CN2873777Y - Production device for synthesizing propylene carbonate from urea and propylene glycol - Google Patents
Production device for synthesizing propylene carbonate from urea and propylene glycol Download PDFInfo
- Publication number
- CN2873777Y CN2873777Y CN 200520129833 CN200520129833U CN2873777Y CN 2873777 Y CN2873777 Y CN 2873777Y CN 200520129833 CN200520129833 CN 200520129833 CN 200520129833 U CN200520129833 U CN 200520129833U CN 2873777 Y CN2873777 Y CN 2873777Y
- Authority
- CN
- China
- Prior art keywords
- pipeline
- reactor
- inlet
- urea
- return channel
- 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.)
- Expired - Lifetime
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- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 title claims abstract description 66
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 239000004202 carbamide Substances 0.000 title claims abstract description 22
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 22
- 230000002194 synthesizing effect Effects 0.000 title claims description 19
- RUOJZAUFBMNUDX-UHFFFAOYSA-N propylene carbonate Chemical compound CC1COC(=O)O1 RUOJZAUFBMNUDX-UHFFFAOYSA-N 0.000 title abstract description 6
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000011084 recovery Methods 0.000 claims abstract description 12
- 239000007788 liquid Substances 0.000 claims abstract description 11
- 239000003054 catalyst Substances 0.000 claims abstract description 10
- 238000009833 condensation Methods 0.000 claims abstract description 7
- 230000005494 condensation Effects 0.000 claims abstract description 7
- -1 acrylic ester Chemical class 0.000 claims description 18
- 238000012360 testing method Methods 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 abstract description 8
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 abstract description 3
- KMTRUDSVKNLOMY-UHFFFAOYSA-N Ethylene carbonate Chemical compound O=C1OCCO1 KMTRUDSVKNLOMY-UHFFFAOYSA-N 0.000 abstract description 3
- 238000010992 reflux Methods 0.000 abstract 3
- 238000000926 separation method Methods 0.000 abstract 1
- 230000000694 effects Effects 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000029058 respiratory gaseous exchange Effects 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 208000027418 Wounds and injury Diseases 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 208000014674 injury Diseases 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses urea and propylene glycol synthetic propylene carbonate's apparatus for producing, including reactor, condensation receiving system, vacuum system and catalyst separation recovery system. The condensation receiving system comprises a heat exchanger and a reaction kettle reflux device. A liquid seal is arranged on a pipeline between the liquid outlet of the reaction kettle reflux device and the inlet of the reaction kettle. The upper end of the reaction kettle reflux device is provided with an inlet of a pipeline connection vacuum system. The bottom discharge port of the reaction kettle is connected with the inlet of a catalyst centrifugal separator through a pipeline, and one outlet of the centrifugal separator is connected with an ethylene glycol tank. A metering tank is arranged on a pipeline between the ethylene glycol pump and the reaction kettle. The device meets the requirements of the production process, achieves high product yield and good selectivity, and can recycle the excessive alcohol; the catalyst is easy to recover. The yield of propylene carbonate synthesized by the device is more than 95%, and the yield of ethylene carbonate is more than 80%.
Description
Affiliated technical field
The utility model relates to a kind of chemical industry synthesizer, particularly the production equipment of urea and propylene glycol synthesizing acrylic ester.Comprise that mainly reactor, condensation accept system, vacuum system and catalyst separating recovery system.
Background technology
Patent CN1421431A discloses the synthesis technique of urea and propylene glycol synthesizing acrylic ester, and the synthesis technique of catalyzer development in this patent and urea and propylene glycol synthesizing acrylic ester is in the leading level in the world.But only rest on laboratory stage, do not have suitability for industrialized production, do not have the device of the synthesis technique of a kind of suitable urea and propylene glycol synthesizing acrylic ester, the separating and reclaiming device of catalyzer also needs to do further research.
The utility model production equipment structure, catalyst separating retrieving arrangement to urea and propylene glycol synthesizing acrylic ester on the basis of patent of invention CN1421431A technology designs, studies, obtain good effect, promoted the suitability for industrialized production of urea and propylene glycol synthesizing acrylic ester.
Summary of the invention
The purpose of this utility model provides the production equipment of a kind of urea and propylene glycol synthesizing acrylic ester, comprises the separating and reclaiming device of supporting with it catalyzer, with urea and the propylene glycol synthesizing acrylic ester suitability for industrialized production that adapts to the recent studies on success.Satisfy the requirement of production technique, make to be reflected under the condition of negative pressure and carry out; Reach the product yield height, selectivity is good, and excessive alcohol recycles, and internal circulating load is little; Catalyzer reclaims easily.And more than 95%, the yield of NSC 11801 is more than 80% by this yield that installs the synthetic propylene carbonate.
The production equipment of urea described in the utility model and propylene glycol synthesizing acrylic ester comprises reactor, condensation receiving system, vacuum system and the catalyst separating recovery system that has agitator.Condensate recovery system comprises interchanger and reactor return channel, and the interchanger liquid outlet has pipeline ligation still return channel inlet.Reactor return channel liquid outlet has pipeline to connect between the reactor inlet.To the pipeline between the reactor inlet, fluid-tight is installed at reactor return channel liquid outlet.Reactor return channel upper end has pipeline to connect the inlet of vacuum system.Vacuum system adopts water jet pump or vapor jet pump, promptly plays reactor return channel vacuum action, and the water tank part of squirt pump has the ammonia effect that generates in the absorption reaction process again.The concentration of byproduct ammoniacal liquor is brought up to more than 17%.Avoid ammonia directly to overflow, cause environmental pollution, to operator's injury.The catalyst separating recovery system comprises.Bottom discharge mouth pipeline at reactor connects catalyzer separating centrifuge inlet.The catalyzer separating centrifuge has two outlets.An outlet connects transferpump, becomes propylene carbonate to export through transferpump synthetic.Another outlet connects the ethylene glycol jar, collects ethylene glycol.Ethylene glycol jar pipeline connects eg pump, and the ethylene glycol that reclaims is transported to reactor, on the pipeline between eg pump and the reactor test tank is arranged, control, metering ethylene glycol add-on.
Described fluid-tight is the inverted U-shaped tube line.Inverted U-shaped tube line two ends are communicated with reactor return channel to the pipeline between the reactor.Inverted U-shaped tube line height is between the 300-600 millimeter.
In order to prevent in urea and the propylene glycol reaction process, the adularescent solid condenses in interchanger and stops up interchanger, coolant temperature in the interchanger of condensate recovery system is controlled between 30-45 ℃, and condensate recovery system adopts shell and tube heat exchanger, and heat-eliminating medium is walked shell side.Each tubulation adopts threaded pipe, the total surface area of threaded pipe is 2.5-3.0 a times of light pipe, except having good heat transfer and flow characteristics, also has unique " self-cleaning " effect, breathing vertically can make attached to the white solid on the inside pipe wall and come off, prevent that inside pipe wall from stopping up, and helps the carrying out that reacts.
The utility model effect: the production equipment structure design of the utility model urea and propylene glycol synthesizing acrylic ester has bigger improvement, makes its urea and propylene glycol synthesizing acrylic ester suitability for industrialized production to adapt to the recent studies on success.Satisfied the requirement of production technique, made to be reflected under the condition of negative pressure and carry out; Reached the product yield height, selectivity is good, and excessive alcohol recycles, and internal circulating load is little; The purpose that catalyzer reclaims easily.And reached this device synthetic propylene carbonate yield more than 95%, the yield of NSC 11801 is more than 80%.This device and overcome urea and the propylene glycol reaction process in, the adularescent solid condenses in interchanger and stops up the deficiency of interchanger; And, adopt the fluid-tight of inverted " U " type, prevent that the steam in the reactor from directly sealing in the return channel.
On manufacturing cost of the present utility model and the products production benefit, meet fully urea and propylene glycol synthesizing acrylic ester production the industry needs and produced handy and practical effect.It is a new and innovative, progressive, practical new design.
Description of drawings
Accompanying drawing is a structural representation of the present utility model, is the connection diagram of each integral part.
Among the figure, 1. eg pump, 2. ethylene glycol jar, 3. reactor, 4. agitator, 5. test tank, 6. interchanger, 7. reactor return channel, 8. fluid-tight, 9. vacuum unit, 10. transferpump, 11. catalyzer separating centrifuges.
Embodiment
In conjunction with the application drawings and Examples, further specify the utility model.
Consult accompanying drawing.The production equipment of urea and propylene glycol synthesizing acrylic ester, reactor (3) capacity that has agitator (4) is 500 liters.The interchanger of condensation receiving system (6) liquid outlet has pipeline ligation still return channel (7) inlet.Condensate recovery system adopts shell and tube heat exchanger, and heat-eliminating medium is walked shell side.Each tubulation adopts threaded pipe, the total surface area of threaded pipe is 2.5-3.0 a times of light pipe, except having good heat transfer and flow characteristics, also has unique " self-cleaning " effect, along tubular axis to breathing can make attached to the white solid on the inside pipe wall and come off, prevent that inside pipe wall from stopping up, and helps the carrying out that reacts.Reactor return channel (7) liquid outlet has pipeline to connect between reactor (3) inlet.To the pipeline between reactor (3) inlet, fluid-tight (8) is installed at reactor return channel (7) liquid outlet.Fluid-tight (8) is an inverted U-shaped tube, and " U " type pipeline two ends are communicated with to the pipeline between the reactor (3) with reactor return channel (7), and there is a valve centre.Fluid-tight (8) height is at 400 millimeters.Reactor return channel (7) upper end has pipeline to connect the inlet of vacuum unit (9).Vacuum unit (9) adopts water jet pump, and the catalyst separating recovery system comprises: the bottom discharge mouth pipeline at reactor (3) connects catalyzer separating centrifuge (11) inlet.The rotating speed of catalyzer separating centrifuge (11) is 15000 rev/mins.Catalyzer separating centrifuge (11) has two outlets.An outlet connects transferpump (10), and another outlet connects ethylene glycol jar (2), and ethylene glycol jar (2) pipeline connects eg pump (1).On the pipeline between eg pump (1) and the reactor (3), be in series with a test tank (5).
Claims (4)
1, the production equipment of a kind of urea and propylene glycol synthesizing acrylic ester, comprise the reactor that has agitator, the condensation receiving system, vacuum system and catalyst separating recovery system, it is characterized in that: the condensation receiving system comprises: interchanger (6) and reactor return channel (7), interchanger (6) liquid outlet has pipeline ligation still return channel (7) inlet, reactor return channel (7) liquid outlet has pipeline to connect between reactor (3) inlet, to the pipeline between reactor (3) inlet fluid-tight (8) is installed at reactor return channel (7) liquid outlet, reactor return channel (7) upper end has pipeline to connect the inlet of vacuum system; Vacuum system adopts water jet pump (9) or vapor jet pump (9); The catalyst separating recovery system comprises: the bottom discharge mouth pipeline at reactor (3) connects catalyzer separating centrifuge (11) inlet, catalyzer separating centrifuge (11) has two outlets, an outlet connects transferpump (10), another outlet connects ethylene glycol jar (2), ethylene glycol jar (2) pipeline connects eg pump (1), on the pipeline between eg pump (1) and the reactor (3) test tank (5) is arranged.
2, the production equipment of urea as claimed in claim 1 and propylene glycol synthesizing acrylic ester, it is characterized in that: described fluid-tight (8) is the inverted U-shaped tube line, inverted U-shaped tube line two ends are communicated with to the pipeline between the reactor (3) with reactor return channel (7), and inverted U-shaped tube line height is between the 300-600 millimeter.
3, the production equipment of urea as claimed in claim 1 or 2 and propylene glycol synthesizing acrylic ester is characterized in that: condensate recovery system adopts shell and tube heat exchanger, and each tubulation adopts threaded pipe.
4, the production equipment of urea as claimed in claim 1 or 2 and propylene glycol synthesizing acrylic ester is characterized in that: the rotating speed of catalyzer separating centrifuge (11) is at 5000-15000 rev/min.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200520129833 CN2873777Y (en) | 2005-10-18 | 2005-10-18 | Production device for synthesizing propylene carbonate from urea and propylene glycol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200520129833 CN2873777Y (en) | 2005-10-18 | 2005-10-18 | Production device for synthesizing propylene carbonate from urea and propylene glycol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2873777Y true CN2873777Y (en) | 2007-02-28 |
Family
ID=37780372
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200520129833 Expired - Lifetime CN2873777Y (en) | 2005-10-18 | 2005-10-18 | Production device for synthesizing propylene carbonate from urea and propylene glycol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2873777Y (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104059047A (en) * | 2014-07-10 | 2014-09-24 | 中国科学院山西煤炭化学研究所 | Continuous reaction technology for urea-synthesized cyclic carbonate, raw material mixer and kettle type reactor |
| CN108905908A (en) * | 2018-09-12 | 2018-11-30 | 江苏金桥油脂化工科技有限公司 | The reaction kettle system of Acrawax |
-
2005
- 2005-10-18 CN CN 200520129833 patent/CN2873777Y/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104059047A (en) * | 2014-07-10 | 2014-09-24 | 中国科学院山西煤炭化学研究所 | Continuous reaction technology for urea-synthesized cyclic carbonate, raw material mixer and kettle type reactor |
| CN104059047B (en) * | 2014-07-10 | 2016-08-24 | 中国科学院山西煤炭化学研究所 | Urea synthesizing cyclic carbonate continuous reaction process |
| CN108905908A (en) * | 2018-09-12 | 2018-11-30 | 江苏金桥油脂化工科技有限公司 | The reaction kettle system of Acrawax |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20070228 |
|
| EXPY | Termination of patent right or utility model |