CN211725719U - System for reinforcing chloroethane preparation based on micro-interface - Google Patents
System for reinforcing chloroethane preparation based on micro-interface Download PDFInfo
- Publication number
- CN211725719U CN211725719U CN201921517498.3U CN201921517498U CN211725719U CN 211725719 U CN211725719 U CN 211725719U CN 201921517498 U CN201921517498 U CN 201921517498U CN 211725719 U CN211725719 U CN 211725719U
- Authority
- CN
- China
- Prior art keywords
- reactor
- micro
- gas
- chlorine
- reaction zone
- 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.)
- Active
Links
- HRYZWHHZPQKTII-UHFFFAOYSA-N chloroethane Chemical compound CCCl HRYZWHHZPQKTII-UHFFFAOYSA-N 0.000 title claims abstract description 45
- 229960003750 ethyl chloride Drugs 0.000 title claims abstract description 45
- 238000002360 preparation method Methods 0.000 title claims abstract description 18
- 230000003014 reinforcing effect Effects 0.000 title description 3
- 238000006243 chemical reaction Methods 0.000 claims abstract description 126
- 239000007788 liquid Substances 0.000 claims abstract description 99
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 76
- 239000000460 chlorine Substances 0.000 claims abstract description 76
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 76
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical group ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 claims abstract description 71
- 239000000203 mixture Substances 0.000 claims abstract description 44
- 238000012546 transfer Methods 0.000 claims abstract description 15
- 238000002156 mixing Methods 0.000 claims abstract description 8
- 238000005728 strengthening Methods 0.000 claims abstract description 5
- 238000004519 manufacturing process Methods 0.000 claims abstract description 4
- 239000000463 material Substances 0.000 claims description 60
- 238000010992 reflux Methods 0.000 claims description 38
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims description 37
- 239000000376 reactant Substances 0.000 claims description 24
- 238000001816 cooling Methods 0.000 claims description 22
- 239000000498 cooling water Substances 0.000 claims description 20
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical group [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 16
- 239000003054 catalyst Substances 0.000 claims description 16
- 229910052742 iron Inorganic materials 0.000 claims description 8
- 238000004891 communication Methods 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 5
- 230000003139 buffering effect Effects 0.000 claims description 4
- 238000011068 loading method Methods 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 3
- 230000002708 enhancing effect Effects 0.000 claims 4
- 230000000694 effects Effects 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract 1
- 238000000034 method Methods 0.000 description 15
- 230000008569 process Effects 0.000 description 15
- UBOXGVDOUJQMTN-UHFFFAOYSA-N 1,1,2-trichloroethane Chemical compound ClCC(Cl)Cl UBOXGVDOUJQMTN-UHFFFAOYSA-N 0.000 description 12
- 239000006227 byproduct Substances 0.000 description 6
- 230000035484 reaction time Effects 0.000 description 6
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 5
- 238000001514 detection method Methods 0.000 description 5
- 229910017604 nitric acid Inorganic materials 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 238000012545 processing Methods 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000975 dye Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- MRMOZBOQVYRSEM-UHFFFAOYSA-N tetraethyllead Chemical compound CC[Pb](CC)(CC)CC MRMOZBOQVYRSEM-UHFFFAOYSA-N 0.000 description 2
- HOQAPVYOGBLGOC-UHFFFAOYSA-N 1-ethyl-9h-carbazole Chemical compound C12=CC=CC=C2NC2=C1C=CC=C2CC HOQAPVYOGBLGOC-UHFFFAOYSA-N 0.000 description 1
- 239000001856 Ethyl cellulose Substances 0.000 description 1
- ZZSNKZQZMQGXPY-UHFFFAOYSA-N Ethyl cellulose Chemical compound CCOCC1OC(OC)C(OCC)C(OCC)C1OC1C(O)C(O)C(OC)C(CO)O1 ZZSNKZQZMQGXPY-UHFFFAOYSA-N 0.000 description 1
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000000443 aerosol Substances 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000000703 anti-shock Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 150000001805 chlorine compounds Chemical class 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229920001249 ethyl cellulose Polymers 0.000 description 1
- 235000019325 ethyl cellulose Nutrition 0.000 description 1
- 239000012021 ethylating agents Substances 0.000 description 1
- 230000008570 general process Effects 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 239000002917 insecticide Substances 0.000 description 1
- 239000000543 intermediate Substances 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 239000003589 local anesthetic agent Substances 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- -1 polypropylene Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 239000001993 wax Substances 0.000 description 1
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to a system based on preparation of ethyl chloride is reinforceed to micro-interface, include: the reactor, the micro-interface generator, the heat exchange unit and the like. The utility model discloses a broken chlorine makes it form micron order bubble of micron yardstick, makes micron order bubble and liquid chloroethylene mix and form gas-liquid mixture to increase the gas-liquid double-phase interfacial area, and reach the effect of strengthening the mass transfer in lower predetermined operating condition scope, reduce the production of accessory substance; meanwhile, the micron-sized chlorine bubbles can be fully mixed with the liquid chloroethylene to form a gas-liquid mixture, and the gas-liquid two-phase full mixing can ensure that the liquid chloroethylene in the system can be fully contacted with the chlorine, so that the reaction efficiency of the system is effectively improved, and the conversion rate of the chloroethane is improved.
Description
Technical Field
The utility model relates to a chloroethane preparation technical field especially relates to a system based on preparation of micro-interface intensive chloroethane.
Background
Ethyl chloride, which has an ether-like odor, is slightly soluble in water, and is miscible in most organic solvents. Chloroethane is mainly used as a raw material of tetraethyl lead, ethyl cellulose, ethyl carbazole dye and the like, can also be used for aerosol, refrigerant, local anesthetic, insecticide, ethylating agent, olefin polymerization solvent, gasoline anti-shock agent and the like, and can also be used for the synthesis of catalysts of polypropylene, solvents of phosphorus, sulfur, grease, resin, wax and the like, pesticides, dyes, medicines and intermediates thereof.
1,1, 2-trichloroethane (ethyl chloride for short) is usually produced by charging 1,1, 2-trichloroethane in advance into a steel tank type reactor (chlorine addition reactor) having a stirrer and a cooling jacket, and then blowing chlorine gas and a slight excess amount of vinyl chloride (for example, 1/1.05 mole ratio) simultaneously thereinto to add chlorine to vinyl chloride to obtain 1,1, 2-trichloroethane. The reaction is carried out with ferric chloride as a catalyst, which is produced by the reaction of iron on the reactor wall with chlorine.
However, in the above-mentioned conventional general process for producing 1,1, 2-trichloroethane, on the one hand, the reaction is carried out at a high temperature to increase the reaction rate, and the amount of by-products having high chlorides is increased. On the other hand, in order to suppress the amount of by-products produced and to improve the purity of 1,1, 2-trichloroethane, the residence time must be extended at low temperatures, resulting in a decrease in the 1,1, 2-trichloroethane production ability.
SUMMERY OF THE UTILITY MODEL
Therefore, the utility model provides a system based on ethyl chloride preparation is reinforceed to micro-interface for realize the conversion rate and the efficiency of ethyl chloride preparation under lower preset condition.
The utility model provides a system based on preparation of ethyl chloride is reinforceed to micro-interface, include:
the reactor is used for providing a reaction place for chlorine and chloroethylene to prepare chloroethane, a catalyst is arranged on the inner wall of the reactor, and the reactor consists of a fully mixed flow reaction zone, a reflux reaction zone and a cooling jacket; the fully mixed flow reaction zone is arranged below the reactor and is used for loading chlorine, chloroethylene, chloroethane solution and a catalyst and providing a reaction space for the chlorine and the chloroethylene; the reflux reaction zone is arranged above the reactor and is used for refluxing unreacted chlorine and enabling the unreacted chlorine and vinyl chloride to react again; the cooling jacket is arranged on the outer side wall of the reactor, the upper end and the lower end of the side wall of the cooling jacket are respectively provided with a cooling water inlet pipe and a cooling water outlet pipe, and cooling water circularly flows in the cooling jacket through the cooling water inlet pipe and the cooling water outlet pipe;
the micro-interface generator converts pressure energy of gas and/or kinetic energy of liquid into surface energy of bubbles and transmits the surface energy of the bubbles to a gas reactant, the gas reactant is crushed into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm so as to improve the mass transfer area between the gas reactant and the liquid reactant, reduce the thickness of a liquid film and reduce mass transfer resistance, and the liquid reactant and the micron-sized bubbles of the gas reactant are mixed to form a gas-liquid mixture after being crushed so as to strengthen the mass transfer efficiency and the reaction efficiency between the liquid reactant and the gas reactant within a preset operating condition range;
and the heat exchange unit is arranged on one side of the reactor and is used for cooling the products in the reactor.
Further, the micro-interface generator includes:
the first micro-interface generator is a pneumatic micro-interface generator, is positioned in a fully mixed flow reaction zone in the reactor, and is used for crushing chlorine to form micron-sized bubbles and outputting the micron-sized bubbles to the fully mixed flow reaction zone in the reactor and mixing liquid chloroethylene in the fully mixed flow reaction zone in the reactor to form a gas-liquid mixture after the micron-sized bubbles are crushed;
the second micro-interface generator is a pneumatic micro-interface generator, is positioned in a fully mixed flow reaction zone in the reactor, and is used for crushing vinyl chloride gas to form micron-sized bubbles and outputting the micron-sized bubbles to the fully mixed flow reaction zone in the reactor for liquefaction after the crushing is finished, and the liquefied vinyl chloride is mixed with chlorine in the fully mixed flow reaction zone in the reactor to form a gas-liquid mixture;
and the third micro-interface generator is a hydraulic micro-interface generator, is positioned in a reflux reaction zone in the reactor, and is used for receiving unreacted chlorine at the upper part of the reflux reaction zone in the reactor, entraining the unreacted chlorine at the upper part of the reflux reaction zone in the reactor and crushing the chlorine to form micron-sized bubbles, mixing the micron-sized bubbles and liquid chloroethylene to form a gas-liquid mixture, and outputting the gas-liquid mixture to the fully mixed flow reaction zone to carry out hedging with the gas-liquid mixture output by the first micro-interface generator and the second micro-interface generator, so that the unreacted chlorine participates in the reaction again.
Further, the fully mixed flow reaction zone comprises:
a chlorine inlet pipe communicated with the first micro-interface generator, the chlorine inlet pipe being configured to transmit chlorine to the first micro-interface generator;
a vinyl chloride inlet pipe in communication with the second micro-interface generator, the vinyl chloride inlet pipe configured to convey vinyl chloride to the second micro-interface generator;
and the material discharge pipe is communicated with the lower end of the reactor and is used for discharging products.
Further, the reflux reaction zone comprises:
one end of the return pipe is communicated with the third micro-interface generator, the other end of the return pipe is positioned at the upper part of the reflux reaction area, and the return pipe is used for transferring unreacted chlorine gas to the third micro-interface generator;
a chlorine gas discharge pipe communicated with the upper end of the reactor, the chlorine gas discharge pipe being configured to discharge excess unreacted chlorine gas;
and the material inlet pipe is communicated with the upper part of the side wall of the reactor and is used for adding liquid reaction materials into the reactor.
Further, the heat exchange unit comprises:
the buffer tank is positioned at one side of the reactor and used for buffering the mixed materials in the reactor;
the first connecting pipe is positioned between the reactor and the cache tank and is communicated with the reactor and the cache tank, and the first connecting pipe is used for conveying the mixed materials in the reactor to the cache tank;
the heat exchanger is positioned at the lower side of the cache tank and used for transferring part of heat in the mixed material in the cache tank to cold flow equipment on the heat exchanger so as to cool the mixed material;
and the second connecting pipe is positioned between the reactor and the cache tank and communicated with the reactor and the cache tank, and is used for transmitting the mixed material with the temperature reduced by the heat exchanger back to the reactor.
And the pump body is arranged on the second connecting pipe and used for giving power to the circulation of the mixed material in the heat exchanger.
Further, the height of the return pipe is larger than the height of the liquid level in the reactor.
Further, the temperature in the reactor is 40-60 ℃, and the pressure is 0.8 atm.
Further, the catalyst is iron.
Further, the heat exchanger is a dividing wall type heat exchanger.
Further, the chlorine gas discharge pipe is communicated with the alkali pool.
Compared with the prior art, the beneficial effects of the utility model reside in that, the utility model discloses a broken chlorine makes its micron order bubble that forms micron yardstick, micron order bubble possesses the physicochemical property that conventional bubble did not possess, can know by the computational formula of spheroid volume and surface area, under the unchangeable circumstances of total volume, the total surface area and the single bubble diameter of bubble are inversely proportional, can know that micron order bubble's total surface area is huge from this, make micron order bubble and liquid chloroethylene mix and form gas-liquid mixture, with the area of contact of increase gas-liquid double-phase, and reach the effect of strengthening the mass transfer in lower preset operating condition scope, effectively improve conversion and the efficiency of preparation chloroethane;
further, the reactor comprises:
the fully mixed flow reaction zone is arranged below the reactor and is used for loading chlorine, chloroethylene, chloroethane solution and a catalyst and providing a reaction space for the chlorine and the chloroethylene;
a reflux reaction zone disposed above the reactor to reflux unreacted chlorine gas and react the unreacted chlorine gas with vinyl chloride again;
and the cooling jacket is arranged on the outer side wall of the reactor, the upper end and the lower end of the side wall of the cooling jacket are respectively provided with a cooling water inlet pipe and a cooling water outlet pipe, and cooling water circularly flows in the cooling jacket through the cooling water inlet pipe and the cooling water outlet pipe.
The cooling jacket has a cooling effect on the reactor so as to keep the reaction temperature in the reactor low and reduce the generation of byproducts.
Further, the micro-interface generator includes:
the first micro-interface generator is a pneumatic micro-interface generator, is positioned in a fully mixed flow reaction zone in the reactor, and is used for crushing chlorine to form micron-sized bubbles and outputting the micron-sized bubbles to the fully mixed flow reaction zone in the reactor and mixing liquid chloroethylene in the fully mixed flow reaction zone in the reactor to form a gas-liquid mixture after the micron-sized bubbles are crushed;
the second micro-interface generator is a pneumatic micro-interface generator, is positioned in a fully mixed flow reaction zone in the reactor, and is used for crushing vinyl chloride gas to form micron-sized bubbles and outputting the micron-sized bubbles to the fully mixed flow reaction zone in the reactor for liquefaction after the crushing is finished, and the liquefied vinyl chloride is mixed with chlorine in the fully mixed flow reaction zone in the reactor to form a gas-liquid mixture;
and the third micro-interface generator is a hydraulic micro-interface generator, is positioned in a reflux reaction zone in the reactor, and is used for receiving unreacted chlorine at the upper part of the reflux reaction zone in the reactor, entraining the unreacted chlorine at the upper part of the reflux reaction zone in the reactor and crushing the chlorine to form micron-sized bubbles, mixing the micron-sized bubbles and liquid chloroethylene to form a gas-liquid mixture, and outputting the gas-liquid mixture to the fully mixed flow reaction zone to carry out hedging with the gas-liquid mixture output by the first micro-interface generator and the second micro-interface generator, so that the unreacted chlorine participates in the reaction again.
Further, the fully mixed flow reaction zone comprises:
a chlorine inlet pipe communicated with the first micro-interface generator, the chlorine inlet pipe being configured to transmit chlorine to the first micro-interface generator;
a vinyl chloride inlet pipe in communication with the second micro-interface generator, the vinyl chloride inlet pipe configured to convey vinyl chloride to the second micro-interface generator;
and the material discharge pipe is communicated with the lower end of the reactor and is used for discharging products.
Further, the reflux reaction zone comprises:
one end of the return pipe is communicated with the third micro-interface generator, the other end of the return pipe is positioned at the upper part of the reflux reaction area, and the return pipe is used for transferring unreacted chlorine gas to the third micro-interface generator;
a chlorine gas discharge pipe communicated with the upper end of the reactor, the chlorine gas discharge pipe being configured to discharge excess unreacted chlorine gas;
and the material inlet pipe is communicated with the upper part of the side wall of the reactor and is used for adding liquid reaction materials into the reactor.
Transmitting chlorine gas and gaseous chloroethylene to the first micro-interface generator and the second micro-interface generator through the chlorine gas inlet pipe and the chloroethylene inlet pipe respectively;
the first micro-interface generator crushes chlorine gas to form micron-sized bubbles and outputs the micron-sized bubbles to a mixed flow reaction zone in the reactor after the crushing is finished, and the micron-sized bubbles are mixed with liquid chloroethylene in the mixed flow reaction zone in the reactor to form a gas-liquid mixture; the second micro-interface generator crushes chloroethylene gas to form micron-sized bubbles and outputs the micron-sized bubbles to a fully mixed flow reaction zone in the reactor for liquefaction after the crushing is finished, the liquefied chloroethylene is mixed with chlorine in the fully mixed flow reaction zone in the reactor to form a gas-liquid mixture, and the chlorine and the chloroethylene react to generate chloroethane; unreacted chlorine rises to the top of the reactor, the third micro-interface generator works to receive the unreacted chlorine at the upper part of the reflux reaction zone in the reactor, the third micro-interface generator sucks the unreacted chlorine at the upper part of the reflux reaction zone in the reactor and breaks the chlorine to form micron-sized bubbles, the micron-sized bubbles and liquid chloroethylene are mixed to form a gas-liquid mixture, the gas-liquid mixture is output to the fully mixed flow reaction zone and is subjected to hedging with the gas-liquid mixture output by the first micro-interface generator and the second micro-interface generator, the unreacted chlorine is enabled to participate in the reaction again, and the micro-interface generator is arranged to enable the preparation efficiency and the conversion rate of the chloroethane to be improved to a large extent.
Further, the heat exchange unit comprises:
the buffer tank is positioned at one side of the reactor and used for buffering the mixed materials in the reactor;
the first connecting pipe is positioned between the reactor and the cache tank and is communicated with the reactor and the cache tank, and the first connecting pipe is used for conveying the mixed materials in the reactor to the cache tank;
the heat exchanger is positioned at the lower side of the cache tank and used for transferring part of heat in the mixed material in the cache tank to cold flow equipment on the heat exchanger so as to cool the mixed material;
and the second connecting pipe is positioned between the reactor and the cache tank and communicated with the reactor and the cache tank, and is used for transmitting the mixed material with the temperature reduced by the heat exchanger back to the reactor.
And the pump body is arranged on the second connecting pipe and used for giving power to the circulation of the mixed material in the heat exchanger.
The heat exchange unit works to cool down the mixed material in the reactor, and the concrete processing process is that the pump body works to lead the mixed material in the reactor to be sucked into the cache tank along the first connecting pipe, and then the mixed material enters into the heat exchanger through the cache tank, and the heat exchanger transfers part of heat in the mixed material to the cold flow equipment on the heat exchanger so as to cool down the mixed material, and the mixed material cooled by the heat exchanger flows back to the reactor along the second connecting pipe, so that the heat exchange unit works to cool down the material, and the generation of byproducts is effectively reduced.
Drawings
Fig. 1 is a schematic structural diagram of a system for reinforcing ethyl chloride preparation based on a micro interface according to the present invention.
Detailed Description
Preferred embodiments of the present invention will be described below with reference to the accompanying drawings. It should be understood by those skilled in the art that these embodiments are only for explaining the technical principle of the present invention, and do not limit the scope of the present invention.
It should be noted that in the description of the present invention, the terms of direction or positional relationship indicated by the terms "upper", "lower", "left", "right", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, which are only for convenience of description, and do not indicate or imply that the device or element must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention.
Furthermore, it should be noted that, in the description of the present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
Please refer to fig. 1, which is a schematic structural diagram of a system for strengthening ethyl chloride preparation based on a micro interface according to the present invention, comprising:
the reactor 1 is used for providing a reaction place for chlorine and chloroethylene to prepare chloroethane, a catalyst is arranged on the inner wall of the reactor, the reactor consists of a fully mixed flow reaction zone 101, a reflux reaction zone 102 and a cooling jacket 103, and the fully mixed flow reaction zone is arranged below the reactor and used for loading chlorine, chloroethylene, chloroethane solution and the catalyst and providing a reaction space for the chlorine and the chloroethylene; the reflux reaction zone is arranged above the reactor and is used for refluxing unreacted chlorine and enabling the unreacted chlorine and vinyl chloride to react again; the cooling jacket is arranged on the outer side wall of the reactor, the upper end and the lower end of the side wall of the cooling jacket are respectively provided with a cooling water inlet pipe and a cooling water outlet pipe, cooling water circularly flows in the cooling jacket through the cooling water inlet pipe and the cooling water outlet pipe, and the cooling jacket plays a role in cooling the reactor so as to keep the low reaction temperature in the reactor and reduce the generation of byproducts;
the micro-interface generator converts pressure energy of gas and/or kinetic energy of liquid into surface energy of bubbles and transmits the surface energy of the bubbles to a gas reactant, the gas reactant is crushed into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm so as to improve the mass transfer area between the gas reactant and the liquid reactant, reduce the thickness of a liquid film and reduce mass transfer resistance, and the liquid reactant and the micron-sized bubbles of the gas reactant are mixed to form a gas-liquid mixture after being crushed so as to strengthen the mass transfer efficiency and the reaction efficiency between the liquid reactant and the gas reactant within a preset operating condition range;
and the heat exchange unit 3 is arranged on one side of the reactor and is used for cooling the products in the reactor.
With continued reference to fig. 1, the micro-interface generator includes:
the first micro-interface generator 201 is a pneumatic micro-interface generator, is located in a fully mixed flow reaction zone in the reactor, and is configured to crush chlorine to form micron-sized bubbles, and output the micron-sized bubbles to the fully mixed flow reaction zone in the reactor after the crushing is completed to mix with liquid vinyl chloride in the fully mixed flow reaction zone in the reactor to form a gas-liquid mixture;
a second micro-interface generator 202, which is a pneumatic micro-interface generator, and is located in the fully mixed flow reaction zone in the reactor, and is configured to crush vinyl chloride gas to form micron-sized bubbles, and output the micron-sized bubbles to the fully mixed flow reaction zone in the reactor for liquefaction after the crushing is completed, and the liquefied vinyl chloride is mixed with chlorine in the fully mixed flow reaction zone in the reactor to form a gas-liquid mixture;
and the third micro-interface generator 203 is a hydraulic micro-interface generator, is located in the reflux reaction zone in the reactor, and is used for receiving unreacted chlorine at the upper part of the reflux reaction zone in the reactor, entraining the unreacted chlorine at the upper part of the reflux reaction zone in the reactor and crushing the chlorine to form micron-sized bubbles, mixing the micron-sized bubbles with liquid chloroethylene to form a gas-liquid mixture, and outputting the gas-liquid mixture to the fully mixed flow reaction zone to be flushed with the gas-liquid mixture output by the first micro-interface generator and the second micro-interface generator, so that the unreacted chlorine participates in the reaction again.
With continued reference to fig. 1, the fully mixed flow reaction zone includes:
a chlorine inlet pipe 104 in communication with the first micro-interface generator, the chlorine inlet pipe configured to deliver chlorine to the first micro-interface generator;
a vinyl chloride inlet pipe 105 in communication with the second micro-interface generator, the vinyl chloride inlet pipe configured to convey vinyl chloride to the second micro-interface generator;
a material discharge pipe 106 communicating with a lower end of the reactor, the material discharge pipe being for discharging a product.
With continued reference to fig. 1, the reflow reaction zone includes:
a reflux pipe 107, one end of which is communicated with the third micro interface generator, and the other end of which is positioned at the upper part of the reflux reaction zone, wherein the reflux pipe is used for transferring the unreacted chlorine gas to the third micro interface generator;
a chlorine gas discharge pipe 108 communicating with an upper end of the reactor, the chlorine gas discharge pipe being configured to discharge excess unreacted chlorine gas;
and a material inlet pipe 109 communicating with the upper portion of the side wall of the reactor, the material inlet pipe being for adding a liquid reaction material into the reactor.
Transmitting chlorine gas and gaseous chloroethylene to the first micro-interface generator and the second micro-interface generator through the chlorine gas inlet pipe and the chloroethylene inlet pipe respectively;
the first micro-interface generator crushes chlorine gas to form micron-sized bubbles and outputs the micron-sized bubbles to a mixed flow reaction zone in the reactor after the crushing is finished, and the micron-sized bubbles are mixed with liquid chloroethylene in the mixed flow reaction zone in the reactor to form a gas-liquid mixture; the second micro-interface generator crushes chloroethylene gas to form micron-sized bubbles and outputs the micron-sized bubbles to a fully mixed flow reaction zone in the reactor for liquefaction after the crushing is finished, the liquefied chloroethylene is mixed with chlorine in the fully mixed flow reaction zone in the reactor to form a gas-liquid mixture, and the chlorine and the chloroethylene react to generate chloroethane; unreacted chlorine rises to the top of the reactor, the third micro-interface generator works to receive the unreacted chlorine at the upper part of the reflux reaction zone in the reactor, the third micro-interface generator sucks the unreacted chlorine at the upper part of the reflux reaction zone in the reactor and breaks the chlorine to form micron-sized bubbles, the micron-sized bubbles and liquid chloroethylene are mixed to form a gas-liquid mixture, the gas-liquid mixture is output to the fully mixed flow reaction zone and is subjected to hedging with the gas-liquid mixture output by the first micro-interface generator and the second micro-interface generator, the unreacted chlorine is enabled to participate in the reaction again, and the micro-interface generator is arranged to enable the preparation efficiency and the conversion rate of the chloroethane to be improved to a large extent.
With continued reference to fig. 1, the heat exchange unit includes:
a buffer tank 301, which is located at one side of the reactor and is used for buffering the mixed materials in the reactor;
a first connection pipe 302 located between and in communication with the reactor and the buffer tank, the first connection pipe being configured to transfer the mixture in the reactor to the buffer tank;
the heat exchanger 303 is positioned at the lower side of the cache tank and used for transferring part of heat of the mixed material in the cache tank to cold flow equipment on the heat exchanger so as to cool the mixed material;
and a second connection pipe 304, which is located between the reactor and the buffer tank and is communicated with the reactor and the buffer tank, and is used for conveying the mixed material with the temperature reduced by the heat exchanger back to the reactor.
A pump body 305 mounted on the second connection pipe for imparting power to the circulation of the mixed material within the heat exchanger.
The heat exchange unit works to cool down the mixed material in the reactor, and the concrete processing process is that the pump body works to lead the mixed material in the reactor to be sucked into the cache tank along the first connecting pipe, and then the mixed material enters into the heat exchanger through the cache tank, and the heat exchanger transfers part of heat in the mixed material to the cold flow equipment on the heat exchanger so as to cool down the mixed material, and the mixed material cooled by the heat exchanger flows back to the reactor along the second connecting pipe, so that the heat exchange unit works to cool down the material, and the generation of byproducts is effectively reduced.
Referring to fig. 1, the present invention provides a process for strengthening ethyl chloride preparation based on a micro interface, comprising:
step 1: adding liquid vinyl chloride to the reactor through the material inlet pipe;
step 2: transmitting chlorine gas and gaseous chloroethylene to the first micro-interface generator and the second micro-interface generator through the chlorine gas inlet pipe and the chloroethylene inlet pipe respectively;
and step 3: the first micro-interface generator crushes chlorine gas to form micron-sized bubbles and outputs the micron-sized bubbles to a mixed flow reaction zone in the reactor after the crushing is finished, and the micron-sized bubbles are mixed with liquid chloroethylene in the mixed flow reaction zone in the reactor to form a gas-liquid mixture; the second micro-interface generator crushes chloroethylene gas to form micron-sized bubbles and outputs the micron-sized bubbles to a fully mixed flow reaction zone in the reactor for liquefaction after the crushing is finished, the liquefied chloroethylene is mixed with chlorine in the fully mixed flow reaction zone in the reactor to form a gas-liquid mixture, and the chlorine and the chloroethylene react to generate chloroethane;
and 4, step 4: the unreacted chlorine gas rises to the top of the reactor in the step 3, the third micro-interface generator works to receive the unreacted chlorine gas on the upper part of the reflux reaction zone in the reactor, the third micro-interface generator sucks the unreacted chlorine gas on the upper part of the reflux reaction zone in the reactor and breaks the chlorine gas into micron-sized bubbles, the micron-sized bubbles and liquid chloroethylene are mixed to form a gas-liquid mixture, the gas-liquid mixture is output to the fully mixed flow reaction zone and is flushed with the gas-liquid mixture output by the first micro-interface generator and the second micro-interface generator, and the unreacted chlorine gas participates in the reaction again;
and 5: a small amount of chlorine gas which is not sucked at the top of the reactor is discharged to an external alkali pool along the chlorine gas discharge pipe to be absorbed;
step 6: the heat exchange unit works to cool the mixed material in the reactor, the specific processing process is that the pump body works to suck the mixed material in the reactor into the cache tank along the first connecting pipe, the mixed material enters the heat exchanger from the cache tank, the heat exchanger transfers part of heat in the mixed material to cold flow equipment on the heat exchanger so as to cool the mixed material, and the mixed material cooled by the heat exchanger flows back into the reactor along the second connecting pipe;
and 7: and discharging the reacted materials along the material discharge pipe.
Example 1
The system and the process are used for preparing the chloroethane, wherein:
the temperature in the reactor is 40 ℃, the pressure in the concentrated nitric acid generator is 0.8atm, and the catalyst in the reactor is iron.
The gas-liquid ratio in the first micro-interface generator is 700: 1.
the gas-liquid ratio in the second micro-interface generator is 700: 1.
the gas-liquid ratio in the third micro-interface generator is 500: 1.
the detection shows that the conversion rate of the chloroethane is 91.0 percent after the system and the process are used.
The reaction time was 9.6 h.
Example 2
The system and the process are used for preparing the chloroethane, wherein:
the temperature in the reactor is 45 ℃, the pressure in the concentrated nitric acid generator is 0.8atm, and the catalyst in the reactor is iron.
The gas-liquid ratio in the first micro-interface generator is 700: 1.
the gas-liquid ratio in the second micro-interface generator is 700: 1.
the gas-liquid ratio in the third micro-interface generator is 500: 1.
the detection shows that the conversion rate of the chloroethane is 91.2% after the system and the process are used.
The reaction time was 9.5 h.
Example 3
The system and the process are used for preparing the chloroethane, wherein:
the temperature in the reactor is 50 ℃, the pressure in the concentrated nitric acid generator is 0.8atm, and the catalyst in the reactor is iron.
The gas-liquid ratio in the first micro-interface generator is 700: 1.
the gas-liquid ratio in the second micro-interface generator is 700: 1.
the gas-liquid ratio in the third micro-interface generator is 500: 1.
the detection shows that the conversion rate of the chloroethane is 91.2% after the system and the process are used.
The reaction time was 9.5 h.
Example 4
The system and the process are used for preparing the chloroethane, wherein:
the temperature in the reactor is 55 ℃, the pressure in the concentrated nitric acid generator is 0.8atm, and the catalyst in the reactor is iron.
The gas-liquid ratio in the first micro-interface generator is 700: 1.
the gas-liquid ratio in the second micro-interface generator is 700: 1.
the gas-liquid ratio in the third micro-interface generator is 500: 1.
the detection shows that the conversion rate of the chloroethane is 91.8% after the system and the process are used.
The reaction time was 9.5 h.
Example 5
The system and the process are used for preparing the chloroethane, wherein:
the temperature in the reactor is 60 ℃, the pressure in the concentrated nitric acid generator is 0.8atm, and the catalyst in the reactor is iron.
The gas-liquid ratio in the first micro-interface generator is 700: 1.
the gas-liquid ratio in the second micro-interface generator is 700: 1.
the gas-liquid ratio in the third micro-interface generator is 500: 1.
the detection shows that the conversion rate of the chloroethane is 91.8% after the system and the process are used.
The reaction time was 9.5 h.
Comparative example
The ethyl chloride preparation was carried out using the prior art, wherein the process parameters selected for this comparative example were the same as those in the example 6.
The ethyl chloride conversion was found to be 69.0%.
The reaction time was 13 h.
So far, the technical solution of the present invention has been described with reference to the preferred embodiments shown in the drawings, but it is easily understood by those skilled in the art that the scope of the present invention is obviously not limited to these specific embodiments. Without departing from the principle of the present invention, a person skilled in the art can make equivalent changes or substitutions to the related technical features, and the technical solutions after these changes or substitutions will fall within the protection scope of the present invention.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention; various modifications and changes may occur to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A system for strengthening ethyl chloride preparation based on a micro interface is characterized by comprising:
the reactor is used for providing a reaction place for chlorine and chloroethylene to prepare chloroethane, a catalyst is arranged on the inner wall of the reactor, and the reactor consists of a fully mixed flow reaction zone, a reflux reaction zone and a cooling jacket; the fully mixed flow reaction zone is arranged below the reactor and is used for loading chlorine, chloroethylene, chloroethane solution and a catalyst and providing a reaction space for the chlorine and the chloroethylene; the reflux reaction zone is arranged above the reactor and is used for refluxing unreacted chlorine and enabling the unreacted chlorine and vinyl chloride to react again; the cooling jacket is arranged on the outer side wall of the reactor, the upper end and the lower end of the side wall of the cooling jacket are respectively provided with a cooling water inlet pipe and a cooling water outlet pipe, and cooling water circularly flows in the cooling jacket through the cooling water inlet pipe and the cooling water outlet pipe;
the micro-interface generator converts pressure energy of gas and/or kinetic energy of liquid into surface energy of bubbles and transmits the surface energy of the bubbles to a gas reactant, the gas reactant is crushed into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm so as to improve the mass transfer area between the gas reactant and the liquid reactant, reduce the thickness of a liquid film and reduce mass transfer resistance, and the liquid reactant and the micron-sized bubbles of the gas reactant are mixed to form a gas-liquid mixture after being crushed so as to strengthen the mass transfer efficiency and the reaction efficiency between the liquid reactant and the gas reactant within a preset operating condition range;
a heat exchange unit disposed at one side of the reactor.
2. The system of claim 1, wherein the micro-interface generator comprises:
the first micro-interface generator is a pneumatic micro-interface generator, is positioned in a fully mixed flow reaction zone in the reactor, and is used for crushing chlorine to form micron-sized bubbles and outputting the micron-sized bubbles to the fully mixed flow reaction zone in the reactor and mixing liquid chloroethylene in the fully mixed flow reaction zone in the reactor to form a gas-liquid mixture after the micron-sized bubbles are crushed;
the second micro-interface generator is a pneumatic micro-interface generator, is positioned in a fully mixed flow reaction zone in the reactor, and is used for crushing vinyl chloride gas to form micron-sized bubbles and outputting the micron-sized bubbles to the fully mixed flow reaction zone in the reactor for liquefaction after the crushing is finished, and the liquefied vinyl chloride is mixed with chlorine in the fully mixed flow reaction zone in the reactor to form a gas-liquid mixture;
and the third micro-interface generator is a hydraulic micro-interface generator, is positioned in a reflux reaction zone in the reactor, and is used for receiving unreacted chlorine at the upper part of the reflux reaction zone in the reactor, entraining the unreacted chlorine at the upper part of the reflux reaction zone in the reactor and crushing the chlorine to form micron-sized bubbles, mixing the micron-sized bubbles and liquid chloroethylene to form a gas-liquid mixture, and outputting the gas-liquid mixture to the fully mixed flow reaction zone to carry out hedging with the gas-liquid mixture output by the first micro-interface generator and the second micro-interface generator, so that the unreacted chlorine participates in the reaction again.
3. The system for enhancing the preparation of ethyl chloride based on the micro-interface as claimed in claim 2, wherein the fully mixed flow reaction zone comprises:
a chlorine inlet pipe communicated with the first micro-interface generator, the chlorine inlet pipe being configured to transmit chlorine to the first micro-interface generator;
a vinyl chloride inlet pipe in communication with the second micro-interface generator, the vinyl chloride inlet pipe configured to convey vinyl chloride to the second micro-interface generator;
and the material discharge pipe is communicated with the lower end of the reactor and is used for discharging products.
4. The system for enhancing ethyl chloride production based on a micro-interface of claim 2, wherein the reflux reaction zone comprises:
one end of the return pipe is communicated with the third micro-interface generator, the other end of the return pipe is positioned at the upper part of the reflux reaction area, and the return pipe is used for transferring unreacted chlorine gas to the third micro-interface generator;
a chlorine gas discharge pipe communicated with the upper end of the reactor, the chlorine gas discharge pipe being configured to discharge excess unreacted chlorine gas;
and the material inlet pipe is communicated with the upper part of the side wall of the reactor and is used for adding liquid reaction materials into the reactor.
5. The system for enhancing ethyl chloride production based on a micro-interface of claim 1, wherein the heat exchange unit comprises:
the buffer tank is positioned at one side of the reactor and used for buffering the mixed materials in the reactor;
the first connecting pipe is positioned between the reactor and the cache tank and is communicated with the reactor and the cache tank, and the first connecting pipe is used for conveying the mixed materials in the reactor to the cache tank;
the heat exchanger is positioned at the lower side of the cache tank and used for transferring part of heat in the mixed material in the cache tank to cold flow equipment on the heat exchanger so as to cool the mixed material;
the second connecting pipe is positioned between the reactor and the cache tank and communicated with the reactor and the cache tank, and the second connecting pipe is used for transmitting the mixed material with the temperature reduced by the heat exchanger back to the reactor;
and the pump body is arranged on the second connecting pipe and used for giving power to the circulation of the mixed material in the heat exchanger.
6. The system of claim 4, wherein the height of the return pipe is greater than the liquid level in the reactor.
7. The system for enhancing the preparation of chloroethane based on a micro-interface as claimed in claim 1, wherein the temperature in the reactor is 40-60 ℃ and the pressure is 0.8 atm.
8. The system of claim 1, wherein the catalyst is iron.
9. The system of claim 5, wherein the heat exchanger is a dividing wall heat exchanger.
10. The system of claim 4, wherein the chlorine gas discharge pipe is in communication with an alkali pool.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921517498.3U CN211725719U (en) | 2019-09-12 | 2019-09-12 | System for reinforcing chloroethane preparation based on micro-interface |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921517498.3U CN211725719U (en) | 2019-09-12 | 2019-09-12 | System for reinforcing chloroethane preparation based on micro-interface |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211725719U true CN211725719U (en) | 2020-10-23 |
Family
ID=72849494
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921517498.3U Active CN211725719U (en) | 2019-09-12 | 2019-09-12 | System for reinforcing chloroethane preparation based on micro-interface |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211725719U (en) |
-
2019
- 2019-09-12 CN CN201921517498.3U patent/CN211725719U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2022041426A1 (en) | Micro-interface preparation system and method for cyclic carbonate | |
| WO2023138074A1 (en) | Method and system for preparing cyclic carbonate by catalyzing carbon dioxide cycloaddition | |
| CN106475020A (en) | A kind of Oscillatory Flow Reactor for isopropylbenzene catalysis oxidation cumyl hydroperoxide and method | |
| CN211725719U (en) | System for reinforcing chloroethane preparation based on micro-interface | |
| CN112044390A (en) | Preparation system and method of cyclic carbonate | |
| CN114105735A (en) | Preparation method and production device of Guerbet alcohol ether | |
| CN212127531U (en) | Nitric acid industry preparation system based on micro-interface is reinforceed | |
| CN112479804A (en) | System and process for strengthening chloroethane preparation based on micro-interface | |
| CN112499597A (en) | System and process for preparing hydrogen peroxide based on isopropanol method | |
| CN213222199U (en) | Reaction device of vinyl ether compound | |
| CN109265384B (en) | Method for preparing di (2-ethylhexyl) peroxydicarbonate | |
| CN112520757B (en) | Continuous production process and device for nitration synthesis of mixed acid | |
| CN216605220U (en) | Apparatus for producing of hydroxyethylidene/propyl ethylenediamine | |
| CN112495310B (en) | System and process for strengthening propylene polymerization | |
| CN111569791A (en) | Enhanced reaction system and process for catalyzing propylene hydration by ionic liquid | |
| WO2021047046A1 (en) | Microinterface-enhanced system and process for preparing ethylene oxide from ethylene | |
| CN213493589U (en) | Reinforced reaction system for catalyzing propylene hydration by ionic liquid | |
| CN112500509B (en) | System and process for strengthening ethylene polymerization | |
| CN212128043U (en) | System for strengthening propylene polymerization | |
| CN213506658U (en) | Immersed propylene hydration micro-interface enhanced reaction system | |
| CN112694389A (en) | Synthesis method for synthesizing 2,6 di-tert-butyltoluene through heterogeneous catalysis | |
| CN111569785B (en) | Immersed propylene hydration micro-interface enhanced reaction system and process | |
| CN212790997U (en) | Chlorine introducing reaction tank group | |
| CN213505990U (en) | Intelligent control system for industrial preparation of nitric acid | |
| CN213506681U (en) | Micro-interface strengthening system for preparing ethylene oxide from ethylene |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |