CN105130760A - New technology for preparation of high purity MTBE - Google Patents
New technology for preparation of high purity MTBE Download PDFInfo
- Publication number
- CN105130760A CN105130760A CN201510487420.1A CN201510487420A CN105130760A CN 105130760 A CN105130760 A CN 105130760A CN 201510487420 A CN201510487420 A CN 201510487420A CN 105130760 A CN105130760 A CN 105130760A
- Authority
- CN
- China
- Prior art keywords
- tower
- removing column
- heavy
- mtbe
- weight
- 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
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/05—Preparation of ethers by addition of compounds to unsaturated compounds
- C07C41/06—Preparation of ethers by addition of compounds to unsaturated compounds by addition of organic compounds only
-
- 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
- Y02P20/10—Process efficiency
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Belonging to the technical field of petrochemical industry, the invention in particular relates to a new technology for preparation of high purity MTBE (methyl tert-butyl ether). The process of the technology includes: subjecting a crude MTBE product produced at the bottom of a catalytic distillation tower and the feedstock of the tower to heat exchange by a heat exchanger, then letting the crude MTBE product enter a de-heavy tower under self-pressure, separating heavy sulfide from MTBE in the de-heavy tower, then discharging the heavy sulfide from the bottom of the de-heavy tower, subjecting the de-heavy tower top oil gas to heat exchange with a de-light tower bottom circulating material by the heat exchanger, then refluxing part of the tower top oil gas into the de-heavy tower, at the same time letting the heavy sulfide removed MTBE enter the de-light tower from the de-heavy tower top under self-pressure; taking the de-heavy tower top oil gas as the de-light tower bottom re-boiling heat source, removing C4 fraction from the de-light tower top, and making the high purity MTBE product flow out from the de-light tower bottom. The technology provided by the invention changes the order of ''first light component removal and then heavy component removal'' of crude MTBE to ''first heavy component removal and then light component removal'', and supplies the de-heavy tower top oil gas as the re-boiling heat source to the de-light tower, is in favor of reducing energy consumption and simplifies operation.
Description
Technical field
The invention belongs to technical field of petrochemical industry, be specifically related to the novel process of a kind of high-purity MTBE.
Background technology
MTBE (methyl tertiary butyl ether) is stop bracket gasoline mediation component the most frequently used both at home and abroad at present, is also the raw material of the high-purity iso-butylene of cracking.The general flow of current production MTBE is iso-butylene and the laggard catalytic distillation tower of methyl alcohol generation etherification reaction, obtains MTBE product at the bottom of tower, and the cut that tower top is rich in methyl alcohol then send the refining methanol tower of series connection and methanol distillation column to reclaim methyl alcohol.Its defect is because separation process is short, and the purity of product MTBE is not high (being generally 98.8%), containing a little carbon four lighter hydrocarbons and heavy sulfide.Along with market is to the demand increasing of high-purity iso-butylene and improving constantly of gasoline quality, the production of high-purity MTBE (usual purity >=99%) is more and more taken seriously.
Existing high-purity MTBE rectificating method is to the MTBE come from the bottom of catalytic distillation tower (tower top working pressure is generally 0.75MPag) tower first de-light (i.e. de-C-4-fraction), more de-heavy (i.e. de-heavy sulfide) (see Fig. 2).Due to weight-removing column working pressure, higher than lightness-removing column, (the former is generally 0.46MPag, corresponding tower top 120 DEG C; The latter is generally 0.18MPag, corresponding column bottom temperature 95 DEG C), therefore be provided with weight-removing column fresh feed pump.This flow process has two defects undoubtedly: one is that two towers are independent, all establishes tower bottom reboiler, energy consumption higher (corresponding tower top cooling load is also high); Two is that the pressure energy of catalytic rectifying tower tower base stream does not utilize, and is provided with weight-removing column fresh feed pump.
Summary of the invention
In order to solve the shortcoming and defect part of above prior art, the object of the present invention is to provide the novel process of a kind of high-purity MTBE.
The object of the invention is achieved through the following technical solutions:
A novel process of high-purity MTBE, the flow process of described technique is as follows:
Iso-butylene and methyl alcohol enter methyltertiarvbutyl ether reactor and react, and methyltertiarvbutyl ether reactor bottom product enters catalytic distillation tower, and catalytic distillation column overhead is rich in the ends fraction backflow of methyl alcohol, Methanol Recovery; The self-pressure after interchanger and this tower charging heat exchange of the thick product of extraction MTBE at the bottom of catalytic distillation tower tower enters weight-removing column, discharge at the bottom of weight-removing column tower after heavy sulfide is separated with MTBE in weight-removing column, refluxing and enter weight-removing column in weight-removing column tower top oil gas recycle stock heat exchange rear section at the bottom of interchanger and lightness-removing column tower, removes the heavy column overhead self-pressure of the MTBE autospasy after heavy sulfide simultaneously and enter lightness-removing column; At the bottom of lightness-removing column tower, boiling hot source is from weight-removing column tower top oil gas again, and C-4-fraction is from lightness-removing column removed overhead, and high-purity MTBE product goes out from lightness-removing column tower bottom flow.
The present invention is based on following principle:
(1) working pressure according to tandem tower is different, utilizes the pressure energy of fluid step by step, exempts from line pump;
(2) changing tower independent operating is hot integrated operation, the tower top high temperature cooling of heavy ends separation column heat is transferred at the bottom of the relatively low light ends separation column tower of service temperature, both eliminated or reduced boiling hot again source (as the steam) consumption of light ends separation column, the equivalent tower top cooling load reducing heavy ends separation column again.
Technique tool of the present invention has the following advantages and beneficial effect:
(1) technology utilization catalytic distillation pressure tower > weight-removing column pressure > lightness-removing column pressure of the present invention, changing thick MTBE " first de-light rear de-heavy " is " first de-heavy rear de-light ", former weight-removing column fresh feed pump can be saved, whole flow process is advanced along the direction gravity flow that pressure reduces gradually, and without the need to line pump;
(2) technique of the present invention changes de-frivolous heavy two tower independent operatings is hot integrated operation, namely under the prerequisite not changing two tower working pressures, liquid at the bottom of lightness-removing column is guided into weight-removing column tower top by newly-increased pipeline and former column bottoms pump, return at the bottom of lightness-removing column tower with after the heat exchange of weight-removing column overhead gas, to provide again boiling hot source to lightness-removing column, thus save the steam consumption that to boil again at the bottom of former lightness-removing column tower, and equivalent reduces weight-removing column tower top cooling load;
(3) technique of the present invention does not change existing etherification technology and etherification procedure parameter, is not only conducive to reducing energy consumption, also helps and makes flow process in order, simplify the operation.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of the high-purity MTBE of comparative example of the present invention;
Fig. 2 is the process flow sheet of the high-purity MTBE of the embodiment of the present invention;
Number description is as follows: 1-methyltertiarvbutyl ether reactor; 2-catalytic distillation tower feed exchanger; 3-catalytic distillation column overhead air cooling; 4-catalytic distillation tower return tank; 5-catalytic distillation tower reflux pump; 6-catalytic distillation tower; 7-catalytic distillation tower tower bottom reboiler; 8-lightness-removing column tower top air cooling; 9-lightness-removing column return tank; 10-lightness-removing column reflux pump; 11-lightness-removing column overhead product water cooler; 12-lightness-removing column; 13-lightness-removing column tower bottom reboiler; Reflux pump at the bottom of 14-lightness-removing column tower; 15-weight-removing column fresh feed pump; 16-weight-removing column tower top air cooling; 17-weight-removing column return tank; 18-weight-removing column reflux pump; The high-purity MTBE water cooler of 19-; 20-weight-removing column; 21-weight-removing column tower bottom reboiler; 22-heavy component water cooler; Liquid interchanger at the bottom of 23-weight-removing column top gas and lightness-removing column.
Embodiment
Below in conjunction with embodiment and accompanying drawing, the present invention is described in further detail, but embodiments of the present invention are not limited thereto.
Comparative example
This comparative example is the technique of high-purity MTBE in prior art, and its process flow sheet as shown in Figure 1.Detailed process is as follows:
Iso-butylene and methyl alcohol enter methyltertiarvbutyl ether reactor 1 and react, methyltertiarvbutyl ether reactor bottom product is by entering catalytic distillation tower 6 after catalytic distillation tower feed exchanger 2 heat exchange, the cut that catalytic distillation column overhead is rich in methyl alcohol enters catalytic distillation tower backflow by catalytic distillation column overhead air cooling 3, catalytic distillation tower return tank 4 and catalytic distillation tower reflux pump 5, Methanol Recovery successively, the thick product of extraction MTBE at the bottom of catalytic distillation tower tower first certainly compresses into lightness-removing column 12 after catalytic distillation tower tower bottom reboiler 7 heats, lightness-removing column trim the top of column component is successively through lightness-removing column tower top air cooling 8, lightness-removing column return tank 9 and lightness-removing column reflux pump 10 backflow enter lightness-removing column, C-4-fraction is discharged after the cooling of lightness-removing column overhead product water cooler 11, the lightness-removing column materials at bottom of tower component that refluxes after lightness-removing column tower bottom reboiler 13 additionally heating is back to dehydrogenation tower by reflux pump 14 at the bottom of lightness-removing column tower, the MTBE removing C-4-fraction enters weight-removing column 20 under the power of weight-removing column fresh feed pump 15, under the heating of weight-removing column tower bottom reboiler 21, enter heavy component water cooler 22 after heavy sulfide is separated with MTBE to cool, discharge at the bottom of weight-removing column tower, remove the high-purity MTBE after heavy sulfide to discharge from weight-removing column tower top after high-purity MTBE water cooler 19 cools, backflow material is successively through weight-removing column tower top air cooling 16, weight-removing column return tank 17 and weight-removing column reflux pump 18 backflow enter weight-removing column.
Embodiment
The novel process of a kind of high-purity MTBE of the present embodiment, its process flow sheet as shown in Figure 2.Detailed process is as follows:
Iso-butylene and methyl alcohol enter methyltertiarvbutyl ether reactor 1 and react, methyltertiarvbutyl ether reactor bottom product is by entering catalytic distillation tower 6 after catalytic distillation tower feed exchanger 2 heat exchange, the cut that catalytic distillation column overhead is rich in methyl alcohol enters catalytic distillation tower backflow by catalytic distillation column overhead air cooling 3, catalytic distillation tower return tank 4 and catalytic distillation tower reflux pump 5, Methanol Recovery successively, the thick product of extraction MTBE at the bottom of catalytic distillation tower tower through catalytic distillation tower tower bottom reboiler 7 heat after with this tower charging heat exchange after self-pressure enter weight-removing column 20, under the heating of weight-removing column tower bottom reboiler 21, enter heavy component water cooler 22 after heavy sulfide is separated with MTBE to cool, discharge at the bottom of weight-removing column tower, weight-removing column tower top oil gas is by liquid interchanger 23 at the bottom of weight-removing column top gas and lightness-removing column and recycle stock heat exchange at the bottom of lightness-removing column tower, backflow material is successively through weight-removing column tower top air cooling 16, weight-removing column return tank 17 and weight-removing column reflux pump 18 backflow enter weight-removing column, remove the heavy column overhead self-pressure of the MTBE autospasy after heavy sulfide simultaneously and enter lightness-removing column 12, be back at the bottom of lightness-removing column tower after the recycle stock absorption weight-removing column top gas heat of relative low temperature at the bottom of lightness-removing column tower, wherein lightness-removing column tower bottom reboiler 13 is without the need to extra heat source, the MTBE entering lightness-removing column through fractionation from lightness-removing column removed overhead C-4-fraction, lightness-removing column trim the top of column component enters lightness-removing column through the backflow of lightness-removing column tower top air cooling 8, lightness-removing column return tank 9 and lightness-removing column reflux pump 10 successively, C-4-fraction is discharged after the cooling of lightness-removing column overhead product water cooler 11, and high-purity MTBE product goes out from lightness-removing column tower bottom flow.
The observable index of embodiment and comparative example is comparatively:
120,000 tons of high-purity MTBE devices (going into operation in device year 8400 hours) are produced per year for certain, in comparative example, the thick MTBE (14.5t/h, 90 DEG C, 0.77MPag) come from the bottom of catalytic distillation tower tower first compresses into lightness-removing column (tower top pressure is 0.18MPag) certainly, and lightness-removing column substrate material is laggard as weight-removing column (tower top pressure is 0.46MPag) through the pressurization of weight-removing column fresh feed pump again; Lightness-removing column tower bottom reboiler 1.0MPa steam does thermal source, and weight-removing column tower bottom reboiler 1.6MPa steam does thermal source; In embodiment, the thick MTBE (14.5t/h, 90 DEG C, 0.77MPag) come from the bottom of catalytic distillation tower tower first compresses into weight-removing column (tower top pressure is 0.46MPag) certainly, from compressing into lightness-removing column (tower top pressure is 0.18MPag) after removing heavy sulfide, correspondence stops former weight-removing column fresh feed pump (former pump power consumption 10kw), and at the bottom of lightness-removing column tower more boiling hot source (lightness-removing column column bottom temperature is 95 DEG C) use weight-removing column tower top oil gas heat (weight-removing column tower top oil gas temperature is 120 DEG C) instead.Table 1 lists the main energy consumption of comparative example and embodiment.
Table 1 comparative example and the main energy consumption comparison of embodiment
As can be seen from Table 1, compared to comparative example, embodiment is under the prerequisite not changing MTBE yield and purity:
1) load that boils again at the bottom of weight-removing column tower does not change (consuming 300 DEG C, 1.6MPag superheated vapour 2.7t/h), and tower top cooling load is from 147.9 × 10
4kcal/h drops to 86.5 × 10
4kcal/h, reduces 64.7 × 10
4kcal/h, the range of decrease is 43.7%;
2) lightness-removing column no longer does boiling hot source with 1.0MPa steam again, and save 250 DEG C, 1.0MPag superheated vapour 1.6t/h, corresponding tower top cooling load remains unchanged;
3) inactive former weight-removing column fresh feed pump, reduces power consumption 10kw (pump efficiency gets 70%).
Add up to 1 ~ 3, calculate by 1.0MPa steam 200 yuan/t, recirculated water unit price 0.4 yuan/t (the recirculated water temperature difference gets 8 DEG C), electricity price 0.75 yuan/kwh, embodiment comparatively comparative example can realize year energy-saving benefit 277.2 ten thousand yuan.
Above-described embodiment is the present invention's preferably embodiment; but embodiments of the present invention are not restricted to the described embodiments; change, the modification done under other any does not deviate from spirit of the present invention and principle, substitute, combine, simplify; all should be the substitute mode of equivalence, be included within protection scope of the present invention.
Claims (1)
1. a novel process of high-purity MTBE, is characterized in that the flow process of described technique is as follows:
Iso-butylene and methyl alcohol enter methyltertiarvbutyl ether reactor and react, and methyltertiarvbutyl ether reactor bottom product enters catalytic distillation tower, and catalytic distillation column overhead is rich in the ends fraction backflow of methyl alcohol, Methanol Recovery; The self-pressure after interchanger and this tower charging heat exchange of the thick product of extraction MTBE at the bottom of catalytic distillation tower tower enters weight-removing column, discharge at the bottom of weight-removing column tower after heavy sulfide is separated with MTBE in weight-removing column, refluxing and enter weight-removing column in weight-removing column tower top oil gas recycle stock heat exchange rear section at the bottom of interchanger and lightness-removing column tower, removes the heavy column overhead self-pressure of the MTBE autospasy after heavy sulfide simultaneously and enter lightness-removing column; At the bottom of lightness-removing column tower, boiling hot source is from weight-removing column tower top oil gas again, and C-4-fraction is from lightness-removing column removed overhead, and high-purity MTBE product goes out from lightness-removing column tower bottom flow.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510487420.1A CN105130760B (en) | 2015-08-10 | 2015-08-10 | A kind of technique of high-purity MTBE |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510487420.1A CN105130760B (en) | 2015-08-10 | 2015-08-10 | A kind of technique of high-purity MTBE |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105130760A true CN105130760A (en) | 2015-12-09 |
| CN105130760B CN105130760B (en) | 2017-04-05 |
Family
ID=54716400
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510487420.1A Active CN105130760B (en) | 2015-08-10 | 2015-08-10 | A kind of technique of high-purity MTBE |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105130760B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106866385A (en) * | 2017-02-28 | 2017-06-20 | 山东京博石油化工有限公司 | A kind of method for producing high-purity methyl tertiary butyl ether(MTBE) |
| CN107226776A (en) * | 2017-05-11 | 2017-10-03 | 黑龙江安瑞佳石油化工有限公司 | Feedstock pre-processing system and processing method |
| CN110423197A (en) * | 2019-09-17 | 2019-11-08 | 凯瑞环保科技股份有限公司 | A kind of device and method using low concentration ethylene glycol production glycol acetate |
| CN112321382A (en) * | 2020-09-23 | 2021-02-05 | 山东齐鲁石化工程有限公司 | 1-butene refining energy-saving process and device with heat pump heat integration |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203095914U (en) * | 2012-12-21 | 2013-07-31 | 中国石油天然气股份有限公司 | Device for removing high-boiling-point sulphide in methyl tertiary butyl ethers |
| CN203904245U (en) * | 2014-06-11 | 2014-10-29 | 中国石油化工股份有限公司 | Device for synthesizing and separating low-sulfur methyl tert-butyl ether |
| CN104370709A (en) * | 2014-10-15 | 2015-02-25 | 洛阳智达石化工程有限公司 | Method for reducing sulfur content in methyl tert-butyl ether and device thereof |
| CN104591944A (en) * | 2013-11-03 | 2015-05-06 | 中国石油化工股份有限公司 | Process for preparing isobutene through methyl tertiary-butyl ether cracking |
| CN104591945A (en) * | 2013-11-03 | 2015-05-06 | 中国石油化工股份有限公司 | Process for preparing isobutene through cracking of methyl tert-butyl ether |
| CN104744194A (en) * | 2015-03-29 | 2015-07-01 | 大连理工大学 | Heat integration process for isobutylene device light component removing and heavy component removing tower |
-
2015
- 2015-08-10 CN CN201510487420.1A patent/CN105130760B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203095914U (en) * | 2012-12-21 | 2013-07-31 | 中国石油天然气股份有限公司 | Device for removing high-boiling-point sulphide in methyl tertiary butyl ethers |
| CN104591944A (en) * | 2013-11-03 | 2015-05-06 | 中国石油化工股份有限公司 | Process for preparing isobutene through methyl tertiary-butyl ether cracking |
| CN104591945A (en) * | 2013-11-03 | 2015-05-06 | 中国石油化工股份有限公司 | Process for preparing isobutene through cracking of methyl tert-butyl ether |
| CN203904245U (en) * | 2014-06-11 | 2014-10-29 | 中国石油化工股份有限公司 | Device for synthesizing and separating low-sulfur methyl tert-butyl ether |
| CN104370709A (en) * | 2014-10-15 | 2015-02-25 | 洛阳智达石化工程有限公司 | Method for reducing sulfur content in methyl tert-butyl ether and device thereof |
| CN104744194A (en) * | 2015-03-29 | 2015-07-01 | 大连理工大学 | Heat integration process for isobutylene device light component removing and heavy component removing tower |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106866385A (en) * | 2017-02-28 | 2017-06-20 | 山东京博石油化工有限公司 | A kind of method for producing high-purity methyl tertiary butyl ether(MTBE) |
| CN106866385B (en) * | 2017-02-28 | 2020-04-17 | 山东京博石油化工有限公司 | Method for producing high-purity methyl tert-butyl ether |
| CN107226776A (en) * | 2017-05-11 | 2017-10-03 | 黑龙江安瑞佳石油化工有限公司 | Feedstock pre-processing system and processing method |
| CN110423197A (en) * | 2019-09-17 | 2019-11-08 | 凯瑞环保科技股份有限公司 | A kind of device and method using low concentration ethylene glycol production glycol acetate |
| CN110423197B (en) * | 2019-09-17 | 2023-11-14 | 凯瑞环保科技股份有限公司 | Device and method for producing ethylene glycol diacetate by using low-concentration ethylene glycol |
| CN112321382A (en) * | 2020-09-23 | 2021-02-05 | 山东齐鲁石化工程有限公司 | 1-butene refining energy-saving process and device with heat pump heat integration |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105130760B (en) | 2017-04-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105218315A (en) | A kind of divided-wall distillation column that uses refines method and the device of methyl alcohol in conjunction with heat pump | |
| CN105130760A (en) | New technology for preparation of high purity MTBE | |
| CN203710716U (en) | Device for improving recycling rate of alcohol ketone components in refining process of cyclohexanone | |
| CN115317945B (en) | Two-tower thermal coupling and heat pump combined separation process and separation device for alkylation reaction product | |
| CN203007175U (en) | Heat integration device for methanol synthesis and rectification | |
| CN109646980B (en) | Fusel-free oil dividing wall tower coupled methanol multi-effect rectification energy-saving device and method | |
| CN101374788B (en) | Method for separating and preparing polymerization stage low carbon olefin hydrocarbon from methanol pyrolysis gas | |
| CN103611328B (en) | Process for extracting naphthalene by continuously rectifying heavy benzol | |
| CN104784953A (en) | Reaction product separation system for preparing propylene with methanol and quenching system of reaction product separation system | |
| CN107144092B (en) | Device for producing high-purity ethylene by ethylene heat pump rectification and production process thereof | |
| CN102050690B (en) | Isoolefine production method | |
| CN104926584B (en) | A kind of system and method preparing iso-butane | |
| CN101531919A (en) | Energy-saving device and operation process for absorption-stabilization system | |
| CN110743189A (en) | Energy-saving carbon disulfide rectification process | |
| CN216536970U (en) | Deisobutanizer energy-saving separation system | |
| CN101503631B (en) | Catalytic cracking fractionating tower oil gas energy-saving apparatus and operation technique | |
| CN205473599U (en) | Retrieve device of cold volume of contact again of reforming | |
| CN104418693A (en) | Energy-saving method of device for preparing butadiene by oxidative dehydrogenation of butene | |
| CN113004120A (en) | Water-saving emission-reducing methanol thermal coupling rectification system and rectification method | |
| CN112409181A (en) | Dimethyl oxalate rectifying device for coal chemical industry | |
| CN101928195A (en) | Method for preparing butane-1 from CPP C4 | |
| CN109181766A (en) | A kind of modified light aromatic hydrocarbons hydrogenation plant and its operating method | |
| CN205061982U (en) | Methyl alcohol system lighter hydrocarbons process systems that energy integration utilized | |
| CN111905395A (en) | Rectification separation system and separation process for preparing ethylene glycol from synthesis gas | |
| CN219848213U (en) | Fractionating system of special solvent oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |