CN110615405B - Multistage fluidized bed series-connected continuous production system and production method for dichlorine monoxide - Google Patents
Multistage fluidized bed series-connected continuous production system and production method for dichlorine monoxide Download PDFInfo
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- CN110615405B CN110615405B CN201810629434.6A CN201810629434A CN110615405B CN 110615405 B CN110615405 B CN 110615405B CN 201810629434 A CN201810629434 A CN 201810629434A CN 110615405 B CN110615405 B CN 110615405B
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- 238000010924 continuous production Methods 0.000 title claims abstract description 36
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 22
- RCJVRSBWZCNNQT-UHFFFAOYSA-N dichloridooxygen Chemical compound ClOCl RCJVRSBWZCNNQT-UHFFFAOYSA-N 0.000 title claims description 70
- 238000006243 chemical reaction Methods 0.000 claims abstract description 69
- 238000003756 stirring Methods 0.000 claims abstract description 44
- 239000000463 material Substances 0.000 claims abstract description 28
- 238000005243 fluidization Methods 0.000 claims abstract description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 208
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 104
- 239000000460 chlorine Substances 0.000 claims description 38
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 37
- 229910052801 chlorine Inorganic materials 0.000 claims description 37
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 24
- 239000007787 solid Substances 0.000 claims description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 239000000843 powder Substances 0.000 claims description 19
- 238000003860 storage Methods 0.000 claims description 15
- 239000011780 sodium chloride Substances 0.000 claims description 12
- 239000002245 particle Substances 0.000 claims description 10
- 238000000034 method Methods 0.000 claims description 9
- 239000002994 raw material Substances 0.000 claims description 9
- 230000005484 gravity Effects 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 4
- 239000012495 reaction gas Substances 0.000 abstract description 11
- 239000011343 solid material Substances 0.000 abstract description 10
- 230000009471 action Effects 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 230000002035 prolonged effect Effects 0.000 abstract description 2
- 125000003963 dichloro group Chemical group Cl* 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 58
- 238000009826 distribution Methods 0.000 description 8
- 238000000926 separation method Methods 0.000 description 8
- 239000000047 product Substances 0.000 description 5
- 230000000903 blocking effect Effects 0.000 description 4
- 239000000498 cooling water Substances 0.000 description 4
- 239000007790 solid phase Substances 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 3
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000007710 freezing Methods 0.000 description 2
- 230000008014 freezing Effects 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000003960 organic solvent Substances 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- VZGDMQKNWNREIO-UHFFFAOYSA-N tetrachloromethane Chemical compound ClC(Cl)(Cl)Cl VZGDMQKNWNREIO-UHFFFAOYSA-N 0.000 description 2
- DEWLEGDTCGBNGU-UHFFFAOYSA-N 1,3-dichloropropan-2-ol Chemical compound ClCC(O)CCl DEWLEGDTCGBNGU-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- YGYAWVDWMABLBF-UHFFFAOYSA-N Phosgene Chemical compound ClC(Cl)=O YGYAWVDWMABLBF-UHFFFAOYSA-N 0.000 description 1
- 150000008065 acid anhydrides Chemical class 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000012320 chlorinating reagent Substances 0.000 description 1
- 150000007973 cyanuric acids Chemical class 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- MQRJBSHKWOFOGF-UHFFFAOYSA-L disodium;carbonate;hydrate Chemical compound O.[Na+].[Na+].[O-]C([O-])=O MQRJBSHKWOFOGF-UHFFFAOYSA-L 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- QWPPOHNGKGFGJK-UHFFFAOYSA-N hypochlorous acid Chemical compound ClO QWPPOHNGKGFGJK-UHFFFAOYSA-N 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B11/00—Oxides or oxyacids of halogens; Salts thereof
- C01B11/02—Oxides of chlorine
- C01B11/021—Chlorine hemioxide (Cl2O)
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a continuous production system and a production method for dichloro in series connection with multiple stages of fluidized beds, wherein the continuous production system comprises the multiple stages of fluidized beds in series connection, the fluidized beds are sequentially arranged from high to low, each stage of fluidized bed is connected with a cyclone separator, a stirring paddle is arranged in each fluidized bed, a flow deflector is arranged on the stirring paddle, fluidization of solid materials is realized through the stirring of the stirring paddle and the cooperation of reaction gas, and the reaction gas forms spirally-rising airflow through the actions of the stirring paddle and the flow deflector, so that the energy consumption of equipment is reduced, and the hardening of the solid materials is avoided; the solid material flows from top to bottom, and the reaction gas moves from bottom to top, so that the contact time of the solid material and the reaction gas is greatly prolonged, and the yield of the conversion rate of the material and the product is improved; the invention has the advantages of high material conversion rate, low power consumption, difficult hardening of solid materials and the like.
Description
Technical Field
The invention relates to the technical field of chemical production, in particular to a continuous production system and a continuous production method for dichlorine monoxide with a series of multistage fluidized beds.
Background
Dichlorine monoxide of the formula Cl 2 O, which is a brown yellow gas at normal temperature and normal pressure and is the acid anhydride of hypochlorous acid; can be dissolved in carbon tetrachloride for storage, is commonly used for strong oxidants and chlorinating agents, and is commonly used for the production of chlorinated isocyanuric acid in industry; in the prior art, chlorine is often reacted with moist sodium carbonate, and the principle is that a mixed gas of chlorine and air is made to pass through a solid sodium carbonate powder layer to generate a mixed gas of dichlorine monoxide, air and carbon dioxide.
Chinese patent publication No. CN106946225a discloses a fluidized bed apparatus and method for producing dichlorine monoxide in 2017, 7 months and 14 days, the fluidized bed apparatus includes: the fluidized bed reactor comprises a gas inlet, a solid inlet, a product outlet, a distribution plate and a finger-shaped pipe; a cyclone separator having an inlet connected to the product outlet of the fluidized bed reactor. The method for producing the dichlorine monoxide by adopting the fluidized bed device comprises the following steps: a reaction stage: introducing the mixed gas containing chlorine into a fluidized bed reactor, and allowing the mixed gas containing chlorine to pass through the hydrated sodium carbonate in a fluidized state for reaction to obtain a gas product carrying solids; a separation stage: solids in the solids-laden gaseous product from the fluidized-bed reactor are separated off by means of a cyclone to give a gas containing dichlorohydrin. The fluidized bed device provided by the invention is used for producing the dichlorine monoxide, water and an organic solvent are avoided being used through a gas-solid reaction, water resources are saved, environmental pollution is avoided, no waste water is generated, and the fluidized bed device is green, environment-friendly and energy-saving.
Although the fluidized bed device disclosed by the patent can improve the conversion rate of sodium carbonate, continuous industrial production is realized, the defect that a large amount of water and organic solvent are required by using the traditional process is overcome, and the purposes of environmental protection, energy conservation, economy and continuous production are realized; however, such production devices still have disadvantages, the main drawbacks of which are: 1. the reaction residence time is short, and the one-way reaction efficiency is low; 2. the byproduct sodium chloride and a large amount of unreacted sodium carbonate need to be discharged from the top of the bed together with reaction gas, and return to the fluidized bed for circular reaction after two-stage cyclone separation, so that a large amount of power is consumed; 3. because the gas velocity of the fluidized bed is certain, sodium carbonate solid containing a small amount of water or generated sodium chloride and unreacted sodium carbonate are wrapped to inevitably form large-particle solid, the solid is larger than the buoyancy of ascending gas and inevitably falls to the bottom of the fluidized bed, partial solid residue accumulated at the bottom of the fluidized bed or agglomeration inevitably causes uneven gas flow distribution, so that the periodic reaction effect of the fluidized bed is easily poor, the total conversion rate of sodium carbonate is poor, and the tube array of the fluidized bed is easy to wear, thereby endangering the production safety; 4. since sodium carbonate contains a small amount of water, sodium chloride has some deliquescence, and thus the mixture thereof may adhere to the surfaces of the tubes or equipment, causing caking, especially when the machine is frequently started and stopped, and being more prone to clogging.
Disclosure of Invention
Aiming at the defects that the blockage of a distribution plate and a finger-shaped Kong Yi in the prior art needs frequent maintenance, the reaction time is short, the material conversion rate is low, the power consumption is high, the material is easy to harden, the product yield is low and the like, the invention provides a continuous production system of dichlorine monoxide with a multistage fluidized bed connected in series, the conversion rate of sodium carbonate and the yield of chlorine can be effectively improved by adopting the system, and the system also has the advantages of automatic separation of solid raw materials, difficulty in hardening, low power consumption and the like.
The invention realizes the purpose through the following technical scheme:
a multistage fluidized bed tandem continuous production system for dichlorine monoxide is characterized in that: the fluidized bed comprises a plurality of fluidized beds which are sequentially connected in series from high to low, and a discharge hole of a fluidized bed at a high position in two adjacent fluidized beds is higher than a feed hole of a fluidized bed at a low position; the fluidized beds at all levels are connected with cyclone separators, the discharge port of each cyclone separator is connected with the material return port of the fluidized bed at the level, and the exhaust port of each cyclone separator is connected with the air inlet of the fluidized bed at the upper level; the fluidized bed at the highest position is connected with a feeding tank, and the fluidized bed at the lowest position is connected with an air compressor and a chlorine storage tank; the outer surface of the fluidized bed is also provided with a half-pipe cooler, and the half-pipe cooler is connected with a chilled water unit; still be provided with the stirring rake in the fluidized bed at each level, the both sides of stirring rake are provided with the water conservancy diversion piece.
The flow deflector is obliquely arranged in a direction deviating from the axis of the fluidized bed, and the oblique angle is 5-10 degrees.
An interstage cooler is further arranged at an exhaust port of the cyclone separator, an inlet cooler is further arranged at the air inlet of the fluidized bed positioned at the bottom, and the interstage cooler and the inlet cooler are both connected with a water chiller.
Control valves for controlling material discharge are arranged between the cyclone separators and the fluidized beds among the fluidized beds at all levels, and the control valves are butterfly valves, knife-shaped valves or plunger valves.
Correspondingly, the invention also discloses a method for producing the dichlorine monoxide by using a dichlorine monoxide production system with a series of multistage fluidized beds, which is characterized by comprising the following steps:
A. a feeding stage: introducing a small amount of compressed air into the fluidized bed, adding sodium carbonate powder into the fluidized bed through a material storage tank positioned at the top, opening a butterfly valve between each stage of fluidized bed to uniformly distribute the sodium carbonate in each stage of fluidized bed through gravity, and simultaneously starting a stirring paddle to fluidize the sodium carbonate in each stage of fluidized bed;
B. an initial reaction stage: introducing mixed gas containing chlorine into the fluidized bed at the lowest position to react the mixed gas with the sodium carbonate in a fluidized state; after the mixed gas reacted in the lowest-stage fluidized bed is separated by the cyclone separator, the gas enters the upper-stage fluidized bed to continuously react with fluidized sodium carbonate, and the solid particles obtained by separation return to the fluidized bed; simultaneously opening an inlet cooler and an interstage cooler for cooling;
C. and (3) a continuous production stage: when the exhaust port of the cyclone separator connected with the highest fluidized bed detects the dichlorine monoxide, the chlorine content of the mixed gas is gradually increased; when the temperature in the lowest stage fluidized bed is reduced or is close to the temperature of the raw material mixed gas, discharging partial sodium chloride through a control valve at the bottom, and supplementing corresponding sodium carbonate into the highest stage fluidized bed according to a corresponding molar ratio; meanwhile, solid materials are transferred downwards step by step from the fluidized bed at the highest position through the control valve, continuous feeding and continuous discharging are achieved, and continuous and stable operation of the whole system is further achieved.
The compressed air flow rate of the feeding stage is 0.1-0.9 m/s, and the preferable flow rate is 0.3-0.6m/s.
The chlorine content of the mixed gas in the initial reaction stage is 1% -4%, and the chlorine content of the mixed gas in the continuous production stage is 3% -15%, preferably 4% -9%; the reaction temperature in each fluidized bed of the initial reaction stage and the continuous production stage is-5-10 ℃, and the preferable temperature is 3-8 ℃.
The pressure in each fluidized bed of the initial reaction stage and the continuous production stage is 0.01Mpa-0.1Mpa, preferably 0.02 Mpa-0.05 Mpa; the rotating speed of the stirring paddle in each fluidized bed in the initial reaction stage and the continuous production stage is 60-120rpm/min.
The adding amount of sodium carbonate in each stage of fluidized bed occupies 7-15% of the volume of the fluidized bed; the bulk density of the sodium carbonate is 0.732g/ml-0.850g/ml; the water content of the sodium carbonate is 5-10%, and the preferable water content of the sodium carbonate is 6-7%.
Compared with the prior art, the invention has the following beneficial effects:
1. the fluidized bed adopted by the dichloro-carbon monoxide production system is internally provided with the stirring paddle, and fluidization is formed in a mode of combining the stirring paddle and the airflow, so that the overhigh requirements on the flow rate and the flow velocity of the reaction gas and the distribution plate are reduced, the power consumption is reduced on one hand, the material loss or the reduction of the reaction efficiency caused by the sudden change of the flow velocity of the gas is avoided, and the reaction is more stable; on the other hand, the requirement of the reaction on the particle size of the material is reduced, the application range of the material is expanded, the production cost is reduced, and the requirement on the precision of the airflow distributor due to the change of the production load is reduced; simultaneously the stirring rake can effectively aggravate the collision between solid phase materials such as sodium carbonate at the in-process of stirring, prevents that sodium carbonate and reaction from generating the sodium chloride caking and on being attached to the pipeline of equipment to improve the protection effect to equipment, prolong the life of equipment, still avoided simultaneously because of the material reaction scheduling problem that large granule material deposit arouses in the fluidized bed bottom inadequately, improved the conversion rate of material.
2. The guide vanes are arranged on two sides of the stirring paddle, the guide vanes are inclined by 5-10 degrees in the direction deviating from the axis of the fluidized bed, and the guide vanes can effectively prevent reaction gas flow from forming vortex on the surface of the stirring paddle, so that the effect of spiral gas flow formed by the reaction gas under the action of the stirring paddle is improved, the energy consumption is further reduced, and the continuity and the stability of system production are ensured.
3. The invention adopts a mode of multistage series fluidized bed reactors to generate the dichlorine monoxide, the solid material enters from the fluidized bed at the highest layer, and the gas enters from the fluidized bed at the lowest layer, thereby realizing the reverse contact reaction of the powder and the gas, prolonging the contact time of the solid material and the reaction gas, and improving the reaction quality; compared with the traditional fluidized bed, the invention realizes the natural separation of gas-phase materials and solid-phase materials, reduces the load of a cyclone separator and the fluidized bed, and simultaneously can improve the concentration of chlorine gas introduced into the fluidized bed, thereby greatly improving the conversion rate of sodium carbonate.
4. The invention adopts a multi-stage series connection mode to generate the dichlorine monoxide, solid phase raw materials enter from the top and are discharged from the bottom, and gas phase raw materials enter from the bottom and are discharged from the top, so that the solid phase materials in a fluidized bed at the top are mainly sodium carbonate, the middle stages are a mixture of the sodium carbonate and sodium chloride, the fluidized bed at the lowest position is mainly sodium chloride, and the solid materials such as the sodium carbonate and the like move from top to bottom under the action of gravity and are finally discharged; the inverted matching relationship between the concentration of the sodium carbonate and the concentration of the chlorine ensures that the sodium carbonate which is not reacted in the previous stage can continuously contact and react with the chlorine in the fluidized bed in the next stage and fully react, thereby greatly prolonging the contact time and reaction efficiency of the sodium carbonate and the chlorine and improving the conversion rate of the sodium carbonate and the chlorine; meanwhile, the invention can control the discharge time and discharge amount of materials through the control valve at the bottom of each stage of fluidized bed, thereby controlling the effective residence time of the sodium carbonate in the fluidized bed, changing the problems of short residence time and low single-pass conversion rate caused by the reaction time determined by the air velocity of the traditional fluidized bed, realizing optimized production and being beneficial to improving the conversion rate of the sodium carbonate and the yield of the dichlorine monoxide.
5. On one hand, the fluidized bed at each stage is connected with the cyclone separator, so that solid particles at the outlet of each stage can be recovered and returned to the bottom of the reactor at the same stage for reaction, and the conversion rate of solid materials is improved; on the other hand, the solid particles are prevented from hardening in the cooler when passing through the cooler, so that the cooler is blocked to influence the passing of air flow, the service life of the equipment is prolonged, the continuous operation of the equipment is ensured, and the reaction efficiency is improved.
6. The invention is provided with the inlet cooler and the interstage cooler, and can effectively remove reaction heat, thereby controlling the temperature of the reaction gas in the fluidized bed and between the fluidized beds at different levels, ensuring the temperature of the reaction gas to be always in the optimal reaction state, avoiding the decomposition of the dichlorine monoxide caused by high temperature, and improving the yield of the dichlorine monoxide and the conversion rate of sodium carbonate.
Drawings
FIG. 1 is a schematic view of a production system of the present invention;
reference numerals: 1. fluidized bed, 2, cyclone separator, 3, feed tank, 4, air compressor, 5, chlorine storage jar, 6, half-pipe cooling tube, 7, refrigerated water unit, 8, stirring rake, 9, water conservancy diversion piece, 10, interstage cooler, 11, entry cooler, 12, control valve, 13, driving motor.
Detailed Description
The invention will be further illustrated by the following specific examples:
example 1
The embodiment is a preferred embodiment of the invention, and discloses a continuous production system of dichloro monoxide with multiple fluidized beds connected in series, the specific structure of which is shown in fig. 1, the system comprises 2 stages of fluidized beds 1 connected in series, the adjacent fluidized beds 1 are connected in series in a manner that a discharge port of the upper stage fluidized bed 1 is connected with a feed port of the lower stage fluidized bed 1, the fluidized beds 1 are sequentially arranged from high to low, a discharge port of the higher position fluidized bed 1 in the adjacent fluidized bed 1 is higher than a feed port of the lower position fluidized bed 1, the feed port of the highest position fluidized bed 1 is connected with a feed tank 3, an air inlet of the lowest position fluidized bed 1 is respectively connected with an air compressor 4 and a chlorine storage tank 5, the top of each stage of fluidized beds 1 is further provided with an air outlet and a return port, the air outlet is connected with an air inlet end of a cyclone separator 2, an air outlet of the cyclone separator 2 is connected with an air inlet of the upper stage fluidized bed 1, a solid discharge port of the cyclone separator 2 is connected with a return port on the current stage fluidized bed 1, a half-pipe cooler 6 connected with a freezing water machine 7 is arranged on the outer surface of the fluidized bed 1, a stirring paddle 8 is arranged in the fluidized bed 1, and a stirring motor 13 is arranged on the top of the fluidized bed 1.
Example 2
The embodiment is another preferred embodiment of the invention, and discloses a continuous production system of dichlorine monoxide with multiple fluidized beds connected in series, the specific structure of which is shown in fig. 1, the system comprises 3 stages of fluidized beds 1 connected in series, the adjacent fluidized beds 1 are connected in series in a manner that a discharge port of the fluidized bed 1 located at a higher position is connected with a feed port of the fluidized bed 1 located at a lower position, the fluidized beds 1 are sequentially arranged from high to low, a discharge port of the fluidized bed 1 located at a higher position in the adjacent fluidized bed 1 is higher than a feed port of the fluidized bed 1 located at a lower position, the feed port of the fluidized bed 1 located at a highest position is connected with a feed tank 3, an air inlet of the fluidized bed 1 located at a lowest position is respectively connected with an air compressor 4 and a storage tank 5, the top of each stage of fluidized bed 1 is further provided with an air outlet and a return port, the air outlet is connected with an air inlet end of a cyclone separator 2, an air outlet of the cyclone separator 2 is connected with an air inlet of the previous stage of the fluidized bed 1, a solid discharge port of the cyclone separator 2 is connected with a return port on the current-carrying bed 1, a diversion paddle 8 is arranged on the outer surface of the fluidized bed 1, and an inclined angle of the stirring paddle of the fluidized bed is 13 degrees, and the stirring paddle of the fluidized bed is inclined fluidized bed.
Example 3
In this embodiment, as another preferred embodiment of the present invention, a continuous production system of dichloro monoxide with multiple fluidized beds connected in series is disclosed, the specific structure of which is shown in fig. 1, the system includes 3 fluidized beds 1 connected in series, the adjacent fluidized beds 1 are connected in series in such a way that a discharge port of the fluidized bed 1 located at a higher position is connected to a feed port of the fluidized bed 1 located at a lower position, the fluidized beds 1 are sequentially arranged from high to low, a discharge port of the fluidized bed 1 located at a higher position in the adjacent fluidized beds 1 is higher than a feed port of the fluidized bed 1 located at a lower position, the feed port of the fluidized bed 1 located at a highest position is connected to a feed tank 3, an air inlet of the fluidized bed 1 located at a lowest position is connected to an air compressor 4 and a storage tank 5, the top of each fluidized bed 1 is further provided with an air outlet and a return port, the air outlet is connected to an air inlet end of a cyclone separator 2, an air outlet of the cyclone separator 2 is connected to an air inlet of the previous fluidized bed 1, a solid discharge port of the cyclone separator 2 is connected to a return port of the current-carrying bed 1, a half-tube cooler 6 connected to a freezing point 7 arranged on the outer surface of the fluidized bed 1, a stirring paddle 8, and a stirring paddle 9 is arranged on the fluidized bed 1, and an inclined angle of the stirring paddle 8 is 10 inclined from the stirring paddle of the stirring paddle 9.
Example 4
The embodiment is used as the best embodiment of the invention, and discloses a continuous production system of dichlorine monoxide with a plurality of stages of fluidized beds connected in series, the specific form of which is shown in figure 1, the system comprises 5 stages of fluidized beds 1 connected in series, the adjacent fluidized beds 1 are connected in series in a way that the discharge port of the upper stage fluidized bed 1 is connected with the feed port of the lower stage fluidized bed 1, the fluidized beds 1 are sequentially arranged from high to low, and the discharge port of the higher stage fluidized bed 1 in the adjacent two stages of fluidized beds 1 is higher than the feed port of the lower stage fluidized bed 1; the feed inlet of the fluidized bed 1 at the highest position is connected with the feed tank 3, the air inlet of the fluidized bed 1 at the lowest position is respectively connected with the outlet ends of the air compressor 4 and the chlorine storage tank 5, and a pressure reducing valve and a glass rotameter are arranged between the air compressor 4 and the fluidized bed 1 and between the chlorine storage tank 5 and the fluidized bed 1; the top of each stage of fluidized bed 1 is also provided with a gas outlet and a material return port, the gas outlet of the fluidized bed 1 is connected with the gas inlet end of a cyclone separator 2, the gas outlet of the cyclone separator 2 is connected with the gas inlet of the previous stage of fluidized bed 1, the solid discharge port of the cyclone separator 2 is connected with the material return port of the current stage of fluidized bed 1, wherein the gas outlet of the cyclone separator 2 connected with the fluidized bed 1 at the highest position is also provided with a dust filter, and the dust filter can be a fiber filter or a wire mesh filter; the outer surface of each stage of fluidized bed 1 is provided with a half-pipe cooler, an interstage cooler 10 is further arranged between the exhaust port of each stage of cyclone separator 2 and the air inlet of the fluidized bed 1, the air inlet of the fluidized bed 1 at the lowest position is provided with an inlet cooler 11, and the half-pipe cooler 6, the interstage cooler 10 and the inlet cooler 11 are all connected with a water chiller 7; a rotating shaft is also arranged in each stage of fluidized bed 1, a stirring paddle 8 is fixedly arranged on the rotating shaft, and the rotating shaft is connected with a driving motor 13 positioned at the top of the fluidized bed 1; the stirring paddle 8 is provided with a flow deflector 9, the flow deflector 9 is arranged in an inclined way towards the direction deviating from the axis of the fluidized bed 1, and the inclination angle is 7 degrees; the discharge port of each fluidized bed 1 and the solid discharge port of the cyclone separator 2 are both provided with a control valve 12 for controlling material discharge, and the control valve 12 is any one of a butterfly valve, a knife valve or a plunger valve; and a pressure sensor and a temperature sensor are also arranged in each stage of fluidized bed 1.
Example 5
The embodiment also discloses a method for producing the dichlorine monoxide by using the multistage fluidized bed series-connection dichlorine monoxide production system as shown in figure 1, which comprises the following specific steps:
A. a feeding stage: introducing a small amount of compressed air into the fluidized bed at the lowest position at the flow rate of 0.1m/s to prevent sodium carbonate from blocking a distribution plate when the sodium carbonate is added, adding sodium carbonate powder with the water content of 5% into the fluidized bed through a material storage tank connected with the fluidized bed at the highest position, wherein the adding mass of the sodium carbonate powder is 29kg, opening butterfly valves between the fluidized beds of all stages, and distributing the sodium carbonate into the fluidized beds of all stages through gravity, wherein the sodium carbonate powder accounts for 7% of the empty bed volume of the fluidized bed; simultaneously starting the stirring paddle to fluidize the sodium carbonate in each fluidized bed, wherein the bulk density of the sodium carbonate in the fluidized state is 0.732g/ml, and the rotating speed of the stirring paddle is 20 rpm/min;
B. an initial reaction stage: closing butterfly valves on each stage of fluidized bed and each stage of cyclone separator after the sodium carbonate is added, and introducing mixed gas containing chlorine into the fluidized bed at the lowest position, wherein the content of the chlorine in the mixed gas is 4%; reacting the mixed gas with sodium carbonate in a fluidized state; after the mixed gas reacted in the lowest-stage fluidized bed is separated by the cyclone separator, the gas enters the upper-stage fluidized bed to continuously react with fluidized sodium carbonate, and the solid particles obtained by separation return to the fluidized bed; opening the inlet cooler and the interstage cooler for cooling at the same time to enable the temperature in the fluidized bed body to be 0 ℃, and adjusting the rotating speed of the stirring paddle to 60 rpm/min;
C. a continuous production stage: when the exhaust port of the cyclone separator connected with the fluidized bed at the highest position detects the dichlorine monoxide, the chlorine content of the mixed gas is gradually increased to 9 percent, and the pressure in each stage of fluidized bed is controlled at 0.01MpaG; simultaneously, adjusting the input quantity of system cooling water, and controlling the reaction temperature of each stage of fluidized bed at 0 ℃; when the temperature in the lowest stage fluidized bed is reduced or is close to the temperature of the raw material mixed gas, a butterfly valve on a discharge port of the fluidized bed at the lowest position is opened to discharge part of sodium chloride, and corresponding sodium carbonate is supplemented into the fluidized bed at the highest position according to a corresponding molar ratio, so that the continuous production of the system is realized, the adding amount of the sodium carbonate in the continuous production stage is 58kg/h, and the conversion rate of the sodium carbonate and the conversion rate of the dichlorine monoxide are respectively 96.5 percent and 94.5 percent through measurement.
Example 6
A. A feeding stage: introducing a small amount of compressed air into the fluidized bed at the lowest position at the flow rate of 0.3 m/s to prevent sodium carbonate from blocking a distribution plate when the sodium carbonate is added, adding sodium carbonate powder with the water content of 5% into the fluidized bed through a material storage tank connected with the fluidized bed at the highest position, wherein the adding amount of the sodium carbonate powder is 29kg, opening butterfly valves between the fluidized beds, and distributing the sodium carbonate into the fluidized beds at all stages through gravity, wherein the sodium carbonate powder accounts for 9% of the empty bed volume of the fluidized bed; simultaneously starting a stirring paddle to fluidize the sodium carbonate in each fluidized bed, wherein the bulk density of the sodium carbonate in the fluidized state is 0.720g/ml, and the rotating speed of the stirring paddle is 20 rpm/min;
B. an initial reaction stage: closing butterfly valves on each stage of fluidized bed and each stage of cyclone separator after the sodium carbonate is added, and introducing mixed gas containing chlorine into the fluidized bed at the lowest position, wherein the content of the chlorine in the mixed gas is 5%; reacting the mixed gas with sodium carbonate in a fluidized state; after the mixed gas reacted in the lowest-stage fluidized bed is separated by the cyclone separator, the gas enters the upper-stage fluidized bed to continuously react with fluidized sodium carbonate, and the solid particles obtained by separation return to the fluidized bed; opening the inlet cooler and the interstage cooler to cool at the same time, so that the temperature in the fluidized bed body is 2 ℃, and adjusting the rotating speed of the stirring paddle to 60 rpm/min;
C. a continuous production stage: when the exhaust port of the cyclone separator connected with the fluidized bed at the highest position detects the dichlorine monoxide, the chlorine content of the mixed gas is gradually increased to 11 percent, and the pressure in each stage of fluidized bed is controlled to be 0.02Mpa; simultaneously adjusting the input quantity of cooling water of the system, and controlling the reaction temperature of each stage of fluidized bed at 2 ℃; when the temperature in the lowest stage fluidized bed is reduced or is close to the temperature of the raw material mixed gas, a butterfly valve on a discharge port of the fluidized bed at the lowest position is opened to discharge part of sodium chloride, and corresponding sodium carbonate is supplemented into the fluidized bed at the highest position according to a corresponding molar ratio, so that the continuous production of the system is realized, the input amount of sodium carbonate powder in the continuous production stage is 58.5kg/h, and the conversion rate of the sodium carbonate and the conversion rate of the dichlorine monoxide are respectively 97 percent and 95 percent through measurement.
Example 7
A. A feeding stage: introducing a small amount of compressed air into the fluidized bed at the lowest position at the flow rate of 0.6m/s to prevent sodium carbonate from blocking a distribution plate when the sodium carbonate is added, adding sodium carbonate powder with the water content of 7% into the fluidized bed through a material storage tank connected with the fluidized bed at the highest position, wherein the adding amount of the sodium carbonate powder is 17.39kg, opening butterfly valves between the fluidized beds of all stages, and distributing the sodium carbonate into the fluidized beds of all stages through gravity, wherein the sodium carbonate powder accounts for 7% of the empty bed volume of the fluidized bed; simultaneously starting a stirring paddle to fluidize the sodium carbonate in each fluidized bed, wherein the bulk density of the sodium carbonate in the fluidized state is 0.725g/ml, and the rotating speed of the stirring paddle is 20 rpm/min;
B. an initial reaction stage: closing butterfly valves on each stage of fluidized bed and each stage of cyclone separator after the sodium carbonate is added, and introducing mixed gas containing chlorine into the fluidized bed at the lowest position, wherein the content of the chlorine in the mixed gas is 3.5%; reacting the mixed gas with sodium carbonate in a fluidized state; after the mixed gas reacted in the lowest-stage fluidized bed is separated by the cyclone separator, the gas enters the upper-stage fluidized bed to continuously react with fluidized sodium carbonate powder, and the separated solid particles return to the fluidized bed; opening the inlet cooler and the interstage cooler to cool at the same time, enabling the temperature in the fluidized bed body to be 5 ℃, and adjusting the rotating speed of the stirring paddle to 60 rpm/min;
C. a continuous production stage: when the exhaust port of the cyclone separator connected with the fluidized bed at the highest position detects the dichlorine monoxide, the chlorine content of the mixed gas is gradually increased to 13 percent, and the pressure in each stage of fluidized bed is controlled to be 0.05Mpa; simultaneously adjusting the input quantity of cooling water of the system, and controlling the reaction temperature of each stage of fluidized bed at 5 ℃; when the temperature in the lowest stage fluidized bed is reduced or is close to the temperature of the raw material mixed gas, a butterfly valve on a discharge port of the fluidized bed at the lowest position is opened to discharge part of sodium chloride, and corresponding sodium carbonate is supplemented into the fluidized bed at the highest position according to a corresponding molar ratio, so that the continuous production of the system is realized, the adding amount of sodium carbonate powder in the continuous production stage is 34.78kg/h, and the conversion rate of the sodium carbonate and the conversion rate of the dichlorine monoxide are respectively determined to be 97.2 percent and 94 percent.
Example 8
A. A feeding stage: introducing a small amount of compressed air into the fluidized bed at the lowest position at the flow rate of 0.9m/s to prevent sodium carbonate from blocking a distribution plate when the sodium carbonate is added, adding sodium carbonate powder with the water content of 7% into the fluidized bed through a material storage tank connected with the fluidized bed at the highest position, wherein the adding amount of the sodium carbonate powder is 17.39kg, opening butterfly valves between the fluidized beds of all stages, and distributing the sodium carbonate into the fluidized beds of all stages through gravity, wherein the sodium carbonate powder accounts for 7% of the empty bed volume of the fluidized bed; simultaneously starting the stirring paddle to fluidize the sodium carbonate in each fluidized bed, wherein the bulk density of the sodium carbonate in the fluidized state is 0.732g/ml, and the rotating speed of the stirring paddle is 20 rpm/min;
B. an initial reaction stage: closing butterfly valves on each stage of fluidized bed and each stage of cyclone separator after the sodium carbonate is added, and introducing mixed gas containing chlorine into the fluidized bed at the lowest position, wherein the content of the chlorine in the mixed gas is 4%; reacting the mixed gas with sodium carbonate in a fluidized state; after the mixed gas reacted in the lowest-stage fluidized bed is separated by the cyclone separator, the gas enters the upper-stage fluidized bed to continuously react with fluidized sodium carbonate, and the solid particles obtained by separation return to the fluidized bed; opening the inlet cooler and the interstage cooler to cool at the same time, enabling the temperature in the fluidized bed body to be 5 ℃, and adjusting the rotating speed of the stirring paddle to 60 rpm/min;
C. a continuous production stage: when the exhaust port of the cyclone separator connected with the fluidized bed at the highest position detects the dichlorine monoxide, the chlorine content of the mixed gas is gradually increased to 15 percent, and the pressure in each stage of fluidized bed is controlled to be 0.1Mpa; simultaneously, adjusting the input quantity of system cooling water, and controlling the reaction temperature of each stage of fluidized bed at 10 ℃; when the temperature in the lowest stage fluidized bed is reduced or approaches to the temperature of the raw material mixed gas, a butterfly valve on a discharge port of the lowest stage fluidized bed is opened to discharge part of sodium chloride, and corresponding sodium carbonate is supplemented into the highest stage fluidized bed according to a corresponding molar ratio, so that the continuous production of the system is realized, the addition amount of the sodium carbonate in the continuous production stage is 17.39kg/h, and the conversion rate of the sodium carbonate and the conversion rate of the dichlorine monoxide are respectively determined to be 98 percent and 94.2 percent.
The following table will disclose a comparison table of the yield of dichlorine monoxide and the sodium carbonate conversion for various reaction conditions:
| initial reaction stage carbonic acid Amount of sodium added (kg) | Sodium carbonate in successive reaction stages Access volume (kg/h) | Chlorine flow (m) ³/min） | Chlorine gas Concentration of | Reaction temperature Degree (. Degree. C.) | Production of dichlorine monoxide Volume (kg/h) | Sodium carbonate Conversion rate | Dichloro-methane monoxide Conversion rate | Sodium carbonate Water content |
| 28.98 | 57.93 | 7.6 | 4% | 5 | 13.75 | 96% | 93% | 7% |
| 25.12 | 50.24 | 8.22 | 4% | 5 | 12.38 | 97% | 93.6% | 7% |
| 17.39 | 34.78 | 5.69 | 4% | 5 | 8.36 | 97% | 94.1% | 7% |
| 17.39 | 17.39 | 2.84 | 4% | 5 | 4.22 | 98% | 94.2% | 7% |
| 17.39 | 34.78 | 6.05 | 3.8% | 5 | 8.41 | 97.1% | 93.6% | 6% |
| 17.39 | 34.78 | 6.57 | 3.5% | 5 | 8.63 | 97.2% | 94% | 6% |
| 28.98 | 57.93 | 3.38 | 9% | 0 | 13.31 | 97% | 90% | 5% |
| 28.5 | 58.0 | 2.77 | 11% | 3 | 13.16 | 98% | 89% | 5% |
| 25.5 | 51.0 | 2.57 | 13% | 6 | 10.47 | 98% | 78% | 5% |
| 17.39 | 35.0 | 1.53 | 15% | 10 | 6.21 | 95% | 70% | 5% |
| 29 | 58.0 | 7.65 | 4% | 0 | 14.025 | 96.5% | 94.5% | 5% |
| 29 | 58.5 | 6.18 | 5% | 2 | 14.18 | 97% | 95% | 5% |
In combination with the above examples, experimental data and relevant data of the reference documents mentioned in the background art, it can be seen that the present invention can greatly improve the conversion rate of sodium carbonate (the conversion rate of sodium carbonate in the reference documents is between 88% and 95%) and the yield of dichlorine monoxide under the condition that the initial states of reactants such as the water content of sodium carbonate and the chlorine content are not different.
Claims (7)
1. A method for producing oxydichlorohydrin by a oxydichlorohydrin continuous production system with a plurality of stages of fluidized beds connected in series is characterized in that:
the production system comprises a plurality of stages of fluidized beds (1) which are sequentially connected in series from high to low, and a discharge hole of a fluidized bed (1) at a high position in the adjacent two stages of fluidized beds (1) is higher than a feed hole of the fluidized bed (1) at a low position; the fluidized beds (1) at all levels are connected with cyclone separators (2), the discharge holes of the cyclone separators (2) are connected with the material return holes of the fluidized beds (1) at the current level, and the exhaust holes of the cyclone separators (2) are connected with the air inlet of the fluidized bed (1) at the previous level; the fluidized bed (1) at the highest position is connected with a feeding tank (3), and the fluidized bed (1) at the lowest position is connected with an air compressor (4) and a chlorine storage tank (5); the outer surface of the fluidized bed (1) is also provided with a half-pipe cooler (6), and the half-pipe cooler (6) is connected with a chilled water unit (7); a stirring paddle (8) is also arranged in each stage of fluidized bed (1), and flow deflectors (9) are arranged on two sides of the stirring paddle (8); the flow deflector (9) is obliquely arranged towards the direction deviating from the axis of the fluidized bed (1), and the oblique angle is 5-10 degrees;
the production method specifically comprises the following steps:
A. a feeding stage: introducing a small amount of compressed air into the fluidized bed, adding sodium carbonate powder into the fluidized bed through a material storage tank positioned at the top, opening a butterfly valve between each stage of fluidized bed to uniformly distribute the sodium carbonate with each stage of fluidized bed through gravity, and simultaneously starting a stirring paddle to fluidize the sodium carbonate in each stage of fluidized bed;
B. an initial reaction stage: introducing mixed gas containing chlorine into the fluidized bed at the lowest position to react the mixed gas with the sodium carbonate in a fluidized state; after the mixed gas reacted in the lowest-stage fluidized bed is separated by the cyclone separator, the gas enters the upper-stage fluidized bed to continuously react with fluidized sodium carbonate, and the separated solid particles return to the fluidized bed; simultaneously opening an inlet cooler and an interstage cooler for cooling;
C. a continuous production stage: when the exhaust port of the cyclone separator connected with the highest fluidized bed detects the dichlorine monoxide, the chlorine content of the mixed gas is gradually increased; when the temperature in the lowest stage fluidized bed is reduced or is close to the temperature of the raw material mixed gas, partial sodium chloride is discharged through a butterfly valve at the bottom, and the corresponding sodium carbonate is supplemented into the highest stage fluidized bed according to the corresponding molar ratio.
2. The method of claim 1, wherein: an interstage cooler (10) is further arranged at an exhaust port of the cyclone separator (2), an inlet cooler (11) is further arranged at an air inlet of the fluidized bed (1) positioned at the bottom, and the interstage cooler (10) and the inlet cooler (11) are both connected with the chilled water unit (7).
3. The method of claim 1, wherein: control valves (12) used for controlling material discharge are arranged between the fluidized beds (1) at all levels and between the cyclone separators (2) and the fluidized beds (1), and the control valves (12) are butterfly valves, knife-shaped valves or plunger valves.
4. The method of claim 1, wherein: the compressed air flow rate of the feeding stage is 0.1-0.9 m/s.
5. The method of claim 1, wherein: the chlorine content of the mixed gas in the initial reaction stage is 4%, and the chlorine content of the mixed gas in the continuous production stage is 3% -15%, preferably 4% -9%; the reaction temperature in each fluidized bed of the initial reaction stage and the continuous production stage is-5-10 ℃.
6. The method of claim 1, wherein: the pressure in each fluidization stage of the initial reaction stage and the continuous production stage is 0.01-0.1 MP a; the rotating speed of the stirring paddle in each stage of the fluidized bed in the initial reaction stage and the continuous production stage is 60-120rpm/min.
7. The method of claim 1, wherein: the adding amount of sodium carbonate in each stage of fluidized bed occupies 7-15% of the volume of the fluidized bed; the bulk density of the sodium carbonate is 0.732g/ml-0.850g/ml; the water content of the sodium carbonate is 5-10%.
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| CN101519707A (en) * | 2008-02-28 | 2009-09-02 | 宝山钢铁股份有限公司 | Hematite prereduction process and multistage fluidized bed thereby |
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