CN106512462A - Turpentine continuous rectification device - Google Patents
Turpentine continuous rectification device Download PDFInfo
- Publication number
- CN106512462A CN106512462A CN201611181343.8A CN201611181343A CN106512462A CN 106512462 A CN106512462 A CN 106512462A CN 201611181343 A CN201611181343 A CN 201611181343A CN 106512462 A CN106512462 A CN 106512462A
- Authority
- CN
- China
- Prior art keywords
- reboiler
- rectifying column
- condenser
- tower
- upper cavity
- 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.)
- Pending
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/001—Processes specially adapted for distillation or rectification of fermented solutions
- B01D3/002—Processes specially adapted for distillation or rectification of fermented solutions by continuous methods
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
- B01D3/322—Reboiler specifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C13/00—Cyclic hydrocarbons containing rings other than, or in addition to, six-membered aromatic rings
- C07C13/28—Polycyclic hydrocarbons or acyclic hydrocarbon derivatives thereof
- C07C13/32—Polycyclic hydrocarbons or acyclic hydrocarbon derivatives thereof with condensed rings
- C07C13/39—Polycyclic hydrocarbons or acyclic hydrocarbon derivatives thereof with condensed rings with a bicyclo ring system containing seven carbon atoms
- C07C13/40—Polycyclic hydrocarbons or acyclic hydrocarbon derivatives thereof with condensed rings with a bicyclo ring system containing seven carbon atoms with a bicycloheptane ring structure
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C13/00—Cyclic hydrocarbons containing rings other than, or in addition to, six-membered aromatic rings
- C07C13/28—Polycyclic hydrocarbons or acyclic hydrocarbon derivatives thereof
- C07C13/32—Polycyclic hydrocarbons or acyclic hydrocarbon derivatives thereof with condensed rings
- C07C13/39—Polycyclic hydrocarbons or acyclic hydrocarbon derivatives thereof with condensed rings with a bicyclo ring system containing seven carbon atoms
- C07C13/42—Polycyclic hydrocarbons or acyclic hydrocarbon derivatives thereof with condensed rings with a bicyclo ring system containing seven carbon atoms with a bicycloheptene ring structure
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a turpentine continuous rectification device which comprises a primary rectification device and a secondary rectification device. The primary rectification device is provided with a rectification tower AI, a condenser AI (2) and a reboiler AI (7) and further provided with a rectification tower AII (5), a condenser AII (6) and a reboiler AII (10), and the secondary rectification device is provided with a rectification tower B (3), a condenser B (4) and a reboiler B (8). The primary rectification device and the second rectification device are arranged to separate alpha-pinene and beta-pinene in turpentine, the primary rectification device is provided with the two rectification towers, and quantity of beta-pinene and the like gathered by the two rectification towers exactly meets needs of one secondary rectification tower, so that production cost and energy consumption are lowered, production efficiency is improved, continuous production can be realized, and yield and purity of alpha-pinene and beta-pinene products can be improved.
Description
Technical field
The present invention relates to compound separation equipment technical field, specifically a kind of turpentine oil continuous rectification apparatus.
Background technology
Turpentine oil is one of important silvichemical of China, is the renewable resource product of China's abundant, and yield is about
Account for global 1/4.Turpentine oil main component has australene, amphene, nopinene, laurene, limonene, p-cymene, Chinese celery
Alkene, 1, 8-Cineole, longifolene and carypohyllene etc., wherein australene, nopinene account for more than 80%.Australene and nopinene are fragrant
The important source material of material, medicine and Minute Organic Synthesis industry.Terebinthine separation and Extraction australene and nopinene are generally using essence
Technique is evaporated, rectification process is the typical unit operation of separation mutually soluble liquids mixture in Chemical Manufacture, its essence is multistage distillation,
I.e. in certain pressure with a temperature of, the boiling point or saturated vapor pressure using mutually soluble liquids mixture each component is different, makes light component
Vaporization, the vaporization of many Partial Liquid Phases of Jing and partial gas phase condensation, make heavy constituent concentration in the light component and liquid phase in gas phase by
Edge up height, so as to realize separating.
From turpentine oil, the traditional handicraft of separating-purifying firpene is：The accessory substance turpentine obtained during rosin production
Oily crude oil is clarified, filtration enters destilling tower evaporation backflow after preheating, and australene is obtained Jing after cooler refrigerated separation, and kettle raffinate is
Nopinene, double penta dilute and longifolene mixed liquors, then the separation of Jing rectifying columns, obtain pure nopinene；Jing rectifying columns are separated respectively again
To double penta dilute, pure longifolenes.The product purity isolated is higher, and application surface is wider, and added value is higher.But, at present from turpentine
Olein evaporates that the australene of extraction, nopinene purity are low, does not reach the requirement for further synthesizing downstream fragrance product.While turpentine oil
After rectifying australene, remaining mix ingredients is complicated, and content is not high, continues isolated in the further rectifying of rectifying column, then can
Cause the problems such as increasing operating time, increase energy consumption, reduction production efficiency, increased operating cost.
The content of the invention
A kind of problem that the present invention is present for existing terebene distillation unit, there is provided turpentine oil continuous rectification apparatus.This
Device has that energy consumption is low, production efficiency is high, low cost, simple structure, the features such as be capable of achieving continuous production, be adapted to industrially push away
Extensively.
In order to realize object above, the technical solution used in the present invention is as follows：
A kind of turpentine oil continuous rectification apparatus, including one-level rectifier unit and two-stage rectification device, the one-level rectifier unit and
Two-stage rectification device is respectively provided with rectifying column, condenser and reboiler；The tower top of the rectifying column A I of the one-level rectifier unit connects
Condenser A I is connected to, the bottom of towe of rectifying column A I is connected with reboiler A I, bottom and the two-stage rectification device of the reboiler A I
The charging aperture of rectifying column B is connected；The tower top of the rectifying column B of the two-stage rectification device is connected with condenser B, the tower of rectifying column B
Bottom is connected with reboiler B, and the bottom of the reboiler B is connected with residual liquid storage tank；The one-level rectifier unit is additionally provided with rectifying
The tower top of tower A II, the rectifying column A II is connected with condenser A II, and the bottom of towe of rectifying column A II is connected with reboiler A II, described
The bottom of reboiler A II is connected with the charging aperture of rectifying column B；The top of the reboiler A I, reboiler A II and reboiler B is also
It is respectively equipped with the return duct being connected with the middle hypomere of rectifying column A I, rectifying column A II and rectifying column B.
Further, the above reboiler A I, reboiler A II and reboiler B include dividing plate, upper cavity, tank body respectively
And lower chamber；The upper cavity is located at the top of tank body, and lower chamber is located at the bottom of tank body, and the inner hub location of upper cavity sets
There is vertical dividing plate, arrange between the base plate and lower chamber of the upper cavity and split pipe.
Further, the above reboiler A I, reboiler A II and reboiler B is respectively shell and tube reboiler, described to split
Pipe by dividing plate by upper cavity split pipe distribution grid be divided into charging split pipe and flow back tubulation.
Further, pipe side difference is split in the upper cavity charging of the above reboiler A I, reboiler A II and reboiler B
It is connected with the bottom of rectifying column A I, rectifying column A II and rectifying column B with feed pipe, reboiler A I, reboiler A II and reboiler B's
Upper cavity backflow tubulation side is connected with the tower body hypomere of rectifying column A I, rectifying column A II and rectifying column B with return duct respectively.
Further, the bottom of the above the condenser A I, condenser A II and condenser B further respectively has and essence
Evaporate the return duct of the upper tower segment connection of tower A I, rectifying column A II and rectifying column B.
Further, the reboiler A I, reboiler A II and reboiler B further respectively have and rectifying column A I, rectifying column A
IIth, the heat pipe of the tower body hypomere connection of rectifying column B.
Further, the above rectifying column A's I, rectifying column A II and rectifying column B is in the same size.
Further, the stage casing of the above rectifying column A I, rectifying column A II and rectifying column B is respectively provided with material inlet, tower
Interior filler is stainless steel wire corrugated wire gauze packing.
The using method of this device is：Turpentine oil is pre-heated to into 100-105 DEG C from raw material storage tank, rectifying is delivered to respectively
Tower A I and rectifying column A II, it is -0.08 ~ -0.09MPa to control vacuum, with 8-10:1 reflux ratio it is isolated go out australene gas
Body, then condense respectively through condenser A I and condenser A II, condensed distillate detection reaches requirement, collects as product.Essence
Evaporate tower A I and II remaining kettle base solutions of rectifying column A respectively enter II heating of reboiler I and reboiler, maintain the temperature at 105-110
DEG C, during heating, the isolated australene gas of reboiler I and reboiler II respectively enters rectifying column A I and rectifying column A from upper cavity again
II, reboiler I and II remaining heavies liquid of reboiler into rectifying column B be heated to 110-115 DEG C it is isolated go out nopinene,
And vacuum is controlled for -0.10 ~ -0.12MPa, the remaining kettle base solutions of rectifying column B are heated to 115-120 DEG C into reboiler B,
Reboiler B isolated nopinene gas enters rectifying column B from upper cavity, and the remaining Liquid Residues of reboiler B enter residual liquid storage tank.
Compared with prior art, advantages of the present invention and have the beneficial effect that：
It is 1st, of the invention by arranging one-level rectifier unit and two-stage rectification device come the australene and nopinene in isolated turpentine oil,
And one-level rectifier unit arranges the amount of two rectifying columns, two rectifying columns enrichment nopinenes etc. and meets just a two-stage rectification
The demand of tower, not only reduces production cost and energy consumption, and improve production efficiency is capable of achieving consecutive production, moreover it is possible to improve australene
Alkene, the yield of nopinene product and purity.
2nd, the rectifying column of present invention design makes which meet nature voluntarily to discharge, and is not required to addition in addition and collects surge tank, reduces
The stability of operation and increase system vacuum etc..
3rd, the filler in rectifying tower of the present invention is stainless steel wire corrugated wire gauze packing, low with efficient, pressure drop and flux is big
The characteristics of.
4th, the reboiler that the present invention is arranged can not only realize the second distillation of rectifying at different levels, recovery section australene and β-pinane
Alkene product, can also rationally utilize heat energy.
5th, when apparatus of the present invention are used for turpentine oil rectifying effective component extracting, yield >=98% of australene, purity >=99%；
Nopinene yield >=95%, purity >=99%.
6th, apparatus of the present invention also have the advantages that simple to operate, simple structure, low cost of manufacture, it is adaptable to continuous chemical industry
Metaplasia is produced, with good Social benefit and economic benefit.
Description of the drawings
Fig. 1 is the structural representation of turpentine oil continuous rectification apparatus of the present invention.
Fig. 2 is that the upper cavity of reboiler of the present invention splits pipe distributing plate structure schematic diagram.
In reference, 1- rectifying columns A I, 2- condensers A I, 3- rectifying column B, 4- condenser B, 5- rectifying columns A II, 6- is cold
Condenser A II, 7- reboiler A I, 8- reboiler B, 9- remain liquid storage tank, 10- reboilers A II；11- dividing plates, 12- upper cavities, 13-
Tank body, 14- lower chambers, 15- upper cavities split pipe distribution grid.
Specific embodiment
Below in conjunction with the drawings and specific embodiments, the present invention is further described, but is not limited to the protection model of the present invention
Enclose.
Embodiment 1
As shown in figure 1 and 2, the turpentine oil continuous rectification apparatus include one-level rectifier unit and two-stage rectification device, described
One-level rectifier unit and two-stage rectification device are respectively provided with rectifying column, condenser and reboiler；The essence of the one-level rectifier unit
The tower top for evaporating tower A I 1 is connected with condenser A I 2, and the bottom of towe of rectifying column A I 1 is connected with reboiler A I 7, the bottom of the reboiler A I 7
End is connected with the charging aperture of the rectifying column B3 of two-stage rectification device；The tower top of the rectifying column B3 of the two-stage rectification device is connected with
The bottom of towe of condenser B4, rectifying column B3 is connected with reboiler B8, and the bottom of the reboiler B8 is connected with residual liquid storage tank 9；Institute
State one-level rectifier unit and be additionally provided with rectifying column A II 5, the tower top of the rectifying column A II 5 is connected with condenser A II 6, rectifying column A II
5 bottom of towe is connected with reboiler A II 10, and the bottom of the reboiler A II 10 is connected with the charging aperture of rectifying column B3；It is described again
Further respectively have and rectifying column A I 1, rectifying column A II 5 and rectifying column B3 at the top of boiling device A I 7, reboiler A II 10 and reboiler B8
The connection of middle hypomere return duct.
Further, the reboiler A I 7, reboiler A II 10 and reboiler B8 respectively include dividing plate 11, upper cavity 12,
Tank body 13 and lower chamber 14；The upper cavity 12 is located at the top of tank body 13, and lower chamber 14 is located at the bottom of tank body 13, upper cavity
12 inner hub location is provided with vertical dividing plate 11, arranges and split pipe between the base plate and lower chamber 14 of the upper cavity 12.
Further, the reboiler A I 7, reboiler A II 10 and reboiler B8 are respectively shell and tube reboiler, described to split
Pipe by dividing plate 11 by upper cavity split pipe distribution grid 15 be divided into charging split pipe and flow back tubulation.
Further, pipe side point is split in the charging of upper cavity 12 of the reboiler A I 7, reboiler A II 10 and reboiler B8
Not Yong feed pipe be connected with the bottom of rectifying column A I 1, rectifying column A II 5 and rectifying column B3, reboiler A I 7, II 10 and of reboiler A
The backflow tubulation of upper cavity 12 side of reboiler B8 is respectively with return duct and rectifying column A I 1, rectifying column A II 5 and rectifying column B3
Tower body hypomere connects.
Further, the bottom of the condenser A I 2, condenser A II 6 and condenser B4 further respectively has and rectifying column A I
1st, the return duct of the upper tower segment connection of rectifying column A II 5 and rectifying column B3.
Further, the reboiler A I 7, reboiler A II 10 and reboiler B8 further respectively have and rectifying column A I 1, essence
Evaporate the heat pipe of the tower body hypomere connection of tower A II 5 and rectifying column B3.
Further, the rectifying column A I 1, rectifying column A II 5 and rectifying column B3's is in the same size.
Further, the stage casing of the rectifying column A I 1, rectifying column A II 5 and rectifying column B3 is respectively provided with material inlet, tower
Interior filler is stainless steel wire corrugated wire gauze packing.
The using method of this device is：Turpentine oil is pre-heated to into 100-105 DEG C from raw material storage tank, rectifying is delivered to respectively
Tower A I 1 and rectifying column A II 5, it is -0.08 ~ -0.09MPa to control vacuum, with 8-10:1 reflux ratio it is isolated go out australene gas
Body, then condense respectively through condenser A I 2 and condenser A II 6, condensed distillate detection reaches requirement, collects as product.
Rectifying column A I 1 and II 5 remaining kettle base solutions of rectifying column A respectively enter reboiler I7 and reboiler II 10 is heated, and maintain the temperature at
105-110 DEG C, during heating, the isolated australene gas of reboiler I7 and reboiler II 10 respectively enters rectifying from upper cavity 12 again
Tower A I 1 and rectifying column A II 7, reboiler I1 and II 7 remaining heavies liquid of reboiler are heated to 110- into rectifying column B8
115 DEG C it is isolated go out nopinene, and control vacuum for -0.10 ~ -0.12MPa, the remaining kettle base solutions of rectifying column B8 are entered and are boiled again
Device B8 is heated to 115-120 DEG C, and reboiler B8 isolated nopinene gas enters rectifying column B3 from upper cavity, and reboiler B8 is remaining
Liquid Residue enter residual liquid storage tank 9.
Claims (8)
1. a kind of turpentine oil continuous rectification apparatus, it is characterised in that：Including one-level rectifier unit and two-stage rectification device, described one
Level rectifier unit and two-stage rectification device are respectively provided with rectifying column, condenser and reboiler；The rectifying of the one-level rectifier unit
Tower A I（1）Tower top be connected with condenser A I（2）, rectifying column A I（1）Bottom of towe be connected with reboiler A I（7）, the reboiler A
Ⅰ（7）Bottom and two-stage rectification device rectifying column B（3）Charging aperture be connected；The rectifying column B of the two-stage rectification device（3）
Tower top be connected with condenser B（4）, rectifying column B（3）Bottom of towe be connected with reboiler B（8）, the reboiler B（8）Bottom
It is connected with residual liquid storage tank（9）；The one-level rectifier unit is additionally provided with rectifying column A II（5）, the rectifying column A II（5）Tower top
It is connected with condenser A II（6）, the bottom of towe of rectifying column A II (5) is connected with reboiler A II (10), the reboiler A II (10)
Bottom be connected with the charging aperture of rectifying column B (3)；The reboiler A I（7）, reboiler A II（10）With reboiler B（8）Top
Portion further respectively has and rectifying column A I（1）, rectifying column A II（5）With rectifying column B（3）Tower body in hypomere connection return duct.
2. turpentine oil continuous rectification apparatus according to claim 1, it is characterised in that：The reboiler A I（7）, reboiler A
Ⅱ（10）With reboiler B（8）Include dividing plate respectively（11）, upper cavity（12）, tank body（13）And lower chamber（14）；The upper cavity
（12）It is located at tank body（13）Top, lower chamber（14）It is located at tank body（13）Bottom, upper cavity（12）Inner hub location
It is provided with vertical dividing plate（11）, the upper cavity（12）Base plate and lower chamber（14）Between arrange split pipe.
3. turpentine oil continuous rectification apparatus according to claim 1 or claim 2, it is characterised in that：The reboiler A I（7）, boil again
Device A II（10）With reboiler B（8）Respectively shell and tube reboiler, the pipe that splits is by dividing plate（11）Upper cavity is split into pipe distribution grid
（15）Be divided into charging split pipe and backflow split pipe.
4. turpentine oil continuous rectification apparatus according to claim 3, it is characterised in that：The reboiler A I（7）, reboiler A
Ⅱ（10）With reboiler B（8）Upper cavity（12）Charging splits pipe side respectively with feed pipe and rectifying column A I（1）, rectifying column A II
（5）With rectifying column B（3）Bottom connection, reboiler A I（7）, reboiler A II（10）With reboiler B（8）Upper cavity（12）Return
Stream tubulation side is respectively with return duct and rectifying column A I（1）, rectifying column A II（5）With rectifying column B（3）Tower body hypomere connection.
5. turpentine oil continuous rectification apparatus according to claim 1, it is characterised in that：The condenser A I（2）, condenser A
Ⅱ（6）With condenser B（4）Bottom further respectively have and rectifying column A I（1）, rectifying column A II（5）With rectifying column B（3）Tower body
The return duct of epimere connection.
6. turpentine oil continuous rectification apparatus according to claim 2, it is characterised in that：The reboiler A I（7）, reboiler A
Ⅱ（10）With reboiler B（8）Further respectively have and rectifying column A I（1）, rectifying column A II（5）, rectifying column B（3）Tower body hypomere connect
The heat pipe for connecing.
7. turpentine oil continuous rectification apparatus according to claim 1, it is characterised in that：The rectifying column A I（1）, rectifying column A
Ⅱ（5）With rectifying column B（3）It is in the same size.
8. turpentine oil continuous rectification apparatus according to claim 7, it is characterised in that：The rectifying column A I（1）, rectifying column A
Ⅱ（5）With rectifying column B（3）Stage casing be respectively provided with material inlet, inner-tower filling material is stainless steel wire corrugated wire gauze packing.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611181343.8A CN106512462A (en) | 2016-12-20 | 2016-12-20 | Turpentine continuous rectification device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611181343.8A CN106512462A (en) | 2016-12-20 | 2016-12-20 | Turpentine continuous rectification device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106512462A true CN106512462A (en) | 2017-03-22 |
Family
ID=58340440
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611181343.8A Pending CN106512462A (en) | 2016-12-20 | 2016-12-20 | Turpentine continuous rectification device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106512462A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113105948A (en) * | 2021-05-08 | 2021-07-13 | 南城县晨风香料有限公司 | Device for preparing longifolene by using high temperature |
| CN113274754A (en) * | 2021-06-04 | 2021-08-20 | 浙江正荣香料有限公司 | Turpentine rectification process |
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| CN101219927A (en) * | 2008-01-07 | 2008-07-16 | 天津大学 | Continuous process and device for the separation of benzyl chloride regular packing column |
| JP2013078294A (en) * | 2011-10-05 | 2013-05-02 | Nippon Steel & Sumikin Engineering Co Ltd | Apparatus and method for producing ethanol |
| CN203144334U (en) * | 2013-03-23 | 2013-08-21 | 河南永胜能源化工集团有限公司 | Reboiler |
| CN203609905U (en) * | 2013-12-17 | 2014-05-28 | 山东庆云长信化学科技有限公司 | Rectificationdevice for furfurylalcohol |
| CN206334372U (en) * | 2016-12-20 | 2017-07-18 | 广西壮族自治区林业科学研究院 | A kind of turpentine oil continuous rectification apparatus |
-
2016
- 2016-12-20 CN CN201611181343.8A patent/CN106512462A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101219927A (en) * | 2008-01-07 | 2008-07-16 | 天津大学 | Continuous process and device for the separation of benzyl chloride regular packing column |
| JP2013078294A (en) * | 2011-10-05 | 2013-05-02 | Nippon Steel & Sumikin Engineering Co Ltd | Apparatus and method for producing ethanol |
| CN203144334U (en) * | 2013-03-23 | 2013-08-21 | 河南永胜能源化工集团有限公司 | Reboiler |
| CN203609905U (en) * | 2013-12-17 | 2014-05-28 | 山东庆云长信化学科技有限公司 | Rectificationdevice for furfurylalcohol |
| CN206334372U (en) * | 2016-12-20 | 2017-07-18 | 广西壮族自治区林业科学研究院 | A kind of turpentine oil continuous rectification apparatus |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113105948A (en) * | 2021-05-08 | 2021-07-13 | 南城县晨风香料有限公司 | Device for preparing longifolene by using high temperature |
| CN113105948B (en) * | 2021-05-08 | 2023-01-13 | 陶泓羽 | Device for preparing longifolene by using high temperature |
| CN113274754A (en) * | 2021-06-04 | 2021-08-20 | 浙江正荣香料有限公司 | Turpentine rectification process |
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