CN102060664A - High-efficiency and energy-saving reaction process for preparing ethylene glycol through hydrogenation of oxalate - Google Patents
High-efficiency and energy-saving reaction process for preparing ethylene glycol through hydrogenation of oxalate Download PDFInfo
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- CN102060664A CN102060664A CN 201010601259 CN201010601259A CN102060664A CN 102060664 A CN102060664 A CN 102060664A CN 201010601259 CN201010601259 CN 201010601259 CN 201010601259 A CN201010601259 A CN 201010601259A CN 102060664 A CN102060664 A CN 102060664A
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- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 title claims abstract description 84
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 33
- 238000005984 hydrogenation reaction Methods 0.000 title abstract description 8
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 title abstract description 6
- 239000007789 gas Substances 0.000 claims abstract description 47
- 238000000034 method Methods 0.000 claims abstract description 23
- 239000001257 hydrogen Substances 0.000 claims abstract description 14
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 14
- 239000002994 raw material Substances 0.000 claims abstract description 14
- 125000005233 alkylalcohol group Chemical group 0.000 claims abstract description 11
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 21
- WYACBZDAHNBPPB-UHFFFAOYSA-N diethyl oxalate Chemical compound CCOC(=O)C(=O)OCC WYACBZDAHNBPPB-UHFFFAOYSA-N 0.000 claims description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 14
- 238000004519 manufacturing process Methods 0.000 claims description 13
- 239000000463 material Substances 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 11
- 229910052757 nitrogen Inorganic materials 0.000 claims description 7
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 6
- 230000004087 circulation Effects 0.000 claims description 5
- 238000009833 condensation Methods 0.000 claims description 5
- 230000005494 condensation Effects 0.000 claims description 5
- 230000002411 adverse Effects 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 3
- 238000012546 transfer Methods 0.000 claims description 3
- LOMVENUNSWAXEN-UHFFFAOYSA-N Methyl oxalate Chemical compound COC(=O)C(=O)OC LOMVENUNSWAXEN-UHFFFAOYSA-N 0.000 claims description 2
- -1 alkyl carbon Chemical compound 0.000 claims description 2
- 238000001816 cooling Methods 0.000 claims description 2
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims 2
- 239000012071 phase Substances 0.000 claims 2
- 229910052786 argon Inorganic materials 0.000 claims 1
- 229910052799 carbon Inorganic materials 0.000 claims 1
- 239000007792 gaseous phase Substances 0.000 claims 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 1
- 238000012423 maintenance Methods 0.000 claims 1
- 238000004904 shortening Methods 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 9
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 8
- 238000010438 heat treatment Methods 0.000 abstract description 7
- 239000003054 catalyst Substances 0.000 abstract description 2
- 238000005265 energy consumption Methods 0.000 abstract description 2
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 15
- 230000008016 vaporization Effects 0.000 description 12
- 239000000203 mixture Substances 0.000 description 10
- 239000000047 product Substances 0.000 description 10
- 230000011218 segmentation Effects 0.000 description 10
- 238000009834 vaporization Methods 0.000 description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 10
- 229960004756 ethanol Drugs 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- 239000006227 byproduct Substances 0.000 description 5
- 150000002431 hydrogen Chemical class 0.000 description 5
- 239000000498 cooling water Substances 0.000 description 4
- 230000009466 transformation Effects 0.000 description 4
- 239000003245 coal Substances 0.000 description 3
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 3
- 239000003208 petroleum Substances 0.000 description 3
- 239000006200 vaporizer Substances 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 229960000935 dehydrated alcohol Drugs 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- 230000002194 synthesizing effect Effects 0.000 description 2
- 229910017813 Cu—Cr Inorganic materials 0.000 description 1
- 241000282326 Felis catus Species 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 239000004902 Softening Agent Substances 0.000 description 1
- 229920004935 Trevira® Polymers 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000005502 peroxidation Methods 0.000 description 1
- 238000005120 petroleum cracking Methods 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 238000011020 pilot scale process Methods 0.000 description 1
- 229920000728 polyester Polymers 0.000 description 1
- 229910052573 porcelain Inorganic materials 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 230000001839 systemic circulation Effects 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
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Abstract
The invention discloses a reaction process for preparing ethylene glycol from oxalate serving as a raw material through hydrogenation in the presence of a catalyst. In the process, only a reaction product and unreacted oxalate in a reaction recycle loop are liquefied and separated by controlling each exit temperature in the reaction process, and fed into a rectification process; and hydrogen and alkyl alcohol required by a reaction cycle are always kept in a gas state and remained in recycle gas, boosted by a recycle blower and returned to a reactor. By the process, reaction heat is fully utilized, so that the temperature of the recycle gas can be increased, and heating energy consumption is reduced.
Description
Technical field
The present invention relates to the production of ethylene glycol, further relate to a kind of technical process, belong to chemical technology field by barkite gas phase hydrogenation synthesizing glycol.
Background technology
China is ethylene glycol (EG) consumption first big country, by the end of 2009 the end of the year China's ethylene glycol manufacturer be 13 families, overall throughput is 243.8 ten thousand tons/year, and import volume in 2009 has reached 582.8 ten thousand tons, degree of self-sufficiency less than 30%.Ethylene glycol can be used for producing trevira, frostproofer, softening agent, nonionogenic tenside etc., and China's ethylene glycol is mainly used in the producd fibers polyester, accounts for aggregate consumption 93.7%.In the domestic manufacturer except that Tongliao Jinmei Chemical Co., Ltd adopts Coal Chemical Industry route technology, other producer all adopts external oil ethene route technology, be that the ethene that petroleum cracking produces obtains oxyethane through peroxidation, then oxyethane and water are made into mixed aqueous solution by a certain percentage, under certain temperature and pressure condition, are converted into ethylene glycol.The production cost of this route depends critically upon the price of oil and derived product thereof, the reaction product water content height that obtains of this method simultaneously, and the subsequent processing device complex process, long flow path, the energy consumption height directly influences the production cost of ethylene glycol.
China is the country of few oily many coals, the national conditions that petroleum resources are deficient have relatively limited with petroleum synthesizing glycol operational path, therefore development is a raw material with coal, can give full play to the advantage of rich coal resources in China by CO through barkite intermediate product hydrogenation preparing ethylene glycol, can possess the advantage of competing mutually with traditional petroleum path.Simultaneously China is the first phosphorus production big country in the world, contains abundant CO(90.7% in the yellow phosphoric tail gas), therefore rationally utilize yellow phosphoric tail gas can effectively reduce the ethylene glycol production cost, and help environment protection.
From the achievement in research of open report, at present on the hydrogenation of oxalate for preparing ethylene glycol technology tend to adopt Cu-SiO more
2Catalyzer replaces early stage Cu-Cr catalyzer, because the Cr element all has greatly harm to human body and environment.Reaction mesoxalic acid ester conversion rate can reach 100%, and glycol selectivity can reach more than 90%.And take place in order effectively to suppress side reaction, it is excessive greatly that hydrogen in reaction needs, add corresponding alkyl alcohol dilution barkite simultaneously (as being that raw material dilutes with methyl alcohol with the dimethyl oxalate, oxalic acid diethyl ester is the raw material alcohol dilution), the mol ratio of hydrogen and barkite is generally 10 ~ 300, and the mol ratio of alkyl alcohol and barkite is 2 ~ 20.In the production technique of routine, because a large amount of nonreactive materials (as alkyl alcohol) circulate in the reactive system circulation loop, reaction end gas need be cooled at least normal temperature makes just now and can coagulate components condense, utilize the separation of by-products of rectificating method again with alkyl alcohol and barkite, ethylene glycol and reaction, and then will need round-robin alkyl alcohol ratio on request to allocate into to carry out carburation by evaporation in the raw material barkite, round-robin hydrogen also reheats and enters reactor, does like this certainly will consume a large amount of heats and cause tremendous economic loss.
Summary of the invention
Goal of the invention of the present invention provides a kind of production technique of new hydrogenation of oxalate for preparing ethylene glycol, reduces reaction process, and saves water coolant and steam is used in heating, thereby conserve energy reduces cost.
This reaction solves the technical scheme that its technical problem adopted: mainly be included in the reaction process, temperature by the outlet of control rough segmentation tower, only reaction product in the reaction cycle loop and the liquefaction of unreacted barkite are separated, send into rectification working process then, and all remaining gaseous state, required hydrogen of reaction cycle and alkyl alcohol be retained in the circulation gas, and, make its Returning reactor by the recycle blower supercharging.In addition, the temperature out by control barkite vaporising device realizes the control to the barkite concentration in the mixed gas, simplifies production technique.
Find that by test of many times condensing equipment can adopt two kinds of forms in the technology of the present invention, a kind of is the combination of rectifying tower and horizontal condenser, and another kind is the vertical (type) condenser of gas and phlegma adverse current.When adopting the combination of rectifying tower and horizontal condenser, only need rectifying section, do not need stripping section and reboiler.And in order to reduce resistance, rectifying section preferably adopts corrugated-plate packed tower.At this moment, condenser is preferably selected fractional distillating tube for use, and material enters shell side, and dispersed phase holdup reaches the purpose of controlling Outlet Gas Temperature to regulate heat transfer area in the shell side by changing.If adopt vertical (type) condenser, two kinds of functions of rectifying and partial condensation are combined in the equipment, and material steam enters tube side by the bottom, and phlegma is drawn by the bottom, and the tail gas that does not coagulate is drawn at the top, and the type of cooling is the most handy air-cooled, by air quantity control Outlet Gas Temperature.
Compared with prior art, the invention has the beneficial effects as follows: reduced separation rectification step, simplified production technique, improved production efficiency, saved energy expenditure and reduced cost most of components in the reaction system.
Description of drawings
The present invention will be further described below in conjunction with the drawings and specific embodiments.
Fig. 1 is a process flow diagram of the present invention, and wherein 1 is interchanger, and 2 ~ 4 is preheater, 5 is partial condenser, 6 is vaporizer, and 7 is hydrogenator, and 8 are the rough segmentation tower, 9 is the barkite raw material storage tank, 10 ~ 11 is the highly pressurised liquid fresh feed pump, and 12 is temperature-sensing valve, and 13 is temperature sensor, 14 ~ 34 is pipeline, and 35 is recycle blower.
Embodiment
Below in conjunction with embodiment foregoing invention content of the present invention is described in further detail.But this should be interpreted as that the scope of the above-mentioned theme of the present invention only limits to following embodiment.Not breaking away under the above-mentioned technological thought situation of the present invention, according to ordinary skill knowledge and customary means, make various replacements and change, all should comprise within the scope of the invention.
Embodiment 1:
Below in conjunction with Fig. 1 embodiment is described.The Cu/SiO of 4 L packs at hydrogenator middle part
2Catalyzer, reactor two ends are equipped with and the equigranular porcelain ring of catalyzer, are raw material with the oxalic acid diethyl ester, and the reaction pressure of hydrogenation reaction is 1.5 MPa(gauge pressures).
Oxalic acid diethyl ester pumps into preheater 2 by highly pressurised liquid fresh feed pump 10, and wherein the inlet amount of oxalic acid diethyl ester is 3.65 kg/h, and the thermal response product generation heat exchange preheating with from pipeline 34 is heated to 108 at preheater 2 mesoxalic acid diethyl esters
oC.Enter the bottom of vaporizer 6 by pipeline 30 through the barkite after the preheating.(mol ratio of hydrogen and nitrogen was 4 in the gas mixture after required additional hydrogen mixed with recycled offgas in the reaction, nitrogen is carrier gas) enter interchanger 1 by pipeline 14, with the reaction end gas generation heat exchange from pipeline 19, gas mixture is heated to 166 in interchanger 1
oC enters vaporizer 6 by pipeline 15, and mixes with barkite from pipeline 30, and mixed gas flow is 38 m
3/ h.Dehydrated alcohol adds in initial reaction stage, treats that systemic circulation stops charging after stable, and keeping the mol ratio of dehydrated alcohol and oxalic acid diethyl ester in the reaction process is between 7.0 ~ 7.3.
In vaporization tower 6, the temperature in of gas mixture is 166
oC.After heat exchange, the vaporization of part oxalic acid diethyl ester is discharged by cat head with hydrogen, and the mixture after the oxalic acid diethyl ester that bottom temp is lower is vaporized 16 enters preheater 4 by the road.The oxalic acid diethyl ester of not vaporizing fully in the vaporization tower is flowed out by vaporization tower 6 bottoms, pump into preheater 3 by pipeline 31 through highly pressurised liquid fresh feed pump 11, after the steam heating vaporization, enter vaporization tower 6 tops and enter preheater 4 with the oxalic acid diethyl ester mixed gas of having vaporized.Tower 6 temperature outs of wherein vaporizing are controlled at 143
oC, because reaction pressure is certain, so temperature out just determined the composition of each material, hydrogen (massfraction) 10.2% wherein, nitrogen 35.9%, ethyl acetate 2.8%, ethanol 34.9%, oxalic acid diethyl ester 15.4%, other component 0.8% such as water.Enter preheater 4 again after reaction mixture gas is come out by vaporization tower 6 and further be heated to 182
oC.Heating back gas mixture enters reactor 7 and catalyzer contact reacts, the transformation efficiency of oxalic acid diethyl ester reaches 100% by analysis, each component of reactor outlet consists of (massfraction): hydrogen 9.3%, nitrogen 35.9%, ethyl acetate 3.0%, ethanol 44.5%, ethylene glycol 6.1%, other component 1.2% such as water.Because reaction is thermopositive reaction, the reactor outlet exhaust temperature is increased to 210
oC.The reaction end gas temperature reduces to 129
oC enters rough segmentation tower 8 to be separated, will be from the material mixed gas of pipeline 14 by 99
oC is heated to 166
oC, from the reaction raw materials gas mixture of pipeline 16 by 143
oC is heated to 182
oC.
After reaction end gas entered rough segmentation tower 8, control rough segmentation tower 8 top gas temperature outs were 106
oC, same because system pressure is constant, temperature determines the saturated vapor pressure of each material, also determine the material composition, wherein contained (massfraction) hydrogen 8.7%, nitrogen 33.5%, ethyl acetate 3.3%, ethanol 53.2%, ethylene glycol 0.02%, other material 1.3% such as water, because top exit gas still also has the ethylene glycol of minute quantity, a spot of ethylene glycol is present in the gas phase can influence catalyst life, and therefore necessary further condensing reflux gets off a spot of ethylene glycol total condensation.In rough segmentation tower 8, ethylene glycol and by product that reaction generates, and unreacted barkite raw material is condensate in the bottom, and take out through preheater 2 by pipeline 34.The gas that is come out by rough segmentation tower 8 tops enters partial condenser 5, the liquid that condensation is got off is back to the rough segmentation tower, gas is discharged by the partial condenser top, the key of this technology is the temperature of control partial condenser outlet simultaneously, thereby aperture control partial condenser 5 Outlet Gas Temperatures of controlling temperature-sensing valve 12 by temperature sensor 13 temperature sensors keep constant ratio and temperature, and partial condenser 5 Outlet Gas Temperatures are controlled at 93
oC wherein contains (massfraction) hydrogen 11.1%, nitrogen 42.7%, ethyl acetate 3.3%, ethanol 41.8%, water 0.5%, other component 0.6%.This gas mixture is being back to system response after recycle blower 34 boosts.And in rough segmentation tower 8 bottom liquids, contain (massfraction) ethyl acetate 1.5%, and ethanol 59.0%, water 0.7%, ethylene glycol 38.0%, other by product 0.8%, bottom expel liquid temperature is 116
oC, this part heat can be used for the heating raw oxalic acid diethyl ester, and rough segmentation tower bottom liquid effluent temperature reduces to 62 after preheater 2 heat exchange
oC takes out, and the raw material oxalic acid diethyl ester is heated to 108 simultaneously
oC sends into vaporization tower 6.Hydrogen and gaseous state alkyl alcohol return interchanger 1 preheating after being boosted by recycle blower 35 through pipeline 23 again, are back to the reactive system reaction then.
Transformation efficiency according to the analytical results oxalic acid diethyl ester is 100%, and the average selectivity of ethylene glycol is 93.8%.
In the prior art, reclaim ethanol and need rectifying.Ethanol rectifying tower overhead condenser loadQ
=m
*C
p* (T
2– T
1)+m * r, wherein m is the overhead product mass rate, kg h
-1C
pBe the overhead product specific heat capacity, kJ K
-1Kg
-1(looking into the related tool handbook); T
1The condenser inlet temperature, K; T
2Be condensator outlet temperature, K; R is product latent heat of vaporization kJ kg
-1(looking into the related tool handbook).The substitution related data gets Q=10092.0 kJ h
-1 , required cooling water inflow W Water =Q
/[C
p* (T
2– T
1)]=96 kg h
-1(T
2Cooling water outlet temperature 313 K; T
1Cooling water inlet temperature 298 K; C
pBe that specific heat of water holds), by product, need cooling water inflow to be about 61 kg/kg products.
Same, the material that rectifying need be come out with prior art production heats once more.In this process, be used for the reboiler Q=m that heats at the bottom of the rectifying tower 1* C
p* (T
2– T
1)+m
2* r, wherein
m 1There are not phase transformation quality product flow, kg h for entering reboiler
-1m
2For entering reboiler phase transformation quality product flow, kg h are arranged
-1C
pBe the mix product mean specific heat, kJ K
-1Kg
-1T
1The reboiler inlet temperature, K; T
2Be reboiler temperature out, K; R is mixing prod latent heat of vaporization kJ kg
-1The substitution related data gets Q
=9902.5 kJ h
-1,
Required180 kPa(absolute pressures) steam 4.48 kg h
-1,, need quantity of steam to be about 3 kg/kg products by product.Distillation ethanol selects for use the steam (corresponding vapour pressure 180 kPa) of 116 ° of C to heat.
The calculating here is by 3.65 kg h among the embodiment 1
-1The production capacity of raw material inlet amount (being equivalent to produce per year the pilot scale of 11 tons of ethylene glycol) calculate.
Because do not need in the flow process of the present invention in the aforementioned calculation rectifying and with the step of reboiler heating, so the energy that can save of the present invention and quantity of steam rectifying of equaling to calculate above and with reboiler heating heat and quantity of steam.
Claims (9)
1. the production method by the continuous preparing ethylene glycol of barkite shortening is characterized in that: by controlled temperature, make the recycle stock in the circulation loop keep gaseous phase, only reaction product and unreacted raw material condensation separation are come out.
2. method according to claim 1 is characterized in that: recycle stock is mainly the permanent gases that adds in the reaction, mainly comprises hydrogen, rare gas element, as nitrogen, argon gas etc. and the alkyl alcohol that adds before reaction; Wherein alkyl substituent is identical with alkyl carbon containing quantity in the barkite in the alkyl alcohol, for example is raw material with the dimethyl oxalate, adopts methyl alcohol; With the oxalic acid diethyl ester is raw material, adopts ethanol.
3. method according to claim 1 is characterized in that: the concentration of controlling the barkite in the mixed gas by the temperature of control barkite vaporising device outlet.
4. method according to claim 3 is characterized in that: the barkite vaporising device that is adopted is to guarantee that gas-liquid fully contacts and the little gas-liquid mass transfer (contact) equipment of gas phase drag mutually.
5. method according to claim 1, it is characterized in that: circulation loop mainly is made up of tower, pump, preheater, gas-liquid flow to be adverse current or and stream, thereby control the purpose that reaches the control Outlet Gas Temperature into the temperature of tower liquid by the heat that adds preheater.
6. method according to claim 1, it is characterized in that: during reaction product is separated, realize only will react the material that generates by control condensator outlet gas temperature and from recycle gas, separate with unreacted barkite, and the constant rate of permanent gases and alkyl alcohol in the maintenance circulation gas.
7. method according to claim 6 is characterized in that: condensing equipment can adopt two kinds of forms, and a kind of is the combination of rectifying tower and horizontal condenser, and another kind is the vertical (type) condenser of gas and phlegma adverse current.
8. method according to claim 7 is characterized in that: the feature of rectifying tower is that rectifying section is only arranged in rectifying tower and the horizontal condenser combination, and no stripping section and reboiler in order to reduce the resistance of tower, preferably adopt corrugated-plate packed tower; Condenser is a fractional distillating tube, it is characterized in that material enters shell side, and dispersed phase holdup reaches the purpose of controlling Outlet Gas Temperature to regulate heat transfer area in the shell side by changing.
9. method according to claim 7, it is characterized in that: two kinds of functions of rectifying in the adverse current vertical (type) condenser and partial condensation are combined in the equipment, material steam enters tube side by the bottom, phlegma is drawn by the bottom, the tail gas that does not coagulate is drawn at the top, the type of cooling is the most handy air-cooled, by air quantity control Outlet Gas Temperature.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102863316A (en) * | 2012-09-27 | 2013-01-09 | 安徽淮化股份有限公司 | Ethylene glycol production device |
| CN103804142A (en) * | 2012-11-07 | 2014-05-21 | 中国石油化工集团公司 | System and method used for preparing glycol via hydrogenation of oxalic ester |
| CN104355966A (en) * | 2014-11-06 | 2015-02-18 | 西南化工研究设计院有限公司 | Optimized reaction technology producing ethylene-glycol by adding hydrogen in oxalate |
| WO2015027897A1 (en) * | 2013-09-02 | 2015-03-05 | 东华工程科技股份有限公司 | Energy-saving ester hydrogenation process |
| CN105418365A (en) * | 2015-12-27 | 2016-03-23 | 安徽淮化股份有限公司 | Novel synthetic-gas-to-ethylene-glycol hydrogenation unit |
| CN109482107A (en) * | 2018-11-30 | 2019-03-19 | 华东理工大学 | The gasification method and vapourizing unit of dimethyl oxalate |
| CN111454151A (en) * | 2020-04-26 | 2020-07-28 | 宁波中科远东催化工程技术有限公司 | Method for vaporizing dimethyl oxalate |
| WO2021047051A1 (en) * | 2019-09-12 | 2021-03-18 | 南京延长反应技术研究院有限公司 | Reaction system and process for enhancing hydrogenation of dimethyl oxalate during preparation of ethylene glycol from coal |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102863316A (en) * | 2012-09-27 | 2013-01-09 | 安徽淮化股份有限公司 | Ethylene glycol production device |
| CN102863316B (en) * | 2012-09-27 | 2015-04-08 | 安徽淮化股份有限公司 | Ethylene glycol production device |
| CN103804142A (en) * | 2012-11-07 | 2014-05-21 | 中国石油化工集团公司 | System and method used for preparing glycol via hydrogenation of oxalic ester |
| CN103804142B (en) * | 2012-11-07 | 2016-05-11 | 中国石油化工集团公司 | A kind of system and method for hydrogenation of oxalate for preparing ethylene glycol |
| WO2015027897A1 (en) * | 2013-09-02 | 2015-03-05 | 东华工程科技股份有限公司 | Energy-saving ester hydrogenation process |
| CN104355966A (en) * | 2014-11-06 | 2015-02-18 | 西南化工研究设计院有限公司 | Optimized reaction technology producing ethylene-glycol by adding hydrogen in oxalate |
| CN105418365A (en) * | 2015-12-27 | 2016-03-23 | 安徽淮化股份有限公司 | Novel synthetic-gas-to-ethylene-glycol hydrogenation unit |
| CN109482107A (en) * | 2018-11-30 | 2019-03-19 | 华东理工大学 | The gasification method and vapourizing unit of dimethyl oxalate |
| WO2021047051A1 (en) * | 2019-09-12 | 2021-03-18 | 南京延长反应技术研究院有限公司 | Reaction system and process for enhancing hydrogenation of dimethyl oxalate during preparation of ethylene glycol from coal |
| CN111454151A (en) * | 2020-04-26 | 2020-07-28 | 宁波中科远东催化工程技术有限公司 | Method for vaporizing dimethyl oxalate |
| CN111454151B (en) * | 2020-04-26 | 2023-04-14 | 宁波中科远东催化工程技术有限公司 | Method for vaporizing dimethyl oxalate |
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