CN107311109B - A kind of circulating fluidized bed system and method with Fluorspar Powder production hydrogen fluoride - Google Patents

A kind of circulating fluidized bed system and method with Fluorspar Powder production hydrogen fluoride Download PDF

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CN107311109B
CN107311109B CN201710334825.0A CN201710334825A CN107311109B CN 107311109 B CN107311109 B CN 107311109B CN 201710334825 A CN201710334825 A CN 201710334825A CN 107311109 B CN107311109 B CN 107311109B
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reaction
reactor
section
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CN107311109A (en
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黄正梁
杨遥
林王旻
孙婧元
刘仲玄
王靖岱
阳永荣
蒋斌波
廖祖维
范小强
王浩同
訾灿
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Zhejiang University ZJU
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    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B7/00Halogens; Halogen acids
    • C01B7/19Fluorine; Hydrogen fluoride
    • C01B7/191Hydrogen fluoride
    • C01B7/192Preparation from fluorspar
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1836Heating and cooling the reactor
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1872Details of the fluidised bed reactor
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique

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  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

The invention discloses a kind of circulating fluidized bed systems and method with Fluorspar Powder production hydrogen fluoride.System includes reactor, cyclic part, solid segregation section, solid segregation section.Reactor part is the place that reaction occurs, and cyclic part isolates the incomplete solid of reaction, back to the reaction was continued in reactor after being settled;Solid separate section separates gas-particle two-phase product, and collects the solid of fully reacting, as solid product;Gas condensation portion will separate remaining gas-phase product out and liquefy and collect in solid segregation section.The invention avoids the appearance that agglomerate glues the abnormal phenomenon such as wall, improve mass transfer, heat transfer efficiency, by the cycling rate of control valve aperture control loop fluidized bed on control tolerance size and inclined tube, the solid product ratio isolated is controlled to control solid reaction degree.Liquid condensation is controlled by condensate temperature and dosage, can control product quality by installing multi-stage condensing device additional when containing other impurities in gaseous product.

Description

A kind of circulating fluidized bed system and method with Fluorspar Powder production hydrogen fluoride
Technical field
The present invention relates to a kind of Circulating Fluidized Bed Process for Fluorspar Powder production hydrogen fluoride.
Technical background
Hydrofluoric acid (HF) is the basic product of entire fluorine chemical industry, is mainly used in fluorohydrocarbon industry, accounts for hydrogen fluoride and always disappear 50% or so of consumption;The inorganic fluorines salt dissolvings such as aluminum fluoride and the ice crystal of electrolytic aluminium and aluminium product industry are followed by produced, Account for 30% or more;Be again pickling of metal, be used as in oil plant iso-butane and butane alkylated reaction catalyst and other The production industry of fluorinated organic compound.China is continuously increased the demand of anhydrous hydrogen fluoride in recent years.
Hydrogen fluoride production mainly passes through fluorite and obtains with sulfuric acid reaction.Calcirm-fluoride and sulfuric acid reaction are an endothermic reactions, It industrially needs to react at high temperature, external heating is needed in production process.Current existing production technology mainly has rotary kiln Technique, gas-solid multicompartment fluidized bed technique, gas-liquid-solid fluidized-bed process, intermittent reaction technique etc..United States Patent (USP) US3102787 is announced The method of two kinds of Fluorspar Powders and sulfuric acid reaction production hydrogen fluoride.One of which is rotary kiln technology, and one is multilayer gas-solid flows Change bed process.Rotary kiln technology is most common production technology in current industry.In the technique, Fluorspar Powder and sulfuric acid pass through premix The modes such as conjunction, stirring, shell revolution react in the rotary kiln with heating rotary shell in mixing.According to internal mix Agitating member is different, is broadly divided into simple rotary kiln, the rotary kiln with premixer, the rotary kiln with pre-reactor, interior returns Return slag rotary kiln and several simultaneous with pre-reactor, interior return slag, the rotary kiln of destroyer in slag rotary kiln, pre-reactor. Rotary kiln technology has obtained sufficient development at present, from production maintenance, operating cost, equipment manufacturing cost, consumption of raw materials be difficult into One step reduces.Gas-solid multicompartment fluidized bed technique uses vapor and SO3As air inlet, gas phase reaction generates sulfuric acid and releases gas Big calorimetric provides reaction raw materials sulfuric acid for device, while providing fluorite and heat needed for sulfuric acid reaction.Gas-solid multicompartment fluidized bed work Skill can be improved the reaction efficiency of reactor and eliminate the problem that fluid sulphuric acid reacts easily tacky with fluorite, has and is swift in response, Fluorite utilization rate is high, the simple feature of facility compact.Chinese patent CN201210276366.2 is further perfect gas-solid fluidized Bed process expands available Fluorspar Powder purity range.But (average grain diameter exists since fluorite grain diameter used in industry is smaller Between 20~40 μm), particle agglomeration caused by strong Van der Waals force makes fluidisation and interlayer transmitting become extremely difficult between particle, more Laminarization bed reaction technique is not yet really applied in industry in practice.
In addition to such a technique, a kind of gas-liquid-solid fluidized-bed process is also disclosed in Chinese patent CN201210489798.1, makes It uses phenyl-hexafluoride as inertia dispersing agent, Fluorspar Powder is dispersed, sulfuric acid is dissolved in phenyl-hexafluoride, is reacted with Fluorspar Powder, releases Hydrogen fluoride gas.The technique is able to solve the problem of Fluorspar Powder bonding, improves the efficiency that powder is contacted with acid.But after reacting The separation of the calcium sulfate and dispersing agent of discharge there is a problem of very big, and dispersing agent entrainment is excessive and is difficult to separate so that the technique is difficult Further to develop.
In view of the above-mentioned problems, the invention proposes a kind of Circulating Fluidized Bed Process for Fluorspar Powder production hydrogen fluoride.
In recirculating fluidized bed, on the one hand high fluidizing gas velocity is able to suppress particle agglomeration and viscous wall, effectively eliminates reunion And influence of the viscous wall to mass-and heat-transfer;It is quickly anti-that another aspect Fluorspar Powder carries out short-time contact progress with sulfuric acid in a fluidized bed Settler should be entered afterwards to settle, be recirculated back in fluidized bed that the reaction was continued.Fast reaction is able to maintain higher sulfuric acid concentration, keeps away The problem of reaction rate caused by reaction later period sulfuric acid deficiency substantially slows down is exempted from, production efficiency can be effectively improved.
Summary of the invention
The present invention provides a kind of Circulating Fluidized Bed Process for Fluorspar Powder production hydrogen fluoride, passes through Fluorspar Powder Rapid Circulation By fluidized-bed reaction, particle agglomeration and viscous wall are effectively inhibited, mass-and heat-transfer efficiency is enhanced, improves production efficiency.
It is an object of the present invention to provide a kind of circulating fluidized bed system for Fluorspar Powder production hydrogen fluoride, packets Include: reactor is made of more than direct tube section, direct tube section expanding reach, direct tube section undergauge section below and closing heating shell; Cyclic part, primary cyclone, solid settling section after being exported by gas reactor are connected to reactor air inlet pipe Control valve and lagging casing in inclined tube section, inclined tube are constituted;Solid segregation section is received by secondary cyclone and solid Tank is constituted;Gas condensation portion, by condenser, Liquid acquisition tank is constituted.Reaction mass by enter below reactor reactor into Row reaction enters cyclic part later and isolates solid reactant.The solid retention time of high conversion rate is long, wears tighter Weight, partial size is smaller, leaves cyclic part above primary cyclone with gas phase reaction material and enters solid segregation section, and Both ends are descended to respectively obtain gas-particle two-phase product on it after secondary cyclone separates.Gas-phase product is after condenser condenses It is received by Liquid acquisition tank, solid product enters solid receiving tank.The isolated reaction mass of cyclic part passes through from lower part Control valve enters the air inlet pipe of reactor lower end and make-up gas is mixed into reactor cycles and reacts.Solid is supplemented from circulation Supplement is added in part.Above-mentioned reaction mass includes inert filler and reaction raw materials etc.;Make-up gas and supplement solid, including need Inert filler and reaction raw materials of supplement etc..Wherein reaction raw materials refer to that Fluorspar Powder, sulfuric acid vapor or sulfur trioxide and vapor are mixed Close gas.
In solid segregation section of the invention, counterbalance valve can be installed additional above solid receiving tank, made in secondary cyclone Deposition solid passes through by phased manner, reduces solid and receives pressure inside the tank.
System according to the present invention, a second object of the present invention is to provide a kind of sides of Fluorspar Powder production hydrogen fluoride Method comprising following steps:
1) make the reaction gas with solid circle enter reactor part to be reacted, output is with reaction is not solid completely The reaction product of body.
2) reaction product with unreacted solid of output enters cyclic part above above-mentioned reactor, isolates partial size Biggish incomplete reaction solid particle enters solid settling section, and gas and the smaller solid particle of high conversion rate enter solid Segregation section.Solid control valve by lower diagonal and thereon into solid settling section enters air inlet pipe and reaction gas is mixed Conjunction is recycled back to reactor.
3) the smaller solid particle of above-mentioned cyclic part is isolated gas and high conversion rate enters the two of solid segregation section Grade cyclone separator, upper and lower ends distinguish isolated gas-solid phase reaction product, and gas-phase product enters condensation portion.
4) above-mentioned isolated gas phase reaction product enters Liquid acquisition tank after entering condenser condensation.
The method of Fluorspar Powder production hydrogen fluoride of the present invention, the reaction condition of reactor, used reaction raw materials Type and its dosage, specific as follows:
The present invention uses reaction raw materials, and sulfuric acid vapor or sulfur trioxide and vapor mixed gas are selected in reactor air inlet At least one of two kinds.The sulfur trioxide and vapor gaseous mixture or 95% or more mass fraction of preferred molar ratio 4:1-1:4 Sulfuric acid vapor.Inert gas can be added into air inlet with reduce sulfuric acid vapor or sulfur trioxide and vapor gaseous mixture divide with Reaction temperature needed for reducing.Nitrogen, hydrogen fluoride gas etc., preferred fluorinated hydrogen, and mole fraction may be selected in inert gas 30% or less.Inert gas content is excessively high to reduce reaction rate.
30-200 μm of Fluorspar Powder average grain diameter, preferably 50-100 μm used in the present invention.Calcium Fluoride Content is greater than in Fluorspar Powder 80%, preferably 90% or more high-purity calcirm-fluoride.
Above-mentioned steps 1) in, 170-400 degrees Celsius of reactor operation temperature, 250-350 degrees Celsius of preferable temperature;Operation pressure Power is 0.5-2bar, preferably 0.8-1.2bar;The preferred 0.9-0.12m/s of operating gas velocity 0.07-0.15m/s.
Above-mentioned steps 2) in, cyclic part primary cyclone operating pressure 0.5-2bar, preferably 0.7-1.1bar;Gu Body settling section operating pressure 0.5-2bar, preferably 0.7-1.1bar.Inclined tube and 30-70 ° of horizontal interfacial angle, preferably 50-60 °, Upper and lower ends difference in height is greater than 10cm.Control valve aperture 0.1-0.7, preferably 0.3-0.5 on inclined tube press predetermined amount of flow with solid Solid deposition section, which will not be entered, by gas is advisable.
Above-mentioned predetermined amount of flow is reaction solid enters solid deposition section flow plus benefit from primary cyclone completely Fill Fluorspar Powder amount of solid.Above-mentioned supplement Fluorspar Powder amount of solid, which is equal in step 3), isolates 0.9-1.2 times of amount of solid, preferably 1- 1.1 again.
Above-mentioned steps 3) in, cyclic part primary cyclone operating pressure;Solid receiving tank operating pressure 0.5- 2bar, preferably 0.7-1.05bar.
Above-mentioned steps 4) in, condenser is divided into two sections, cooling using cooling water and chilled brine respectively.Or cooling is used only Water, wherein second segment cooling water temperature is lower than 15 degrees Celsius.
There are two types of schemes according to unstrpped gas type difference is used for above-mentioned shell of reactor.One preferred embodiment is to select sulphur Acid vapor is as unstripped gas, installs closing heating shell needed for needing additional amount of heat to provide reaction, outside reactor additional, uses electricity Heating.Another preferred embodiment is to select sulfur trioxide and vapor gaseous mixture as unstripped gas, and heat needed for reacting is by sulfur trioxide It being reacted with water and sulfuric acid heat release offer is provided, additional closing heating shell can be changed to lagging casing or still use closing heating shell, Use electrical heat tracing.
Using method of the invention, high-purity anhydrous hydrogen fluoride can be produced.
The present invention has the characteristics that prominent and effect as follows compared with prior art:
1, solid-phase reactant quickly flows in reactor, avoids the appearance that agglomerate glues the abnormal phenomenon such as wall, improves Mass transfer, heat transfer efficiency, being capable of the effectively save energy.
2, the Fluorspar Powder of different-grain diameter being separated using cyclone separator, the large-sized residence time is short, and conversion ratio is low, into Enter cyclic part to be recycled;The degree of wear of small particle is high, and the residence time is long, and conversion ratio is also high, close to reaction completely, enters Solid segregation section isolates system as solid reaction product.It is tired to solve the existing reaction late phase reaction of other techniques in this way Difficulty, the problem of reaction time length.It can be fluidized simultaneously by control valve aperture control loop on control tolerance size and inclined tube The cycling rate of bed controls the solid product ratio isolated to control solid reaction degree.
3, liquid condensation is controlled by condensate temperature and dosage, causes to contain in gaseous product when charging proportion is led to the problem of Product quality can be controlled by installing multi-stage condensing device additional when other impurities by having.
Detailed description of the invention
Fig. 1 is the circulating fluidized bed device schematic diagram that Fluorspar Powder of the present invention produces hydrogen fluoride;
Description of symbols:
1 reactor, 2 primary cyclones, 3 solids deposition section, 4 inclined tubes, 5 control valves, 6 secondary cyclones, 7 Counterbalance valve, 8 solid receiving tanks, 9 condensers, 10 Liquid acquisition tanks.
Specific embodiment
Following embodiment is the range being not intended to limit the present invention in order to further illustrate the present invention.
Reaction gas with solid circle enters 1 reactor and is reacted, and output is anti-with incomplete reaction solid Product is answered to enter cyclic part, 2 primary cyclones isolate the biggish incomplete reaction solid particle of partial size into 3 solids Settling section, and gas and the smaller solid particle of high conversion rate enter solid segregation section.Solid into solid settling section passes through 4 inclined tube of lower section and 5 control valves thereon enter air inlet pipe and reaction gas mixing circulation returns reactor.Cyclic part is isolated Gas and the smaller solid particle of high conversion rate enter 6 secondary cyclones of solid segregation section, upper and lower ends are divided respectively From gas-solid phase reaction product is obtained, gas-phase product enters condensation portion, and solid product enters 8 solid receiving tanks by 7 counterbalance valves. Gas phase reaction product enters 10 Liquid acquisition tanks after entering the condensation of 9 condensers.
Embodiment 1
It is Celsius to be previously heated to 300 as unstripped gas for sulfur trioxide, vapor and the HF gaseous mixture of molar ratio 1:1:1.5 Degree, with 10.0m3/ h gas velocity enters reactor air inlet pipe, is mixed into reactor with solid circle and is reacted.Reactor operation 350 degrees Celsius of temperature, pressure 1.2bar.Output enters cyclic part with the reaction product of not reaction solid completely, into level-one Cyclone separator isolates the biggish incomplete reaction solid particle of partial size.Primary cyclone pressure drop 0.05bar.Sink solid Body enters solid settling section, and gas and the smaller solid particle of high conversion rate enter solid segregation section.Into solid settling section Solid control valve by lower diagonal and thereon enter air inlet pipe and reaction gas mixing circulation returns reactor.Inclined tube is long 25cm, upper and lower ends difference in height 20cm.The smaller solid particle of gas and high conversion rate that cyclic part is isolated enters solid The secondary cyclone of segregation section, secondary cyclone pressure drop 0.05bar.Its upper and lower ends distinguishes isolated gas-solid phase Reaction product, gas-phase product enter condensation portion, and solid product enters solid receiving tank by counterbalance valve.Gas phase reaction product into Enter Liquid acquisition tank after entering condenser condensation.Condenser is condensed to obtain hydrogen fluoride liquid using 5 degrees Celsius of chilled brines.
Using 35 μm of average grain diameter, the Fluorspar Powder of Calcium Fluoride Content 94% adds below solid settling section as supplement solid Enter.It is 5.42kg/min that it, which supplements flow,.
It obtains containing calcirm-fluoride 0.8% in solid product, contains 90% or more hydrogen fluoride in the condensate liquid of gaseous product.
Embodiment 2
The sulfuric acid vapor and HF gas of mass fraction 98% are mixed using molar ratio 1:1.5 as unstripped gas, are previously heated to 350 degrees Celsius, with 8.0m3/ h gas velocity enters reactor air inlet pipe, is mixed into reactor with solid circle and is reacted.Reaction 350 degrees Celsius of device operation temperature, pressure 0.95bar.Tiny structure can reduce the leakage probability of hazardous reaction object and product.Reactor Output with not completely reaction solid reaction product enter cyclic part, by primary cyclone isolate partial size compared with Big does not react solid particle completely.Primary cyclone pressure drop 0.05bar.Sinking solids enter solid settling section, and gas Body and the smaller solid particle of high conversion rate enter solid segregation section.Solid into solid settling section passes through lower diagonal and its On control valve enter air inlet pipe and reaction gas mixing circulation and return reactor.The long 25cm of inclined tube, upper and lower ends difference in height 15cm.The smaller solid particle of gas and high conversion rate that cyclic part is isolated enters the second level cyclonic separation of solid segregation section Device, secondary cyclone pressure drop 0.05bar.Its upper and lower ends distinguishes isolated gas-solid phase reaction product, gas-phase product into Enter condensation portion, solid product enters solid receiving tank by counterbalance valve.Gas phase reaction product enters after entering condenser condensation Liquid acquisition tank.One section of condenser uses 20 degrees Celsius of cooling waters, and two sections are successively condensed using 10 degrees Celsius of cooling waters, are obtained To hydrogen fluoride liquid.
Using 30 μm of average grain diameter, the Fluorspar Powder of Calcium Fluoride Content 97% adds below solid settling section as supplement solid Enter.It is 5.21kg/min that it, which supplements flow,.
It obtains containing calcirm-fluoride 0.8% in solid product, contains 90% or more hydrogen fluoride in the condensate liquid of gaseous product.

Claims (9)

1. a kind of circulating fluidized bed system with Fluorspar Powder production hydrogen fluoride, comprising:
1) reactor, by expanding reach, direct tube section undergauge section below and closing heating shell structure more than direct tube section, direct tube section At undergauge section has the internal diameter being gradually reduced downwards, and is equipped with air inlet pipe in its bottom, and entire reactor is outer by closing heating Shell is isolated from the outside, and expanding reach side has outlet for connecting cyclic part;
2) cyclic part, by primary cyclone, solid settling section, the inclined tube section for being connected to reactor air inlet pipe, inclined tube Control valve and lagging casing constitute, primary cyclone import is connected with reactor expanding reach side exit, solid Settling section is the straight tube that one side is equipped with solid supplement adapter tube, solid settling section upper end and primary cyclone outlet at bottom phase Even, lower end is connected with inclined tube section, and inclined tube section is connected with the air inlet pipe side wall of reactor undergauge section bottom;Entire cyclic part by Lagging casing cladding;
3) solid segregation section is made of secondary cyclone and solid receiving tank, and secondary cyclone entrance and level-one are revolved Wind separator top exit is connected, and solid receiving tank is connected with secondary cyclone outlet at bottom, and solid segregation section separates gas Gu two-phase product, and the solid of fully reacting is collected, as solid product;
4) gas condensation portion, by condenser, Liquid acquisition tank is constituted, and gas condensation portion will separate remaining in solid segregation section Gas-phase product out liquefies and collects.
2. a kind of method of the Fluorspar Powder production hydrogen fluoride using system described in claim 1, it is characterised in that including following step It is rapid:
1) make the reaction gas with solid circle enter reactor to be reacted, output is with the not reaction of reaction solid completely Product;
2) reaction product with not reaction solid completely of output enters cyclic part, one cyclonic point above above-mentioned reactor The biggish incomplete reaction solid particle of partial size is isolated from device, into solid settling section, and gas and high conversion rate is smaller Solid particle enters solid segregation section, into solid settling section solid by lower diagonal and control valve thereon into Tracheae and reaction gas mixing circulation return reactor;
3) the smaller solid particle of cyclic part is isolated gas and high conversion rate enters the second level whirlwind point of solid segregation section From device, upper and lower ends respectively obtain gas-solid phase reaction product, and gas-phase product enters condensation portion, and solid phase reaction product enters solid Receiving tank;
4) the isolated gas phase reaction product of above-mentioned secondary cyclone enters Liquid acquisition tank after entering condenser condensation.
3. method according to claim 2, it is characterised in that: in step 1), 170-400 degrees Celsius of reactor operation temperature, Operating pressure 0.5-2 bar, operating gas velocity 0.07-0.15 m/s.
4. method according to claim 2, it is characterised in that: in step 1), 250-350 degrees Celsius of reactor operation temperature, Operating pressure 0.8-1.2 bar, operating gas velocity 0.9-0.12 m/s.
5. method according to claim 2, it is characterised in that: in step 2, cyclic part primary cyclone operation pressure 30-70 ° of power 0.5-2 bar, solid settling section operating pressure 0.5-2 bar, inclined tube and horizontal interfacial angle, upper and lower ends height Difference is greater than 10 cm, control valve aperture 0.1-0.7 on inclined tube.
6. method according to claim 2, it is characterised in that: in step 2, cyclic part primary cyclone operation pressure Power 0.7-1.1 bar;50-60 ° of solid settling section operating pressure 0.7-1.1 bar, inclined tube and horizontal interfacial angle, upper and lower ends Difference in height is greater than 10 cm, control valve aperture 0.3-0.5 on inclined tube.
7. method according to claim 2, it is characterised in that:
Reactor predetermined amount of flow is not react solid completely to enter solid settling section flow plus supplement from primary cyclone Fluorspar Powder amount of solid, above-mentioned supplement Fluorspar Powder amount of solid are equal to secondary cyclone lower part in step 3) and obtain solid reaction production 0.9-1.2 times of object amount.
8. method according to claim 2, it is characterised in that: select sulfuric acid vapor as unstripped gas.
9. method according to claim 2, it is characterised in that: select sulfur trioxide and vapor gaseous mixture as unstripped gas, Heat needed for reaction, which is reacted by sulfur trioxide with water, generates sulfuric acid heat release offer.
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