CN211123731U - Intelligent control reaction system for preparing ethylene glycol based on ethylene hydration method - Google Patents
Intelligent control reaction system for preparing ethylene glycol based on ethylene hydration method Download PDFInfo
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- CN211123731U CN211123731U CN201921518004.3U CN201921518004U CN211123731U CN 211123731 U CN211123731 U CN 211123731U CN 201921518004 U CN201921518004 U CN 201921518004U CN 211123731 U CN211123731 U CN 211123731U
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- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 title claims abstract description 547
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 61
- 239000005977 Ethylene Substances 0.000 title claims abstract description 61
- 238000000034 method Methods 0.000 title claims abstract description 58
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 55
- 230000036571 hydration Effects 0.000 title claims abstract description 23
- 238000006703 hydration reaction Methods 0.000 title claims abstract description 23
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 claims abstract description 87
- 239000007788 liquid Substances 0.000 claims abstract description 72
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 40
- 239000008367 deionised water Substances 0.000 claims abstract description 35
- 229910021641 deionized water Inorganic materials 0.000 claims abstract description 35
- 239000000203 mixture Substances 0.000 claims abstract description 15
- 238000012546 transfer Methods 0.000 claims abstract description 11
- 239000007789 gas Substances 0.000 claims description 98
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 41
- 239000001301 oxygen Substances 0.000 claims description 41
- 229910052760 oxygen Inorganic materials 0.000 claims description 41
- 239000012535 impurity Substances 0.000 claims description 25
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- 238000006297 dehydration reaction Methods 0.000 claims description 13
- 238000007599 discharging Methods 0.000 claims description 13
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 11
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims description 9
- 239000003054 catalyst Substances 0.000 claims description 9
- 229910052709 silver Inorganic materials 0.000 claims description 9
- 239000004332 silver Substances 0.000 claims description 9
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- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 3
- -1 amine compounds Chemical class 0.000 description 3
- 229920000728 polyester Polymers 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- IKHGUXGNUITLKF-UHFFFAOYSA-N Acetaldehyde Chemical compound CC=O IKHGUXGNUITLKF-UHFFFAOYSA-N 0.000 description 2
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- WOZVHXUHUFLZGK-UHFFFAOYSA-N dimethyl terephthalate Chemical compound COC(=O)C1=CC=C(C(=O)OC)C=C1 WOZVHXUHUFLZGK-UHFFFAOYSA-N 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
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- KMTRUDSVKNLOMY-UHFFFAOYSA-N Ethylene carbonate Chemical compound O=C1OCCO1 KMTRUDSVKNLOMY-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
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- MLUCVPSAIODCQM-NSCUHMNNSA-N crotonaldehyde Chemical compound C\C=C\C=O MLUCVPSAIODCQM-NSCUHMNNSA-N 0.000 description 1
- MLUCVPSAIODCQM-UHFFFAOYSA-N crotonaldehyde Natural products CC=CC=O MLUCVPSAIODCQM-UHFFFAOYSA-N 0.000 description 1
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- 229910017604 nitric acid Inorganic materials 0.000 description 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
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Images
Abstract
The utility model relates to an intelligent control reaction system based on ethylene hydration method preparation ethylene glycol, include: the reactor, intelligent control module and micro-interface generator. The intelligent control module controls the work of the whole system, so that the whole system has good operation stability and continuity, the size of the whole system is reduced, and the simplification degree is higher. The gas containing ethylene oxide is crushed by the micro-interface generator to form micron-sized bubbles with micron scale, and the micron-sized bubbles are mixed with deionized water to form a gas-liquid mixture, so that the phase interface area of gas and liquid phases is increased, and the effect of strengthening mass transfer within a lower preset operation condition range is achieved; meanwhile, the micron-sized bubbles can be fully mixed with the deionized water to form a gas-liquid mixture, and the gas-liquid mixture can ensure that the deionized water in the system can be fully contacted with the gas containing ethylene oxide by fully mixing the gas phase and the liquid phase, so that the reaction efficiency of the system is effectively improved, and the conversion rate of the ethylene glycol is improved.
Description
Technical Field
The utility model relates to an ethylene glycol preparation technical field especially relates to an intelligent control reaction system based on ethylene hydration method preparation ethylene glycol.
Background
Ethylene glycol is an important chemical raw material, is found to react with terephthalic acid to generate dimethyl terephthalate, and can be used as a raw material of polyester fiber and polyester plastic, so that the consumption of the ethylene glycol is greatly increased.
At present, glycol is mainly used for manufacturing polyester fiber, and the dosage of the glycol accounts for more than 40 percent of the total dosage of the glycol; secondly, the main raw material of the antifreezing agent accounts for 35 percent of the total amount; in other aspects, such as a chemical reagent, ethylene glycol is mainly used in a stationary liquid for gas chromatography for analyzing low-boiling oxygen-containing compounds, amine compounds, oxygen and nitrogen heterocyclic compounds, and the like, and in addition to the above-mentioned uses, ethylene glycol is widely used in fuel, paint, adhesives, solvents, lubricants, softeners, thickeners, explosives, and the like, and the production technology of ethylene glycol is continuously improved.
According to the literature, the process of synthesizing ethylene glycol can be roughly classified into the ethylene direct hydration method, the ethylene hydration method, the formaldehyde synthesis method, the ethylene carbonate method, the synthesis gas method, the oxidative coupling method, etc., wherein the ethylene hydration method is also called the ethylene oxide hydration method, which is the main method currently used for producing ethylene glycol, and the principle thereof comprises
First, ethylene is converted to ethylene oxide by vapor phase catalytic oxidation using oxygen in the presence of a silver catalyst. The gas containing the ethylene oxide is contacted with a large amount of water, and the gas containing the ethylene oxide is contacted with a large amount of water to generate ethylene glycol dilute solution;
secondly, the ethylene glycol dilute solution passes through a heat exchanger, is cooled after passing through the heat exchanger, enters an expander, blows out volatile components such as acetaldehyde and crotonaldehyde in the expander, and then flows into a storage tank;
and finally, injecting the ethylene glycol dilute solution in the storage tank into an evaporator through a pump body for concentration, and finally feeding the ethylene glycol dilute solution subjected to multiple times of evaporation into a dehydration tower to remove moisture to prepare pure ethylene glycol.
In the above-mentioned prior processes for producing ethylene glycol, the conversion of ethylene glycol is usually achieved by pressurizing and raising the temperature during the contact of the ethylene oxide-containing gas with water.
Based on the technical principle of preparing ethylene glycol by the ethylene hydration method, the prior ethylene hydration method ethylene glycol preparation system and the prior ethylene hydration method ethylene glycol preparation process have the following problems:
firstly, the stability and continuity of the system operation are poor, and the whole reactor is large in volume, so that the occupied space is large;
secondly, in the contact process of the gas containing the ethylene oxide and the water, the gas and the liquid are mixed to generate more large bubbles, and the gas and the liquid cannot be fully mixed due to the more and the larger bubbles, so that the conversion rate of the ethylene glycol is reduced, and the reaction rate of the whole gas-liquid system is reduced.
SUMMERY OF THE UTILITY MODEL
Therefore, the utility model provides an intelligent control reaction system based on ethylene hydration method preparation ethylene glycol for overcome the stability of system operation, continuity subalternation problem.
The utility model provides an intelligent control reaction system based on ethylene hydration method preparation ethylene glycol, include:
the reactor is used for providing a reaction site for the gas containing the ethylene oxide and the deionized water to prepare ethylene glycol dilute solution;
an ethylene oxide generator disposed at one side of the reactor to provide a reaction site for ethylene gas and oxygen to produce ethylene oxide, a heat exchanger disposed between the ethylene oxide generator and the reactor to reduce the temperature of the ethylene oxide-containing gas;
the micro-interface generator is arranged in the reactor, converts the pressure energy of gas and/or the kinetic energy of liquid into the surface energy of bubbles and transmits the surface energy to the gas containing ethylene oxide, so that the gas containing ethylene oxide 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 between deionized water and the gas containing ethylene oxide is increased, the thickness of a liquid film is reduced, the mass transfer resistance is reduced, and the deionized water and the micron-sized bubbles containing ethylene oxide are mixed to form a gas-liquid mixture after crushing, so that the mass transfer efficiency and the reaction efficiency between the deionized water and the gas containing ethylene oxide are enhanced within a preset operating condition range;
the impurity removal unit is arranged on one side of the reactor and is used for removing volatile components in the ethylene glycol dilute solution;
the concentration unit is arranged on one side of the impurity removal unit and is used for concentrating the ethylene glycol dilute solution;
the intelligent control module comprises a P L C controller, a sensor and a cloud processor, wherein the sensor transmits acquired electric signals to the cloud processor, the cloud processor performs screening comparison in a cloud database according to reaction parameters returned by the sensor, and sends corresponding commands to the P L C controller after an optimal control method is screened out.
Further, the micro-interface generator is a pneumatic micro-interface generator, and the micro-interface generator is arranged in the reactor and used for crushing the gas containing ethylene oxide to form micron-sized bubbles and outputting the micron-sized bubbles into the reactor after the crushing is finished to be mixed with the deionized water in the reactor to form a gas-liquid mixture.
Further, the P L C controller includes:
a first P L C controller for controlling the operation of the reactor;
a second P L C controller for controlling the operation of the ethylene oxide generator;
the third P L C controller is used for controlling the micro-interface generator to work;
the fourth P L C controller is used for controlling the operation of the impurity removing unit;
a fifth P L C controller for controlling operation of the concentration unit.
Furthermore, the upper part of the side wall of the reactor is communicated with a first liquid inlet pipe, a first pump body and a first flow meter are arranged on the first liquid inlet pipe, and the first liquid inlet pipe is used for conveying deionized water into the reactor.
Further, the intercommunication is provided with ethylene intake pipe and oxygen intake pipe on ethylene oxide generator's the lateral wall, be provided with the second pump body and second flow meter in the ethylene intake pipe, be provided with the third pump body and third flow meter in the oxygen intake pipe, the ethylene intake pipe with the oxygen intake pipe be used for respectively to gaseous and oxygen of transmission ethylene in the ethylene oxide generator, the inside of ethylene oxide generator is provided with the silver catalyst, the silver catalyst is used for catalyzing gaseous and oxygen of ethylene, the ethylene oxide generator with little interface generator is linked together, and the ethylene oxide generator with be provided with the eighth pump body between the little interface generator.
Further, the impurity removing unit comprises:
the first cooler is communicated with the reactor, a fourth pump body is arranged between the first cooler and the reactor, and the first cooler is used for cooling the ethylene glycol dilute solution;
the expander is communicated with the first cooler and used for removing volatile components in the cooled ethylene glycol dilute solution, a gas outlet is formed in the upper end of the expander and used for discharging the volatile components, the lower end of the expander is communicated with the reactor and used for transmitting part of the ethylene glycol dilute solution in the expander back to the reactor for repeated reaction, and a fifth pump body is arranged between the expander and the reactor.
And the ethylene glycol dilute solution storage tank is communicated with the expander, a fourth flow meter is arranged between the ethylene glycol storage tank and the expander, and the ethylene glycol dilute solution storage tank is used for receiving the ethylene glycol dilute solution in the expander after the volatile components are removed.
Further, the concentration unit comprises:
the evaporator is communicated with the impurity removal unit, a sixth pump body and a sixth flowmeter are arranged between the evaporator and the impurity removal unit, the evaporator is used for evaporating and concentrating the ethylene glycol dilute solution, a second liquid inlet pipe is communicated with the middle of the side wall of the evaporator and used for receiving the ethylene glycol dilute solution transmitted by the impurity removal unit and transmitting the ethylene glycol dilute solution into the evaporator, a gas discharge pipe is communicated with the upper end of the evaporator and used for discharging evaporated gas, a liquid discharge pipe is communicated with the lower end of the evaporator and used for discharging the concentrated ethylene glycol dilute solution;
the second cooler is communicated with the evaporator, a seventh pump body is arranged between the second cooler and the evaporator, and the second cooler is used for cooling the evaporated gas discharged from the evaporator into liquid and transmitting the liquid back to the evaporator for re-evaporation;
and the dehydrating tower is communicated with the evaporator, the lower end of the dehydrating tower is provided with an electric control valve and a seventh flow meter, and the dehydrating tower is used for dehydrating the concentrated glycol solution.
Further, the sensor includes:
a temperature sensor disposed within the reactor to monitor a reaction temperature within the reactor;
a pressure sensor disposed within the reactor to monitor a reaction pressure within the reactor.
Further, the evaporator is a central circulating pipe type circulating evaporator.
Further, the dehydration tower is a plate tower.
Compared with the prior art, the utility model has the advantages that the utility model discloses a work of whole system is controlled to intelligent control module, wherein through P L C controller control reactor, ethylene oxide generator, little interface generator, edulcoration unit and concentration unit cooperation work, make raw materials supply volume and reactant yield all obtain the record, can find out corresponding optimum technical parameter according to the record, in order to reuse, the addition of intelligent control module makes whole system operational stability, the continuity is good, reduce whole system volume, make its degree of retrenching higher;
the utility model discloses a broken gaseous micron order bubble that contains ethylene oxide makes it form micron yardstick, micron order bubble possesses the physicochemical property that conventional bubble did not possess, can know by the computational formula of spheroid volume and surface area, under the unchangeable condition of total volume, the total surface area and the single bubble diameter of bubble are inversely proportional, can know micron order bubble's total surface area is huge from this, make micron order bubble and deionized water mix and form gas-liquid mixture, with the double-phase area of contact of increase gas-liquid, and reach the effect of strengthening the mass transfer at lower preset operating condition within range, effectively improve the conversion rate and the efficiency of preparation ethylene glycol.
Furthermore, the micro-interface generator is a pneumatic micro-interface generator, is arranged in the reactor and is used for crushing the gas containing ethylene oxide to form micron-sized bubbles, outputting the micron-sized bubbles into the reactor after the crushing is finished and mixing the micron-sized bubbles with the deionized water in the reactor to form a gas-liquid mixture, and effectively improves the conversion rate and efficiency of preparing the ethylene glycol.
The reactor is controlled to work through the first P L C controller, the first pump body is controlled to work, deionized water is added into the reactor, the first flowmeter measures the inflow of the deionized water, the eighth pump body is controlled to work through controlling the second P L C controller, cooled gas containing ethylene oxide generated in the ethylene oxide generator is transmitted into the micro interface generator, the micro interface generator is controlled to work through the third P L C controller, the micro interface generator crushes the gas containing ethylene oxide into micron-scale bubbles, the micron-scale bubbles are output into the reactor and mixed with the deionized water in the reactor to form a gas-liquid mixture after the crushing is completed, the ethylene oxide in the gas reacts with the deionized water to generate ethylene glycol, the temperature of the ethylene glycol and the temperature of the dilute solution in the reactor are monitored in real time, and the cloud pressure sensor is monitored in real time.
The ethylene oxide generator is characterized in that an ethylene inlet pipe and an oxygen inlet pipe are communicated with the side wall of the ethylene oxide generator, a second pump body and a second flow meter are arranged on the ethylene inlet pipe, a third pump body and a third flow meter are arranged on the oxygen inlet pipe, the ethylene inlet pipe and the oxygen inlet pipe are respectively used for transmitting ethylene gas and oxygen into the ethylene oxide generator, a silver catalyst is arranged inside the ethylene oxide generator and used for catalyzing the ethylene gas and the oxygen, the ethylene oxide generator is communicated with the micro-interface generator, an eighth pump body is arranged between the ethylene oxide generator and the micro-interface generator, the second P L C controller is used for controlling the ethylene oxide generator to work, the specific control process comprises controlling the second pump body and the third pump body to work, transmitting the ethylene gas and the oxygen into the ethylene oxide generator, meanwhile, the second flow meter and the third flow meter are used for respectively measuring the air inflow of the ethylene gas and the oxygen, and the ethylene gas and the oxygen are catalyzed by the silver to generate the ethylene oxide gas catalyst.
Further, the impurity removing unit comprises:
the first cooler is communicated with the reactor, a fourth pump body is arranged between the first cooler and the reactor, and the first cooler is used for cooling the ethylene glycol dilute solution;
the expander is communicated with the first cooler and used for removing volatile components in the cooled ethylene glycol dilute solution, a gas outlet is formed in the upper end of the expander and used for discharging the volatile components, the lower end of the expander is communicated with the reactor and used for transmitting part of the ethylene glycol dilute solution in the expander back to the reactor for repeated reaction, and a fifth pump body is arranged between the expander and the reactor.
And the ethylene glycol dilute solution storage tank is communicated with the expander, a fourth flow meter is arranged between the ethylene glycol storage tank and the expander, and the ethylene glycol dilute solution storage tank is used for receiving the ethylene glycol dilute solution in the expander after the volatile components are removed.
Through fourth P L C controller control edulcoration unit work, specific control process includes control fourth pump body work, will the dilute solution of ethylene glycol in the reactor transmit to cool back in the first cooler will the dilute solution of ethylene glycol in the first cooler transmits to in the expander, the dilute solution of ethylene glycol is in further decompressed and cooling in the expander for volatile component in the dilute solution of ethylene glycol passes through the gas outlet discharges, and the dilute solution of ethylene glycol through the edulcoration partly enters into in the dilute solution of ethylene glycol holding vessel, and simultaneously the operation of fourth flow meter enters into the dilute solution of ethylene glycol volume in the dilute solution of ethylene glycol holding vessel measures, controls fifth pump body work, transmits another part of the dilute solution of ethylene glycol back to carry out the repetitive reaction in the reactor, and the recycle carries out the repeated edulcoration with the dilute solution of ethylene glycol here, effectively promotes the edulcoration effect.
Further, the concentration unit comprises:
the evaporator is communicated with the impurity removal unit, a sixth pump body and a sixth flowmeter are arranged between the evaporator and the impurity removal unit, the evaporator is used for evaporating and concentrating the ethylene glycol dilute solution, a second liquid inlet pipe is communicated with the middle of the side wall of the evaporator and used for receiving the ethylene glycol dilute solution transmitted by the impurity removal unit and transmitting the ethylene glycol dilute solution into the evaporator, a gas discharge pipe is communicated with the upper end of the evaporator and used for discharging evaporated gas, a liquid discharge pipe is communicated with the lower end of the evaporator and used for discharging the concentrated ethylene glycol dilute solution;
the second cooler is communicated with the evaporator, a seventh pump body is arranged between the second cooler and the evaporator, and the second cooler is used for cooling the evaporated gas discharged from the evaporator into liquid and transmitting the liquid back to the evaporator for re-evaporation;
and the dehydrating tower is communicated with the evaporator, the lower end of the dehydrating tower is provided with an electric control valve and a seventh flow meter, and the dehydrating tower is used for dehydrating the concentrated glycol solution.
The fifth P L C controller controls the operation of the concentration unit, and the specific control process includes controlling the operation of the sixth pump body, and the dilute ethylene glycol solution entering the dilute ethylene glycol solution storage tank in step 3 is transmitted to the concentration unit, in the concentration unit, the dilute ethylene glycol solution firstly enters the evaporator through the second liquid inlet pipe, and at the same time, the sixth flow meter meters the dilute ethylene glycol solution entering the evaporator, and the evaporated gas is discharged through the gas discharge pipe by the evaporation action of the evaporator, and the seventh pump body is controlled to operate, and the discharged gas is transmitted to the second cooler along the second liquid inlet pipe, and the evaporated gas is cooled into liquid by the cooling action of the second cooler, and the cooled liquid is transmitted back to the evaporator by the seventh pump body for re-evaporation, and the dilute ethylene glycol solution is concentrated after being evaporated by the evaporator, and the moisture in the dilute ethylene glycol solution is evaporated for multiple times by the evaporator, so that the moisture in the ethylene glycol solution is effectively removed, that the dilute ethylene glycol is sufficiently concentrated.
And the concentrated ethylene glycol dilute solution enters the dehydrating tower, is dehydrated to obtain ethylene glycol with high purity, controls the electric control valve to be opened, discharges the high-purity ethylene glycol through the dehydrating tower, and simultaneously measures the discharge amount of the high-purity ethylene glycol by the seventh flowmeter.
Further, the evaporator is a central circulating pipe type circulating evaporator.
The dehydration tower is a plate tower, the plate tower is a device for separating vapor-liquid or liquid-liquid systems, and the device comprises a cylindrical tower body and horizontal tower plates at certain intervals, the ethylene glycol solution enters the dehydration tower and sequentially flows through each pedal from top to bottom in the motion process of the ethylene glycol solution in the dehydration tower, and is discharged from the bottom of the dehydration tower, and simultaneously, under the action of high temperature, the moisture in the ethylene glycol solution is evaporated from bottom to top and is discharged from the top of the dehydration tower, so that the aim of preparing high-purity ethylene glycol is fulfilled.
Drawings
Fig. 1 is a schematic structural diagram of an intelligent control reaction system for preparing ethylene glycol based on an ethylene hydration method.
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 an intelligent control reaction system for preparing ethylene glycol based on an ethylene hydration method according to the present invention, comprising:
a reactor 1 for providing a reaction site for ethylene oxide-containing gas and deionized water to prepare a dilute ethylene glycol solution;
an ethylene oxide generator 2 disposed at one side of the reactor to provide a reaction site for ethylene gas and oxygen to produce ethylene oxide, and a heat exchanger 6 disposed between the ethylene oxide generator and the reactor to reduce the temperature of the ethylene oxide-containing gas;
the micro-interface generator 3 is arranged in the reactor, converts the pressure energy of gas and/or the kinetic energy of liquid into the surface energy of bubbles and transmits the surface energy to the gas containing ethylene oxide, so that the gas containing ethylene oxide 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 between deionized water and the gas containing ethylene oxide is increased, the thickness of a liquid film is reduced, the mass transfer resistance is reduced, and the deionized water and the micron-sized bubbles containing ethylene oxide are mixed to form a gas-liquid mixture after crushing, so that the mass transfer efficiency and the reaction efficiency between the deionized water and the gas containing ethylene oxide are enhanced within the range of preset operating conditions;
the impurity removal unit 4 is arranged on one side of the reactor and is used for removing volatile components in the ethylene glycol dilute solution;
and the concentration unit 5 is arranged on one side of the impurity removal unit and is used for concentrating the ethylene glycol dilute solution.
The intelligent control module comprises a P L C controller, a sensor and a cloud processor, wherein the sensor transmits acquired electric signals to the cloud processor, the cloud processor performs screening comparison in a cloud database according to reaction parameters returned by the sensor, and sends corresponding commands to the P L C controller after an optimal control method is screened out.
Referring to fig. 1, the micro-interface generator is a pneumatic micro-interface generator, and the micro-interface generator is disposed in the reactor and is configured to crush the gas containing ethylene oxide to form micron-sized bubbles, and output the micron-sized bubbles into the reactor after the crushing is completed to mix with the deionized water in the reactor to form a gas-liquid mixture, so as to effectively improve the conversion rate and efficiency of ethylene glycol preparation.
Referring to fig. 1, a first liquid inlet pipe is arranged on the upper portion of the side wall of the reactor in a communicating manner, a first pump body 701 and a first flow meter are arranged on the first liquid inlet pipe, the first liquid inlet pipe is used for conveying deionized water into the reactor, the first P L C controller is used for controlling the reactor to work, the specific control process includes controlling the first pump body to work, adding deionized water into the reactor, simultaneously, the first flow meter is used for metering the deionized water inlet amount, the second P L C controller is used for controlling the eighth pump body 708 to work, conveying the cooled gas containing ethylene oxide generated in the ethylene oxide generator into the micro interface generator, controlling the micro interface generator to work through the third P L C controller, the micro interface generator is used for crushing the gas containing ethylene oxide to form micron-sized bubbles, mixing the micron-sized bubbles with the deionized water in the reactor to form a gas-liquid mixture after the crushing is completed, generating ethylene oxide and reacting, generating ethylene glycol, and feeding back the temperature sensor and the dilute pressure sensor of the deionized water to the reactor, and monitoring the cloud temperature and the temperature of the reaction solution in real-time.
Referring to fig. 1, an ethylene inlet pipe and an oxygen inlet pipe are communicated with a side wall of the ethylene oxide generator, a second pump body 702 and a second flow meter are arranged on the ethylene inlet pipe, a third pump 703 and a third flow meter are arranged on the oxygen inlet pipe, the ethylene inlet pipe and the oxygen inlet pipe are respectively used for transmitting ethylene gas and oxygen into the ethylene oxide generator, a silver catalyst is arranged inside the ethylene oxide generator and used for catalyzing ethylene gas and oxygen, the ethylene oxide generator is communicated with the micro-interface generator, an eighth pump body 708 is arranged between the ethylene oxide generator and the micro-interface generator, the second P L C controller is used for controlling the ethylene oxide generator to work, the specific control process includes controlling the second pump body and the third pump body to work, transmitting ethylene gas and oxygen into the ethylene oxide generator, and the second flow meter and the third flow meter are respectively used for measuring the air inflow of ethylene gas and oxygen, and the ethylene gas and oxygen are catalyzed by the silver catalyst to generate ethylene oxide gas.
With continued reference to FIG. 1, the abatement unit includes:
a first cooler 401, which is communicated with the reactor, and a fourth pump 704 is arranged between the first cooler and the reactor, wherein the first cooler is used for cooling the ethylene glycol dilute solution;
the expander 402 is communicated with the first cooler, the expander is used for removing volatile components in the cooled ethylene glycol dilute solution, a gas outlet is formed in the upper end of the expander and used for discharging the volatile components, the lower end of the expander is communicated with the reactor and used for transmitting part of the ethylene glycol dilute solution inside the expander back to the reactor for repeated reaction, and a fifth pump body 705 is arranged between the expander and the reactor.
And a glycol dilute solution storage tank 403 which is communicated with the expander, wherein a fourth flow meter is arranged between the glycol storage tank and the expander, and the glycol dilute solution storage tank is used for receiving the glycol dilute solution in the expander after the volatile components are removed.
Through fourth P L C controller control edulcoration unit work, specific control process includes control fourth pump body work, will the dilute solution of ethylene glycol in the reactor transmit to cool back in the first cooler will the dilute solution of ethylene glycol in the first cooler transmits to in the expander, the dilute solution of ethylene glycol is in further decompressed and cooling in the expander for volatile component in the dilute solution of ethylene glycol passes through the gas outlet discharges, and the dilute solution of ethylene glycol through the edulcoration partly enters into in the dilute solution of ethylene glycol holding vessel, and simultaneously the operation of fourth flow meter enters into the dilute solution of ethylene glycol volume in the dilute solution of ethylene glycol holding vessel measures, controls fifth pump body work, transmits another part of the dilute solution of ethylene glycol back to carry out the repetitive reaction in the reactor, and the recycle carries out the repeated edulcoration with the dilute solution of ethylene glycol here, effectively promotes the edulcoration effect.
With continued reference to fig. 1, the concentrator includes:
the evaporator 501 is communicated with the impurity removal unit, a sixth pump body 706 and a sixth flowmeter are arranged between the evaporator and the impurity removal unit, the evaporator is used for evaporating and concentrating the ethylene glycol dilute solution, a second liquid inlet pipe is communicated with the middle of the side wall of the evaporator and used for receiving the ethylene glycol dilute solution transmitted by the impurity removal unit and transmitting the ethylene glycol dilute solution into the evaporator, a gas discharge pipe is communicated with the upper end of the evaporator and used for discharging the evaporated gas, a liquid discharge pipe is communicated with the lower end of the evaporator and used for discharging the concentrated ethylene glycol dilute solution;
a second cooler 502, which is communicated with the evaporator, wherein a seventh pump body 707 is arranged between the second cooler and the evaporator, and the second cooler is used for cooling the evaporated gas discharged from the evaporator into liquid and transmitting the liquid back to the evaporator for re-evaporation;
and the dehydrating tower 503 is communicated with the evaporator, the lower end of the dehydrating tower is provided with an electric control valve 8 and a seventh flow meter, and the dehydrating tower is used for dehydrating the concentrated glycol solution.
The fifth P L C controller controls the operation of the concentration unit, and the specific control process includes controlling the operation of the sixth pump body, and the dilute ethylene glycol solution entering the dilute ethylene glycol solution storage tank in step 3 is transmitted to the concentration unit, in the concentration unit, the dilute ethylene glycol solution firstly enters the evaporator through the second liquid inlet pipe, and at the same time, the sixth flow meter meters the dilute ethylene glycol solution entering the evaporator, and the evaporated gas is discharged through the gas discharge pipe by the evaporation action of the evaporator, and the seventh pump body is controlled to operate, and the discharged gas is transmitted to the second cooler along the second liquid inlet pipe, and the evaporated gas is cooled into liquid by the cooling action of the second cooler, and the cooled liquid is transmitted back to the evaporator by the seventh pump body for re-evaporation, and the dilute ethylene glycol solution is concentrated after being evaporated by the evaporator, and the moisture in the dilute ethylene glycol solution is evaporated for multiple times by the evaporator, so that the moisture in the ethylene glycol solution is effectively removed, that the dilute ethylene glycol is sufficiently concentrated.
And the concentrated ethylene glycol dilute solution enters the dehydrating tower, is dehydrated to obtain ethylene glycol with high purity, controls the electric control valve to be opened, discharges the high-purity ethylene glycol through the dehydrating tower, and simultaneously measures the discharge amount of the high-purity ethylene glycol by the seventh flowmeter.
With reference to fig. 1, the dehydration tower is a plate tower, which is a kind of equipment for vapor-liquid or liquid-liquid system separation, and is composed of a cylindrical tower body and horizontal tower plates at certain intervals, the ethylene glycol solution moves in the dehydration tower, and flows through the pedals from top to bottom in sequence in the dehydration tower, and is discharged from the bottom of the dehydration tower, and simultaneously, under the action of high temperature, the water in the ethylene glycol solution is evaporated from bottom to top and is discharged from the top of the dehydration tower, thereby achieving the purpose of preparing high-purity ethylene glycol.
With continuing reference to fig. 1, the present invention provides an intelligent control reaction process for preparing ethylene glycol based on ethylene hydration method, comprising:
step 1, controlling the ethylene oxide generator to work through the second P L C controller, wherein the specific control process comprises controlling the second pump body and the third pump body to work, transmitting ethylene gas and oxygen into the ethylene oxide generator, simultaneously measuring the air inflow of the ethylene gas and the oxygen through the second flow meter and the third flow meter respectively, and catalyzing the ethylene gas and the oxygen through the silver catalyst to generate ethylene oxide gas;
step 4, controlling the concentration unit to work through the fifth P L C controller, wherein the specific control process comprises controlling the sixth pump body to work, transmitting the ethylene glycol dilute solution entering the ethylene glycol dilute solution storage tank in the step 3 to the concentration unit, in the concentration unit, firstly, the ethylene glycol dilute solution enters the evaporator through the second liquid inlet pipe, simultaneously, the sixth flow meter measures the ethylene glycol dilute solution entering the evaporator, the evaporated gas is discharged through the gas discharge pipe through the evaporation effect of the evaporator, controlling the seventh pump body to work, transmitting the discharged gas to the second cooler along the second liquid inlet pipe, cooling the evaporated gas into liquid through the cooling effect of the second cooler, transmitting the cooled liquid back to the evaporator through the seventh pump body, re-evaporating, and concentrating the ethylene glycol dilute solution after being evaporated through the evaporator;
and 5: and 4, enabling the concentrated ethylene glycol dilute solution in the step 4 to enter the dehydrating tower, dehydrating the ethylene glycol dilute solution to obtain ethylene glycol with higher purity, controlling the electric control valve to be opened, discharging the high-purity ethylene glycol through the dehydrating tower, and metering the discharge amount of the high-purity ethylene glycol by the seventh flow meter.
Example 1
The ethylene glycol preparation is carried out by using the system and the process, wherein:
the temperature of the reactor is 60 ℃, and the pressure in the reactor is 1 atm;
the feed temperature of ethylene gas and oxygen was 168 ℃;
the gas-liquid ratio in the micro-interface generator is 700: 1.
after the system and the process are used, the conversion rate of the ethylene glycol is 92 percent.
The reaction time was 10 h.
Example 2
The ethylene glycol preparation is carried out by using the system and the process, wherein:
the temperature of the reactor is 70 ℃, and the pressure in the reactor is 1.1 atm;
the feed temperature of ethylene gas and oxygen was 168 ℃;
the gas-liquid ratio in the micro-interface generator is 700: 1.
after the system and the process are used, the conversion rate of the ethylene glycol is 93 percent.
The reaction time was 10 h.
Example 3
The ethylene glycol preparation is carried out by using the system and the process, wherein:
the temperature of the reactor is 80 ℃, and the pressure in the reactor is 1.2 atm;
the feed temperature of ethylene gas and oxygen was 168 ℃;
the gas-liquid ratio in the micro-interface generator is 700: 1.
after the system and the process are used, the conversion rate of the ethylene glycol is 92 percent.
The reaction time was 10 h.
Example 4
The ethylene glycol preparation is carried out by using the system and the process, wherein:
the temperature of the reactor is 85 ℃, and the pressure in the reactor is 1.1 atm;
the feed temperature of ethylene gas and oxygen was 168 ℃;
the gas-liquid ratio in the micro-interface generator is 700: 1.
after the system and the process are used, the conversion rate of the ethylene glycol is 93 percent.
The reaction time was 10 h.
Example 5
The ethylene glycol preparation is carried out by using the system and the process, wherein:
the temperature of the reactor is 90 ℃, and the pressure in the reactor is 1.2 atm;
the feed temperature of ethylene gas and oxygen was 168 ℃;
the gas-liquid ratio in the micro-interface generator is 700: 1.
after the system and the process are used, the conversion rate of the ethylene glycol is 92 percent.
The reaction time was 10 h.
Example 6
The ethylene glycol preparation is carried out by using the system and the process, wherein:
the temperature of the reactor is 90 ℃, and the pressure in the reactor is 1 atm;
the feed temperature of ethylene gas and oxygen was 168 ℃;
the gas-liquid ratio in the micro-interface generator is 700: 1.
after the system and the process are used, the conversion rate of the ethylene glycol is 93 percent.
The reaction time was 10 h.
Comparative example
The nitric acid preparation was carried out using the prior art, wherein the process parameters selected for this comparative example were the same as those in example 6.
The ethylene glycol conversion was determined to be 61%.
The reaction time was 34 h.
So far, the technical solution of the present invention has been described with reference to the preferred embodiments shown in the drawings, but it is easily understood by those skilled in the art that the scope of the present invention is obviously not limited to these specific embodiments. Without departing from the principle of the present invention, a person skilled in the art can make equivalent changes or substitutions to the related technical features, and the technical solutions after these changes or substitutions will fall within the protection scope of the present invention.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention; various modifications and changes may occur to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. An intelligent control reaction system for preparing ethylene glycol based on an ethylene hydration method is characterized by comprising:
the reactor is used for providing a reaction site for the gas containing the ethylene oxide and the deionized water to prepare ethylene glycol dilute solution;
an ethylene oxide generator disposed at one side of the reactor to provide a reaction site for ethylene gas and oxygen to produce ethylene oxide, a heat exchanger disposed between the ethylene oxide generator and the reactor to reduce the temperature of the ethylene oxide-containing gas;
the micro-interface generator is arranged in the reactor, converts the pressure energy of gas and/or the kinetic energy of liquid into the surface energy of bubbles and transmits the surface energy to the gas containing ethylene oxide, so that the gas containing ethylene oxide 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 between deionized water and the gas containing ethylene oxide is increased, the thickness of a liquid film is reduced, the mass transfer resistance is reduced, and the deionized water and the micron-sized bubbles containing ethylene oxide are mixed to form a gas-liquid mixture after crushing, so that the mass transfer efficiency and the reaction efficiency between the deionized water and the gas containing ethylene oxide are enhanced within a preset operating condition range;
the impurity removal unit is arranged on one side of the reactor and is used for removing volatile components in the ethylene glycol dilute solution;
the concentration unit is arranged on one side of the impurity removal unit and is used for concentrating the ethylene glycol dilute solution;
the intelligent control module comprises a P L C controller, a sensor and a cloud processor, wherein the sensor transmits acquired electric signals to the cloud processor, the cloud processor performs screening comparison in a cloud database according to reaction parameters returned by the sensor, and sends corresponding commands to the P L C controller after an optimal control method is screened out.
2. The system of claim 1, wherein the micro-interface generator is a pneumatic micro-interface generator, and the micro-interface generator is disposed in the reactor and is configured to crush gas containing ethylene oxide to form micron-sized bubbles and output the micron-sized bubbles into the reactor after the crushing is completed to mix with deionized water in the reactor to form a gas-liquid mixture.
3. The intelligent control reaction system for preparing ethylene glycol based on ethylene hydration method as claimed in claim 1, wherein the P L C controller comprises:
a first P L C controller for controlling the operation of the reactor;
a second P L C controller for controlling the operation of the ethylene oxide generator;
the third P L C controller is used for controlling the micro-interface generator to work;
the fourth P L C controller is used for controlling the operation of the impurity removing unit;
a fifth P L C controller for controlling operation of the concentration unit.
4. The system of claim 1, wherein a first liquid inlet pipe is arranged at the upper part of the side wall of the reactor in a communicating manner, a first pump body and a first flow meter are arranged on the first liquid inlet pipe, and the first liquid inlet pipe is used for conveying deionized water into the reactor.
5. The intelligent control reaction system for preparing ethylene glycol based on the ethylene hydration method according to claim 1, wherein an ethylene inlet pipe and an oxygen inlet pipe are arranged on the side wall of the ethylene oxide generator in a communicated manner, a second pump body and a second flow meter are arranged on the ethylene inlet pipe, a third pump body and a third flow meter are arranged on the oxygen inlet pipe, the ethylene inlet pipe and the oxygen inlet pipe are respectively used for transmitting ethylene gas and oxygen into the ethylene oxide generator, a silver catalyst is arranged inside the ethylene oxide generator and used for catalyzing ethylene gas and oxygen, the ethylene oxide generator is communicated with the micro-interface generator, and an eighth pump body is arranged between the ethylene oxide generator and the micro-interface generator.
6. The intelligent control reaction system for preparing the ethylene glycol based on the ethylene hydration method according to claim 1, wherein the impurity removal unit comprises:
the first cooler is communicated with the reactor, a fourth pump body is arranged between the first cooler and the reactor, and the first cooler is used for cooling the ethylene glycol dilute solution;
the expander is communicated with the first cooler and used for removing volatile components in the cooled ethylene glycol dilute solution, a gas outlet is formed in the upper end of the expander and used for discharging the volatile components, the lower end of the expander is communicated with the reactor and used for transmitting part of the ethylene glycol dilute solution in the expander back to the reactor for repeated reaction, and a fifth pump body is arranged between the expander and the reactor;
and the ethylene glycol dilute solution storage tank is communicated with the expander, a fourth flow meter is arranged between the ethylene glycol storage tank and the expander, and the ethylene glycol dilute solution storage tank is used for receiving the ethylene glycol dilute solution in the expander after the volatile components are removed.
7. The intelligent control reaction system for preparing ethylene glycol based on the ethylene hydration method as claimed in claim 1, wherein the concentration unit comprises:
the evaporator is communicated with the impurity removal unit, a sixth pump body and a sixth flowmeter are arranged between the evaporator and the impurity removal unit, the evaporator is used for evaporating and concentrating the ethylene glycol dilute solution, a second liquid inlet pipe is communicated with the middle of the side wall of the evaporator and used for receiving the ethylene glycol dilute solution transmitted by the impurity removal unit and transmitting the ethylene glycol dilute solution into the evaporator, a gas discharge pipe is communicated with the upper end of the evaporator and used for discharging evaporated gas, a liquid discharge pipe is communicated with the lower end of the evaporator and used for discharging the concentrated ethylene glycol dilute solution;
the second cooler is communicated with the evaporator, a seventh pump body is arranged between the second cooler and the evaporator, and the second cooler is used for cooling the evaporated gas discharged from the evaporator into liquid and transmitting the liquid back to the evaporator for re-evaporation;
and the dehydrating tower is communicated with the evaporator, the lower end of the dehydrating tower is provided with an electric control valve and a seventh flow meter, and the dehydrating tower is used for dehydrating the concentrated glycol solution.
8. The system of claim 1, wherein the sensor comprises:
a temperature sensor disposed within the reactor to monitor a reaction temperature within the reactor;
a pressure sensor disposed within the reactor to monitor a reaction pressure within the reactor.
9. The intelligent control reaction system for preparing the ethylene glycol based on the ethylene hydration method as claimed in claim 7, wherein the evaporator is a central circulating pipe type circulating evaporator.
10. The intelligent control reaction system for preparing the ethylene glycol based on the ethylene hydration method as claimed in claim 7, wherein the dehydration tower is a plate tower.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112441878A (en) * | 2020-11-30 | 2021-03-05 | 南京延长反应技术研究院有限公司 | Intelligent reaction system and method for preparing ethylene glycol by gas-phase catalytic hydration method |
| WO2022110872A1 (en) * | 2020-11-30 | 2022-06-02 | 南京延长反应技术研究院有限公司 | Enhanced reaction system and method for preparing ethylene glycol by means of gas-phase catalytic hydration method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112441878A (en) * | 2020-11-30 | 2021-03-05 | 南京延长反应技术研究院有限公司 | Intelligent reaction system and method for preparing ethylene glycol by gas-phase catalytic hydration method |
| WO2022110872A1 (en) * | 2020-11-30 | 2022-06-02 | 南京延长反应技术研究院有限公司 | Enhanced reaction system and method for preparing ethylene glycol by means of gas-phase catalytic hydration method |
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