CN104355966A - Optimized reaction technology producing ethylene-glycol by adding hydrogen in oxalate - Google Patents
Optimized reaction technology producing ethylene-glycol by adding hydrogen in oxalate Download PDFInfo
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- CN104355966A CN104355966A CN201410616912.1A CN201410616912A CN104355966A CN 104355966 A CN104355966 A CN 104355966A CN 201410616912 A CN201410616912 A CN 201410616912A CN 104355966 A CN104355966 A CN 104355966A
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- 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
- C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
- C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
- C07C29/147—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof
- C07C29/149—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
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- 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
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- 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
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to the field of chemical engineering, and relates to a production technology for ethylene-glycol, in particular to an optimized reaction technology producing ethylene-glycol by adding hydrogen in oxalate. The technology comprises the following steps: adding a raw material oxalate in a vaporization tower directly first; circulating the oxalate in the tower; enabling the oxalate and heated circulating gas in the tower to conduct continuous gas-liquid contact; gradually increasing temperature to a vaporization temperature; taking the oxalate after vaporization and the circulating gas as reaction gas for preheating; pumping the oxalate and the circulating gas in a reactor; heating reaction gas by the product gas after reaction; generating vapor as a byproduct by surplus heat after temperature reduction; reducing the temperature to the temperature required by the inlet of a circulating compressor through air cooling or water cooling. Through the adoption of the technology, equipment investment can be reduced effectively; energy consumption and cost are reduced.
Description
Technical field
The invention belongs to chemical field, relate to the production technique of ethylene glycol, be specially a kind of hydrogenation of oxalate for preparing ethylene glycol and optimize reaction process.
Background technology
Ethylene glycol (EG) is a kind of important basic chemical industry raw material, can be used for producing unsaturated polyester resin, trevira, coating, frostproofer, softening agent, nonionogenic tenside etc.China is that the first big country consumed by ethylene glycol, but the degree of self-sufficiency is less than 30%, and most of producer all adopts external oil ethene route technology, the reaction product water content that the method obtains is high, subsequent processing device complex process, long flow path, energy consumption is high, and the price of oil and derived product thereof has a strong impact on production cost, along with the scarcity day by day of petroleum resources, this route will be faced with formidable challenges.
The many coals of few oil according to the national conditions of China, therefore be restricted with petroleum path synthesizing glycol operational path, but development is raw material with coal, the advantage of rich coal resources in China can be given full play to by this intermediate product of CO gas phase coupling synthesis of oxalate and then Hydrogenation for ethylene glycol route, the advantage of competing mutually with conventional petroleum route can be possessed.Simultaneously China is the first phosphorus production big country in the world, containing abundant CO(90.7% in yellow phosphoric tail gas), therefore Appropriate application yellow phosphoric tail gas can effectively reduce ethylene glycol production cost, reduces exhaust gas emission, is conducive to Appropriate application and the environment protection of resource.
Technique report about hydrogenation of oxalate for preparing ethylene glycol is more, a kind of energy-saving ester through hydrogenation technique CN201310393262.4, openly report use and first evaporate post-heating flow process, the supplementary view of reasonable employing fresh hydrogen, adopt high-efficiency evaporating tower and highly effective hydrogenation reactor, reduce investment and energy consumption.This technique uses shell and tube isothermal reactor, utilizes drum to control temperature of reaction, and patent of the present invention adopts adiabatic reactor and foregoing invention to have the difference of essence.CN201010587850.8 reports a kind of technique adopting the preparing glycol through oxalate hydrogenation of adiabatic reaction system, and utilizes reaction heat reacting by heating material to realize energy-conservation object.But this technique is considered not enough to the comprehensive energy consumption of whole hydrogenation flow process.It is that raw material is by controlling each temperature out in reaction process with barkite that a kind of energy-efficient reaction process CN201010601259.3 of hydrogenation of oxalate for preparing ethylene glycol has openly reported, only reaction product in reaction cycle loop and the liquefaction of unreacted barkite are separated and send into rectification working process, and hydrogen and alkyl alcohol remain in circulation gas, make full use of reaction heat and increase circulation gas temperature, reduce energy consumption.But this process heat utilizes still incomplete, the thermal load entering air cooler is large, and energy consumption increases, and the preheating of barkite needs to use independent heating installation, increases facility investment.
Summary of the invention
The object of the invention is to, for above technical problem, provide and effectively can reduce facility investment, save energy consumption, a kind of hydrogenation of oxalate for preparing ethylene glycol reduced costs optimizes reaction process.
The object of the invention is realized by following technical proposals:
A kind of hydrogenation of oxalate for preparing ethylene glycol optimizes reaction process, this technique is: raw material barkite is directly entered vaporization tower, at tower internal recycle, with by the continuous gas-to-liquid contact of circulation gas heated, be warmed up to vaporization temperature gradually, the barkite after vaporization enters reactor as reaction gas through preheating together with circulation gas, reacted gas product reacting by heating gas, heat byproduct steam more more than needed after cooling, the temperature finally required by air cooling or water-cooled to recycle compressor entrance.
Described vaporization tower adopts gas-liquid material and stream mode enters tower, avoids the generation of liquid flooding, reduces the tower diameter of vaporization tower, saved cost of equipment.The hot heating raw barkite utilizing circulation gas to obtain, makes it to vaporize in vaporization tower, without the need to additional heating plant.
The preheating of recycle gas, the preheating of reaction gas is all utilize outlet high-temperature material heat exchange and exothermic heat of reaction to realize, and utilizes excess of heat byproduct steam, the steam consumption of other devices of supply.
Utilize circulation gas cooling temperature to control the amount of saturated alkyl alcohol in gas phase, the alkyl alcohol in the air inlet of guarantee reactor and the charge ratio of raw material barkite.
Hydrogenation of oxalate for preparing ethylene glycol optimizes reaction process, and these technique concrete steps are: first in the middle part of hydrogenator, load Cu/SiO
2catalyzer, and equigranular filler with catalyzer is housed at reactor two ends, take oxalic acid diethyl ester as raw material, under certain temperature and reaction pressure, fills into hydrogen, enters after making it to mix with circulation gas after interchanger heat exchange from vaporization tower tower top, pump into vaporization tower top after the raw material oxalic acid diethyl ester that system fills into and the barkite that circulates of vaporization tower reactor mix, flow into vaporization tower vaporize with gas mixture, after interchanger heat exchange, adiabatic reactor is entered again through vaporization tower gas mixture out, reaction feed material after preheater preheats is lowered the temperature, Btu utilization byproduct steam is continued again through waste heat boiler, again after interchanger heat exchange by circulating hydrogen preheating, reduce through Btu utilization after product temperature degree, the mix products of gas-liquid two-phase enters rough segmentation tower together, air cooler is equivalent to overhead condenser, in rough segmentation tower, the liquid phase material that gaseous phase materials and the overhead condensation of continuous rising get off carries out vapour-liquid mass and realizes being separated, overhead vapours enters air cooler, control the cooling temperature of outlet, cooled mixed phase carries out gas-liquid separation in knockout drum, liquid-phase product backflow enters rough segmentation tower, gaseous products by analysis in controlled circulation gas the content of hydrogen component determine to discharge tolerance.
The hot heating raw barkite utilizing circulation gas to obtain, makes it to vaporize in vaporization tower, without the need to additional heating plant, saves facility investment.
The preheating of recycle gas, the preheating of reaction gas is all utilize outlet high-temperature material heat exchange and exothermic heat of reaction to realize, heat integration is considered, utilize rationally, both the consumption of steam needed for reacting by heating gas had been decreased, again reduce the thermal load of the cold needed for chilled product gas as air cooler or the consumption of recirculated cooling water, the excess of heat also can byproduct steam, the steam consumption of other devices of supply.
Its reaction can show as:
Main reaction (COOC
2h
5)
2+ 4 H
2→ (CH
2oH)
2+ 2 C
2h
5oH
Side reaction (1) (COOC
2h
5)
2+ 5 H
2→ 3 C
2h
5oH+H
2o
（2） (COOC
2H
5)
2+ 3 H
2→CH
3COOC
2H
5+ C
2H
5OH + H
2O
Compared with prior art, beneficial effect of the present invention is:
(1) vaporization of raw material barkite utilizes the gaseous phase partial pressure of a large amount of circulation gas reduce hold-up vapour pressure thus reduce vaporization temperature, direct boiling is under a certain pressure avoided to increase power consumption, barkite adopts components vaporize, guarantee the material purity entering reactor, the liquid starting material interval discharge system of not vaporizing.In the present invention, recycle stock is mainly the part resultant alkyl alcohol saturated in circulation gas that excess hydrogen, rare gas element gas nitrogen or the argon gas etc. that add in reaction and conventional condensation device can not cool down completely, wherein in alkyl alcohol, alkyl substituent is identical with the alkyl carbon content in barkite, it is such as raw material with oxalic acid diethyl ester, generate ethanol, take dimethyl oxalate as raw material, methanol.
(2) in the device normal cycle of operation, barkite is from front rectification working process, and temperature can directly meet the bubble point temperature after contacting with the circulation gas of certain temperature, can direct boiling.But start-up, raw material barkite is from outside battery limit (BL), temperature is generally room temperature, contact could vaporize with circulation gas after needing to absorb heat to certain temperature, the heat of start-up heating cycle gas of the present invention, from the well heater that goes into operation used during catalyst reduction, is passed to barkite by the circulation gas heated by circulation, is made it to reach certain temperature in vaporization tower, this method can save the interchanger of heating barkite separately, saves facility investment.
(3) gas-phase feed of vaporization tower and liquid phase feeding adopt and stream mode enters from tower top, avoid and adopt conventional liquid phase to spray from tower top, the Concerning Flooding Phenomenon that the backward feed mode that gas phase enters from tower reactor produces.The effect of vaporization tower filler is just conducive to being uniformly distributed of liquid phase material, increase gasifying surface, do not relate to mass transfer separation efficiency problem, therefore number of theoretical plate not requirement, there is certain gas-liquid mass transfer space, and there is not Concerning Flooding Phenomenon because liquid phase also flows, therefore tower diameter does not need increase along with load and increase, and therefore this feeding manner significantly can reduce the investment of device.
(4) combination of rough segmentation tower and condenser is the simple separation device only having the rectifying section not section of profit reduction and reserving, because gas-phase product thermal loads a large amount of in charging is enough to the outer supplying heat source of alternative tower reactor reboiler, rough segmentation tower serves certain mass transfer centrifugation to a certain amount of ethanol and water, the material composition of exported product gas is controlled, mainly the content of saturated alkyl alcohol in controlled circulation gas by overhead condenser temperature out.
(5) waste heat boiler utilizes the gas product excess of heat can produce low-grade steam, reduces the thermal load of follow up device air cooler or water cooler simultaneously.The steam produced also can be warmed oneself etc. for other devices outside device or factory for production barkite process portion device.
Accompanying drawing explanation
Fig. 1 is process flow diagram of the present invention;
Wherein E101-102 is interchanger, and E103 is waste heat boiler, and E104 is air cooler, and T101 is vaporization tower, and T102 is rough segmentation tower, and R101 is hydrogenator, and P101 is liquid feed pump, V101 knockout drum, and 1 ~ 17 is pipeline, and C101 is recycle compressor.
Embodiment
Arbitrary feature disclosed in this specification sheets (comprising any accessory claim, summary), unless specifically stated otherwise, all can be replaced by other equivalences or the alternative features with similar object.That is, unless specifically stated otherwise, each feature is an example in a series of equivalence or similar characteristics.
Embodiment 1:
The Cu/SiO of 4 L is loaded in the middle part of hydrogenator
2catalyzer, it, as porcelain ring, take oxalic acid diethyl ester as raw material that equigranular filler with catalyzer is equipped with at reactor two ends, the temperature of hydrogenation reaction 220 DEG C, and reaction pressure is 3.0 MPa(gauge pressures).
System fills into hydrogen 1 flow 1.3 Nm
3/ h, temperature 60 C, pressure 3.2MPa, after mixing with circulation gas, 2 reach 139 DEG C through E101 heat exchange, enter from T101 vaporization tower tower top.
The raw material oxalic acid diethyl ester 4 flow 2kg/h that system fills into, pressure 3.05MPa, temperature 139.0 DEG C, mixes afterwards with the barkite that circulate of vaporization tower reactor and gas mixture flow into vaporizer and gasify.
Through vaporizer gas mixture 6 flow 42.5Nm out
3/ h, temperature 141 DEG C, pressure 3.05MPa, mole consists of: 86.3% hydrogen, 9.45% nitrogen, 0.06% ethyl acetate, 3.29% ethanol, 0.18% water, 0.72% barkite, temperature of reaction 220 DEG C is reached again through E102 heat exchange, pressure 3.0MPa enters adiabatic reactor R101, and the transformation efficiency measuring raw material barkite by analysis reaches 100%, and exit gas 8 moles consists of: 84.61% hydrogen, 9.58% nitrogen, 0.06% ethyl acetate, 4.84% ethanol, 0.26% water, 0.65% ethylene glycol, gas flow 42.3 Nm
3/ h, temperature 247 DEG C, pressure 2.94MPa, after E102 preheating reaction feed material 7, temperature is down to 167 DEG C, continue Btu utilization through E103 waste heat boiler again and can be about 0.44kg/h by by-product 0.3MPa steam, product gas 10 temperature drops to 148 DEG C, circulating hydrogen 2 can be preheating to 139.5 DEG C through E101 again, temperature through a series of Btu utilization after product gas 11 drops to 109.4 DEG C, gas-liquid two-phase, liquid-phase product quality accounts for 8.3% of total amount, gas-liquid two-phase enters T102 rough segmentation tower together, E104 air cooler is equivalent to overhead condenser, in rough segmentation tower, the liquid phase material that gaseous phase materials and the overhead condensation of continuous rising get off carries out vapour-liquid mass and realizes being separated to a certain degree.Overhead vapours 12 enters air cooler and controls outlet 13 cooling temperature 80 DEG C.Cooled mixed phase carries out gas-liquid separation in V101, and liquid-phase product 16 backflow enters rough segmentation tower, gaseous products 14 by analysis in controlled circulation gas the content of hydrogen component determine to discharge tolerance.All the other are by recycle compressor Returning reacting system, and circulation gas mole consists of: 89.12% hydrogen, 10.08% nitrogen, 0.02% ethyl acetate, 0.73% ethanol, 0.05% water.Liquid-phase product 17 goes subsequent product to refine.
Embodiment 2:
The Cu/SiO of 4 L is loaded in the middle part of hydrogenator
2catalyzer, it, as porcelain ring, take oxalic acid diethyl ester as raw material that equigranular filler with catalyzer is equipped with at reactor two ends, the temperature of hydrogenation reaction 210 DEG C, and reaction pressure is 2.51MPa(gauge pressure).
System fills into hydrogen 1 flow 1.27 Nm
3/ h, temperature 83 DEG C, pressure 2.53MPa, after mixing with circulation gas, 2 reach 140.0 DEG C through E101 heat exchange, enter from T101 vaporization tower tower top.
The raw material oxalic acid diethyl ester 4 flow 2.0kg/h that system fills into, pressure 2.53MPa, temperature 140.0 DEG C, mix afterwards 5 and gas mixture 3 flow into vaporization tower and vaporize with the barkite that circulate of vaporization tower reactor.
Through vaporization tower gas mixture 6 flow 42.4Nm out
3/ h, temperature 138.4 DEG C, pressure 2.52MPa, mole consists of: 74.9% hydrogen, 21.3% nitrogen, 2.9% ethanol, 0.1% water, 0.7% barkite, all the other are other, then reach temperature of reaction 210 DEG C through E102 heat exchange, pressure 2.51MPa enters adiabatic reactor R101, and the transformation efficiency measuring raw material barkite by analysis reaches 100%, and exit gas 8 moles consists of: 73.2% hydrogen, 21.6% nitrogen, 4.4% ethanol, 0.1% water, 0.7% ethylene glycol, all the other are other, gas flow 41.8 Nm
3/ h, temperature 236.4 DEG C, pressure 2.48MPa, after E102 preheating reaction feed material 7, temperature is down to 164.4 DEG C, continuing Btu utilization through E103 waste heat boiler again can by-product 0.28MPa(gauge pressure) steam is about 0.47kg/h, product gas 10 temperature drops to 148.0 DEG C, circulating hydrogen 2 can be preheating to 140.0 DEG C through E101 again, temperature through a series of Btu utilization after product gas 11 drops to 104.0 DEG C, gas-liquid two-phase, liquid-phase product quality accounts for 9.0% of total amount, gas-liquid two-phase enters T102 rough segmentation tower together, overhead vapours 12 enters air cooler and controls outlet 13 cooling temperature 80 DEG C.Cooled mixed phase carries out gas-liquid separation in V101, liquid-phase product 16 backflow enters rough segmentation tower, gaseous products 14 by analysis in controlled circulation gas the content of hydrogen component determine to discharge tolerance, all the other are by recycle compressor Returning reacting system, circulation gas mole consists of: 74.4% hydrogen, 22.08% nitrogen, 3.4% ethanol, 0.1% water. all the other are other.Liquid-phase product 17 goes subsequent product to refine.
Claims (6)
1. a hydrogenation of oxalate for preparing ethylene glycol optimizes reaction process, it is characterized in that: raw material barkite is directly entered vaporization tower, at tower internal recycle, with by the continuous gas-to-liquid contact of circulation gas heated, be warmed up to vaporization temperature gradually, the barkite after vaporization enters reactor as reaction gas through preheating together with circulation gas, reacted gas product reacting by heating gas, heat byproduct steam more more than needed after cooling, the temperature finally required by air cooling or water-cooled to recycle compressor entrance.
2. hydrogenation of oxalate for preparing ethylene glycol according to claim 1 optimizes reaction process, it is characterized in that: described vaporization tower adopts gas-liquid material and stream mode enters tower, avoids the generation of liquid flooding, reduces the tower diameter of vaporization tower, saved cost of equipment.
3. hydrogenation of oxalate for preparing ethylene glycol according to claim 1 optimizes reaction process, it is characterized in that: the hot heating raw barkite utilizing circulation gas to obtain, makes it to vaporize in vaporization tower, without the need to additional heating plant.
4. hydrogenation of oxalate for preparing ethylene glycol according to claim 1 optimizes reaction process, it is characterized in that: the preheating of recycle gas, the preheating of reaction gas is all utilize outlet high-temperature material heat exchange and exothermic heat of reaction to realize, and utilizes excess of heat byproduct steam, the steam consumption of other devices of supply.
5. hydrogenation of oxalate for preparing ethylene glycol according to claim 3 optimizes reaction process, it is characterized in that: utilize circulation gas cooling temperature to control the amount of saturated alkyl alcohol in gas phase, the alkyl alcohol in the air inlet of guarantee reactor and the charge ratio of raw material barkite.
6. hydrogenation of oxalate for preparing ethylene glycol according to claim 1 optimizes reaction process, it is characterized in that: first in the middle part of hydrogenator, load Cu/SiO
2catalyzer, and equigranular filler with catalyzer is housed at reactor two ends, take oxalic acid diethyl ester as raw material, under certain temperature and reaction pressure, fills into hydrogen, enters after making it to mix with circulation gas after interchanger heat exchange from vaporization tower tower top, pump into vaporization tower top after the raw material oxalic acid diethyl ester that system fills into and the barkite that circulates of vaporization tower reactor mix, flow into vaporization tower vaporize with gas mixture, after interchanger heat exchange, adiabatic reactor is entered again through vaporization tower gas mixture out, the gas product of reactor outlet is first through preheater preheats reaction feed material, Btu utilization byproduct steam is continued again through waste heat boiler, after interchanger warm-up cycle hydrogen, temperature reduces again, the mix products forming gas-liquid two-phase enters rough segmentation tower together, air cooler is equivalent to overhead condenser, in rough segmentation tower, the liquid phase material that gaseous phase materials and the overhead condensation of continuous rising get off carries out vapour-liquid mass and realizes being separated, overhead vapours enters air cooler, control the cooling temperature of outlet, cooled mixed phase carries out gas-liquid separation in knockout drum, liquid-phase product backflow enters rough segmentation tower, gaseous products by analysis in controlled circulation gas the content of hydrogen component determine to discharge tolerance.
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|---|---|---|---|
| CN201410616912.1A CN104355966A (en) | 2014-11-06 | 2014-11-06 | Optimized reaction technology producing ethylene-glycol by adding hydrogen in oxalate |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107082741A (en) * | 2017-06-16 | 2017-08-22 | 四川天科技股份有限公司 | A kind of method of oxalate deep hydrogenation catalytic reaction synthesizing glycol |
| CN109422623A (en) * | 2017-08-20 | 2019-03-05 | 杭州林达化工技术工程有限公司 | A kind of energy-saving acetic acid adds the production technology and its device of hydrogen or ethyl acetate preparation of ethanol by hydrogenating |
| CN109482107A (en) * | 2018-11-30 | 2019-03-19 | 华东理工大学 | The gasification method and vapourizing unit of dimethyl oxalate |
| CN112759505A (en) * | 2019-10-21 | 2021-05-07 | 中国石油化工股份有限公司 | Method and system for preparing ethylene glycol |
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| CN102060664A (en) * | 2010-12-23 | 2011-05-18 | 西南化工研究设计院 | High-efficiency and energy-saving reaction process for preparing ethylene glycol through hydrogenation of oxalate |
| CN102086146A (en) * | 2010-12-15 | 2011-06-08 | 西南化工研究设计院 | Process for preparing glycol by oxalate hydrogenation in heat insulation reaction system |
-
2014
- 2014-11-06 CN CN201410616912.1A patent/CN104355966A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102086146A (en) * | 2010-12-15 | 2011-06-08 | 西南化工研究设计院 | Process for preparing glycol by oxalate hydrogenation in heat insulation reaction system |
| CN102060664A (en) * | 2010-12-23 | 2011-05-18 | 西南化工研究设计院 | High-efficiency and energy-saving reaction process for preparing ethylene glycol through hydrogenation of oxalate |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107082741A (en) * | 2017-06-16 | 2017-08-22 | 四川天科技股份有限公司 | A kind of method of oxalate deep hydrogenation catalytic reaction synthesizing glycol |
| CN107082741B (en) * | 2017-06-16 | 2021-01-26 | 西南化工研究设计院有限公司 | Method for synthesizing ethylene glycol through oxalate deep hydrogenation catalytic reaction |
| CN109422623A (en) * | 2017-08-20 | 2019-03-05 | 杭州林达化工技术工程有限公司 | A kind of energy-saving acetic acid adds the production technology and its device of hydrogen or ethyl acetate preparation of ethanol by hydrogenating |
| CN109482107A (en) * | 2018-11-30 | 2019-03-19 | 华东理工大学 | The gasification method and vapourizing unit of dimethyl oxalate |
| CN112759505A (en) * | 2019-10-21 | 2021-05-07 | 中国石油化工股份有限公司 | Method and system for preparing ethylene glycol |
| CN112759505B (en) * | 2019-10-21 | 2024-01-30 | 中国石油化工股份有限公司 | Method and system for preparing ethylene glycol |
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