CN106699502A - Turpentine rectification tower vacuum system - Google Patents
Turpentine rectification tower vacuum system Download PDFInfo
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- CN106699502A CN106699502A CN201611181330.0A CN201611181330A CN106699502A CN 106699502 A CN106699502 A CN 106699502A CN 201611181330 A CN201611181330 A CN 201611181330A CN 106699502 A CN106699502 A CN 106699502A
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- CN
- China
- Prior art keywords
- rectifying column
- reboiler
- vacuum system
- turpentine oil
- water
- Prior art date
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- 241000779819 Syncarpia glomulifera Species 0.000 title abstract description 7
- 239000001739 pinus spp. Substances 0.000 title abstract description 7
- 229940036248 turpentine Drugs 0.000 title abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 47
- 239000002699 waste material Substances 0.000 claims abstract description 5
- 239000001293 FEMA 3089 Substances 0.000 claims description 36
- 239000000463 material Substances 0.000 claims description 10
- 238000012856 packing Methods 0.000 claims description 4
- 229910001220 stainless steel Inorganic materials 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 238000011049 filling Methods 0.000 claims description 3
- 239000011229 interlayer Substances 0.000 claims description 3
- 229930006722 beta-pinene Natural products 0.000 abstract description 23
- WTARULDDTDQWMU-UHFFFAOYSA-N Pseudopinene Natural products C1C2C(C)(C)C1CCC2=C WTARULDDTDQWMU-UHFFFAOYSA-N 0.000 abstract description 22
- 239000007788 liquid Substances 0.000 abstract description 10
- 238000003860 storage Methods 0.000 abstract description 7
- 239000007791 liquid phase Substances 0.000 abstract description 5
- 239000012071 phase Substances 0.000 abstract description 5
- 238000003912 environmental pollution Methods 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 2
- GRWFGVWFFZKLTI-UHFFFAOYSA-N α-pinene Chemical compound CC1=CCC2C(C)(C)C1C2 GRWFGVWFFZKLTI-UHFFFAOYSA-N 0.000 abstract 2
- WTARULDDTDQWMU-RKDXNWHRSA-N (+)-β-pinene Chemical compound C1[C@H]2C(C)(C)[C@@H]1CCC2=C WTARULDDTDQWMU-RKDXNWHRSA-N 0.000 abstract 1
- WTARULDDTDQWMU-IUCAKERBSA-N (-)-Nopinene Natural products C1[C@@H]2C(C)(C)[C@H]1CCC2=C WTARULDDTDQWMU-IUCAKERBSA-N 0.000 abstract 1
- GRWFGVWFFZKLTI-IUCAKERBSA-N 1S,5S-(-)-alpha-Pinene Natural products CC1=CC[C@@H]2C(C)(C)[C@H]1C2 GRWFGVWFFZKLTI-IUCAKERBSA-N 0.000 abstract 1
- XCPQUQHBVVXMRQ-UHFFFAOYSA-N alpha-Fenchene Natural products C1CC2C(=C)CC1C2(C)C XCPQUQHBVVXMRQ-UHFFFAOYSA-N 0.000 abstract 1
- MVNCAPSFBDBCGF-UHFFFAOYSA-N alpha-pinene Natural products CC1=CCC23C1CC2C3(C)C MVNCAPSFBDBCGF-UHFFFAOYSA-N 0.000 abstract 1
- 230000002708 enhancing effect Effects 0.000 abstract 1
- LCWMKIHBLJLORW-UHFFFAOYSA-N gamma-carene Natural products C1CC(=C)CC2C(C)(C)C21 LCWMKIHBLJLORW-UHFFFAOYSA-N 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 13
- 238000001514 detection method Methods 0.000 description 6
- 238000004821 distillation Methods 0.000 description 6
- 230000008901 benefit Effects 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 239000004615 ingredient Substances 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- HEVGGTGPGPKZHF-UHFFFAOYSA-N 1-(1,2-dimethyl-3-methylidenecyclopentyl)-4-methylbenzene Chemical compound CC1C(=C)CCC1(C)C1=CC=C(C)C=C1 HEVGGTGPGPKZHF-UHFFFAOYSA-N 0.000 description 2
- WEEGYLXZBRQIMU-UHFFFAOYSA-N Eucalyptol Chemical compound C1CC2CCC1(C)OC2(C)C WEEGYLXZBRQIMU-UHFFFAOYSA-N 0.000 description 2
- PDSNLYSELAIEBU-UHFFFAOYSA-N Longifolene Chemical compound C1CCC(C)(C)C2C3CCC2C1(C)C3=C PDSNLYSELAIEBU-UHFFFAOYSA-N 0.000 description 2
- ZPUKHRHPJKNORC-UHFFFAOYSA-N Longifolene Natural products CC1(C)CCCC2(C)C3CCC1(C3)C2=C ZPUKHRHPJKNORC-UHFFFAOYSA-N 0.000 description 2
- XMGQYMWWDOXHJM-UHFFFAOYSA-N limonene Chemical compound CC(=C)C1CCC(C)=CC1 XMGQYMWWDOXHJM-UHFFFAOYSA-N 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- HFPZCAJZSCWRBC-UHFFFAOYSA-N p-cymene Chemical compound CC(C)C1=CC=C(C)C=C1 HFPZCAJZSCWRBC-UHFFFAOYSA-N 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000006641 stabilisation Effects 0.000 description 2
- 238000011105 stabilization Methods 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- RSWGJHLUYNHPMX-UHFFFAOYSA-N Abietic-Saeure Natural products C12CCC(C(C)C)=CC2=CCC2C1(C)CCCC2(C)C(O)=O RSWGJHLUYNHPMX-UHFFFAOYSA-N 0.000 description 1
- 241000599805 Apium graveolens Secalinum Group Species 0.000 description 1
- 206010054949 Metaplasia Diseases 0.000 description 1
- 235000000365 Oenanthe javanica Nutrition 0.000 description 1
- 235000008331 Pinus X rigitaeda Nutrition 0.000 description 1
- 235000011613 Pinus brutia Nutrition 0.000 description 1
- 241000018646 Pinus brutia Species 0.000 description 1
- 235000011609 Pinus massoniana Nutrition 0.000 description 1
- 241000018650 Pinus massoniana Species 0.000 description 1
- KHPCPRHQVVSZAH-HUOMCSJISA-N Rosin Natural products O(C/C=C/c1ccccc1)[C@H]1[C@H](O)[C@@H](O)[C@@H](O)[C@@H](CO)O1 KHPCPRHQVVSZAH-HUOMCSJISA-N 0.000 description 1
- 235000013559 Schnittsellerie Nutrition 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 125000003783 beta-pinene group Chemical group 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 229940087305 limonene Drugs 0.000 description 1
- 235000001510 limonene Nutrition 0.000 description 1
- 230000015689 metaplastic ossification Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- KHPCPRHQVVSZAH-UHFFFAOYSA-N trans-cinnamyl beta-D-glucopyranoside Natural products OC1C(O)C(O)C(CO)OC1OCC=CC1=CC=CC=C1 KHPCPRHQVVSZAH-UHFFFAOYSA-N 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
Classifications
-
- 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
-
- 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
- B01D3/10—Vacuum distillation
- B01D3/106—Vacuum distillation with the use of a pump for creating vacuum and for removing the distillate
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a turpentine rectification tower vacuum system which comprises a rectification tower (1), a condenser (3), water ring vacuum pumps (6) and a reboiler (7), wherein a discharge port on the top of the rectification tower (1) is connected with the condenser (3); the bottom of the rectification tower is connected with a feed port on the top of the reboiler (7); the bottom of the reboiler (7) is connected with a waste liquid storage tank (13); the water ring vacuum pumps (6) are connected with the top of the rectification tower (1); and the water ring vacuum pumps (6) are also connected with an oil-water separator (5). The two water ring vacuum pumps constitute the vacuum system, so that the vacuum degree of the rectification tower is stabler, the effective components can be volatilized more conveniently, and the substance and energy exchanges between the gas phase and liquid phase of the turpentine can be kept stable. The circulation of the circulating water can utilized to take a small amount of the turpentine component out of the vacuum system, thereby enhancing the purity and yield of the alpha-pinene and beta-pinene products, and reducing the environmental pollution.
Description
Technical field
The present invention relates to fine chemistry industry equipment technical field, specifically a kind of vacuum system of turpentine oil rectifying column.
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 are different, make light component
Vaporization, condenses through the vaporization of multiple Partial Liquid Phase and partial gas phase, make heavy constituent concentration in the light component and liquid phase in gas phase by
Edge up height, so as to realize separating.
The traditional handicraft of separating-purifying firpene is from turpentine oil：Accessory substance-the turpentine obtained during rosin production
Oily crude oil is clarified, enter rectifying column after filtering preheating evaporates backflow, after cooler refrigerated separation australene, kettle raffinate is
Nopinene, double penta dilute and longifolene mixed liquors, then separated through rectifying column, obtain pure nopinene.Turpentine oil distillation process is usually
Carry out under vacuum conditions, but existing vacuum system vacuum is unstable in the course of the work, vavuum pump is easily damaged, on a small quantity
Turpentine oil ingredient can be taken out of by vacuum system so that the yield reduction of product.
The content of the invention
A kind of problem that the present invention exists for existing rectifying vacuum system, there is provided vacuum system of turpentine oil rectifying column.
The present invention constitutes vacuum system by designing two water ring vacuum pumps so that the vacuum of rectifying column is more stable, it can be ensured that turpentine
Material, the stabilization of energy exchange between oil gas phase and liquid phase；Vacuum system can be reclaimed takes a small amount of turpentine oil ingredient out of simultaneously, enters
And the yield of australene and nopinene product is improved, and reduce environmental pollution.
In order to realize the above object the technical solution adopted by the present invention is as follows：
A kind of vacuum system of turpentine oil rectifying column, including rectifying column, condenser, water ring vacuum pump and reboiler are set；It is described
The discharging opening of rectifying column tower top is connected with condenser, and the bottom of towe of rectifying column is connected with the charging aperture at the top of reboiler, described to boil again
The bottom of device is connected with waste tank, and the water ring vacuum pump is connected with the tower top of rectifying column, and water ring vacuum pump also divides with profit
From device connection.
Further, the water ring vacuum pump is arranged in parallel two.
Further, the charging aperture of the rectifying column is located at the stage casing of rectifying column.
Further, the reboiler is shell and tube reboiler, and setting includes tank body, upper cavity and lower chamber；On described
Cavity (10) 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 the upper cavity is provided with vertically
Dividing plate, set between the base plate and lower chamber of the upper cavity and split pipe, it is described split pipe by dividing plate will be divided into charging split pipe with
Backflow tubulation.
Further, the charging tubulation side feed pipe of the upper cavity is connected with the bottom of rectifying column, upper cavity
Backflow tubulation side return-flow catheter is connected with the tower body hypomere of rectifying column.
Further, the reboiler is also connected by heat conducting pipe with the interlayer of rectifying column.
Further, the inner-tower filling material of the rectifying column is stainless steel wire corrugated wire gauze packing.
The application method of present system is：
Turpentine oil is preheated to 100-105 DEG C in raw material storage tank rectifying column is delivered to by feed pump, start water ring vacuum pump,
A small amount of turpentine oil enters vacuum tube and reaches water ring vacuum pump, by the circulation of Water-ring vacuum water pumping pipe recirculated water, reaches oil
Separator, because turpentine oil is lighter than water, through water-oil separating, can reclaim turpentine oil in oil water separator recovery port.Distillation process
The vacuum of middle control system is -0.08 ~ -0.09MPa, with 8-10:1 reflux ratio it is isolated go out australene gas, australene
Again respectively through condenser, condensed distillate detection reaches requirement to gas, is collected as product.The vacuum of control system
It is -0.10 ~ -0.12MPa, is heated to the nopinene gas that 110-115 DEG C of rectifying column evaporate and is condensed by condenser, condensation
Distillate detection afterwards reaches requirement, is collected as product.The remaining kettle base solution of rectifying column is heated to 115-120 into reboiler
DEG C, the isolated nopinene gas of reboiler enters rectifying column from upper cavity, and the remaining Liquid Residue of reboiler enters residual liquid storage tank.
Compared with prior art, advantages of the present invention and have the beneficial effect that：
1st, the present invention constitutes vacuum system by two water ring vacuum pumps so that the vacuum of rectifying column is more stable, more conducively effectively
The volatilization of composition, while can ensure that material between turpentine oil gas phase and liquid phase, the stabilization of energy exchange；By the circulation of recirculated water
Vacuum system can be reclaimed and take a small amount of turpentine oil ingredient out of, and then improve the purity and yield of australene and nopinene product, and
Reduce environmental pollution.
2nd, vavuum pump of the invention is water ring vacuum pump, with conventional sliding valve vacuum pump, can be effectively increased the longevity of vavuum pump
Life, while designing two water ring vacuum pumps, by controlling the vacuum of rectifying column, realizes turpentine oil rectifying australene, nopinene
Continuous production.
3rd, the reboiler that present system is set can not only realize the second distillation of rectifying at different levels, and recovery section nopinene is produced
Product, can also rationally utilize heat energy.
4th, the rectifying column that the present invention is set makes it 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., while the filler in rectifying tower is stainless steel wire corrugated wire gauze packing, with height
The characteristics of effect, low pressure drop and big flux.
5th, when present system is used for rectified oil of turpentine active ingredient, the yield of australene product is up to 98%, nopinene product
Yield up to 97%, the purity of australene product is up to the purity of 99%, nopinene product up to 99%.
6th, present system also has consume energy low, simple to operate, simple structure, low cost and other advantages, easily realizes industry
Metaplasia is produced, with good Social benefit and economic benefit.
Brief description of the drawings
Fig. 1 is the structural representation of the vacuum system of turpentine oil rectifying column of the present invention.
In accompanying drawing mark：1- rectifying columns, 2- return ducts, 3- condensers, 4- heat conducting pipes, 5- oil water separators, 6- water rings are true
Empty pump, 7- reboilers, 8- return-flow catheters, 9- dividing plates, 10- upper cavities, 11- tank bodies, 12- lower chambers, 13- waste tanks.
Specific embodiment
Below in conjunction with the drawings and specific embodiments, the present invention is further described, but is not limited to protection model of the invention
Enclose.
Embodiment 1
As shown in Figure 1, the vacuum system of the turpentine oil rectifying column, including rectifying column 1, condenser 3, water ring vacuum pump are set
6 and reboiler 7；The discharging opening of the tower top of the rectifying column 1 is connected with condenser 3, entering at the top of the bottom of towe and reboiler 7 of rectifying column
Material mouth is connected, and the bottom of the reboiler 7 is connected with waste tank 13, and the water ring vacuum pump 6 connects with the tower top of rectifying column 1
Connect, water ring vacuum pump 6 is also connected with oil water separator 5.
Further, the water ring vacuum pump 6 is arranged in parallel two.
Further, the charging aperture of the rectifying column 1 is located at the stage casing of rectifying column 1.The inner-tower filling material of rectifying column 1 is stainless
Steel wire corrugated wire gauze packing.
Further, the reboiler 7 is shell and tube reboiler, and setting includes tank body 11, upper cavity 10 and lower chamber 12；
The upper cavity 10 is located at the top of tank body 11, and lower chamber 12 is located at the bottom of tank body 11, the inside center of the upper cavity 10
Position is provided with vertical dividing plate 9, is set between the base plate and lower chamber 12 of the upper cavity 10 and splits pipe, and the pipe that splits is by dividing plate 11
Charging will be divided into and split pipe and backflow tubulation.The charging tubulation side feed pipe of the upper cavity 10 and the bottom of rectifying column 1
Connection, the backflow tubulation side of upper cavity 10 is connected with return-flow catheter 8 with the tower body hypomere of rectifying column 1.
Further, the reboiler 7 is also connected by heat conducting pipe 4 with the interlayer of rectifying column 1.
By Turpentine Oil From Pinus Massoniana（α-firpene content is that 79.8%, β-firpene content is 8.5% in turpentine oil）In raw material
Storage tank is preheated to 105 DEG C and is delivered to rectifying column by feed pump, starts water ring vacuum pump, and a small amount of turpentine oil enters vacuum tube
And water ring vacuum pump is reached, by the circulation of Water-ring vacuum water pumping pipe recirculated water, oil water separator is reached, because turpentine oil compares water
Gently, through water-oil separating, turpentine oil can be reclaimed in oil water separator recovery port.In distillation process the vacuum of control system for-
0.08MPa, with 8:1 reflux ratio it is isolated go out australene gas, australene gas again respectively through condenser, condensed distillate
Detection reaches requirement, is collected as product.The vacuum of control system is -0.10MPa, is heated to 115 DEG C of rectifying columns and evaporates
Nopinene gas condensed by condenser, the detection of condensed distillate reaches requirement, is collected as product.Rectifying column is remaining
Kettle base solution is heated to 120 DEG C into reboiler, and the isolated nopinene gas of reboiler enters rectifying column from upper cavity, and reboiler is remained
Remaining Liquid Residue enters residual liquid storage tank.
The yield of australene product is 98.02% in the present embodiment, and up to 96.81%, australene is produced the yield of nopinene product
The purity of product is up to the purity of 99.15%, nopinene product up to 98.98%.
Embodiment 2
Water ring vacuum pump 6 sets one in the present embodiment, and remaining setting is identical with embodiment 1.
By wet-land pine tree turpentine oil（Australene content is that 62.17%, β-firpene content is 26.45% in turpentine oil）In original
Material storage tank is preheated to 100 DEG C and is delivered to rectifying column by feed pump, starts water ring vacuum pump, and a small amount of turpentine oil enters vacuum
Water ring vacuum pump is managed and reached, by the circulation of Water-ring vacuum water pumping pipe recirculated water, oil water separator is reached, due to turpentine oil ratio
Water is light, through water-oil separating, can reclaim turpentine oil in oil water separator recovery port.In distillation process the vacuum of control system for-
0.09MPa, with 10:1 reflux ratio it is isolated go out australene gas, australene gas is condensed to evaporate again respectively through condenser
Liquid detection reaches requirement, is collected as product.The vacuum of control system is -0.12MPa, is heated to 110 DEG C of rectifying column evaporations
The nopinene gas for going out is condensed by condenser, and condensed distillate detection reaches requirement, is collected as product.Rectifying column is remaining
Kettle base solution be heated to 115 DEG C into reboiler, the isolated nopinene gas of reboiler enters rectifying column, reboiler from upper cavity
Remaining Liquid Residue enters residual liquid storage tank.
The yield of australene product is 97.12% in the present embodiment, and up to 95.91%, australene is produced the yield of nopinene product
The purity of product is up to the purity of 98.82%, nopinene product up to 98.29%.
Claims (7)
1. a kind of vacuum system of turpentine oil rectifying column, it is characterised in that：Including setting rectifying column（1）, condenser（3）, water ring
Vavuum pump（6）And reboiler（7）；The rectifying column（1）The discharging opening and condenser of tower top（3）Connection, the bottom of towe of rectifying column with
Reboiler（7）The charging aperture connection at top, the reboiler（7）Bottom be connected with waste tank（13）, the Water-ring vacuum
Pump（6）With rectifying column（1）Tower top connection, water ring vacuum pump（6）Also with oil water separator（5）Connection.
2. the vacuum system of turpentine oil rectifying column according to claim 1, it is characterised in that：The water ring vacuum pump（6）And
Connection sets two.
3. the vacuum system of turpentine oil rectifying column according to claim 1, it is characterised in that：The rectifying column（1）Charging
Mouth is located at rectifying column（1）Stage casing.
4. the vacuum system of turpentine oil rectifying column according to claim 1, it is characterised in that：The reboiler（7）It is tubulation
Formula reboiler, setting includes tank body (11), upper cavity (10) and lower chamber (12)；The upper cavity (10) is located at tank body (11)
Top, lower chamber (12) is located at the bottom of tank body (11), and the inner hub location of the upper cavity (10) is provided with vertical dividing plate
(9), set between the base plate and lower chamber (12) of the upper cavity (10) and split pipe, it is described split pipe by dividing plate (11) will be divided into
Material splits pipe and backflow tubulation.
5. the vacuum system of turpentine oil rectifying column according to claim 4, it is characterised in that：The charging of the upper cavity (10)
Tubulation side feed pipe and rectifying column（1）Bottom connection, the backflow tubulation side return-flow catheter of upper cavity (10)（8）With
Rectifying column（1）Tower body hypomere connection.
6. the vacuum system of turpentine oil rectifying column according to claim 1, it is characterised in that：The reboiler（7）Also pass through
Heat conducting pipe（4）With rectifying column（1）Interlayer connection.
7. according to claim any one of 1-6 turpentine oil rectifying column vacuum system, it is characterised in that：The rectifying column
（1）Inner-tower filling material be stainless steel wire corrugated wire gauze packing.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611181330.0A CN106699502A (en) | 2016-12-20 | 2016-12-20 | Turpentine rectification tower vacuum system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611181330.0A CN106699502A (en) | 2016-12-20 | 2016-12-20 | Turpentine rectification tower vacuum system |
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| Publication Number | Publication Date |
|---|---|
| CN106699502A true CN106699502A (en) | 2017-05-24 |
Family
ID=58939233
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611181330.0A Pending CN106699502A (en) | 2016-12-20 | 2016-12-20 | Turpentine rectification tower vacuum system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107501034A (en) * | 2017-07-24 | 2017-12-22 | 江苏新化化工有限公司 | Turpentine oil continuous separation method and device |
| CN111960922A (en) * | 2020-08-18 | 2020-11-20 | 广西壮族自治区林业科学研究院 | Method for separating natural terpineol from heavy turpentine |
| CN117964450A (en) * | 2023-12-26 | 2024-05-03 | 浙江正荣香料有限公司 | Separation process for purifying beta-pinene production |
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