CN110002411A - A kind of acid regeneration equipment and technique - Google Patents
A kind of acid regeneration equipment and technique Download PDFInfo
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- CN110002411A CN110002411A CN201910355615.9A CN201910355615A CN110002411A CN 110002411 A CN110002411 A CN 110002411A CN 201910355615 A CN201910355615 A CN 201910355615A CN 110002411 A CN110002411 A CN 110002411A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8603—Removing sulfur compounds
- B01D53/8609—Sulfur oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
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- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/90—Separation; Purification
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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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- Y02P20/50—Improvements relating to the production of bulk chemicals
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Abstract
The present invention provides a kind of acid regeneration equipment, including passing through the sequentially connected incinerator of pipeline, filter, first-stage reactor, first-stage condenser, second reactor, secondary condenser and activated carbon reactor, wherein, the incinerator is for raw material to be pyrolyzed, light pipe heat exchanger is additionally provided with inside the incinerator at gas outlet, the light pipe heat exchanger cools down the high-temperature gas after burning in the incinerator；The process gas that the incinerator is discharged the filter filters；Then sulfuric acid, remaining SO in the process gas that the secondary condenser is discharged the activated carbon reactor are reacted and are condensed into first-stage reactor, first-stage condenser, second reactor, secondary condenser2Gas oxidation, tail gas are discharged by chimney.In addition, the present invention also provides the techniques for using above-mentioned acid regeneration equipment to carry out acid regeneration.Above-mentioned acid regeneration equipment and its total sulphur recovery efficiency of technique are high, low energy consumption for long-term operation, installation area is small, environmental protection index is high.
Description
Technical field
The invention belongs to waste acidity recovery technical fields, and in particular to a kind of acid regeneration equipment and technique.
Background technique
Use there are two types of more waste Acid Recovery Process at present: one is " dry method ", and one is " wet processes "." dry method " work
Skill process is longer, land occupation is big, has a small amount of discharge of wastewater；" wet process " technique, with process is short, takes up little area, non-wastewater discharge, energy consumption
Low advantage, but it is difficult to realize the preparation of high-concentration sulfuric acid.
Summary of the invention
Technical problem to be solved by the invention is to provide a kind of acid regeneration equipment and technique, so as to be suitable for
Alkyl plant Waste Sulfuric Acid is raw material, is handled using the chemical process that burning cracking+reaction converts+is condensed into acid.Using
Advanced low nitrogen incinerator, by first-stage reactor+first-stage condenser+second reactor+secondary condenser (two turn two is solidifying), instead
Proprietary efficient honeycomb platinum catalyst and common catalytic component based on vanadium should be used, is filled at acid system using proprietary glass pipework condensation
It sets, obtains high-concentration sulfuric acid product, vent gas treatment uses proprietary activated-carbon catalyst catalyzed conversion, and final exhaust emissions meets
SO2≤50mg/m3、NOx≤50mg/m3, acid mist≤5mg/m3(being based on 3% oxygen content).The surplus heat of device generates setting steam
Generating system generates steam.
To achieve the goals above, the technical solution used in the present invention is: a kind of acid regeneration equipment, including pass through pipe
The sequentially connected incinerator in road, filter, first-stage reactor, first-stage condenser, second reactor, secondary condenser and active carbon
Reactor,
Wherein, the incinerator is additionally provided with light pipe at gas outlet inside the incinerator and changes for raw material to be pyrolyzed
Hot device, the light pipe heat exchanger cool down the high-temperature gas after burning in the incinerator；
The process gas that the incinerator is discharged the filter filters；
The filtered process gas of the filter is carried out catalytic oxidation by the first-stage reactor；
Process gas after the first-stage reactor catalysis oxidation is converted to sulfuric acid and condenses concentration by the first-stage condenser；
The second reactor receives the process gas of the first-stage condenser discharge, and carries out catalytic oxidation again；
Process gas after the second reactor catalysis oxidation is converted to sulfuric acid and condenses concentration by the secondary condenser；
Remaining SO in the process gas that the secondary condenser is discharged the activated carbon reactor2Gas oxidation, tail gas
It is discharged by chimney.
Above-mentioned acid regeneration equipment provided by the invention can be alkyl plant Waste Sulfuric Acid by incinerator cracking, mistake
Filter, first-stage reactor, first-stage condenser, second reactor, secondary condenser, activated carbon reactor processing, obtain high concentration sulphur
Acid.
Based on the above technical solution, the present invention can also have following further specific choice or optimum choice.
Specifically, the filter is ceramic fiber filter.Pipe between the filter and the first-stage reactor
Road is additionally provided with finned heat exchanger and blower, and the finned heat exchanger will cool down by the process gas of the filter, passes through institute
It states blower and the process gas after cooling is delivered to the first reactor.
Specifically, the first-stage reactor is vertically arranged, top is equipped with air inlet and bottom end is equipped with gas outlet, inner cavity
It is set from top to bottom there are four catalytic bed, the catalytic bed is respectively provided with a honeycomb platinum catalyst and three bulk cargos from top to bottom
Vanadium catalyst catalyst, wherein finned tube heat exchange is additionally provided with below each catalytic bed equipped with bulk cargo vanadium catalyst catalyst
Device.
Specifically, the first-stage condenser and secondary condenser are vertically arranged, top is equipped with gas outlet and lower part
Side wall is equipped with air inlet, and inner cavity is successively arranged electrostatic precipitator and at least one glass heat exchange of heat pipe from top to bottom, described cold
Condenser bottom is equipped with the outlet of condensation acid.Specifically, the glass heat exchange of heat pipe is horizontal.Preferably, the glass heat exchange of heat pipe
It is three.
Specifically, the second reactor is vertically arranged, top is equipped with air inlet and bottom end is equipped with gas outlet, inner cavity
Catalytic bed there are three setting from top to bottom, three catalytic beds are respectively provided with SCR denitration from top to bottom, honeycomb platinum is urged
Agent and bulk cargo vanadium catalyst catalyst, wherein be additionally provided at least one above the catalytic bed equipped with SCR denitration
Finned tube exchanger is additionally provided with the heat exchange of at least one finned tube below the catalytic bed equipped with bulk cargo vanadium catalyst catalyst
Device.
Specifically, further including fused salt tank and steam generator, the fused salt outlet of the fused salt tank is changed with the light pipe respectively
Hot device is connected to the fused salt entrance of finned tube exchanger, and the outlet of the fused salt of the light pipe heat exchanger and finned tube exchanger and steaming
The fused salt entrance of vapour generator is connected to, and the fused salt outlet of the steam generator is connected to the fused salt entrance of the fused salt tank.Tool
Body, heat exchange substance is fused salt in light pipe heat exchanger and finned tube exchanger.
Specifically, the gas outlet of the incinerator is connected to the air inlet of the filter, the gas outlet of the filter
It is connected to the air inlet of the first-stage reactor (between the gas outlet of the filter and the air inlet of the first-stage reactor also
Optionally it is equipped with finned heat exchanger), the gas outlet of the first-stage reactor is connected to the air inlet of the first-stage condenser, described
The gas outlet of first-stage condenser preheats in glass heat exchange of heat pipe and is connected to the air inlet of the second reactor, and the second level is anti-
The gas outlet of device and the air inlet of the secondary condenser is answered to be connected to, the gas outlet of the secondary condenser and the active carbon are anti-
The air inlet of device is answered to be connected to, the gas outlet of the activated carbon reactor is directly connect with chimney.
In addition, the present invention also provides the techniques for using above-mentioned acid regeneration equipment to carry out acid regeneration comprising as follows
Step:
1) raw material is passed through in the incinerator；
2) gas exported after burning in the incinerator is filtered in the filter；
3) the filtered process gas of the filter is carried out catalytic oxidation by the first-stage reactor, enables SO2Conversion
SO3Conversion ratio is not less than 95%；
4) process gas after first-stage reactor catalysis is converted to sulfuric acid and in gravity by the first-stage condenser
Lower condensation concentration；
5) process gas that the first-stage condenser is discharged the second reactor carries out catalytic oxidation, enables SO2Turn
Change SO3Conversion ratio is not less than 98%；
6) process gas after second reactor catalysis is converted to sulfuric acid and in gravity by the secondary condenser
Lower condensation concentration；
7) process gas after the secondary condenser passes through activated carbon reactor, remaining SO2It is oxidized, clean gas
Body is eventually by smoke stack emission into atmosphere.
Based on the above technical solution, the present invention can also have following further specific choice or optimum choice.
Specifically, it is 1000 that the feeding amount in step 1) by combustion air, which controls and adjusts the burning in-furnace temperature,
DEG C, the process gas of the incinerator gas outlet controls under the action of the light pipe heat exchanger at 500 DEG C.
Specifically, positive pressure is kept in step 3) in the first-stage reactor, and its gas outlet temperature be 295 DEG C with
Under.
Specifically, temperature of the process gas in the first-stage condenser and secondary condenser exit is 75 DEG C or less.
Specifically, from the process gas being discharged in the first-stage condenser described one before entering the second reactor
250 DEG C or more are preheated in the glass heat exchange of heat pipe of grade condenser.Specifically, the tube side of the glass heat exchange of heat pipe is usually used
As refrigerant, shell side is used to cool down the process gas in the condenser surrounding air, utilizes original herein in order to carry out energy conservation
Then, heat exchange is carried out using the process gas being discharged in the first-stage condenser as process gas internal in refrigerant and first-stage condenser
To achieve the purpose that heat the process gas being discharged in first-stage condenser.Preferably, it is discharged in the first-stage condenser
Process gas preheated in first-stage condenser the lowermost glass heat exchange of heat pipe before entering the second reactor.
It should be noted that the raw material of above-mentioned technique is alkyl plant spent acid, spent acid is pyrolyzed by incinerator, described to help
Combustion air takes surrounding air, and surrounding air is preheated to about 400 DEG C by heat exchanger, and incinerator pressure remains micro- negative by blower
Pressure, filter filtering remove the impurity in process gas.Between the catalyst bed of the first-stage reactor equipped with finned heat exchanger to
Interlayer cooling and extraction reaction heat.Acid is condensed in glass tube heat exchanger shell pass in the first-stage condenser and secondary condenser
From flowing in sour tank, process gas temperature is cooled to 75 DEG C, and the not condensed acid mist to get off will be removed in the electrostatic in process gas
It is removed in day with fog.The catalyst bed either above or below of the second reactor equipped with finned heat exchanger to heating process gas and
Extract reaction heat.
Compared with prior art, the beneficial effects of the present invention are:
1) total sulphur recovery efficiency is high: wet process acid regeneration technique provided by the invention takes the lead in realizing two turn of two solidifying technique, adopts
With the comprehensive low nitrogen incinerator of advanced more media, the glass pipework condensation of proprietary efficient molding porous oxidation catalyst and patent
Device, total sulfur recovery are more than 99.9%.
2) low energy consumption for long-term operation: by using proprietary high-temperature ceramic fibre filter, flue gas cool-down being avoided to heat up again
Caused by energy consumption, while use efficient finned tube heat-exchange system, more than the oxidation heat liberation, hydration heat, burning generated in system
Heat is recycled, by-product high-quality steam.
3) installation area is small: being accounted for using efficient conversion, condensation and heat recovery apparatus, system compact and reasonable arrangement
Ground area is small.
4) environmental protection index is high: controlling acid mist to less than 5mg/Nm using the efficient wet electrostatic precipitator of patent3；Using peculiar
Activated carbon catalysis oxidation technology processing tail gas in SO2, make SO2Discharge is less than 50mg/Nm3, while it is useless not generate any waste water
Liquid；Using low nitrogen burning and SCR technique, NOx emission is made to be less than 50mg/Nm3；Made using ceramic high temperature filter granular material discharged
Less than 5mg/Nm3(the above index is butt, converts as 3%v oxygen content).In summary discharge index meets country to flue gas
The requirement of ultra-clean discharge.
Detailed description of the invention
Fig. 1 is a kind of acid regeneration device structure schematic diagram and material flow figure of offer of the invention；
Fig. 2 is a kind of acid regeneration device structure schematic diagram and fused salt heat exchanging piping arrangement of offer of the invention.
In attached drawing, parts list represented by the reference numerals are as follows:
1, incinerator；2, filter；3, first-stage reactor；4, first-stage condenser；5, second reactor；6, B-grade condensation
Device；7, activated carbon reactor；8, fused salt tank；9, steam generator；11, light pipe heat exchanger.
Specific embodiment
For a better understanding of the present invention, with reference to the accompanying drawing and the specific embodiment content that the present invention is furture elucidated,
But the contents of the present invention are not limited solely to the following examples.
The present invention provides a kind of acid regeneration equipment, including pass through the sequentially connected incinerator 1 of pipeline, filter 2, one
Stage reactor 3, first-stage condenser 4, second reactor 5, secondary condenser 6 and activated carbon reactor 7,
Wherein, for the incinerator 1 for raw material to be pyrolyzed, 1 inside of incinerator is additionally provided with light pipe at gas outlet
Heat exchanger 11, the light pipe heat exchanger 11 cool down the high-temperature gas after burning in the incinerator 1；
The process gas that the incinerator 1 is discharged the filter 2 filters；
The filtered process gas of the filter 2 is carried out catalytic oxidation by the first-stage reactor 3；
Process gas after 3 catalysis oxidation of first-stage reactor is converted to sulfuric acid and condensed dense by the first-stage condenser 4
Contracting；
The second reactor 5 receives the process gas that the first-stage condenser 4 is discharged, and it is anti-to carry out catalysis oxidation again
It answers；
Process gas after 5 catalysis oxidation of second reactor is converted to sulfuric acid and condensed dense by the secondary condenser 6
Contracting；
Remaining SO in the process gas that the secondary condenser is discharged the activated carbon reactor 72Gas oxidation, tail gas
It is discharged by chimney.
Above-mentioned acid regeneration equipment provided by the invention can be alkyl plant Waste Sulfuric Acid by the cracking of incinerator 1, mistake
Filter 2, first-stage reactor 3, first-stage condenser 4, second reactor 5, secondary condenser 6, the processing of activated carbon reactor 7, obtain
High-concentration sulfuric acid.
Based on the above technical solution, the present invention can also have following further specific choice or optimum choice.
Specifically, the filter 2 is ceramic fiber filter.Between the filter 2 and the first-stage reactor 3
Finned heat exchanger and blower are additionally provided on pipeline, the finned heat exchanger will cool down by the process gas of the filter 2, pass through
Technique pneumatic transmission after blower contribute cooling is to the first reactor 3.
Specifically, the first-stage reactor 3 is vertically arranged, top is equipped with air inlet and bottom end is equipped with gas outlet, in
Chamber is set from top to bottom there are four catalytic bed, and the catalytic bed is respectively provided with a honeycomb platinum catalyst from top to bottom and three dissipate
Expect vanadium catalyst catalyst, wherein be additionally provided with finned tube below each catalytic bed equipped with bulk cargo vanadium catalyst catalyst and change
Hot device.
Specifically, the first-stage condenser 4 and secondary condenser 6 are vertically arranged, top be equipped with gas outlet and under
Portion's side wall is equipped with air inlet, and inner cavity is successively arranged electrostatic precipitator and at least one glass heat exchange of heat pipe from top to bottom, described
Condenser bottom is equipped with the outlet of condensation acid.Specifically, the glass heat exchange of heat pipe is horizontal.Preferably, the glass tube heat exchange
Device is three.
Specifically, the second reactor 5 is vertically arranged, top is equipped with air inlet and bottom end is equipped with gas outlet, in
Chamber is set from top to bottom there are three catalytic bed, and three catalytic beds are respectively provided with SCR denitration, honeycomb platinum from top to bottom
Catalyst and bulk cargo vanadium catalyst catalyst, wherein be additionally provided at least one above the catalytic bed equipped with SCR denitration
A finned tube exchanger is additionally provided with the heat exchange of at least one finned tube below the catalytic bed equipped with bulk cargo vanadium catalyst catalyst
Device.
Specifically, further include fused salt tank 8 and steam generator 9, the fused salt outlet of the fused salt tank respectively with the light pipe
Heat exchanger 11 is connected to the fused salt entrance of finned tube exchanger, and the fused salt of the light pipe heat exchanger 11 and finned tube exchanger goes out
Mouth is connected to the fused salt entrance of steam generator 9, and the fused salt outlet of the steam generator 9 and the fused salt of the fused salt tank 8 enter
Mouth connection.Specifically, heat exchange substance is fused salt in light pipe heat exchanger 11 and finned tube exchanger.
Specifically, the gas outlet of the incinerator 1 is connected to the air inlet of the filter 2, the outlet of the filter 2
Mouth is connected to the (air inlet of the gas outlet of the filter 2 and the first-stage reactor 3 with the air inlet of the first-stage reactor 3
Between also optionally be equipped with finned heat exchanger), the air inlet of the gas outlet of the first-stage reactor 3 and the first-stage condenser 4
Connection, the gas outlet of the first-stage condenser 4 preheats in glass heat exchange of heat pipe to be connected with the air inlet of the second reactor 5
Logical, the gas outlet of the second reactor 5 is connected to the air inlet 6 of the secondary condenser, the outlet of the secondary condenser
Mouth is connected to the air inlet of the activated carbon reactor 7, and the gas outlet of the activated carbon reactor is directly connect with chimney.
In addition, the present invention also provides the techniques for using above-mentioned acid regeneration equipment to carry out acid regeneration comprising as follows
Step:
1) raw material is passed through in the incinerator 1；
2) gas exported after burning in the incinerator 1 is filtered in the filter 2；
3) the filtered process gas of the filter 2 is carried out catalytic oxidation by the first-stage reactor 3, enables SO2Turn
Change SO3Conversion ratio is not less than 95%；
4) process gas after the first-stage reactor 3 catalysis is converted to sulfuric acid and made in gravity by the first-stage condenser 4
It is concentrated with lower condensation；
5) process gas that the first-stage condenser 4 is discharged the second reactor 5 carries out catalytic oxidation, enables SO2
Convert SO3Conversion ratio is not less than 98%；
6) process gas after the second reactor 5 catalysis is converted to sulfuric acid and made in gravity by the secondary condenser 6
It is concentrated with lower condensation；
7) process gas after the secondary condenser 6 passes through activated carbon reactor 7, remaining SO2It is oxidized, clean
Gas is eventually by smoke stack emission into atmosphere.
Based on the above technical solution, the present invention can also have following further specific choice or optimum choice.
Specifically, it is 1000 that the feeding amount in step 1) by combustion air, which controls and adjusts temperature in the incinerator 1,
DEG C, the process gas of 1 gas outlet of incinerator controls under the action of light pipe heat exchanger 11 at 500 DEG C or less.
Specifically, positive pressure is kept in step 3) in the first-stage reactor 3, and its gas outlet temperature is 295 DEG C
Below.
Specifically, temperature of the process gas in 6 exit of the first-stage condenser 4 and secondary condenser is 75 DEG C or less.
Specifically, from the process gas being discharged in the first-stage condenser 4 described before entering the second reactor 5
250 DEG C or more are preheated in the glass heat exchange of heat pipe of first-stage condenser 4.
It should be noted that the raw material of above-mentioned technique is alkyl plant spent acid, spent acid is pyrolyzed by incinerator 1, described
Combustion air takes surrounding air, and surrounding air is preheated to about 400 DEG C by heat exchanger, and incinerator pressure remains micro- negative by blower
Pressure, the filtering of filter 2 remove the impurity in process gas.It is used between the catalyst bed of the first-stage reactor 3 equipped with finned heat exchanger
With interlayer cooling and extract reaction heat.Acid is in glass tube heat exchanger shell pass quilt in the first-stage condenser 4 and secondary condenser 6
Condensation is from flowing in sour tank, and process gas temperature is cooled to 75 DEG C, and the not condensed acid mist to get off will be described quiet in process gas
It is removed in electrostatic precipitator.The catalyst bed either above or below of the second reactor 6 is equipped with finned heat exchanger to heater
Skill gas and extraction reaction heat.
Embodiment:
Unit scale is 1.6 ten thousand tons/year, and raw material is alkyl plant spent acid 2095kg/h, and spent acid is by 1 warm of incinerator
Solution, burning room temperature are 1000 DEG C, and pressure is -0.1KPa (g), and combustion air is heated to 252 DEG C by glass heat exchange of heat pipe,
It is sent by blower to finned tube exchanger and continues to be heated to 400 DEG C, process gas takes heat drop temperature by light pipe heat exchanger 11 after burning
To 495 DEG C；The filtering removal impurity of high-temperature ceramic fibre filter 2 is subsequently entered, process gas is dropped through finned tube exchanger after filtering
Temperature is sent into first-stage reactor 3 to 440 DEG C, by blower；First-stage reactor 3 inlet pressure 2KPa (g), outlet pressure -0.1KPa
(g), 295 DEG C of outlet temperature, SO in first-stage reactor 32Convert SO3Conversion ratio is 95%.3 outlet process gas of first-stage reactor into
Entering in first-stage condenser 4, process gas is successively cooled to 255 DEG C, 130 DEG C, 75 DEG C through glass tube heat exchanger shell pass from bottom to top,
1847kg/h high-concentration sulfuric acid is condensed in glass tube heat exchanger shell pass from flowing in sour tank, not condensed in process gas to get off
Acid mist removes in electrostatic precipitator, and process gas enters in glass heat exchange of heat pipe by blower is preheated to 250 DEG C, enters back into second level
Reactor 5；Second reactor 5 inlet pressure 0.4KPa (g), outlet pressure -1.6KPa (g), the process gas in second reactor
300 DEG C, 392 DEG C are successively heated to through finned tube exchanger, after through SCR denitration, catalytic conversion reaction, remaining SO2Turned
Turn to SO3, SO in second reactor 52Convert SO3Conversion ratio is 99%, and 5 outlet temperature of second reactor is 295 DEG C.Second level is anti-
5 outlet process gas of device is answered to enter secondary condenser 6, process gas is successively cooled to 125 through glass tube heat exchanger shell pass from bottom to top
DEG C, 100 DEG C, 75 DEG C, 96kg/h high-concentration sulfuric acid is condensed in glass tube heat exchanger shell pass from flowing in sour tank, in process gas not
The acid mist being condensed removes in electrostatic precipitator, and process gas that treated is sent to activated carbon reactor by blower
In.The temperature of activated carbon reactor is 42 DEG C, and pressure is 1.6KPa (g), and process gas slow transits through active-carbon bed, remaining SO2
It is finally collected on the surface in the micropore of charcoal and is oxidized, form diluted acid after washing, diluted acid is sent to incinerator and cold
Condenser continues to recycle, and clean gas is eventually by smoke stack emission into atmosphere.
The thermally conductive salt of finned tube exchanger tube side comes from fused salt tank 8, controls temperature of reactor using thermally conductive salt heat-exchange system,
The reaction heat of recycling generates 1100KPa (g) by steam generator 9,230 DEG C of high-quality steams.
Reached using the sulfuric acid product index that the present embodiment produces:
The foregoing is merely presently preferred embodiments of the present invention, is not intended to limit the invention, it is all in spirit of the invention and
Within principle, any modification, equivalent replacement, improvement and so on be should all be included in the protection scope of the present invention.
Claims (10)
1. a kind of acid regeneration equipment, which is characterized in that including by the sequentially connected incinerator of pipeline (1), filter (2),
First-stage reactor (3), first-stage condenser (4), second reactor (5), secondary condenser (6) and activated carbon reactor (7),
Wherein, for the incinerator (1) for raw material to be pyrolyzed, the incinerator (1) is internal to be additionally provided with light pipe at gas outlet
Heat exchanger (11), the light pipe heat exchanger (11) cool down the high-temperature gas after burning in the incinerator (1)；
The process gas that the incinerator (1) is discharged the filter (2) filters；
The filtered process gas of the filter (2) is carried out catalytic oxidation by the first-stage reactor (3)；
Process gas after the first-stage reactor (3) catalysis oxidation is converted to sulfuric acid and condensed dense by the first-stage condenser (4)
Contracting；
The second reactor (5) receives the process gas of first-stage condenser (4) discharge, and it is anti-to carry out catalysis oxidation again
It answers；
Process gas after the second reactor (5) catalysis oxidation is converted to sulfuric acid and condensed dense by the secondary condenser (6)
Contracting；
Remaining SO in the process gas that the secondary condenser is discharged the activated carbon reactor (7)2Gas oxidation, tail gas are logical
Cross chimney discharge.
2. a kind of acid regeneration equipment according to claim 1, it is characterised in that: the filter (2) and the level-one
Finned heat exchanger and blower are additionally provided on pipeline between reactor (3), the finned heat exchanger will pass through the filter (2)
Process gas cooling, the process gas after cooling is delivered to the first reactor (3) by the blower.
3. a kind of acid regeneration equipment stated according to claim 2, it is characterised in that: the first-stage reactor (3) is vertically arranged,
Its top is equipped with air inlet and bottom end and is equipped with gas outlet, and inner cavity is set from top to bottom there are four catalytic bed, and the catalytic bed is from upper
A honeycomb platinum catalyst and three bulk cargo vanadium catalyst catalyst are respectively provided under and, wherein touch equipped with bulk cargo vanadium each
Finned tube exchanger is additionally provided with below the catalytic bed of matchmaker's catalyst.
4. a kind of acid regeneration equipment according to claim 3, it is characterised in that: the second reactor (5) sets vertically
It sets, top is equipped with air inlet and bottom end and is equipped with gas outlet, and inner cavity sets that there are three catalytic bed, three catalysis from top to bottom
Bed is respectively provided with SCR denitration, honeycomb platinum catalyst and bulk cargo vanadium catalyst catalyst from top to bottom, wherein is being equipped with
It is additionally provided at least one finned tube exchanger above the catalytic bed of SCR denitration, is catalyzed equipped with bulk cargo vanadium catalyst
At least one finned tube exchanger is additionally provided with below the catalytic bed of agent.
5. a kind of acid regeneration equipment according to claim 4, it is characterised in that: further include fused salt tank (8) and steam hair
The fused salt of raw device (9), the fused salt tank exports the fused salt entrance with the light pipe heat exchanger (11) and finned tube exchanger respectively
Connection, and the outlet of the fused salt of the light pipe heat exchanger (11) and finned tube exchanger and the fused salt entrance of steam generator (9) connect
Logical, the fused salt outlet of the steam generator (9) is connected to the fused salt entrance of the fused salt tank (8).
6. a kind of acid regeneration equipment according to any one of claims 1 to 5, it is characterised in that: the first-stage condenser
(4) it is vertically arranged with secondary condenser (6), top is equipped with gas outlet and lower sides are equipped with air inlet, and inner cavity is certainly
Electrostatic precipitator and at least one glass heat exchange of heat pipe are successively arranged under above, the condenser bottom is equipped with the outlet of condensation acid.
7. a kind of technique for being carried out acid regeneration using acid regeneration equipment described in any one of claims 1-6, feature are existed
In including the following steps:
1) raw material is passed through in the incinerator (1)；
2) gas exported after burning in the incinerator (1) is filtered in the filter (2)；
3) the filtered process gas of the filter (2) is carried out catalytic oxidation by the first-stage reactor (3), enables SO2Conversion
SO3Conversion ratio is not less than 95%；
4) process gas after the first-stage reactor (3) catalysis is converted to sulfuric acid and made in gravity by the first-stage condenser (4)
It is concentrated with lower condensation；
5) process gas that the first-stage condenser (4) is discharged the second reactor (5) carries out catalytic oxidation, enables SO2Turn
Change SO3Conversion ratio is not less than 98%；
6) process gas after the second reactor (5) catalysis is converted to sulfuric acid and made in gravity by the secondary condenser (6)
It is concentrated with lower condensation；
7) process gas after the secondary condenser (6) passes through activated carbon reactor (7), remaining SO2It is oxidized, clean
Gas is eventually by smoke stack emission into atmosphere.
8. acid regeneration technique according to claim 7, which is characterized in that in the first-stage reactor (3) in step 3)
Interior holding positive pressure, and its gas outlet temperature is 295 DEG C or less.
9. acid regeneration technique according to claim 7, which is characterized in that process gas in the first-stage condenser (4) and
The temperature in secondary condenser (6) exit is 75 DEG C or less.
10. acid regeneration technique according to claim 7, which is characterized in that from what is be discharged in the first-stage condenser (4)
Process gas is preheated to 250 DEG C or more in the first-stage condenser (4) before entering the second reactor (5).
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110624494A (en) * | 2019-10-31 | 2019-12-31 | 攀钢集团攀枝花钢铁研究院有限公司 | Gas-liquid reactor for improving titanium white waste acid concentration |
| CN110748895A (en) * | 2019-10-29 | 2020-02-04 | 中冶南方都市环保工程技术股份有限公司 | High-sulfur waste incineration treatment system and treatment method |
| CN117326533A (en) * | 2023-06-15 | 2024-01-02 | 广东宏瑞能源科技股份有限公司 | Method for preparing reagent-grade sulfuric acid by wet acid preparation process and system for producing multi-concentration high-grade sulfuric acid |
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| CN117326533A (en) * | 2023-06-15 | 2024-01-02 | 广东宏瑞能源科技股份有限公司 | Method for preparing reagent-grade sulfuric acid by wet acid preparation process and system for producing multi-concentration high-grade sulfuric acid |
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