CN112593034A - Dry-method cooperative deacidification system and method for blast furnace clean gas - Google Patents
Dry-method cooperative deacidification system and method for blast furnace clean gas Download PDFInfo
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Abstract
A dry method synergic deacidification system and method for blast furnace clean gas. The invention discloses a dry deacidification system device and a dry deacidification method for simultaneously removing components containing chlorine and sulfuric acid from blast furnace gas, which improve the anticorrosion conditions of equipment such as a blast furnace gas pipeline and TRT blades and fully utilize the residual heat of the residual pressure of the gas through the cooperation of multiple systems.
Description
Technical Field
The invention relates to a system device and a process for removing acidic components including sulfur and chlorine in blast furnace gas by a dry method and regenerating a deacidification agent, belonging to the technical field of blast furnace gas purification.
Background
The dry dedusting process and the residual pressure waste heat power generation technology of the blast furnace top gas are advanced technologies for promoting energy conservation, emission reduction and circular economy development of the steel industry in China. The blast furnace top gas dry dedusting technology gradually replaces the traditional wet dedusting with the advantages of water saving, high dedusting efficiency, full utilization of sensible heat of gas, high residual pressure power generation amount of gas and the like, and becomes the first choice of the blast furnace gas purification technology. Practice proves that compared with the traditional wet dust removal, the dry dust removal technology can save 35% of investment, 7-9 t of circulating water, 60% -70% of electricity, 30% of newly added power generation and greatly reduce the discharge of sewage and sludge. However, the blast furnace gas after dry dedusting can cause serious corrosion of gas pipelines, blades of a residual pressure turbine power generation device (TRT for short) and other accessory equipment, thereby causing the vibration of the TRT blades, gas leakage, the reduction of the heat storage efficiency of checker bricks of the hot blast stove and the like, seriously influencing the normal operation of the residual pressure waste heat recovery device and the normal smelting of the blast furnace and bringing about great potential safety production hazards.
The research on the blast furnace gas dry dedusting process and the relevant corrosion state shows that: the corrosion is caused by a large amount of components such as chlorine, sulfur and the like carried in the coal gas after dry dedusting and an acidic liquid environment. A large amount of acid components such as chlorine, sulfur and the like in the blast furnace raw gas, which are derived from raw materials, cannot be brought away by water as in wet dust removal treatment, but remain in the clean gas, and are synthesized into an acid solution with saturated water which is separated out from the gas due to temperature drop and the like caused by the raw materials or temperature adjustment by water spraying, so that metal parts in contact with the acid solution are corroded.
Aiming at the corrosion mechanism of blast furnace gas in dry dedusting, the corrosion prevention is divided into passive and active. The passive corrosion prevention is realized by adopting corrosion-resistant materials, corrosion-resistant coatings and the like to strengthen the corrosion resistance of metal parts. This can only partially and to some extent alleviate the effects of corrosion and does not solve the problem fundamentally. Active anticorrosion, such as changing raw fuel components, wet spraying acid washing, dry deacidification and the like, aims to reduce the content of acid components in the coal gas. The method is an effective method for controlling the acid components in raw fuels such as iron ore, coal powder and the like from the source, but the measure is limited by conditions such as ore grade, raw material supply and the like, and the selectable scope is not large. The reduction of the introduction of acidic components in each smelting process has obvious corrosion treatment effect, for example, chlorine-containing auxiliaries are not used in a sintering process, the use of wastewater in the processes of desulfurization, coking and the like in each process is controlled, the acidic components in coal gas can be effectively reduced, but the treatment load and the environmental protection investment of the production wastewater which cannot be recycled are greatly increased. The wet alkali liquor spraying washing can also effectively reduce the acid components in the coal gas, but the alkali liquor can also cause corrosion, scaling, blockage and the like, thereby increasing sewage treatment and environmental pollution, and offsetting the advantages of water saving, utilization of sensible heat of the coal gas and the like of dry dedusting to a great extent.
Compared with wet acid washing, dry deacidification is carried out by utilizing a solid alkaline deacidification agent to react with acid components in blast furnace gas for removal. The dry deacidification method inherits the advantages of the dry dedusting process and gradually becomes the exploration trend of the blast furnace gas deep purification technology. Therefore, the invention provides a device and a process for a dry-method cooperative deacidification system for a blast furnace gas dry-method deacidification in iron and steel enterprises, and has great significance.
Therefore, those skilled in the art are devoted to develop a system device and a process for dry-process cooperative deacidification in steel enterprises.
Disclosure of Invention
In view of the above defects in the prior art, the technical problem to be solved by the present invention is to provide a dry deacidification system and a dry deacidification method for removing chlorine and sulfuric acid components from blast furnace gas, so as to open up a new way for corrosion prevention of blast furnace gas pipelines, TRT blades and other equipment and fully utilize residual heat of gas excess pressure.
In order to achieve the above object, the present invention provides in a first aspect a blast furnace clean gas dry method cooperative deacidification system, comprising a dedusted blast furnace clean gas supply subsystem, a tower dechlorination subsystem, a tower organic sulfur hydrolysis subsystem, and a tower secondary desulfurization subsystem; wherein:
the blast furnace clean gas supply subsystem is configured to firstly send clean gas obtained after raw gas generated at the top of the blast furnace passes through the gravity dust collector and the bag-type dust collector into the tower-type dechlorination subsystem through a supply pipeline;
the tower type dechlorination subsystem is configured to be provided with a dechlorination reaction bed in the middle, a dechlorination agent is arranged in the dechlorination reaction bed, a dechlorination agent replacing device is arranged in the dechlorination reaction bed, a first temperature adjusting device and a circulating water device are further arranged in the dechlorination reaction bed, and the tower type dechlorination subsystem further comprises a first detachable tower bottom arranged at the bottom of the tower;
the blast furnace clean gas feed subsystem is configured to feed clean gas passing through the tower dechlorination subsystem into the tower hydrolysis organosulfur subsystem;
the tower-type hydrolysis organic sulfur subsystem is configured to be provided with an organic sulfur catalytic reaction bed in the middle of the system, an organic sulfur catalyst is arranged in the organic sulfur catalytic reaction bed, an organic sulfur catalyst replacing device is arranged in the organic sulfur catalytic reaction bed, a second temperature regulating device is further arranged in the organic sulfur catalytic reaction bed, and the tower-type hydrolysis organic sulfur subsystem further comprises a first N arranged at the top of the tower2Gas inlet and first N arranged at bottom of tower2The tower type hydrolysis organic sulfur subsystem further comprises a second detachable tower bottom arranged at the bottom of the tower;
the blast furnace clean gas supply subsystem is configured to feed clean gas passing through the tower type hydrolysis organosulfur subsystem into the tower type secondary desulfurization subsystem;
the tower type secondary desulfurization subsystem is characterized in that a desulfurization reaction bed is arranged at the middle part of the tower type secondary desulfurization subsystem, a desulfurizer is arranged in the desulfurization reaction bed, a desulfurizer replacing device is arranged in the desulfurization reaction bed, a third temperature regulating device is further arranged in the desulfurization reaction bed, and the tower type secondary desulfurization subsystem further comprises a second N arranged at the top of the tower2Gas inlet and O2Gas inlet and N arranged at the bottom of the tower2Gas and O2The tower type secondary desulfurization subsystem also comprises a third detachable tower bottom arranged at the bottom of the tower;
the blast furnace clean gas supply subsystem is configured to send the clean gas passing through the tower type secondary desulfurization subsystem out of the blast furnace clean gas dry-method cooperative deacidification system.
Further, the dechlorinating agent is metal ions and Na2CO3The prepared dechlorinating agent.
Further, the organic sulfur catalyst is metal ion, KOH and Na2CO3The catalyst is prepared.
Further, the desulfurizer is made of metal oxide.
The invention provides a blast furnace clean gas dry method synergic deacidification method in a second aspect, which comprises the following steps:
(1) providing a dry-method cooperative deacidification system for blast furnace clean gas, which comprises a dedusted blast furnace clean gas supply subsystem, a tower-type dechlorination subsystem, a tower-type organic sulfur hydrolysis subsystem and a tower-type secondary desulfurization subsystem; wherein:
the blast furnace clean gas supply subsystem is configured to firstly send clean gas obtained after raw gas generated at the top of the blast furnace passes through the gravity dust collector and the bag-type dust collector into the tower-type dechlorination subsystem through a supply pipeline;
the tower type dechlorination subsystem is configured to be provided with a dechlorination reaction bed in the middle, a dechlorination agent is arranged in the dechlorination reaction bed, a dechlorination agent replacing device is arranged in the dechlorination reaction bed, a first temperature adjusting device and a circulating water device are further arranged in the dechlorination reaction bed, and the tower type dechlorination subsystem further comprises a first detachable tower bottom arranged at the bottom of the tower;
the blast furnace clean gas feed subsystem is configured to feed clean gas passing through the tower dechlorination subsystem into the tower hydrolysis organosulfur subsystem;
the tower-type hydrolysis organic sulfur subsystem is configured to be provided with an organic sulfur catalytic reaction bed in the middle of the system, an organic sulfur catalyst is arranged in the organic sulfur catalytic reaction bed, an organic sulfur catalyst replacing device is arranged in the organic sulfur catalytic reaction bed, a second temperature regulating device is further arranged in the organic sulfur catalytic reaction bed, and the tower-type hydrolysis organic sulfur subsystem further comprises a first N arranged at the top of the tower2Gas inlet and first N arranged at bottom of tower2The tower type hydrolysis organic sulfur subsystem further comprises a second detachable tower bottom arranged at the bottom of the tower;
the blast furnace clean gas supply subsystem is configured to feed clean gas passing through the tower type hydrolysis organosulfur subsystem into the tower type secondary desulfurization subsystem;
the tower type secondary desulfurization subsystem is characterized in that a desulfurization reaction bed is arranged at the middle part of the tower type secondary desulfurization subsystem, a desulfurizer is arranged in the desulfurization reaction bed, a desulfurizer replacing device is arranged in the desulfurization reaction bed, a third temperature regulating device is further arranged in the desulfurization reaction bed, and the tower type secondary desulfurization subsystem further comprises a second N arranged at the top of the tower2Gas inlet and O2Gas inlet and N arranged at the bottom of the tower2Gas and O2The tower type secondary desulfurization subsystem also comprises a third detachable tower bottom arranged at the bottom of the tower;
the blast furnace clean gas supply subsystem is configured to send the clean gas passing through the tower type secondary desulfurization subsystem out of the blast furnace clean gas dry method cooperative deacidification system;
(2) performing deacidification treatment on the blast furnace clean gas through the blast furnace clean gas dry method cooperated with a deacidification system;
(3) when the dechlorination agent is penetrated to fail, heating the dechlorination agent to 85 ℃ by using the first temperature regulating device, and enabling the space velocity to be 2Hr-1The circulating water flows through the dechlorinating agent through the circulating water device, and the dechlorinating agent is regenerated after the circulating water is subjected to closed loop circulating treatment for 2 hours; after the dechlorination effect of the dechlorination agent is greatly reduced after the dechlorination agent is regenerated for a plurality of times, the dechlorination agent is replaced by using the dechlorination agent replacing device;
(4) heating the organosulfur catalyst to 250 ℃ while adding N using the second temperature adjustment device after the organosulfur catalyst is breakthrough-deactivated2Gas from the first N2Gas inlet is fed to the first N2Discharging the gas from a gas outlet, and blowing at constant temperature for 3 hours to regenerate the organic sulfur catalyst; after the catalytic effect of the organic sulfur catalyst is greatly reduced after the organic sulfur catalyst is regenerated for many times, the organic sulfur catalyst is replaced by using the organic sulfur catalyst replacing device;
(5) when the desulfurizer is penetrated and failed, the third temperature regulating device is used for heating the desulfurizer to 200 ℃, and N is added at the same time2Gas from the second N2Gas is fed in from a gas inlet to the merging outlet and is discharged, and the constant temperature purging 2h; thereafter heating the desulfurizing agent to 350 ℃ to remove O2Gas from said O2Gas inlet fed with2And N2Blowing gas together at constant temperature for 4h until the gas is discharged from the merging outlet, finally heating the desulfurizer to 500 ℃, and only using N2Blowing for 2h at constant temperature to regenerate the desulfurizer. (ii) a After the desulfurization effect of the desulfurizer regenerated for many times is greatly reduced, the desulfurizer is replaced by using the desulfurizer replacing device;
(6) when the tower-type dechlorination subsystem, the tower-type hydrolysis organic sulfur subsystem and the tower-type secondary desulfurization subsystem use the dregs accumulated at the bottom of the reaction bed and falling for a long time, the first detachable tower bottom, the second detachable tower bottom and the third detachable tower bottom are detached for cleaning and reinstallation.
Further, the dechlorinating agent is metal ions and Na2CO3The prepared dechlorinating agent.
Further, the organic sulfur catalyst is metal ion, KOH and Na2CO3The catalyst is prepared.
Further, the desulfurizer is made of metal oxide.
The reaction principle involved in the invention is as follows:
1. basic principle of utilizing dechlorinating agent to realize absorption and desorption reaction with hydrogen chloride
The principle of removing HCl in the gas of the blast furnace gas after gravity dust removal and cloth bag dust removal is that a dechlorinating agent arranged on a fixed bed layer of a dechlorinating tower and HCl in the gas are subjected to chemical reaction and physical adsorption to remove HCl in the gas, so that the effect of dechlorinating the gas is achieved. The industry and the site where dechlorinations are used have a relatively large impact on the active components of the dechlorination agent. The dechlorination agent active component aiming at the HCl in the blast furnace gas mainly refers to a substance which actually reacts with the HCl in the blast furnace gas in the dechlorination agent. The active component of the dechlorination agent may include metal oxides, carbonates, bicarbonates, hydroxides, and the like. Common possible active ingredients of dechlorinating agents are mainly: ZnO, CuO, Fe2O3、Na2CO3、MgCO3、CaCO3、NaHCO3、KOH、Ca(OH)2. The chemical reaction equation for these species with HCl includes:
ZnO+2HCl(g)——→ZnCl2+H2O(g) (1)
CuO+2HCl(g)——→CuCl2+H2O(g) (2)
2Fe2O3+6HCl(g)——→2FeCl3+3H2O(g) (3)
Na2CO3+2HCl(g)——→2NaCl+H2O(g)+CO2(g) (4)
MgCO3+2HCl(g)——→MgCl2+H2O(g)+CO2(g) (5)
CaCO3+2HCl(g)——→CaCl2+H2O(g)+CO2(g) (6)
NaHCO3+HCl(g)——→NaCl+H2O(g)+CO2(g) (7)
KOH+HCl(g)——→KCl+H2O(g) (8)
Ca(OH)2+2HCl(g)——→CaCl2+2H2O(g) (9)
2. basic principle for realizing organic sulfur hydrolysis of blast furnace gas after dechlorination by using catalyst
Blast furnace gas contains not only HCl acid gas but also sulfide acid components, which are also one of the factors that cause acid corrosion of the equipment. Blast furnace gas mainly contains organic sulfur and inorganic hydrogen sulfide. The organic sulfur can affect the removal of inorganic sulfur, and the principle of organic sulfur removal mainly converts organic sulfur into inorganic hydrogen sulfide which is easy to remove, and the hydrogen sulfide is removed by a dry desulfurizing agent. Organic sulfur includes carbonyl sulfide (COS) and carbon disulfide (CS)2) Organic sulfur removal is accomplished primarily by two typical reaction chemistries:
and (3) hydrolysis reaction: COS(g)+H2O(g)——→H2S(g)+CO2(g) (10)
CS2(g)+H2O(g)——→H2S(g)+CO2(g) (11)
Hydrogenolysis reaction: COS(g)+H2(g)——→H2S(g)+CO(g) (12)
CS2(g)+2H2(g)——→2H2S(g)+C (13)
The hydrolysis method has the advantages of suitable reaction conditions and good conversion effect, and has the advantages of low investment and low operating cost.
3. The basic principle of utilizing the desulfurizer to realize the reaction with the original hydrogen sulfide in the coal gas and the hydrogen sulfide obtained by hydrolysis conversion for absorption and removal
H2The S source is mainly the existence of blast furnace gas and the organic sulfur is converted by hydrolysis. H2The S removal is carried out by adopting a dry desulfurizing agent and is divided into the following two types:
H2s and oxygen generate sulfur under the action of a catalyst. The main reaction is as follows:
an adsorption process: organic sulfur such as hydrogen sulfide, thiophene and thioether is adsorbed on the surface of the catalyst.
And (3) desulfurization reaction: h2S(g)+O2(g)——→S+H2O(g) (14)
H2S and the desulfurizer are absorbed and removed through chemical reaction, and metal oxide is mostly adopted as the inorganic sulfur desulfurizer.
The main reaction is as follows:
MO+H2S(g)——→MS+H2O(g) (15)
4. basic principle for realizing regeneration of acid removal agent by using temperature regulating system, circulating water system, nitrogen supply system and oxygen supply system
The principle of dechlorination agent regeneration is as follows: at a certain temperature, water introduced into a dechlorinating agent bed layer reacts with metal chloride to form metal ions, and then the metal ions react with the water to generate corresponding metal oxide compounds, so that the dechlorinating capability of the metal oxide compounds is recovered;
the regeneration principle of the organic sulfur hydrolysis catalyst is as follows: when the catalyst is hydrolyzed and adsorbed, solid sulfate and elemental sulfur are generated on the surface of the catalyst to block the pore passages of the catalyst, and N is used2Blowing at a certain flow rate is beneficial to dredging blockage; meanwhile, when the catalyst is heated to a certain temperature, the failed catalyst is subjected to thermal decomposition, and the catalytic hydrolysis capability of the catalyst is recovered;
the regeneration principle of the desulfurizer is as follows: n is a radical of2Organic matters and other reducing substances attached to the surface of the deactivated desulfurizing agent can be removed by blowing; introduction of O2The carbon and sulfur components in the adsorbent can be removed by high-temperature roasting; introduction of N2Roasting at high temperature to make O2The byproduct sulfuric acid oxide generated by roasting and unreacted sulfide react to generate a regenerated target product metal oxide, and the desulfurization capability of the regenerated target product metal oxide is recovered.
The blast furnace gas dry method synergic deacidification system device and the process have the advantages that: the hydrogen chloride gas, the sulfide and other acidic gases in the blast furnace gas are removed simultaneously by utilizing a step-by-step process, so that the defect that the hydrogen chloride or the sulfide in the blast furnace gas can only be removed in a single way in the traditional industry is overcome; meanwhile, regeneration after the deacidification agent is out of work is designed in the deacidification tower, the investment and the energy consumption of the regeneration method are relatively small, and the capital loss of iron and steel enterprises caused by the corrosion problem of blast furnace equipment can be greatly saved. Compared with the traditional desulfurization or dechlorination deacidification effect and the equipment anticorrosion effect, the deacidification agent has the advantages of higher investment saving and energy saving performance due to regeneration.
The conception, the specific structure and the technical effects of the present invention will be further described with reference to the accompanying drawings to fully understand the objects, the features and the effects of the present invention.
Drawings
FIG. 1 is a flow chart of a blast furnace gas dry method synergic deacidification system device and a process flow chart.
Detailed Description
The technical contents of the preferred embodiments of the present invention will be more clearly and easily understood by referring to the drawings attached to the specification. The present invention may be embodied in many different forms of embodiments and the scope of the invention is not limited to the embodiments set forth herein.
Referring to fig. 1, the system device comprises a dedusted blast furnace clean gas supply system, a dechlorination system of a dechlorination tower, a hydrolyzed organic sulfur system of an organic sulfur hydrolysis tower, and a secondary desulfurization tower desulfurization system; the system is characterized in that the structural composition of each system and the connection mode of the configured devices are as follows:
firstly, a dust-removed blast furnace clean gas supply system: clean gas generated by raw gas generated at the top of the blast furnace after passing through a gravity dust collector and a bag-type dust collector enters a dechlorination tower 2 through a gas pipeline 1, is deacidified and then is discharged through a gas pipeline 7 to enter a next TRT and a pressure regulating valve bank;
secondly, a dechlorinating system of a dechlorinating tower: the system is connected behind a gas pipeline 1, a dechlorinating agent bed layer 2b is arranged in the middle of the dechlorinating tower and is filled with metal ions and Na2CO3The prepared dechlorinating agent; a temperature adjusting device 2a is arranged on the dechlorinating agent bed layer 2 b; a circulating water system is arranged on the surface of the dechlorinating agent bed layer 2b, circulating water enters from an inlet 2c and is discharged from an outlet 2 d; a dechlorinating agent replacing device 2g is arranged on the side surface of the dechlorinating agent bed layer 2 b; the bottom of the dechlorination tower is provided with a first detachable tower bottom 2e-2 f;
thirdly, the organic sulfur hydrolysis tower hydrolyzes the organic sulfur system: the system is connected behind a gas pipeline 5 at the outlet of a dechlorinating tower, an organic sulfur catalyst bed layer 3b is arranged in the middle part in an organic sulfur hydrolysis tower, and metal ions, KOH and Na are filled in the organic sulfur hydrolysis tower2CO3Preparing a catalyst; a temperature adjusting device 3a is arranged on the catalyst bed layer 3 b; the top and the bottom of the hydrolysis tower are provided with N2Gas source inlet and outlet, N 23c is controlled to enter through a valve, and 3d is controlled to discharge through the valve; a catalyst replacing device 3i is arranged on the side surface of the catalyst bed layer 3 b; the bottom of the organic sulfur hydrolysis tower is provided with a second detachable tower bottom for 3g-3 h;
fourthly, a second-stage desulfurizing tower desulfurizing system: the system is connected with coal gas at the outlet of the organic sulfur hydrolysis towerAfter the pipeline 6, a desulfurizer bed layer 4b is arranged in the middle of the secondary desulfurization tower and is filled with a dechlorinating agent made of metal oxide; a temperature adjusting device 4a is arranged on the desulfurizer bed layer 4 b; o is arranged at the top of the secondary desulfurizing tower2And N2A gas source inlet, a gas outlet arranged at the bottom, and a gas outlet2From 4c via valve control, N2From 4d via valve control inlet and from 4e via valve control outlet. A desulfurizer replacing device 4j is arranged on the side surface of the desulfurizer bed layer 4 b; the bottom of the second-stage desulfurization tower is provided with a third detachable tower bottom 4h-4 i;
in the invention, a temperature regulating system, a circulating water system and N are arranged on a reaction bed layer in each tower2/O2The supply system is used for regenerating the spent dechlorinating agent, the spent hydrolysis catalyst and the spent desulfurizing agent, greatly improves the effective utilization rate of the dechlorinating agent, saves the complicated process flow of replacing the deacidification agent and brings great economic benefit for enterprises.
The blast furnace clean gas at 150 ℃ discharged from a bag-type dust collector enters a dechlorinating tower 2 through a gas pipeline 1, when the gas passes through a dechlorinating agent bed layer 2b, HCl in the gas reacts with active components in a dechlorinating agent to generate metal chloride which is attached to the surface of the dechlorinating agent, and simultaneously, the active components of the dechlorinating agent also react with partial inorganic sulfide H in the gas2S reacts to generate metal sulfide which is attached to the surface of the dechlorinating agent, and the HCl and most of H in the blast furnace gas are removed after the blast furnace gas passes through the dechlorinating agent bed layer 2b2S；
The coal gas from the dechlorination tower enters an organic sulfur hydrolysis tower 3 through a coal gas pipeline 5, and organic sulfur COS and CS in the coal gas pass through a hydrolysis catalyst bed layer 3b2The water vapor in the coal gas is subjected to hydrolysis reaction under the driving action of a catalyst and is converted into inorganic sulfur H2S, the blast furnace gas passes through the hydrolysis catalyst bed layer 3b to convert organic sulfur into H2S；
The coal gas from the organic sulfur hydrolysis tower enters a secondary desulfurization tower 4 through a coal gas pipeline 6, and H which is not completely removed and hydrolyzed originally in the coal gas passes through a desulfurizer bed layer 4b2S reacts with active components in the desulfurizer to generate metal sulfides which are attached to the surface of the desulfurizer, and the blast furnace gas is desulfurizedRemoving H in the agent bed layer 4b2S。
After the dechlorinating agent in the dechlorinating tower 2 is penetrated and failed, the dechlorinating agent is regenerated by using the temperature regulating device 2a and the circulating water device, resources are repeatedly utilized, and the cost consumption is saved. The temperature adjusting device 2a is used for heating the penetrating dechlorinating agent to 85 ℃, circulating water enters from the 2c and is discharged from the 2d, and the space velocity of the circulating water flowing through the penetrating dechlorinating agent bed layer 2b is 2Hr-1Performing closed loop circulation treatment for 2 hours to obtain a regenerated dechlorinating agent; after the dechlorination effect of the dechlorination agent is greatly reduced after the dechlorination agent is regenerated for a plurality of times, 2g of the dechlorination agent replacing device is used for replacing the dechlorination agent;
after the hydrolysis catalyst agent in the organic sulfur hydrolysis tower 3 is penetrated and failed, the temperature regulating device 3a and the N2 purging device are utilized to realize the regeneration of the catalyst. Closing the gas pipeline valve 3f at the top and the gas pipeline valve 3e at the bottom of the hydrolysis tower, heating the catalyst to 250 ℃ by using a temperature adjusting device 3a, and blowing N2 into the catalyst bed 3b in the tower from 3c through valve control to purge the catalyst bed 3b2And 3d via valve control exhaust. Blowing at the constant temperature of 250 ℃ for 3h in the whole regeneration process of the hydrolysis catalyst to obtain a regenerated organic sulfur hydrolysis catalyst; after the catalytic effect of the organic sulfur catalyst regenerated for many times is greatly reduced, the organic sulfur catalyst is replaced by using an organic sulfur catalyst replacing device 3 i;
after the penetration failure of the secondary desulfurizer in the secondary desulfurizing tower 4, the temperature adjusting devices 4a and O are utilized2/N2The purging device realizes the regeneration of the catalyst. Closing the gas pipeline valve 4f at the top and the gas pipeline valve 4g at the bottom of the secondary desulfurization tower, and heating the desulfurizing agent to 200 ℃ by using a temperature adjusting device 4a to penetrate the desulfurizing agent, wherein N is2Entering the tower from 4c through valve control to purge a desulfurizer bed layer 4b, discharging purged N2 from 4e through valve control, and purging at the constant temperature of 200 ℃ for 2 h; then the desulfurizer is heated and penetrated to 350 ℃ by using a temperature adjusting device 4a, and N is2From 4c into the column via valve control, with O2The mixture enters the tower from 4d through valve control to purge the desulfurizer bed layer 4b together, and the purged N2+O2Discharging from the 4e through valve control, and purging at 350 deg.C for 4 h; finally, the desulfurizer is heated and penetrated by a temperature adjusting device 4a to 500 ℃ by heating, N2The mixture enters the tower from the 4c through valve control to blow a desulfurizer bed layer 4b, and the blown N2Discharging from the 4e through valve control, and blowing at the constant temperature of 500 ℃ for 2h to obtain a regenerated desulfurizer; after the desulfurization effect of the repeated regeneration of the desulfurizer is greatly reduced, the desulfurizer is replaced by using a desulfurizer replacing device 4 j;
when the dechlorination tower 2, the organic sulfur hydrolysis tower 3 and the secondary desulfurization tower 4 use the excessive dregs accumulated at the bottom of the reaction bed and dropped for a long time, the first detachable tower bottom 2e-2f, the second detachable tower bottom 3g-3h and the third detachable tower bottom 4h-4i are used for disassembly cleaning and reinstallation.
The foregoing detailed description of the preferred embodiments of the invention has been presented. It should be understood that numerous modifications and variations could be devised by those skilled in the art in light of the present teachings without departing from the inventive concepts. Therefore, the technical solutions available to those skilled in the art through logic analysis, reasoning and limited experiments based on the prior art according to the concept of the present invention should be within the scope of protection defined by the claims.
Claims (8)
1. A blast furnace clean gas dry method is cooperated with the deacidification system, which is characterized by comprising a dedusted blast furnace clean gas supply subsystem, a tower-type dechlorination subsystem, a tower-type organic sulfur hydrolysis subsystem and a tower-type secondary desulfurization subsystem; wherein:
the blast furnace clean gas supply subsystem is configured to firstly send clean gas obtained after raw gas generated at the top of the blast furnace passes through the gravity dust collector and the bag-type dust collector into the tower-type dechlorination subsystem through a supply pipeline;
the tower type dechlorination subsystem is configured to be provided with a dechlorination reaction bed in the middle, a dechlorination agent is arranged in the dechlorination reaction bed, a dechlorination agent replacing device is arranged in the dechlorination reaction bed, a first temperature adjusting device and a circulating water device are further arranged in the dechlorination reaction bed, and the tower type dechlorination subsystem further comprises a first detachable tower bottom arranged at the bottom of the tower;
the blast furnace clean gas feed subsystem is configured to feed clean gas passing through the tower dechlorination subsystem into the tower hydrolysis organosulfur subsystem;
the tower-type hydrolysis organic sulfur subsystem is configured to be provided with an organic sulfur catalytic reaction bed in the middle of the system, an organic sulfur catalyst is arranged in the organic sulfur catalytic reaction bed, an organic sulfur catalyst replacing device is arranged in the organic sulfur catalytic reaction bed, a second temperature regulating device is further arranged in the organic sulfur catalytic reaction bed, and the tower-type hydrolysis organic sulfur subsystem further comprises a first N arranged at the top of the tower2Gas inlet and first N arranged at bottom of tower2The tower type hydrolysis organic sulfur subsystem further comprises a second detachable tower bottom arranged at the bottom of the tower;
the blast furnace clean gas supply subsystem is configured to feed clean gas passing through the tower type hydrolysis organosulfur subsystem into the tower type secondary desulfurization subsystem;
the tower type secondary desulfurization subsystem is characterized in that a desulfurization reaction bed is arranged at the middle part of the tower type secondary desulfurization subsystem, a desulfurizer is arranged in the desulfurization reaction bed, a desulfurizer replacing device is arranged in the desulfurization reaction bed, a third temperature regulating device is further arranged in the desulfurization reaction bed, and the tower type secondary desulfurization subsystem further comprises a second N arranged at the top of the tower2Gas inlet and O2Gas inlet and N arranged at the bottom of the tower2Gas and O2The tower type secondary desulfurization subsystem also comprises a third detachable tower bottom arranged at the bottom of the tower;
the blast furnace clean gas supply subsystem is configured to send the clean gas passing through the tower type secondary desulfurization subsystem out of the blast furnace clean gas dry-method cooperative deacidification system.
2. The blast furnace clean gas dry-process cooperative deacidification system as defined in claim 1, wherein said dechlorinating agent is metal ion, Na2CO3The prepared dechlorinating agent.
3. The blast furnace clean gas dry-process cooperative deacidification system as defined in claim 1, wherein said organic sulfur catalyst is metal ion, KOH and Na2CO3The catalyst is prepared.
4. The blast furnace clean gas dry-method cooperative deacidification system as defined in claim 1, wherein said desulfurizer is a metal oxide desulfurizer.
5. A dry method synergic deacidification method for blast furnace clean gas is characterized by comprising the following steps:
(1) providing a dry-method cooperative deacidification system for blast furnace clean gas, which comprises a dedusted blast furnace clean gas supply subsystem, a tower-type dechlorination subsystem, a tower-type organic sulfur hydrolysis subsystem and a tower-type secondary desulfurization subsystem; wherein:
the blast furnace clean gas supply subsystem is configured to firstly send clean gas obtained after raw gas generated at the top of the blast furnace passes through the gravity dust collector and the bag-type dust collector into the tower-type dechlorination subsystem through a supply pipeline;
the tower type dechlorination subsystem is configured to be provided with a dechlorination reaction bed in the middle, a dechlorination agent is arranged in the dechlorination reaction bed, a dechlorination agent replacing device is arranged in the dechlorination reaction bed, a first temperature adjusting device and a circulating water device are further arranged in the dechlorination reaction bed, and the tower type dechlorination subsystem further comprises a first detachable tower bottom arranged at the bottom of the tower;
the blast furnace clean gas feed subsystem is configured to feed clean gas passing through the tower dechlorination subsystem into the tower hydrolysis organosulfur subsystem;
the tower-type hydrolysis organic sulfur subsystem is configured to be provided with an organic sulfur catalytic reaction bed in the middle of the system, an organic sulfur catalyst is arranged in the organic sulfur catalytic reaction bed, an organic sulfur catalyst replacing device is arranged in the organic sulfur catalytic reaction bed, a second temperature regulating device is further arranged in the organic sulfur catalytic reaction bed, and the tower-type hydrolysis organic sulfur subsystem further comprises a first N arranged at the top of the tower2Gas inlet and first N arranged at bottom of tower2The tower type hydrolysis organic sulfur subsystem further comprises a second detachable tower bottom arranged at the bottom of the tower;
the blast furnace clean gas supply subsystem is configured to feed clean gas passing through the tower type hydrolysis organosulfur subsystem into the tower type secondary desulfurization subsystem;
the tower type secondary desulfurization subsystem is characterized in that a desulfurization reaction bed is arranged at the middle part of the tower type secondary desulfurization subsystem, a desulfurizer is arranged in the desulfurization reaction bed, a desulfurizer replacing device is arranged in the desulfurization reaction bed, a third temperature regulating device is further arranged in the desulfurization reaction bed, and the tower type secondary desulfurization subsystem further comprises a second N arranged at the top of the tower2Gas inlet and O2Gas inlet and N arranged at the bottom of the tower2Gas and O2The tower type secondary desulfurization subsystem also comprises a third detachable tower bottom arranged at the bottom of the tower;
the blast furnace clean gas supply subsystem is configured to send the clean gas passing through the tower type secondary desulfurization subsystem out of the blast furnace clean gas dry method cooperative deacidification system;
(2) performing deacidification treatment on the blast furnace clean gas through the blast furnace clean gas dry method cooperated with a deacidification system;
(3) when the dechlorination agent is penetrated to fail, heating the dechlorination agent to 85 ℃ by using the first temperature regulating device, and enabling the space velocity to be 2Hr-1The circulating water flows through the dechlorinating agent through the circulating water device, and the dechlorinating agent is regenerated after the circulating water is subjected to closed loop circulating treatment for 2 hours; after the dechlorination agent is regenerated for a plurality of times and is subjected to dechlorination failure, the dechlorination agent is replaced by using the dechlorination agent replacing device;
(4) heating the organosulfur catalyst to 250 ℃ while adding N using the second temperature adjustment device after the organosulfur catalyst is breakthrough-deactivated2Gas from the first N2Gas inlet is fed to the first N2Discharging the gas from a gas outlet, and blowing at constant temperature for 3 hours to regenerate the organic sulfur catalyst; after the organic sulfur catalyst is regenerated and failed for many times, replacing the organic sulfur catalyst by using the organic sulfur catalyst replacing device;
(5) when the desulfurizer is penetrated and failed, the third temperature regulating device is used for heating the desulfurizer to 200 ℃, and N is added at the same time2Gas from the second N2Feeding gas from the gas inlet to the combined outlet, discharging, and blowing at constant temperature2 h; thereafter heating the desulfurizing agent to 350 ℃ to remove O2Gas from said O2Gas inlet fed with2And N2Blowing gas together at constant temperature for 4h until the gas is discharged from the merging outlet, finally heating the desulfurizer to 500 ℃, and only using N2Blowing at constant temperature for 2h to regenerate the desulfurizer; after the desulfurizer fails in regeneration for many times, the desulfurizer is replaced by using the desulfurizer replacing device;
(6) when the tower-type dechlorination subsystem, the tower-type hydrolysis organic sulfur subsystem and the tower-type secondary desulfurization subsystem use the dregs accumulated at the bottom of the reaction bed and falling for a long time, the first detachable tower bottom, the second detachable tower bottom and the third detachable tower bottom are detached for cleaning and reinstallation.
6. A dry method synergic deacidification method for blast furnace clean gas is provided, wherein the dechlorinating agent is metal ions and Na2CO3The prepared dechlorinating agent.
7. A dry-method synergic deacidification method for blast furnace clean gas is disclosed, wherein the organic sulfur catalyst is metal ions, KOH and Na2CO3The catalyst is prepared.
8. A dry method synergic deacidification method for blast furnace clean gas is disclosed, wherein the desulfurizer is prepared from metal oxide.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113372965A (en) * | 2021-06-28 | 2021-09-10 | 中晶环境科技股份有限公司 | Blast furnace gas desulfurization process |
| CN114015480A (en) * | 2021-11-22 | 2022-02-08 | 国家电投集团远达环保装备制造有限公司 | Process system for deeply purifying blast furnace gas and producing high-purity carbon dioxide as byproduct |
| CN114181742A (en) * | 2021-11-11 | 2022-03-15 | 北京铝能清新环境技术有限公司 | Blast furnace gas source treatment system |
| CN114196448A (en) * | 2022-02-16 | 2022-03-18 | 北京中航天业科技有限公司 | Full-flow dry type blast furnace gas fine desulfurization system and method |
| CN114392643A (en) * | 2021-12-30 | 2022-04-26 | 北京北科环境工程有限公司 | Preparation method of dechlorinating agent for blast furnace gas |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2494711A1 (en) * | 1980-11-26 | 1982-05-28 | Didier Eng | Treatment of coke-oven gas and blast furnace off-gas - by methanation in admixture with carbon mon:oxide from blast furnace off-gas, to give substitute natural gas |
| CN102534082A (en) * | 2012-02-29 | 2012-07-04 | 中冶赛迪工程技术股份有限公司 | Dry-process dust-removing and dechlorination combined device for blast furnace gas |
| CN110218828A (en) * | 2019-07-15 | 2019-09-10 | 湖北申昙环保新材料有限公司 | Blast furnace gas purification method |
| CN110452744A (en) * | 2019-08-08 | 2019-11-15 | 佰利天控制设备（北京）有限公司 | Blast furnace coal gas comprehensive management of environmental protection system and technique |
| CN110484307A (en) * | 2019-08-20 | 2019-11-22 | 安徽宝天新能源科技有限公司 | A kind of blast furnace gas dechlorination, desulphurization system and technique |
| CN111004652A (en) * | 2019-12-16 | 2020-04-14 | 首钢集团有限公司 | System and method for removing sulfur-containing compounds in blast furnace gas |
-
2020
- 2020-04-30 CN CN202010360494.XA patent/CN112593034B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2494711A1 (en) * | 1980-11-26 | 1982-05-28 | Didier Eng | Treatment of coke-oven gas and blast furnace off-gas - by methanation in admixture with carbon mon:oxide from blast furnace off-gas, to give substitute natural gas |
| CN102534082A (en) * | 2012-02-29 | 2012-07-04 | 中冶赛迪工程技术股份有限公司 | Dry-process dust-removing and dechlorination combined device for blast furnace gas |
| CN110218828A (en) * | 2019-07-15 | 2019-09-10 | 湖北申昙环保新材料有限公司 | Blast furnace gas purification method |
| CN110452744A (en) * | 2019-08-08 | 2019-11-15 | 佰利天控制设备（北京）有限公司 | Blast furnace coal gas comprehensive management of environmental protection system and technique |
| CN110484307A (en) * | 2019-08-20 | 2019-11-22 | 安徽宝天新能源科技有限公司 | A kind of blast furnace gas dechlorination, desulphurization system and technique |
| CN111004652A (en) * | 2019-12-16 | 2020-04-14 | 首钢集团有限公司 | System and method for removing sulfur-containing compounds in blast furnace gas |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113372965A (en) * | 2021-06-28 | 2021-09-10 | 中晶环境科技股份有限公司 | Blast furnace gas desulfurization process |
| CN113372965B (en) * | 2021-06-28 | 2024-05-28 | 中晶环境科技股份有限公司 | Desulfurization process for blast furnace gas |
| CN114181742A (en) * | 2021-11-11 | 2022-03-15 | 北京铝能清新环境技术有限公司 | Blast furnace gas source treatment system |
| CN114015480A (en) * | 2021-11-22 | 2022-02-08 | 国家电投集团远达环保装备制造有限公司 | Process system for deeply purifying blast furnace gas and producing high-purity carbon dioxide as byproduct |
| CN114392643A (en) * | 2021-12-30 | 2022-04-26 | 北京北科环境工程有限公司 | Preparation method of dechlorinating agent for blast furnace gas |
| CN114392643B (en) * | 2021-12-30 | 2022-09-23 | 北京北科环境工程有限公司 | Preparation method of dechlorinating agent for blast furnace gas |
| CN114196448A (en) * | 2022-02-16 | 2022-03-18 | 北京中航天业科技有限公司 | Full-flow dry type blast furnace gas fine desulfurization system and method |
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