CN104607114A - Apparatus and process for producing chlorinated high polymer - Google Patents
Apparatus and process for producing chlorinated high polymer Download PDFInfo
- Publication number
- CN104607114A CN104607114A CN201410308204.1A CN201410308204A CN104607114A CN 104607114 A CN104607114 A CN 104607114A CN 201410308204 A CN201410308204 A CN 201410308204A CN 104607114 A CN104607114 A CN 104607114A
- Authority
- CN
- China
- Prior art keywords
- high polymer
- fluidized
- gas
- bed reactor
- riser
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 229920000642 polymer Polymers 0.000 title claims abstract description 154
- 238000000034 method Methods 0.000 title claims abstract description 55
- 230000008569 process Effects 0.000 title abstract description 32
- 239000007789 gas Substances 0.000 claims abstract description 104
- 238000005660 chlorination reaction Methods 0.000 claims abstract description 48
- 238000006243 chemical reaction Methods 0.000 claims abstract description 34
- 238000010438 heat treatment Methods 0.000 claims abstract description 22
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000000460 chlorine Substances 0.000 claims abstract description 16
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 16
- 239000000463 material Substances 0.000 claims abstract description 14
- 238000005243 fluidization Methods 0.000 claims abstract description 13
- 238000003756 stirring Methods 0.000 claims abstract description 13
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 12
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims abstract description 12
- 230000004913 activation Effects 0.000 claims abstract description 3
- 238000012546 transfer Methods 0.000 claims description 21
- 239000012535 impurity Substances 0.000 claims description 15
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 12
- 239000002245 particle Substances 0.000 claims description 12
- 239000002994 raw material Substances 0.000 claims description 11
- 230000009467 reduction Effects 0.000 claims description 11
- 239000012530 fluid Substances 0.000 claims description 10
- 230000000694 effects Effects 0.000 claims description 9
- 238000010276 construction Methods 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 5
- 238000006073 displacement reaction Methods 0.000 claims description 5
- 230000001105 regulatory effect Effects 0.000 claims description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L calcium carbonate Substances [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 4
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 4
- 230000001276 controlling effect Effects 0.000 claims description 4
- 239000005543 nano-size silicon particle Substances 0.000 claims description 4
- 206010020843 Hyperthermia Diseases 0.000 claims description 2
- 230000003321 amplification Effects 0.000 claims description 2
- 230000036031 hyperthermia Effects 0.000 claims description 2
- 238000003199 nucleic acid amplification method Methods 0.000 claims description 2
- 238000011144 upstream manufacturing Methods 0.000 claims description 2
- 238000004026 adhesive bonding Methods 0.000 claims 1
- 239000011261 inert gas Substances 0.000 abstract description 9
- 230000033001 locomotion Effects 0.000 abstract description 3
- 238000007599 discharging Methods 0.000 abstract description 2
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 abstract 2
- 239000012495 reaction gas Substances 0.000 abstract 2
- 230000005284 excitation Effects 0.000 abstract 1
- 230000001737 promoting effect Effects 0.000 abstract 1
- 239000012071 phase Substances 0.000 description 16
- 241000196324 Embryophyta Species 0.000 description 14
- 238000004519 manufacturing process Methods 0.000 description 14
- 230000003197 catalytic effect Effects 0.000 description 11
- 238000006555 catalytic reaction Methods 0.000 description 11
- 238000002156 mixing Methods 0.000 description 9
- 229920000915 polyvinyl chloride Polymers 0.000 description 7
- 239000004800 polyvinyl chloride Substances 0.000 description 7
- 230000003134 recirculating effect Effects 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 239000003708 ampul Substances 0.000 description 6
- 108010066057 cabin-1 Proteins 0.000 description 6
- 238000010586 diagram Methods 0.000 description 6
- 230000005012 migration Effects 0.000 description 6
- 238000013508 migration Methods 0.000 description 6
- 239000010453 quartz Substances 0.000 description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 239000008246 gaseous mixture Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 239000000725 suspension Substances 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- 239000004801 Chlorinated PVC Substances 0.000 description 3
- 229920000457 chlorinated polyvinyl chloride Polymers 0.000 description 3
- 241000208340 Araliaceae Species 0.000 description 2
- 235000005035 Panax pseudoginseng ssp. pseudoginseng Nutrition 0.000 description 2
- 235000003140 Panax quinquefolius Nutrition 0.000 description 2
- 235000008434 ginseng Nutrition 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- -1 polyethylene Polymers 0.000 description 2
- 238000012805 post-processing Methods 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 238000007790 scraping Methods 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000006392 deoxygenation reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 238000009832 plasma treatment Methods 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 239000002861 polymer material Substances 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000002787 reinforcement Effects 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000010532 solid phase synthesis reaction Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
- B01J19/12—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electromagnetic waves
- B01J19/122—Incoherent waves
- B01J19/123—Ultraviolet light
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical 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
- B01J8/26—Chemical 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 with two or more fluidised beds, e.g. reactor and regeneration installations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical 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
- B01J8/38—Chemical 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 with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
- B01J8/384—Chemical 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 with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
- B01J8/388—Chemical 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 with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Toxicology (AREA)
- Physics & Mathematics (AREA)
- Electromagnetism (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Abstract
The invention provides an apparatus and process for producing a chlorinated high polymer. According to the invention, plasma or ultraviolet lamps are used to excite chlorine gas so as to prepare the chlorinated high polymer. Under the action of fluidization gas and fluidization-aiding gas, the chlorinated high polymer is produced by a pretreated high polymer under the excitation of plasma or ultraviolet light through stirring and heating, wherein the fluidization gas is composed of pretreated chlorine gas and hydrogen chloride gas or inert gas in proportion. Due to the gradient control of the chlorination reaction heat, two or more fluidized bed reactors are installed in the apparatus and connected by risers which are easy to adjust length and each of which is internally provided with an ultraviolet light tube or a plasma discharging device, wherein the risers are mainly used for exciting reaction gas, prolonging gas activation time, dissipating heat and promoting uniform reaction. The high polymer and the reaction gas circulate between the two fluidized bed reactors through the risers, so the phenomenon of uneven chlorination caused by backmixing occurred in single-bed fluidization can be avoided and the phenomenon of non-smooth movement of materials caused by the height restriction of a high polymer layer can be overcome; and thus, reaction heat is better controlled, and the high polymer meets the requirement of uniform chlorine content.
Description
Technical field
The invention belongs to Chemical Manufacture and manufacture field, especially a kind of device and technique of producing chlorinated high polymers.
Background technology
Existing chlorinated polymeric production technology mainly comprises solwution method, water phase suspension, gas solid method.Produce chlorinated polymeric due to solvent method and can produce organic solvent that is harmful in a large number and heavy damage atmospheric ozone layer, so progressively eliminated by domestic and international manufacturer at present.Water phase suspension production technology is the main method that current most enterprises produces haloflex and chliorinated polyvinyl chloride.But water phase suspension production technology needs a large amount of water body resources as carrier, causes larger waste and pollution to the water source of China water-deficient area, thus developing new clean and effective type production technology is the key solving root problem.Gas solid method is that Corvic is in continuous-flow in circulating fluid bed reactor and riser reactor under dry state situation, carries out degree of depth chlorination obtain chliorinated polyvinyl chloride with chlorine reaction.Gas solid method due to its technique simple, the features such as equipment corrosion is little, and production cost is low are paid close attention to widely.
Existing gas solid method utilizes separately ultraviolet light or plasma-catalytic, is a kind of conventional, promising high polymer chlorination catalytic way.Ultraviolet catalytic can reduce reaction temperature, and energy stabilization, and power consumption is little, and plasma-catalytic reduce further reaction temperature, at room temperature just can catalytic chlorination, but power consumption is higher, more difficult assurance on energy stability.Patent 201010165999.7 proposes and adopts recirculating fluidized bed in riser reactor with the method for the preparing chlorinated polyvinyl chloride by gas-solid phase method of ultraviolet catalytic, only have recirculating fluidized bed and the air inlet of riser reactor two-way, there is no blanking auxiliary air passage, easy generation tremie pipe blocking, uniform blanking is poor; Simultaneously easily there is material air-teturning mixed phenomenon, chlorination uniformity cannot be ensured, due to chlorination value to a certain extent time, this reaction is Fast exothermic process and cannot carry out effective transfer of heat.Patent 200910092928.6 " method of preparing chlorinated polyvinyl chloride by low-temperature plasma circulating fluidize bed and equipment " proposes to adopt low temperature plasma can activate the feature of chlorine and polyvinyl chloride surface simultaneously, the process efficiently exciting chlorinated polyvinyl chloride to react is achieved in down-flow fluidized bed using ECT, and in riser and turbulent bed, realize the process that surperficial chlorine internally rotates migration further, thus be speed two steps by whole chlorination process decoupling zero, production efficiency is obviously better than ultraviolet chlorination and water phase suspension adds chlorine process; But material is in concentrated phase flow regime in descending-bed reactor, solid-gas ratio is high, the chlorine radical that gas is formed after plasma treatment is few, the probability that chlorination reaction occurs is little, add plant maintenance operation, and utilization rate of equipment and installations is low, and plasma relative temperature is high, and this reaction mid-term is Fast exothermic reaction, therefore heat can not effectively shift.Patent 201110061421.1 " method and apparatus of low temperature plasma circulation fluidized bed continuous seepage chliorinated polyvinyl chloride " proposes to adopt low temperature plasma catalysis to produce the method for chliorinated polyvinyl chloride, the quick chlorination of PVC is realized in recirculating fluidized bed, two groups of fluidized-bed reactor operated in turn realize continuous seepage simultaneously, such one is that of avoiding due to reactor shutdowns, the problems such as the production efficiency reduction that discharging brings; Blower fan and exhaust gas processing device etc. can be avoided on the other hand to stop restart, save energy resource consumption, extend equipment life, but also there is material in descending-bed reactor and be in concentrated phase flow regime, solid-gas ratio is high, and the probability that chlorination reaction occurs is little, and chlorination is uneven, material easily blocks, back-mixing, temperature can not effectively control, and increases the workload of plant maintenance simultaneously.
Summary of the invention
The object of this invention is to provide a kind of device and technique of producing chlorinated high polymers, utilize two or more recirculating fluidized bed specifically, with being convenient to regulate length and the inner riser being provided with plasma or uviol lamp connects, by stirring and the combination of fluidized gas device; The riser utilizing two or more inside to be provided with plasma or uviol lamp carries out connection recirculating fluidized bed lower end and top, in conjunction with chuck; Solve the problem such as back-mixing, catalysis time controls, heat transfer, realize chlorination even, heat transfer rapidly, conduct heat that uniformity is consistent, the object of prolongation catalytic action time between particle; Meanwhile, utilize vacuum extractor, achieve the process before and after chloride reaction; Cleaner production, riser have employed circular-gap structure, successfully solves transfer of heat in the transfer of high polymer and course of reaction.
Technical scheme of the present invention is as follows: a kind of device producing chlorinated high polymers, by the fluidized-bed reactor 11 connected successively, riser 9, regulator 13, vacuum plant 12, gas knot screen 8, heating system 6, wherein to be linked in sequence two or more fluidized-bed reactor 11 with riser 9, at high polymer by temperature during polymer reaction effectively can be regulated during riser 9, reacting gas can be made fully to mix with high polymer, the setting of two fluidized-bed reactors 11, make at high polymer after a fluidized-bed reactor 11A to another fluidized-bed reactor 11B, do not remain in First fluidized-bed reactor 11A, thus avoid back-mixing, ensure that the high polymer of same batch catalysis number of times under the catalytic environment of plasma or uviol lamp is identical simultaneously, catalysis time is close as much as possible, regulator 13 is connected in fluidized-bed reactor 11, for regulating the pressure of fluidized-bed reactor 11, vacuum plant 12 is connected in fluidized-bed reactor 11, for providing fluidized-bed reactor 11 negative pressure, gas knot screen 8 is connected in high polymer upstream end, for gas purification, deoxygenation, heating system 6 is connected in fluidized-bed reactor 11 and riser 9, for regulating reaction system thermal balance.
Technical process for said apparatus can be carried out in accordance with the following steps:
A, reacting gas be chlorine, hydrogen chloride gas and inert gas (inert gas namely: the gas not participating in this technological reaction, being called for short inert gas herein) proportioning forms, removal of impurities, deoxidation is carried out, by heating system 6 heated air by gas knot screen 8 pairs of gases; Wherein, chlorine and hydrogen chloride volume proportion are 0.3-0.9; Deoxidation reaches below 500ppm; Gas-heated is to 25-160 DEG C, and Stress control is at 0.01-0.1MPa; Gas by after gas knot screen 8, by fluidized gas device 5 with help gas device 7 to enter reaction system; Fluidized gas device 5 and help gas device 7 to be provided with fluidized gas device.
B, high polymer enter raw material cabin 1 through pretreatment, enter amplification section 2 and fall into fluidized-bed reactor A after oven dry; Wherein, high polymer can be polyethylene, polyvinyl chloride, polypropylene etc.; Pretreated particle diameter is 80-150 μm, and removes the gas of attached collection on particle; After high polymer enters fluidized-bed reactor A, carry out reacting gas displacement, reacting gas is incorporated, attached collection is to particle surface and inside.
C, from fluidized gas device 5 fluidized gas and help gas device 7 help the effect of gas under, utilize stirring 3 fluidisation high polymer, heating system 6 fluid bedreactors 11 chuck carries out being heated to 25-160 DEG C simultaneously, utilize regulator 13, regulate fluidized-bed reactor 11A, the pressure reduction at fluidized-bed reactor 11B two ends, under the effect of pressure reduction, high polymer, by fluidized-bed reactor 11A, enters fluidized-bed reactor 11B by riser 9; Wherein, help gas and high polymer by ultraviolet lamp tube 19 activation being arranged on riser 9 inside, make high polymer generation chlorination; High polymer passes through connect successively two risers 9 arranged, prolongation gas, high polymer soak time, and convenient adjustment, reinforcement heat transfer and promotion polymer reaction are even; Continue the pressure reduction of reconciling fluidized-bed reactor 11A and B, realize high polymer and the circulation of gas between fluidized-bed reactor 11A, B, high polymer in fluidized-bed reactor is all sent into another fluidized-bed reactor 11 by each circulation completely, avoid the generation of single fluidized-bed reactor 11 air-teturning mixed phenomenon, high polymer is at two or more fluidized-bed reactor and promote in-pipe, until high polymer chlorinity reaches requirement, the motion of high polymer is not by the restriction of bed depth, in-pipe can be promoted in two or more, improve chlorination uniformity.
After d, chlorination value reach requirement, utilize vacuum plant 12, fluid bedreactors carries out Negative pressure, removes the residual gas be adsorbed on reactant; After Negative pressure, pass into air, replace; After high polymer be transported to finished product bin 10.
Fluidized-bed reactor 11 as above is in series for two or more, realizes the continuous prodution of high polymer, strengthens heat transfer, avoids the back-mixing of high polymer.
Stirring as above is provided with scrapes wall construction 20 and cooling device 21; Utilization is scraped wall construction and is removed the high polymer be bonded on fluidized-bed reactor 11 inwall, prevents localized hyperthermia from occurring; Refrigerating device inside enhances high polymer heat transfer simultaneously.
Riser 9 as above is annular space structure, and arranges outer tube chuck 18, ensure that the uniformity of high polymer chlorination, strengthens heat transfer and reaction temperature control.
Riser 9 inside as above arranges ultraviolet lamp tube 19, and outer setting outer tube chuck 18, forms annular space between quartz ampoule 17 and outer tube chuck 18.
Riser 9 inside of another kind of form as above arranges electrode 15 in plasma, and outside sets gradually plasma external electrode 16, outer tube chuck 18, and composition, with the riser 9 of plasma discharge apparatus, forms annular space between quartz ampoule 17 and outer tube chuck 18.
Fluidized-bed reactor 11 as above is provided with and amplifies section 2, and in running, bottom is close phase state, and amplifying section is dilute phase state, and riser is also dilute phase, and ultraviolet irradiation district is also dilute phase state, is convenient to ultraviolet and causes catalysis.
Technical process as above, high polymer is by being dilute phase state during riser 9, and chlorination helps gas temperature higher than high polymer temperature early stage, and the chlorination later stage helps gas temperature lower than high polymer temperature.
Technical process as above, helps gas as the high polymer in conveying hoisting pipe 9 and control temperature.
Technical process as above, for ensureing the control of temperature, riser 9 can arrange outer tube chuck 18, for controlling the temperature of high polymer in riser 9.
For solving the problem such as back-mixing, catalysis time controls, heat control, realize chlorination even, heat transfer rapidly, conduct heat that uniformity is consistent, the object of prolongation catalytic action time between particle, the present invention can also by following art scheme: comprise the fluidized-bed reactor 11, riser 9, regulator 13, vacuum plant 12, gas knot screen 8, the heating system 6 that connect successively, wherein to be linked in sequence more than two fluidized-bed reactors 11 with 6 risers 9, riser 9 points two kinds, a kind of riser 14 of interior uviol lamp structure, one does not install ultraviolet lamp tube 19, for extending riser 9, two kinds of risers 9 are separated connection, at high polymer by temperature during polymer reaction effectively can be regulated during riser 9, reacting gas is fully mixed with high polymer, the setting of more than two fluidized-bed reactors 11, make at high polymer after a fluidized-bed reactor 11A to another fluidized-bed reactor 11B, do not remain in the fluidized-bed reactor 11A of foreground, thus avoid back-mixing, ensure that the high polymer of same batch catalysis number of times under the catalytic environment of plasma or uviol lamp is identical simultaneously, catalysis time is close as much as possible, riser 9 outer wall arranges chuck and controls for temperature.Add the nanometer powder that nano-calcium carbonate, nano silicon, nano aluminium oxide etc. can eliminate high polymer electrostatic entering in high polymer in its technical process, all the other are with last scheme.
Device as above, electrode 15, plasma external electrode 16, quartz ampoule 17, outer tube chuck 18 and plasma power supply in plasma, connect composition plasma discharge apparatus, i.e. a kind of circular-gap dielectric barrier discharge plasma generating means successively.
Principle of the present invention is the feature utilizing riser reactor material to be dilute phase, by controlling the flow of riser and helping the temperature of gas air-flow, the stirring structure of fluidized-bed reactor, the setting position of ultraviolet lamp tube, the version of reactor, the process of raw material etc. control the reaction temperature of high polymer particle, thus avoid the quick chlorination of high polymer and produce reunion.
Beneficial effect of the invention process is:
1, after chlorination initial stage and chlorination, all adopt vacuum plant, remove the gas of attached collection in high polymer, further improve chlorination efficiency, and make finished product material without alkali cleaning generic operation, be more conducive to environmental protection.
2, catalytic unit using plasma and ultraviolet light combination, the chlorination initial stage adopts plasma method, reduce further chlorination temperature, and the chlorination later stage adopts ultraviolet method, reduces energy consumption.
3, the riser adopting two or more to combine, and the design of fluidized-bed reactor A, B, strengthen heat radiation and the heat transfer of system, better can control reaction temperature.Extend the reaction time, avoid the single easy temperature runaway of recirculating fluidized bed, the easy back-mixing of high polymer material, reacts unequal shortcoming; And adopt circular-gap project organization and jacket structured, be more conducive to controlling reaction temperature and production scale is amplified.
4, under utilizing dilute phase conditions in chlorination process, temperature control is carried out to the particle in high polymer chlorination process, thus control the temperature of W-response, reach the uniformity needed for material.
Accompanying drawing explanation
Fig. 1 is W-response flow process and reaction unit schematic diagram;
Fig. 2 is riser schematic diagram;
Fig. 3 is riser internal structure schematic diagram;
Fig. 4 is that wall construction and internal heat transfer structural representation are scraped in stirring;
Fig. 5 is many cascaded structure schematic diagrames;
Fig. 6 is flow process and the reaction unit schematic diagram of single fluidised bed reactor;
Fig. 7 is horizontal reacting apparatus schematic diagram.
Drawing reference numeral: 1 is raw material cabin; 2 for amplifying section; 3 for stirring; 4 is reactor jacket; 5 is fluidized gas device; 6 is heating system; 7 for helping gas device; 8 is gas knot screen; 9 is riser; 10 is finished product bin; 11,11A, 11B, 11C, 11D are fluidized-bed reactor, fluidized-bed reactor A, B, C, D; 12 is vacuum plant; 13 is regulator; 14 is the riser of ultraviolet lamp tube structure; 15 is electrode in plasma; 16 is plasma external electrode; 17 is quartz ampoule; 18 is outer tube chuck; 19 is ultraviolet lamp tube; 20 for scraping wall construction; 21 is cooling device; 22 is auger; 23 is horizontal reactor.
Detailed description of the invention
embodiment 1:
With reference to Figure of description 1; Pressurizeed by raw material cabin 1, high polymer falls into fluidized-bed reactor 11A after flowing into and amplifying section 2.Open vacuum plant 12, process is vacuumized to high polymer, remove the gaseous impurity of attached collection on high polymer.The gaseous mixture of chlorine and hydrogen chloride gas or inert gas carries out removal of impurities, deoxidation by device 8, and heating, and gas-heated temperature is 20-130 DEG C.Gas after heating, enters fluidized-bed reactor 11A by fluidized gas device 5, carries out fluidisation to high polymer, and after prechlorination 10-60 minute, open heating system 6, fluid bedreactors and riser heat, and temperature is 20-130 DEG C.By regulator 13 couples of 11A, fluidized-bed reactor 11B carries out pressure adjustment, improves the internal pressure of fluidized-bed reactor 11A.Help gas body to enter into bottom riser by helping gas device 7, under the effect of pressure reduction, powder flows into riser 9, opens plasma discharge apparatus and the ultraviolet lamp tube 19 of riser inside, activates high polymer and gas.After high polymer enters into fluidized-bed reactor 11B completely, change A and B pressure reduction and the direction helping gas, high polymer starts to flow to fluidized-bed reactor 11A, completes a circulation.After high polymer temperature rise is to 60-80 DEG C, open ultraviolet lamp tube, utilize ultraviolet to activate, through repeatedly circulating.After high polymer chlorinity meets the demands, close fluidized gas and help gas, utilize the chlorine that vacuum plant 12 pairs of high polymers adsorb, hydrogen chloride and inert gas carry out removal of impurities.After removal of impurities, pass into air, high polymer inside is filled, after, high polymer is unloaded to finished product bin 10, completes chlorination and removal of impurities.
embodiment 2:
With reference to Figure of description 5; Pressurizeed by raw material cabin 1, high polymer falls into fluidized-bed reactor 11A after flowing into and amplifying section 2.Open vacuum plant 12, process is vacuumized to high polymer, remove the gaseous impurity of attached collection on high polymer.The gaseous mixture of chlorine and hydrogen chloride gas or inert gas carries out removal of impurities, deoxidation by gas knot screen 8, and gas-heated temperature is 25-160 DEG C.Gas after heating, enters fluidized-bed reactor 11A by fluidized gas device 5, carries out fluidisation to high polymer, and after prechlorination 10-60 minute, open heating system 6, fluid bedreactors and riser heat, and temperature is 25-160 DEG C.Carry out pressure adjustment by regulator 13 fluid bedreactors 11A, improve the internal pressure of fluidized-bed reactor A.Help gas body to enter into bottom riser by helping gas device 7, under the effect of pressure reduction, high polymer flows into riser 9, opens plasma discharge apparatus and the ultraviolet lamp tube 19 of riser 9 inside, activates high polymer and gas.After high polymer enters into fluidized-bed reactor 11B completely, continue through and add the good reacting gas of proportioning and carry out fluidisation, reach the internal migration of high polymer chlorination reaction.After fluidized-bed reactor A feeding, continue to be fed to fluidized-bed reactor A from raw material cabin 1, carry out high polymer prechlorination.Regulate fluidized-bed reactor B, the pressure reduction of C, high polymer flows to fluidized-bed reactor 11C by riser 9, and high polymer carries out the internal migration of high polymer chlorination reaction in fluidized-bed reactor C.After, regulate the pressure of fluidized-bed reactor C and fluidized-bed reactor D, complete migration and the fluidisation of high polymer, after chlorination, undertaken vacuumizing process by vacuum plant 12 fluid bedreactors D, remove the remaining hydrogen chloride of attached collection on high polymer and chlorine.Pass into air, after completing displacement, high polymer is squeezed into finished bin 10.Repeat above-mentioned steps, realize continuous prodution.
embodiment 3:
With reference to Figure of description 1 and 2; The difference of embodiment 3 and embodiment 1,2 is the structure of riser 9, a riser 14 being ultraviolet lamp tube mechanism, another is electrode 15 and plasma external electrode 16 and quartz ampoule 17 in plasma, outer tube chuck 18 forms circular-gap plasma producing apparatus as shown in Figure of description 2,3.
embodiment 4:
With reference to Figure of description 1-5, the present embodiment and above embodiment difference are: to the pretreatment of high polymer, removal of impurities, screening, heating were all carried out before entering fluidized-bed reactor 11A, riser 9 is linked in sequence 5 fluidized-bed reactors 11, high polymer is from entering after First fluidized-bed reactor 11 proceeding through riser 9 and subsequent fluidized bed reactor 11, carry out post processing after reaching chlorination requirement, then enter finished product bin 10.When First high polymer enters second or a follow-up arbitrary fluidized-bed reactor 11 completely, the high polymer that pretreatment completes can enter fluidized-bed reactor 11 successively, thus reaches continuous seepage.
embodiment 5:
With reference to Figure of description 6, the pretreatment of the present embodiment high polymer is arbitrary identical with embodiment 1-4 with post processing, unlike only connecting with riser 9 with a fluidized-bed reactor 11, high polymer from fluidized-bed bottom out, by riser 9 under the effect helping gas device 7, enter from the top of fluidized-bed reactor 11, through the circulation of appropriate time and the control of temperature, undertaken vacuumizing process by vacuum plant 12 fluid bedreactors 11, remove the remaining hydrogen chloride of attached collection on high polymer and chlorine.Pass into air, after completing displacement, high polymer is squeezed into finished bin 10.
embodiment 6:
With reference to Figure of description 2,3,4,6, the present embodiment comprise connect successively 1, raw material cabin, 5, fluidized gas device, 6, heating system, 7, gas device is helped, 8, gas knot screen, 9, riser, 10, finished product bin, 11, fluidized-bed reactor, (namely ultraviolet lamp tube 19 is not installed in riser 9 inside wherein to use circular-gap riser, only quartz ampoule 17 is installed) connect the outlet at bottom of fluidized-bed reactor 11 and top inlet, ultraviolet lamp tube 19 is arranged on fluidized-bed reactor 11 inwall, gas device 7 constant temperature gas is out helped to carry high polymer secretly by riser 9, high polymer helps gas and high polymer particle fully to mix when flowing in riser 9, temperature during gas regulation high polymer particle reaction with constant temperature, fluidized-bed reactor inside arranges stirring 3, stirring 3 is provided with and scrapes wall construction 20 and cooling device 21, make high polymer be unlikely to overheated and be bonded on the wall of fluidized-bed reactor 11.Raw material cabin 1 pressurizes by its technical process, and high polymer falls into fluidized-bed reactor 11 after flowing into and amplifying section 2.The gaseous mixture of chlorine and hydrogen chloride gas or inert gas carries out removal of impurities, deoxidation by gas knot screen 8, and gas-heated temperature is 25-160 DEG C.Gas after heating, enters fluidized-bed reactor 11 by fluidized gas device 5, carries out fluidisation to high polymer, and after prechlorination 10-60 minute, open heating system 6, fluid bedreactors and riser heat, and temperature is 25-160 DEG C.Help gas body to enter into bottom riser by helping gas device 7, under the effect of pressure reduction, high polymer flows into riser 9, opens ultraviolet lamp tube 19, activates high polymer and gas.Continue through and add the good reacting gas of proportioning and carry out fluidisation, reach the internal migration of high polymer chlorination reaction.High polymer in fluidized-bed reactor 11 from lower end through riser 9, continuous print flow into upper inlet, until complete migration and the fluidisation of high polymer, utilize riser 9 and pass through fluidized gas control reaction temperature, reaction rate; After chlorination, remove the remaining hydrogen chloride of attached collection on high polymer and chlorine.Pass into air, after completing displacement, high polymer is squeezed into finished bin 10.Repeat above-mentioned steps, realize continuous prodution.
embodiment 7:
With reference to Figure of description 2,3,4,6, the difference of the present embodiment and embodiment 6 is, ultraviolet lamp tube 19 is used instead as uviol lamp pearl, multiplely be arranged on the blade scraping wall construction 20 of stirring, its technical process is similar to embodiment 6, unlike for control temperature that reaction temperature helps gas in the reaction the later stage lower than the temperature of fluidized-bed reactor 11, the materials such as nano silicon, nano-calcium carbonate, nano aluminium oxide are added in high polymer raw material, for eliminating the electrostatic that high polymer produces, prevent the generation of sticky wall.Technical process is with embodiment 6.
embodiment 8:
The present invention can also provide following embodiment, and reactor wall arranges ultraviolet lamp tube 9 specifically, with being convenient to regulate the riser 9 of length to connect, by stirring the combination of 3 and fluidized gas device 5; Utilize two or more riser 9, connect recirculating fluidized bed lower end and top, solve the problems such as back-mixing, catalysis time controls, heat transfer, realize chlorination even, heat transfer rapidly, conduct heat that uniformity is consistent, the object of prolongation catalytic action time between particle; Meanwhile, utilize vacuum extractor 12, achieve the process before and after chloride reaction, cleaner production; Riser have employed circular-gap structure, improves the area of dissipation in riser, accelerates the movement velocity of high polymer in riser, successfully solves transfer of heat in the transfer of high polymer and course of reaction.With embodiment 6 in technical process, unlike adding the materials such as nano silicon, nano-calcium carbonate, nano aluminium oxide in high polymer, for eliminating the electrostatic that high polymer produces, preventing the generation of sticky wall, solving material uniformity.
Embodiment 9:
Ginseng Figure of description 7, the present invention can also provide following embodiment, and the inwall of reactor dilute-phase zone arranges the horizontal reactor 23 of ultraviolet lamp tube 19 specifically, by the combination of auger 22 and fluidized gas device 5; Solve the problem such as back-mixing, catalysis time controls, heat transfer, realize chlorination even, heat transfer rapidly, conduct heat that uniformity is consistent, the object of prolongation catalytic action time between particle; Meanwhile, utilize vacuum extractor 12, realize the process before and after chloride reaction, cleaner production; Raw material cabin 1 pressurizes by technical process, and high polymer flows into horizontal reactor, opens vacuum plant 12, vacuumizes process to high polymer, removes the gaseous impurity of attached collection on high polymer.The gaseous mixture of chlorine and hydrogen chloride gas or inert gas carries out removal of impurities, deoxidation by device 8, and heating, and gas-heated temperature is 20-130 DEG C.Gas after heating, enters horizontal reactor by fluidized gas device 5, carries out fluidisation to high polymer, after prechlorination 10-60 minute, opens heating system 6, heats horizontal reactor, and temperature is 20-130 DEG C.Open reactor ultraviolet lamp tube 19, high polymer and gas are activated.Under the effect of auger 22 power, high polymer continuous print moves from left to right, continuous chlorination, and the high polymer of low order end enters knot screen, after removal of impurities, high polymer is unloaded to finished product bin 10, completes chlorination and removal of impurities.In this embodiment, the setting of horizontal reactor makes material in a reactor, can have emulsion zone again by existing dilute-phase zone, and catalysis and reaction is solved in same reactor, ultraviolet is arranged on dilute-phase zone, auger 22 and fluidized gas device 5 is utilized to solve the problem of chlorination uniformity, thus it is large to avoid vertical reactor installation difficulty, invest high, the problem that equipment is many, its technique continuous and stable production can also be made.
Embodiment 10:
Ginseng Figure of description 7, embodiments of the present invention as different from Example 9, auger 22 leaf arrange uviol lamp pearl, are stirring limit by under the effect of ultraviolet irradiation, prevent material because of the problem of ultraviolet irradiation generation adhesion uviol lamp wall; Its technical process is identical with embodiment 9.
Claims (10)
1. produce a device for chlorinated high polymers, this device comprises: the fluidized-bed reactor connected successively, riser, regulator, vacuum plant, gas knot screen, heating system; It is characterized in that being linked in sequence two or more fluidized-bed reactor with the riser of jacketed, regulator is connected in fluidized-bed reactor, vacuum plant is connected in fluidized-bed reactor, gas knot screen is connected in high polymer upstream end, heating system is connected in fluidized-bed reactor and riser, and plasma and uviol lamp are arranged on riser inside.
2. the technique for device described in claim 1 is:
A, be heated to 25-160 DEG C, by arranging the fluidized gas device of fluidized gas device and helping gas device to enter reaction system after the chlorine of 0.3-0.9 and hydrogen chloride gas carry out deoxidation removal of impurities by volume ratio;
B, through pretreatment and dry after high polymer enter amplify section fall into fluidized-bed reactor A, carry out reacting gas displacement, make gas incorporate attached collection to high polymer particle surface and inside;
C, fluidized gas and help gas effect under, utilize agitating device fluidisation high polymer, heating system fluid bedreactors chuck heats simultaneously, opening regulator makes fluidized-bed reactor A and fluidized-bed reactor B produce pressure reduction, high polymer, by fluidized-bed reactor A, enters fluidized-bed reactor B by the riser of jacketed; By the plasma or ultraviolet lamp tube that are arranged on riser inside, arbitrary or the two activation helps gas and high polymer, makes high polymer generation chlorination; By riser, extend gas and high polymer soak time, strengthen heat transfer and promote that polymer reaction is even; Continue the pressure reduction regulating fluidized-bed reactor A and B, realize high polymer at fluidized-bed reactor A, circulation between B, high polymer in fluidized-bed reactor is all sent to another fluidized-bed reactor by each circulation completely, high polymer is at two or more fluidized-bed reactor and promote in-pipe, until high polymer chlorinity reaches requirement;
After d, chlorination value reach requirement, remove the residual gas be adsorbed on high polymer, then replace, go out finished product.
3., by a kind of device producing chlorinated high polymers according to claim 1, it is characterized in that fluidized-bed reactor is two or more being in series, realize the continuous prodution of high polymer.
4., by a kind of device producing chlorinated high polymers according to claim 1, it is characterized in that stirring is provided with and scrape wall construction and cooling device; Utilization is scraped wall device and is removed the high polymer be bonded on fluidized-bed reactor inwall, prevents localized hyperthermia from occurring; Cooling device enhances the heat transfer of high polymer simultaneously.
5. by a kind of device producing chlorinated high polymers according to claim 1, it is characterized in that riser inside arranges ultraviolet lamp tube, outer setting outer tube chuck, be annular space structure, ensure that the uniformity of high polymer chlorination, strengthen heat transfer and reaction temperature control.
6., by the arbitrary described a kind of device producing chlorinated high polymers of claim 1,5, it is characterized in that riser inside arranges electrode in plasma, outside sets gradually plasma external electrode, outer tube chuck.
7. by a kind of technique of producing chlorinated high polymers according to claim 2, fluidized-bed reactor is provided with amplification section, and in running, bottom is close phase state, and amplifying section is dilute phase state, and riser is dilute phase state.
8., by a kind of technique of producing chlorinated high polymers according to claim 2, high polymer is by being dilute phase state during riser, and chlorination helps gas temperature higher than high polymer temperature early stage, and the chlorination later stage helps gas temperature lower than high polymer temperature.
9., by a kind of technique of producing chlorinated high polymers according to claim 2, for ensureing the control of temperature, riser can arrange outer tube chuck, for controlling the temperature of high polymer in riser.
10. by a kind of technique of producing chlorinated high polymers according to claim 2, before chlorination starts, adding the arbitrary or two or more material of nano silicon, nano-calcium carbonate, nano aluminium oxide in high polymer raw material, for eliminating the electrostatic that high polymer produces, preventing high polymer from gluing the generation of wall.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410308204.1A CN104607114B (en) | 2014-07-01 | 2014-07-01 | Apparatus and process for producing chlorinated high polymer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410308204.1A CN104607114B (en) | 2014-07-01 | 2014-07-01 | Apparatus and process for producing chlorinated high polymer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104607114A true CN104607114A (en) | 2015-05-13 |
| CN104607114B CN104607114B (en) | 2017-02-15 |
Family
ID=53141918
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410308204.1A Active CN104607114B (en) | 2014-07-01 | 2014-07-01 | Apparatus and process for producing chlorinated high polymer |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104607114B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109580716A (en) * | 2018-11-23 | 2019-04-05 | 浙江大学 | The recognition methods of recirculating fluidized bed raising section gas-solid flow pattern based on electrostatic detection |
| CN109745937A (en) * | 2019-03-19 | 2019-05-14 | 福州大学 | A kind of photocatalysis fluid bed device of two dimension |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE69110349D1 (en) * | 1990-05-15 | 1995-07-20 | Exxon Research Engineering Co | Catalyst distribution system for regenerators of FCC plants. |
| CN101754801A (en) * | 2007-07-17 | 2010-06-23 | 埃克森美孚研究工程公司 | Reduced elevation catalyst return line for a fluid catalytic cracking unit |
| CN101831021A (en) * | 2010-05-10 | 2010-09-15 | 河北科技大学 | Device for preparing chlorinated polyvinyl chloride by gas-solid phase method and method thereof |
| CN202016967U (en) * | 2011-03-15 | 2011-10-26 | 清华大学 | Device for continuously producing chlorinated poly vinyl chloride (PVC) through low-temperature plasma circulating bed |
| CN202671471U (en) * | 2012-07-06 | 2013-01-16 | 新疆天业（集团）有限公司 | Device for preparing chlorinated polyvinyl chloride by plasma gas solid phase method |
| CN102872772A (en) * | 2011-07-12 | 2013-01-16 | 中国石油化工股份有限公司 | Reaction unit for co-producting dimethyl ether and ethene by using methanol and ethanol as raw materials |
| CN103347601A (en) * | 2010-11-05 | 2013-10-09 | 国际热化学恢复股份有限公司 | Solids circulation system and method for capture and conversion of reactive solid |
-
2014
- 2014-07-01 CN CN201410308204.1A patent/CN104607114B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE69110349D1 (en) * | 1990-05-15 | 1995-07-20 | Exxon Research Engineering Co | Catalyst distribution system for regenerators of FCC plants. |
| CN101754801A (en) * | 2007-07-17 | 2010-06-23 | 埃克森美孚研究工程公司 | Reduced elevation catalyst return line for a fluid catalytic cracking unit |
| CN101831021A (en) * | 2010-05-10 | 2010-09-15 | 河北科技大学 | Device for preparing chlorinated polyvinyl chloride by gas-solid phase method and method thereof |
| CN103347601A (en) * | 2010-11-05 | 2013-10-09 | 国际热化学恢复股份有限公司 | Solids circulation system and method for capture and conversion of reactive solid |
| CN202016967U (en) * | 2011-03-15 | 2011-10-26 | 清华大学 | Device for continuously producing chlorinated poly vinyl chloride (PVC) through low-temperature plasma circulating bed |
| CN102872772A (en) * | 2011-07-12 | 2013-01-16 | 中国石油化工股份有限公司 | Reaction unit for co-producting dimethyl ether and ethene by using methanol and ethanol as raw materials |
| CN202671471U (en) * | 2012-07-06 | 2013-01-16 | 新疆天业（集团）有限公司 | Device for preparing chlorinated polyvinyl chloride by plasma gas solid phase method |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109580716A (en) * | 2018-11-23 | 2019-04-05 | 浙江大学 | The recognition methods of recirculating fluidized bed raising section gas-solid flow pattern based on electrostatic detection |
| CN109580716B (en) * | 2018-11-23 | 2020-10-30 | 浙江大学 | Method for identifying gas-solid flow pattern of lifting section of circulating fluidized bed based on electrostatic detection |
| CN109745937A (en) * | 2019-03-19 | 2019-05-14 | 福州大学 | A kind of photocatalysis fluid bed device of two dimension |
| CN109745937B (en) * | 2019-03-19 | 2021-03-02 | 福州大学 | Two-dimensional photocatalytic fluidized bed device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104607114B (en) | 2017-02-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103608633B (en) | The drying means of moist polymer powder and the device being suitable for described method | |
| WO2011009252A1 (en) | Chemical reactor and its usage in chemical reaction | |
| CN107384449B (en) | Pyrolysis system and pyrolysis method for gas, liquid and solid materials | |
| CN104607114A (en) | Apparatus and process for producing chlorinated high polymer | |
| CN106635114B (en) | Device and method for realizing co-production of catalytic cracking oil gas by waste rubber powder in fluidized state | |
| CN1767893A (en) | Method and plant for the conveyance of fine-grained solids | |
| CN107088387B (en) | Integrated tower type circulating flow reactor applied to fine chemical production and production method | |
| CN102161718B (en) | Method and device for continuously producing chlorinated polyvinyl chloride by low-temperature plasma circulating bed | |
| CN101654493B (en) | Method for preparing chlorinated polyvinyl chloride by low-temperature plasma circulating fluidize bed and device | |
| CN101759819B (en) | Device for preparing chlorosulfonated polyethylene by gas-solid phase method | |
| CN202671471U (en) | Device for preparing chlorinated polyvinyl chloride by plasma gas solid phase method | |
| CN108706786A (en) | A kind of semi-fluidized bed formula Fenton oxidation wastewater treatment equipment | |
| CN210511726U (en) | Organic pollution medium processing apparatus of continuous smoldering reaction | |
| CN112742185B (en) | Flue gas desulfurization reactor, flue gas treatment system and process method | |
| CN208771389U (en) | Continuous reaction apparatus and system | |
| CN106082576A (en) | A kind of low temperature continuous pyrolysis processes mud fixed bed reactors and method | |
| CN207121570U (en) | A kind of pyrolysis system for three kinds of state materials of gas, liquid, solid | |
| CN102674716A (en) | Cyclic calcining and decomposing process for powdered materials | |
| CN105837435B (en) | A kind of method that continuous esterification prepares compounding acetic isoborneol ester | |
| CN101649010B (en) | Spouted bed reactor and method thereof for synthesizing chlorinated polyvinyl chloride by using low-temperature plasmas | |
| CN202016967U (en) | Device for continuously producing chlorinated poly vinyl chloride (PVC) through low-temperature plasma circulating bed | |
| CA2812275A1 (en) | Systems and methods for separating mine tailings from water-absorbing polymers and regenerating the separated water-absorbing polymers | |
| CN105885891A (en) | Self-heating type biomass fluidization bed rapid pyrolysis process | |
| CN102199230A (en) | Multilayer bed reactor and method for synthesizing chlorinated polyvinyl chloride by using low temperature plasmas | |
| CN105536643A (en) | Ceramic powder granulation processing device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |