WO2022110872A1 - 一种气相催化水合法制备乙二醇的强化反应系统及方法 - Google Patents
一种气相催化水合法制备乙二醇的强化反应系统及方法 Download PDFInfo
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- ethylene glycol
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- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 title claims abstract description 221
- 238000006703 hydration reaction Methods 0.000 title claims abstract description 135
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 69
- 238000000034 method Methods 0.000 title claims abstract description 48
- 230000036571 hydration Effects 0.000 title claims abstract description 47
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 34
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 claims abstract description 61
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 51
- 238000001704 evaporation Methods 0.000 claims abstract description 20
- 230000008020 evaporation Effects 0.000 claims abstract description 19
- 239000003054 catalyst Substances 0.000 claims description 38
- 239000007788 liquid Substances 0.000 claims description 33
- 239000012071 phase Substances 0.000 claims description 31
- 239000000463 material Substances 0.000 claims description 23
- 238000007670 refining Methods 0.000 claims description 20
- 238000000746 purification Methods 0.000 claims description 17
- 238000003860 storage Methods 0.000 claims description 17
- 238000006297 dehydration reaction Methods 0.000 claims description 16
- 230000018044 dehydration Effects 0.000 claims description 15
- 239000007791 liquid phase Substances 0.000 claims description 13
- 238000000926 separation method Methods 0.000 claims description 9
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 claims description 4
- CMWINYFJZCARON-UHFFFAOYSA-N 6-chloro-2-(4-iodophenyl)imidazo[1,2-b]pyridazine Chemical compound C=1N2N=C(Cl)C=CC2=NC=1C1=CC=C(I)C=C1 CMWINYFJZCARON-UHFFFAOYSA-N 0.000 claims description 2
- ZRGUXTGDSGGHLR-UHFFFAOYSA-K aluminum;triperchlorate Chemical compound [Al+3].[O-]Cl(=O)(=O)=O.[O-]Cl(=O)(=O)=O.[O-]Cl(=O)(=O)=O ZRGUXTGDSGGHLR-UHFFFAOYSA-K 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- 235000015497 potassium bicarbonate Nutrition 0.000 claims description 2
- 239000011736 potassium bicarbonate Substances 0.000 claims description 2
- 229910000028 potassium bicarbonate Inorganic materials 0.000 claims description 2
- 229910000027 potassium carbonate Inorganic materials 0.000 claims description 2
- 235000011181 potassium carbonates Nutrition 0.000 claims description 2
- TYJJADVDDVDEDZ-UHFFFAOYSA-M potassium hydrogencarbonate Chemical compound [K+].OC([O-])=O TYJJADVDDVDEDZ-UHFFFAOYSA-M 0.000 claims description 2
- 238000002360 preparation method Methods 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 239000002994 raw material Substances 0.000 abstract description 5
- 239000000047 product Substances 0.000 description 26
- 239000007789 gas Substances 0.000 description 24
- 238000004519 manufacturing process Methods 0.000 description 10
- 238000012546 transfer Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 150000007529 inorganic bases Chemical class 0.000 description 5
- 150000007522 mineralic acids Chemical class 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- 239000003957 anion exchange resin Substances 0.000 description 4
- -1 aryl ethylene glycol Chemical compound 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000010992 reflux Methods 0.000 description 4
- KMTRUDSVKNLOMY-UHFFFAOYSA-N Ethylene carbonate Chemical compound O=C1OCCO1 KMTRUDSVKNLOMY-UHFFFAOYSA-N 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 3
- MYRTYDVEIRVNKP-UHFFFAOYSA-N 1,2-Divinylbenzene Chemical compound C=CC1=CC=CC=C1C=C MYRTYDVEIRVNKP-UHFFFAOYSA-N 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- 239000003377 acid catalyst Substances 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 2
- 229910000323 aluminium silicate Inorganic materials 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 239000011964 heteropoly acid Substances 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000003456 ion exchange resin Substances 0.000 description 2
- 229920003303 ion-exchange polymer Polymers 0.000 description 2
- 125000001453 quaternary ammonium group Chemical group 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- PUPZLCDOIYMWBV-UHFFFAOYSA-N (+/-)-1,3-Butanediol Chemical compound CC(O)CCO PUPZLCDOIYMWBV-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- 239000004593 Epoxy Substances 0.000 description 1
- 239000004793 Polystyrene Substances 0.000 description 1
- 229910006069 SO3H Inorganic materials 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 229920000180 alkyd Polymers 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 230000002528 anti-freeze Effects 0.000 description 1
- 239000003125 aqueous solvent Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000003990 capacitor Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003729 cation exchange resin Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 239000003792 electrolyte Substances 0.000 description 1
- 229920006351 engineering plastic Polymers 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 229920001225 polyester resin Polymers 0.000 description 1
- 239000004645 polyester resin Substances 0.000 description 1
- 229920002223 polystyrene Polymers 0.000 description 1
- 150000003242 quaternary ammonium salts Chemical class 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/09—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis
- C07C29/10—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis of ethers, including cyclic ethers, e.g. oxiranes
- C07C29/103—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis of ethers, including cyclic ethers, e.g. oxiranes of cyclic ethers
- C07C29/106—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis of ethers, including cyclic ethers, e.g. oxiranes of cyclic ethers of oxiranes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Definitions
- the invention relates to the field of ethylene glycol preparation, in particular to an enhanced reaction system and method for preparing ethylene glycol by a gas-phase catalytic hydration method.
- Ethylene glycol is an important aliphatic diol with a wide range of uses, mainly in the production of polyester resins, including fibers, films and engineering plastics. It can also be directly used as a coolant and antifreeze, and is also an indispensable material for the production of alkyd resins, plasticizers, paints, adhesives, surfactants, explosives and capacitor electrolytes.
- the preparation of ethylene glycol with ethylene oxide as a raw material is mainly divided into two methods.
- One is the direct hydration method, that is, ethylene oxide directly reacts with water to generate ethylene glycol under certain conditions, and the reaction does not require a catalyst. It is divided into two methods: catalytic hydration and non-catalytic hydration; the other method is the ethylene carbonate method, that is, under the action of a catalyst, ethylene oxide first reacts with CO2 to generate ethylene carbonate, and then hydrolyzes to generate ethylene glycol alcohol.
- the non-catalytic hydration process of direct hydration method is used in industrial preparation of ethylene glycol, also called pressurized hydration.
- This method does not use catalyst, and the molar ratio of reaction feed water and ethylene oxide (hereinafter referred to as water ratio) is 20 ⁇ 25:1, the reaction temperature is 150 ⁇ 200°C, the reaction pressure is 0.8 ⁇ 2.0MPa, the conversion rate of ethylene oxide is close to 100%, and the selectivity of ethylene glycol is about 90%.
- water ratio the molar ratio of reaction feed water and ethylene oxide
- the reaction temperature is 150 ⁇ 200°C
- the reaction pressure is 0.8 ⁇ 2.0MPa
- the conversion rate of ethylene oxide is close to 100%
- the selectivity of ethylene glycol is about 90%.
- the unconverted ethylene oxide continues to react with the product ethylene glycol to generate diethylene glycol, triethylene glycol, etc.
- the earliest method of industrial catalytic hydration to produce ethylene glycol uses inorganic acid or base as catalyst, such as sulfuric acid or phosphoric acid as catalyst, ethylene oxide can be completely converted, and the yield of ethylene glycol is about 90%, but inorganic acid
- the catalyst causes corrosion to equipment and pollutes the environment; when using inorganic bases as catalysts, it is easy to promote the production of some high molecular weight by-products and reduce product selectivity. Therefore, although acids and bases have obvious catalytic effects on the hydration of ethylene oxide, the traditional acid-base catalyzed hydration processes have been eliminated and are no longer used.
- Ion exchange resins are used as catalysts, one is a strongly acidic cation exchange resin with -SO3H, -PO(OH)2 groups, the other is a basic anion exchange resin containing quaternary ammonium salts, and based on metal oxygen Acid-catalyzed anion exchange resin.
- US Patent 5,874,653 discloses an anion exchange resin with quaternary ammonium groups cross-linked by styrene and divinylbenzene as an ethylene oxide hydration catalyst. Under the conditions of reaction temperature of 80-200°C, reaction pressure of 200-3000KPa, and water ratio of 1-15:1, the conversion rate of ethylene oxide is close to 100%, and the selectivity of ethylene glycol is 95%.
- the compound of heteropoly acid salt is used as a catalyst, such as JP82106631 discloses a K2MoO4-KI catalyst, which makes ethylene oxide react with carbon dioxide at 160 ° C to generate ethylene carbonate, the conversion rate of ethylene oxide is 99.9%, and ethylene oxide is 99.9%.
- the alcohol selectivity is 100%; then, using alumina as a catalyst, at a reaction temperature of 140°C and a reaction pressure of 2.25MPa, hydrolyzed to obtain an ethylene glycol product, the ethylene oxide conversion rate is 100%, and the ethylene glycol selectivity is 99.8%.
- the remarkable feature of using the above-mentioned heteropoly acid salt catalyst is: when the catalyst is soluble in water, the ethylene oxide conversion rate and product selectivity are high, but the catalyst is easily lost, which brings unnecessary trouble to the post-treatment process; When the catalyst is insoluble in water, the conversion of ethylene oxide is significantly reduced, and the selectivity of ethylene glycol is poor.
- Hei 06-179633 discloses a method for producing aryl ethylene glycol.
- the patent is to treat aryl ethylene oxide with niobic acid in water and an aqueous solvent. Using the niobate catalyst can effectively The epoxy ring part in the aryl oxirane is hydrolyzed, and the yield of the aryl ethylene glycol is above 95%.
- the disadvantage of this method is that the water ratio is too high, and the existence of a large amount of water brings huge energy consumption to the separation of the ethylene glycol product.
- Japanese Patent Laid-Open No. 7-53219 introduces a niobate particle and its preparation method.
- the niobic acid prepared by this method can exist stably for a long time under hydrothermal conditions.
- the acidity of the niobic acid catalyst is too strong, more than 50% of which is a strong acid content of H0:-5.6 or less, and is not suitable for the reaction of ethylene oxide catalyzed by hydration to prepare ethylene glycol.
- the first object of the present invention is to provide an enhanced reaction system for preparing ethylene glycol by a gas-phase catalytic hydration method.
- the reaction system effectively guarantees the epoxy Ethane and water are fully reacted.
- the second object of the present invention is to provide a reaction method for preparing ethylene glycol by using a reaction system.
- the ethylene glycol obtained by the reaction has high purity, is widely used, and improves the applicability of ethylene glycol itself, which is worthy of widespread application.
- the invention provides an enhanced reaction system for preparing ethylene glycol by a gas-phase catalytic hydration method, comprising: a hydration reaction rectifier, an enhanced hydration reaction rectifier and an evaporation tower; the side wall of the hydration reaction rectifier is provided with Ethylene oxide inlet; the bottom of the hydration reaction rectifier is provided with a water inlet;
- the hydration reaction rectifier is provided with a pneumatic micro-interface generator and a first hydraulic micro-interface generator, and the pneumatic micro-interface generator is arranged below the first hydraulic micro-interface generator; the pneumatic micro-interface generator The micro-interface generator and the first hydraulic micro-interface generator are both connected to the ethylene oxide inlet for breaking the micro-bubbles of the ethylene oxide gas to the micron level;
- a second hydraulic micro-interface generator is arranged inside the enhanced hydration reaction rectifier; a material outlet is arranged at the bottom of the hydration reaction rectifier; the material outlet is connected with a first reboiler; from the material outlet The discharged material is divided into two streams of gas and liquid by the first reboiler.
- a material outlet is arranged at the bottom of the hydration reaction rectifier; the material outlet is connected with a first reboiler; from the material outlet The discharged material is divided into two streams of gas and liquid by the first reboiler.
- the bottom of the enhanced hydration reaction rectifier is provided with an ethylene glycol outlet for the discharge of product ethylene glycol, and the ethylene glycol discharged from the ethylene glycol outlet is divided into two streams of gas and liquid through the second reboiler, The gas-phase stream is circulated back to the intensified hydration reaction rectifier, and the liquid-phase stream flows into the evaporation tower for gas-liquid separation.
- Patent RU2001901C1 adopts a series process of multiple displacement flow reactors, and uses a bicarbonate-containing quaternary ammonium polystyrene anion exchanger as a catalyst to promote the reaction.
- Patent US5488184 discloses an anion exchange resin catalyst for ethylene oxide hydration.
- patent CN1237953A discloses a method for the production of dihydric alcohol, and the reaction is promoted by aluminosilicate zeolite, amorphous aluminosilicate and acidic ion exchange resin as catalysts. It can be seen that in the prior art, a large amount of catalyst is required to promote the reaction, the catalyst is highly dependent, and the production cost is high.
- a pneumatic micro-interface generator and a first hydraulic micro-interface generator are arranged inside the hydration reaction rectifier, so as to realize that the ring entering the hydration reaction rectifier can be
- the oxyethane is dispersed and broken into microbubbles, which improves the mass transfer effect, greatly increases the mass transfer rate, reduces the temperature and pressure of the hydrogenation reaction, and reduces the dependence on the catalyst; by strengthening the hydration reaction rectifier in series, it will be The incompletely reacted ethylene oxide in the hydration reaction rectifier is input into it, and it is dispersed and broken by the second hydraulic micro-interface generator inside the hydration reaction rectifier, which can ensure that the remaining ethylene oxide is sufficient. Reflect, improve the utilization rate of raw materials.
- the pneumatic micro-interface generator in the hydration reaction rectifier is arranged opposite to the outlet of the first hydraulic micro-interface generator, and the pneumatic micro-interface generator is opposite to the first hydraulic micro-interface generator.
- the outlets of the micro-interface generators are all provided with guide discs for evenly distributing the generated micro-bubbles.
- the guide disc is tapered; a plurality of guide holes are evenly distributed on the guide disc.
- the guiding curve of the guiding disc is any one of a hyperbola, a parabola, a two-segment broken line and a logarithmic curve.
- the outlet of the second hydrodynamic micro-interface generator inside the enhanced hydration reaction rectifier is provided with a screen for evenly distributing the generated micro-bubbles.
- the bottom of the enhanced hydration reaction rectifier is provided with a liquid inlet for introducing water.
- a pneumatic micro-interface generator and a first hydraulic micro-interface generator are arranged inside the hydration reaction rectifier, wherein the pneumatic micro-interface generator is arranged below the first hydraulic micro-interface generator, and the ethylene oxide
- the alkane enters the pneumatic micro-interface generator and the first hydraulic micro-interface generator through the ethylene oxide inlet, and at the same time, the water enters the hydration reaction rectifier through the liquid inlet.
- the water enters the pneumatic micro-interface generator and the first hydraulic micro-interface generator, and acts as a medium in close contact with the incoming ethylene oxide, thus ensuring that the ethylene oxide can be fully dispersed and broken, and
- the pneumatic micro-interface generator and the first hydraulic micro-interface generator each have a micro-interface system, which improves the efficiency of dispersion and crushing. Opposing the pneumatic micro-interface generator to the outlet of the first hydraulic micro-interface generator is also to achieve a hedging effect, so as to achieve uniform distribution of micro-bubbles.
- a guide disc is also arranged at the outlet of the pneumatic micro-interface generator and the first hydraulic micro-interface generator, and a plurality of guide holes are evenly distributed on the guide disc, and the diameter of the guide holes is along the direction away from the feed port. increase sequentially.
- the guide disc can change the running direction of the micro-bubbles, so that the bubbles are evenly distributed; at the same time, the guide holes on the guide disc can also redistribute the micro-bubbles, so that the micro-bubbles are distributed more evenly in the hydration reaction rectifier , which is conducive to the reaction. Therefore, the present invention improves the application effect of the micro-interface generator itself by combining the micro-interface generator with the guide disc.
- the present invention is also provided with an intensified hydration reaction rectifier connected in series with the hydration reaction rectifier, and a second liquid-dynamic micro-interface generator is also arranged inside the intensified hydration reaction rectifier. It can be fully dispersed and broken inside the second hydraulic micro-interface generator.
- the bottom of the enhanced hydration reaction rectifier is provided with a liquid inlet, and water enters from the liquid inlet as a medium.
- a screen mesh is arranged at the outlet of the second hydraulic micro-interface generator, in order to uniformly distribute the generated micro-bubbles in the medium of the intensified hydration reaction rectifier, which is beneficial to improve the reaction rate.
- the application effect of the second hydraulic micro-interface generator itself is improved by the cooperation of the second hydraulic micro-interface generator with the screen.
- micro-interface generator used in the present invention has been embodied in the inventor's prior patents, such as application numbers CN201610641119. Patents of CN205833127U and CN207581700U. In the previous patent CN201610641119.6, the specific product structure and working principle of the micro-bubble generator (that is, the micro-interface generator) were introduced in detail.
- the body is provided with an inlet communicating with the cavity, the opposite first and second ends of the cavity are open, wherein the cross-sectional area of the cavity is from the middle of the cavity to the first and second ends of the cavity.
- the second end is reduced; the secondary crushing piece is arranged at at least one of the first end and the second end of the cavity, a part of the secondary crushing piece is arranged in the cavity, and both ends of the secondary crushing piece and the cavity are open An annular channel is formed between the through holes of the micro-bubble generator.
- the micro-bubble generator also includes an air inlet pipe and a liquid inlet pipe.” From the specific structure disclosed in the application document, we can know that its specific working principle is: the liquid enters the micron tangentially through the liquid inlet pipe.
- the micro-bubble generator in this patent belongs to the pneumatic micro-interface generation. device.
- the previous patent 201610641251.7 records that the primary bubble breaker has a circulating liquid inlet, a circulating gas inlet and a gas-liquid mixture outlet, and the secondary bubble breaker communicates the feed port with the gas-liquid mixture outlet, indicating that the bubble breaker is both It needs to be mixed with gas and liquid.
- the primary bubble breaker mainly uses circulating liquid as power, so in fact, the primary bubble breaker belongs to the hydraulic micro-interface generator, and the secondary bubble breaker is a gas-liquid breaker. The mixture is simultaneously fed into the elliptical rotating ball for rotation, so that the bubbles are broken during the rotation, so the secondary bubble breaker is actually a gas-liquid linkage type micro-interface generator.
- both hydraulic micro-interface generators and gas-liquid linkage micro-interface generators belong to a specific form of micro-interface generators.
- the micro-interface generators used in the present invention are not limited to the above-mentioned forms.
- the specific structure of the bubble breaker described in the prior patent is only one of the forms that the micro-interface generator of the present invention can take.
- the previous patent 201710766435.0 recorded that "the principle of the bubble breaker is to achieve high-speed jets to achieve gas collision", and also stated that it can be used in micro-interface enhanced reactors to verify the relationship between the bubble breaker and the micro-interface generator.
- the top of the bubble breaker is the liquid phase inlet, and the side is the gas phase inlet.
- the liquid phase entering from the top provides the entrainment power, so as to achieve the effect of crushing into ultra-fine bubbles, which can also be seen in the accompanying drawings.
- the bubble breaker has a conical structure, and the diameter of the upper part is larger than that of the lower part, so that the liquid phase can provide better entrainment power.
- micro-interface generator Since the micro-interface generator was just developed in the early stage of the previous patent application, it was named as micro-bubble generator (CN201610641119.6), bubble breaker (201710766435.0), etc., and later changed its name to micro-interface generator with continuous technological improvement.
- the micro-interface generator in the present invention is equivalent to the previous micro-bubble generator, bubble breaker, etc., but the names are different.
- the micro-interface generator of the present invention belongs to the prior art, although some bubble breakers belong to the type of pneumatic bubble breakers, some belong to the type of hydraulic bubble breakers, and some belong to the type of gas bubble breakers.
- the type of liquid-linked bubble breaker but the difference between the types is mainly selected according to the specific working conditions.
- the connection between the micro-interface generator and the reactor and other equipment, including the connection structure and connection position depends on the micro-interface generator. It depends on the structure of the interface generator, which is not limited.
- the evaporation tower is connected with a dehydration tower, the material from the bottom of the evaporation tower is divided into two streams of gas and liquid through the third reboiler, the gas phase stream is recycled back to the evaporation tower, and the liquid phase stream enters the Further separation and purification are carried out in the dehydration tower.
- the dehydration tower is connected with a purification tower for further purification and purification of the material discharged from the dehydration tower. After purification, the mixed water in the ethylene glycol product can be removed, and the product purity can be improved.
- the refining tower is connected with a product storage tank, and the product refined by the refining tower flows to the product storage tank for storage.
- the top of the hydration reactive rectifier and the enhanced hydration reactive rectifier are both provided with an additive channel for adding catalyst.
- a first condenser is connected to the top of the hydration reactive rectifier, and unreacted water and ethylene oxide are condensed by the first condenser and then refluxed into the hydration reactive rectifier.
- the top of the enhanced hydration reaction rectifier is provided with a second condenser, and the second condenser can condense and reflux the unreacted ethylene oxide gas in the enhanced hydration reaction rectifier to the enhanced hydration reaction rectifier in the device.
- a third condenser is connected to the top of the refining column, and the gas phase components at the top of the refining column are condensed by the third condenser and then refluxed to the top of the refining column.
- the top of the refining tower is fully refluxed, and the gaseous ethylene glycol is condensed into a liquid phase by the third condenser, and returned to the refining tower through the reflux line.
- the present invention also provides a reaction method for preparing the enhanced reaction system of ethylene glycol by applying the above-mentioned gas-phase catalytic hydration method, comprising the following steps:
- the micro-interface is dispersed and broken, and then the catalytic hydration reaction is carried out, and then ethylene glycol is obtained after separation, purification and purification; the temperature of the catalytic hydration reaction is 150-165° C.
- the catalyst for the catalytic hydration reaction is any one or a mixture of potassium carbonate, potassium bicarbonate, aluminum perchlorate and aluminum trifluoromethanesulfonate.
- a pneumatic micro-interface generator and a first hydraulic micro-interface generator connected to the ethylene oxide inlet are arranged inside the hydration reaction rectifier, so that the hydration of the ethylene oxide and the raw material water is carried out.
- it is broken into micro-bubbles with a diameter greater than or equal to 1 ⁇ m and less than 1 mm, so that ethylene oxide is in contact with water in the state of micro-bubbles, so as to increase the phase boundary transfer between ethylene oxide and water during the hydration reaction.
- the mass area is fully mixed and then the hydration reaction is carried out, thereby reducing the amount of water and catalyst required for the reaction and improving the reaction efficiency.
- the ethylene glycol product obtained by the reaction method of the present invention has good quality and high yield.
- the preparation method itself has low reaction temperature, greatly reduced pressure and significantly reduced cost.
- the intensified reaction system that the gas-phase catalytic hydration method of the present invention prepares ethylene glycol effectively guarantees that ethylene oxide and water fully react by setting the hydration reaction rectifier and the intensified hydration reaction rectifier connected in series with it;
- the reaction method of the present invention is easy to operate, the ethylene glycol obtained by the reaction has high purity, is widely used, and improves the applicability of ethylene glycol itself, and is worthy of widespread application.
- FIG. 1 is a schematic structural diagram of an enhanced reaction system for preparing ethylene glycol by a gas-phase catalytic hydration method according to an embodiment of the present invention.
- the terms “installed”, “connected” and “connected” should be understood in a broad sense, unless otherwise expressly specified and limited, for example, it may be a fixed connection or a detachable connection Connection, or integral connection; can be mechanical connection, can also be electrical connection; can be directly connected, can also be indirectly connected through an intermediate medium, can be internal communication between two elements.
- installed should be understood in a broad sense, unless otherwise expressly specified and limited, for example, it may be a fixed connection or a detachable connection Connection, or integral connection; can be mechanical connection, can also be electrical connection; can be directly connected, can also be indirectly connected through an intermediate medium, can be internal communication between two elements.
- the present embodiment provides an enhanced reaction system for preparing ethylene glycol by a gas-phase catalytic hydration method, including: a hydration reaction rectifier 10, an enhanced hydration reaction rectifier 20 and an evaporation tower 30; a hydration reaction rectifier 30; An ethylene oxide inlet 104 is arranged on the side wall of the still 10; a water inlet 106 is arranged at the bottom of the hydration reaction rectifier 10; the ethylene oxide inlet 104 is connected with the ethylene oxide storage tank 70; The storage tank 80 is connected, and a water pump 90 is arranged between the water storage tank 80 and the water inlet 106 .
- the top of the hydration reaction rectifier 10 and the enhanced hydration reaction rectifier 20 are both provided with a dosing channel 101 for adding catalyst.
- the top of the hydration reactive rectifier 10 is also connected with a first condenser 107 , and the unreacted water and ethylene oxide are condensed by the first condenser 107 and then return to the hydration reactive rectifier 10 .
- the hydration reaction rectifier 10 is provided with a pneumatic micro-interface generator 105 and a first hydraulic micro-interface generator 102, and the pneumatic micro-interface generator 105 is arranged below the first hydraulic micro-interface generator 102; the pneumatic micro-interface generates
- the device 105 and the first hydraulic micro-interface generator 102 are both connected to the ethylene oxide inlet 104 for breaking the micro-bubbles whose ethylene oxide gas is micron;
- the interface generator 105 is arranged opposite to the outlet of the first hydraulic micro-interface generator 102, and both the pneumatic micro-interface generator 105 and the outlet of the first hydraulic micro-interface generator 102 are provided with a guide disc 103 for generating The microbubbles are evenly distributed.
- the guide disc 103 is tapered; a plurality of guide holes are evenly distributed on the guide disc 103 . Further, the guiding curve of the guiding disc 103 is any one of a hyperbola, a parabola, a two-segment polyline and a logarithmic curve.
- a second hydraulic micro-interface generator 201 is arranged inside the enhanced hydration reaction rectifier 20; a screen 202 is arranged at the outlet of the second hydraulic micro-interface generator 201 for evenly distributing the generated micro-bubbles.
- the bottom of the hydration reaction rectifier 10 is provided with a material outlet 109; the material outlet 109 is connected with a first reboiler 108; the material discharged from the material outlet 109 is divided into two streams of gas and liquid through the first reboiler 108, and the gas stream passes through the first reboiler 108.
- the two-hydraulic micro-interface generator 201 enters the intensified hydration reaction rectifier 20, and the liquid stream flows directly into the intensified hydration reaction rectifier 20;
- the bottom of the enhanced hydration reaction rectifier 20 is provided with an ethylene glycol outlet 203 for the discharge of product ethylene glycol, and the ethylene glycol discharged from the ethylene glycol outlet 203 is divided into two streams of gas and liquid through the second reboiler 204, The gas-phase stream is circulated back to the enhanced hydration reaction rectifier 20, and the liquid-phase stream flows into the evaporation tower 30 for gas-liquid separation.
- the bottom of the enhanced hydration reaction rectifier 20 is provided with a liquid inlet for introducing water. The liquid inlet is connected to the water storage tank 80 .
- the top of the enhanced hydration reaction rectifier 20 is also provided with a second condenser 205, and the second condenser 205 can condense and reflux the unreacted ethylene oxide gas in the enhanced hydration reaction rectifier 20 to the enhanced hydration reaction rectifier. device 20.
- the evaporation tower 30 is connected with the dehydration tower 40, the material from the bottom of the evaporation tower 30 is divided into two streams of gas and liquid through the third reboiler 301, the gas phase stream is circulated back to the evaporation tower 30, and the liquid phase stream enters the Further separation and purification are carried out in the dehydration tower 40 .
- the dehydration tower 40 is connected with a purification tower 50 for further purification and purification of the material discharged from the dehydration tower 40. After purification, the mixed water in the ethylene glycol product can be removed, and the product purity can be improved.
- the refining tower 50 is connected with a product storage tank 60, and the product refined by the refining tower 50 flows to the product storage tank 60 for storage.
- a third condenser 501 is connected to the top of the refining column 50 , and the gas phase components at the top of the refining column are condensed by the third condenser 501 and then refluxed to the top of the refining column 50 .
- the top of the refining tower 50 is fully refluxed, and the gaseous ethylene glycol is condensed into a liquid phase by the third condenser 501, and is returned to the refining tower through the reflux line.
- a fourth reboiler 401 is arranged between the dehydration tower 40 and the refining tower 50 ; a fifth reboiler 502 is arranged in the refining tower 50 and the product storage tank 60 .
- the fourth reboiler 401 and the fifth reboiler 502 partially vaporize the passing material, the liquid phase continues to be output, and the gas phase is refluxed, which can further purify the material.
- the top of the hydration reactive rectifier 10 is connected with the second reboiler 204
- the top of the enhanced hydration reactive rectifier 20 is connected with the third reboiler 301
- the top of the evaporation tower 30 is connected with the fourth reboiler 401
- the dehydration tower The top of 40 is connected to the fifth reboiler 502, so that the steam of the previous stage can be used as the heat source of the reboiler of the next stage, and the utilization efficiency of energy can be improved.
- the enhanced reaction system of the present invention has fewer equipment components, small footprint, low energy consumption, low cost, high safety, and controllable reaction. , the raw material conversion rate is high, which is equivalent to providing a reaction system with stronger operability for the field of ethylene glycol preparation, which is worthy of widespread application.
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Abstract
本发明提供了一种气相催化水合法制备乙二醇的强化反应系统，包括：水合反应精馏器、强化水合反应精馏器和蒸发塔；所述水合反应精馏器的侧壁上设置有环氧乙烷进口；所述水合反应精馏器底部设置有进水口；所述水合反应精馏器内部设置有气动式微界面发生器和第一液动式微界面发生器，所述气动式微界面发生器设置在所述第一液动式微界面发生器的下方。本发明的强化反应系统设备组件少、占地面积小、能耗低、成本低、安全性高、反应可控，原料转化率高，相当于为乙二醇制备领域提供了一种操作性更强的反应系统，值得广泛推广应用。
Description
本发明涉及乙二醇制备领域，具体而言，涉及一种气相催化水合法制备乙二醇的强化反应系统及方法。
乙二醇是重要的脂肪族二元醇，用途广泛，主要用途是生产聚酯树脂，包括纤维、薄膜及工程塑料。还可直接用作冷却剂和防冻剂，同时也是生产醇酸树脂、增塑剂、油漆、胶粘剂、表面活性剂、炸药及电容器电解液等产品不可缺少的物质。
以环氧乙烷为原料制备乙二醇，主要分为两种方法，一种为直接水合法，即环氧乙烷在一定条件下直接与水反应生成乙二醇，反应不需要催化剂就可以进行，分为催化水合和非催化水合两种方法；另一种方法为碳酸亚乙酯法，即环氧乙烷在催化剂作用下，先与CO2反应生成碳酸亚乙酯，然后水解生成乙二醇。
目前工业上制备乙二醇采用直接水合法的非催化水合工艺，也称加压水合，该方法不使用催化剂，反应进料水和环氧乙烷的摩尔比(以下简称水比)为20～25∶1，反应温度150～200℃，反应压力0.8～2.0MPa，环氧乙烷转化率接近100％，乙二醇选择性90％左右。反应中，由于乙二醇与环氧乙烷反应活性高于水与环氧乙烷的反应活性，未转化的环氧乙烷继续和产物乙二醇反应，生成二甘醇、三甘醇等副产物，因此工业上常采取水为大过量的办法，来提高乙二醇选择性。该方法的最大缺点是生产中大量的能量用于蒸发产品中85％以上的水份。例如，在乙二醇产品提纯步骤中，当进料水比为20时，通过蒸发除去大约为乙二醇19倍的无用水，所需的热以每摩尔乙二醇计为170千卡， 意味着生产1吨乙二醇需要消耗大约5.5吨蒸汽，造成该方法能源耗费巨大，生产成本偏高。因此，为了减少反应水比，降低能耗，国内外研究者竞相开展了多种环氧乙烷催化水合反应技术的研究。
最早工业催化水合生产乙二醇的方法，用无机酸或碱作催化剂，如用硫酸或磷酸等作为催化剂时，环氧乙烷可全部转化，乙二醇收率为90％左右，但无机酸催化剂对设备造成腐蚀，污染环境；使用无机碱作催化剂时，易促进产生一些高分子量的副产物，降低产品选择性。因此，尽管酸、碱对环氧乙烷水合具有明显的催化作用，但传统意义上的酸碱催化水合工艺都已经淘汰，不再使用。
为克服无机酸和碱催化水合的缺点，人们对环氧乙烷催化水合的方法及催化剂进行了多方面的改进研究。
用离子交换树脂作催化剂，一类是带有-SO3H、-PO(OH)2基团的强酸性阳离子交换树脂，另一类是含季胺盐地碱性阴离子交换树脂，以及基于金属含氧酸根催化作用的阴离子交换树脂。如USPatent5,874,653公开了一种由苯乙烯和二乙烯基苯交联的带有季铵基的阴离子交换树脂作为环氧乙烷水合催化剂。在反应温度80～200℃、反应压力200～3000KPa，水比1～15∶1的条件下反应，环氧乙烷的转化率接近100％，乙二醇的选择性95％。但该催化体系的显著缺点是树脂催化剂耐热性能差，即使在比较低的温度范围内(＜95℃)，催化剂的膨胀仍较严重，从而导致反应器床层压降上升较快，催化剂更换频繁，给工业生产带来不利。因而尽管上述研究工作取得了很大进展，但仍限制了它的应用范围。用杂多酸盐的复合物作催化剂，如JP82106631公开了一种K2MoO4-KI催化剂，使环氧乙烷与二氧化碳在160℃反应生成碳酸亚乙酯，环氧乙烷转化率99.9％，乙二醇选择性100％；然后以氧化铝为催化剂，在反应温度140℃，反应压力2.25MPa条件下，水解得到乙二醇产品，环氧乙烷转化率100％，乙二醇选择性99.8％。使用上述杂多酸盐催化剂的显著特点是：当催化剂可溶解于水时，环氧乙烷转化率及产品选择性较高，但催化剂易流失，给后处理工序 带来了不必要的麻烦；当催化剂不溶于水时，环氧乙烷转化率明显降低，乙二醇的选择性较差。日本专利特开平06-179633公开了一种芳基乙二醇的制造方法，该专利是将芳基环氧乙烷在水和含水溶剂中用铌酸处理，使用该铌酸催化剂可有效地将芳基环氧乙烷中的环氧环部分加水分解，芳基乙二醇的收率在95％以上。但该方法的缺点是水比过高，大量水的存在给乙二醇产品的分离带来巨大能耗。日本专利特开平7-53219介绍了一种铌酸颗粒及其制备方法。应用该方法制备的铌酸可以在水热条件下长时间稳定存在。但该铌酸催化剂的酸性过强，50％以上为H0：-5.6以下的强酸量，不适合用于环氧乙烷催化水合制乙二醇反应。
有鉴于此，特提出本发明。
发明内容
本发明的第一目的在于提供一种气相催化水合法制备乙二醇的强化反应系统，该反应系统通过设置水合反应精馏器以及与之串联的强化水合反应精馏器，有效保证了环氧乙烷和水充分反应，通过在水合反应精馏器内部设置气动式微界面发生器和第一液动式微界面发生器以及在强化水合反应精馏器内部设置第二水合反应精馏器，使得在环氧乙烷与水进行催化水合反应之前将环氧乙烷破碎为微气泡，提高环氧乙烷与水之间的相界传质面积，提高了反应效率，催化剂的添加量减少，能源消耗少，生产成本低。
本发明的第二目的在于提供一种采用反应系统制备乙二醇的反应方法，反应得到的乙二醇纯度高，应用广泛，提高了乙二醇本身的适用面，值得广泛推广应用。
为了实现本发明的上述目的，特采用以下技术方案：
本发明提供了一种气相催化水合法制备乙二醇的强化反应系统，包括：水合反应精馏器、强化水合反应精馏器和蒸发塔；所述水合反应精馏器的侧壁上 设置有环氧乙烷进口；所述水合反应精馏器底部设置有进水口；
所述水合反应精馏器内部设置有气动式微界面发生器和第一液动式微界面发生器，所述气动式微界面发生器设置在所述第一液动式微界面发生器的下方；所述气动式微界面发生器与所述第一液动式微界面发生器均与所述环氧乙烷进口相连以用于破碎环氧乙烷气体为微米级别的微气泡；
所述强化水合反应精馏器内部设置有第二液动式微界面发生器；所述水合反应精馏器底部设置有物料出口；所述物料出口连接有第一再沸器；从所述物料出口排出的物料通过所述第一再沸器分成气液两股物流，气相物流通过所述第二液动式微界面发生器进入所述强化水合反应精馏器中，液相物流直接流入所述强化水合反应精馏器中；
所述强化水合反应精馏器底部设置有乙二醇出口以用于产品乙二醇的排出，从所述乙二醇出口排出的乙二醇经第二再沸器分成气液两股物流，气相物流循环返回所述强化水合反应精馏器中，液相物流流入所述蒸发塔中进行气液分离。
现有技术中，工业催化水合生产乙二醇的方法，用无机酸或碱作催化剂，如用硫酸或磷酸等作为催化剂时，环氧乙烷可全部转化，乙二醇收率为90％左右，但无机酸催化剂对设备造成腐蚀，污染环境；使用无机碱作催化剂时，易促进产生一些高分子量的副产物，降低产品选择性。专利RU2001901C1采用多个置换流反应器串联工艺，以含碳酸氢盐的季铵基聚苯乙烯阴离子交换剂做催化剂推动反应进行，专利US5488184公开一种环氧乙烷水合的阴离子交换树脂催化剂，通过树脂催化剂推动反应进行，专利CN1237953A公开了一种生产二元醇的方法，通过硅铝酸盐沸石，无定形硅铝酸盐和酸性离子交换树脂作为催化剂推动反应进行。可见现有技术均需要大量的催化剂推动反应进行，对催化剂的依赖较大，生产成本高。
本发明的制备乙二醇的强化反应系统，通过在水合反应精馏器的内部设置气动式微界面发生器和第一液动式微界面发生器，从而实现了将进入水合反应 精馏器内的环氧乙烷进行分散破碎成微气泡，提高了传质效果，大幅度提高传质速率，降低了加氢反应温度与压力，减少了对催化剂的依赖；通过串联强化水合反应精馏器，将在水合反应精馏器中未完全反应的环氧乙烷输入其中，并通过强化水合反应精馏器内部的第二液动式微界面发生器对其进行分散破碎，能够保证剩余的环氧乙烷充分反映，提高了原料的利用率。
优选的，所述水合反应精馏器中的所述气动式微界面发生器与所述第一液动式微界面发生器的出口相对设置，且所述气动式微界面发生器与所述第一液动式微界面发生器的出口均设置有导向圆盘以用于使产生的微气泡均匀分布。
优选的，所述导向圆盘呈锥形；所述导向圆盘上均匀分布有多个导向孔。进一步的，所述导向圆盘的导向曲线为双曲线、抛物线、两段折线和对数曲线中的任意一种。
优选的，所述强化水合反应精馏器内部的所述第二液动式微界面发生器的出口处设置有用于将产生的微气泡均匀分布的筛网。
优选的，所述强化水合反应精馏器底部设置有进液口以用于通入水。
本发明在水合反应精馏器的内部设置有气动式微界面发生器和第一液动式微界面发生器，其中的气动式微界面发生器设置在第一液动式微界面发生器的下方，环氧乙烷通过环氧乙烷进口进入到气动式微界面发生器和第一液动式微界面发生器的内部，与此同时水通过进液口进入水合反应精馏器中，随着水在水合反应精馏器中的增多，水进入气动式微界面发生器和第一液动式微界面发生器中，并作为介质与进入的环氧乙烷密切的接触，从而保证了环氧乙烷能够充分分散破碎，且气动式微界面发生器和第一液动式微界面发生器中各进行了一次微界面体系，提高了分散破碎的效率。将气动式微界面发生器和第一液动式微界面发生器的出口相对，也是为了能够起到对冲效果，以实现微气泡的均匀分布。
本发明在气动式微界面发生器和第一液动式微界面发生器的出口处还设置有导向圆盘，导向圆盘上均匀分布有多个导向孔，且导向孔沿远离进料口的 方向直径依次增大。导向圆盘能够改变微气泡的运行方向，使气泡均匀分布；同时，导向圆盘上的导向孔也能够对微气泡起到再分布作用，使微气泡在水合反应精馏器内分布的更加均匀，有利于反应的进行。因此，本发明正是通过将微界面发生器与导向圆盘结合应用，提高了本身微界面发生器的应用效果。
本发明还设置有与水合反应精馏器相串联的强化水合反应精馏器，在强化水合反应精馏器内部还设置有第二液动式微界面发生器，经第一再沸器的气相物流能够在第二液动式微界面发生器内部得到充分的分散破碎，强化水合反应精馏器底部设置有进液口，水从进液口进入以作为介质。第二液动式微界面发生器的出口处设置有筛网，是为了产生的微气泡在强化水合反应精馏器的介质中的均匀分布，有利于提高反应速率。通过第二液动式微界面发生器与筛网相配合，提高了第二液动式微界面发生器本身的应用效果。
本领域所属技术人员可以理解的是，本发明所采用的微界面发生器在本发明人在先专利中已有体现，如申请号CN201610641119.6、201610641251.7、CN201710766435.0、CN106187660、CN105903425A、CN109437390A、CN205833127U及CN207581700U的专利。在先专利CN201610641119.6中详细介绍了微米气泡发生器(即微界面发生器)的具体产品结构和工作原理，该申请文件中记载了“微米气泡发生器包括本体和二次破碎件、本体内具有空腔，本体上设有与空腔连通的进口，空腔的相对的第一端和第二端均敞开，其中空腔的横截面积从空腔的中部向空腔的第一端和第二端减小；二次破碎件设在空腔的第一端和第二端中的至少一个处，二次破碎件的一部分设在空腔内，二次破碎件与空腔两端敞开的通孔之间形成一个环形通道。微米气泡发生器还包括进气管和进液管。”从该申请文件中公开的具体结构可以知晓其具体工作原理为：液体通过进液管切向进入微米气泡发生器内，超高速旋转并切割气体，使气体气泡破碎成微米级别的微气泡，从而提高液相与气相之间的传质面积，而且该专利中的微米气泡发生器属于气动式微界面发生器。
另外，在先专利201610641251.7中有记载一次气泡破碎器具有循环液进 口、循环气进口和气液混合物出口，二次气泡破碎器则是将进料口与气液混合物出口连通，说明气泡破碎器都是需要气液混合进入，另外从后面的附图中可知，一次气泡破碎器主要是利用循环液作为动力，所以其实一次气泡破碎器属于液动式微界面发生器，二次气泡破碎器是将气液混合物同时通入到椭圆形的旋转球中进行旋转，从而在旋转的过程中实现气泡破碎，所以二次气泡破碎器实际上是属于气液联动式微界面发生器。其实，无论是液动式微界面发生器，还是气液联动式微界面发生器，都属于微界面发生器的一种具体形式，然而本发明所采用的微界面发生器并不局限于上述几种形式，在先专利中所记载的气泡破碎器的具体结构只是本发明微界面发生器可采用的其中一种形式而已。此外，在先专利201710766435.0中记载到“气泡破碎器的原理就是高速射流以达到气体相互碰撞”，并且也阐述了其可以用于微界面强化反应器，验证本身气泡破碎器与微界面发生器之间的关联性；而且在先专利CN106187660中对于气泡破碎器的具体结构也有相关的记载，具体见说明书中第[0031]-[0041]段，以及附图部分，其对气泡破碎器S-2的具体工作原理有详细的阐述，气泡破碎器顶部是液相进口，侧面是气相进口，通过从顶部进来的液相提供卷吸动力，从而达到粉碎成超细气泡的效果，附图中也可见气泡破碎器呈锥形的结构，上部的直径比下部的直径要大，也是为了液相能够更好的提供卷吸动力。由于在先专利申请的初期，微界面发生器才刚研发出来，所以早期命名为微米气泡发生器(CN201610641119.6)、气泡破碎器(201710766435.0)等，随着不断技术改进，后期更名为微界面发生器，现在本发明中的微界面发生器相当于之前的微米气泡发生器、气泡破碎器等，只是名称不一样。
综上所述，本发明的微界面发生器属于现有技术，虽然有的气泡破碎器属于气动式气泡破碎器类型，有的气泡破碎器属于液动式气泡破碎器类型，还有的属于气液联动式气泡破碎器类型，但是类型之间的差别主要是根据具体工况的不同进行选择，另外关于微界面发生器与反应器、以及其他设备的连接，包括连接结构、连接位置，根据微界面发生器的结构而定，此不作限定。
优选的，所述蒸发塔连接有脱水塔，从所述蒸发塔底部出来的物料经第三再沸器分成气液两股物流，气相物流循环返回所述蒸发塔中，液相物流进入所述脱水塔中进行进一步分离纯化。进一步的，所述脱水塔连接有精制塔，以用于将从所述脱水塔中排出的物料进行进一步精制纯化。经过纯化，能够去除乙二醇产物中混杂的水，提高产物纯度。
优选的，所述精制塔连接有产物储存罐，经所述精制塔精制后的产物流至所述产物储存罐储存。
优选的，所述水合反应精馏器和强化水合反应精馏器顶部均设置有加剂通道以用于添加催化剂。
优选的，所述水合反应精馏器顶部连接有第一冷凝器，未反应的水和环氧乙烷经所述第一冷凝器冷凝后，回流至所述水合反应精馏器中。
优选的，所述强化水合反应精馏器顶部设置有第二冷凝器，所述第二冷凝器能够将强化水合反应精馏器中未反应的环氧乙烷气体冷凝回流至强化水合反应精馏器中。
优选的，所述精制塔顶部连接有第三冷凝器，所述精制塔顶部的气相组分经所述第三冷凝器冷凝后，回流至所述精制塔顶部。精制塔顶部全回流，气态的乙二醇经第三冷凝器冷凝为液相，经回流管线返回精制塔中。
本发明还提供了一种应用上述的气相催化水合法制备乙二醇的强化反应系统的反应方法，包括如下步骤：
将环氧乙烷和水混合后经微界面分散破碎后进行催化水合反应，再进行分离纯化精制后得到乙二醇；催化水合反应的温度为150-165℃，压力为0.5-0.8MPa。
优选的，所述催化水合反应的催化剂为碳酸钾、碳酸氢钾、过氯酸铝和三氟甲基磺酸铝中的任意一种或几种的混合。
具体地，该制备方法通过在水合反应精馏器内部设置与环氧乙烷进口相连 接的气动式微界面发生器和第一液动式微界面发生器，使得在环氧乙烷和原料水进行水合反应之前，破碎成直径为大于等于1μm、小于1mm的微气泡，使得环氧乙烷以微气泡的状态与水接触，以增大水合反应过程中环氧乙烷和水之间的相界传质面积，并进行充分混合再进行水合反应，从而减少了反应需要的水和催化剂的量，提高了反应效率。
采用本发明的反应方法得到的乙二醇产品品质好、收率高。且该制备方法本身反应温度低、压力大幅度下降，成本显著降低。
与现有技术相比，本发明的有益效果在于：
(1)本发明的气相催化水合法制备乙二醇的强化反应系统通过设置水合反应精馏器以及与之串联的强化水合反应精馏器，有效保证了环氧乙烷和水充分反应；
(2)通过在水合反应精馏器内部设置气动式微界面发生器和第一液动式微界面发生器以及在强化水合反应精馏器内部设置第二水合反应精馏器，使得在环氧乙烷与水进行催化水合反应之前将环氧乙烷破碎为微气泡，提高环氧乙烷与水之间的相界传质面积，提高了反应效率，催化剂的添加量减少，能源消耗少，生产成本低；
(3)本发明的反应方法操作简便，反应得到的乙二醇纯度高，应用广泛，提高了乙二醇本身的适用面，值得广泛推广应用。
通过阅读下文优选实施方式的详细描述，各种其他的优点和益处对于本领域普通技术人员将变得清楚明了。附图仅用于示出优选实施方式的目的，而并不认为是对本发明的限制。而且在整个附图中，用相同的参考符号表示相同的部件。在附图中：
图1为本发明实施例提供的气相催化水合法制备乙二醇的强化反应系统的结构示意图。
其中：
10-水合反应精馏器； 101-加剂通道；
102-第一液动式微界面发生器； 103-导向圆盘；
104-环氧乙烷进口； 105-气动式微界面发生器；
106-进水口； 107-第一冷凝器；
108-第一再沸器； 109-物料出口；
20-强化水合反应精馏器； 201-第二液动式微界面发生器；
202-筛网； 203-乙二醇出口；
204-第二再沸器； 205-第二冷凝器；
30-蒸发塔； 301-第三再沸器；
40-脱水塔； 401-第四再沸器；
50-精制塔； 501-第三冷凝器；
502-第五再沸器； 60-产物储存罐；
70-环氧乙烷储罐； 80-水储罐；
90-水泵。
下面将结合附图和具体实施方式对本发明的技术方案进行清楚、完整地描述，但是本领域技术人员将会理解，下列所描述的实施例是本发明一部分实施例，而不是全部的实施例，仅用于说明本发明，而不应视为限制本发明的范围。基于本发明中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例，都属于本发明保护的范围。实施例中未注明具体条件者，按照常规条件或制造商建议的条件进行。所用试剂或仪器未注明生产厂商 者，均为可以通过市售购买获得的常规产品。
在本发明的描述中，需要说明的是，术语“中心”、“上”、“下”、“左”、“右”、“竖直”、“水平”、“内”、“外”等指示的方位或位置关系为基于附图所示的方位或位置关系，仅是为了便于描述本发明和简化描述，而不是指示或暗示所指的装置或元件必须具有特定的方位、以特定的方位构造和操作，因此不能理解为对本发明的限制。此外，术语“第一”、“第二”、“第三”仅用于描述目的，而不能理解为指示或暗示相对重要性。
在本发明的描述中，需要说明的是，除非另有明确的规定和限定，术语“安装”、“相连”、“连接”应做广义理解，例如，可以是固定连接，也可以是可拆卸连接，或一体地连接；可以是机械连接，也可以是电连接；可以是直接相连，也可以通过中间媒介间接相连，可以是两个元件内部的连通。对于本领域的普通技术人员而言，可以具体情况理解上述术语在本发明中的具体含义。
为了更加清晰的对本发明中的技术方案进行阐述，下面以具体实施例的形式进行说明。
实施例
参阅图1所示，本实施例提供了一种气相催化水合法制备乙二醇的强化反应系统，包括：水合反应精馏器10、强化水合反应精馏器20和蒸发塔30；水合反应精馏器10的侧壁上设置有环氧乙烷进口104；水合反应精馏器10底部设置有进水口106；环氧乙烷进口104与环氧乙烷储罐70相连；进水口106与水储罐80相连，水储罐80与进水口106间设置有水泵90。
其中，水合反应精馏器10和强化水合反应精馏器20顶部均设置有加剂通道101以用于添加催化剂。水合反应精馏器10顶部还连接有第一冷凝器107，未反应的水和环氧乙烷经第一冷凝器107冷凝后，回流至水合反应精馏器10中。水合反应精馏器10内部设置有气动式微界面发生器105和第一液动式微 界面发生器102，气动式微界面发生器105设置在第一液动式微界面发生器102的下方；气动式微界面发生器105与第一液动式微界面发生器102均与环氧乙烷进口104相连以用于破碎环氧乙烷气体为微米级别的微气泡；具体的，水合反应精馏器10中的气动式微界面发生器105与第一液动式微界面发生器102的出口相对设置，且气动式微界面发生器105与第一液动式微界面发生器102的出口均设置有导向圆盘103以用于使产生的微气泡均匀分布。
导向圆盘103呈锥形；导向圆盘103上均匀分布有多个导向孔。进一步的，导向圆盘103的导向曲线为双曲线、抛物线、两段折线和对数曲线中的任意一种。
强化水合反应精馏器20内部设置有第二液动式微界面发生器201；第二液动式微界面发生器201的出口处设置有用于将产生的微气泡均匀分布的筛网202。水合反应精馏器10底部设置有物料出口109；物料出口109连接有第一再沸器108；从物料出口109排出的物料通过第一再沸器108分成气液两股物流，气相物流通过第二液动式微界面发生器201进入强化水合反应精馏器20中，液相物流直接流入强化水合反应精馏器20中；
强化水合反应精馏器20底部设置有乙二醇出口203以用于产品乙二醇的排出，从乙二醇出口203排出的乙二醇经第二再沸器204分成气液两股物流，气相物流循环返回强化水合反应精馏器20中，液相物流流入蒸发塔30中进行气液分离。强化水合反应精馏器20底部设置有进液口以用于通入水。进液口与水储罐80相连。
另外，强化水合反应精馏器20顶部还设置有第二冷凝器205，第二冷凝器205能够将强化水合反应精馏器20中未反应的环氧乙烷气体冷凝回流至强化水合反应精馏器20中。
在本实施例中，蒸发塔30连接有脱水塔40，从蒸发塔30底部出来的物料经第三再沸器301分成气液两股物流，气相物流循环返回蒸发塔30中，液相物流进入脱水塔40中进行进一步分离纯化。进一步的，脱水塔40连接有精制 塔50，以用于将从脱水塔40中排出的物料进行进一步精制纯化。经过纯化，能够去除乙二醇产物中混杂的水，提高产物纯度。精制塔50连接有产物储存罐60，经精制塔50精制后的产物流至产物储存罐60储存。
精制塔50顶部连接有第三冷凝器501，精制塔顶部的气相组分经第三冷凝器501冷凝后，回流至精制塔50顶部。精制塔50顶部全回流，气态的乙二醇经第三冷凝器501冷凝为液相，经回流管线返回精制塔中。
其中，脱水塔40与精制塔50间设置有第四再沸器401；精制塔50与产物储存罐60内设置有第五再沸器502。第四再沸器401与第五再沸器502将通过的物料部分气化，液相继续输出，气相回流，能够使物料进一步纯化。
另外，水合反应精馏器10顶部与第二再沸器204相连，强化水合反应精馏器20顶部与第三再沸器301相连，蒸发塔30顶部与第四再沸器401相连，脱水塔40顶部与第五再沸器502相连，这样能够将前一级的蒸汽用于下一级的再沸器热源，提高能量的利用效率。
具体反应过程中，将20g催化剂、200g环氧乙烷和600g水通入水合反应精馏器10中，加热水合反应精馏器10至150℃，水和反应器内压力设置为0.7MPa。环氧乙烷和水在水合反应精馏器10中进行反应，反应后的物料流入强化水合反应精馏器20中继续进行水合反应；产生的乙二醇从强化水合反应精馏器20中流出后经蒸发塔30和脱水塔40脱水处理后，在精制塔50中精制纯化，纯化后的乙二醇输出至产物储存罐60中。
总之，与现有技术的气相催化水合法制备乙二醇的反应系统相比，本发明的强化反应系统设备组件少、占地面积小、能耗低、成本低、安全性高、反应可控，原料转化率高，相当于为乙二醇制备领域提供了一种操作性更强的反应系统，值得广泛推广应用。
最后应说明的是：以上各实施例仅用以说明本发明的技术方案，而非对其限制；尽管参照前述各实施例对本发明进行了详细的说明，本领域的普通技术人员应当理解：其依然可以对前述各实施例所记载的技术方案进行修改，或者 对其中部分或者全部技术特征进行等同替换；而这些修改或者替换，并不使相应技术方案的本质脱离本发明各实施例技术方案的范围。
Claims (10)
- 一种气相催化水合法制备乙二醇的强化反应系统，其特征在于，包括：水合反应精馏器、强化水合反应精馏器和蒸发塔；所述水合反应精馏器的侧壁上设置有环氧乙烷进口；所述水合反应精馏器底部设置有进水口；所述水合反应精馏器内部设置有气动式微界面发生器和第一液动式微界面发生器，所述气动式微界面发生器设置在所述第一液动式微界面发生器的下方；所述气动式微界面发生器与所述第一液动式微界面发生器均与所述环氧乙烷进口相连以用于破碎环氧乙烷气体为微米级别的微气泡；所述强化水合反应精馏器内部设置有第二液动式微界面发生器；所述水合反应精馏器底部设置有物料出口；所述物料出口连接有第一再沸器；从所述物料出口排出的物料通过所述第一再沸器分成气液两股物流，气相物流通过所述第二液动式微界面发生器进入所述强化水合反应精馏器中，液相物流直接流入所述强化水合反应精馏器中；所述强化水合反应精馏器底部设置有乙二醇出口以用于产品乙二醇的排出，从所述乙二醇出口排出的乙二醇经第二再沸器分成气液两股物流，气相物流循环返回所述强化水合反应精馏器中，液相物流流入所述蒸发塔中进行气液分离。
- 根据权利要求1所述的气相催化水合法制备乙二醇的强化反应系统，其特征在于，所述水合反应精馏器中的所述气动式微界面发生器与所述第一液动式微界面发生器的出口相对设置，且所述气动式微界面发生器与所述第一液动式微界面发生器的出口均设置有导向圆盘以用于使产生的微气泡均匀分布。
- 根据权利要求2所述的气相催化水合法制备乙二醇的强化反应系统，其特征在于，所述导向圆盘呈锥形；所述导向圆盘上均匀分布有多个导向孔。
- 根据权利要求1所述的气相催化水合法制备乙二醇的强化反应系统，其特征在于，所述强化水合反应精馏器内部的所述第二液动式微界面发生器的出口处设置有用于将产生的微气泡均匀分布的筛网。
- 根据权利要求1所述的气相催化水合法制备乙二醇的强化反应系统，其特征在于，所述强化水合反应精馏器底部设置有进液口以用于通入水。
- 根据权利要求1所述的气相催化水合法制备乙二醇的强化反应系统，其特征在于，所述蒸发塔连接有脱水塔，从所述蒸发塔底部出来的物料经第三再沸器分成气液两股物流，气相物流循环返回所述蒸发塔中，液相物流进入所述脱水塔中进行进一步分离纯化。
- 根据权利要求5所述的气相催化水合法制备乙二醇的强化反应系统，其特征在于，所述脱水塔连接有精制塔，以用于将从所述脱水塔中排出的物料进行进一步精制纯化。
- 根据权利要求6所述的气相催化水合法制备乙二醇的强化反应系统，其特征在于，所述精制塔连接有产物储存罐，经所述精制塔精制后的产物流至所述产物储存罐储存。
- 采用权利要求1-8任一项所述的气相催化水合法制备乙二醇的强化反应系统的反应方法，其特征在于，包括如下步骤：将环氧乙烷和水混合后经微界面分散破碎后进行催化水合反应，再进行分离纯化精制后得到乙二醇；催化水合反应的温度为150-165℃，压力为0.5-0.8MPa。
- 根据权利要求9所述的反应方法，其特征在于，所述催化水合反应的催化剂为碳酸钾、碳酸氢钾、过氯酸铝和三氟甲基磺酸铝中的任意一种或几种的混合。
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