Title of Invention

A DEVICE USEFUL FOR THE DISTILLATION OF ESSENTIAL OILS

Abstract A device useful for the distillation of essential oils by distillation tank having an external jacket connected to means for steam supply and steam trap; the distillation tank being provided at its bottom portion with means for steam spurging, auxiliary heating, and an outlet; above the spurger and auxiliary heatrs being provided a removably fixed grating above the grating being provided at least one opening for discharging of spent materials; the distillation tank being provided at its top portion with removably sealed cover having at least one opening for charging of materials and atleast one vapour outlet, one or more vapour outlet(s) being connected by known means to the bottom end of one or more known cohobation head column(s) being connected by known means to the inlet of a known condenser unit, the outlet of the said condenser being connected through pipe to the inlet of a tubular oil separator, the outlet of the said tubular oil separator being fed to a known receiver-cum-separator.
Full Text The present invention relates to a device useful for the distillation of essential oils.
The present invention particularly relates to a device useful for the distillation of essential oils and process thereof for distillation of essential oils such as rose oil, lavender oil, chamomile oil, celery seed oil, tagetes oil, vetiver root oil, and so on, in general, being of versatile design and hence suitable for multipurpose use. Specifically, the device and process of the present i-nvention is for rose oil distillation.
This unit is useful to distill the essential oils from fresh flowers of Rosa damascene, Lavandula officinalis, Matricaria chamomilla, seeds of Apium graveolens, biomass of Tagetes minuta, roots of Vetivarea zizanioides and so on by all the three methods of hydrodistillation. There is no need to comminute the rose flowers before charging into the still, which decreases recurring cost and time of processing. The process provides minimum dilution and charring effect of the charged materials. Due to built-in cohobation column, within the system, the yield of direct rose oil comes up to 70% of total oil. The unit is most suitable for covering commercial scale plantation of scented roses for bulk production of rose water and rose oil.
The traditional rose oil distillation unit is shown in fig.:l of the drawings accompanying this specification. Reference may be made
to (1) Kahol, A.P. and Aggarwal, K.K. "Improved Technology for Production of Rose oil" Indian Perfumer 27 (2), pp.137-142. 1983. (2) Sharma, M.L. Cultivation of Rose and Manufacture of its Products in India. In: Cultivation and Utilization of Aromatic Plants. Regional Research Laboratory (CSIR) Jammu Tawi, pp. 537. 1982.
The traditional rose oil distillation unit comprises : directly fired copper vessel of spherical shape called Deg (a) of 250-500 lit. capacity to process 50-100 kg of rose flowers per batch, a long necked copper vessel immersed in a cold water tank employed as a condenser-cum-receiver for collecting distillate called Babhka (b) and a bamboo pipe serving as the vapour connection (c). The water in the cooling tank (d) has to be changed from time to time. The water charged into still is 3 to 4 times the weight of rose flowers. The heating is done by a slow burning fire wood or cow-dung from the hearth (e) below. The "first water" collected from several stills is redistilled very slowly until 15-20% of total rose water charged is collected as a distillate ("second rose water"). Mud and cloth are used to seal the system. The oil recovery is 0.01% to 0.02%.
The major drawback of this system is the lack of controlling devices for temperature, pressure and for monitoring the rate of distillation. Charring of rose flowers occurs, if fire is not controlled well. The use of poor sealing agents like mud and cloth

often fails to hold the Deg lid (f) in case of pressure generated inside the system. Due to short length of the Deg connection (c), a part of vapour line, the pollen and other low volatile components also get mixed with oil vapour resulting into poor quality of rose water and rose oil. Due to uncontrolled heating and inability to monitor the process, high amount of water has to be charged in the still leading to the high dilution of rose water causing poor recovery of rose oil and separation of rose oil from water becomes tedious. There are always chances of leakage or bursting because of the use of receiver as condenser owing to its insufficient heat transfer area and poor sealing agents.
An improvement of the traditional unit has been reported by Sharma, M.L. Rosa damascena Mill. - A Source of Natural Perfume. Indian Rose Annual V, pp. 162 - 169. 1986. The unit consists of a directly fired distillation vessel provided with a false bottom to avoid direct contact of the flowers with the heating surface, a tubular condenser with provision of running water, a separating funnel for separating rose water & rose oil and a pipe connecting separating funnel and the still for recycling of rose water. The major limitation of this method is that the recycled rose water gets continuously mixed with the refuse resulting into deterioration of quality. The refuse of the charged material after certain period of heating starts producing burnt off-notes. Because of the recycling of the rose water into the still, the subsequently extracted lot of rose
oil contains such off-notes and fetches very low price in the market. The unit is also not suitable for bulk distillation being small sized. Another draw back of this unit is that it can not be used to distill the plant materials by steam distillation.
Other improvements of the rose oil distillation unit have been
*
reported: (1) V. Chandra, Oil Bearing Rose. In : Advances in Horticulture. Vol. 11. Eds. K.L.Chadha and Rajendra Gupta. Malhotra Publishing House, New Delhi-110 064. INDIA, 1995. (2) Kahol, A.P. and Aggarwal, K.K. "Improved Technology for Production of Rose oil" Indian Perfumer 27 (2), pp.137-142. 1983. This involves a separate redistillation unit provided with a cohobation tower for subsequent processing of rose water to rose oil . The heating in the system is done by steam jacket. This improvement because of its two step nature requires more time and energy for distillation leading to higher recurring and non-recurring production cost. Because of the lack of stirring effect of the flowers, the petals lying just adjacent to the steam jacket get charred resulting into poor quality oil.
Another improvement of the direct fired distillation unit {CSIR News vol. 46, No. 7, 15th April, 1996.} involving recycling through the same still involves an efficient and evenly distributed heating system achieved by an increased heating surface area through horizontal set of exhaust pipes at the base of the still (calandria),

and very long vertical part of the vapour line which gives cohobation effect. The major drawback of this design is very high risk of charring even upon slight overloading of the still resulting into settling down of the flower mass through the false bottom then on to the calandria. Moreover, the per batch capacity of the still is only 150 kg rose flowers.
Steam distillation is a universal process for the distillation of number of aromatic herbs for production of essential oils. The said process is performed on simple field distillation units which are used in essential oil industry for primary distillation of essential oils at commercial scale. A schematic diagram of such a field distillation unit is shown in fig. : 2 of the drawings accompanying this specification. These units comprises of a distillation tank (A) without steam jacket and cohobation column. The plant material is charged above the false bottom (D) from the top of the tank after removing the top lid (C). Before charging, the chains (B) for removing the false bottom (along with the processed material after the completion of distillation process) are lifted and then the material is charged. Then the lid is closed and the bolts are tightened. Steam generated in a separate boiler is fed to the unit through the steam spurger (E) below the false bottom (D). The tank is connected through a small inclined vapour line (F) to a condenser (G) where vapours are condensed. The distillate from condenser is collected in a receiver (H) through oil & water out let pipe (I). The essential
oil, being lighter than water, settles as upper layer. The excess water from the receiver (H) is drained out through water out let (J) continuously. The settled essential oil is again send to the oil receiver (K) through oil drain pipe line (L).
The main draw back of this system is that the device can not be used to distill high valued essential oil for the reason being its low recoveries due to the lack of cohobation column. Another disadvantage is that it can not be used to distill the plant material such as freshly harvested scented rose flowers by water distillation process.
Thus, all the distillation units and process mentioned above have one or the other major drawbacks like poor oil quality, low oil recovery, low efficiency in terms of fuel and time, low batch capacity, high non-recurring costs and inefficient to perform all the three types of hydrodistillations.
The main object of the present invention is to provide a device useful for the distillation of essential oils and a process thereof which obviates the drawbacks as detailed above.
Another object of the present invention is to provide a device for higher recovery of essential oils such as rose oil, lavender oil, chamomile oil, celery seed oil, tagetes oil, vetiver root oil, and so on with low capital investment.

Still another object of the present invention is to provide a device for industrial production of essential oils such as rose oil, lavender oil, chamomile oil, celery seed oil, tagetes oil, vetiver root oil, and so on covering large area of cultivation.
Yet another very specific object of the present invention is to provide a device useful for cost effective rose oil distillation of 400 to 425 kg batch capacity, providing quality grade rose oil with 0.035% oil recovery.
In fig.: 3 of the drawings accompanying this specification, a schematic diagram of the device of the present invention is shown. The device of the present invention essentially consists of a distillation tank unit (I), a cohobation head column (II), condenser unit (III) and a receiver-cum-separator unit (IV).
Accordingly the present invention provides a device useful for the distillation of essential oils, which comprises a distillation tank (1) having an external jacket (2) connected to means (3,4) for steam supply (3) and steam trap (4); the distillation tank being provided at its bottom portion with means (5,6,7) for steam spurging (5), auxiliary heating (6), and an outlet (7); above the said steam spurger and auxiliary heaters being provided a removably fixed grating (8); above the said grating (8) being provided at least one opening (9) for discharging of spent materials; the said distillation tank
being provided at its top portion with removably sealed cover (10) having at least one opening (20) for charging of materials and atleast one vapour outlet (11), the said one or more vapour outlet(s) being connected by known means (12) to the bottom end of one or more known cohobation head column(s) (13), the top of the said cohobation head column(s) being connected by known means (12) to the inlet (14) of a known condenser unit (23), the outlet (15) of the said condenser (23) being connected through pipe (19) to the inlet (16) of a tubular oil separator, the outlet of the said tubular oil separator being fed to a known receiver-cum-separator (17).
In an embodiment of the present invention the distillation tank may be provided with means (18) for measuring parameters such as temperature, pressure, water level.
In another embodiment of the present invention the distillation tank may have length to diameter ratio in the range of 1 to 2.
In still another embodiment the means used for auxiliary heating may be such as steam, electric heating elements.
In yet another embodiment the cohobation head column used may be such as corrugated, hollow., packed, with sieve trays, bubble cap trays.
In another embodiment the inlet (16) of the tubular oil separator may be such as having a plurality of vertical tubes for retention of oil .
In still another embodiment the receiver-cum-separator unit (17) may be connected by a pipe line (24) to the cohobation column to enable reflux.
Accordingly the present invention provides a process for the distillation of essential oils, which comprises charging aromatic botanical and water, in a ratio in the range of 1:0 to 1:5 in the distillation tank of the device as described above, preheating, if required, the said mass using the auxiliary heating means to a temperature to minimise condensation of steam, injecting steam on to the mass through the steam spurger to effect distillation, allowing the vapours so formed to pass through cohobation head column to enable vapour enrichment, allowing the enriched vapour to pass through a condenser to obtain liquid distillate at a temperature in the range of 25 to 35° C, collecting the said distillate in the receiver-cum-separator through tubular oil separator to obtain the essential oil and raffinate (saturated with essential oil) water, redistilling the said raffinate water, if desired.
The device of present invention comprises a distillation still of suitable capacity, fitted with multiple heating system, integrating the said still with at least one compatible cohobation head column, and the said cohobation head column being connected to a compatible heat exchanger for efficient condensation of the vapours and a tubular oil separator for collection and separation of essential oil
from distillate and lastly a receiver-cum-separator which hold any remaining droplets of oil on the surface of distillate.
The outer jacket of the distillation still may be a Mild Steel (MS) steam jacket, 4mm thick., ID=1400mm and length = 1000mm to cover Stainless Steel (SS) tank from outside and bottom, is provided to redistill the First rose water/ distillate collected from different batches for further separation of rose oil from it.
The still employed in the distillation unit may be made by any bio-compatible material like stainless steel, glass, and copper heavily lined with tin.
The still may be in cylindrical, spherical, or square shapes.
The still may be provided with and without steam jacket for indirect heating of the material.
The multiple heating system may be characterised by direct, indirect steam injection and heating elements.
The direct steam may be applied through a spurger of suitable dimensions and shape to ensure even distribution of steam over the charge.
The type of condenser, to be used in the system may be selected out of shell and tube 1-1 or 1-2 or 2-4 heat exchangers with stationary or floating head; or U-Tube bundle.
The heat exchangers may be installed vertically or horizontally.
The bottom of the still and receiver-cum-separator may be flat
end or 2:1 semi-ellipsoidal dished end, torrispherical dished end, or tapered in shape.
The cohobation column may be hollow or packed or designed for sieve trays or bubble cap trays.
The packing material for cohobation column may be selected out of berl saddles, intalox saddles, raschig rings pall rings and any othei compatible standard packing material.
The type of packing for cohobation column may be symmetric or random.
The distillation unit may be used for water distillation, steam distillation and steam and water distillation.
The process of the present invention for distillation of essential oils is detailed below:
The flower material is charged in the still along with sufficient quantity of water. The heaters are switched on prior to steam injection to allow minimum condensation of steam inside the still. Then the steam is directly forced through the spurger in to the flower mass which keeps on stirring the mass besides providing heat for distillation. The vapours evolved from the tank are enriched with more volatile constituents in the cohobation column. The vapours with desirable constituents coming out of the cohobation column are condensed in the condenser and collected in the receiver. The distillate in the receiver is separated on the basis of density difference into first rose oil and first rose water. The rose water
from three batches is pooled and is redistilled to recover the remaining rose oil. Redistillation of rose water employs heating through steam jacket and heaters.
A mixture of two mutually insoluble compounds, like oil and water, boil when its temperature is raised to the point where the combined vapour pressure becomes equal to the surrounding pressure. The basic principle of steam distillation, therefore, consists in bringing the two mutually insoluble liquids into contact at a temperature very close to the boiling point of the more volatile liquid of the two. At this stage small addition of vapour pressure by the low volatile fluid, make the combined pressure equal to the surrounding pressure. The mixture then boil and the oil vapourise into the passing steam as fast as its requirement of latent heat can be fulfilled.
Steam generated in a separate boiler is passed through mass. Steam imparts its latent heat to the mass by way of condensation on the surface of flower which, ultimately causes the transfer of oil from glands to the surface of the flower. Further, no sooner the temperature of any layer of mass reaches to an equilibrium point the droplets of oil on the surface of flower start vapourising and the necessary current to lift the vapours of oil from surface of material to the top is provided by latent heat of steam.
The following examples are given by way of illustration of the device and the process of the present invention for the distillation of essential oils and should not be construed to limit the scope of the present invention.
Example 1:
The essential oil distillation unit shown in fig.: 3 with the following features was constructed and installed at an altitude of 1350 m msL (mean sea level) where the water boils at a temperature of
96 C with vapour pressure 644.4 mm Hg (0.876 kg/cm). Processing o 1200 kg flowers of Rosa damascena was standardised for the production of quality grade rose oil.
(A) Constructional Features : -
The unit comprised four parts;
1. The still
2. The condenser
3. The receiver-cum-separator
4. A boiler for generation of steam.
l.The Still:-
The still commonly called as "tank" (1) with actual volume = 2235.75 lit. (excluding top lid volume = 82.33 lit.) and thickness = 4mm primarily serving as a container for holding the plant material, and as a vessel in which the water and/or steam contacts the material
and vapourises its essential oil was used. In its simple form the still consisted of merely a cylindrical container with length egua! to 1.7 times the diameter of tank and equipped with a removable cove (10) device used for holding the top of the still and consists of simple water seal (21). A charging hole (20) was introduced on the still top/lid to charge the plant material and water into the still. Similarly, a discharging hole (9) on one side of the cylindrical tank (1) was welded just above the false bottom (8) to remove the spent material after processing and for any other related operations. Electric kettle elements of 2 kW (6 nos.) (6) were fixed in the actual bottom of the still. A false bottom (8) was placed sufficiently far above the real bottom of the still so that it could hold the herbal materials and do not come in contact with the heaters (6) below to avoid charring. A perforated coil of 3/4"ø pipe with cross (5) below the false bottom (8) which enters through the side of the still was provided to pass the live steam. Holes of l/8"ø were drilled on the top of each arm throughout its length to ensure optimum and even steam distribution. The distance between bottom of the retort (1) and to false bottom (8) was 250 mm to permit any water condensing within the retort. The bottom of the still was provided with a drain valve of 2"ø (gate valve) (?) so that the
spent water could easily be drained off along with some fine suspended spent plant material after completion of the process. Around the cylindrical tank within the steam jacket (2) portion four stiffeners of 25x25x3 thick iron angles were welded on vessel at 200mm
intervals. This was required, to prevent buckling when high pressure of steam was introduced in the steam jacket. This steam jacket (2) was made up of Mild Steel (MS) with a thickness of 4mm, internal diameter (ID) = 1400 mm with cylindrical height of 1000mm to cover the stainless steel tank (1) from outside and bottom. Steam jacket (2) was provided with a pressure gauge (18) span 0-100 psig, 6" dial type, i"ø vent cock by its side to release the unwanted/excess steam or air and to maintain it at a required pressure. A safety valve was also provided on the steam jacket. A dial type temperature gauge with extension lead having a temperature range of 0-150 ° C with 1 ° division to measure the temperature inside the tank was fixed. Another temperature gauge and pressure gauge (18) was placed at a height of 1500 mm (approx.) from the vapour outlet (11) of the still. Actual height of cohobation column (13) was 1500 mm, and had four spherical loops of ID = 200 mm, ID of column = 100 mm and was well insulated so that optimum condensation occurs in the vapour line. All joints were welded and steam tight, as any steam leak could lead to loss of essential oil and fuel.
2.The Condenser:-
The details of condenser used are given below; SHEpL AND TUBE EXCHANGER DATA SHEET;
1. Service of the unit : Mixture of vapours (oil & water)
2. Type : Simple shell and tube (1-1) counter flow condenser.
3. Horizontal/Vertical : Horizontal
4. Surface area : 23,56,195 mm2
(Table Removed)
3. The Oil Receiver-cum-Separator:-
The material of construction (MoC) of the receiver-cum-separator (17) was Stainless Steel-304 having a diameter = 500 mm and could hold 110 lit. of distillate in it. A long stemmed funnel (16) was welded onto the separator for receiving the distillate. The lower outlet of the funnel was turned upward. On an average the separator received water to oil weight ratio of 4760:1. To remove excess water continuously', a water outlet (22) 25 mm SS pipe, 16 BWG was provided. For collecting oil after completion of the process, a 10 mm stainless steel pipe was welded at the top of the receiver with an anfle of 15° slightly above the condensate outlet pipe. The inner wall of the receiver-cum-separator (17) was highly polished.
4. A Boiler for Steam generation:-
The boiler with a capacity to generate 500 kg of steam per hour was
used.
(B) Working details _:-
In the beginning, 400 lit. of fresh water was charged into the sterilised/rinsed still (1). Then heaters (6) were switched on to heat the water to 601. Four hundred kilograms of freshly plucked rose flowers were charged into the still through the charging hole (20). Then the charging hole (20) was tightened so that the vapours do not escape during the process. Live steam was used to heat the mixture in the still (1), through perforated steam coil (spurger) (5). After reaching the boiling point of the mixture in the still, the steam
was controlled so that the gauge pressure of the steam in the boiler
2 was maintained between 2-4 kg/cm and the flow rate of the same was
adjusted such that the flow rate of distillate must be around 50 lit/hr. The range of shell side fluid flow rate in condenser (23) is maintained at 200 to 250 lit/hr. The distillate was collected in an oil receiver-cum-separator (17). The total distillate collected equaled to the fresh water fed into the still (1) in the beginning. The rose oil was separated from rose water. The collected rose water was stored. In the same way 3 batches of rose water collected was charged in the still (1) and was heated by electric heaters (6) and by passing the steam through the means (3) to the steam jacket (2). 400 lit. of rose water was collected @ 35-40 lit/hr. Some of the oil first retained in a tubular rose oil separator further the distillate along with some oil droplets were collected in the receiver-cum-separator. The rose oil settled in the receiver above the rose water was separated out after circulating tepid water around the receiver-cum-separator (17). The separated rose oil was dried by adding anhydrous sodium sulphate. The dried rose oil was measured and stored in aluminum containers for three months to attain maturation of the oil. The oil was then further analysed for its quality and results given below.
23. 24. 25. 26.
Design Pressure (DP) =3 kg/on2
Test Pressure (TP) = 0.876 kg/on2
= 110 °C
= 96 °C
Design Temperature (DT) Working Temperature (WT)


27. SS Tubes:OD ID BWG Length Thk. Pitch Nos.19.05 15.75 16 15001.65 28
5028. Shel1 cover: Welded to tube sheet29. Channel: Welded with dished ends
30, Tube sheets : Stationary
31. Baffles: Type Spacing Thickness Hole Dia.
25% cut 165 2.0 20
32, Gasket:MoCODID
Thickness
Firefly 400
2803.0
33. Corrosion allowances= 1.0 mm
34. Tube to tube sheet joint
34. Tubes are screwed into tube sheet

and then welded.
35. Radiography
Spot
36. TEMA Class-C
37. Remarks:
A) All dimensions are in mm until unless stated
B) The condenser is to be cleaned once in a season
C) Stress relief : Nil.
(a) Quantitative results:
given herein;

(Table Removed)
Example 2:
$team distillation of Lavender Oil :
Three hundred and twenty five kilograms of freshly plucked lavender spikes were charged into the still, through the charging hole. Then the charging hole was tightened. The process was best started with steam of low pressure (saturated steam) with rapid distillation, followed by steam of higher pressure towards the end of the distillation. The water below the false bottom was drained off from time to time through the spent water outlet to control the ester aaponification to increase the ester value which is the main constituent in quality determination. The uniqueness in the system was the steam inside the steam jacket prevented the condensation of any steam within the still and maintained the quality of lavender oil.
The vapour evolved from the still was condensed in the horizontally fixed condenser (23) and the distillate was collected in the receiver-cum-separator (17) through distillate carrier line (19). The process was continued for 3| hours. The oil settled in the receiver-cum-separator (17) was separated, dried, weighed and then stored in aluminum bottles. The recovery of the oil was 1.4%.
Example 3:
Water distillation of celery seed oil:
Three hundred kilograms of celery seeds were churned with 1200 lit of cold water in churning tank till the slurry of seeds and water formed. The churning was done with the mechanical stirrer, driven by an electric motor. The time for churning was about an hour. The slurry of seeds was soaked for 12 hrs. The slurry was transferred to distillation still with the help of slurry pump. After the slurry was fed into the distillation still, the whole mass was heated by indirect steam to effect the distillation. Once the distillation started, the temperature inside the still is maintained at 95 ° C by controlling indirect steam. During the process of distillation the live steam was injected into the slurry within the still for a period of 5 minutes at an interval of 30 minutes.
The oil vapours along with the steam passes through the cohobation column, then to the condenser where the mixture of vapours were cooled to a temperature of 20 to 25 ° C in order to avoid the congealing of the lighter fraction of the oil, which distill over at first. 360 lit. of distillate was collected in 8 hours. The oil settled in the receiver above the distillate was separated. The water traces in the separated oil were removed by the addition of sodium sulphate. The oil is then decanted from sodium sulphate and stored in prescribed bottles. The recovery of the oil was 2.1%.
The main advantages of the present invention are :
1. This improved distillation unit enables the unique distillation
process employing a synergistic combination of water and steam
distillation and steam distillation which significantly enhances the
rose oil recovery and its quality on commercial scale.
2. The distillation unit can be used for any one or more of the
hydrodistillation techniques viz., water distillation, water and steam
distillation and steam distillation.
3. This distillation unit has the unique advantage that the flowers
do not need to be comninute before charging. Thus, saving time and
money as wel1.
4. The built-in cohobation column helps in getting 70 to 80% of
the total essential oil as decanted/first oil. Qualitatively, the
decanted or direct oil is better than water oil or redistilled oil.
5. Tubular oil separator specifically designed for better rose oil
separation, helps in retaining the rose oil in tubes by virtue of its
surface tension and adhesive forces, from rose water.
6. The provision of heating elements inside the still allows
heating of charged water before steam injection. Thereby minimises
the condensation of steam, thus maintaining essential oil quality by
avoiding dilution effect.
7. A perforated steam coil/spurger helps in passing live steam to
transfer its latent heat directly to the aromatic botanical without
forming agglutinates and eliminating the problems of charring of rose
flowers which is important in maintaining the quality of essential
oil.
8. The chargeable quantity in the still is about 25% more in this
steam based distillation unit compared with direct fired distillation
unit.




We claim :
1. A device useful for the distillation of essential oils which comprises a
distillation tank (1) having an external jacket (2) connected to means
(3,4) for steam supply (3) and steam trap (4); the distillation tank being
provided at its bottom portion with means (5,6,7) for steam spurging
(5), auxiliary heating (6), and an outlet (7); above the said steam
spurger and auxiliary heatrs being provided a removably fixed grating
(8), above the said grating (8) being provided atleast one opening (9)
for discharging of spent materials; the said distillation tank being
provided at its top portion with removably sealed cover (10) having at
least one opening (20) for charging of materials and atleast one vapour
outlet (11), the said one or more vapour outlet(s) being connected by
known means (12) to the bottom end of one or more known cohobation
head column(s) being connected by known means (12) to the inlet (14)
of a known condenser unit (23), the outlet (15) of the said condenser
(23) being connected through pipe (19) to the inlet (16) of a tubular oil
separator, the outlet of the said tubular oil separator being fed to a
known receiver-cum-separator (17).
2. A device as claimed in claim 1 wherein the distillation tank is provided
with means (18) for measuring parameters such as temperature,
pressure, water level.
3. A device as claimed in claims 1 & 2 wherein the distillation tank has
length to diameter ratio in the range of 1 to 2.
4. A device as claimed in claims 1-3 wherein the means used for auxiliary
heating is such as steam, electric heating elements.
5. A device as claimed in claims 1-4 wherein the cohobation head column
used is such as corrugated, hollow, packed, with sieve trays, bubble
cap trays.
6. A device as claimed in claims 1-5 wherein the inlet (16) of the tubular
oil separator is such as having a plurality of vertical tubes for retention
of oil.
7. A device as claimed in claims 1-6 wherein the receiver-cum-separator
unit (17) is connected by a pipe line (24) to the cohobation column to
enable reflux.
8. A device useful for the distillation of essential oils substantially as
herein described with reference to the examples and drawings
accompanying this specifications.

Documents:

272-del-1999-abstract.pdf

272-del-1999-claims.pdf

272-del-1999-correspondence-others.pdf

272-del-1999-correspondence-po.pdf

272-del-1999-description (complete).pdf

272-del-1999-drawings.pdf

272-del-1999-form-1.pdf

272-del-1999-form-19.pdf

272-del-1999-form-2.pdf


Patent Number 230990
Indian Patent Application Number 272/DEL/1999
PG Journal Number 13/2009
Publication Date 27-Mar-2009
Grant Date 28-Feb-2009
Date of Filing 19-Feb-1999
Name of Patentee COUNCIL OF SCIENTIFIC & INDUSTRIAL RESEARCH
Applicant Address RAFI MARG, NEW DELHI-110001, INDIA.
Inventors:
# Inventor's Name Inventor's Address
1 GARIKIPATI. D. KIRAN BABU INSTITUTE OF HIMALAYAN BIORESOURCE TECHNOLOGY, PALAMPUR, (H. P.), INDIA.
2 VIJAY KUMAR KAUL INSTITUTE OF HIMALAYAN BIORESOURCE TECHNOLOGY, PALAMPUR, (H. P.), INDIA.
3 RAM PRAKASH SOOD INSTITUTE OF HIMALAYAN BIORESOURCE TECHNOLOGY, PALAMPUR, (H.P.), INDIA.
4 VIRENDRA SINGH INSTITUTE OF HIMALAYAN BIORESOURCE TECHNOLOGY, PALAMPUR, (H. P.), INDIA.
5 BIKRAM SINGH INSTITUTE OF HIMALAYAN BIORESOURCE TECHNOLOGY, PALAMPUR, (H. P.), INDIA.
PCT International Classification Number C11B9/02
PCT International Application Number N/A
PCT International Filing date
PCT Conventions:
# PCT Application Number Date of Convention Priority Country
1 NA