CN106698363A - Use method of device in evaporation work procedure for preparing insoluble sulfur - Google Patents
Use method of device in evaporation work procedure for preparing insoluble sulfur Download PDFInfo
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- CN106698363A CN106698363A CN201710129231.6A CN201710129231A CN106698363A CN 106698363 A CN106698363 A CN 106698363A CN 201710129231 A CN201710129231 A CN 201710129231A CN 106698363 A CN106698363 A CN 106698363A
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- heating
- sulphur
- saturated vapor
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- gas
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 139
- 238000000034 method Methods 0.000 title claims abstract description 51
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 41
- 239000011593 sulfur Substances 0.000 title claims abstract description 41
- 238000001704 evaporation Methods 0.000 title abstract description 5
- 230000008020 evaporation Effects 0.000 title abstract description 4
- 238000010438 heat treatment Methods 0.000 claims abstract description 111
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 42
- 239000007789 gas Substances 0.000 claims abstract description 24
- 239000007791 liquid phase Substances 0.000 claims abstract description 17
- 239000012071 phase Substances 0.000 claims abstract description 13
- 238000003860 storage Methods 0.000 claims abstract description 13
- 230000005068 transpiration Effects 0.000 claims abstract description 10
- 238000013021 overheating Methods 0.000 claims abstract description 7
- 239000005864 Sulphur Substances 0.000 claims description 82
- 239000007788 liquid Substances 0.000 claims description 35
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 25
- 239000000203 mixture Substances 0.000 claims description 18
- 239000012530 fluid Substances 0.000 claims description 17
- 238000002347 injection Methods 0.000 claims description 11
- 239000007924 injection Substances 0.000 claims description 11
- 238000002156 mixing Methods 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 10
- 229910052757 nitrogen Inorganic materials 0.000 claims description 10
- 238000012546 transfer Methods 0.000 claims description 8
- 238000009826 distribution Methods 0.000 claims description 7
- 238000013461 design Methods 0.000 claims description 6
- 238000010926 purge Methods 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 5
- 239000000843 powder Substances 0.000 claims description 5
- 239000007921 spray Substances 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 3
- 239000003546 flue gas Substances 0.000 claims description 3
- XAQHXGSHRMHVMU-UHFFFAOYSA-N [S].[S] Chemical compound [S].[S] XAQHXGSHRMHVMU-UHFFFAOYSA-N 0.000 claims description 2
- 238000010025 steaming Methods 0.000 claims description 2
- 230000015572 biosynthetic process Effects 0.000 claims 1
- 238000007664 blowing Methods 0.000 claims 1
- 239000000463 material Substances 0.000 abstract description 8
- 238000001816 cooling Methods 0.000 abstract description 5
- 229920000642 polymer Polymers 0.000 abstract description 2
- 239000012855 volatile organic compound Substances 0.000 abstract 1
- 239000002912 waste gas Substances 0.000 abstract 1
- 229920001971 elastomer Polymers 0.000 description 7
- 238000002360 preparation method Methods 0.000 description 6
- 230000000630 rising effect Effects 0.000 description 6
- 238000000889 atomisation Methods 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 238000003756 stirring Methods 0.000 description 5
- 150000001875 compounds Chemical class 0.000 description 4
- 238000002844 melting Methods 0.000 description 4
- 230000008018 melting Effects 0.000 description 4
- 238000006116 polymerization reaction Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 238000004073 vulcanization Methods 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000012043 crude product Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003292 glue Substances 0.000 description 2
- 238000004806 packaging method and process Methods 0.000 description 2
- 238000004513 sizing Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000003381 stabilizer Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- QGJOPFRUJISHPQ-NJFSPNSNSA-N carbon disulfide-14c Chemical compound S=[14C]=S QGJOPFRUJISHPQ-NJFSPNSNSA-N 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000004132 cross linking Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 239000008247 solid mixture Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- 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
- C01B17/02—Preparation of sulfur; Purification
- C01B17/12—Insoluble sulfur (mu-sulfur)
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to the technical field of volatile organic compound waste gas governance, in particular to a use method of a device in an evaporation work procedure for preparing insoluble sulfur. The method is characterized by comprising the use method of a saturated vapor heating kettle assembly, an overheating device, an overheating sulfur steam intermediate tank and a sulfur powder storage tank. A two-section heating mode is used for preparing overheating sulfur steam; firstly, materials are heated to a molten state (liquid phase), and are then heated into the overheating sulfur steam (gas phase); after sharp cooling, sulfur polymers are obtained; a transpiration principle is used, a transpiration convection pipe and a circulation convection pipe are designed for connecting heating devices at the low-temperature section and the high-temperature section, and the technical process is completed.
Description
Technical field
The present invention relates to insoluble sulfur technical field, and in particular to one kind prepares insoluble sulfur evaporization process device
Application method.
Background technology
Insoluble sulfur（IS）Also known as polymerised sulphur, also known as μ types sulphur refers to the sulphur insoluble in carbon disulfide, is the long-chain of sulphur
Polymer, with chemically and physically inertia.It is 1% in the solubility of rubber due to using common sulphur, common sulphur is in rubber
Consumption exceed its dissolving part sizing material cooling after can spray surface, i.e. bloom.Bloom will be influenceed between semifinished part
Stickiness simultaneously brings adverse effect to product vulcanization uniformity, therefore in sulfur consumption appropriate to the occasion use insoluble sulfur higher, it is insoluble
Sulphur does not dissolve in rubber, only dispersed in elastomeric compound, and product vulcanization crosslinking point is uniform, has with its rubber for vulcanizing optimal
No blooming, and can effectively prevent sizing material from occurring early stage incipient scorch in process and promote rubber and steel wire or chemical fibre curtain
The bonding of sub-line, is the dedicated vulcanization agent of radial tyre production.Chinese invention patent（Patent No. 201310511371.1,
Patent name is a kind of method for preparing insoluble sulfur）A kind of method for preparing insoluble sulfur is disclosed, it is characterized in that：1）
Melting：Raw material sulphur is directly heated to 280~400 DEG C, it is melted；2）Atomization：Sulphur liquid after melting is through atomizer
Centrifugal atomizing is into 10 μm~50 μm of sulphur droplet；3）Polymerization：Nitrogen at room is mixed with sulphur droplet after being distributed through gas distributor
Close；Sulphur drop is stopped 2~25 seconds on tower body top, and nitrogen outlet temperature control is at 180~240 DEG C；4）Chilling：After polymerization
Sulphur is cooled to -40~0 DEG C and mixes through the nitrogen after gas distributor distribution with through cooling device again, into tower body bottom,
Less than 60 DEG C were cooled at 2~20 seconds；5）Separate packaging：Cyclonic separation, collects, and packaging obtains insoluble sulfur product.China
Patent of invention（Patent No. 02157245.3, patent name is the preparation method of insoluble sulfur）Disclose insoluble sulfur
Preparation method, it is characterized in that：1. a kind of preparation method of non-oil-filled type insoluble sulfur, it is characterised in that non-oil-filled type is insoluble
Sulfur product mainly includes following preparation process：(1) by common sulphur and the compound stabilizer of mass percent 0.01~0.2%
In adding with heating, the container of stirring, it is filled with inert gas and protects, the constant temperature 10- at a temperature of 250~350 DEG C
90min, after the cooling via superheater, spray gun, atomisation tower and heat exchanger, can obtain conversion ratio be 53~55% it is insoluble
Sulphur crude product；Compound stabilizer is made up of I2 or Br2 with rubber accelerator DM or DZ；(2) by insoluble sulfur crude product with
The solid-to-liquid ratio mixing of leaching agent in mass ratio 1: 15~20, stirs 5~60min at a temperature of 45~80 DEG C, filters while hot, can
Obtain the non-oil-filled type product of high content insoluble sulfur.
Conventional example one discloses a kind of method for preparing insoluble sulfur, and mainly prepare that rubber tyre uses is insoluble
Property sulphur, cooling medium is liquid nitrogen, technological process be melting, atomization, polymerization, chilling, separation pack, it is critical only that how to protect
Sulphur liquid after card melting through atomizer centrifugal atomizing into 20 μm of average grain diameter sulphur droplet, will to reach above technology
Ask, it is necessary to ensure that atomizer at high operating temperatures still being capable of reliably working（Centrifugal atomizing needs atomizer high-speed rotation）, it is many
It is well known, according to the 280-400 DEG C of production environment of high temperature, batch industrialization production it is difficult to ensure that atomizer can normal work and
Ensure the Particle size requirements of sulphur droplet；Conventional example two discloses the preparation method of insoluble sulfur, and main innovation point is
Complete the preparation of insoluble sulfur using normal pressure or low-voltage equipment, main production plant be heat, the container that stirs, superheater,
Spray gun, atomisation tower and heat exchanger, be with immediate technical scheme of the invention, but do not disclose process units details and its
Application method.
The content of the invention
In view of the shortcomings of the prior art, insoluble sulfur evaporization process device is prepared it is an object of the invention to provide one kind
Application method, it is characterized in that：
Step one, first by inert nitrogen gas purging saturated vapor heating kettle component, superheater, overheat sulphur steam in the middle of
Tank, Cosan storage tank, time 5-8 minutes, then inject Cosan to storage tank body, while being passed through toward saturated vapor heating coil full
And steam, heating saturated vapor heating kettle makes its temperature remain 180-190 DEG C, and is passed through high temperature cigarette to Hot-blast Heating chuck
Gas, heating Hot-blast Heating body of heater makes its temperature reach 460-480 DEG C.
Step 2, the startup defeated powder control system of gas, are protection gas using inert nitrogen gas, set nitrogen output pressure
It is 0.4MPa, adjusts nitrogen flow, Cosan is fed through saturated vapor heating kettle component according to the production efficiency requirement of design
Mouth at the uniform velocity injection saturated vapor heating kettle, rotating the uniform device and agitating paddle of mixing component makes Cosan uniformly fall into saturation steaming
Vapour heating coil contact surface is heated, and sulphur switchs to molten condition, and Molten sulphur enters in transpiration lower edge transpiration convection tube and divides
Cloth endless tube, support base located jet pipe injection direction and be arranged along with the tangential direction of Hot-blast Heating inboard wall of furnace body circular arc, guide liquid
Body sulphur is ejected into Hot-blast Heating inboard wall of furnace body tangent to periphery direction, in 460-480 DEG C of high-temperature heating of Hot-blast Heating inboard wall of furnace body
Rapidly gasification forms gas-liquid mixture, and gas-liquid mixture fluid declines along Hot-blast Heating inboard wall of furnace body spiral, and liquid phase part is in rotation
Wind is thrown toward Hot-blast Heating furnace body wall in the presence of separating continues to evaporate, and gas phase portion is enriched with to Hot-blast Heating body of heater top, not
Evaporate complete liquid phase part and be enriched in Hot-blast Heating body of heater bottom through circulative convection pipe return saturated vapor heating kettle, gas phase
Part（Overheat sulphur steam）Enter overheat sulphur steam pipeline through gas-liquid separator, overheat sulphur steam steams through overheating sulphur
Steam pipe enters overheat sulphur steam intermediate tank storage, and it is 0.4MPa to set overheat sulphur steam intermediate tank storage pressure.
Step 3, the gas-liquid of the liquid phase that the sulphur fluid for heating kettle through circulative convection pipe return saturated vapor is enrichment are mixed
Compound, the Cosan for purging injection from bottom to top in saturated vapor heating kettle body forms the fluid-mixing of convection current, in stirring group
With the help of the uniform device and agitating paddle of part, it is fully contacted with saturated vapor heating coil heating surface, sulphur fluid obtains abundant
Mass-and heat-transfer, then through rising convection tube, distribution device assembly enter hot-blast heater body formed a closed fluid circulation loop.
Inventor has found that overheat sulphur steam can be used two sections of mode of heatings and directly heat mode and obtains, described direct
Mode of heating is flashed for Cosan more than boiling temperature, i.e., sulphur is directly changed into gas phase, two sections of mode of heatings from solid phase
It is overheat sulphur steam to be first to heat to molten condition (liquid phase) and then reheating（Gas phase）, the former sulphur condensate after chilling
（Insoluble sulfur）Yield is higher, and the former power consumption is lower.
Inventor has found that two sections of mode of heatings of present invention design are divided into low-temperature zone and high temperature section, and the heating of low-temperature zone is situated between
Matter selects saturated vapor, and heating-up temperature is 180-190 DEG C, and high temperature section heating medium selects high-temperature flue gas, and heating-up temperature is 460-
480℃.Using rising principle design, rising pipe and circulation pipe complete material conveying, mass transfer, heat transfer operational process of craft.Two
Section mode of heating makes sulphur complete mass-and heat-transfer technical process, the heat exchange between heater with gas-liquid mixture flow morphology
Mode is convection current, conduction, and directly heats mode（Flash distillation）The heat exchange mode only conduction pattern of overheat sulphur steam is produced, i.e.,
Conduction heating of the heater to sulphur solid, it is well known that fluid convection heat exchange mode exchanges heat compared with solid conduction heat exchange mode
Area is big, the coefficient of heat transfer is high, heat exchange rate is high, therefore its mode of production more energy-conservation, production efficiency is higher.
Inventor has found, because jet pipe injection direction is arranged along with Hot-blast Heating inboard wall of furnace body tangential direction, guides liquid
Sulphur is ejected into Hot-blast Heating inboard wall of furnace body tangent to periphery direction, in 460-480 DEG C of high-temperature heating urgency of Hot-blast Heating inboard wall of furnace body
Speed gasification forms gas-liquid mixture, and gas-liquid mixture fluid declines along Hot-blast Heating inboard wall of furnace body spiral, and liquid phase part is in hot blast
Heating furnace body heating is lower to be continued to realize that cyclone liquid gas are separated while evaporation, is not evaporated liquid phase part and is enriched in Hot-blast Heating body of heater
Bottom returns to saturated vapor heating kettle through circulative convection pipe.
Inventor has found that sulphur is existed with gas-liquid mixture flow morphology in superheater, to ensure heat exchange efficiency
And protection equipment, using the principle of cyclonic separation, liquid phase part is thrown to Hot-blast Heating inboard wall of furnace body and consistently form one layer of liquid film,
Constantly it is evaporated to overheat sulphur steam and is enriched with to superheater top.Sulphur is with gas in saturated vapor heating kettle body in operation
Liquid-solid mixture flow morphology exist, with the help of mixing component so that sulphur fluid fully with saturated vapor heating dish
Pipe contact is heated, and improves heat exchange efficiency.
Relative to prior art, the present invention is at least containing having the advantage that：First, prior art prepares sulphur glue（It is insoluble
Sulphur）Atomization is drop chilling polymerization again after technological process makes sulphur be in molten condition for 180~240 DEG C of heating-up temperature, compared with
The rapid type of cooling produces sulphur glue after being heated to its boiling temperature overheat sulphur steam formed above（Insoluble sulfur）Yield
It is low；Second, it is to be first to heat to molten condition (liquid phase) and then again that the present invention prepares overheat sulphur steam using two sections of mode of heatings
It is heated to be overheat sulphur steam（Gas phase）, the sulphur condensate obtained after chilling（Insoluble sulfur）Yield is higher, consumes energy lower；The
Four, the heater of rising convection tube and circulative convection pipe connection low-temperature zone and high temperature section is completed using rising principle design
Material is conveyed, and instead of high temperature conveying device；3rd, the present apparatus work when, material liquid phase state be heated development for bubble in length
Greatly, it is gas-liquid mixture phase by continuous phase transistion during rupturing, substantially instead of atomizer, it is commonly known that atomizer
It is also insecure for working at high operating temperatures；4th, material is with gas-liquid mixture phase in saturated vapor heating kettle component, transpiration
Circulated in convection tube, superheater, circulative convection pipe, so that material obtains sufficient mass-and heat-transfer, improve production effect
Rate and reducing energy consumption；5th, because jet pipe injection direction is arranged along with Hot-blast Heating inboard wall of furnace body tangential direction, guide liquid sulfur
Sulphur is ejected into Hot-blast Heating inboard wall of furnace body tangent to periphery direction, in 460-480 DEG C of high-temperature heating of Hot-blast Heating inboard wall of furnace body rapidly
Gasification forms gas-liquid mixture, and gas-liquid mixture fluid declines along Hot-blast Heating inboard wall of furnace body spiral, and liquid portion adds in hot blast
Hot body of heater heating is lower to be continued to realize that cyclone liquid gas are separated while evaporation, and liquid portion is enriched in Hot-blast Heating body of heater bottom through following
Ring convection tube returns to saturated vapor heating kettle.Sulphur is existed with gas-liquid mixture flow morphology in superheater, to ensure
Heat exchange efficiency and protection equipment, using the principle of cyclonic separation, make liquid phase part throw to Hot-blast Heating inboard wall of furnace body and consistently form
One layer of liquid film, is constantly evaporated to overheat sulphur steam and is enriched with to superheater top；6th, operational process of craft is closed
Carried out in process units, the probability for firing sulphur steam be reduced to it is extremely low, while making the probability of pollution environment becomes extremely low.
Brief description of the drawings
Fig. 1 is that a kind of front view structure of the application method for preparing insoluble sulfur evaporization process device of the present invention is illustrated
Figure.
Fig. 2 is that a kind of plan structure of the application method for preparing insoluble sulfur evaporization process device of the present invention is illustrated
Figure.
Fig. 3 is a kind of A partial enlargement structures of the application method for preparing insoluble sulfur evaporization process device of the present invention
Schematic diagram.
Fig. 4 is that a kind of B-B cross-section structures of the application method for preparing insoluble sulfur evaporization process device of the present invention show
It is intended to.
Fig. 5 is that a kind of C-C cross-section structures of the application method for preparing insoluble sulfur evaporization process device of the present invention show
It is intended to.
Fig. 6 is a kind of D partial enlargement structures of the application method for preparing insoluble sulfur evaporization process device of the present invention
Schematic diagram.
Fig. 7 is a kind of E partial enlargement structures of the application method for preparing insoluble sulfur evaporization process device of the present invention
Schematic diagram.
The defeated powder control system 3- storage tank bodies of 1- Cosan storage tank 2- gases
4- charging aperture 5- mixing component 6- uniform device 7- saturated vapors heat kettle
8- saturated vapor heating coils 9- transpiration convection tube 10- agitating paddles
11- saturated vapor heating kettle component 12- circulative convection pipe 13- gas-liquid separators
14- superheater 15- Hot-blast Heating chucks 16- is distributed device assembly
17- Hot-blast Heating bodies of heater 18- overheats sulphur steam pipeline 19- jet pipes
20- distribution endless tube 21- support bases 22- overheat sulphur steam pans.
Specific embodiment
The present apparatus is described further with specific embodiment below in conjunction with the accompanying drawings.
As shown in accompanying drawing 1, Fig. 2, Fig. 3, Fig. 4, Fig. 5, Fig. 6, Fig. 7, one kind prepares insoluble sulfur evaporization process to the present invention
With the application method of device, it is characterized in that：Step one, first by inert nitrogen gas purge saturated vapor heating kettle component
11st, superheater 14, overheat sulphur steam pans 22, Cosan storage tank, 1 time 5-8 minute, then to the injection sulphur of storage tank body 3
Sulphur powder, while being passed through saturated vapor toward saturated vapor heating coil 8, heating saturated vapor heating kettle 7 remains its temperature
180-190 DEG C, and high-temperature flue gas are passed through to Hot-blast Heating chuck 15, heating Hot-blast Heating body of heater 17 makes its temperature reach 460-
480℃。
Step 2, the startup defeated powder control system 2 of gas, are protection gas using inert nitrogen gas, set nitrogen output and press
Power is 0.4MPa, adjusts nitrogen flow, according to the production efficiency requirement of design by Cosan through saturated vapor heating kettle component 11
Charging aperture 4 at the uniform velocity injects saturated vapor heating kettle 7, and the uniform device 6 and agitating paddle 10 for rotating mixing component 5 make Cosan uniform
Fall into the contact surface of saturated vapor heating coil 8 to be heated, sulphur switchs to molten condition, Molten sulphur is right in transpiration lower edge transpiration
Flow tube 9 enters distribution endless tube 20, and support base 21 located the injection direction of jet pipe 19 along with the inwall circular arc of Hot-blast Heating body of heater 17
Tangential direction arranges that guiding Molten sulphur is ejected into the inwall tangent to periphery direction of Hot-blast Heating body of heater 17, in Hot-blast Heating body of heater
460-480 DEG C of high-temperature heating of inwall rapidly gasifies to form gas-liquid mixture, and gas-liquid mixture fluid is along Hot-blast Heating body of heater 17
Wall spiral declines, and liquid phase part is thrown toward the wall of Hot-blast Heating body of heater 17 in the presence of cyclonic separation to be continued to evaporate, gas phase portion
To the enrichment of the top of Hot-blast Heating body of heater 17, not evaporating complete liquid phase part, to be enriched in the bottom of Hot-blast Heating body of heater 17 right through circulating
Flow tube 12 returns to saturated vapor heating kettle 7, gas phase portion（Overheat sulphur steam）Enter overheat sulphur through gas-liquid separator 13
Steam pipeline 18, overheat sulphur steam is stored through overheating sulphur steam pipeline 18 into overheat sulphur steam pans 22,
It is 0.4MPa to set the pressure store of overheat sulphur steam pans 22.
The gas of step 3, the liquid phase that the sulphur fluid for heating kettle 7 through the return saturated vapor of circulative convection pipe 12 is enrichment
Liquid mixture, the Cosan for purging injection from bottom to top in saturated vapor heating kettle 7 forms the fluid-mixing of convection current, is stirring
Mix with the help of the uniform device 6 and agitating paddle 10 of component 5, be fully contacted with the heating surface of saturated vapor heating coil 8, sulphur fluid
Sufficient mass-and heat-transfer is obtained, then enters Hot-blast Heating body of heater 17 through rising convection tube 9, distribution device assembly 16 and form a closure
Fluid circulation loop.
The announcement and teaching of book according to the above description, those skilled in the art in the invention can also be to above-mentioned embodiment party
Formula is changed and changed.Therefore, the invention is not limited in specific embodiment disclosed and described above, to of the invention
Some modifications and changes should also be as falling into scope of the claims of the invention.Although additionally, being used in this specification
Some specific terms, but these terms are merely for convenience of description, do not constitute any limitation to the present invention.
Claims (5)
1. a kind of application method for preparing insoluble sulfur evaporization process device, it is characterized in that：Step one, first by inertia
Saturated vapor heating kettle component, superheater, overheat sulphur steam pans, Cosan storage tank, time 5-8 points are swept in the GN 2 air-blowing
Clock, then injects Cosan to storage tank body；Step 2, the startup defeated powder control system of gas, are protection using inert nitrogen gas
Gas, the uniform device and agitating paddle for rotating mixing component makes Cosan uniformly fall into saturated vapor heating coil contact surface to be heated, sulphur
Sulphur switchs to molten condition, and Molten sulphur enters distribution endless tube in transpiration lower edge transpiration convection tube, in hot-blast heater body
460-480 DEG C of high-temperature heating of wall rapidly gasifies to form gas-liquid mixture, and gas-liquid mixture fluid is along Hot-blast Heating inboard wall of furnace body spiral shell
Drop is screwed off, liquid phase part is thrown toward Hot-blast Heating furnace body wall in the presence of cyclonic separation to be continued to evaporate, and gas phase portion is to hot blast
The enrichment of heating furnace body top, does not evaporate complete liquid phase part and is enriched in Hot-blast Heating body of heater bottom and is returned through circulative convection pipe and satisfy
With steam heating pot body, gas phase portion（Overheat sulphur steam）Enter overheat sulphur steam pipeline, overheat through gas-liquid separator
Sulphur steam enters overheat sulphur steam intermediate tank storage through overheating sulphur steam pipe, sets overheat sulphur steam intermediate tank storage
Pressure is 0.4MPa；Step 3, the liquid phase that the sulphur fluid for heating kettle through circulative convection pipe return saturated vapor is enrichment
Gas-liquid mixture, the Cosan for purging injection from bottom to top in saturated vapor heating kettle body forms the fluid-mixing of convection current,
With the help of the uniform device and agitating paddle of mixing component, it is fully contacted with saturated vapor heating coil heating surface, sulphur fluid is obtained
Obtain sufficient mass-and heat-transfer.
2. a kind of application method for preparing insoluble sulfur evaporization process device according to claim 1, it is characterized in that：
Saturated vapor is passed through toward saturated vapor heating coil, heating saturated vapor heating kettle makes its temperature remain 180-190 DEG C, to
Hot-blast Heating chuck is passed through high-temperature flue gas, and heating Hot-blast Heating body of heater makes its temperature reach 460-480 DEG C.
3. a kind of application method for preparing insoluble sulfur evaporization process device according to claim 1, it is characterized in that：
The sulphur fluid that saturated vapor heats kettle is returned to through the circulative convection pipe of superheater, from lower in saturated vapor heating kettle body
The Cosan of upper purging injection forms the fluid-mixing of convection current, is fully contacted with saturated vapor heating coil heating surface, then through steaming
Rise convection tube, distribution device assembly and enter hot-blast heater body one closed fluid circulation loop of formation.
4. a kind of application method for preparing insoluble sulfur evaporization process device according to claim 1, it is characterized in that：
Setting nitrogen output pressure is 0.4MPa, adjusts nitrogen flow, and Cosan is steamed through saturation according to the production efficiency requirement of design
Vapour heating kettle inlet at the uniform velocity injects saturated vapor heating kettle.
5. a kind of application method for preparing insoluble sulfur evaporization process device according to claim 1, it is characterized in that：
Support base located jet pipe injection direction and be arranged along with the tangential direction of Hot-blast Heating inboard wall of furnace body circular arc, guiding Molten sulphur spray
It is mapped to Hot-blast Heating inboard wall of furnace body tangent to periphery direction.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108203080A (en) * | 2018-03-07 | 2018-06-26 | 张炳文 | A kind of quenching device and its application method |
| CN115283174A (en) * | 2022-09-28 | 2022-11-04 | 德州晶华药用玻璃有限公司 | Prevent little burst crack defect's of antibiotic injection bottle sulphur steam injection device |
Citations (5)
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| CN103754832A (en) * | 2013-12-18 | 2014-04-30 | 河南理工大学 | High temperature gasification furnace for production of insoluble sulfur |
| CN106379865A (en) * | 2016-12-06 | 2017-02-08 | 山东阳谷华泰化工股份有限公司 | Insoluble sulphur reaction device and insoluble sulphur reaction method |
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| CN1986388A (en) * | 2005-12-22 | 2007-06-27 | 南化集团研究院 | Medium grade insoluble sulphur preparing process and producing apparatus |
| CN102070127A (en) * | 2011-02-17 | 2011-05-25 | 四川晨辉化工有限公司 | Method for producing insoluble sulfur |
| CN102491283A (en) * | 2011-09-30 | 2012-06-13 | 洁星环保科技投资（上海）有限公司 | Production equipment and production process for insoluble sulphur |
| CN103754832A (en) * | 2013-12-18 | 2014-04-30 | 河南理工大学 | High temperature gasification furnace for production of insoluble sulfur |
| CN106379865A (en) * | 2016-12-06 | 2017-02-08 | 山东阳谷华泰化工股份有限公司 | Insoluble sulphur reaction device and insoluble sulphur reaction method |
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| CN108203080A (en) * | 2018-03-07 | 2018-06-26 | 张炳文 | A kind of quenching device and its application method |
| CN115283174A (en) * | 2022-09-28 | 2022-11-04 | 德州晶华药用玻璃有限公司 | Prevent little burst crack defect's of antibiotic injection bottle sulphur steam injection device |
| CN115283174B (en) * | 2022-09-28 | 2022-12-09 | 德州晶华药用玻璃有限公司 | Prevent little burst crack defect's of antibiotic injection bottle sulphur steam injection device |
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| CN106698363B (en) | 2018-10-12 |
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