CN112500372A - Intelligent control system and process for preparing ethylene oxide from ethylene - Google Patents
Intelligent control system and process for preparing ethylene oxide from ethylene Download PDFInfo
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- CN112500372A CN112500372A CN201910867735.7A CN201910867735A CN112500372A CN 112500372 A CN112500372 A CN 112500372A CN 201910867735 A CN201910867735 A CN 201910867735A CN 112500372 A CN112500372 A CN 112500372A
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- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 109
- 239000005977 Ethylene Substances 0.000 title claims abstract description 109
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 title claims abstract description 77
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 13
- QWPPOHNGKGFGJK-UHFFFAOYSA-N hypochlorous acid Chemical compound ClO QWPPOHNGKGFGJK-UHFFFAOYSA-N 0.000 claims abstract description 139
- 238000006243 chemical reaction Methods 0.000 claims abstract description 128
- 239000007788 liquid Substances 0.000 claims abstract description 69
- 238000007127 saponification reaction Methods 0.000 claims abstract description 69
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 36
- 239000000460 chlorine Substances 0.000 claims abstract description 36
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 36
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 30
- 238000000926 separation method Methods 0.000 claims abstract description 28
- 239000000839 emulsion Substances 0.000 claims abstract description 24
- 238000000746 purification Methods 0.000 claims abstract description 20
- 239000012071 phase Substances 0.000 claims description 75
- 239000000463 material Substances 0.000 claims description 44
- 238000000034 method Methods 0.000 claims description 43
- 238000003786 synthesis reaction Methods 0.000 claims description 42
- 230000015572 biosynthetic process Effects 0.000 claims description 41
- 238000012545 processing Methods 0.000 claims description 39
- 239000007791 liquid phase Substances 0.000 claims description 38
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 31
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 31
- 239000004571 lime Substances 0.000 claims description 31
- 239000008267 milk Substances 0.000 claims description 31
- 210000004080 milk Anatomy 0.000 claims description 31
- 235000013336 milk Nutrition 0.000 claims description 31
- 230000008569 process Effects 0.000 claims description 22
- SZIFAVKTNFCBPC-UHFFFAOYSA-N 2-chloroethanol Chemical compound OCCCl SZIFAVKTNFCBPC-UHFFFAOYSA-N 0.000 claims description 20
- 239000000203 mixture Substances 0.000 claims description 20
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims description 18
- 238000002156 mixing Methods 0.000 claims description 8
- 238000012546 transfer Methods 0.000 claims description 8
- 238000001514 detection method Methods 0.000 claims description 4
- 238000012216 screening Methods 0.000 claims description 3
- 239000002351 wastewater Substances 0.000 claims description 3
- 230000005501 phase interface Effects 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 19
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 7
- XENVCRGQTABGKY-ZHACJKMWSA-N chlorohydrin Chemical compound CC#CC#CC#CC#C\C=C\C(Cl)CO XENVCRGQTABGKY-ZHACJKMWSA-N 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 239000002994 raw material Substances 0.000 description 4
- 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
- 239000012530 fluid Substances 0.000 description 3
- -1 polyethylene Polymers 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
- 238000010586 diagram Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- 239000004698 Polyethylene Substances 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
- 230000004075 alteration Effects 0.000 description 1
- 230000000844 anti-bacterial effect Effects 0.000 description 1
- 239000003899 bactericide agent Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 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
- 239000002917 insecticide Substances 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
- 239000002245 particle Substances 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 229920001223 polyethylene glycol Polymers 0.000 description 1
- 229920000915 polyvinyl chloride Polymers 0.000 description 1
- 239000004800 polyvinyl chloride Substances 0.000 description 1
- 239000003380 propellant Substances 0.000 description 1
- 238000010992 reflux Methods 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
- 238000005728 strengthening Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/02—Synthesis of the oxirane ring
- C07D301/24—Synthesis of the oxirane ring by splitting off HAL—Y from compounds containing the radical HAL—C—C—OY
- C07D301/26—Y being hydrogen
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/32—Separation; Purification
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D303/00—Compounds containing three-membered rings having one oxygen atom as the only ring hetero atom
- C07D303/02—Compounds containing oxirane rings
- C07D303/04—Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
Abstract
The invention relates to an intelligent control system and a process for preparing ethylene oxide from ethylene, which comprises the following steps: the device comprises a chlorohydrination reaction unit, a saponification reaction unit, a separation and purification unit, a micro-interface generator and an intelligent control unit. According to the invention, the chlorine and the ethylene are treated by additionally arranging the micro-interface generator, the chlorine or the ethylene is crushed to form micron-sized bubbles, the micron-sized bubbles of the chlorine are mixed with water to form a gas-liquid emulsion, the micron-sized bubbles of the ethylene are mixed with hypochlorous acid to form the gas-liquid emulsion, so that the phase interface area of gas-liquid two phases is increased, the reaction efficiency of the chlorine or the ethylene is improved, the utilization rate of the chlorine or the ethylene is improved, the production cost of the ethylene oxide is reduced, through the intelligent control unit, a worker can know the real-time condition of each data transmitted back by the intelligent sensing module at any time through mobile equipment, and can realize the accurate control of the temperature and the pressure in the whole reactor by changing the preset value, so that.
Description
Technical Field
The invention relates to the technical field of ethylene preparation of ethylene oxide, in particular to an intelligent control system and process for preparing ethylene oxide from ethylene.
Background
Ethylene oxide is the simplest cyclic ether, belongs to heterocyclic compounds, is an important organic chemical product in ethylene industrial derivatives, is second to polyethylene and polyvinyl chloride, is an organic synthesis intermediate with wide application, is mainly used for producing ethylene glycol and ethoxylates in detergent industry, wherein ethylene oxide of about 3/4 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.
Thirdly, the method cannot automatically optimize and regulate the temperature and pressure of the system according to the real-time parameters of the reaction system, so that the reaction efficiency of the system is influenced.
Disclosure of Invention
Therefore, the invention provides an intelligent control system and process for preparing ethylene oxide from ethylene, which are used for solving the problem of low system reaction efficiency caused by-products generated by nonuniform mixing of materials in the prior art.
In one aspect, the present invention provides an intelligent control system for ethylene to ethylene oxide, comprising:
the hypochlorous acid synthesis unit is used for providing reaction sites for chlorine and water and separating generated materials;
the chlorohydrination reaction unit is connected with the hypochlorous acid synthesis unit and is used for providing a reaction site for the output material of the hypochlorous acid synthesis unit and ethylene;
the saponification reaction unit is connected with the chlorohydrination reaction unit and is used for providing a reaction site for outputting a liquid-phase material and lime milk by the chlorohydrination reaction unit;
the separation and purification unit is connected with the saponification reaction unit and is used for rectifying and separating the output liquid-phase material;
the micro-interface generators are arranged in the hypochlorous acid synthesis unit and the chlorohydrination reaction unit respectively, convert the pressure energy of gas and/or the kinetic energy of liquid into the surface energy of bubbles and transmit the surface energy to the gas-phase component, so that the gas-phase gas is crushed into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm, the mass transfer area of the gas-phase component and the liquid-phase component is increased, the thickness of a liquid film is reduced, the mass transfer resistance is reduced, 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 the range of preset operating conditions;
an intelligent control unit which is connected with the hypochlorous acid synthesis unit and the chlorohydrination reaction unit and is used for intelligently controlling the system, wherein the intelligent control unit comprises an intelligent sensing module, a cloud processing module, an intelligent control module, an emergency early warning module and a power supply module, the intelligent sensing module, the intelligent control module, the emergency early warning module and the power supply module are all connected with the cloud processing module, the intelligent sensing module is used for collecting data and transmitting the collected electric signals to the cloud processing module, the cloud processing module is used for carrying out cloud database analysis, screening and comparison on data parameters returned by the intelligent sensing module, optimizing optimal control parameters and sending corresponding control instructions to the intelligent control module, and meanwhile, when the data parameters reach preset values of operation limits, the cloud processing module sends corresponding instructions to the emergency early warning module, and the intelligent control module is used for controlling and adjusting the system, the emergency early warning module is used for early warning the operation limit, and the power supply module is used for supplying electric energy to the automatic control unit.
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;
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;
the ethylene feeding pipeline is arranged on the side wall of the chlorohydrination reactor, 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;
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:
the saponification reactor is connected with the chlorohydrination reactor 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 disposed in a side wall of the saponification reactor for conveying lime milk into the saponification reactor;
further, the separation and purification unit comprises:
the heat exchanger is connected with the saponification reaction unit and is used for exchanging energy between the material output by the saponification reaction unit and ethylene oxide;
and the rectifying tower is connected with the heat exchanger and is used for rectifying and separating the materials output by the saponification reaction unit.
Further, the smart sensor module includes:
the temperature sensors are arranged in the hypochlorous acid reactor and the chlorohydrination reactor and are respectively used for detecting the reaction temperature in the hypochlorous acid reactor and the chlorohydrination reactor;
the pressure sensor is used for detecting pressure and arranged in the chlorohydrination reactor and used for detecting the reaction pressure in the hypochlorous acid reactor and the chlorohydrination reactor;
and the flow sensor is used for detecting flow, is arranged in the gas-phase feeding pipeline and the ethylene feeding pipeline and is respectively used for detecting the chlorine and the ethylene flow.
Further, the intelligent control module comprises:
a first controller for controlling the hypochlorous acid reactor to work;
and the second controller is used for controlling the chlorohydrination reactor to work.
Further, the intelligent control module further comprises:
the first control valve is arranged on the gas-phase feeding pipeline and used for controlling the air inflow of the hypochlorous acid reactor;
and the second control valve is arranged on the ethylene feeding pipeline and used for controlling the air inflow entering the chlorohydrination reactor.
In another aspect, an intelligently controlled process for the production of ethylene oxide from ethylene, comprising:
presetting an intelligent control procedure:
step 1: the method comprises the steps that a preset value is set for the temperature of a hypochlorous acid synthesis unit through a cloud processing module, preset values are set for the temperature and the pressure of a chlorohydrination reaction unit, the temperature in a hypochlorous acid reactor is detected through a temperature sensor, the temperature and the pressure in the chlorohydrination reactor are detected through a temperature sensor and a pressure sensor, when the temperature or the pressure are not matched with the preset values, the corresponding temperature sensor or the pressure sensor sends an electric signal to the cloud processing module, the cloud processing module sends a control command to a first controller and a second controller of the corresponding units to control and adjust the temperature or the pressure, and when the temperature or the pressure reach a preset limit value, the cloud processing module receives the electric signal, transmits the signal to an emergency early warning module and gives an alarm;
a hypochlorous acid synthesis procedure:
and step 3: conveying water into the hypochlorous acid reactor through the liquid-phase feeding pipeline, conveying chlorine into the hypochlorous acid reactor through the gas-phase feeding pipeline, conveying the chlorine gas to the first micro-interface generator through the gas-phase feeding pipeline, crushing the chlorine gas by the first micro-interface generator to form micron-scale micron-sized bubbles, outputting the micron-scale micron-sized bubbles to the hypochlorous acid reactor by the first micro-interface generator after crushing is completed, mixing the micron-scale micron-sized bubbles with the water to form a gas-liquid emulsion, and reacting the gas-liquid emulsion to generate a hypochlorous acid mixture;
and 4, step 4: 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 5: 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:
step 6: the 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, the second micro-interface generator crushes the ethylene to form micron-sized bubbles, after crushing is completed, the second micro-interface generator outputs the micron-sized bubbles to the chlorohydrination reactor 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 chloroethanol solution, and the chloroethanol solution in the chlorohydrination reactor flows out and is conveyed 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.
Compared with the prior art, the system has the advantages that the main structure of the system 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, and the chlorine is crushed to form micron-sized bubbles, so that the micron-sized bubbles are mixed with water to form a gas-liquid emulsion, the gas-liquid two-phase interfacial area is increased, the synthetic efficiency of hypochlorous acid is improved, the chlorine reaction efficiency is improved, and the cost is saved; the system of the invention is provided with a hypochlorous acid synthesis unit for providing reaction places for chlorine and water and separating the generated materials, a chlorohydrination reaction unit connected with the hypochlorous acid synthesis unit for providing a reaction place for the output materials of the hypochlorous acid synthesis unit and ethylene, a saponification reaction unit connected with the chlorohydrination reaction unit for providing a reaction place for the output liquid phase materials of the chlorohydrination reaction unit and lime milk, and a separation and purification unit connected with the saponification reaction unit for rectifying and separating the output liquid phase materials. 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.
Particularly, the hypochlorous acid synthesis unit is internally provided with a hypochlorous acid reactor, a gas phase feeding pipeline, a liquid phase feeding pipeline, a first gas phase return pipe and a gas-liquid separator, the hypochlorous acid reactor is improved to provide reaction places for chlorine and water, the chlorine is conveyed into the first micro-interface generator through the gas phase feeding pipeline, the micro-interface generator is enabled to crush the chlorine, the water is conveyed into the hypochlorous acid reactor through the liquid phase feeding pipe, the gas phase components are conveyed back into the hypochlorous acid reactor through the first gas phase return pipe, and the gas-liquid separator is used for carrying out gas-liquid separation on the output materials of the hypochlorous acid reactor, so that the high-efficiency reaction of the water and the chlorine is realized, and the utilization rate of the chlorine raw materials is.
Particularly, the chlorohydrination reaction unit is provided with a chlorohydrination reactor, an ethylene feeding pipeline and a second gas phase return pipe, a reaction place is provided for hypochlorous acid and ethylene through the chlorohydrination reactor 21, ethylene is conveyed into a second micro-interface generator through the ethylene feeding pipeline, the micro-interface generator is used for crushing the ethylene, and gas phase components are conveyed back into the chlorohydrination reactor through the second gas phase return pipe, so that the high-efficiency reaction of the ethylene and the hypochlorous acid is realized, and the utilization rate of ethylene raw materials is improved.
Particularly, the saponification reaction unit is provided with a saponification reactor and a lime milk feeding pipeline, the saponification reactor provides a reaction place for the liquid-phase material output by the chlorohydrination reaction unit and the lime milk, the lime milk is conveyed into the saponification reactor through the lime milk feeding pipeline, and ethylene oxide is obtained through saponification reaction of chlorohydrin and the lime milk.
In particular, the separation and purification unit 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.
Furthermore, an intelligent control unit is arranged in the whole reaction system, so that a worker can know the real-time situation of each data transmitted back by the intelligent sensing module at any time through the mobile equipment, and can realize accurate control of the temperature and the pressure in the whole reactor through changing a preset value, thereby further improving the reaction efficiency.
Drawings
FIG. 1 is a schematic diagram of the structure of an intelligent control system for ethylene-to-ethylene oxide production according to the present invention;
FIG. 2 is a control flow chart of the intelligent control system for preparing ethylene oxide from ethylene according to the invention.
Detailed Description
Preferred embodiments of the present invention are 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 in a specific orientation, and be operated, 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 meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
Fig. 1 is a schematic structural diagram of an intelligent control system for preparing ethylene oxide from ethylene according to the present invention, which includes a chlorohydrination reaction unit 1, a chlorohydrination reaction unit 2, a saponification reaction unit 3, a separation and purification unit 4, a micro-interface generator 5, and an intelligent control unit. 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 components of the micro-interface generator 5 are crushed to form micron-sized bubbles with micron scale and the mixture of the micron-sized bubbles and the catalyst solution 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-interfaces, micro-nano interfaces, ultra-micro interfaces, micro-bubble biochemical reactors or micro-bubble bioreactors, 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-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-bubbles, micro-micron-sized bubble flow, micro-foams, micro-bubble flow, micro-gas-liquid flow, gas-liquid-micro-nano emulsified 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;
the second micro-interface generator 52 is disposed at the bottom of the reaction zone of the chlorohydrination reaction unit 2, and is configured to crush ethylene to form micron-sized bubbles, and output the micron-sized bubbles into the chlorohydrination reaction unit after crushing is completed to mix with the liquid-phase material output by the hypochlorous acid synthesis unit 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;
it is understood that the materials and dimensions of the gas phase feeding pipe 12, the liquid phase feeding pipe 13 and the first gas phase return pipe 14 are not particularly limited in this embodiment, as long as the gas phase feeding pipe 12, the liquid phase feeding pipe 13 and the first gas phase return pipe 14 can deliver a given volume of material in a given time.
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;
it will be understood that the materials and dimensions of ethylene feed line 22 and second vapor return line 23 are not particularly limited in this embodiment, provided that ethylene feed line 22 and second vapor return line 23 are capable of delivering a given volume of material in a given 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 pipe 32 provided at a side wall of the saponification reactor 31 for conveying lime milk into the saponification reactor;
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 to the saponification reaction unit 3 and is used for exchanging energy between the material output from the saponification reaction unit and ethylene oxide, and 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 its specified working state;
and 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.
Referring to fig. 1 and 2, an intelligent control unit, which is connected to the hypochlorous acid synthesis unit 1 and the chlorohydrination reaction unit 2 for intelligently controlling the system, includes an intelligent sensing module, a cloud processing module, an intelligent control module, an emergency early warning module and a power supply module, wherein the intelligent sensing module, the intelligent control module, the emergency early warning module and the power supply module are connected to the cloud processing module, the intelligent sensing module is used for collecting data and transmitting collected electric signals to the cloud processing module, the cloud processing module is used for performing cloud database analysis, screening and comparison on data parameters returned by the intelligent sensing module, optimizing optimal control parameters and sending corresponding control instructions to the intelligent control module, and when the data parameters reach a preset value of an operation limit, the cloud processing module sends corresponding instructions to the emergency early warning module, the intelligent control module is used for controlling and adjusting the system, the emergency early warning module is used for early warning the operation limit, and the power supply module is used for supplying electric energy to the automatic control unit.
The intelligent sensing module comprises:
the temperature sensors are arranged in the hypochlorous acid reactor and the chlorohydrination reactor and are respectively used for detecting the reaction temperature in the hypochlorous acid reactor and the chlorohydrination reactor;
the pressure sensor is used for detecting pressure and arranged in the chlorohydrination reactor and used for detecting the reaction pressure in the hypochlorous acid reactor and the chlorohydrination reactor;
and the flow sensor is used for detecting flow, is arranged in the gas-phase feeding pipeline and the ethylene feeding pipeline and is respectively used for detecting the chlorine and the ethylene flow.
The intelligent control module comprises:
a first controller for controlling the hypochlorous acid reactor to work;
and the second controller is used for controlling the chlorohydrination reactor to work.
Further, the intelligent control module further comprises:
the first control valve is arranged on the gas-phase feeding pipeline and used for controlling the air inflow of the hypochlorous acid reactor;
and the second control valve is arranged on the ethylene feeding pipeline and used for controlling the air inflow entering the chlorohydrination reactor.
In order that the objects and advantages of the invention will be more clearly understood, the invention is further described below with reference to examples; it should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
An intelligent control process for preparing ethylene oxide from ethylene, comprising:
presetting an intelligent control procedure:
step 1: the method comprises the steps that a preset value is set for the temperature of a hypochlorous acid synthesis unit through a cloud processing module, preset values are set for the temperature and the pressure of a chlorohydrination reaction unit, the temperature in a hypochlorous acid reactor is detected through a temperature sensor, the temperature and the pressure in the chlorohydrination reactor are detected through a temperature sensor and a pressure sensor, when the temperature or the pressure are not matched with the preset values, the corresponding temperature sensor or the pressure sensor sends an electric signal to the cloud processing module, the cloud processing module sends a control command to a first controller and a second controller of the corresponding units to control and adjust the temperature or the pressure, and when the temperature or the pressure reach a preset limit value, the cloud processing module receives the electric signal, transmits the signal to an emergency early warning module and gives an alarm;
a hypochlorous acid synthesis procedure:
and step 3: conveying water into the hypochlorous acid reactor through the liquid-phase feeding pipeline, conveying chlorine into the hypochlorous acid reactor through the gas-phase feeding pipeline, conveying the chlorine gas to the first micro-interface generator through the gas-phase feeding pipeline, crushing the chlorine gas by the first micro-interface generator to form micron-scale micron-sized bubbles, outputting the micron-scale micron-sized bubbles to the hypochlorous acid reactor by the first micro-interface generator after crushing is completed, mixing the micron-scale micron-sized bubbles with the water to form a gas-liquid emulsion, and reacting the gas-liquid emulsion to generate a hypochlorous acid mixture;
and 4, step 4: 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 5: 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:
step 6: the 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, the second micro-interface generator crushes the ethylene to form micron-sized bubbles, after crushing is completed, the second micro-interface generator outputs the micron-sized bubbles to the chlorohydrination reactor 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 chloroethanol solution, and the chloroethanol solution in the chlorohydrination reactor flows out and is conveyed 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 35 ℃ and 0.13 MPa;
the gas-liquid ratio in the second micro-interface generator is 110: 1;
the reaction temperature in the saponification reactor is 93 ℃ and normal pressure.
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 13 ℃ and normal pressure;
the gas-liquid ratio in the first micro-interface generator is 124: 1;
the reaction temperature in the chlorohydrination reactor is 37 ℃ and 0.15 MPa;
the gas-liquid ratio in the second micro-interfacial generator was 116: 1;
the reaction temperature in the saponification reactor is 95 ℃ and normal pressure.
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 15 ℃ and normal pressure;
the gas-liquid ratio in the first micro-interface generator is 127: 1;
the reaction temperature in the chlorohydrination reactor is 39 ℃ and 0.17 MPa;
the gas-liquid ratio in the second micro-interface generator is 121: 1;
the reaction temperature in the saponification reactor is 98 ℃, and the reaction temperature is normal pressure.
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 18 ℃ and normal pressure;
the gas-liquid ratio in the first micro-interface generator is 129: 1;
the reaction temperature in the chlorohydrination reactor is 40 ℃ and 0.18 MPa;
the gas-liquid ratio in the second micro-interfacial generator was 124: 1;
the reaction temperature in the saponification reactor is 99 ℃, and the reaction temperature is normal pressure.
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 131: 1;
the reaction temperature in the chlorohydrination reactor is 42 ℃ and 0.19 MPa;
the gas-liquid ratio in the second micro-interfacial generator was 127: 1;
the reaction temperature in the saponification reactor is 100 ℃, and the reaction is carried out under normal pressure.
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 detection, the ethylene conversion rate and the synthesis efficiency improvement rate are shown in the following table after the system and the process and the prior art are used:
so far, the technical solutions of the present invention have been described in connection with 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. Equivalent changes or substitutions of related technical features can be made by those skilled in the art without departing from the principle of the invention, and the technical scheme after the changes or substitutions can fall into the protection scope of the 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 alterations to this invention will become apparent 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. An intelligent control system for preparing ethylene oxide from ethylene, which is characterized by comprising:
the hypochlorous acid synthesis unit is used for providing reaction sites for chlorine and water and separating generated materials;
the chlorohydrination reaction unit is connected with the hypochlorous acid synthesis unit and is used for providing a reaction site for the output material of the hypochlorous acid synthesis unit and ethylene;
the saponification reaction unit is connected with the chlorohydrination reaction unit and is used for providing a reaction site for outputting a liquid-phase material and lime milk by the chlorohydrination reaction unit;
the separation and purification unit is connected with the saponification reaction unit and is used for rectifying and separating the output liquid-phase material;
the micro-interface generators are arranged in the hypochlorous acid synthesis unit and the chlorohydrination reaction unit respectively, convert the pressure energy of gas and/or the kinetic energy of liquid into the surface energy of bubbles and transmit the surface energy to the gas-phase component, so that the gas-phase gas is crushed into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm, the mass transfer area of the gas-phase component and the liquid-phase component is increased, the thickness of a liquid film is reduced, the mass transfer resistance is reduced, 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 the range of preset operating conditions;
an intelligent control unit which is connected with the hypochlorous acid synthesis unit and the chlorohydrination reaction unit and is used for intelligently controlling the system, wherein the intelligent control unit comprises an intelligent sensing module, a cloud processing module, an intelligent control module, an emergency early warning module and a power supply module, the intelligent sensing module, the intelligent control module, the emergency early warning module and the power supply module are all connected with the cloud processing module, the intelligent sensing module is used for collecting data and transmitting the collected electric signals to the cloud processing module, the cloud processing module is used for carrying out cloud database analysis, screening and comparison on data parameters returned by the intelligent sensing module, optimizing optimal control parameters and sending corresponding control instructions to the intelligent control module, and meanwhile, when the data parameters reach preset values of operation limits, the cloud processing module sends corresponding instructions to the emergency early warning module, and the intelligent control module is used for controlling and adjusting the system, the emergency early warning module is used for early warning the operation limit, and the power supply module is used for supplying electric energy to the automatic control unit.
2. The intelligent control system for ethylene to ethylene oxide according to claim 1, wherein the micro-interface generator is a pneumatic micro-interface generator, and the micro-interface generator 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.
3. The intelligent control system for ethylene to ethylene oxide of claim 1, 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;
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.
4. The intelligent control system for ethylene to ethylene oxide according to claim 1, 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;
the ethylene feeding pipeline is arranged on the side wall of the chlorohydrination reactor, 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;
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.
5. The intelligent control system for ethylene to ethylene oxide according to claim 1, wherein the saponification reaction unit comprises:
the saponification reactor is connected with the chlorohydrination reactor 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 disposed in a side wall of the saponification reactor for conveying lime milk into the saponification reactor.
6. The intelligent control system for ethylene to ethylene oxide as claimed in claim 1, wherein the separation and purification unit comprises:
the heat exchanger is connected with the saponification reaction unit and is used for exchanging energy between the material output by the saponification reaction unit and ethylene oxide;
and the rectifying tower is connected with the heat exchanger and is used for rectifying and separating the materials output by the saponification reaction unit.
7. The intelligent control system for ethylene to ethylene oxide as claimed in claim 1, wherein the intelligent sensing module comprises:
the temperature sensors are arranged in the hypochlorous acid reactor and the chlorohydrination reactor and are respectively used for detecting the reaction temperature in the hypochlorous acid reactor and the chlorohydrination reactor;
the pressure sensor is used for detecting pressure and arranged in the chlorohydrination reactor and used for detecting the reaction pressure in the hypochlorous acid reactor and the chlorohydrination reactor;
and the flow sensor is used for detecting flow, is arranged in the gas-phase feeding pipeline and the ethylene feeding pipeline and is respectively used for detecting the chlorine and the ethylene flow.
8. The intelligent control system for ethylene to ethylene oxide as claimed in claim 1, wherein the intelligent control module comprises:
a first controller for controlling the hypochlorous acid reactor to work;
and the second controller is used for controlling the chlorohydrination reactor to work.
9. The intelligent control system for ethylene to ethylene oxide as claimed in claim 1, wherein the intelligent control module further comprises:
the first control valve is arranged on the gas-phase feeding pipeline and used for controlling the air inflow of the hypochlorous acid reactor;
and the second control valve is arranged on the ethylene feeding pipeline and used for controlling the air inflow entering the chlorohydrination reactor.
10. An intelligent control process for preparing ethylene oxide from ethylene, which is characterized by comprising the following steps:
presetting an intelligent control procedure:
step 1: the method comprises the steps that a preset value is set for the temperature of a hypochlorous acid synthesis unit through a cloud processing module, preset values are set for the temperature and the pressure of a chlorohydrination reaction unit, the temperature in a hypochlorous acid reactor is detected through a temperature sensor, the temperature and the pressure in the chlorohydrination reactor are detected through a temperature sensor and a pressure sensor, when the temperature or the pressure are not matched with the preset values, the corresponding temperature sensor or the pressure sensor sends an electric signal to the cloud processing module, the cloud processing module sends a control command to a first controller and a second controller of the corresponding units to control and adjust the temperature or the pressure, and when the temperature or the pressure reach a preset limit value, the cloud processing module receives the electric signal, transmits the signal to an emergency early warning module and gives an alarm;
step 2, setting preset values for the flow rates of chlorine entering a hypochlorous acid synthesis unit and ethylene entering a chlorohydrination reaction unit through a cloud processing module, detecting the flow rates of the chlorine and the ethylene through flow sensors, sending an electric signal to the cloud processing module by the corresponding flow sensor when a detection value is not matched with the preset value, sending a control command to a first control valve or a second control valve by the cloud processing module to adjust the corresponding flow, and when the flow reaches a preset limit value, receiving the electric signal by the cloud processing module, transmitting the signal to an emergency early warning module and giving an alarm;
a hypochlorous acid synthesis procedure:
and step 3: conveying water into the hypochlorous acid reactor through the liquid-phase feeding pipeline, conveying chlorine into the hypochlorous acid reactor through the gas-phase feeding pipeline, conveying the chlorine gas to the first micro-interface generator through the gas-phase feeding pipeline, crushing the chlorine gas by the first micro-interface generator to form micron-scale micron-sized bubbles, outputting the micron-scale micron-sized bubbles to the hypochlorous acid reactor by the first micro-interface generator after crushing is completed, mixing the micron-scale micron-sized bubbles with the water to form a gas-liquid emulsion, and reacting the gas-liquid emulsion to generate a hypochlorous acid mixture;
and 4, step 4: 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 5: 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:
step 6: the 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, the second micro-interface generator crushes the ethylene to form micron-sized bubbles, after crushing is completed, the second micro-interface generator outputs the micron-sized bubbles to the chlorohydrination reactor 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 chloroethanol solution, and the chloroethanol solution in the chlorohydrination reactor flows out and is conveyed 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.
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| CN201910867735.7A CN112500372A (en) | 2019-09-14 | 2019-09-14 | Intelligent control system and process for preparing ethylene oxide from ethylene |
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| CN201910867735.7A CN112500372A (en) | 2019-09-14 | 2019-09-14 | Intelligent control system and process for preparing ethylene oxide from ethylene |
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