CN213506681U - Micro-interface strengthening system for preparing ethylene oxide from ethylene - Google Patents
Micro-interface strengthening system for preparing ethylene oxide from ethylene Download PDFInfo
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- CN213506681U CN213506681U CN201921524170.4U CN201921524170U CN213506681U CN 213506681 U CN213506681 U CN 213506681U CN 201921524170 U CN201921524170 U CN 201921524170U CN 213506681 U CN213506681 U CN 213506681U
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- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 82
- 239000005977 Ethylene Substances 0.000 title claims abstract description 82
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 title claims abstract description 71
- 238000005728 strengthening Methods 0.000 title claims description 9
- 238000006243 chemical reaction Methods 0.000 claims abstract description 110
- QWPPOHNGKGFGJK-UHFFFAOYSA-N hypochlorous acid Chemical compound ClO QWPPOHNGKGFGJK-UHFFFAOYSA-N 0.000 claims abstract description 101
- 239000007788 liquid Substances 0.000 claims abstract description 66
- 238000007127 saponification reaction Methods 0.000 claims abstract description 66
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 29
- 238000000926 separation method Methods 0.000 claims abstract description 27
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 26
- 239000000460 chlorine Substances 0.000 claims abstract description 26
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 26
- 239000000839 emulsion Substances 0.000 claims abstract description 22
- 238000000746 purification Methods 0.000 claims abstract description 18
- 238000004519 manufacturing process Methods 0.000 claims abstract description 8
- 239000012071 phase Substances 0.000 claims description 63
- 239000000463 material Substances 0.000 claims description 37
- 239000007791 liquid phase Substances 0.000 claims description 36
- 230000015572 biosynthetic process Effects 0.000 claims description 30
- 238000003786 synthesis reaction Methods 0.000 claims description 30
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 26
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 26
- 239000004571 lime Substances 0.000 claims description 26
- 239000008267 milk Substances 0.000 claims description 25
- 210000004080 milk Anatomy 0.000 claims description 25
- 235000013336 milk Nutrition 0.000 claims description 25
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims description 17
- 238000002156 mixing Methods 0.000 claims description 5
- 230000002787 reinforcement Effects 0.000 claims 1
- 230000003014 reinforcing effect Effects 0.000 claims 1
- 239000000203 mixture Substances 0.000 abstract description 18
- 238000002360 preparation method Methods 0.000 abstract description 6
- 239000007789 gas Substances 0.000 description 46
- 238000000034 method Methods 0.000 description 39
- 230000008569 process Effects 0.000 description 29
- 239000000243 solution Substances 0.000 description 19
- XENVCRGQTABGKY-ZHACJKMWSA-N chlorohydrin Chemical compound CC#CC#CC#CC#C\C=C\C(Cl)CO XENVCRGQTABGKY-ZHACJKMWSA-N 0.000 description 11
- SZIFAVKTNFCBPC-UHFFFAOYSA-N 2-chloroethanol Chemical compound OCCCl SZIFAVKTNFCBPC-UHFFFAOYSA-N 0.000 description 10
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 7
- 239000012530 fluid Substances 0.000 description 7
- 238000001514 detection method Methods 0.000 description 5
- 239000007792 gaseous phase Substances 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 239000007787 solid Substances 0.000 description 4
- 230000005587 bubbling Effects 0.000 description 3
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 description 3
- -1 other alcohols Chemical compound 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- 239000002202 Polyethylene glycol Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000000844 anti-bacterial effect Effects 0.000 description 1
- 239000003899 bactericide agent Substances 0.000 description 1
- 210000000481 breast Anatomy 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 150000004292 cyclic ethers Chemical class 0.000 description 1
- 239000000645 desinfectant Substances 0.000 description 1
- 239000003599 detergent Substances 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002316 fumigant Substances 0.000 description 1
- 150000002391 heterocyclic compounds Chemical class 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical compound Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000002917 insecticide Substances 0.000 description 1
- 239000002085 irritant Substances 0.000 description 1
- 231100000021 irritant Toxicity 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000002105 nanoparticle Substances 0.000 description 1
- 239000002736 nonionic surfactant Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000006213 oxygenation reaction Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 229920001223 polyethylene glycol Polymers 0.000 description 1
- 239000003380 propellant Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 235000013599 spices Nutrition 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 0.000 description 1
Images
Abstract
The utility model relates to a system is reinforceed to ethylene preparation ethylene oxide's micro-interface, include: a chlorohydrination reaction unit, a saponification reaction unit, a separation and purification unit and a micro-interface generator. The utility model discloses an install little interfacial generator additional and handle chlorine and ethylene, broken chlorine or ethylene make its micron order bubble that forms micron yardstick, make chlorine micron order bubble and water mix and form the gas-liquid emulsion, ethylene micron order bubble forms the gas-liquid emulsion with the hypochlorous acid is mixed, with the double-phase interfacial area of increase gas-liquid, reduce liquid film thickness, reduce mass transfer resistance, the mass transfer efficiency and the reaction efficiency that improve chlorine or ethylene of gas-liquid component improve at the operating condition within range of predetermineeing, in order to ensure that the abundant of reaction is effectively gone on, improve chlorine or ethylene utilization ratio, and then guarantee reaction rate, the purpose of intensive reaction has been reached, reduce ethylene oxide's manufacturing cost.
Description
Technical Field
The utility model relates to an ethylene preparation ethylene oxide technical field especially relates to a system is reinforceed to ethylene preparation ethylene oxide's micro-interface.
Background
The epoxy ethane is the simplest cyclic ether, belongs to heterocyclic compounds, and is colorless transparent liquid at the low temperature of below 10.7 ℃ and colorless gas at normal temperature and normal pressure. It is irritant to eyes, throat and nose when exposed to ethylene oxide gas. The ethylene oxide produced in the industry can be divided into a large amount of ethylene oxide and high-purity ethylene oxide according to purity division, and is mainly used for producing ethylene glycol and ethoxylates in the detergent industry, wherein about 3/4 of ethylene oxide is used for producing ethylene glycol, the special ternary ring structure of the ethylene oxide determines the special reaction activity of the ethylene oxide, and a series of very important fine chemical products can be obtained by deriving the ethylene oxide, such as other alcohols, such as polyethylene glycol, diethylene glycol, triethylene glycol and the like, ethanolamine, glycol ethers, nonionic surfactants, antifreezing agents, plasticizers, additives, solvents, spices, high-energy fuels, propellants and the like. In addition, because of the characteristics of broad spectrum, high efficiency and low temperature sterilization, the ethylene oxide is also used as a fumigant, an insecticide, a bactericide, a disinfectant of disposable medical instruments and the like, and the market demand of the ethylene oxide is vigorous due to the wide application of the ethylene oxide.
The main production methods of ethylene oxide include a chlorohydrin process and an ethylene direct oxidation process, wherein the chlorohydrin process is the earliest industrial method for preparing ethylene oxide, and the chlorohydrin process comprises two reactions:
the first step is that ethylene and chlorine are introduced into water to generate 2-chloroethanol;
the second step is to react alkali (usually lime milk) with 2-chloroethanol to produce ethylene oxide, the ethylene is acidified by hypochloride to produce chloroethanol, then saponified with calcium hydroxide to produce ethylene oxide crude product, and then fractionated to obtain ethylene oxide.
Chinese patent publication No.: CN103896882A discloses a method for preparing ethylene oxide by a chlorohydrination method, wherein ethylene and chlorine are used as raw materials, the main process is divided into two steps, the first step is that the chlorine reacts with water to form hypochlorous acid, and the molar ratio is 1: 1-2; the reaction molar ratio of the hypochlorous acid to the ethylene is 1: 0.5-1; generating chloroethanol; secondly, ethylene oxide is generated by saponification of chloroethanol; the reactor for producing the ethylene oxide by the chlorohydrination method has various forms, the most resident mechanism uses a tower type, and water and chlorine gas enter from the bottom of the tower to generate hypochlorous acid; introducing ethylene at a high position, reacting with hypochlorous acid to generate chloroethanol, and overflowing chloroethanol aqueous solution from the top of the tower, wherein the reaction temperature is 10-50 ℃ and the reaction is normal pressure; the saponification process can be carried out in a kettle type or tower type reactor, lime milk is used as a saponifier, the reaction temperature is 100-102 ℃, the retention time is about thirty minutes, and the saponification can be completed; a tower reactor is adopted and also used as a distillation tower, a chlorohydrin solution and lime milk are simultaneously added into the tower, light component ethylene oxide is evaporated from the top of the tower, and a calcium chloride aqueous solution containing organic matters is discharged from the bottom of the tower. It can be seen that the method has the following problems:
firstly, in the method, ethylene is only introduced at a high position to react with hypochlorous acid to generate chloroethanol, and gas-phase component ethylene enters a reactor to form large bubbles, but the bubbles cannot be fully contacted with liquid-phase components due to overlarge volume, so that the reaction efficiency of the system is reduced.
Secondly, the reaction rate of ethylene and hypochlorous acid is reduced in the method, so that the utilization rate of ethylene is reduced, raw materials are wasted to a great extent, the production cost of ethylene oxide is increased, and the method does not meet the requirement of the existing circular economy.
SUMMERY OF THE UTILITY MODEL
Therefore, the utility model provides a system is reinforceed to ethylene preparation ethylene oxide's micro-interface for overcome the problem that the system reaction efficiency that the inhomogeneous production accessory substance that mixes among the prior art material leads to is low.
The utility model provides a system is reinforceed to ethylene preparation ethylene oxide's micro-interface, include:
a hypochlorous acid synthesis unit for providing reaction sites for chlorine and water;
the chlorohydrination reaction unit is connected with the hypochlorous acid synthesis unit;
the saponification reaction unit is connected with the chlorohydrination reaction unit;
the separation and purification unit is connected with the saponification reaction unit;
the micro-interface generators are arranged in the hypochlorous acid synthesis unit and the chlorohydrination reaction unit respectively, convert pressure energy of gas and/or kinetic energy of liquid into bubble surface energy and transmit the bubble surface energy to the gas-phase component, the gas-phase gas is crushed to form 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 of the gas-phase component and the liquid-phase component, reduce the thickness of a liquid film and reduce mass transfer resistance, and the liquid-phase component and the micron-sized bubbles are mixed to form a gas-liquid emulsion after crushing, so that the mass transfer efficiency and the reaction efficiency of the gas-liquid component are enhanced within a preset operation condition range.
Further, the micro-interface generator is a pneumatic micro-interface generator, and comprises a first micro-interface generator and a second micro-interface generator;
the first micro-interface generator is arranged at the bottom of the reaction zone of the hypochlorous acid synthesis unit and used for crushing chlorine to form micron-sized bubbles and outputting the micron-sized bubbles into the hypochlorous acid synthesis unit after crushing and mixing with water to form a gas-liquid emulsion;
the second micro-interface generator is arranged at the bottom of the reaction area of the chlorohydrination reaction unit and used for crushing ethylene to form micron-scale bubbles and outputting the micron-scale bubbles into the chlorohydrination reaction unit after crushing is finished to be mixed with the liquid-phase material output by the hypochlorous acid synthesis unit to form a gas-liquid emulsion.
Further, the hypochlorous acid synthesis unit comprises:
the hypochlorous acid reactor is used for providing a reaction site for chlorine and water;
the gas phase feeding pipeline is arranged on the side wall of the hypochlorous acid reactor, is connected with the first micro-interface generator, and is used for conveying chlorine gas into the first micro-interface generator and enabling the micro-interface generator to crush the chlorine gas;
a liquid phase feed conduit disposed in a sidewall of the hypochlorous acid reactor and above the gas phase feed conduit to deliver water into the hypochlorous acid reactor;
further, the hypochlorous acid synthesis unit further comprises:
the first gas phase return pipe is arranged on the hypochlorous acid reactor, is connected with the first micro-interface generator and is used for returning gas phase components to the hypochlorous acid reactor;
and the gas-liquid separator is connected with the hypochlorous acid reactor and is used for carrying out gas-liquid separation on the output materials of the hypochlorous acid reactor.
Further, the chlorohydrination reaction unit comprises:
the chlorohydrination reactor is connected with the gas-liquid separator and is used for providing a reaction site for hypochlorous acid and ethylene;
and the ethylene feeding pipeline is arranged on the side wall of the chlorohydrination reactor and is connected with the second micro-interface generator, and is used for conveying ethylene into the second micro-interface generator and enabling the micro-interface generator to crush the ethylene.
Further, the chlorohydrination reaction unit also comprises:
and the second gas phase return pipe is arranged on the chlorohydrination reactor, is connected with the second micro-interface generator and is used for returning the gas phase components to the chlorohydrination reactor.
Further, the saponification reaction unit comprises:
and the saponification reactor is connected with the chlorohydrination reactor and is used for providing a reaction site for outputting the liquid-phase material and the lime milk for the chlorohydrination reaction unit.
Further, the saponification reaction unit also comprises:
a lime milk feed conduit disposed in a side wall of the saponification reactor for conveying lime milk into the saponification reactor.
Further, the separation and purification unit comprises:
and the rectifying tower is connected with the saponification reaction unit and is used for rectifying and separating the materials output by the saponification reaction unit.
Further, the separation and purification unit further comprises:
and the heat exchanger is connected with the saponification reaction unit and the rectifying tower and is used for exchanging energy between the material output by the saponification reaction unit and ethylene oxide.
Compared with the prior art, the utility model has the advantages that the main structure of the system of the utility model is formed by the chlorohydrination reaction unit, the saponification reaction unit, the separation and purification unit, the micro-interface generator and the intelligent control unit, micron-sized bubbles are formed by crushing chlorine gas, and the micron-sized bubbles are mixed with water to form gas-liquid emulsion, so that the gas-liquid two-phase interfacial area is increased, the synthetic efficiency of hypochlorous acid is improved, the chlorine gas reaction efficiency is improved, and the cost is saved; the utility model discloses through hypochlorous acid synthetic unit in the system for chlorine and water provide the reaction site, and separate the resultant, chlorohydrination reaction unit links to each other with hypochlorous acid synthetic unit, be used for providing the reaction site for hypochlorous acid synthetic unit output material and ethylene, saponification reaction unit links to each other with chlorohydrination reaction unit, be used for providing the reaction site for chlorohydrination reaction unit output liquid phase material and lime breast, separation purification unit links to each other with saponification reaction unit, be used for carrying out the rectification separation for exporting the liquid phase material. The method can flexibly adjust the range of the preset operation conditions of the chlorine gas according to different product requirements so as to ensure the full and effective reaction, further ensure the reaction rate and achieve the purpose of strengthening the reaction.
Especially, the utility model discloses a hypochlorous acid has set up the hypochlorous acid reactor in the synthetic unit of hypochlorous acid, gaseous phase feed pipeline, liquid phase feed pipeline, first gaseous phase back flow and vapour and liquid separator, it provides the reaction site for chlorine gas and water to improve the hypochlorous acid reactor, carry chlorine to first micro-interface generator in through gaseous phase feed pipeline, and make micro-interface generator carry out the breakage to chlorine gas, carry water to the hypochlorous acid reactor in through the liquid phase inlet pipe, pass through first gaseous phase back flow with gaseous phase component feedback to the hypochlorous acid reactor in, carry out gas-liquid separation to hypochlorous acid reactor output material through vapour and liquid separator, realize water and chlorine high efficiency reaction, improve chlorine material utilization ratio.
In particular, the chlorohydrination reaction unit of the present invention is provided with a chlorohydrination reactor, an ethylene feeding pipe and a second gas phase return pipe, and through the chlorohydrination reactor, a reaction site is provided for hypochlorous acid and ethylene, ethylene is fed into the second micro-interface generator through the ethylene feeding pipe, and the micro-interface generator is used for crushing ethylene. And the gas-phase components are returned to the chlorohydrination reactor through the second gas-phase return pipe, so that the high-efficiency reaction of ethylene and hypochlorous acid is realized, and the utilization rate of ethylene raw materials is improved.
Especially, the utility model discloses a saponification reaction unit has set up saponification reactor and lime milk charge-in pipeline, provides the reaction site for chlorohydrination reaction unit output liquid phase material and lime milk through the saponification reactor, carries lime milk to the saponification reactor in through lime milk charge-in pipeline, obtains ethylene oxide through the saponification reaction of chlorohydrin with lime milk.
In particular, the separation and purification unit of the utility model is provided with a heat exchanger and a rectifying tower; energy exchange is carried out on the saponification reaction unit output material and ethylene oxide through the heat exchanger, rectification separation is carried out on the saponification reaction unit output material through the rectifying tower, wherein the ethylene oxide gas exchanges heat with the ethylene oxide mixture in the heat exchanger, the energy utilization rate is improved, and the energy consumption is saved.
Drawings
Fig. 1 is a schematic structural diagram of a system of a micro-interface strengthening system for preparing ethylene oxide from ethylene 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 micro interface strengthening system for preparing ethylene oxide from ethylene according to the present invention, including a chlorohydrination reaction unit 1, a chlorohydrination reaction unit 2, a saponification reaction unit 3, a separation and purification unit 4, and a micro interface generator 5. The hypochlorous acid synthesis unit 1 is used for providing reaction places for chlorine and water and separating generated materials, the chlorohydrination reaction unit 2 is connected with the hypochlorous acid synthesis unit 1 and is used for providing a reaction place for the output materials of the hypochlorous acid synthesis unit and ethylene, the saponification reaction unit 3 is connected with the chlorohydrination reaction unit 2 and is used for providing a reaction place for the output liquid phase materials of the chlorohydrination reaction unit and lime milk, the separation and purification unit 4 is connected with the saponification reaction unit and is used for rectifying and separating the output liquid phase materials, the micro-interface generator 5 is respectively arranged at the established positions of the hypochlorous acid synthesis unit 1 and the chlorohydrination reaction unit 2 and converts the pressure energy and/or the kinetic energy of the liquid into the surface energy of bubbles and transmits the surface energy to a gas phase component to crush the gas phase to form a material with a diameter of more than or equal to 1 mu m, And micron-sized bubbles smaller than 1 mm.
When the system is operated, the gas-phase component of the micro-interface generator 5 is crushed to form micron-scale micro-bubbles and the mixture of the micron-scale micro-bubbles and the liquid-phase component is mixed to form gas-liquid emulsion. It will be understood by those skilled in the art that the micro-interface generator 5 of the present invention can also be used in other multi-phase reactions, such as by micro-interface, micro-nano interface, micro-micro interface, micro-bubble biochemical reactor or micro-bubble bioreactor, using micro-mixing, micro-fluidization, micro-bubble fermentation, micro-bubble bubbling, micro-bubble mass transfer, micro-bubble reaction, micro-bubble absorption, micro-bubble oxygenation, micro-bubble contact, etc. to form multi-phase micro-mixed flow, multi-phase micro-nano flow, multi-phase emulsified flow, multi-phase micro-structured flow, gas-liquid-solid micro-mixed flow, gas-liquid-solid micro-nano flow, gas-liquid-solid emulsified flow, gas-liquid-solid micro-structured flow, micro-micron-sized bubble flow, micro-foam flow, micro-bubble liquid flow, gas-liquid-micro-nano emulsified flow, micro-mixed flow, micro-, The multiphase fluid formed by micron-scale particles such as micro-bubbling flow, micro-nano bubbling and micro-nano bubbling flow or the multiphase fluid formed by micro-nano-scale particles (micro-interface fluid for short) effectively increases the phase boundary mass transfer area between the gas phase and/or the liquid phase and/or the solid phase in the reaction process.
With continued reference to fig. 1, the micro-interface generator 5 is a pneumatic micro-interface generator, and the micro-interface generator 5 includes a first micro-interface generator 51 and a second micro-interface generator 52;
the first micro-interface generator 51 is arranged at the bottom of the reaction zone of the hypochlorous acid synthesis unit 1 and is used for crushing chlorine gas to form micron-sized bubbles and outputting the micron-sized bubbles into the hypochlorous acid synthesis unit after crushing is finished and mixing the micron-sized bubbles with water to form a gas-liquid emulsion;
when the system is operated, the gas-phase component chlorine of the first micro-interface generator 51 is broken to form micron-scale micro-scale bubbles and the micron-scale bubbles and the mixture of the liquid-phase component water are mixed to form a gas-liquid emulsion;
the second micro-interface generator 52 is arranged at the bottom of the reaction zone of the chlorohydrination reaction unit 2 and is used for crushing ethylene to form micron-sized bubbles, outputting the micron-sized bubbles into the chlorohydrination reaction unit after crushing is finished, and mixing the micron-sized bubbles with a liquid-phase material output by the hypochlorous acid synthesis unit to form a gas-liquid emulsion;
when the system is operated, the gas-phase component ethylene of the second micro-interface generator 52 is broken to form micron-scale micro-bubbles and the micro-bubbles are mixed with a mixture of the liquid-phase component hypochlorous acid to form a gas-liquid emulsion.
With continued reference to figure 1, the hypochlorous acid synthesis unit 1 includes: a hypochlorous acid reactor 11, a gas phase feeding pipeline 12, a liquid phase feeding pipeline 13, a first gas phase return pipe 14 and a gas-liquid separator 15;
a hypochlorous acid reactor 11 for providing a reaction site for chlorine and water;
a gas phase feed pipe 12, which is arranged on the side wall of the hypochlorous acid reactor 1 and is connected with the first micro-interface generator 51, and is used for conveying chlorine gas into the first micro-interface generator and enabling the micro-interface generator to crush the chlorine gas;
a liquid phase feed conduit 13 disposed at a sidewall of the hypochlorous acid reactor 1 and above the gas phase feed conduit 11, for delivering water into the hypochlorous acid reactor;
a first gas phase reflux pipe 14 disposed on the hypochlorous acid reactor 1 and connected to the first micro-interface generator 51, for feeding back gas phase components into the hypochlorous acid reactor;
the gas-liquid separator 15 is connected with the hypochlorous acid reactor 1 and is used for carrying out gas-liquid separation on the output materials of the hypochlorous acid reactor;
when the system is operated, the hypochlorous acid reactor 11 is used as a reactor of chlorine and water, water is conveyed into the hypochlorous acid reactor 11 through the liquid phase feeding pipeline 13, chlorine is conveyed into the first micro-interface generator 51 through the gas phase feeding pipeline 12, the chlorine is crushed by the first micro-interface generator 51 to form micron-scale micro-bubbles, after the crushing is completed, the micron-scale micro-bubbles are output to the hypochlorous acid reactor 11 by the first micro-interface generator 51 and are mixed with water to form a gas-liquid emulsion, the gas-liquid emulsion is reacted to generate a hypochlorous acid mixture, the chlorine which is not fully reacted in the hypochlorous acid reactor 1 flows back into the first micro-interface generator 51 along the first gas phase return pipe 14 at the top of the hypochlorous acid reactor 1, the chlorine is crushed by the first micro-interface generator 51 and is further reacted with water, the liquid phase components in the hypochlorous acid reactor 1 flow into the gas-liquid separator 15, after gas-liquid separation, tail gas is discharged along a gas phase outlet at the top of the gas-liquid separator 15, and hypochlorous acid solution is discharged along a liquid phase outlet at the bottom of the gas-liquid separator 15 and is transmitted to the chlorohydrination reaction unit 2, it can be understood that the material and size of the gas phase feed pipeline 12, the liquid phase feed pipeline 13 and the first gas phase return pipe 14 are not particularly limited in this embodiment, as long as the requirement that the gas phase feed pipeline 12, the liquid phase feed pipeline 13 and the first gas phase return pipe 14 can convey materials with specified volume within specified time is met.
With continued reference to FIG. 1, the chlorohydrination reaction unit 2 includes: a chlorohydrination reactor 21, an ethylene feed line 22 and a second gas phase return line 23;
a chlorohydrination reactor 21 connected to the gas-liquid separator 15 to provide a reaction site for hypochlorous acid and ethylene;
an ethylene feeding pipe 22, which is arranged on the side wall of the chlorohydrination reactor 2 and is connected to the second micro-interfacial generator 52, for feeding ethylene into the second micro-interfacial generator and causing the micro-interfacial generator to crush ethylene;
a second gas phase return pipe 23, which is arranged on the chlorohydrination reactor 2 and connected with the second micro-interface generator 52, for returning the gas phase components to the chlorohydrination reactor;
when the system is in operation, the hypochlorous acid solution enters the chlorohydrination reactor 21, ethylene is conveyed into the chlorohydrination reactor 21 through the ethylene feed pipe 22, the ethylene feed pipe 22 conveys ethylene gas to the second micro-interface generator 52, the second micro-interface generator 52 crushes ethylene to form micron-sized bubbles, after the crushing is completed, the second micro-interface generator 52 outputs the micron-sized bubbles to the chlorohydrination reactor 21 and mixes the micron-sized bubbles with the hypochlorous acid solution to form a gas-liquid emulsion, the gas-liquid emulsion reacts to generate a chlorohydrin solution, the chlorohydrin solution in the chlorohydrination reactor 21 flows out and is conveyed to the saponification reaction unit 3, the ethylene which is not fully reacted in the chlorohydrination reactor 21 flows back into the second micro-interface generator 52 along the second gas-phase return pipe 23 at the top of the chlorohydrination reactor 21, and ethylene is crushed by the second micro-interface generator 52 and further reacts with hypochlorous acid solution, it is understood that the materials and dimensions of the ethylene feeding pipe 22 and the second gas phase reflux pipe 23 are not particularly limited in this embodiment as long as the ethylene feeding pipe 22 and the second gas phase reflux pipe 23 can deliver the specified volume of the material within the specified time.
With continued reference to FIG. 1, the saponification reaction unit 3 includes: a saponification reactor 31 and a lime milk feed line 32;
the saponification reactor 31 is connected with the chlorohydrination reactor 21 and is used for providing a reaction site for outputting a liquid-phase material and lime milk for the chlorohydrination reaction unit;
a lime milk feed conduit 32 arranged in the side wall of the saponification reactor 31 for conveying lime milk into the saponification reactor.
When the system is in operation, the chlorohydrin solution flows into the saponification reaction unit 3, lime milk, the main component of which is calcium hydroxide and has strong basicity, is conveyed into the saponification reaction unit 31 through a lime milk feeding pipe 32, and saponification reaction is carried out between the lime milk and the chlorohydrin solution in the saponification reaction unit 3 to generate an ethylene oxide mixture, and the ethylene oxide mixture flows out in the saponification reaction and is conveyed to a separation and purification unit 4.
With continued reference to fig. 1, the separation and purification unit 4 includes: a heat exchanger 41 and a rectifying column 42;
the heat exchanger 41 is connected with the saponification reaction unit 3 and is used for exchanging energy between the material output by the saponification reaction unit and ethylene oxide;
the rectifying tower 42 is connected with the heat exchanger 41 and is used for rectifying and separating the materials output by the saponification reaction unit;
when the system is operated, the ethylene oxide mixture flows into the separation and purification unit 4, wherein the ethylene oxide mixture flows through the heat exchanger 41 and enters the rectification tower 42 for rectification, the light component (low-boiling-point substance) in the liquid phase is transferred into the gas phase and the heavy component (high-boiling-point substance) in the gas phase is transferred into the liquid phase by utilizing the property that each component in the mixture has different volatility, namely the vapor pressure of each component is different at the same temperature, so that the separation purpose is realized, the gas-phase material output by the rectification tower 42 is ethylene oxide gas, other waste water is discharged along the bottom of the rectification tower 42, wherein the ethylene oxide gas exchanges heat with the ethylene oxide mixture in the heat exchanger 41, the heat transfer between the materials is realized between the ethylene oxide product with different temperatures and two fluids of the saponification reaction unit output material through the heat exchanger 41, so that the heat is transferred from the fluid with higher temperature to the fluid with lower temperature, the fluid temperature is enabled to reach the index specified by the flow, energy is saved, emission is reduced, and an ethylene oxide product is obtained, it can be understood that the type and power of the heat exchanger 41 are not specifically limited in this embodiment as long as the heat exchanger 41 can reach the specified working state, the rectifying tower 42 can be of any type, such as a plate type and a packing type, and the type of the rectifying tower 42 are not specifically limited in this embodiment as long as the rectifying tower 42 can reach the specified working state.
In order to make the objects and advantages of the present invention more apparent, the present invention will be further described with reference to the following embodiments; it should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
A micro-interface strengthening process for preparing ethylene oxide from ethylene comprises the following steps:
a hypochlorous acid synthesis procedure:
step 1: delivering water into the hypochlorous acid reactor through the liquid phase feed conduit;
step 2: conveying chlorine gas into the hypochlorous acid reactor through the gas-phase feeding pipeline, wherein the gas-phase feeding pipeline can convey the chlorine gas to the first micro-interface generator, the first micro-interface generator is used for crushing the chlorine gas to form micron-scale micron-sized bubbles, after crushing is completed, the first micro-interface generator outputs the micron-scale bubbles to the hypochlorous acid reactor and mixes the micron-scale bubbles with water to form a gas-liquid emulsion, and the gas-liquid emulsion reacts to generate a hypochlorous acid mixture;
and step 3: the chlorine gas which is not fully reacted in the hypochlorous acid reactor flows back to the first micro-interface generator along the first gas phase return pipe at the top of the hypochlorous acid reactor, and is crushed by the first micro-interface generator and further reacts with water;
and 4, step 4: the liquid phase components in the hypochlorous acid reactor flow into the gas-liquid separator, after gas-liquid separation, tail gas is discharged along a gas phase outlet at the top of the gas-liquid separator, and hypochlorous acid solution is discharged along a liquid phase outlet at the bottom of the gas-liquid separator and is transmitted to a chlorohydrination reaction unit;
chlorohydrination reaction procedure:
and 5: a hypochlorous acid solution enters the chlorohydrination reactor, ethylene is conveyed into the chlorohydrination reactor through the ethylene feeding pipeline, the ethylene feeding pipeline conveys ethylene gas to the second micro-interface generator, and the second micro-interface generator crushes the ethylene to form micron-sized bubbles;
step 6: after the crushing is finished, the second micro-interface generator outputs micron-sized bubbles to the chlorohydrination reactor and mixes the micron-sized bubbles with hypochlorous acid solution to form gas-liquid emulsion, the gas-liquid emulsion reacts to generate chlorohydrin solution, and the chlorohydrin solution in the chlorohydrination reactor flows out and is transmitted to a saponification reaction unit;
and 7: ethylene which is not fully reacted in the chlorohydrination reactor flows back to the second micro-interface generator along the second gas phase return pipe at the top of the chlorohydrination reactor, and the ethylene is crushed by the second micro-interface generator and further reacts with hypochlorous acid solution;
a saponification process:
and 8: a chloroethanol solution flows into the saponification reaction unit, lime milk is conveyed into the saponification reaction unit through a lime milk feeding pipeline, saponification reaction is carried out on the lime milk and the chloroethanol solution in the saponification reaction unit to generate an ethylene oxide mixture, and the ethylene oxide mixture in the saponification reaction flows out and is conveyed to a separation and purification unit;
a separation and purification process:
and step 9: and the ethylene oxide mixture flows into the separation and purification unit, wherein the ethylene oxide mixture flows through the heat exchanger and enters the rectifying tower for rectification, the gas-phase material output by the rectifying tower is ethylene oxide gas, other wastewater is discharged along the tower bottom of the rectifying tower, and the ethylene oxide gas exchanges heat with the ethylene oxide mixture in the heat exchanger and is discharged, so that an ethylene oxide product is obtained.
Example 1
The above system and process are used for ethylene to ethylene oxide, wherein:
in the process, the reaction temperature in the hypochlorous acid reactor is 10 ℃ and normal pressure;
the gas-liquid ratio in the first micro-interface generator is 120: 1;
the reaction temperature in the chlorohydrination reactor is 37 ℃ and 0.13 MPa;
the gas-liquid ratio in the second micro-interfacial generator was 115: 1;
the reaction temperature in the saponification reactor is 89 ℃, and the reaction temperature is normal pressure.
After detection, the ethylene conversion rate is 98.7% and the synthesis efficiency of the process is improved by 3.7% after the system and the process are used.
Example 2
The above system and process are used for ethylene to ethylene oxide, wherein:
in the process, the reaction temperature in a hypochlorous acid reactor is 12 ℃ and normal pressure;
the gas-liquid ratio in the first micro-interface generator is 123: 1;
the reaction temperature in the chlorohydrination reactor is 39 ℃ and 0.16 MPa;
the gas-liquid ratio in the second micro-interfacial generator was 118: 1;
the reaction temperature in the saponification reactor is 89 ℃, and the reaction temperature is normal pressure.
After detection, the ethylene conversion rate is 98.6% and the synthesis efficiency of the process is improved by 3.8% after the system and the process are used.
Example 3
The above system and process are used for ethylene to ethylene oxide, wherein:
in the process, the reaction temperature in the hypochlorous acid reactor is 17 ℃ and normal pressure;
the gas-liquid ratio in the first micro-interface generator is 127: 1;
the reaction temperature in the chlorohydrination reactor is 41 ℃ and 0.18 MPa;
the gas-liquid ratio in the second micro-interfacial generator was 123: 1;
the reaction temperature in the saponification reactor is 93 ℃ and normal pressure.
After detection, the ethylene conversion rate is 98.8% and the synthesis efficiency of the process is improved by 3.8% after the system and the process are used.
Example 4
The above system and process are used for ethylene to ethylene oxide, wherein:
in the process, the reaction temperature in the hypochlorous acid reactor is 19 ℃ and normal pressure;
the gas-liquid ratio in the first micro-interface generator is 128: 1;
the reaction temperature in the chlorohydrination reactor is 45 ℃ and 0.19 MPa;
the gas-liquid ratio in the second micro-interfacial generator was 124: 1;
the reaction temperature in the saponification reactor is 96 ℃, and the reaction temperature is normal pressure.
After detection, the ethylene conversion rate is 98.9% and the synthesis efficiency of the process is improved by 3.9% after the system and the process are used.
Example 5
The above system and process are used for ethylene to ethylene oxide, wherein:
in the process, the reaction temperature in the hypochlorous acid reactor is 20 ℃ and normal pressure;
the gas-liquid ratio in the first micro-interface generator is 130: 1;
the reaction temperature in the chlorohydrination reactor is 47 ℃ and 0.19 MPa;
the gas-liquid ratio in the second micro-interfacial generator was 125: 1;
the reaction temperature in the saponification reactor is 97 ℃ and the pressure is normal.
Through detection, after the system and the process are used, the conversion rate of ethylene is 99.0%, and the synthesis efficiency of the process is improved by 4.0%.
Comparative example
The ethylene preparation of ethylene oxide was carried out using the prior art, wherein the process parameters selected in this example were the same as those in the example 5.
After the system and the process are used, the ethylene conversion rate is 73.3 percent.
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 micro-interfacial strengthening of ethylene to ethylene oxide, comprising:
a hypochlorous acid synthesis unit for providing reaction sites for chlorine and water;
the chlorohydrination reaction unit is connected with the hypochlorous acid synthesis unit;
the saponification reaction unit is connected with the chlorohydrination reaction unit;
the separation and purification unit is connected with the saponification reaction unit;
the micro-interface generators are arranged in the hypochlorous acid synthesis unit and the chlorohydrination reaction unit respectively, convert pressure energy of gas and/or kinetic energy of liquid into bubble surface energy and transmit the bubble surface energy to the gas-phase component, the gas-phase gas is crushed to form 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 of the gas-phase component and the liquid-phase component, reduce the thickness of a liquid film and reduce mass transfer resistance, and the liquid-phase component and the micron-sized bubbles are mixed to form a gas-liquid emulsion after crushing, so that the mass transfer efficiency and the reaction efficiency of the gas-liquid component are enhanced within a preset operation condition range.
2. The system of claim 1, wherein the micro-interface generator is a pneumatic micro-interface generator comprising a first micro-interface generator and a second micro-interface generator;
the first micro-interface generator is arranged at the bottom of the reaction zone of the hypochlorous acid synthesis unit and used for crushing chlorine to form micron-sized bubbles and outputting the micron-sized bubbles into the hypochlorous acid synthesis unit after crushing and mixing with water to form a gas-liquid emulsion;
the second micro-interface generator is arranged at the bottom of the reaction area of the chlorohydrination reaction unit and used for crushing ethylene to form micron-scale bubbles and outputting the micron-scale bubbles into the chlorohydrination reaction unit after crushing is finished to be mixed with the liquid-phase material output by the hypochlorous acid synthesis unit to form a gas-liquid emulsion.
3. The micro-interfacial strengthening system for ethylene oxide production according to claim 2, wherein the hypochlorous acid synthesis unit comprises:
the hypochlorous acid reactor is used for providing a reaction site for chlorine and water;
the gas phase feeding pipeline is arranged on the side wall of the hypochlorous acid reactor, is connected with the first micro-interface generator, and is used for conveying chlorine gas into the first micro-interface generator and enabling the micro-interface generator to crush the chlorine gas;
a liquid phase feed conduit disposed in a sidewall of the hypochlorous acid reactor and above the gas phase feed conduit to deliver water into the hypochlorous acid reactor.
4. The micro-interfacial strengthening system for ethylene oxide production according to claim 3, wherein the hypochlorous acid synthesis unit further comprises:
the first gas phase return pipe is arranged on the hypochlorous acid reactor, is connected with the first micro-interface generator and is used for returning gas phase components to the hypochlorous acid reactor;
and the gas-liquid separator is connected with the hypochlorous acid reactor and is used for carrying out gas-liquid separation on the output materials of the hypochlorous acid reactor.
5. The system for micro-interfacial reinforcement of ethylene oxide according to claim 4, wherein the chlorohydrination reaction unit comprises:
the chlorohydrination reactor is connected with the gas-liquid separator and is used for providing a reaction site for hypochlorous acid and ethylene;
and the ethylene feeding pipeline is arranged on the side wall of the chlorohydrination reactor and is connected with the second micro-interface generator, and is used for conveying ethylene into the second micro-interface generator and enabling the micro-interface generator to crush the ethylene.
6. The micro-interface enhancement system for preparing ethylene oxide from ethylene according to claim 5, wherein the chlorohydrination reaction unit further comprises:
and the second gas phase return pipe is arranged on the chlorohydrination reactor, is connected with the second micro-interface generator and is used for returning the gas phase components to the chlorohydrination reactor.
7. The micro-interface reinforcing system for preparing ethylene oxide from ethylene according to claim 1, wherein the saponification reaction unit comprises:
and the saponification reactor is connected with the chlorohydrination reactor and is used for providing a reaction site for outputting the liquid-phase material and the lime milk for the chlorohydrination reaction unit.
8. The micro-interface enhancement system for ethylene to ethylene oxide of claim 7, wherein the saponification reaction unit further comprises:
a lime milk feed conduit disposed in a side wall of the saponification reactor for conveying lime milk into the saponification reactor.
9. The micro-interface enhancement system for preparing ethylene oxide from ethylene according to claim 1, wherein the separation and purification unit comprises:
and the rectifying tower is connected with the saponification reaction unit and is used for rectifying and separating the materials output by the saponification reaction unit.
10. The system of claim 9, wherein the separation and purification unit further comprises:
and the heat exchanger is connected with the saponification reaction unit and the rectifying tower and is used for exchanging energy between the material output by the saponification reaction unit and ethylene oxide.
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