CN101381309A - Method for separating low concentration dimethyl carbonate by double-column process in dimethyl oxalate process - Google Patents

Method for separating low concentration dimethyl carbonate by double-column process in dimethyl oxalate process Download PDF

Info

Publication number
CN101381309A
CN101381309A CNA2008102017374A CN200810201737A CN101381309A CN 101381309 A CN101381309 A CN 101381309A CN A2008102017374 A CNA2008102017374 A CN A2008102017374A CN 200810201737 A CN200810201737 A CN 200810201737A CN 101381309 A CN101381309 A CN 101381309A
Authority
CN
China
Prior art keywords
tower
constant boiling
dimethyl oxalate
dmc
methylcarbonate
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CNA2008102017374A
Other languages
Chinese (zh)
Other versions
CN101381309B (en
Inventor
李伟
吴志泉
计扬
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
East China University of Science and Technology
Original Assignee
East China University of Science and Technology
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by East China University of Science and Technology filed Critical East China University of Science and Technology
Priority to CN200810201737A priority Critical patent/CN101381309B/en
Publication of CN101381309A publication Critical patent/CN101381309A/en
Application granted granted Critical
Publication of CN101381309B publication Critical patent/CN101381309B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Landscapes

  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention discloses a method for separating light-concentration methyl carbonate during the process of synthesizing dimethyl oxalate by using coal-based synthesis gas as a raw material. During the process of synthesizing the dimethyl oxalate, methyl nitrite and carbon monoxide are subjected to gas phase catalytic coupled reaction on a catalyst to produce dimethyl oxalate (DMO); meanwhile, side reaction produces methyl carbonate (DMC), so the separation and the removal of the light-concentration methyl carbonate is the key technology for the production of dimethyl oxalate. The method comprises the following steps: after the DMO is separated from mixture after methanol cleaning solution recycles the DMO and the DMC in recycle gas in a dimethyl oxalate separating tower, overhead distillate azeotrope (ME/DMC) and methanol (ME) are delivered to a twin tower process formed by decompression constant boiling rectifying tower-pressurizing constant boiling rectifying tower so as to separate and remove the dimethyl oxalate, and allow the recycle of the methanol to be recycled and repeatedly used.

Description

The method of double-column process separating low concentration methylcarbonate in the dimethyl oxalate building-up process
Technical field
The method of separating low concentration methylcarbonate is that to be applied to the coal be raw material in the dimethyl oxalate building-up process disclosed by the invention, in the technical process by the synthetic gas synthesizing dimethyl oxalate, can from circulating reaction gas, reclaim dimethyl oxalate and methylcarbonate and isolate the methylcarbonate of lower concentration with this method, reclaim methyl alcohol, recycle.
Background technology
Along with the rise of petroleum price, adopt coal to become current research direction for the raw material production organic chemicals, be the new technology route of synthesis of organic chemical product therefore with coal based synthetic gas synthesizing dimethyl oxalate, ethylene glycol.In the process of synthesizing dimethyl oxalate, methyl nitrite and CO are at the enterprising promoting the circulation of qi of catalyzer catalyzed coupling reaction mutually, generate dimethyl oxalate (DMO), the methylcarbonate (DMC) that exists side reaction to generate simultaneously, reacted gas is through cooling, and part DMO condensation separation is come out, gas enters the methanol wash tower then, with methyl alcohol (ME) washing, reclaim DMO and DMC in the gas, gas circulates then.In the methanol wash liquid (containing ME-MDO-DMC), the concentration of methyl alcohol (ME) is greater than 85% (mol), and the concentration of DMC is less than 13% (mol), so the key implemented of process is separating between methylcarbonate (DMC) and the methyl alcohol (ME).
The present invention proposes a kind of method of separating low concentration methylcarbonate, isolates DMC by decompression sequence of constant boiling and rectification-pressurization sequence of constant boiling and rectification double-column process from the DMC-ME mixed solution, and makes methyl alcohol obtain reclaiming, and recycles.
Summary of the invention
The object of the invention provides the method for double-column process separating low concentration methylcarbonate in a kind of dimethyl oxalate building-up process.
The present invention forms by constant boiling point and the azeotropic of DMC-ME under the analog calculation different pressures, sets up decompression sequence of constant boiling and rectification-pressurization sequence of constant boiling and rectification double tower model simultaneously and carries out analog calculation.
1.DMC-ME azeotropic form
The separation of DMO-ME-DMC mixture, principal feature are that DMC and ME form the binary azeotrope, have calculated T-x-y figure and the x-y figure of the DMC-ME under the different pressures for this reason, and the constant boiling point and the azeotropic that can obtain DMC-ME are thus formed, and be as shown in table 1.
DMC-M constant boiling point under table 1. different pressures and azeotropic are formed
Figure A200810201737D00041
2. technical process
(1) material balance
The separation process scheme of design MDO-ME-DMC mixed solution, as shown in Figure 1.
T101 is dimethyl oxalate (DMO) knockout tower, isolates DMO at the bottom of the tower, and cat head distillates methyl alcohol (ME) and azeotrope (ME/DMC), atmospheric operation.
T102 is the decompression sequence of constant boiling and rectification as the methyl alcohol knockout tower, isolates methyl alcohol at the bottom of the tower, and cat head distillates azeotrope (ME/DMC), decompression operation, and for example the 30kPa azeotrope is formed ME/DMC=80/20 (mol/mol).
T103 is as the pressurization sequence of constant boiling and rectification double tower of methylcarbonate (DMC) knockout tower, isolates methylcarbonate at the bottom of the tower, and cat head distillates azeotrope, pressurized operation, and for example azeotrope is formed ME/DMC=95/5 (mol/mol) during 1000kPa.
If enter T101 tower ME-DMC-DMO mixed solution, ME95mol, DMC5mol, DMO10mol can get mass balance type thus
T101?M 1＝M 2＝95；D 1＝D 2＝5
M is a methyl alcohol in the formula, and D is a methylcarbonate, is designated as the logistics numbering down.
T102?M 2+M 6—M 4＝M 5＝95；D 2+D 6—D 4＝0；M 4/D 4＝80/20
T103?M 4＝M 6；D 4＝D 6+D 7＝D 6+5
Thus, logistics Theoretical Calculation as shown in Figure 1 the results are shown in Table 2, and the difference that the azeotropic that utilizes under the different pressures is formed is described, adopts double-column process can realize separating between ME and the DMC.
The logistics table of table 2. Theoretical Calculation
Component 1 2 3 4 5 6 7
ME，mol 95 95 - 25.33 95 25.33 -
DMC，mol 5 5 - 6.33 - 1.33 5
DMO，mol 10 - 10 - - - -
(2) technical process
In the dimethyl oxalate building-up process, separate remove methylcarbonate the double tower process flow process as shown in Figure 2.
3. knockout tower
T101 is the dimethyl oxalate knockout tower, theoretical plate number is 10～20, reflux ratio 0.5～3.0, feed composition is ME-DMC-DMO, because ME-DMC forms azeotrope, the concentration owing to DMC in the isolating washings is different and lower simultaneously, so the key ingredient of T101 tower is ME-DMC in separation, because the key ingredient boiling-point difference is big, so separate easily.
T102 is the decompression sequence of constant boiling and rectification of methyl alcohol knockout tower, theoretical plate number is 10～20, reflux ratio 0.5～3.0, overhead distillate is azeotrope (ME/DMC), at the bottom of the tower methyl alcohol (ME), because the boiling-point difference very little (relative volatility is little) between methyl alcohol and the azeotrope, therefore separate difficulty relatively, in design, should consider to separate required theoretical plate number, also need consider simultaneously stage number change the tower that the pressure drop cause causes at the bottom of the elevation of boiling point in allowed limits, select the low high efficiency packing of pressure drop usually for this reason.Described filler adopts corrugated wire gauze packing.
The mixed solution that will contain 0.01～0.15 mole of dimethyl oxalate, 0.01～0.13 mole of methylcarbonate methyl alcohol usually is a raw material, enters the decompression sequence of constant boiling and rectification tower as methanol distillation column, and the working pressure scope is 10～50kPa, and tower top temperature is 10～55 ℃.
T103 is the pressurization sequence of constant boiling and rectification double tower as the methylcarbonate knockout tower, and theoretical plate number is 10～20, reflux ratio 0.5～3.0, overhead distillate is azeotrope (ME/DMC), be DMC at the bottom of the tower, because the boiling point between azeotrope and the DMC differs bigger, so DMC also is easier to separate.Usually the working pressure scope of pressurization sequence of constant boiling and rectification tower is 400～1000kPa, and tower top temperature is 70～140 ℃, reclaims the methylcarbonate product at the bottom of this tower, and the cat head azeotrope is delivered to decompression sequence of constant boiling and rectification tower.
Description of drawings
Accompanying drawing 1 material balance figure.
The process flow sheet of accompanying drawing 2 dimethyl oxalate building-up process mesolow sequence of constant boiling and rectification-high pressure sequence of constant boiling and rectification double tower separating low concentration methylcarbonate
Nomenclature
T101, T102 and T103 be respectively the DMO knockout tower, as the decompression sequence of constant boiling and rectification of methyl alcohol knockout tower with as the pressurization sequence of constant boiling and rectification double tower of DMC knockout tower;
P101 and P102 are respectively former material conveying pump and vacuum distillation tower azeotrope transferpump;
E101, E103 and E105 are the overhead condenser of T101, T102 and T103;
E102, E104 and E106 are the tower still reboiler of T101, T102 and T103;
E107 and E108 are DMO and DMC reactor product cooler;
V101 is a ME-DMC-DMO mixed solution storage tank;
V102 is the DMO storage tank;
V103 is a T101 overhead product storage tank;
V104, V105/V106 and V110 are medial launder, Receiving bin and the storage tank of T102 cat head azeotrope; V107/V108 and V109 are the Receiving bin and the storage tank of methyl alcohol;
V111, V112 and V113/V114 are medial launder, Receiving bin and the storage tank of T103 cat head azeotrope; V115 and V116 are medial launder and the storage tank of DMC.
Specific implementation method
The present invention will be helped further to understand by following embodiment, but content of the present invention can not be limited.
Embodiment 1
Vacuum distillation tower T102 pressure 30kPa, pressurizing tower T103 pressure 800kPa, DMC/ME=0.05/0.95 (mol/mol), the group of products that raw material and separation obtain becomes to see the following form.
Raw material The T101 bottom product The T102 bottom product The T103 bottom product
ME(mol/h) 95 0.295 94.705 -
DMC(mol/h) 5 0.003 0.029 4.968
DMO(mol/h) 10 10 - -
P(kPa) 101.3 101.3 30 800
T(K) 320 436.9 309.6 445
Embodiment 2
Vacuum distillation tower T102 pressure 30kPa, pressurizing tower T103 pressure 800kPa, DMC/ME=0.1121/0.8879 (mol/mol), the group of products that raw material and separation obtain becomes to see the following form
Raw material The T101 bottom product The T102 bottom product The T103 bottom product
ME(mol/h) 95 - 94.985 0.015
DMC(mol/h) 12 - 0.015 11.985
DMO(mol/h) 20 20 - -
P(kPa) 101.3 101.3 30 800
T(K) 320 436.9 309.6 445
Embodiment 3
Vacuum distillation tower T102 pressure 30kPa, pressurizing tower T103 pressure 500kPa, DMC/ME=0.054/0.946 (mol/mol), the group of products that raw material and separation obtain becomes to see the following form..
Raw material The T101 bottom product The T102 bottom product The T103 bottom product
ME(mol/h) 95 0.012 94.988 -
DMC(mol/h) 6 0.001 0.012 5.987
DMO(mol/h) 10 10 - -
P(kPa) 101.3 101.3 30 500
T(K) 320 436.9 309.6 423
Embodiment 4
Vacuum distillation tower T102 pressure 30kPa, pressurizing tower T103 pressure 400kPa, DMC/ME=0.054/0.946 (mol/mol), the group of products that raw material and separation obtain becomes to see the following form.
Raw material The T101 bottom product The T102 bottom product The T103 bottom product
ME(mol/h) 95 0.001 94.980 0.019
DMC(mol/h) 6 0.001 0.013 5.986
DMO(mol/h) 10 10 - -
P(kPa) 101.3 101.3 30 400
T(K) 320 436.9 309.6 412
Embodiment 4
As shown in Figure 2, the ME-DMC-DMO mixed solution is sent into dimethyl oxalate knockout tower (T101) by storage tank (V101) through pump (P101), methyl alcohol and azeotrope (ME/DMC) distillate from cat head, (E101) is condensed to liquid through condenser, flow into storage tank (V103), bottom product is dimethyl oxalate (DMO), flows into DMO storage tank (V102) after water cooler (E107) cooling, E102 is a T101 tower reboiler, and the heat of rectifying tower is provided.Same E104 and E106 are the reboiler of T102 tower and T103 tower.
T101 distillate ME-DMC mixed solution is entered the decompression sequence of constant boiling and rectification (T102) of methyl alcohol knockout tower by V103, T102 is a vacuum operating, feed liquid directly sucks, in addition, T103 cat head azeotrope (ME/DMC mixed solution) is sucked by azeotrope storage tank (V114) and enters the T102 tower, and overhead distillate adopts chilled brine to be condensed into liquid through condenser (E103), flows into medial launder (V104) then, medial launder (V104) is connected with vacuum unit, the T102 tower is kept under reduced pressure operated.Azeotrope flows into Receiving bin (V105/V106) by medial launder then, two grooves are used alternatingly (decompression/normal pressure), it when making receiver decompression state, and be connected with vacuum unit, when storage tank is full of, another storage tank is made receiver, close its vacuum, open atmospheric valve, make azeotrope flow into azeotrope storage tank (V110), methyl alcohol flows into storage tank (V107/V108) at the bottom of the tower, and two grooves are used alternatingly (decompression/normal pressure), its operation is similar to the operation of cat head storage tank, and last methyl alcohol enters methyl alcohol storage tank (V109).
The ME of azeotrope storage tank (V110) and DMC mixed solution, deliver to methylcarbonate knockout tower (T103) by pump (P102), T103 is a pressurized operation, cat head distilled azeotrope enters medial launder (V111) after condenser (E105) condensation, flow into azeotrope Receiving bin (V112) then, flow into azeotrope storage tank (V113/V114) at last, azeotrope storage tank (V113/V114) is used alternatingly (pressurization/normal pressure), enters the T102 tower to help azeotrope.Bottom product DMC sends into medial launder (V115) after water cooler (E108) cooling, force feed is to storage tank (V116) then.

Claims (6)

1. the method for separating low concentration methylcarbonate in the dimethyl oxalate building-up process, it is characterized in that adopting decompression sequence of constant boiling and rectification-pressurization sequence of constant boiling and rectification double-column process, remove the lower concentration methylcarbonate with separation, 0.01～0.15 mole of dimethyl oxalate will be contained in system, 0.01 the mixed solution of～0.13 mole of methylcarbonate methyl alcohol is a raw material, enter decompression sequence of constant boiling and rectification tower as methanol distillation column, theoretical plate number is 10～20, reflux ratio 0.5～3.0, the working pressure scope is 10～50kPa, tower top temperature is 10～55 ℃, reclaim methyl alcohol at the bottom of the tower, the cat head azeotrope is delivered to the pressurization sequence of constant boiling and rectification tower as the methylcarbonate knockout tower, the working pressure scope of pressurization sequence of constant boiling and rectification tower is 400～1000kPa, theoretical plate number is 10～20, and reflux ratio 0.5～3.0, tower top temperature are 70～140 ℃, reclaim the methylcarbonate product at the bottom of this tower, the cat head azeotrope is delivered to decompression sequence of constant boiling and rectification tower.
2. the method for claim 1 is characterized in that described decompression sequence of constant boiling and rectification tower adopts the efficient low-resistance packing tower.
3. method as claimed in claim 2 is characterized in that described filler is a corrugated wire gauze packing.
4. the method for claim 1, the concentration that it is characterized in that containing in the azeotrope of described decompression sequence of constant boiling and rectification tower methylcarbonate is 0.14～0.23 mole.
5. the method for claim 1, the concentration range that it is characterized in that containing in the cat head azeotrope of described pressurization sequence of constant boiling and rectification tower methylcarbonate is 0.05～0.12 mole.
6. the method for claim 1 is characterized in that the overhead product that described mixed solution raw material is the dimethyl oxalate knockout tower or the overhead product and the pressurization sequence of constant boiling and rectification tower as claimed in claim 1 of dimethyl oxalate knockout tower.
CN200810201737A 2008-10-24 2008-10-24 Method for separating low concentration dimethyl carbonate by double-column process in dimethyl oxalate process Active CN101381309B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN200810201737A CN101381309B (en) 2008-10-24 2008-10-24 Method for separating low concentration dimethyl carbonate by double-column process in dimethyl oxalate process

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN200810201737A CN101381309B (en) 2008-10-24 2008-10-24 Method for separating low concentration dimethyl carbonate by double-column process in dimethyl oxalate process

Publications (2)

Publication Number Publication Date
CN101381309A true CN101381309A (en) 2009-03-11
CN101381309B CN101381309B (en) 2012-10-24

Family

ID=40461390

Family Applications (1)

Application Number Title Priority Date Filing Date
CN200810201737A Active CN101381309B (en) 2008-10-24 2008-10-24 Method for separating low concentration dimethyl carbonate by double-column process in dimethyl oxalate process

Country Status (1)

Country Link
CN (1) CN101381309B (en)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101830806A (en) * 2010-05-21 2010-09-15 上海浦景化工技术有限公司 Method and device for co-producing dimethyl carbonate and dimethyl oxalate
CN102580435A (en) * 2012-01-19 2012-07-18 安徽淮化股份有限公司 Gas-liquid separator and application thereof in separation of dimethyl oxalate
CN102807490A (en) * 2012-08-30 2012-12-05 安徽淮化股份有限公司 System for treating and recovering dimethyl oxalate
CN102911046A (en) * 2011-08-02 2013-02-06 中国石油化工股份有限公司 Dimethyl oxalate purification method during CO coupling dimethyl oxalate synthesis process
CN105272857A (en) * 2014-07-03 2016-01-27 中国石油化工股份有限公司 Method for separating low-concentration dimethyl carbonate during process of synthesizing dimethyl oxalate with coal-based synthetic gas as raw material
CN106316848A (en) * 2016-08-19 2017-01-11 中石化上海工程有限公司 Method for separating dimethyl oxalate and dimethyl carbonate at low energy consumption
AU2015203733B2 (en) * 2014-07-03 2019-06-27 China Petroleum & Chemical Corporation Method for recycling methanol in the process of preparing dimethyl oxalate from synthesis gas
CN111072481A (en) * 2020-01-08 2020-04-28 凯瑞环保科技股份有限公司 Device and method for producing high-concentration dimethyl carbonate
CN111269084A (en) * 2018-12-04 2020-06-12 上海浦景化工技术股份有限公司 Method for removing methyl formate and/or dimethyl carbonate in methanol
CN111440065A (en) * 2018-12-27 2020-07-24 上海浦景化工技术股份有限公司 Preparation method of electrolyte grade dimethyl carbonate
CN111848399A (en) * 2020-07-14 2020-10-30 上海交通大学 Method for separating dimethyl oxalate and dimethyl carbonate with low energy consumption
CN112479869A (en) * 2020-12-10 2021-03-12 新疆天业汇合新材料有限公司 Method for rectifying dimethyl oxalate in coal chemical industry

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101830806A (en) * 2010-05-21 2010-09-15 上海浦景化工技术有限公司 Method and device for co-producing dimethyl carbonate and dimethyl oxalate
CN102911046A (en) * 2011-08-02 2013-02-06 中国石油化工股份有限公司 Dimethyl oxalate purification method during CO coupling dimethyl oxalate synthesis process
CN102580435A (en) * 2012-01-19 2012-07-18 安徽淮化股份有限公司 Gas-liquid separator and application thereof in separation of dimethyl oxalate
CN102580435B (en) * 2012-01-19 2014-10-29 安徽淮化股份有限公司 Gas-liquid separator and application thereof in separation of dimethyl oxalate
CN102807490A (en) * 2012-08-30 2012-12-05 安徽淮化股份有限公司 System for treating and recovering dimethyl oxalate
AU2015203733B2 (en) * 2014-07-03 2019-06-27 China Petroleum & Chemical Corporation Method for recycling methanol in the process of preparing dimethyl oxalate from synthesis gas
CN105272857A (en) * 2014-07-03 2016-01-27 中国石油化工股份有限公司 Method for separating low-concentration dimethyl carbonate during process of synthesizing dimethyl oxalate with coal-based synthetic gas as raw material
CN105272857B (en) * 2014-07-03 2019-09-06 中国石油化工股份有限公司 Coal based synthetic gas is the method for separating low concentration dimethyl carbonate during Material synthesis dimethyl oxalate
CN106316848A (en) * 2016-08-19 2017-01-11 中石化上海工程有限公司 Method for separating dimethyl oxalate and dimethyl carbonate at low energy consumption
CN106316848B (en) * 2016-08-19 2019-03-05 中石化上海工程有限公司 The method of low energy consumption separation of dimethyl oxalate and dimethyl carbonate
CN111269084A (en) * 2018-12-04 2020-06-12 上海浦景化工技术股份有限公司 Method for removing methyl formate and/or dimethyl carbonate in methanol
CN111440065A (en) * 2018-12-27 2020-07-24 上海浦景化工技术股份有限公司 Preparation method of electrolyte grade dimethyl carbonate
CN111440065B (en) * 2018-12-27 2023-05-12 上海浦景化工技术股份有限公司 Preparation method of electrolyte grade dimethyl carbonate
CN111072481A (en) * 2020-01-08 2020-04-28 凯瑞环保科技股份有限公司 Device and method for producing high-concentration dimethyl carbonate
CN111848399A (en) * 2020-07-14 2020-10-30 上海交通大学 Method for separating dimethyl oxalate and dimethyl carbonate with low energy consumption
CN112479869A (en) * 2020-12-10 2021-03-12 新疆天业汇合新材料有限公司 Method for rectifying dimethyl oxalate in coal chemical industry
CN112479869B (en) * 2020-12-10 2023-04-28 新疆天业汇合新材料有限公司 Method for rectifying dimethyl oxalate in coal chemical industry

Also Published As

Publication number Publication date
CN101381309B (en) 2012-10-24

Similar Documents

Publication Publication Date Title
CN101381309B (en) Method for separating low concentration dimethyl carbonate by double-column process in dimethyl oxalate process
US7329774B2 (en) Method and plant for the manufacture of carboxylic acid ester by means of a reactive distillation
CN101998945B (en) Process and apparatus for efficient recovery of dichlorohydrins
CN1189441C (en) Method for production of formic acid
US10246390B2 (en) Process for the separation of glycols using glycerol
CN101657403A (en) Multi-stage process and apparatus for recovering dichlorohydrins
CN104447243B (en) The reactive distillation method of low pressure oxo process butyraldehyde and device
CN1216843C (en) Method for hydroformylation of olefins comprising 2 to 8 carbon atoms
CN105218306A (en) Methanol Recovery method in coal based synthetic gas preparing ethylene glycol process
US20100105965A1 (en) Process and apparatus for azeotropic recovery of dichlorohydrins
JP2010523699A (en) Method and apparatus for reducing the formation of heavy by-products during distillation
CN101709025A (en) Compound cross-flow liquid-liquid extraction separation method of methylal-methanol azeotropic system
CN105272857A (en) Method for separating low-concentration dimethyl carbonate during process of synthesizing dimethyl oxalate with coal-based synthetic gas as raw material
CN102911046A (en) Dimethyl oxalate purification method during CO coupling dimethyl oxalate synthesis process
CN105330542A (en) Production method of dimethyl oxalate
JP2010523701A (en) Method and apparatus for recovering dichlorohydrin by co-distillation
JP3960528B2 (en) Method for producing dimethyl carbonate and ethylene glycol
US10550052B2 (en) Method for separating and purifying isobutylene and method for producing isobutylene
CN1079729A (en) Produce the method for two (fluoro methyl) ethers and methylene fluoride
CN105085165A (en) Ethylene glycol and diethylene glycol separation method
JP2002155027A (en) Method for producing fatty acid lower alkyl ester
CN101998944A (en) Multi-stage process and apparatus for recovering dichlorohydrins
CN204342703U (en) The reaction and rectification device of low pressure oxo process butyraldehyde
CN102701920A (en) Method for purifying vinyl isobutyl ether
CN103842322A (en) Method for preparing a mixture of alcohols

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant
EE01 Entry into force of recordation of patent licensing contract

Application publication date: 20090311

Assignee: Pujing Chemical Industry (Shanghai) Ltd.

Assignor: East China University of Science and Technology

Contract record no.: 2013310000006

Denomination of invention: Method for separating low concentration dimethyl carbonate by double-column process in dimethyl oxalate process

Granted publication date: 20121024

License type: Common License

Record date: 20130129

LICC Enforcement, change and cancellation of record of contracts on the licence for exploitation of a patent or utility model
EE01 Entry into force of recordation of patent licensing contract

Application publication date: 20090311

Assignee: PUJING CHEMICAL INDUSTRY Co.,Ltd.

Assignor: East China University of Science and Technology

Contract record no.: 2015310000058

Denomination of invention: Method for separating low concentration dimethyl carbonate by double-column process in dimethyl oxalate process

Granted publication date: 20121024

License type: Common License

Record date: 20150415

LICC Enforcement, change and cancellation of record of contracts on the licence for exploitation of a patent or utility model
EE01 Entry into force of recordation of patent licensing contract

Application publication date: 20090311

Assignee: PUJING CHEMICAL INDUSTRY Co.,Ltd.

Assignor: East China University of Science and Technology

Contract record no.: 2017310000030

Denomination of invention: Method for separating low concentration dimethyl carbonate by double-column process in dimethyl oxalate process

Granted publication date: 20121024

License type: Common License

Record date: 20170630

Application publication date: 20090311

Assignee: PUJING CHEMICAL INDUSTRY Co.,Ltd.

Assignor: East China University of Science and Technology

Contract record no.: 2017310000032

Denomination of invention: Method for separating low concentration dimethyl carbonate by double-column process in dimethyl oxalate process

Granted publication date: 20121024

License type: Common License

Record date: 20170630

Application publication date: 20090311

Assignee: PUJING CHEMICAL INDUSTRY Co.,Ltd.

Assignor: East China University of Science and Technology

Contract record no.: 2017310000031

Denomination of invention: Method for separating low concentration dimethyl carbonate by double-column process in dimethyl oxalate process

Granted publication date: 20121024

License type: Common License

Record date: 20170630

EE01 Entry into force of recordation of patent licensing contract
EE01 Entry into force of recordation of patent licensing contract

Application publication date: 20090311

Assignee: PUJING CHEMICAL INDUSTRY Co.,Ltd.

Assignor: East China University of Science and Technology

Contract record no.: 2018310000013

Denomination of invention: Method for separating low concentration dimethyl carbonate by double-column process in dimethyl oxalate process

Granted publication date: 20121024

License type: Common License

Record date: 20180511

Application publication date: 20090311

Assignee: PUJING CHEMICAL INDUSTRY Co.,Ltd.

Assignor: East China University of Science and Technology

Contract record no.: 2018310000012

Denomination of invention: Method for separating low concentration dimethyl carbonate by double-column process in dimethyl oxalate process

Granted publication date: 20121024

License type: Common License

Record date: 20180511

Application publication date: 20090311

Assignee: PUJING CHEMICAL INDUSTRY Co.,Ltd.

Assignor: East China University of Science and Technology

Contract record no.: 2018310000014

Denomination of invention: Method for separating low concentration dimethyl carbonate by double-column process in dimethyl oxalate process

Granted publication date: 20121024

License type: Common License

Record date: 20180511

EE01 Entry into force of recordation of patent licensing contract
EC01 Cancellation of recordation of patent licensing contract

Assignee: PUJING CHEMICAL INDUSTRY Co.,Ltd.

Assignor: EAST CHINA University OF SCIENCE AND TECHNOLOGY

Contract record no.: 2017310000031

Date of cancellation: 20230802

Assignee: PUJING CHEMICAL INDUSTRY Co.,Ltd.

Assignor: EAST CHINA University OF SCIENCE AND TECHNOLOGY

Contract record no.: 2017310000032

Date of cancellation: 20230802

Assignee: PUJING CHEMICAL INDUSTRY Co.,Ltd.

Assignor: EAST CHINA University OF SCIENCE AND TECHNOLOGY

Contract record no.: 2017310000030

Date of cancellation: 20230802

Assignee: Pujing Chemical Industry (Shanghai) Ltd.

Assignor: EAST CHINA University OF SCIENCE AND TECHNOLOGY

Contract record no.: 2013310000006

Date of cancellation: 20230802

Assignee: PUJING CHEMICAL INDUSTRY Co.,Ltd.

Assignor: EAST CHINA University OF SCIENCE AND TECHNOLOGY

Contract record no.: 2018310000014

Date of cancellation: 20230802

Assignee: PUJING CHEMICAL INDUSTRY Co.,Ltd.

Assignor: EAST CHINA University OF SCIENCE AND TECHNOLOGY

Contract record no.: 2018310000013

Date of cancellation: 20230802

Assignee: PUJING CHEMICAL INDUSTRY Co.,Ltd.

Assignor: EAST CHINA University OF SCIENCE AND TECHNOLOGY

Contract record no.: 2018310000012

Date of cancellation: 20230802

Assignee: PUJING CHEMICAL INDUSTRY Co.,Ltd.

Assignor: EAST CHINA University OF SCIENCE AND TECHNOLOGY

Contract record no.: 2015310000058

Date of cancellation: 20230802

EC01 Cancellation of recordation of patent licensing contract
EE01 Entry into force of recordation of patent licensing contract

Application publication date: 20090311

Assignee: PUJING CHEMICAL INDUSTRY Co.,Ltd.

Assignor: EAST CHINA University OF SCIENCE AND TECHNOLOGY

Contract record no.: X2023980039236

Denomination of invention: A Method for Separating Low Concentration Dimethyl Carbonate in the Synthesis of Dimethyl Oxalate Using a Dual Tower Process

Granted publication date: 20121024

License type: Exclusive License

Record date: 20230809

EE01 Entry into force of recordation of patent licensing contract