CN201981142U - Process device for producing dipropylene glycol and co-producing tripropylene glycol - Google Patents
Process device for producing dipropylene glycol and co-producing tripropylene glycol Download PDFInfo
- Publication number
- CN201981142U CN201981142U CN2011201268211U CN201120126821U CN201981142U CN 201981142 U CN201981142 U CN 201981142U CN 2011201268211 U CN2011201268211 U CN 2011201268211U CN 201120126821 U CN201120126821 U CN 201120126821U CN 201981142 U CN201981142 U CN 201981142U
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- China
- Prior art keywords
- tower
- producing
- rectifying tower
- tubular reactor
- glycol
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- 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 - Fee Related
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- 238000000034 method Methods 0.000 title claims abstract description 16
- SZXQTJUDPRGNJN-UHFFFAOYSA-N dipropylene glycol Chemical compound OCCCOCCCO SZXQTJUDPRGNJN-UHFFFAOYSA-N 0.000 title claims abstract description 14
- LCZVSXRMYJUNFX-UHFFFAOYSA-N 2-[2-(2-hydroxypropoxy)propoxy]propan-1-ol Chemical compound CC(O)COC(C)COC(C)CO LCZVSXRMYJUNFX-UHFFFAOYSA-N 0.000 title claims abstract description 13
- 230000003068 static effect Effects 0.000 claims abstract description 14
- 238000002156 mixing Methods 0.000 claims abstract description 10
- 239000000463 material Substances 0.000 claims abstract description 9
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 229910000851 Alloy steel Inorganic materials 0.000 claims description 3
- 229910000975 Carbon steel Inorganic materials 0.000 claims description 3
- 239000010962 carbon steel Substances 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 abstract description 10
- 239000012530 fluid Substances 0.000 abstract description 3
- 230000035484 reaction time Effects 0.000 abstract description 3
- 238000010924 continuous production Methods 0.000 abstract description 2
- 238000006356 dehydrogenation reaction Methods 0.000 abstract 1
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 description 12
- 239000000203 mixture Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 238000000746 purification Methods 0.000 description 3
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000010923 batch production Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- -1 contains two kinds Chemical compound 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000004434 industrial solvent Substances 0.000 description 1
- 229920000570 polyether Polymers 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 235000013599 spices Nutrition 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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Classifications
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- 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
- C07C41/02—Preparation of ethers from oxiranes
- C07C41/03—Preparation of ethers from oxiranes by reaction of oxirane rings with hydroxy groups
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a process device for producing dipropylene glycol and co-producing tripropylene glycol, which comprises a material-mixing pot (1), a synthetic tower (2), a dehydrogenation tower (3), a dipropylene glycol (DPG) rectifying tower (4) and a tripropylene glycol (TPG) rectifying tower (5), wherein the synthetic tower (2) is a static tubular reactor. When the process device is adopted, a synthetic reaction is completed in the static tubular reactor. Because single-tube multi-rotation fluid mixing pipes are arranged in the static tubular reactor, materials are distributed into teams, simultaneously crossed vortex reverse rotation is generated, accordingly reacted materials are mixed quickly, the reaction time is greatly shortened, and continuous production can be realized.
Description
Technical field
The utility model relates to a kind of process unit of producing dipropylene glycol and coproduction tripropylene glycol, comprises mixing tank, synthetic tower, lightness-removing column, DPG rectifying tower, TPG rectifying tower.
Background technology
The industrial process of preparation dipropylene glycol mainly contains two kinds, and the one, a large amount of DPG by-products that produce in the polyethers production process, but its quality is lower, can only be applied to the raw materials for production of industrial solvent and some Chemicals; The 2nd, by propylene glycol and propylene oxide condensation, get through rectification under vacuum again, the by-product tripropylene glycol, the DPG content that this method makes is higher, and colourity is low, is mainly used in the field of high-quality raw materials requirement such as spices, makeup, washing composition, foodstuff additive.
Produce the process unit that dipropylene glycol adopted at present and comprise mixing tank, synthetic tower, lightness-removing column, DPG rectifying tower and TPG rectifying tower, wherein synthetic tower is a reactor.When PO and PG synthesize, operation that can only a still one still, reaction is slow, and generated time is long, the energy consumption height; And can only batch production, complex operation.
The utility model content
The technical problems to be solved in the utility model provide a kind ofly react fast, energy consumption is low, can realize that quantity-produced produces the process unit of dipropylene glycol and coproduction tripropylene glycol.
In order to solve the problems of the technologies described above, the process unit of production dipropylene glycol of the present utility model and coproduction tripropylene glycol comprises mixing tank, synthetic tower, lightness-removing column, DPG rectifying tower, TPG rectifying tower, and described synthetic tower is static tubular reactor.
The manufactured materials of described static tubular reactor, lightness-removing column, DPG rectifying tower, TPG rectifying tower is preferably carbon steel or steel alloy.
The reactions steps of material in this cover process unit is as follows:
(1) building-up reactions: propylene oxide, propylene glycol, three kinds of materials of catalyzer are mixed contact at static tubular reactor, and the mixing molar ratio is PO:PG:CAT=1:1-5:0.005-0.05, and temperature is at 130-200 ℃, and pressure is at 0.1-1.0MPa.
(2) product rectification and purification: the synthetic tower products therefrom separates purification propylene glycol, dipropylene glycol, tripropylene glycol through lightness-removing column, DPG rectifying tower, TPG rectifying tower respectively, and propylene glycol is re-used as raw material and returns reaction.
Adopt this process unit, building-up reactions is finished in static tubular reactor, establishes many rotary fluids of single tube mixing tube in the static tubular reactor, make material diversion become team, produce the reverse rotation of intersection vortex simultaneously, the reaction mass short mix, shorten the reaction times greatly, and realize continuous production.
Description of drawings
Fig. 1 is a structural representation of the present utility model.
Embodiment
Below in conjunction with accompanying drawing embodiment of the present utility model is elaborated.
Fig. 1 shows concrete structure of the present utility model.The process unit of production dipropylene glycol of the present utility model and coproduction tripropylene glycol mainly comprises mixing tank 1, synthetic tower 2, lightness-removing column 3, DPG rectifying tower 4, TPG rectifying tower 5.Wherein, synthetic tower 2 is static tubular reactor, and height is a 10-20 rice, and the pipe diameter is 200-1000mm; The tower height of lightness-removing column 3 is 8-16m, and the tower diameter is 600-2000mm; The tower height of DPG rectifying tower 4 is 10-25m, and the tower diameter is 800-2500mm; The tower height of TPG rectifying tower 5 is 8-20m, and the tower diameter is 600-2000mm.
The manufactured materials of static tubular reactor, lightness-removing column 3, DPG rectifying tower 4, TPG rectifying tower 5 is carbon steel or steel alloy.
Building-up reactions is finished in static tubular reactor, the synthetic tower product is successively through lightness-removing column 3, DPG rectifying tower 4, TPG rectifying tower 5 difference rectification and purification, it is black once finally can to make DPG purity more than 99.6%, colourity 10, TPG purity more than 99%, colourity 15 black products once, PG is re-used as the raw material Returning reacting system.
The static tubular reactor that synthetic tower 2 adopts is a kind of novel mix reaction equipment, in establish many rotary fluids of single tube mixing tube, make material diversion become team, produce simultaneously and intersect the vortex reverse rotation, with the reaction mass short mix, shorten the reaction times greatly.Simultaneously, process unit production continuity of the present utility model is strong, sufficient reacting, and stability is high, safe operation process, energy-conservation.
Claims (2)
1. process unit of producing dipropylene glycol and coproduction tripropylene glycol, comprise mixing tank (1), synthetic tower (2), lightness-removing column (3), DPG rectifying tower (4), TPG rectifying tower (5), it is characterized in that: described synthetic tower (2) is static tubular reactor.
2. the process unit of production dipropylene glycol according to claim 1 and coproduction tripropylene glycol is characterized in that: the manufactured materials of static tubular reactor, lightness-removing column (3), DPG rectifying tower (4), TPG rectifying tower (5) is carbon steel or steel alloy.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201268211U CN201981142U (en) | 2011-04-27 | 2011-04-27 | Process device for producing dipropylene glycol and co-producing tripropylene glycol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201268211U CN201981142U (en) | 2011-04-27 | 2011-04-27 | Process device for producing dipropylene glycol and co-producing tripropylene glycol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201981142U true CN201981142U (en) | 2011-09-21 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011201268211U Expired - Fee Related CN201981142U (en) | 2011-04-27 | 2011-04-27 | Process device for producing dipropylene glycol and co-producing tripropylene glycol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201981142U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2013111839A1 (en) * | 2012-01-27 | 2013-08-01 | 住友化学株式会社 | Method for producing dipropylene glycol and/or tripropylene glycol |
| EP2792663A4 (en) * | 2011-12-13 | 2015-08-05 | Sumitomo Chemical Co | Method for producing glycol from oxirane compound |
| EP2848602A4 (en) * | 2012-05-11 | 2015-12-30 | Sumitomo Chemical Co | Method for producing glycols from oxirane compound |
-
2011
- 2011-04-27 CN CN2011201268211U patent/CN201981142U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2792663A4 (en) * | 2011-12-13 | 2015-08-05 | Sumitomo Chemical Co | Method for producing glycol from oxirane compound |
| WO2013111839A1 (en) * | 2012-01-27 | 2013-08-01 | 住友化学株式会社 | Method for producing dipropylene glycol and/or tripropylene glycol |
| EP2848602A4 (en) * | 2012-05-11 | 2015-12-30 | Sumitomo Chemical Co | Method for producing glycols from oxirane compound |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 244000 Anhui city of Tongling Province Lake Road six Tongling nonferrous circular economy industrial park Patentee after: TONGLING JINTAI CHEMICAL INDUSTRIAL CO., LTD. Address before: 244000 Anhui city of Tongling Province Lake Road six Tongling nonferrous circular economy industrial park Patentee before: Tongling Jintai Chemical Industrial Co., Ltd. |
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20110921 Termination date: 20190427 |
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| CF01 | Termination of patent right due to non-payment of annual fee |