CN114907889A - Efficient blast furnace gas dechlorination and desulfurization system and process - Google Patents
Efficient blast furnace gas dechlorination and desulfurization system and process Download PDFInfo
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- CN114907889A CN114907889A CN202210433040.XA CN202210433040A CN114907889A CN 114907889 A CN114907889 A CN 114907889A CN 202210433040 A CN202210433040 A CN 202210433040A CN 114907889 A CN114907889 A CN 114907889A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/024—Dust removal by filtration
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/028—Dust removal by electrostatic precipitation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
- C10K1/122—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors containing only carbonates, bicarbonates, hydroxides or oxides of alkali-metals (including Mg)
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/34—Purifying combustible gases containing carbon monoxide by catalytic conversion of impurities to more readily removable materials
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Abstract
The invention discloses a high-efficiency blast furnace gas dechlorination and desulfurization system and a process. The system comprises; (a) at least one stage of gravity dust collector; (b) at least one stage of bag-type dust collector/electric dust collector; (c) at least one stage of blast furnace gas dechlorination tower; (d) at least one stage of blast furnace gas catalytic tower; and (f) at least one desulfurization tower; a blast furnace TRT and a pressure regulating valve bank are arranged between the blast furnace gas dechlorinating tower and the blast furnace gas catalyzing tower in parallel; the blast furnace gas catalytic tower comprises: a column body having a catalyst supported therein; the feeding component is used for adding the spherical catalyst into the tower body, the feeding component is provided with a feeding cavity communicated with the tower body, the feeding cavity is provided with a control valve which can isolate the air environment from the feeding cavity, so that the resistance loss is controlled below 1.5kPa, and the outlet pressure of the blast furnace gas catalytic tower is 160-165 kPa.
Description
Technical Field
The invention belongs to the technical field of environment-friendly equipment, and particularly relates to a high-efficiency dechlorination and desulfurization system and process for blast furnace gas.
Background
The blast furnace gas is a byproduct combustible gas in the production process of the blast furnace, has large yield and wide application, and can be used as a fuel for blast furnaces of power plants, hot blast furnaces of steel mills and heating furnaces of iron works. The main components of the blast furnace gas are CO and CO 2 、N 2 And also contains small amount of COS and H 2 S、Cl - Dust, etc. Because of SO in flue gas discharged by blast furnace gas users (such as blast furnace of power plant, hot blast furnace of steel mill and heating furnace of iron-making plant) 2 Content, Cl - The content of the SO-containing catalyst can not meet the national ultra-clean emission requirement, and the SO in the flue gas discharged by the catalyst usually reaches the national ultra-clean emission requirement 2 The content is more than 50mg/m 3 Some production plants discharge SO in flue gas 2 Even up to 200mg/m 3 The above.
The existing gas desulfurization/desulfurization equipment mainly removes sulfur, namely H, of coke oven gas or artificial gas 2 S, the sulfur in the blast furnace gas is mainly COS, the blast furnace gas desulfurization is mainly used for removing the COS, and the existing gas desulfurization process cannot remove the COS in the blast furnace gas, so that the existing gas desulfurization process cannot meet the requirement of the blast furnace gas desulfurization.
In addition, with the popularization of blast furnace gas dry dedusting, most of domestic blast furnace gas of iron and steel enterprises adopts dry dedusting, the chloride ions in the blast furnace gas subjected to dry dedusting exceed the standard, so that the corrosion of TRT blades and a gas pipe network is very serious, the gas pipelines of the iron and steel enterprises which are not subjected to dechlorination treatment are generally used for about 3 years, the gas pipelines are corroded and perforated to different degrees, the pipelines are required to be replaced about 6 years generally, and great potential safety hazards are brought to the safety production of the enterprises. Because the general station main pipe of blast furnace gas pipeline does not have reserve pipeline or trip valve, change the house steward often and need the enterprise to stop production to change, seriously influence steel enterprise's normal production, cause huge potential safety hazard, change the pipeline simultaneously also greatly increased the manufacturing cost of enterprise.
By search, Chinese patent CN110484307A disclosesA dechlorinating and desulfurizing system for blast furnace gas is composed of a dechlorinating tower for blast furnace gas, a desulfurizing system for blast furnace gas, a gravitational dust collector, a dry cloth bag dust collector, a TRT or pressure regulating valve set for the dechlorinated blast furnace gas, a desulfurizing system for the gas from the dechlorinating tower, and a catalytic tower for converting the COS into H 2 S; conveying the blast furnace gas treated by the catalytic tower to a desulfurizing tower of a blast furnace gas desulfurizing system, and enabling the blast furnace gas desulfurizing tower to remove H in the blast furnace gas 2 S, carrying out desulfurization treatment; the treated blast furnace gas is transmitted to a blast furnace gas main pipe of a plant area through a gas pipe network for each user to use. The invention integrates the processes of dechlorination and dechlorination of the blast furnace gas, and can effectively solve the problem of SO in flue gas generated after the blast furnace gas is combusted 2 And the problem of exceeding standard is solved, and in addition, the dechlorinated blast furnace gas greatly delays the corrosion of TRT blades and the corrosion of blast furnace gas pipelines.
Disclosure of Invention
1. Problems to be solved
In view of the above, the present invention aims to provide a high-efficiency dechlorination and desulfurization system for blast furnace gas, which can effectively remove COS and chloride ions in the blast furnace gas; meanwhile, on the premise of not influencing the production of the whole system as much as possible, the spherical catalyst is rapidly added on line.
The invention also provides a high-efficiency blast furnace gas dechlorination and desulfurization process based on the above, which can effectively remove sulfur and chlorine in the blast furnace gas, so that the flue gas discharged after the blast furnace gas is combusted meets the national environmental protection requirement, and the problem of blast furnace gas pipeline corrosion can be effectively solved.
2. Technical scheme
In order to achieve the purpose, the invention adopts the following technical scheme:
the high-efficiency blast furnace gas dechlorination and desulfurization system comprises; (a) at least one stage of gravity dust collector capable of removing large particles in blast furnace gas; (b) at least one stage of bag-type dust collector/electric dust collector capable of removing tiny particles in blast furnace gas; (c) at least one stage of blast furnace gas dechlorinating tower; (d) at least one stage of blast furnace gas catalytic tower; and (f) at least one desulfurization tower; a blast furnace TRT and a pressure regulating valve bank are arranged between the blast furnace gas dechlorinating tower and the blast furnace gas catalytic tower in parallel; the blast furnace gas catalytic tower comprises: a column body having a catalyst supported therein; the feeding component is used for additionally arranging the spherical catalyst in the tower body, the feeding component is provided with a feeding cavity communicated with the tower body in a connecting way, and the feeding cavity is provided with a control valve which can isolate the air environment from the feeding cavity, so that the resistance loss is controlled below 1.5kPa, and the outlet pressure of the blast furnace gas catalytic tower is 160-165 kPa.
Through the reinforced cavity that sets up above the tower body and this body coupling intercommunication of tower, reinforced cavity has a plurality of compartment cavities to the cooperation has control valve, at reinforced in-process, reduces the inside environment of tower body and air UNICOM as far as, thereby reduces the inside pressure variation of catalytic tower, guarantees that entire system's pressure value is stable, the smooth of guarantee production goes on.
In one possible embodiment of the present invention, the particle size of the spherical catalyst is 4-10 μm, and the reaction temperature is 110-; the spherical catalyst is an alumina-based alkali metal/alkaline earth metal/transition metal catalyst or a titania-based alkali metal/alkaline earth metal/transition metal catalyst; 0.2-0.5 wt% of naphthoate is loaded on the catalyst carrier, wherein the naphthoate is one or more of nickel, cobalt and molybdenum salts.
In a possible embodiment of the invention, the charging member has at least a first charging chamber and a second charging chamber arranged longitudinally, the first charging chamber being provided with a first control valve and the second charging chamber being provided with a second control valve.
In a possible embodiment of the present invention, the first feeding cavity and the second feeding cavity have the same structural shape, the first feeding cavity is in an inverted cone shape, and the lower end of the first feeding cavity is provided with a discharge hole; the first control valve is arranged on one side of the discharge hole.
In a possible embodiment of the present invention, the first charging chamber is configured with a vacuum pump, and the vacuum pump is connected to the first charging chamber through a pipe. When the pressure value inside the feeding cavity changes due to the fact that the pressure value is communicated with the external air environment, the numerical value is displayed through the vacuum pressure displayer, the vacuum pumping air pump works to timely extract air in the feeding cavity, and the stability of the ambient pressure value inside the feeding cavity is guaranteed.
In a possible implementation manner of the present invention, the vacuum pressure display is disposed on the first charging cavity, so as to immediately reflect an ambient pressure value inside the charging cavity, thereby facilitating timely control and operation.
In a possible embodiment of the present invention, the charging member has an elongated charging chamber, and two control valves are longitudinally disposed on the charging chamber to divide the charging chamber into at least two spaces.
In a possible embodiment of the invention, the cross-sectional shape of the charging chamber is circular, elliptical, square, triangular, pentagonal or hexagonal.
In a possible implementation manner of the invention, the system comprises a primary rough removal tower and a secondary fine removal tower which is connected with the primary rough removal tower in series, wherein the tops of the primary desulfurization tower and the secondary fine removal tower are communicated through an inter-tower connecting pipeline; a plurality of rows of spray guns are arranged at the upper part in the primary rough removal tower and spray alkali-containing water for desulfurization and dechlorination; the upper part in the secondary fine threshing tower is provided with a plurality of spray guns and a diversion cone; the bottom of the primary blast furnace gas rough stripping tower enters, alkali-containing water sprayed by the spray gun is subjected to desulfurization treatment, then enters from the upper part of the secondary fine stripping tower through an inter-tower connecting pipeline, is subjected to secondary desulfurization treatment, and then passes through the flow guide cone and is output from the blast furnace gas outlet at the top of the secondary fine stripping tower.
The process of the high-efficiency blast furnace gas dechlorination and desulfurization system comprises the following steps of:
step S101: after the blast furnace gas is dedusted by the gravity deduster and the bag deduster/electric deduster, the dust content is not more than 10mg/Nm 3 And then is conveyed to a blast furnace gas dechlorinating tower;
step S102:the dechlorinated blast furnace gas passes through a pressure regulating valve bank or a residual pressure turbine power generation device and then enters a blast furnace gas catalytic tower, and a spherical catalyst is arranged in the blast furnace gas catalytic tower; the particle size of the spherical catalyst is 4-10 microns, and the reaction temperature is 110-250 ℃; the spherical catalyst is an alumina-based alkali metal/alkaline earth metal/transition metal catalyst or a titania-based alkali metal/alkaline earth metal/transition metal catalyst, wherein the alkali metal comprises sodium and potassium; the alkaline earth metal includes magnesium, calcium, strontium, and barium; transition metals include manganese, iron, copper, zinc; 0.2-0.5 wt% of naphthoate is loaded on the catalyst carrier; the space velocity of the spherical catalyst is 0-10000h -1 The COS in the blast furnace gas is catalytically converted into H 2 S, conversion reaction process: COS + H 2 O＝H 2 S+CO 2 Converting COS in the blast furnace gas;
step S103: the blast furnace gas treated by the blast furnace gas catalytic tower enters a blast furnace gas desulfurization tower;
step S104: a spray gun is arranged in the blast furnace gas desulfurization tower, the blast furnace gas is sprayed with alkali-containing water with the pH value of 9.8-11.8, and H in the blast furnace gas is treated 2 S and Cl - Carrying out desulfurization and dechlorination treatment, wherein the reaction comprises the following steps: 2NaOH + H 2 S＝Na 2 S+2H 2 O，NaOH+HCl＝NaCl+H 2 And O, the blast furnace gas is treated by the desulfurizing tower and then is transmitted to each user through a blast furnace gas pipe network.
3. Advantageous effects
Compared with the prior art, the invention has the beneficial effects that:
according to the high-efficiency dechlorination and desulfurization system for the blast furnace gas, the blast furnace gas is subjected to dechlorination and desulfurization treatment, so that the corrosion of the blast furnace gas on TRT blades and a gas pipeline can be greatly relieved, the service lives of the TRT blades and the gas pipeline are prolonged, and the production safety risk and the operation cost of enterprises are reduced.
Drawings
The technical solutions of the present invention will be described in further detail below with reference to the accompanying drawings and examples, but it should be understood that these drawings are designed for illustrative purposes only and thus do not limit the scope of the present invention. Furthermore, unless otherwise indicated, the drawings are intended to be illustrative of the structural configurations described herein and are not necessarily drawn to scale.
FIG. 1 is a schematic structural diagram of a high-efficiency blast furnace gas dechlorination and desulfurization system of the present invention;
fig. 2 is a layout of a blast furnace gas catalytic tower of the present invention;
FIG. 3 is a schematic view of the structure of a blast furnace gas catalytic tower according to example 1;
FIG. 4 is a schematic view of the structure of a blast furnace gas catalytic tower according to example 2;
fig. 5 is a SEM image of the blast furnace gas catalyst naphthenate loading.
Description of reference numerals:
100. a gravity dust collector;
200. a bag-type dust collector;
300. a blast furnace gas dechlorination tower;
400. a blast furnace gas catalytic tower; 410. a tower body; 411. a catalytic layer; 420. a charging member; 421. a charging cavity; 4211. a first charging chamber; 4212. a discharge port; 4213. a vacuum air pump is pumped; 4214. a vacuum pressure display; 4215. a second charging cavity; 422. a control valve; 4221. a first control valve; 4222. a second control valve;
500. blast furnace TRT;
600. a pressure regulating valve bank;
700. provided is a blast furnace gas desulfurization tower.
Detailed Description
The detailed description and exemplary embodiments of the invention will be better understood when read in conjunction with the appended drawings, where the elements and features of the invention are identified by reference numerals.
Example 1
The blast furnace gas contains CO and CO 2 、N 2 In addition, it also contains COS and H 2 S、Cl - The components are equal, if the blast furnace gas is not desulfurized and dechlorinated, the pipeline of the whole plant is seriously corroded, and the SO meets the national environmental protection requirement 2 The emission index needs to set flue gas desulfurization for users using blast furnace gas in the whole plant. The invention carries out desulfurization on blast furnace gasDechlorinating, and separating COS and H in blast furnace gas 2 S、Cl - After the gas is completely removed, the blast furnace gas is transmitted to each user for use, SO that SO in the flue gas of each user can be ensured 2 The discharge is less than 35mg/m 3 And meets the requirements of national environmental protection policy.
However, the main component of sulfur in blast furnace gas is carbonyl sulfide (COS), and the hydrolytic conversion of carbonyl sulfide is affected by three factors: 1) oxygen in the gas: when the temperature of oxygen in the coal gas is 100-; 2) chloride ions in the coal gas: chloride ions can damage the hydrolysis catalyst substrate, causing the hydrolysis catalyst to lose effectiveness; 3) coal gas dust content: the dust is attached to the surface of the hydrolysis catalyst, so that the blockage of the hydrolysis catalytic tower is easily caused, and the production of a blast furnace is influenced.
As shown in figure 1, the high-efficiency blast furnace gas dechlorination and desulfurization system comprises a gas supply device, a gas supply device and a gas supply device; (a) a gravity precipitator 100 capable of removing large particles from blast furnace gas; (b) the bag-type dust collector 200/electric dust collector can remove tiny particles in blast furnace gas; (c) a blast furnace gas dechlorination tower 300; (d) a blast furnace gas catalytic tower 400; and (f) a desulfurization tower 700; a blast furnace TRT500 and a pressure regulating valve bank 600 are arranged between the blast furnace gas dechlorinating tower and the blast furnace gas catalytic tower in parallel, and the blast furnace gas catalytic tower 400 is arranged behind the blast furnace TRT500 or the pressure regulating valve bank, so that a catalyst layer in the catalytic tower is provided with a heating facility, and the influence on the catalyst caused by the separation of gas condensate water when extreme low temperature occurs is avoided.
The blast furnace gas passes through a gravity dust collector 100 and a dry cloth bag dust collector 200 and then is input into a blast furnace gas dechlorinating tower 300, and Cl in the blast furnace gas is removed through the blast furnace gas dechlorinating tower 300 - Absorbing, conveying the absorbed gas to a catalytic tower in a gas desulfurization system of the blast furnace through a TRT/or silencing pressure regulating valve bank, and converting COS in the gas into H by the catalytic tower 2 S, conveying the converted coal gas to a blast furnace gas desulfurization tower to remove H in the blast furnace gas 2 S, carrying out desulfurization treatment, and transmitting the treated blast furnace gas to a blast furnace gas main pipe of a plant area through a gas pipe network for supplyingIs used by each user.
The catalytic tower is used for treating the COS in the blast furnace gas and catalyzing the COS in the blast furnace gas to convert the COS into H 2 S, facilitating the subsequent process to absorb H 2 S, outlet H 2 S concentration is less than or equal to 5mg/Nm 3 The desulfurization efficiency can meet 90-98%, thereby removing sulfur in the blast furnace gas. The system has higher requirement on the pressure parameter in the treatment process, thus the operation reduces the gas resistance of the catalytic tower as much as possible, the resistance loss is controlled below 1.5kPa, the outlet pressure of the catalytic tower is 160-165kPa, the temperature of blast furnace gas is 110-250 ℃, the vertical catalytic tower adopts a spherical catalyst, and under the general condition, as shown in figure 2, two catalytic towers are arranged in parallel and are both connected to a dechlorination tower at the front end.
In this embodiment, as shown in fig. 3-4, the blast furnace gas catalytic tower 400 includes a tower body 410 having a catalyst supported therein; the feeding component 420 is used for adding a spherical catalyst into the tower body 410, the feeding component 420 is provided with a feeding cavity 421 which is communicated with the tower body 410, and the feeding cavity 420 is provided with a control valve 422 which can isolate the air environment from the feeding cavity 421.
Wherein the particle size of the spherical catalyst is 4-10 microns, as shown in FIG. 5, the particle size of the spherical catalyst is 8 microns, and the reaction temperature is 110-250 ℃; the spherical catalyst is an alumina-based alkali metal/alkaline earth metal/transition metal catalyst or a titania-based alkali metal/alkaline earth metal/transition metal catalyst; a large number of tests prove that the hydrolysis catalyst has better oxidation resistance and improves the oxidation resistance of the hydrolysis catalyst, 0.2-0.5 wt% of naphthoate is loaded on the catalyst carrier, as shown in figure 5, the black part is the naphthoate, wherein the naphthoate is one or more of nickel, cobalt and molybdenum salts, and has better oxygen absorption effect, and meanwhile, the nickel, the cobalt and the molybdenum can play a role in catalyzing COS hydrolysis.
For example, the catalyst may be prepared by a method comprising: 1) to canSoluble titanium salt and iron salt are added into soluble aluminum salt as catalyst carrier precursor, and the three are mixed with deionized water according to the formula of gamma-Al 2 O 3 80wt％、TiO 2 5 wt% and Fe 2 O 3 Mixing at 15 wt%, adding more than one pore-forming agent (such as sodium bicarbonate) and binder (such as chitosan), mixing, drying at 120 deg.C for 8 hr, and baking at 400 deg.C for 6 hr to obtain carrier with particle diameter of 4-10 μm; 2) mixing the carrier with 0.2 wt% of naphthoate and 10 wt% of sodium salt, potassium salt or lithium salt aqueous solution, and carrying out ultrasonic impregnation for 3 h; 3) and (3) drying the solid obtained in the step (2) at 120 ℃ to constant weight to obtain the catalyst particles.
Further, as shown in fig. 3, the charging member 420 has at least a first charging chamber 4211 and a second charging chamber 4215 arranged longitudinally, the first charging chamber 4211 is provided with a first control valve 4221, and the second charging chamber 4215 is provided with a second control valve 4222. When the catalyst is added, the first control valve 4221 is opened, the spherical catalyst closed by the second control valve 4222 enters the second addition cavity 4215 from the first addition cavity 4211, and when the catalyst is added to a rated amount, the second control valve 4222 is opened after the first control valve 4221 is closed, and the spherical catalyst is added into the catalytic tower.
On the basis of the above structure, the first charging cavity 4211 and the second charging cavity 4215 may have the same or different structural shapes, preferably, the first charging cavity 4211 and the second charging cavity 4215 have the same structural shape, the first charging cavity 4211 is in an inverted cone shape, and the lower end of the first charging cavity 4211 is provided with a discharge hole 4212; the first control valve 4211 is installed at one side of the discharge hole 4212. The spherical catalyst can easily enter the column body 410 along the inverted conical feed chamber 421.
While the first control valve 4221 is opened, air in the first feeding chamber 4211 also enters the second feeding chamber 4215, and opening the second control valve 4222 causes instantaneous fluctuation of the internal environment of the column body 410, which is not favorable for monitoring. Thus, as shown in FIG. 3, a vacuum pressure indicator 4214 is provided on the first loading chamber 4211. The first charging chamber 4211 is provided with a vacuum air pump 4213, and the vacuum air pump 4213 is connected to the first charging chamber 4211 through a pipeline. When the pressure value in the charging cavity 421 changes due to the communication with the external air environment, the value is displayed by the vacuum pressure display 4214, and the vacuum air pump 4213 works to timely extract the air in the charging cavity 421, so that the stability of the ambient pressure value in the charging cavity 421 is ensured.
Through the structural improvement, when the catalyst is added into the catalytic tower on line, the stability of the internal ambient pressure value of the tower body is realized. Taking the blast furnace gas of a certain steel plant as an example, the temperature of the blast furnace gas is 200 ℃, and the resistance loss of the catalytic tower is controlled to be about 1.3kPa through dust removal and dechlorination at the front end, the outlet pressure of the catalytic tower is 165kPa, and the smooth production is ensured.
According to the field situation, the blast furnace gas dechlorination tower and the blast furnace gas dechlorination tower 300 can adopt two (one for one) or one single arrangement in parallel, and are provided with by-pass pipes, when the dechlorination tower is abnormal, the by-pass pipes can be taken away, the influence on the normal production of the blast furnace is avoided, when the by-pass pipes are used in parallel, when the dechlorination agents of the dechlorination towers reach the service life, the dechlorination agents reach the service life, the dechlorination towers are switched to the standby dechlorination tower, then the dechlorination agents reaching the service life are replaced, and the influence on the normal production of the blast furnace is avoided.
In this embodiment, the blast furnace gas desulfurization tower 700 employs two-stage desulfurization, including a primary rough-removal tower, a secondary fine-removal tower, and inter-tower connecting pipes; the primary rough stripping tower and the secondary fine stripping tower are arranged in series, and the tops of the primary rough stripping tower and the secondary fine stripping tower are communicated through an inter-tower connecting pipeline; the upper part in the primary rough removal tower is provided with a plurality of rows of spray guns for spraying alkali-containing water for desulfurization and dechlorination; the upper part in the secondary fine threshing tower is provided with a plurality of spray guns and a diversion cone; the bottom of the primary blast furnace gas rough stripping tower enters, alkali-containing water sprayed by the spray gun is subjected to desulfurization treatment, then enters from the upper part of the secondary fine stripping tower through an inter-tower connecting pipeline, is subjected to secondary desulfurization treatment, and then passes through the flow guide cone and is output from the blast furnace gas outlet at the top of the secondary fine stripping tower.
A gas dechlorination tower is arranged in front of the blast furnace TRT or the pressure regulating valve bank to remove Cl in the gas - And the dechlorination tower can see the scene situationThe condition setting is used for one time or independently.
The flow velocity of blast furnace gas passing through a primary rough removal tower of the blast furnace gas desulfurization tower is 1-5 m/s, and the gas retention time is at least 10 seconds; the flow velocity of the blast furnace gas passing through the secondary fine-removing tower of the blast furnace gas desulfurization tower is 8-25 m/s; the pH value of the alkali-containing water sprayed in the blast furnace gas desulfurization tower is 9.8-11.8; the bottoms of the dechlorinating agent layer and the catalysis layer in the blast furnace gas dechlorinating and desulfurizing tower are respectively provided with a discharge opening and a feed opening; a separator (not marked in the figure) is arranged below a gas outlet of the blast furnace gas desulfurization tower; an airflow distributor (not marked in the figure) is arranged in the primary rough removal tower of the blast furnace gas desulfurization tower and above a blast furnace gas inlet; and a spray gun (not marked in the figure) is arranged in the secondary fine removal tower of the blast furnace gas desulfurization tower and above the diversion cone and is used for spraying alkali-containing water for desulfurization and dechlorination.
The system comprises blast furnace gas desulfurization towers 700 arranged in series; two sets of blast furnace gas desulfurizing towers 700 arranged in series carry out two times of deep desulfurizing treatment on the blast furnace gas.
Example 2
As shown in fig. 4, the charging member 420 has an elongated charging chamber 421, the cross-sectional shape of the charging chamber 421 is circular, oval, square, triangular, pentagonal or hexagonal, preferably the cross-sectional shape of the charging chamber is square, and two control valves 422 are longitudinally arranged on the charging chamber 421 to divide the charging chamber 421 into at least two spaces. The square structure of the charging chamber 421 is selected to facilitate the edge sealing of the control valve 422.
When the upper control valve 422 is opened, air also enters the feeding cavity 422, and then the lower control valve 422 is opened, which may cause instant fluctuation of the internal environment of the tower body 410, and is not favorable for monitoring that the feeding cavity 421 is configured with a vacuum air pump 4213, and the vacuum air pump 4213 is connected to the feeding cavity 421 through a pipeline. A vacuum pressure display 4214 is arranged on the charging cavity 421. When the pressure value inside reinforced cavity 421 changes owing to appear when UNICOM with external air environment, through vacuum pressure display numerical value to by the work of evacuation air pump, in time extract the air in the reinforced cavity, guarantee reinforced cavity 421 inside ambient pressure value stability.
Through the structural improvement, when the catalyst is added into the catalytic tower on line, the stability of the internal ambient pressure value of the tower body is realized, the temperature of blast furnace gas in a certain steel plant is 180 ℃, and the resistance loss is controlled to be about 1.41kPa through the front-end dust removal and dechlorination, and the outlet pressure of the catalytic tower is 162kPa, so that the smooth production is ensured.
Example 3
According to the purpose of the invention, the charging part is provided with a charging bag with two ends capable of being sealed, or at least provided with blowing bins arranged in series, each blowing bin can be isolated from air to form an internal space, and the purpose of isolating the air environment from the charging cavity can be realized.
Example 4
The process based on the high-efficiency blast furnace gas dechlorination and desulfurization system comprises the following steps:
step S101: after the blast furnace gas is dedusted by the gravity deduster 100 and the bag-type deduster 200, the dust content is not more than 10mg/Nm 3 And then is transmitted to a blast furnace gas dechlorinating tower;
step S102: the dechlorinated blast furnace gas passes through a pressure regulating valve bank or a residual pressure turbine power generation device and then enters a blast furnace gas catalytic tower 400, and a spherical catalyst is arranged in the blast furnace gas catalytic tower 400; the particle size of the spherical catalyst is 6 microns, and the reaction temperature is 200 ℃; the spherical catalyst is an alumina-based sodium catalyst; 0.2 wt% of nickel naphthoate is loaded on the catalyst carrier; the space velocity of the spherical catalyst is 10000h -1 The COS in the blast furnace gas is catalytically converted into H 2 S, conversion reaction process: COS + H 2 O＝H 2 S+CO 2 Converting COS in the blast furnace gas;
step S103: the blast furnace gas treated by the blast furnace gas catalytic tower enters a blast furnace gas desulfurization tower 700;
step S104: a spray gun is arranged in the blast furnace gas desulfurization tower and is used for the blast furnaceSpraying alkaline water with pH value of 9.8 on the coal gas to remove H in the blast furnace coal gas 2 S and Cl - Carrying out desulfurization and dechlorination treatment, wherein the reaction comprises the following steps: 2NaOH + H 2 S＝Na 2 S+2H 2 O，NaOH+HCl＝NaCl+H 2 And O, the blast furnace gas is treated by the desulfurizing tower and then is transmitted to each user through a blast furnace gas pipe network.
Example 5
The process of the high-efficiency blast furnace gas dechlorination and desulfurization system based on the embodiment comprises the following steps:
step S101: after the blast furnace gas is dedusted by the gravity deduster and the electric deduster, the dust content is not more than 10mg/Nm 3 And then is transmitted to a blast furnace gas dechlorinating tower;
step S102: the dechlorinated blast furnace gas passes through a pressure regulating valve bank or a residual pressure turbine power generation device and then enters a blast furnace gas catalytic tower, and a spherical catalyst is arranged in the blast furnace gas catalytic tower; the particle size of the spherical catalyst is 4 microns, and the reaction temperature is 110-250 ℃; the spherical catalyst is an alumina-based Fe catalyst; 0.5 wt% of cobalt naphthanate is loaded on the catalyst carrier; the space velocity of the spherical catalyst is 8000h -1 The COS in the blast furnace gas is catalytically converted into H 2 S, conversion reaction process: COS + H 2 O＝H 2 S+CO 2 Converting COS in the blast furnace gas;
step S103: the blast furnace gas treated by the blast furnace gas catalytic tower enters a blast furnace gas desulfurization tower;
step S104: a spray gun is arranged in the blast furnace gas desulfurization tower, alkaline water with the pH value of 10.5 is sprayed on the blast furnace gas, and H in the blast furnace gas is sprayed 2 S and Cl - Carrying out desulfurization and dechlorination treatment, wherein the reaction comprises the following steps: 2NaOH + H 2 S＝Na 2 S+2H 2 O，NaOH+HCl＝NaCl+H 2 And O, the blast furnace gas is treated by the desulfurizing tower and then is transmitted to each user through a blast furnace gas pipe network.
Example 6
The process of the high-efficiency blast furnace gas dechlorination and desulfurization system based on the embodiment comprises the following steps:
step S101: blast furnace gas weightAfter dust is removed by a force dust remover and a bag-type dust remover, the dust content is not more than 10mg/Nm 3 And then is transmitted to a blast furnace gas dechlorinating tower;
step S102: the dechlorinated blast furnace gas passes through a pressure regulating valve bank or a residual pressure turbine power generation device and then enters a blast furnace gas catalytic tower, and a spherical catalyst is arranged in the blast furnace gas catalytic tower; the particle size of the spherical catalyst is 10 microns, and the reaction temperature is 180 ℃; the spherical catalyst is a titanium oxide-based sodium catalyst; 0.4 wt% of molybdenum naphthoate is loaded on the catalyst carrier; the space velocity of the spherical catalyst is 5000h -1 The COS in the blast furnace gas is catalytically converted into H 2 S, conversion reaction process: COS + H 2 O＝H 2 S+CO 2 Converting COS in the blast furnace gas;
step S103: the blast furnace gas treated by the blast furnace gas catalytic tower enters a blast furnace gas desulfurization tower;
step S104: a spray gun is arranged in the blast furnace gas desulfurization tower, alkaline water with the pH value of 11.8 is sprayed on the blast furnace gas, and H in the blast furnace gas is sprayed 2 S and Cl - Carrying out desulfurization and dechlorination treatment, wherein the reaction comprises the following steps: 2NaOH + H 2 S＝Na 2 S+2H 2 O，NaOH+HCl＝NaCl+H 2 And O, the blast furnace gas is treated by the desulfurizing tower and then is transmitted to each user through a blast furnace gas pipe network.
It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments, and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. Any reference sign in a claim should not be construed as limiting the claim concerned.
Claims (10)
1. A high-efficiency blast furnace gas dechlorination and desulfurization system comprises; (a) at least one stage of a gravity precipitator (100) capable of removing large particles from blast furnace gas; (b) at least one stage of bag-type dust collector (200)/electric dust collector which can remove tiny particles in blast furnace gas; (c) at least one blast furnace gas dechlorination tower (300); (d) at least one stage of a blast furnace gas catalytic tower (400); and (f) at least one desulfurization tower (700); a blast furnace TRT (500) and a pressure regulating valve bank (600) are arranged between the blast furnace gas dechlorination tower (300) and the blast furnace gas catalytic tower (400) in parallel; characterized in that the blast furnace gas catalytic tower (400) comprises a tower body (410) internally carrying a catalyst; the feeding component (420) is used for adding the spherical catalyst into the tower body (410), the feeding component (420) is provided with a feeding cavity (421) which is communicated with the tower body (410), the feeding cavity (421) is provided with a control valve (422) which can isolate the air environment from the feeding cavity (421), so that the drag loss is controlled below 1.5kPa, and the outlet pressure of the blast furnace gas catalytic tower (400) is 160-165 kPa.
2. The high-efficiency blast furnace gas dechlorination and desulfurization system according to claim 1, wherein the particle size of the spherical catalyst is 4-10 μm, and the reaction temperature is 110-250 ℃; the spherical catalyst is an alumina-based alkali metal/alkaline earth metal/transition metal catalyst or a titania-based alkali metal/alkaline earth metal/transition metal catalyst; 0.2-0.5 wt% of naphthoate is loaded on the catalyst carrier, wherein the naphthoate is one or more of nickel, cobalt and molybdenum salts.
3. The high-efficiency blast furnace gas dechlorination and desulfurization system according to claim 2, characterized in that the charging member (420) has at least a first charging chamber and a second charging chamber (4215) arranged longitudinally, the first charging chamber (4211) is provided with a first control valve (4221), and the second charging chamber (4215) is provided with a second control valve (4222).
4. The high-efficiency blast furnace gas dechlorination and desulfurization system according to claim 3, characterized in that the first charging chamber (4211) and the second charging chamber (4215) have the same structural shape, the first charging chamber (4211) is in the shape of an inverted cone, and the lower end of the first charging chamber is provided with a discharge hole (4212); the first control valve (4221) is arranged on one side of the discharge hole (4212).
5. The high-efficiency blast furnace gas dechlorination and desulfurization system according to claim 4, characterized in that the first charging chamber (4211) is provided with a vacuum gas pump (4213), and the vacuum gas pump (4213) is connected to the first charging chamber (4211) through a pipe.
6. The high-efficiency blast furnace gas dechlorination and desulfurization system according to claim 5, characterized in that the first charging chamber (4211) is provided with a vacuum pressure display (4214).
7. The high-efficiency blast furnace gas dechlorination and desulfurization system according to claim 1, wherein the charging component (420) has an elongated charging chamber (421), and two control valves (422) are longitudinally arranged on the charging chamber (421) to divide the charging chamber (421) into at least two spaces.
8. The high efficiency blast furnace gas dechlorination and desulfurization system according to claim 7, characterized in that the cross-sectional shape of the charging chamber (421) is circular, oval, square, triangular, pentagonal or hexagonal.
9. The high-efficiency blast furnace gas dechlorination and desulfurization system according to any one of claims 1 to 8, characterized by comprising a primary rough desulfurization tower and a secondary fine desulfurization tower connected in series with the primary rough desulfurization tower, wherein the primary desulfurization tower (700) is communicated with the top of the secondary fine desulfurization tower through an inter-tower connecting pipeline; a plurality of rows of spray guns are arranged at the upper part in the primary rough removal tower, and alkali-containing water for desulfurization and dechlorination is sprayed; the upper part in the secondary fine threshing tower is provided with a plurality of spray guns and a diversion cone; the bottom of the primary blast furnace gas rough stripping tower enters, alkali-containing water sprayed by the spray gun is subjected to desulfurization treatment, then enters from the upper part of the secondary fine stripping tower through an inter-tower connecting pipeline, is subjected to secondary desulfurization treatment, and then passes through the flow guide cone and is output from the blast furnace gas outlet at the top of the secondary fine stripping tower.
10. The process of the high-efficiency blast furnace gas dechlorination and desulfurization system based on the claims 1 to 9, which is characterized by comprising the following steps of:
step S101: after the blast furnace gas is dedusted by the gravity deduster (100), the bag-type deduster (200)/the electric deduster, the dust content is not more than 10mg/Nm 3 And is conveyed to a blast furnace gas dechlorination tower (300);
step S102: the dechlorinated blast furnace gas passes through a pressure regulating valve bank (600) or a residual pressure turbine power generation device and then enters a blast furnace gas catalytic tower (400), and a spherical catalyst is arranged in the blast furnace gas catalytic tower (400); the particle size of the spherical catalyst is 4-10 microns, and the reaction temperature is 110-250 ℃; the spherical catalyst is an alumina-based alkali metal/alkaline earth metal/transition metal catalyst or a titania-based alkali metal/alkaline earth metal/transition metal catalyst; 0.2-0.5 wt% of naphthoate is loaded on the catalyst carrier; the space velocity of the spherical catalyst is 0-10000h -1 The COS in the blast furnace gas is catalytically converted into H 2 S, conversion reaction process: COS + H 2 O＝H 2 S+CO 2 Converting COS in the blast furnace gas;
step S103: the blast furnace gas treated by the blast furnace gas catalytic tower (400) enters a blast furnace gas desulfurization tower (700);
step S104: a spray gun is arranged in the blast furnace gas desulfurization tower (700), alkali-containing water with the pH value of 9.8-11.8 is sprayed on the blast furnace gas, and H in the blast furnace gas is treated 2 S and Cl are subjected to desulfurization and dechlorination treatment, and the reaction is as follows: 2NaOH + H 2 S＝Na 2 S+2H 2 O，NaOH+HCl＝NaCl+H 2 And O, the blast furnace gas is treated by the desulfurizing tower (700) and then is transmitted to each user through a blast furnace gas pipe network.
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