CN110217760A - A kind of desulphurization waste liquid of coke oven gas relieving haperacidity preparation process - Google Patents
A kind of desulphurization waste liquid of coke oven gas relieving haperacidity preparation process Download PDFInfo
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- CN110217760A CN110217760A CN201910434387.4A CN201910434387A CN110217760A CN 110217760 A CN110217760 A CN 110217760A CN 201910434387 A CN201910434387 A CN 201910434387A CN 110217760 A CN110217760 A CN 110217760A
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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
- C01B17/76—Preparation by contact processes
- C01B17/765—Multi-stage SO3-conversion
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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
- C01B17/76—Preparation by contact processes
- C01B17/80—Apparatus
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
- C01C1/242—Preparation from ammonia and sulfuric acid or sulfur trioxide
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
- C01C1/245—Preparation from compounds containing nitrogen and sulfur
- C01C1/246—Preparation from compounds containing nitrogen and sulfur from sulfur-containing ammonium compounds
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/16—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being hot liquid or hot vapour, e.g. waste liquid, waste vapour
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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
- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention discloses a kind of desulphurization waste liquid of coke oven gas relieving haperacidity preparation processes, the technique include using desulphurization waste liquid of coke oven gas and sulphur foam as raw material, successively using drying process with atomizing, fluidized-bed roasting process, acid-scrubbing cleaning technique and double-absorption technique contact method relieving haperacidity production technology；The master device used in the desulfurization waste liquor acid-making process includes six units in total: feed material preparation units burn sulphur unit, clean unit, dry suction unit, conversion unit and tail gas treating unit.Secondary pollution waste material will not be generated using above-mentioned technique, need to be further processed, also there is the features such as low energy consumption, small to equipment corrosion using the technique.
Description
Technical field
The present invention relates to sulfuric acid production process technical fields, and in particular to a kind of desulphurization waste liquid of coke oven gas relieving haperacidity preparation work
Skill.
Background technique
Currently, can be generally divided into two classes with the technical solution that coke-oven plant's Recovered sulphur is waste industrial sulphuric acid:
One kind is that solid sulfur is made by modes such as filtering, filters pressing, molten sulphur in sulphur foam, and the method mature technology is reliable, for
Numerous coke-oven plants are used, but since in Recovered sulphur more or less production sulphur can be directly used as containing impurity such as ammonium salts
The raw material of acid can bring very detrimental effect to sulphuric acid process, while desulphurization system also needs to be discharged a large amount of waste liquid and needs
It further to handle.
Second class is to be configured to expect by the sulphur foam of sweetening process recycling and desulfurization waste liquor using whitewashing incineration method technique
Sulphur is carried out incineration oxidation under the high temperature conditions as fuel using coal gas while ammonium salt substance also can under the high temperature conditions by slurry
It decomposes, be oxidized to the furnace gas containing sulfur dioxide, then industrial sulphuric acid is made by the technical process such as purification, dry, conversion, absorption.
For this method in foreign countries using more, technique also comparative maturity is collectively referred to as FRC method technique together with wet desulphurization.The technique it is excellent
Point is to handle sulphur foam together with desulfurization waste liquor industrial sulphuric acid product is made, and does not need that liquid waste processing facility is arranged again, technique
Process is continuous, the degree of automation is higher, and the product sulfuric acid quality produced is preferable.The major defect of the technique first is that energy consumption is high,
The burning of slurry needs to consume a large amount of coal gas；Second is that heat utilization rate is low, it is mainly manifested in slurry a large amount of moisture and is burning
It burns vaporization in furnace and needs to absorb a large amount of heat, when using waste heat boiler recycling heat, since moisture content is high in furnace gas, is
Condensation condensation phenomenon is prevented, needs to control higher heat boiler outlet temperature (usually 350 DEG C of >), which steams
Vapour contains a large amount of sensible heat and latent heat, and needs to remove during flue gas cleaning, consumes two parts thermal energy more；Third is that high
The sulfur dioxide furnace gas corrosivity of warm, high water capacity is stronger, therefore incinerator and waste heat boiler will consider that just wanting special prevents
Corruption requires, and equipment manufacturing cost is higher；Fourth is that the large quantity of moisture contained in slurry is condensed again in purification process, cleaning procedure
Produce load it is very big, while generating a large amount of acid waste water, form pollution source.
If the solids crude sulphur amount that coke-oven plant's recycling generates is smaller, it is not enough to produce sulfuric acid and generates scale effect, then
It is contemplated that only building drying system and recycling thick sulphur powder, it is suitable for transport to be sent outside to gas washing in SA production factory raw directly as sulfuric acid
Raw material is produced to use.If the solids crude sulphur amount that coke-oven plant's recycling generates more just needs to consider to build high production efficiency, can reach
The desulphurization waste liquid of coke oven gas relieving haperacidity preparation process required to energy conservation and environmental protection.
Summary of the invention
It is an object of the present invention to overcome defect existing in the prior art, a kind of desulphurization waste liquid of coke oven gas system is provided
Sour preparation process, the technique include using desulphurization waste liquid of coke oven gas and sulphur foam as raw material, successively using drying process with atomizing,
The contact method relieving haperacidity production technology of fluidized-bed roasting process, acid-scrubbing cleaning technique and double-absorption technique；In the desulfurization waste liquor system
The master device used in sour technique includes six units in total: feed material preparation units burn sulphur unit, clean unit, dry suction list
Member, conversion unit and tail gas treating unit.
It in order to avoid repetitive operation, reduces operating cost and facilitates management, deactivate existing sulphur foamed filter, filters pressing etc. and set
It applies, preferred technical solution is, in the drying process with atomizing, desulphurization waste liquid of coke oven gas and sulphur foam are pre- in the raw material
Dilute sulphur foam in processing unit directly by desulfurization regeneration tower production is sent into filter and filter press, after sulphur foam is first filtered again
Carry out filters pressing.It both can be convenient operation in this way, reduced energy consumption, while dilute sulphur foam also compares aspect using pipeline, it will not
The problems such as generating line clogging.
The main purpose of desulphurization waste liquid of coke oven gas relieving haperacidity preparation process construction is all to handle coke oven gas desulfurization
The waste liquid that process generates, therefore the technological design of pretreatment of raw material process should meet the operation needs of desulfurizer comprehensively, do
To synchronous operation.Since the desulphurization waste liquid of coke oven gas relieving haperacidity preparation process project wastewater treatment capacity is big, the dry volume needed
It is very big, while for the ease of adjusting produce load at any time, facilitating operational administrative, reduction energy consumption and operating cost, by technique core
It calculates, the drying of sulphur foam and desulfurization waste liquor uses two system paired runnings.
Further preferred technical solution is, in the drying process with atomizing；
(1) the sulphur foam that will be generated in the sweetening process, directly with sulphur foam filter is pumped into, after filtering by sulphur
To solid about 20%~30% or so (according to mass balance) is contained, formation sulphur cream is put into sulphur cream storage tank to be stored Foam concentration, will
The master device of the clear liquid filtered out back to desulfurization waste liquor relieving haperacidity is interior to be recycled.The concentration rate of sulphur foam is according to desulphurization system
The requirement of balance and waste liquid amount require to automatically control.
(2) the sulphur cream in sulphur cream storage tank is pumped into spiral-flow type spray drying tower by screw rod again, by centrifugal atomizing
After device atomization, cocurrent enters in drying tower simultaneously with hot-air, and the sulphur foam after drying tower is atomization is changed with hot-air
Heat, solidification, drying are acted on by the cyclonic separation of drying tower, and granular thick sulphur of the major part after dry is collected into tower bottom,
By the cooling of cold wind spiral case, the automatic control of Pneumatic butterfly valve, enters and gather materials on belt feeder.
(3) tail gas of drying tower is sent into further purified treatment in tail gas washing tower by air-introduced machine.
(4) hot-air required for drying tower, is generated by fuel gas hot-blast stove.
(5) degree of drying for recycling the thick sulphur of powdery is controlled by adjusting exhaust temperature, is measured by exhaust temperature
Signal, the flow of feedback regulation feed pump.
(6) due to the thick sulphur of powdery have the characteristics that easily melt, the temperature of drying tower import hot-air be also required into
Row control.At 200 DEG C or so, temperature is controlled by adjusting the additional amount of hot wind producer gas for the temperature control of import hot-air
System, passes through the temperature measurement signal of import hot-air, the additional amount of feedback regulation coal gas
(7) feeding quantity of drying tower can also realize automatic control, pass through the level gauging signal of sulphur foam tank, feedback regulation
The motor inverter of screw pump.
(8) the drying tail gas after dedusting is made a gift to someone tail gas absorber by air-introduced machine, is vented after being handled with water cyclic absorption.
The ammonia and a small amount of sulphur that drying process volatilizes have been dissolved in washing water, and the supplement water for sweetening process can be recycled.
(9) operation for the ease of the maintenance of device in desulfurization waste liquor acid-making process without influencing coking agent set, dress
Solid sulfur storage warehouse is also provided in setting, in the maintenance of sulfuric acid preparation facilities, the thick sulphur of material unit production can be longer
It is temporally stored in sulfur warehouse, while outsourcing fraction solids sulphur may be implemented also to supplement the deficiency of raw materials for production, protect
Sulfuric acid preparation facilities is demonstrate,proved often in production run under higher load, yield is improved, increases economic benefit.
It is about 1.5m by estimating solid content in 20% desulfurization waste liquor and sulphur foam spray drying flow3/ h, hot-blast stove go out
It is 200 DEG C or so that mouthful hot wind, which enters spray drying tower inlet temperature, and spray drying tower goes out tower exhaust temperature at 90 DEG C or so, hot wind
Furnace consumes coke-oven coal tolerance about 350Nm3/ h, the hot blast rate of generation about 32000Nm3/h。
Further preferred technical solution is in addition, in the fluidized-bed roasting process, using the roaster burnt in sulphur unit,
By the thick sulphur of solid powder and granule shape, by gathering materials, belt feeder is made a gift to someone into roaster, is boiled together with the air that air-blaster is blown
Burning is risen, about 1100 DEG C of high temperature SO is generated2Furnace gas, temperature drops to 350 DEG C or so entrance after waste heat boiler recycles heat
Low temperature exhaust heat boiler further recycles heat, and temperature is reduced to about 220 DEG C or so and is transported to clean unit purification again.
Further preferred technical solution is in addition, the roaster being arranged in sulphur unit that burns uses pyrite fluosolid roaster
Structure maintains the stability and reliability of operation, in the roasting by the way that specific fixing layer is arranged as accumulation of heat and conduction material
It burns and is provided with two, three times air-supply structure on furnace, for the operation temperature of regulation and control roaster, while it is big to meet produce load
The requirement of range fluctuation.The thick sulphur charging belt of solid powder and granule shape adjusts control using frequency converter, measures waste heat pot using oxygen table
Remaining oxygen content in outlet of still furnace gas, the feeding quantity of feedback automatic adjustment roaster, under normal circumstances, the operation of roaster
Realize automation control.Coal gas burner, heating and driving for roaster are set.Coal is additionally provided on the roaster
Gas burner, peep hole, to observe and monitor the mode of operation and operating condition of roaster.In order to make full use of residual heat of reaction,
Cooling element is not provided in roaster, whole reaction thermal energy, which passes through furnace gas, to be brought into waste heat boiler and recycled, generated
Steam.Adequate operation temperature in roaster is by adjusting air quantity, control outlet furnace gas SO2The method of concentration is controlled.
It is calculated by material and heat balance, out the furnace gas normal control SO of roaster2Content is about 12.5%.
According to the operating parameter of factory's low-pressure steam pipe network, the pressure rating for designing low-pressure steam is 1.0Mpa, the present apparatus
Waste Heat Boiler Design pressure is 1.25Mpa, and can be automatically adjusted according to the parameter of steam pipe network.
Further preferred technical solution is in addition, the acid-scrubbing cleaning technique is using dynamic wave high energy scrubber and filler
Scrubbing tower is to high temperature SO2Furnace gas is washed, by about 220 DEG C exported by low temperature exhaust heat boiler of furnace in the clean unit
Gas is first fed into dynamic wave high energy scrubber, and spray people recycles diluted acid and after being well atomized, furnace gas SO2It is dilute with atomization
Sour close contact makes furnace gas SO by adiabatic evaporation2Humidification, cooling, cooling and primary wash purification, are efficiently washed by dynamic wave
Wash the wet furnace gas SO that device outlet excludes2Cooling cycle diluted acid after gas-liquid separation, into stuffing washing tower, with tower top spray
Counter current contacting, washing, purifying remove impurity and steam therein, and subsequently into acid mist is removed in electrostatic precipitator, it is single to send to dry suction
Member.
Using adiabatic evaporation, cooling, diluted acid recycles washing flow to dynamic wave scrubber, and the impurity such as ammonia salt in furnace gas pass through
Washing enters in circulation fluid, and a small amount of extra diluted acid is discharged in vent gas treatment slot, is jointly processed by with tail gas absorption liquid.
Scrubbing tower uses packed tower, tower slot integral structure, diluted acid circulation washing.The diluted acid of circulating-pump outlet passes through diluted acid
After plate heat exchanger is cooling, it is sent to tower top spray washing furnace gas.Extra diluted acid seals in washer circulating slot, keeps water flat
Weighing apparatus.Diluted acid plate heat exchanger uses circulating water.The a small amount of diluted acid string being discharged in electrostatic precipitator to scrubbing tower circulating slot.For
Prevent SO in purification process2Equal toxic and harmful gas leakage pollution environment, purification system use negative-pressure operation.To prevent negative pressure mistake
High, protection cleaning equipment and process pipe safety, are provided with Safety water seal on electrostatic precipitator outlet conduit.
Further preferred technical solution is in addition, the double-absorption technique uses slot → pump → acid cooler → tower → slot
Circulation technology, wherein dry inhale sour circulation absorption system using two kinds of acid circulations, drying tower uses 94%H2SO4Circulation, absorption tower
Using 98%H2SO4Circulation, three towers, three slot process, the absorption tower You Liangtai acid cooler and a drying tower acid cooler composition follow
The cooling dry suction unit of naphthenic acid；Future auto purification unit furnace gas, after supplementing suitable air, control enter conversion unit furnace
SO in gas2Content (controls when produce load is lower for 8.0~8.5% and is transformed into SO in mouthful furnace gas2Content is 8.5%) by bottom
Air inlet enters drying tower, is absorbed moisture content in furnace gas from 94% concentrated sulfuric acid that tower top sprays, use moisture content in tower air≤
0.1g/Nm3, the dry acid after absorbing moisture flows into dry tower acid circulating slot from tower bottom, with coming from the first absorption tower acid circulating pump
String acid-mixed be bonded to 94% concentration, sent by drying tower acid circulating pump to drying tower acid cooler and cooled down, concentrated acid after cooling into
Enter drying tower and carries out circulated sprinkling.
Gas from converter third section through the cooling of the Vth heat exchanger, enters the first suction after economizer recycles heat
Tower is received, then through absorbing the SO in furnace gas from 98% concentrated sulfuric acid that tower top sprays3, after absorption acid from tower bottom flow into one suction tower acid follow
Annular groove is sent to acid cooler by a suction acid circulating pump and is cooled down, and concentrated acid after cooling enters the first absorption tower and carries out circulation spray
Leaching；
The 4th section of inverting device of gas in the future enters second absorption tower after the cooling of the IVth heat exchanger, through spraying from tower top
98% concentrated sulfuric acid of leaching absorbs the SO in furnace gas3Process tail gas afterwards enters tail gas absorption processing；It is sour from tower bottom stream after absorption
Enter two suction acid circulating slots, is sent by two suction acid circulating pumps to acid cooler and cooled down, concentrated acid after cooling enters second absorption tower
Carry out circulated sprinkling；
It is provided with automatic water-feeding device addition process water in sour circulating slot absorbing, absorbs the dense of acid for regulation and control
Degree；When producing 93% acid, the extra recycle acid of absorption cycle slot is sealed in drying tower, draws conduct after dry acid cooler
Product；When producing 98% acid, the extra acid of absorption cycle slot is as product, from acid cooler outlet discharge is absorbed, by electricity
After magnetic flowmeter metering, it is sent to concentrated sulfuric acid relay reservoir, is periodically taken to store in sulfuric acid basin.
In order to accurately measure sulphuric acid output, it is provided with electromagnetic flowmeter.In order to which female acid is added when device driving and conveniently sets
Standby maintenance is provided with underground acid tank and acid pump.
Further preferred technical solution is in addition, the conversion unit is used through drying tower drying and through tower top wire mesh
Cold air after demister demisting is by SO2After sequentially entering the heating of the III, the I heat exchanger heater after air blower boosting, temperature liter
The first segment for entering converter to 420 DEG C is converted；Furnace gas temperature is increased to about 585 DEG C into the Ith heat exchanger after reacted
With come from SO2The cold air of air blower, which exchanges heat, to cool down, and furnace gas after cooling enters converter second segment catalyst bed and urged
Change reaction, then converter further reacts after entering the cooling of the IIth heat exchanger into converter third section catalyst bed out.
Further preferred technical solution is in addition, from the gas that the converter third section exports, into the IIIth heat exchanger
Tube side, temperature enter heating boiler feed water in economizer after being down to 230 DEG C, temperature drops to 175 DEG C and enters the first absorption tower, absorbs
SO in gas3, and after the acid mist that the mesh mist eliminator of tower top removes in gas, sequentially enter the IV, the II heat exchanger, gas
Body enters the 4th section of catalyst bed of converter and carries out second of conversion after being heated；The gas of the 4th section of bed enters the IVth out
Heat exchanger and black furnace gas carry out heat exchange cooling, and temperature is reduced to about 165 DEG C and enters second absorption tower, absorbs a small amount of in gas
SO3, then it is vented after tail gas absorber purifies.
Furnace gas heats up when to drive, and is provided with two electric furnaces.For regulation and control conversion section temperature, being provided with must
The process pipe by-pass and regulating valve wanted.
Further preferred technical solution is in addition, the tail gas treating unit inhales the process tail gas head that tower conveying comes from second
It is introduced into ammonia absorber, carries out cyclic absorption with ammonium hydroxide, the SO in tail gas2、SO3And sulfuric acid mist and NH3Reaction generates (NH4)
2SO3(NH4)2SO4, being discharged in the tail gas of second absorption tower has a small amount of Ammonia valatilization to come out, then is inhaled by Ammonic washing tower with diluted acid
Receive NH therein3Afterwards, it is emptied by chimney；Absorb NH3Absorbing liquid, the purification process of dilute sulfuric acid and second absorption tower discharge afterwards
The dilute sulfuric acid of generation is passed in decomposer, decomposes ammonium sulfite with dilute sulfuric acid, is generated ammonium sulfate liquor and is sent to sulphur ammonium unit
Produce ammonium sulfate, the SO decomposited2Gas is sent in drying tower import furnace gas pipeline and recycles.
The advantages and beneficial effects of the present invention are: described is by the sulphur foam of sweetening process recycling and desulfurization waste liquor configuration
At slurry, after filtering and concentrating, dry solidification in spray drying tower is sprayed into, the solids crude sulphur of saliferous is recycled；By saliferous
Solids crude sulphur directly burns, and generates SO2Furnace gas, then product sulphur is made through processes such as waste heat recycling, purification, conversion and absorptions
Acid.If the solids crude sulphur amount that single factory's recycling generates is smaller, is not enough to produce sulfuric acid and generates scale effect, then it is contemplated that
It only goes up drying system and recycles thick sulphur powder, be suitable for transport to be sent outside to gas washing in SA production factory makes directly as gas washing in SA production raw material
With.Secondary pollution waste material will not be generated using above-mentioned technique, need to be further processed.Also have that low energy consumption using the technique, it is right
The features such as equipment corrosion is small.
Detailed description of the invention
Fig. 1 is the process flow chart of inventive desulfurization waste liquid acid-making process；
Fig. 2 is the master device system construction drawing used in inventive desulfurization waste liquid acid-making process；
Fig. 3 to Fig. 8 be one of segmentation enlarged drawing of the system of Fig. 2 to it six, one of system diagram to it between six for successively
Interconnected relationship.
In figure: 1, tube body；2, insulating layer；3, metal layer；4, stitch；5, conducting wire；6, plug connector；7, controller；8, sheath.
Specific embodiment
With reference to the accompanying drawings and examples, further description of the specific embodiments of the present invention.Following embodiment is only
For clearly illustrating technical solution of the present invention, and not intended to limit the protection scope of the present invention.
According to the current coke annual output of certain coal chemical enterprise at 2,000,000 tons/year, coke-stove gas occurrence quantity is about the present invention
100000Nm3/h；H before coke oven gas desulfurization2S content is 5~6g/Nm3, H after desulfurization2S content is 0.05g/Nm3；Elemental sulfur is raw
At about 8.4t/ days (being converted into pure sulfur content 100%) of amount；Doctor solution yield about 70m containing secondary salt3/ day, secondary salt in doctor solution
Content is 200-250g/l, wherein (NH4)2S2O3Content 60-80g/l, NH4SCN content 120-140g/l, separately there is (NH4)2SO4
Content 0g/l.
Design scale in the embodiment of the present invention:
According to the design condition of offer, production requirement, and through specific design basis data, by raw materials for production
MaterialBalance Computation, to determine specific gas washing in SA production scale.
(1) year runing time: 8000 hours, 333.3 days.
(2) annual production capacity: 2,000,000 tons/year of coke desulfurating waste liquid Sulphuric acids, nominal capacity are 1.5 ten thousand tons/year of sulfuric acid
(folding 100%H2SO4).
(3) design operation range: 70~110%.
(4) useless solid-liquid processing capacity: depending on raw material actual conditions.
The embodiment of the present invention is to produce industrial sulphuric acid, product supply sulphur ammonium work using coking desulfurization waste liquor and sulphur foam as raw material
Duan Zuowei sulphur ammonia produces the raw material of sulphur ammonia, while making full use of the waste heat of production process, byproduct steam.According to project construction locality
The factors such as meteorological condition, process water balance, product purpose, product characteristic, public utility specification, determine that products scheme is as follows:
Purpose major product of the embodiment of the present invention is industrial sulphuric acid, the determination of sulfuric acid product specification, mainly according to its use
Way and meteorological condition.The concentrated sulfuric acid easily crystallizes, its crystallization temperature of the sulfuric acid of various concentration changes greatly, and wherein concentration is 98.0% sulphur
The crystallization temperature of acid is -0.7 DEG C, the crystallization temperature that concentration is 93.0% sulfuric acid is -29 DEG C, according to project construction meteorological condition
To determine that producing 98% sulfuric acid still produces 93% sulfuric acid.Product quality is up to state standards the wanting of Grade A in GB/T534-2002
It asks.
Byproduct: waste heat recycles byproduct steam.This project production scale is small sulfuric device, and steam production is not high, dress
Set has low-pressure steam pipeline to pass through nearby, while enterprise needs using a large amount of low-pressure steam, to avoid steam long distance delivery
Excessively high thermal losses is caused, it is thus determined that product specification is low-pressure saturated steam.Low-pressure steam is steamed according to the existing low pressure of enterprise
The design of vapour ductwork pressure grade.
As shown in Fig. 1 to Fig. 8 the present invention is a kind of desulphurization waste liquid of coke oven gas relieving haperacidity preparation process, the technique include with
Desulphurization waste liquid of coke oven gas and sulphur foam are raw material, successively use drying process with atomizing, fluidized-bed roasting process, acid-scrubbing cleaning technique
With the contact method relieving haperacidity production technology of double-absorption technique；The master device used in the desulfurization waste liquor acid-making process is wrapped in total
Containing six units: feed material preparation units burn sulphur unit, clean unit, dry suction unit, conversion unit and tail gas treating unit.
It in order to avoid repetitive operation, reduces operating cost and facilitates management, deactivate existing sulphur foamed filter, filters pressing etc. and set
It applies, the preferred embodiment of the invention is, in the drying process with atomizing, desulphurization waste liquid of coke oven gas and sulphur foam are described
Dilute sulphur foam in feed material preparation units directly by desulfurization regeneration tower production is sent into filter and filter press, by the first mistake of sulphur foam
Filters pressing is carried out after filter again.It both can be convenient operation in this way, reduced energy consumption, while dilute sulphur foam is also relatively more square using pipeline
Face, the problems such as line clogging will not be generated.
The main purpose of desulphurization waste liquid of coke oven gas relieving haperacidity preparation process construction is all to handle coke oven gas desulfurization
The waste liquid that process generates, therefore the technological design of pretreatment of raw material process should meet the operation needs of desulfurizer comprehensively, do
To synchronous operation.Since the desulphurization waste liquid of coke oven gas relieving haperacidity preparation process project wastewater treatment capacity is big, the dry volume needed
It is very big, while for the ease of adjusting produce load at any time, facilitating operational administrative, reduction energy consumption and operating cost, by technique core
It calculates, the drying of sulphur foam and desulfurization waste liquor uses two system paired runnings.
Further preferred embodiment of the present invention is, in the drying process with atomizing；
(1) the sulphur foam that will be generated in the sweetening process, directly with sulphur foam filter is pumped into, after filtering by sulphur
To solid about 20%~30% or so (according to mass balance) is contained, formation sulphur cream is put into sulphur cream storage tank to be stored Foam concentration, will
The master device of the clear liquid filtered out back to desulfurization waste liquor relieving haperacidity is interior to be recycled.The concentration rate of sulphur foam is according to desulphurization system
The requirement of balance and waste liquid amount require to automatically control.
(2) the sulphur cream in sulphur cream storage tank is pumped into spiral-flow type spray drying tower by screw rod again, by centrifugal atomizing
After device atomization, cocurrent enters in drying tower simultaneously with hot-air, and the sulphur foam after drying tower is atomization is changed with hot-air
Heat, solidification, drying are acted on by the cyclonic separation of drying tower, and granular thick sulphur of the major part after dry is collected into tower bottom,
By the cooling of cold wind spiral case, the automatic control of Pneumatic butterfly valve, enters and gather materials on belt feeder.
(3) tail gas of drying tower is sent into further purified treatment in tail gas washing tower by air-introduced machine.
(4) hot-air required for drying tower, is generated by fuel gas hot-blast stove.
(5) degree of drying for recycling the thick sulphur of powdery is controlled by adjusting exhaust temperature, is measured by exhaust temperature
Signal, the flow of feedback regulation feed pump.
(6) due to the thick sulphur of powdery have the characteristics that easily melt, the temperature of drying tower import hot-air be also required into
Row control.At 200 DEG C or so, temperature is controlled by adjusting the additional amount of hot wind producer gas for the temperature control of import hot-air
System, passes through the temperature measurement signal of import hot-air, the additional amount of feedback regulation coal gas
(7) feeding quantity of drying tower can also realize automatic control, pass through the level gauging signal of sulphur foam tank, feedback regulation
The motor inverter of screw pump.
(8) the drying tail gas after dedusting is made a gift to someone tail gas absorber by air-introduced machine, is vented after being handled with water cyclic absorption.
The ammonia and a small amount of sulphur that drying process volatilizes have been dissolved in washing water, and the supplement water for sweetening process can be recycled.
(9) operation for the ease of the maintenance of device in desulfurization waste liquor acid-making process without influencing coking agent set, dress
Solid sulfur storage warehouse is also provided in setting, in the maintenance of sulfuric acid preparation facilities, the thick sulphur of material unit production can be longer
It is temporally stored in sulfur warehouse, while outsourcing fraction solids sulphur may be implemented also to supplement the deficiency of raw materials for production, protect
Sulfuric acid preparation facilities is demonstrate,proved often in production run under higher load, yield is improved, increases economic benefit.
It is about 1.5m by estimating solid content in 20% desulfurization waste liquor and sulphur foam spray drying flow3/ h, hot-blast stove go out
It is 200 DEG C or so that mouthful hot wind, which enters spray drying tower inlet temperature, and spray drying tower goes out tower exhaust temperature at 90 DEG C or so, hot wind
Furnace consumes coke-oven coal tolerance about 350Nm3/ h, the hot blast rate of generation about 32000Nm3/h。
Further preferred embodiment of the present invention is in addition, in the fluidized-bed roasting process, using burning in sulphur unit
Roaster, by the thick sulphur of solid powder and granule shape, by gathering materials, belt feeder is made a gift to someone into roaster, the air blown with air-blaster
Boiling Combustion together generates about 1100 DEG C of high temperature SO2Furnace gas, temperature drops to 350 DEG C of left sides after waste heat boiler recycles heat
Right further to recycle heat into low temperature exhaust heat boiler, temperature is reduced to about 220 DEG C or so and is transported to clean unit purification again.
Further preferred embodiment of the present invention is in addition, the roaster being arranged in sulphur unit that burns is boiled using troilite
The structure for rising furnace maintains the stability and reliability of operation by the specific fixing layer of setting as accumulation of heat and conduction material,
It is provided with two, three times air-supply structure on the roaster, for the operation temperature of regulation and control roaster, while meeting production
The requirement of load wide fluctuations.The thick sulphur charging belt of solid powder and granule shape adjusts control using frequency converter, is measured using oxygen table
Remaining oxygen content in heat boiler outlet furnace gas, the feeding quantity of feedback automatic adjustment roaster, under normal circumstances, roaster
Operation realize automation control.Coal gas burner, heating and driving for roaster are set.It is also set on the roaster
It is equipped with coal gas burner, peep hole, to observe and monitor the mode of operation and operating condition of roaster.In order to make full use of reaction
Waste heat, is not provided with cooling element in roaster, whole reaction thermal energy pass through furnace gas bring into waste heat boiler recycled,
Generate steam.Adequate operation temperature in roaster is by adjusting air quantity, control outlet furnace gas SO2The method of concentration is controlled
System.It is calculated by material and heat balance, out the furnace gas normal control SO of roaster2Content is about 12.5%.
According to the operating parameter of factory's low-pressure steam pipe network, the pressure rating for designing low-pressure steam is 1.0Mpa, the present apparatus
Waste Heat Boiler Design pressure is 1.25Mpa, and can be automatically adjusted according to the parameter of steam pipe network.
Further preferred embodiment of the present invention is in addition, the acid-scrubbing cleaning technique is using dynamic wave high energy scrubber
With stuffing washing tower to high temperature SO2Furnace gas is washed, about 220 will exported by low temperature exhaust heat boiler in the clean unit
DEG C furnace gas be first fed into dynamic wave high energy scrubber, spray people recycles diluted acid and after being well atomized, furnace gas SO2With mist
The diluted acid close contact of change makes furnace gas SO by adiabatic evaporation2Humidification, cooling, cooling and primary wash purification, by dynamic wave
The wet furnace gas SO that high energy scrubber outlet excludes2After gas-liquid separation, into stuffing washing tower, the cooling with tower top spray is followed
Ring diluted acid counter current contacting, washing, purifying remove impurity and steam therein, subsequently into acid mist is removed in electrostatic precipitator, send to
It is dry to inhale unit.
Using adiabatic evaporation, cooling, diluted acid recycles washing flow to dynamic wave scrubber, and the impurity such as ammonia salt in furnace gas pass through
Washing enters in circulation fluid, and a small amount of extra diluted acid is discharged in vent gas treatment slot, is jointly processed by with tail gas absorption liquid.
Scrubbing tower uses packed tower, tower slot integral structure, diluted acid circulation washing.The diluted acid of circulating-pump outlet passes through diluted acid
After plate heat exchanger is cooling, it is sent to tower top spray washing furnace gas.Extra diluted acid seals in washer circulating slot, keeps water flat
Weighing apparatus.Diluted acid plate heat exchanger uses circulating water.The a small amount of diluted acid string being discharged in electrostatic precipitator to scrubbing tower circulating slot.For
Prevent SO in purification process2Equal toxic and harmful gas leakage pollution environment, purification system use negative-pressure operation.To prevent negative pressure mistake
High, protection cleaning equipment and process pipe safety, are provided with Safety water seal on electrostatic precipitator outlet conduit.
Further preferred embodiment of the present invention in addition, the double-absorption technique using slot → pump → acid cooler →
Tower → slot circulation technology, wherein dry inhale sour circulation absorption system using two kinds of acid circulations, drying tower uses 94%H2SO4Circulation,
Absorption tower uses 98%H2SO4Circulation, three towers, three slot process, the absorption tower You Liangtai acid cooler and a drying tower acid cooler
Form the cooling dry suction unit of recycle acid；Future auto purification unit furnace gas, after supplementing suitable air, it is single that control enters conversion
SO in the furnace gas of member2Content (controls when produce load is lower for 8.0~8.5% and is transformed into SO in mouthful furnace gas28.5%) content is
Drying tower is entered by bottom air inlet, through absorbing moisture content in furnace gas from 94% concentrated sulfuric acid that tower top sprays, uses water in tower air
Part≤0.1g/Nm3, it is dry sour from the dry tower acid circulating slot of tower bottom inflow after absorbing moisture, it is followed with from the first absorption tower acid
Ring pump string acid-mixed is bonded to 94% concentration, is sent by drying tower acid circulating pump to drying tower acid cooler and is cooled down, after cooling dense
Acid enters drying tower and carries out circulated sprinkling.
Gas from converter third section through the cooling of the Vth heat exchanger, enters the first suction after economizer recycles heat
Tower is received, then through absorbing the SO in furnace gas from 98% concentrated sulfuric acid that tower top sprays3, after absorption acid from tower bottom flow into one suction tower acid follow
Annular groove is sent to acid cooler by a suction acid circulating pump and is cooled down, and concentrated acid after cooling enters the first absorption tower and carries out circulation spray
Leaching；
The 4th section of inverting device of gas in the future enters second absorption tower after the cooling of the IVth heat exchanger, through spraying from tower top
98% concentrated sulfuric acid of leaching absorbs the SO in furnace gas3Process tail gas afterwards enters tail gas absorption processing；It is sour from tower bottom stream after absorption
Enter two suction acid circulating slots, is sent by two suction acid circulating pumps to acid cooler and cooled down, concentrated acid after cooling enters second absorption tower
Carry out circulated sprinkling；
It is provided with automatic water-feeding device addition process water in sour circulating slot absorbing, absorbs the dense of acid for regulation and control
Degree；When producing 93% acid, the extra recycle acid of absorption cycle slot is sealed in drying tower, draws conduct after dry acid cooler
Product；When producing 98% acid, the extra acid of absorption cycle slot is as product, from acid cooler outlet discharge is absorbed, by electricity
After magnetic flowmeter metering, it is sent to concentrated sulfuric acid relay reservoir, is periodically taken to store in sulfuric acid basin.
In order to accurately measure sulphuric acid output, it is provided with electromagnetic flowmeter.In order to which female acid is added when device driving and conveniently sets
Standby maintenance is provided with underground acid tank and acid pump.
Further preferred embodiment of the present invention is in addition, the conversion unit is used through drying tower drying and through tower top gold
Cold air after belonging to mesh mist eliminator demisting is by SO2After sequentially entering the heating of the III, the I heat exchanger heater after air blower boosting,
Temperature is raised to the first segment that 420 DEG C enter converter and is converted；Furnace gas temperature is increased to about 585 DEG C into the Ith after reacted
Heat exchanger with come from SO2The cold air of air blower, which exchanges heat, to cool down, and furnace gas after cooling enters converter second segment catalyst bed
Catalysis reaction is carried out, it is further to enter converter third section catalyst bed after then converter cools down into the IIth heat exchanger out
Reaction.
Further preferred embodiment of the present invention is in addition, from the gas that the converter third section exports, into the IIIth
Heat exchanger tube pass, temperature enter heating boiler feed water in economizer after being down to 230 DEG C, temperature drops to 175 DEG C and enters the first absorption
Tower absorbs the SO in gas3, and after the acid mist that the mesh mist eliminator of tower top removes in gas, it sequentially enters the IV, the II and changes
Hot device, gas enter the 4th section of catalyst bed of converter and carry out second of conversion after being heated；The gas of 4th section of bed out
Heat exchange cooling is carried out into the IVth heat exchanger and black furnace gas, temperature is reduced to about 165 DEG C and enters second absorption tower, absorbs in gas
A small amount of SO3, then it is vented after tail gas absorber purifies.
Furnace gas heats up when to drive, and is provided with two electric furnaces.For regulation and control conversion section temperature, being provided with must
The process pipe by-pass and regulating valve wanted.
Further preferred embodiment of the present invention is in addition, the tail gas treating unit inhales the technique that tower conveying comes from second
Tail gas initially enters ammonia absorber, carries out cyclic absorption with ammonium hydroxide, the SO in tail gas2、SO3And sulfuric acid mist and NH3Reaction generates
(NH4)2SO3(NH4)2SO4, being discharged in the tail gas of second absorption tower has a small amount of Ammonia valatilization to come out, then by Ammonic washing tower with dilute
Acid absorbs NH therein3Afterwards, it is emptied by chimney；Absorb NH3Absorbing liquid, the purification of dilute sulfuric acid and second absorption tower discharge afterwards
The dilute sulfuric acid that process generates is passed in decomposer, decomposes ammonium sulfite with dilute sulfuric acid, is generated ammonium sulfate liquor and is sent to sulphur ammonium
Cellular manufacture ammonium sulfate, the SO decomposited2Gas is sent in drying tower import furnace gas pipeline and recycles.
Capital equipment list
Main economic and technical indices
(1) production capacity: 1.5 ten thousand tons/year (100%H2SO4 meter)
(2) norm quota of consumption is in terms of 100%H2SO4 per ton；
(3) at 333.3 days day is operated year, it is 24 hours daily (8000 hours).
(4) raw material, power (water, electricity, the vapour, gas) norm quota of consumption and consumption
2. including sulfuric acid master device, raw material workshop section power consumption；
2. including process water and circulating water system.
3. three waste discharge
Three waste discharge standard
Present apparatus three waste discharge must reach national environmental protection three waste discharge standard.Device is of less demanding to be referred in following discharge
Mark:
Table 1-1 " three wastes " discharge standard
Industrial gas emission.Discharge amount of exhaust gas under discharge amount of exhaust gas and abnormal conditions generally under normal circumstances is all
To reach the discharge standard of national regulation by washing, purifying.
Discharge of wastewater
Technique waste water discharge, sulfuric acid master device are discharged without technique waste water under normal circumstances.Purification, dry absorption section are sour on a small quantity
Property terrace flushing water send device reuse after collecting.
The discharge of sanitary wastewater, sanitary sewage enter Shandong Tiexiong Metallurgy Technology Co., Ltd.'s drainage system and are uniformly processed.
Solid waste and dust.Generated waste material and in various solids when due to overhauling or producing abnormal conditions
Material, raw material, finished product etc. have bad luck and storage process in the waste material that generates all need to recycle by certain mode
The above is only a preferred embodiment of the present invention, it is noted that for the ordinary skill people of the art
For member, without departing from the technical principles of the invention, several improvements and modifications can also be made, these improvements and modifications
Also it should be regarded as protection scope of the present invention.
Claims (10)
1. a kind of desulphurization waste liquid of coke oven gas relieving haperacidity preparation process, which is characterized in that the technique includes with coke oven gas desulfurization
Waste liquid and sulphur foam are raw material, successively use drying process with atomizing, fluidized-bed roasting process, acid-scrubbing cleaning technique and double-absorption work
The contact method relieving haperacidity production technology of skill；The master device used in the desulfurization waste liquor acid-making process includes six units in total:
Feed material preparation units burn sulphur unit, clean unit, dry suction unit, conversion unit and tail gas treating unit.
2. desulphurization waste liquid of coke oven gas relieving haperacidity preparation process as described in claim 1, which is characterized in that in the spray drying
In technique, desulphurization waste liquid of coke oven gas and sulphur foam are in the feed material preparation units directly by the dilute of desulfurization regeneration tower production
Sulphur foam is sent into filter and filter press, carries out filters pressing after sulphur foam is first filtered again.
3. desulphurization waste liquid of coke oven gas relieving haperacidity preparation process as claimed in claim 2, which is characterized in that in the spray drying
In technique, the sulphur foam that will be generated in the sweetening process, directly with sulphur foam filter is pumped into, after filtering by sulphur foam
It is concentrated to containing solid about 20%~30% or so, formation sulphur cream, which is put into sulphur cream storage tank, to be stored, and the clear liquid that will filter out returns to
It is recycled in the master device of desulfurization waste liquor relieving haperacidity；The sulphur cream in sulphur cream storage tank spiral-flow type is pumped by screw rod again to do by spraying
In dry tower, after centrifugal atomizer is atomized, cocurrent enters in drying tower simultaneously with hot-air, the sulphur after drying tower is atomization
Foam is exchanged heat with hot-air, is solidified, is dried, and is acted on by the cyclonic separation of drying tower, by the powder after most of drying
The thick sulphur of shape is collected into tower bottom, by the cooling of cold wind spiral case, the automatic control of Pneumatic butterfly valve, enters and gathers materials on belt feeder.
4. desulphurization waste liquid of coke oven gas relieving haperacidity preparation process as claimed in claim 3, which is characterized in that in the fluidized bed roasting
In technique, the thick sulphur of solid powder and granule shape is made a gift to someone by the belt feeder that gathers materials to roaster using the roaster burnt in sulphur unit
In, the Boiling Combustion together with the air that air-blaster is blown generates 1100 DEG C of high temperature SO2Furnace gas is returned by waste heat boiler
Temperature drops to 350 DEG C or so and further recycles heat into low temperature exhaust heat boiler after receipts heat, and temperature is reduced to about 220 DEG C or so
It is transported to clean unit purification again.
5. desulphurization waste liquid of coke oven gas relieving haperacidity preparation process as claimed in claim 4, which is characterized in that described to burn in sulphur unit
The roaster of setting uses the structure of pyrite fluosolid roaster, by the way that specific fixing layer is arranged as accumulation of heat and conduction material, dimension
The stability and reliability for holding operation are provided with two, three times air-supply structure on the roaster, roast for regulation and control
The operation temperature of furnace；The thick sulphur charging belt of solid powder and granule shape adjusts control using frequency converter, measures waste heat boiler using oxygen table
Export the remaining oxygen content in furnace gas, the feeding quantity of feedback automatic adjustment roaster；Coal gas burning is provided on the roaster
Mouth, peep hole；Adequate operation temperature in roaster is by adjusting air quantity, control outlet furnace gas SO2The method of concentration carries out
Control.
6. desulphurization waste liquid of coke oven gas relieving haperacidity preparation process as claimed in claim 5, which is characterized in that the acid-scrubbing cleaning work
Skill is using dynamic wave high energy scrubber and stuffing washing tower to high temperature SO2Furnace gas is washed, will in the clean unit
It is first fed into dynamic wave high energy scrubber by about 220 DEG C of the furnace gas that low temperature exhaust heat boiler exports, spray people recycles diluted acid simultaneously
After being well atomized, furnace gas SO2Furnace gas SO is made by adiabatic evaporation with the diluted acid close contact of atomization2Humidification, cooling, drop
Mild primary wash purification, the wet furnace gas SO excluded by the outlet of dynamic wave high energy scrubber2After gas-liquid separation, into filler
Scrubbing tower, with tower top spray cooling cycle diluted acid counter current contacting, washing, purifying, remove impurity and steam therein, then into
Enter and remove acid mist in electrostatic precipitator, sends to dry suction unit.
7. desulphurization waste liquid of coke oven gas relieving haperacidity preparation process as claimed in claim 6, which is characterized in that the double-absorption work
Skill uses slot → pump → acid cooler → tower → slot circulation technology, wherein dry acid circulation absorption system of inhaling is followed using two kinds of acid
Ring, drying tower use 94%H2SO4Circulation, absorption tower use 98%H2SO4Circulation, three towers, three slot process, by two absorption tower acids
The dry suction unit of cooler and a drying tower acid cooler composition recycle acid cooling；Future auto purification unit furnace gas, supplement
After suitable air, control enters SO in the furnace gas of conversion unit2Content enters drying by bottom air inlet for 8.0~8.5%
Tower uses moisture content≤0.1g/Nm in tower air through absorbing moisture content in furnace gas from 94% concentrated sulfuric acid that tower top sprays3, absorb moisture
Dry acid afterwards flows into dry tower acid circulating slot from tower bottom, dense with being bonded to 94% from the first absorption tower acid circulating pump string acid-mixed
Degree, is sent to drying tower acid cooler by drying tower acid circulating pump and is cooled down, concentrated acid after cooling enters drying tower and recycled
Spray；Gas from converter third section through the cooling of the Vth heat exchanger, enters the first absorption after economizer recycles heat
Tower, then through absorbing the SO in furnace gas from 98% concentrated sulfuric acid that tower top sprays3, sour from one suction tower acid circulation of tower bottom inflow after absorption
Slot is sent to acid cooler by a suction acid circulating pump and is cooled down, and concentrated acid after cooling enters the first absorption tower and carries out circulated sprinkling；
The 4th section of inverting device of gas in the future enters second absorption tower after the cooling of the IVth heat exchanger, 98% through spraying from tower top
The concentrated sulfuric acid absorbs the SO in furnace gas3Process tail gas afterwards enters tail gas absorption processing；Acid after absorption flows into two from tower bottom and inhales acid
Circulating slot is sent to acid cooler by two suction acid circulating pumps and is cooled down, and concentrated acid after cooling enters second absorption tower and recycled
Spray；It is provided with automatic water-feeding device addition process water in sour circulating slot absorbing, the concentration of acid is absorbed for regulation and control；When
When 93% acid of production, the extra recycle acid of absorption cycle slot is sealed in drying tower, is drawn after dry acid cooler and is used as product；
When producing 98% acid, the extra acid of absorption cycle slot is as product, from acid cooler outlet discharge is absorbed, by Electromagnetic Flow
After meter metering, it is sent to concentrated sulfuric acid relay reservoir, is periodically taken to store in sulfuric acid basin.
8. desulphurization waste liquid of coke oven gas relieving haperacidity preparation process as claimed in claim 7, which is characterized in that the conversion unit is adopted
With the cold air through drying tower drying and after tower top wire mesh demister demisting by SO2The is sequentially entered after air blower boosting
III, after the heating of I heat exchanger heater, temperature is raised to the first segment that 420 DEG C enter converter and is converted；Furnace gas temperature after reacted
Degree is increased to about 585 DEG C and enters the Ith heat exchanger and come from SO2The cold air of air blower, which exchanges heat, to cool down, and furnace gas after cooling enters
Converter second segment catalyst bed carries out catalysis reaction, and then converter enters converter after entering the cooling of the IIth heat exchanger out
Third section catalyst bed further reacts.
9. desulphurization waste liquid of coke oven gas relieving haperacidity preparation process as claimed in claim 8, which is characterized in that from the converter
The gas of three sections of outlets, into the IIIth heat exchanger tube pass, temperature enters heating boiler feed water in economizer, temperature after being down to 230 DEG C
Degree drops to 175 DEG C and enters the first absorption tower, absorbs the SO in gas3, and removed in gas by the mesh mist eliminator of tower top
After acid mist, the IV, the II heat exchanger is sequentially entered, gas enters the 4th section of catalyst bed of converter after being heated carries out second
Conversion；The gas of the 4th section of bed enters the IVth heat exchanger and black furnace gas and carries out heat exchange cooling out, temperature be reduced to about 165 DEG C into
Enter second absorption tower, absorbs a small amount of SO in gas3, then it is vented after tail gas absorber purifies.
10. desulphurization waste liquid of coke oven gas relieving haperacidity preparation process as claimed in claim 9, which is characterized in that the vent gas treatment
Unit initially enters ammonia absorber from the process tail gas that the second suction tower conveying comes, and cyclic absorption is carried out with ammonium hydroxide, in tail gas
SO2、SO3And sulfuric acid mist and NH3Reaction generates (NH4)2SO3(NH4)2SO4, being discharged in the tail gas of second absorption tower has on a small quantity
Ammonia valatilization comes out, then absorbs NH therein by Ammonic washing tower diluted acid3Afterwards, it is emptied by chimney；Absorb NH3Dilute sulfuric acid afterwards
The dilute sulfuric acid generated with the absorbing liquid of second absorption tower discharge, purification process is passed in decomposer, is decomposed with dilute sulfuric acid sub-
Ammonium sulfate generates ammonium sulfate liquor and send to sulphur ammonium cellular manufacture ammonium sulfate, the SO decomposited2Gas is sent to drying tower import furnace gas
It is recycled in pipeline.
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| CN111017884A (en) * | 2019-12-21 | 2020-04-17 | 山东绿知源环保工程有限公司 | Method for preparing industrial sulfuric acid from desulfurization waste liquid by slurry spraying method |
| CN111232934A (en) * | 2020-03-19 | 2020-06-05 | 四川华茂聚源建筑工程设计有限公司 | Device for utilizing desulfurization waste liquid and operation method thereof |
| CN111285335A (en) * | 2020-02-22 | 2020-06-16 | 江苏康茂环保工程有限公司 | System for preparing sulfuric acid by using sulfur foam and desulfurization waste liquid semidry method and acid preparation method |
| CN113460973A (en) * | 2021-06-30 | 2021-10-01 | 内蒙古金陶股份有限公司 | Method for preparing sulfuric acid by using sulfur concentrate |
| CN114538385A (en) * | 2021-12-31 | 2022-05-27 | 新兴铸管股份有限公司 | Process for preparing concentrated sulfuric acid from desulfurization waste liquid by dry method |
| CN114620692A (en) * | 2022-03-24 | 2022-06-14 | 唐山中大科技有限公司 | Process for preparing sulfuric acid by carrying out salt extraction and co-firing on coking desulfurization foam sulfur melting and desulfurization waste liquid melting method |
| CN114890389A (en) * | 2022-03-31 | 2022-08-12 | 铜陵泰富特种材料有限公司 | Pretreatment method of coking desulfurization acid-making raw material |
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| CN113460973A (en) * | 2021-06-30 | 2021-10-01 | 内蒙古金陶股份有限公司 | Method for preparing sulfuric acid by using sulfur concentrate |
| CN114538385A (en) * | 2021-12-31 | 2022-05-27 | 新兴铸管股份有限公司 | Process for preparing concentrated sulfuric acid from desulfurization waste liquid by dry method |
| CN114620692A (en) * | 2022-03-24 | 2022-06-14 | 唐山中大科技有限公司 | Process for preparing sulfuric acid by carrying out salt extraction and co-firing on coking desulfurization foam sulfur melting and desulfurization waste liquid melting method |
| CN114890389A (en) * | 2022-03-31 | 2022-08-12 | 铜陵泰富特种材料有限公司 | Pretreatment method of coking desulfurization acid-making raw material |
| CN114890389B (en) * | 2022-03-31 | 2024-04-09 | 铜陵泰富特种材料有限公司 | Pretreatment method of coking desulfurization acid-making raw material |
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