bed 21 to calculate the amount of SO 2 , and based on this, the second injection amount of ammonia required to react with SO 2 is calculated. The reaction formula of SO 2 and ammonia is as follows.

2SO 2 + 4 NH 3 + 2H 2 O + O 2 → 2 (NH 4 ) 2 SO 4 … Equation (3)

Since SO 2 reacts with ammonia at an equivalent ratio of 1: 2, the second injection amount can be calculated to be twice the amount of SO 2 .

Next, ammonia in an amount corresponding to the first injection amount and the second injection amount is injected into the sintered exhaust gas (S400). As time passes, the amount of SO 2 that is not completely removed from the SOx bed 21 increases, so that the second injection amount increases. The ammonia of the sum of the first injection amount and the second injection amount is injected from the ammonia chamber 12 through the ammonia injector 30 and mixed with the sintered flue gas.

Sintered flue gas mixed with sufficient ammonia is passed through the NOx bed to remove NO and excess SO2 (S500). The sintered exhaust gas from which NO and SO 2 are removed exits the chamber 10 through the sintered exhaust gas outlet 14.

On the other hand, the amount of sintered exhaust gas can be used to operate a plurality of activated carbon adsorption tower at the same time, when the same sintered exhaust gas is injected into each activated carbon adsorption tower, the concentration value of SO 2 measured in one activated carbon adsorption tower is ammonia 2 Can be used to calculate the injection volume. Since each activated carbon adsorption column is under similar conditions, the amount of SO 2 that exits the SOx bed 21 is similar.

It will be apparent to those skilled in the art that various modifications and variations can be made in the present invention without departing from the spirit or scope of the invention as defined in the appended claims. It will be understood that the invention may be varied and varied without departing from the scope of the invention.

10 chamber 12 ammonia chamber
13: Sintered flue gas inlet 14: Sintered flue gas outlet
21: SOx Bed 22: NOx Bed
30: Ammonia Injector
41: SO 2 sensor 42: NO sensor

Claims (5)

Passing sintered flue gas through the SOx bed;
Calculating a first injection amount of ammonia required for reacting with NO contained in the sintered flue gas;
Calculating a second injection amount of ammonia required to react with SO 2 contained in the sintered flue gas by measuring the concentration of SO 2 in the sintered flue gas passed through the SOx bed;
Injecting an amount of ammonia corresponding to the first injection amount and the second injection amount into the sintered exhaust gas; And
Sintered exhaust gas purification method comprising the step of passing the sintered exhaust gas through the NOx bed. The method of claim 1,
The calculating of the first injection amount is
And measuring the NO concentration of the sintered flue gas passing through the SOx bed to calculate the amount of ammonia required to react with the NO contained in the sintered flue gas. The method of claim 1,
Calculating the first injection amount is
A method for purifying sintered flue gas, characterized by calculating the ammonia required to react with NO contained in the sintered flue gas in an equivalent ratio of 1: 1. The method of claim 1,
Calculating the second injection amount is
A method for purifying sintered flue gas, characterized by calculating ammonia required to react with SO 2 contained in the sintered flue gas in a 1: 2 equivalent ratio. The method of claim 1,
There are a plurality of activated carbon adsorption towers
When the same sintered flue gas is blown into each activated carbon adsorption column,
A method for purifying sintered flue gas, characterized in that the concentration value of SO 2 measured in one activated carbon adsorption column is used to calculate the second ammonia injection amount of another activated carbon adsorption column.
KR1020100061228A 2010-06-28 2010-06-28 Method for refining sinter flue gas KR20120000772A (en)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20180116206A (en) * 2016-08-08 2018-10-24 종예 창티엔 인터내셔날 엔지니어링 컴퍼니 리미티드 METHOD AND APPARATUS FOR CONTROLLING AMPLITUDE OF AMMONIA IN ACTIVATED CARBON DEFENSE AND NOx
CN110585909A (en) * 2019-09-18 2019-12-20 大连理工大学 Process for simultaneously desulfurizing and denitrifying and method for preparing compound fertilizer from product
KR20200085060A (en) 2019-01-04 2020-07-14 이상무 Water supply device for raising insects

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20180116206A (en) * 2016-08-08 2018-10-24 종예 창티엔 인터내셔날 엔지니어링 컴퍼니 리미티드 METHOD AND APPARATUS FOR CONTROLLING AMPLITUDE OF AMMONIA IN ACTIVATED CARBON DEFENSE AND NOx
KR20200085060A (en) 2019-01-04 2020-07-14 이상무 Water supply device for raising insects
CN110585909A (en) * 2019-09-18 2019-12-20 大连理工大学 Process for simultaneously desulfurizing and denitrifying and method for preparing compound fertilizer from product

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