CN102898276A - Method and device for recycling propanediol and dipropylene glycol from propanediol kettle residual liquid - Google Patents
Method and device for recycling propanediol and dipropylene glycol from propanediol kettle residual liquid Download PDFInfo
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- CN102898276A CN102898276A CN2012103794757A CN201210379475A CN102898276A CN 102898276 A CN102898276 A CN 102898276A CN 2012103794757 A CN2012103794757 A CN 2012103794757A CN 201210379475 A CN201210379475 A CN 201210379475A CN 102898276 A CN102898276 A CN 102898276A
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Abstract
The invention discloses a method for recycling propanediol and dipropylene glycol from propanediol kettle residual liquid, which comprises steps as follows: (a) heat-conducting oil preheated to specified temperature is input into a jacket of a double-shaft stirring reboiler through a heat-conducting oil inlet; (b) propanediol and dipropylene glycol steam enters a propanediol rectification tower from a steam outlet of the double-shaft stirring reboiler via a pipeline; (c) after the propanediol and dipropylene glycol mixture is heated by a bottom reboiler of the propanediol rectification tower, gas-phase propanediol is condensed into liquid by an overhead condenser, and the liquid flows into a propanediol collecting tank; and (d) the dipropylene glycol enriched on the bottom of the propanediol tower enters a dipropylene glycol rectification tower through a pipeline, and is heated by a bottom reboiler of the dipropylene glycol rectification tower, the gas-phase dipropylene glycol is condensed into liquid by an overhead condenser, and the liquid flows into a dipropylene glycol collecting tank. The method can be used for recycling all propanediol and dipropylene glycol.
Description
Technical field
The present invention relates to a kind ofly can all reclaim propylene glycol in the propylene glycol still kettle raffinate and method and the device of dipropylene glycol.
Background technology
Propylene glycol be unsaturated polyester, Resins, epoxy, urethane resin important source material, the consumption of this respect accounts for about 45% of propylene glycol aggregate consumption, this unsaturated polyester is used for topcoating and reinforced plastics in a large number.The viscosity of propylene glycol and good hygroscopicity, and nontoxic, thereby in food, medicine and cosmetic industry, be widely used as moisture adsorbent, antifreezing agent, lubricant and solvent.In foodstuffs industry, propylene glycol and fatty acid response generate propylene glycol fatty acid ester, mainly as food emulsifier; Propylene glycol is the fine solvent of seasonings and pigment.Propylene glycol is commonly used for solvent, tenderizer and the vehicle etc. of making all kinds of ointment, ointment in medicine industry, because propylene glycol has better mutual solubility with all kinds of spices, thereby also be used as the solvent of makeup and tenderizer etc.Propylene glycol is also as tobacco moistening agent, mould inhibitor, the solvent of food processing plant lubricating oil and food labeling printing ink.The aqueous solution of propylene glycol is effective antifreezing agent.
As the byproduct of methylcarbonate production equipment, the refining distillation operation that usually adopts of propylene glycol.Often contain the propylene glycol of 10-15% and a contracting dipropylene glycol of about 80% during rectifying still is residual, this still residue amount accounts for about 10% of propanediol.For reclaiming the propylene glycol of rectifying still in residual, usually adopt the batch fractionating operation, as shown in Figure 1, rectifier bottoms connects a reboiler, the propylene glycol distillation still residue that disposable input is a large amount of, by the material in the heating medium for heating reboiler, product component becomes gas phase and enters rectifying tower, through overhead condenser condensation extraction, in this process under the different service temperature, collect the cut of different boiling ranges, be collected into respectively in the corresponding products pot, guarantee the rate of recovery and product purity, front-end volatiles and after cut add again again carries out multiple steaming in the reboiler, this method separation efficiency is low, and energy consumption is high; In the propylene glycol rectifying still of carbonate device by-product, have carbonate, if a contracting propylene glycol is steamed only, will separate out the carbonate solid in reboiler, the equipment such as interchanger result in blockage.This tradition reclaims the method for propylene glycol and dipropylene glycol, the product component in the propylene glycol distillation still residue all can not be reclaimed, and has increased enterprise's production cost, and the waste sludge discharge amount is large, contaminate environment.
Summary of the invention
The object of the invention is to overcome the shortcoming of prior art, provide a kind of product recovery rate high, energy-conservation and reduce propylene glycol in whole recovery propylene glycol still raffinates of solid waste quantity discharged and method and the device of dipropylene glycol.
Propylene glycol in the recovery propylene glycol still raffinate of the present invention and the method for dipropylene glycol, it may further comprise the steps:
(a) preheating thermal oil to 220～250 ℃, open hot oil pump, be input to the thermal oil that is preheating to assigned temperature in the chuck of Double shaft stirring reboiler by heat conductive oil inlet, after the heat exchange, then return the deep fat tank through pipeline from thermal oil outlet outflow and recycle, in propylene glycol rectifying tower and dipropylene glycol rectifying tower condenser, pass into water coolant simultaneously;
(b) when Double shaft stirring reboiler temperature in the kettle reaches the service temperature of design, propylene glycol still raffinate is disposable or press design discharge from Double shaft stirring reboiler throat-fed, open simultaneously agitator motor, red-tape operati pressure, propylene glycol and dipropylene glycol steam enter the propylene glycol rectifying tower from the vapour outlet of Double shaft stirring reboiler through pipeline, propylene glycol and dipropylene glycol are steamed the salt of only separating out, and push to the deslagging tank by the stir shaft of Double shaft stirring reboiler through slag-drip opening;
(c) propylene glycol and dipropylene glycol mixture are after the tower bottom reboiler heating of described propylene glycol rectifying tower, the gas phase propylene glycol is condensed into liquid through overhead condenser and flows in the propylene glycol holding tank, dipropylene glycol is enriched in the propylene glycol tower bottom of rectifying tower, the cat head service temperature of described propylene glycol rectifying tower is 85～100 ℃, and the cat head working pressure is 1～10KPa;
(d) dipropylene glycol that is enriched in described propylene glycol Tata still enters the dipropylene glycol rectifying tower by pipeline, heat through dipropylene glycol rectifying tower tower bottom reboiler, the gas phase dipropylene glycol is condensed into liquid through overhead condenser and flows in the dipropylene glycol holding tank, organic heavy seeds is enriched in the dipropylene glycol tower reactor, intermittently put clean, described dipropylene glycol rectifying tower cat head service temperature is 115～130 ℃, and the cat head working pressure is 1～10KPa.
Propylene glycol in the recovery propylene glycol still raffinate of the present invention and the device of dipropylene glycol, it comprises the Double shaft stirring reboiler, the propylene glycol rectifying tower, the dipropylene glycol rectifying tower, the rotating shaft of described Double shaft stirring reboiler links to each other with the output shaft of agitator motor, at described Double shaft stirring reboiler housing overcoat chuck is arranged, have heat conductive oil inlet at described chuck, the thermal oil outlet, have opening for feed at described Double shaft stirring reboiler housing, slag-drip opening and vapour outlet, described vapour outlet links to each other with the side entry feed mouth of propylene glycol rectifying tower by the discharging pipeline, cat head at described propylene glycol rectifying tower and dipropylene glycol rectifying tower is connected with respectively condenser, at the bottom of the tower of described propylene glycol rectifying tower and dipropylene glycol rectifying tower, be connected with respectively reboiler, the cat head discharge port of described propylene glycol rectifying tower links to each other with the propylene glycol holding tank, the cat head discharge port of described dipropylene glycol rectifying tower links to each other with the dipropylene glycol holding tank, and discharge port links to each other with the side entry feed mouth of dipropylene glycol rectifying tower by pipeline at the bottom of the tower of described propylene glycol rectifying tower.
Adopt beneficial effect of the present invention:
A) present, the production capacity of China's propylene glycol is more than 40 ten thousand tons, the amount of the still raffinate that can't process that produces is calculated by 10% of output, wherein, callable propylene glycol has 8000 tons approximately, and dipropylene glycol has 28000 tons approximately, by the existing market calculation of price, adopt the present invention to reclaim that the method for propylene glycol and dipropylene glycol reclaims whole propylene glycol and dipropylene glycol in the propylene glycol distillation still residue, it is 35,000 ten thousand yuan that the direct economy of its generation is worth;
B) adopt the present invention to reclaim the method for propylene glycol and dipropylene glycol in the propylene glycol distillation still residue, can effectively reduce the quantity discharged of waste residue, the level of residue of discharging only is 10% of traditional technology, and be bar-shaped solid after the residue cooling, very easily process, workman's Working environment improves, and has reduced labour intensity;
C) adopt the present invention to reclaim the method for propylene glycol and dipropylene glycol in the propylene glycol distillation still residue, avoid the situation of the carbonate occluding device of separating out to occur, thereby realize continuous temperature production, enhance productivity;
Description of drawings
Fig. 1 is traditional technology device sketch;
Fig. 2 is the process flow diagram that the present invention reclaims the method for propylene glycol and dipropylene glycol in the propylene glycol distillation still residue.
Embodiment
Below in conjunction with the drawings and specific embodiments the present invention is done to describe in detail.
Reclaim the process flow diagram of the method for propylene glycol and dipropylene glycol in the propylene glycol distillation still residue in conjunction with Fig. 2, operation steps of the present invention comprises: (a) preheating thermal oil to 220～250 ℃, open hot oil pump, be input to the thermal oil that is preheating to assigned temperature in the chuck of Double shaft stirring reboiler 1 by heat conductive oil inlet 8, after the heat exchange, then return the deep fat tank through pipeline from thermal oil outlet 9 outflows and recycle, in propylene glycol rectifying tower and dipropylene glycol rectifying tower condenser, pass into water coolant simultaneously; (b) when Double shaft stirring reboiler 1 temperature in the kettle reaches the service temperature (service temperature can be determined according to analog calculation) of design, propylene glycol still raffinate is disposable or press design discharge from 10 chargings of Double shaft stirring reboiler opening for feed, open simultaneously agitator motor 7, red-tape operati pressure (working pressure can be determined according to the analog calculation result), propylene glycol and dipropylene glycol steam enter propylene glycol rectifying tower 2 from the vapour outlet 12 of Double shaft stirring reboiler 1 through pipeline, and the salt that propylene glycol and dipropylene glycol steaming are separated out only pushes to deslagging tank 6 by the stir shaft of Double shaft stirring reboiler 1 through slag-drip opening; (c) propylene glycol and dipropylene glycol mixture are after the tower bottom reboiler heating of described propylene glycol rectifying tower 2, the gas phase propylene glycol is condensed into liquid through overhead condenser and flows in the propylene glycol holding tank 4, dipropylene glycol is enriched in the propylene glycol tower bottom of rectifying tower, the cat head service temperature of described propylene glycol rectifying tower is 85～100 ℃, and the cat head working pressure is 1～10KPa; (d) dipropylene glycol that is enriched in described propylene glycol Tata still enters dipropylene glycol rectifying tower 3 by pipeline, heat through dipropylene glycol rectifying tower tower bottom reboiler, the gas phase dipropylene glycol is condensed into liquid through overhead condenser and flows in the dipropylene glycol holding tank 5, organic heavy seeds is enriched in the dipropylene glycol tower reactor, intermittently put clean, described dipropylene glycol rectifying tower cat head service temperature is 115～130 ℃, and the cat head working pressure is 1～10KPa.The Double shaft stirring reboiler that method of the present invention adopts is the disclosed device of ZL200810053594.7.
The reflux ratio of preferred described propylene glycol rectifying tower is 1～10, and the reflux ratio of described dipropylene glycol rectifying tower is 1～10.
As the propylene glycol in the recovery propylene glycol still raffinate of a kind of embodiment of the inventive method and the device of dipropylene glycol, it comprises Double shaft stirring reboiler 1, propylene glycol rectifying tower 2, dipropylene glycol rectifying tower 3, the rotating shaft of described Double shaft stirring reboiler 1 links to each other with the output shaft of agitator motor 7, at described Double shaft stirring reboiler 1 housing overcoat chuck is arranged, have heat conductive oil inlet 8 at described chuck, thermal oil outlet 9, have opening for feed 10 at described Double shaft stirring reboiler 1 housing, slag-drip opening 11 and vapour outlet 12, described vapour outlet 12 links to each other with the side entry feed mouth of propylene glycol rectifying tower 2 by the discharging pipeline, cat head at described propylene glycol rectifying tower 2 and dipropylene glycol rectifying tower 3 is connected with respectively condenser, at the bottom of the tower of described propylene glycol rectifying tower 2 and dipropylene glycol rectifying tower 3, be connected with respectively reboiler, the cat head discharge port of described propylene glycol rectifying tower 2 links to each other with propylene glycol holding tank 4, the cat head discharge port of described dipropylene glycol rectifying tower 2 links to each other with dipropylene glycol holding tank 5, and discharge port links to each other with the side entry feed mouth of dipropylene glycol rectifying tower 3 by pipeline at the bottom of the tower of described propylene glycol rectifying tower 2.
The rectifying section bed stuffing height of preferred described propylene glycol rectifying tower is 3～5 meters, and the stripping section bed stuffing height is 3～5 meters; Described dipropylene glycol rectifying tower rectifying section bed stuffing height is 4～6 meters, and the bed stuffing height of stripping section is 4～6 meters.Column internals selects structured packing, and its pressure drop is little, and energy consumption is low, and separation efficiency is high.
The filler of preferred described propylene glycol rectifying tower and dipropylene glycol rectifying tower selects corrugated plate packing 350Y, 500Y, also can select screen waviness packings BX, CY.
Embodiment 1
A) preheating thermal oil to 220 ℃, open hot oil pump, be input to the thermal oil that is preheating to assigned temperature in the chuck of Double shaft stirring reboiler 1 by heat conductive oil inlet 8, after the heat exchange, flow out from thermal oil outlet 9, return the deep fat tank through pipeline and recycle, in propylene glycol rectifying tower and dipropylene glycol rectifying tower condenser, pass into water coolant; B) when Double shaft stirring reboiler 1 temperature in the kettle reaches 120 ℃, from 1.0 kilograms of propylene glycol stills of Double shaft stirring reboiler opening for feed 10 chargings raffinate, open simultaneously agitator motor 7, red-tape operati pressure is 1KPa, propylene glycol and dipropylene glycol steam enter propylene glycol rectifying tower 2 from the vapour outlet 12 of Double shaft stirring reboiler 1 through pipeline, propylene glycol and dipropylene glycol are steamed the salt of only separating out, and push to deslagging tank 6 by the stir shaft of Double shaft stirring reboiler 1 through slag-drip opening; C) propylene glycol and dipropylene glycol mixture are after the tower bottom reboiler heating of described propylene glycol rectifying tower 2, the gas phase propylene glycol is condensed into liquid through overhead condenser and flows in the propylene glycol holding tank 4, dipropylene glycol is enriched in the propylene glycol tower bottom of rectifying tower, described propylene glycol rectifying tower cat head service temperature is 85 ℃, and working pressure is 1KPa; The reflux ratio of described propylene glycol rectifying tower is 10, d) dipropylene glycol that is enriched in described propylene glycol Tata still enters dipropylene glycol rectifying tower 3 by pipeline, heat through tower bottom reboiler, the gas phase dipropylene glycol is condensed into liquid through overhead condenser and flows in the dipropylene glycol holding tank 5, organic heavy seeds is enriched in the dipropylene glycol tower reactor, intermittently put only, described dipropylene glycol rectifying tower cat head service temperature is 115 ℃, and working pressure is 1KPa.The reflux ratio of described dipropylene glycol rectifying tower is 10.
Analyze after testing, the mass percent purity of propylene glycol and dipropylene glycol reaches more than 99%, discharges the content of product component in the residue below 0.5%.
Embodiment 2
2.a) preheating thermal oil to 240 ℃, open hot oil pump, be input to the thermal oil that is preheating to assigned temperature in the chuck of Double shaft stirring reboiler 1 by heat conductive oil inlet 8, after the heat exchange, flow out from thermal oil outlet 9, return the deep fat tank through pipeline and recycle, in propylene glycol rectifying tower and dipropylene glycol rectifying tower condenser, pass into water coolant; B) when Double shaft stirring reboiler 1 temperature in the kettle reaches 120 ℃ of design, from 1.5 kilograms of propylene glycol stills of Double shaft stirring reboiler opening for feed 10 chargings raffinate, open simultaneously agitator motor 7, red-tape operati pressure is 5KPa, propylene glycol and dipropylene glycol steam enter propylene glycol rectifying tower 2 from the vapour outlet 12 of Double shaft stirring reboiler 1 through pipeline, because propylene glycol and dipropylene glycol are steamed the salt of only separating out, push to deslagging tank 6 by the stir shaft of Double shaft stirring reboiler 1 through slag-drip opening; C) propylene glycol and dipropylene glycol mixture are after the tower bottom reboiler heating of described propylene glycol rectifying tower 2, the gas phase propylene glycol is condensed into liquid through overhead condenser and flows in the propylene glycol holding tank 4, dipropylene glycol is enriched in the propylene glycol tower bottom of rectifying tower, described propylene glycol rectifying tower cat head service temperature is 92 ℃, and working pressure is 5KPa; The reflux ratio of described propylene glycol rectifying tower is 5, d) dipropylene glycol that is enriched in described propylene glycol Tata still enters dipropylene glycol rectifying tower 3 by pipeline, heat through tower bottom reboiler, the gas phase dipropylene glycol is condensed into liquid through overhead condenser and flows in the dipropylene glycol holding tank 5, organic heavy seeds is enriched in the dipropylene glycol tower reactor, intermittently put only, described dipropylene glycol rectifying tower cat head service temperature is 125 ℃, and working pressure is 5KPa.The reflux ratio of described dipropylene glycol rectifying tower is 5.
3. analyze after testing, the mass percent purity of propylene glycol and dipropylene glycol mixture reaches more than 99%, discharges the content of product component in the residue below 0.5%.
Embodiment 3
4.a) preheating thermal oil to 250 ℃, open hot oil pump, be input to the thermal oil that is preheating to assigned temperature in the chuck of Double shaft stirring reboiler 1 by heat conductive oil inlet 8, after the heat exchange, flow out from thermal oil outlet 9, return the deep fat tank through pipeline and recycle, in propylene glycol rectifying tower and dipropylene glycol rectifying tower condenser, pass into water coolant; B) when Double shaft stirring reboiler 1 temperature in the kettle reaches 120 ℃ of design, from Double shaft stirring reboiler opening for feed 10 with 0.5 kg/hour flow charging propylene glycol still raffinate 2 hours, open simultaneously agitator motor 7, control pressure is at 10KPa, propylene glycol and dipropylene glycol steam enter propylene glycol rectifying tower 2 from the vapour outlet 12 of Double shaft stirring reboiler 1 through pipeline, because propylene glycol and dipropylene glycol are steamed the salt of only separating out, push to deslagging tank 6 by the stir shaft of Double shaft stirring reboiler 1 through slag-drip opening; C) propylene glycol and dipropylene glycol mixture are after the tower bottom reboiler heating of described propylene glycol rectifying tower 2, the gas phase propylene glycol is condensed into liquid through overhead condenser and flows in the propylene glycol holding tank 4, dipropylene glycol is enriched in the propylene glycol tower bottom of rectifying tower, described propylene glycol rectifying tower cat head service temperature is 100 ℃, and working pressure is 10KPa; The reflux ratio of described propylene glycol rectifying tower is 1.D) dipropylene glycol that is enriched in described propylene glycol Tata still enters dipropylene glycol rectifying tower 3 by pipeline, heat through tower bottom reboiler, the gas phase dipropylene glycol is condensed into liquid through overhead condenser and flows in the dipropylene glycol holding tank 5, organic heavy seeds is enriched in the dipropylene glycol tower reactor, intermittently put clean, described dipropylene glycol rectifying tower cat head service temperature is 130 ℃, and working pressure is 10KPa, and the reflux ratio of described dipropylene glycol rectifying tower is 1.
Analyze after testing, the mass percent purity of propylene glycol and dipropylene glycol mixture reaches more than 99%, discharges the content of product component in the residue below 0.5%.
Claims (5)
1. reclaim propylene glycol in the propylene glycol still raffinate and the method for dipropylene glycol, it is characterized in that it may further comprise the steps:
(a) preheating thermal oil to 220～250 ℃, open hot oil pump, be input to the thermal oil that is preheating to assigned temperature in the chuck of Double shaft stirring reboiler by heat conductive oil inlet, after the heat exchange, then return the deep fat tank through pipeline from thermal oil outlet outflow and recycle, in propylene glycol rectifying tower and dipropylene glycol rectifying tower condenser, pass into water coolant simultaneously;
(b) when Double shaft stirring reboiler temperature in the kettle reaches the service temperature of design, propylene glycol still raffinate is disposable or press design discharge from Double shaft stirring reboiler throat-fed, open simultaneously agitator motor, red-tape operati pressure, propylene glycol and dipropylene glycol steam enter the propylene glycol rectifying tower from the vapour outlet of Double shaft stirring reboiler through pipeline, propylene glycol and dipropylene glycol are steamed the salt of only separating out, and push to the deslagging tank by the stir shaft of Double shaft stirring reboiler through slag-drip opening;
(c) propylene glycol and dipropylene glycol mixture are after the tower bottom reboiler heating of described propylene glycol rectifying tower, the gas phase propylene glycol is condensed into liquid through overhead condenser and flows in the propylene glycol holding tank, dipropylene glycol is enriched in the propylene glycol tower bottom of rectifying tower, the cat head service temperature of described propylene glycol rectifying tower is 85～100 ℃, and the cat head working pressure is 1～10KPa;
(d) dipropylene glycol that is enriched in described propylene glycol Tata still enters the dipropylene glycol rectifying tower by pipeline, heat through dipropylene glycol rectifying tower tower bottom reboiler, the gas phase dipropylene glycol is condensed into liquid through overhead condenser and flows in the dipropylene glycol holding tank, organic heavy seeds is enriched in the dipropylene glycol tower reactor, intermittently put clean, described dipropylene glycol rectifying tower cat head service temperature is 115～130 ℃, and the cat head working pressure is 1～10KPa.
2. the propylene glycol in the recovery propylene glycol still raffinate according to claim 1 and the method for dipropylene glycol, it is characterized in that: the reflux ratio of described propylene glycol rectifying tower is 1～10, the reflux ratio of described dipropylene glycol rectifying tower is 1～10.
3. realize propylene glycol in the recovery propylene glycol still raffinate of claim 1 method and the device of dipropylene glycol, it is characterized in that: it comprises the Double shaft stirring reboiler, the propylene glycol rectifying tower, the dipropylene glycol rectifying tower, the rotating shaft of described Double shaft stirring reboiler links to each other with the output shaft of agitator motor, at described Double shaft stirring reboiler housing overcoat chuck is arranged, have heat conductive oil inlet at described chuck, the thermal oil outlet, have opening for feed at described Double shaft stirring reboiler housing, slag-drip opening and vapour outlet, described vapour outlet links to each other with the side entry feed mouth of propylene glycol rectifying tower by the discharging pipeline, cat head at described propylene glycol rectifying tower and dipropylene glycol rectifying tower is connected with respectively condenser, at the bottom of the tower of described propylene glycol rectifying tower and dipropylene glycol rectifying tower, be connected with respectively reboiler, the cat head discharge port of described propylene glycol rectifying tower links to each other with the propylene glycol holding tank, the cat head discharge port of described dipropylene glycol rectifying tower links to each other with the dipropylene glycol holding tank, and discharge port links to each other with the side entry feed mouth of dipropylene glycol rectifying tower by pipeline at the bottom of the tower of described propylene glycol rectifying tower.
4. the propylene glycol in the recovery propylene glycol still raffinate according to claim 3 and the device of dipropylene glycol, it is characterized in that: the rectifying section bed stuffing height of described propylene glycol rectifying tower is 3～5 meters, the stripping section bed stuffing height is 3～5 meters; Described dipropylene glycol rectifying tower rectifying section bed stuffing height is 4～6 meters, and the bed stuffing height of stripping section is 4～6 meters.
5. the propylene glycol in the recovery propylene glycol still raffinate according to claim 4 and the device of dipropylene glycol is characterized in that: the filler of described propylene glycol rectifying tower and dipropylene glycol rectifying tower is corrugated plate packing or is screen waviness packings.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012103794757A CN102898276A (en) | 2012-09-29 | 2012-09-29 | Method and device for recycling propanediol and dipropylene glycol from propanediol kettle residual liquid |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2012103794757A CN102898276A (en) | 2012-09-29 | 2012-09-29 | Method and device for recycling propanediol and dipropylene glycol from propanediol kettle residual liquid |
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| CN2012103794757A Pending CN102898276A (en) | 2012-09-29 | 2012-09-29 | Method and device for recycling propanediol and dipropylene glycol from propanediol kettle residual liquid |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115697549A (en) * | 2020-06-26 | 2023-02-03 | 利安德化学技术有限公司 | Use of monopropylene glycol from a purge stream in the preparation of an epoxidation catalyst |
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|---|---|---|---|---|
| US3574772A (en) * | 1968-10-25 | 1971-04-13 | Halcon International Inc | Preparation of pure mono- and dipropylene glycol by plural stage distillation with side stream recovery |
| DE2831210A1 (en) * | 1978-07-15 | 1980-01-24 | Huels Chemische Werke Ag | METHOD FOR PURIFYING ETHYLDIGLYCOL AND DIPROPYLENE GLYCOL |
| US20050085673A1 (en) * | 2003-10-15 | 2005-04-21 | Krishnan Viswanathan | Tripropylene glycol production |
| CN1304384C (en) * | 2002-07-23 | 2007-03-14 | 巴斯福股份公司 | Method for the continuous production of propylene glycol |
| CN101774888A (en) * | 2009-12-24 | 2010-07-14 | 山东海科化工集团有限公司 | Novel technique for purifying high-quality propylene glycol in production process of dimethyl carbonate |
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2012
- 2012-09-29 CN CN2012103794757A patent/CN102898276A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3574772A (en) * | 1968-10-25 | 1971-04-13 | Halcon International Inc | Preparation of pure mono- and dipropylene glycol by plural stage distillation with side stream recovery |
| DE2831210A1 (en) * | 1978-07-15 | 1980-01-24 | Huels Chemische Werke Ag | METHOD FOR PURIFYING ETHYLDIGLYCOL AND DIPROPYLENE GLYCOL |
| CN1304384C (en) * | 2002-07-23 | 2007-03-14 | 巴斯福股份公司 | Method for the continuous production of propylene glycol |
| US20050085673A1 (en) * | 2003-10-15 | 2005-04-21 | Krishnan Viswanathan | Tripropylene glycol production |
| CN101774888A (en) * | 2009-12-24 | 2010-07-14 | 山东海科化工集团有限公司 | Novel technique for purifying high-quality propylene glycol in production process of dimethyl carbonate |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115697549A (en) * | 2020-06-26 | 2023-02-03 | 利安德化学技术有限公司 | Use of monopropylene glycol from a purge stream in the preparation of an epoxidation catalyst |
| US11806701B2 (en) | 2020-06-26 | 2023-11-07 | Lyondell Chemical Technology, L.P. | Use of monopropylene glycol from purge streams in epoxidation catalyst preparation |
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Application publication date: 20130130 |