CN106957214A - Methanol heat-pump distillation system and method - Google Patents
Methanol heat-pump distillation system and method Download PDFInfo
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- CN106957214A CN106957214A CN201710243313.3A CN201710243313A CN106957214A CN 106957214 A CN106957214 A CN 106957214A CN 201710243313 A CN201710243313 A CN 201710243313A CN 106957214 A CN106957214 A CN 106957214A
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- rectifying column
- tower
- column tower
- reboiler
- methanol
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
- C07C31/02—Monohydroxylic acyclic alcohols
- C07C31/04—Methanol
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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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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a kind of methanol heat-pump distillation system and method, belong to heat pump distillation field.System includes 4 grades of heat pump separators being sequentially connected in series, wherein every grade of heat pump separator includes rectifying column tower（2）, vapour compression machine（3）, reboiler（5）, condenser（4）;Wherein rectifying column tower（2）Overhead vapours is exported and vapour compression machine（3）Entrance is connected, vapour compression machine（3）Outlet and reboiler（5）Thermal source inlet is connected, reboiler（5）Thermal source outlet and condenser（4）Entrance is connected, condenser（4）Outlet is divided into two-way, all the way as a point tower top discharging pipeline, all the way with rectifying column tower（2）Refluxing opening is connected;Reboiler（5）Material outlet and rectifying column tower（2）Material inlet is connected, rectifying column tower（2）Material outlet and reboiler（5）Material inlet is connected.The present invention fully applies the latent heat of overhead vapours, with significant economic benefit.
Description
Technical field
The invention belongs to heat pump distillation field, it is related to a kind of methanol heat-pump distillation system and method.
Background technology
Methanol is one of modern chemical industry basic organic, mainly for the manufacture of formaldehyde, acetic acid, chloromethanes, methylamine and sulphur
A variety of organic products such as dimethyl phthalate.Methanol is used to produce octane number additive methyl tertiary butyl ether(MTBE), methanol gasoline, methanol
Fuel, and the product such as Methanol Protein, promote development and the market needs of methanol production.
In synthesizing methanol commercial process, the refined of crude carbinol is the important operation list for ensureing methanol product quality
Member, while the energy consumption during refining methanol is also to influence the key factor of methanol production cost, directly influences industrial life
The cost of production.Therefore, it is very important to reduce rectifying column tower running cost by engineering technology means.
The content of the invention
It is an object of the invention to provide a kind of methanol heat-pump distillation system and method, the energy in Conventional process is reduced
Consumption.
A kind of methanol heat-pump distillation system, it is characterised in that：Including the 4 grades of heat pump being sequentially connected in series separators, wherein often
Level heat pump separator includes rectifying column tower, vapour compression machine, reboiler, condenser；Wherein rectifying column tower tower top steams
Vapor outlet is connected with vapour compression machine entrance, and vapour compression machine outlet is connected with reboiler thermal source inlet, reboiler thermal source outlet
It is connected with condenser inlet, condensator outlet is divided into two-way, all the way as a point tower top discharging pipeline, is returned all the way with rectifying column tower
Head piece is connected；Reboiler material outlet is connected with rectifying column tower material inlet, rectifying column tower material outlet and reboiler thing
Expect that entrance is connected；In above-mentioned 4 grades of heat pump separators, the rectifying column tower entrance of the 1st grade of heat pump separator enters for crude carbinol
Mouthful, the rectifying column tower entrance of the 2nd to 4 grade of heat pump separator and the outlet of the rectifying column tower of upper level heat pump separator
It is connected.
Described rectifying column tower is plate column or packed tower.
Described reboiler is plate type heat exchanger or forced circulation heat exchange or falling-film heat exchanger.
Described vapour compression machine is roots-type or centrifugal or double-screw type.
The methanol heat-pump distillation system and method, it is characterised in that：Per in one-level heat pump separator, methanol solution enters
Enter rectifying column tower and carry out rectifying, overhead extraction light component steam is pressurized heating, the light component after compression by vapour compression machine
Steam is divided into two parts, part discharge a, part is made as the thermal source of reboiler after the condensed device cooling of reboiler discharge liquor
For the phegma of rectifying column tower；In above-mentioned 4 grades of heat pump separators, rectifying column tower is entered in the 1st grade of heat pump separator
Methanol solution be crude carbinol, the methanol solution that rectifying column tower is entered in the 2nd to 4 grade of heat pump separator is upper level heat pump
The solution that the outlet of the rectifying column tower of separator is excluded.
The methanol heat-pump distillation system and method, it is characterised in that：The rectifying column tower operating pressure at different levels is
100kPa-800kPa, reflux ratio is 1.5-5；Described vapour compression machine, compression ratio is 1.5-3.63.
The advantage of the invention is that：By the use of heat pump distillation as the refined mode of methanol, the vapor action after compression is boiled again
The thermal source of device, fully applies the latent heat of overhead vapours, with significant economic benefit.
Brief description of the drawings
Fig. 1 heat pump technology flow charts；
Label title in figure:1：Crude carbinol；2:Rectifying column tower；3：Vapour compression machine；4：Condenser；5：Reboiler.
Example is embodied
Embodiment 1
Certain existing unit needs to refine 710,000 tons of methanol per hour, it is desirable to refined methanol product requirement：Meet the United States Federal's industry
Methanol standard " AA " level index.8000 hours operating times of year.
Crude carbinol composition is shown in Table 1 (mass percent)
The crude carbinol of table 1 constitutes (mass percent)
Technique is described：
The preliminary rectifying of crude carbinol 1 (313K, 71t/h) entrance one-level rectifying column tower progress, tower top methanol steam (343K,
Heating 130KPa) is pressurized by compressor 3, operation compression ratio is 2.15, and methanol steam (362K, 280KPa) is used as rectifying after pressure
The thermal source of the reboiler 5 of tower tower body 2, the condensed device 4 of reboiler discharge liquor (362K) is divided into two parts after cooling down, and a part of tower top goes out
Expect (1.5t/h, 313K), a part of overhead reflux as rectifying column tower.(348K, methanol is dense for the discharging of rectifying column tower tower reactor
Spend 91Wt%) enter two grades of smart rectifying column towers progress rectifying, overhead extraction tower top methanol steam (356K, 200KPa) is through overvoltage
The supercharging heating of contracting machine, operation compression ratio is 1.5, and methanol steam (368K, 300KPa) is used as rectifying column tower reboiler after pressure
Thermal source, is divided into two parts after the cooling of reboiler discharge liquor (368K) condensed device, a part discharge as tower top (30t/h,
313K), a part of overhead reflux (75t/h, 313K) as rectifying column tower.The discharging of rectifying column tower tower reactor (361K, methanol
Concentration 84Wt%) enter the progress rectifying of three-level rectifying column tower, tower top methanol steam (340K, 110KPa) passes through compressor boost
Heating, operation compression ratio is 2.4, and methanol steam (363K, 260KPa) then boils as the thermal source of rectifying column tower reboiler after pressure
It is divided into two parts after the condensed device cooling of device discharge liquor (363K), a part discharges (29.5t/h, 313K) as tower top, one
It is allocated as the overhead reflux (59t/h, 313K) for rectifying column tower.The discharging of rectifying column tower tower reactor (356K, methanol concentration
39Wt%) enter level Four rectifying column tower and carry out rectifying, tower top methanol steam (346K, 110KPa) passes through compressor boost liter
Temperature, operation compression ratio is 3.63, and methanol steam (380K, 400KPa) then boils as the thermal source of rectifying column tower reboiler after pressure
It is divided into two parts after the condensed device cooling of device discharge liquor (380K), a part discharges (4.5t/h, 313K) as tower top, a part
It is used as the overhead reflux (4.5t/h, 313K) of rectifying column tower.
Described one-level rectifying column tower operating pressure is 130kPa, and tower top temperature is 343K, bottom temperature 348K.
The compressor of described one-level rectifying column tower is centrifugal compressor, and compression ratio is 2.15, compressor air-discharging pressure
Power is 280kPa.
Described two-stage rectification tower tower body operating pressure is 200kPa, and tower top temperature is 356K, bottom temperature 361K.
The compressor of described two-stage rectification tower tower body is Roots Compressor, and compression ratio is 1.5, Compressor Discharge Pressure
For 300kPa.
Described three-level rectifying column tower operating pressure is 110kPa, and tower top temperature is 340K, bottom temperature 363K.
The compressor of described three-level rectifying column tower is centrifugal compressor, and compression ratio is 2.4, Compressor Discharge Pressure
For 260kPa.
Described level Four rectifying column tower operating pressure is 110kPa, and tower top temperature is 336K, bottom temperature 372K.
The compressor of described level Four rectifying column tower is twin-screw compressor, and compression ratio is 3.63, compressor air-discharging
Pressure is 400kPa.
, can steam saving 80t/h, recirculated water 8250m3/h using heat pump rectification system compared with traditional distillation system
(32 DEG C -38 DEG C), increase power consumption 5991kW.Calculated with current price, 160 yuan/t of steam, 0.2 yuan/m3 of recirculated water, electricity
Take 0.8 yuan/degree, the two year Operation cost comparison such as following table (annual run time is calculated by 8000h)：
| Project | Traditional three-tower rectification | Heat pump distillation new technology |
| Steam expends (ten thousand yuan/8000h) | 10240 | 0 |
| Recirculated water (ten thousand yuan/8000h) | 1600 | 280 |
| The electricity charge (ten thousand yuan/8000h) | 3834 | |
| Amount to (ten thousand yuan/8000h) | 11840 | 4114 |
As can be seen from the above table, it is more traditional using the annual operating cost of heat pump distillation for 71t/h refining methanol devices
More than 7,736 ten thousand yuan of three-tower rectification saving, about 70%, the investment of enterprise has greatly been saved, energy consumption is reduced.Embodiment 2
A kind of methanol heat-pump new technology：
The preliminary rectifying of crude carbinol 1 (313K, 50t/h) entrance one-level rectifying column tower progress, tower top methanol steam (337K,
Heating 100KPa) is pressurized by compressor 3, operation compression ratio is 1.7, and methanol steam (348K, 170KPa) is used as rectifying after pressure
The thermal source of the reboiler 5 of tower tower body 2, the condensed device 4 of reboiler discharge liquor (348K) is divided into two parts after cooling down, and a part of tower top goes out
Expect (1.5t/h, 313K), a part of overhead reflux as rectifying column tower.(342K, methanol is dense for the discharging of rectifying column tower tower reactor
Spend 91Wt%) enter the progress rectifying of two-stage rectification tower tower body, tower top methanol steam (337K, 100KPa) passes through compressor boost liter
Temperature, operation compression ratio is 1.8, and methanol steam (352K, 180KPa) is used as the thermal source of rectifying column tower reboiler, reboiler after pressure
It is divided into two parts after the condensed device cooling of discharge liquor (352K), a part discharges (30t/h, 313K) as tower top, and a part is made
For the overhead reflux (75t/h, 313K) of rectifying column tower.Rectifying column tower tower reactor discharges (345K, methanol concentration 76.6Wt%)
Rectifying is carried out into three-level rectifying column tower, tower top methanol steam (337K, 100KPa) is pressurized through compressor and heated up, operation compression
Than for 2, methanol steam (356K, 200KPa) is used as the thermal source of rectifying column tower reboiler, reboiler discharge liquor (356K) after pressure
It is divided into two parts after condensed device cooling, a part discharges (8.5t/h, 313K) as tower top, and a part is used as rectifying column tower
Overhead reflux (17t/h, 313K).Rectifying column tower tower reactor discharging (349K, methanol concentration 57Wt%) enters level Four rectifying column
Tower body carries out rectifying, and tower top methanol steam (338K, 100KPa) heats up by compressor boost, and operation compression ratio is 2.8, after pressure
Methanol steam (366K, 280KPa) is as the thermal source of rectifying column tower reboiler, and reboiler discharge liquor (366K) condensed device is cold
But it is divided into two parts afterwards, a part discharges (4.5t/h, 313K) as tower top, a part of overhead reflux as rectifying column tower
(4.5t/h, 313K).
Described one-level rectifying column tower operating pressure is 100kPa, and tower top temperature is 337K, bottom temperature 342K.
The compressor of described one-level rectifying column tower is Roots Compressor, and compression ratio is 1.7, Compressor Discharge Pressure
For 170kPa.
Described two-stage rectification tower tower body operating pressure is 100kPa, and tower top temperature is 337K, bottom temperature 345K.
The compressor of described two-stage rectification tower tower body is centrifugal compressor, and compression ratio is 1.8, Compressor Discharge Pressure
For 180kPa.
Described three-level rectifying column tower operating pressure is 100kPa, and tower top temperature is 337K, bottom temperature 349K.
The compressor of described three-level rectifying column tower is Roots Compressor, and compression ratio is 2, and Compressor Discharge Pressure is
200kPa。
Described level Four rectifying column tower operating pressure is 100kPa, and tower top temperature is 338K, bottom temperature 359K.
The compressor of described level Four rectifying column tower is twin-screw compressor, and compression ratio is 2.8, compressor air-discharging pressure
Power is 280kPa.
Embodiment 3
The preliminary rectifying of crude carbinol 1 (313K, 20t/h) entrance one-level rectifying column tower progress, tower top methanol steam (337K,
Heating 100KPa) is pressurized by compressor 3, operation compression ratio is 1.6, and methanol steam (348K, 160KPa) is used as rectifying after pressure
The thermal source of the reboiler 5 of tower tower body 2, the condensed device 4 of reboiler discharge liquor (348K) is divided into two parts after cooling down, and a part of tower top goes out
Expect (1t/h, 313K), a part of overhead reflux as rectifying column tower.The discharging of rectifying column tower tower reactor (342K, methanol concentration
91Wt%) enter two-stage rectification tower tower body and carry out rectifying, tower top methanol steam (401K, 800KPa) passes through compressor boost liter
Temperature, operation compression ratio is 2, and methanol steam (413K, 1600KPa) is used as the thermal source of rectifying column tower reboiler, reboiler after pressure
It is divided into two parts after the condensed device cooling of discharge liquor (413K), a part discharges (12t/h, 313K) as tower top, and a part is made
For the overhead reflux (24t/h, 313K) of rectifying column tower.Rectifying column tower tower reactor discharging (406K, methanol concentration 76Wt%) is entered
Enter three-level rectifying column tower and carry out rectifying, tower top methanol steam (337K, 100KPa) heats up by compressor boost, operation compression
Than for 2, methanol steam (356K, 200KPa) is used as the thermal source of rectifying column tower reboiler, reboiler discharge liquor (356K) after pressure
It is divided into two parts after condensed device cooling, a part discharges (3t/h, 313K) as tower top, and a part is used as rectifying column tower
Overhead reflux (6t/h, 313K).Rectifying column tower tower reactor discharging (349K, methanol concentration 58Wt%) enters level Four rectifying column tower
Rectifying is carried out, tower top methanol steam (338K, 100KPa) heats up by compressor boost, operation compression ratio is methanol after 2.9, pressure
Steam (367K, 290KPa) as rectifying column tower reboiler thermal source, after the cooling of reboiler discharge liquor (367K) condensed device
Be divided into two parts, a part discharges (2t/h, 313K) as tower top, a part as rectifying column tower overhead reflux (2t/h,
313K)。
Described one-level rectifying column tower operating pressure is 100kPa, and tower top temperature is 337K, bottom temperature 342K.
The compressor of described one-level rectifying column tower is Roots Compressor, and compression ratio is 1.67, compressor air-discharging pressure
Power is 160kPa.
Described two-stage rectification tower tower body operating pressure is 800kPa, and tower top temperature is 401K, bottom temperature 406K.
The compressor of described two-stage rectification tower tower body is centrifugal compressor, and compression ratio is 2, and Compressor Discharge Pressure is
1600kPa。
Described three-level rectifying column tower operating pressure is 100kPa, and tower top temperature is 337K, bottom temperature 349K.
The compressor of described three-level rectifying column tower is Roots Compressor, and compression ratio is 2, and Compressor Discharge Pressure is
200kPa。
Described level Four rectifying column tower operating pressure is 100kPa, and tower top temperature is 338K, bottom temperature 361K.
The compressor of described level Four rectifying column tower is twin-screw compressor, and compression ratio is 2.9, compressor air-discharging pressure
Power is 290kPa.
Claims (6)
1. a kind of methanol heat-pump distillation system, it is characterised in that：
Including the 4 grades of heat pump being sequentially connected in series separators;
Wherein every grade heat pump separator includes rectifying column tower（2）, vapour compression machine（3）, reboiler（5）, condenser
（4）;Wherein rectifying column tower（2）Overhead vapours is exported and vapour compression machine（3）Entrance is connected, vapour compression machine（3）Outlet with
Reboiler（5）Thermal source inlet is connected, reboiler（5）Thermal source outlet and condenser（4）Entrance is connected, condenser（4）Outlet is divided into
Two-way, all the way as a point tower top discharging pipeline, all the way with rectifying column tower（2）Refluxing opening is connected;Reboiler（5）Material outlet
With rectifying column tower（2）Material inlet is connected, rectifying column tower（2）Material outlet and reboiler（5）Material inlet is connected；
In above-mentioned 4 grades of heat pump separators, the rectifying column tower of the 1st grade of heat pump separator（2）Entrance is crude carbinol（1）Enter
Mouthful, the rectifying column tower entrance of the 2nd to 4 grade of heat pump separator and the outlet of the rectifying column tower of upper level heat pump separator
It is connected.
2. the methanol heat-pump distillation system according to claim 1, it is characterised in that：Described rectifying column tower（2）And essence
Tower tower body is evaporated for plate column or packed tower.
3. methanol heat-pump distillation system according to claim 1, it is characterised in that：Described reboiler（5）For plate-type heat-exchange
Device or forced circulation heat exchange or falling-film heat exchanger.
4. methanol heat-pump distillation system according to claim 1, it is characterised in that：Described vapour compression machine (3) is Roots
Formula or centrifugal or double-screw type.
5. methanol heat-pump rectificating method according to claim 1, it is characterised in that：
Per in one-level heat pump separator, methanol solution enters rectifying column tower and carries out rectifying, overhead extraction light component steam warp
Vapour compression machine supercharging heating is crossed, the light component steam after compression is used as the thermal source of reboiler, the condensed device of reboiler discharge liquor
It is divided into two parts, part discharge, a part of phegma as rectifying column tower after cooling；
In above-mentioned 4 grades of heat pump separators, the methanol solution in the 1st grade of heat pump separator into rectifying column tower is thick first
The methanol solution for entering rectifying column tower in alcohol, the 2nd to 4 grade of heat pump separator is the rectifying column of upper level heat pump separator
The solution that the outlet of tower body is excluded.
6. methanol heat-pump rectificating method according to claim 4, it is characterised in that：The rectifying column tower operating pressure at different levels
For 100kPa-800kPa, reflux ratio is 1.5-5；Described vapour compression machine, compression ratio is 1.5-3.63.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201710243313.3A CN106957214A (en) | 2017-04-14 | 2017-04-14 | Methanol heat-pump distillation system and method |
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| CN201710243313.3A CN106957214A (en) | 2017-04-14 | 2017-04-14 | Methanol heat-pump distillation system and method |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107694138A (en) * | 2017-10-11 | 2018-02-16 | 肥城金威机械有限公司 | Rectifier unit, method and its application for fusel oil |
| CN109665940A (en) * | 2019-01-07 | 2019-04-23 | 天津乐科节能科技有限公司 | Methanol is from backheat distillation system and application |
| CN109745724A (en) * | 2019-01-24 | 2019-05-14 | 山东伯仲真空设备股份有限公司 | MVR rectifying stripping set composite and its process |
| CN110963890A (en) * | 2019-12-30 | 2020-04-07 | 中国天辰工程有限公司 | Refining method of gaseous methanol |
| CN111995499A (en) * | 2020-08-26 | 2020-11-27 | 吴嘉 | Methanol heat pump rectification method and device |
| CN113024354A (en) * | 2019-12-09 | 2021-06-25 | 中国科学院大连化学物理研究所 | Heat pump rectification system for dehydrating biomass ethylene glycol |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101786940A (en) * | 2010-03-05 | 2010-07-28 | 惠生工程（中国）有限公司 | Methanol heat-pump rectifying process |
| CN103566613A (en) * | 2012-08-06 | 2014-02-12 | 南通醋酸纤维有限公司 | Rectification device and process for low-concentration organic solvent aqueous liquor recycling heat pump |
| CN105669362A (en) * | 2016-03-14 | 2016-06-15 | 江苏乐科节能科技股份有限公司 | Trichloromethane solvent recovery heat pump rectification process |
| CN105669412A (en) * | 2016-03-14 | 2016-06-15 | 江苏乐科节能科技股份有限公司 | Acetone solvent recovery heat-pump distillation technology |
| CN105749573A (en) * | 2016-03-14 | 2016-07-13 | 江苏乐科节能科技股份有限公司 | Heat-pump distillation system, heat-pump distillation method and application of heat-pump distillation method to ethanol recovery |
| CN205549650U (en) * | 2016-03-14 | 2016-09-07 | 江苏乐科节能科技股份有限公司 | Heat pump rectification system |
-
2017
- 2017-04-14 CN CN201710243313.3A patent/CN106957214A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101786940A (en) * | 2010-03-05 | 2010-07-28 | 惠生工程（中国）有限公司 | Methanol heat-pump rectifying process |
| CN103566613A (en) * | 2012-08-06 | 2014-02-12 | 南通醋酸纤维有限公司 | Rectification device and process for low-concentration organic solvent aqueous liquor recycling heat pump |
| CN105669362A (en) * | 2016-03-14 | 2016-06-15 | 江苏乐科节能科技股份有限公司 | Trichloromethane solvent recovery heat pump rectification process |
| CN105669412A (en) * | 2016-03-14 | 2016-06-15 | 江苏乐科节能科技股份有限公司 | Acetone solvent recovery heat-pump distillation technology |
| CN105749573A (en) * | 2016-03-14 | 2016-07-13 | 江苏乐科节能科技股份有限公司 | Heat-pump distillation system, heat-pump distillation method and application of heat-pump distillation method to ethanol recovery |
| CN205549650U (en) * | 2016-03-14 | 2016-09-07 | 江苏乐科节能科技股份有限公司 | Heat pump rectification system |
Non-Patent Citations (1)
| Title |
|---|
| 叶鑫等: "甲醇热泵精馏新工艺", 《化工进展》 * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107694138A (en) * | 2017-10-11 | 2018-02-16 | 肥城金威机械有限公司 | Rectifier unit, method and its application for fusel oil |
| CN109665940A (en) * | 2019-01-07 | 2019-04-23 | 天津乐科节能科技有限公司 | Methanol is from backheat distillation system and application |
| CN109745724A (en) * | 2019-01-24 | 2019-05-14 | 山东伯仲真空设备股份有限公司 | MVR rectifying stripping set composite and its process |
| CN113024354A (en) * | 2019-12-09 | 2021-06-25 | 中国科学院大连化学物理研究所 | Heat pump rectification system for dehydrating biomass ethylene glycol |
| CN110963890A (en) * | 2019-12-30 | 2020-04-07 | 中国天辰工程有限公司 | Refining method of gaseous methanol |
| CN110963890B (en) * | 2019-12-30 | 2024-04-16 | 中国天辰工程有限公司 | Refining method of gaseous methanol |
| CN111995499A (en) * | 2020-08-26 | 2020-11-27 | 吴嘉 | Methanol heat pump rectification method and device |
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