Title of Invention	A PROCESS OF PRODUCING DISTILLED FATTY ACIDS AND A SYSTEM THEREFORE
Abstract	This invention relates to a process for producing distilled fatty acid comprising the steps of feeding pre heated crude split oil and distilling the same in a distillation column in an atmosphere of a carrier gas such as nitrogen, steam or inert gases, said distillation being carried out at a temperature below 260˚c and at a pressure marginally above atmospheric pressure condensing the vapours of fatty acids therefrom in at least one condenser, cooling and collecting the condensate (DFA), recycling the carrier gas from the condenser, to the distillation column after heating. This invention also includes a system for carrying out the process described.

Title of Invention

A PROCESS OF PRODUCING DISTILLED FATTY ACIDS AND A SYSTEM THEREFORE

Abstract

This invention relates to a process for producing distilled fatty acid comprising the steps of feeding pre heated crude split oil and distilling the same in a distillation column in an atmosphere of a carrier gas such as nitrogen, steam or inert gases, said distillation being carried out at a temperature below 260˚c and at a pressure marginally above atmospheric pressure condensing the vapours of fatty acids therefrom in at least one condenser, cooling and collecting the condensate (DFA), recycling the carrier gas from the condenser, to the distillation column after heating. This invention also includes a system for carrying out the process described.

Full Text	FORM 2 THE PATENTS ACT 1970 (39 of 1970) & THE PATENTS RULES, 2003 COMPLETE SPECIFICATION (See Section 10; rule 13) TITLE OF THE INVENTION A Process Of Producing Distilled Fatty Acid And A System Therefor APPLICANTS TCE Consulting Engineers Limited, Matulya Centre A 249 Senapati Bapat Marg, Lower Parel (West) Mumbai 400 013, Maharashtra, India, an Indian Company INVENTOR Bhaurao M Nichat an Indian National of TCE Consulting Engineers Limited, Matulya Centre A 249 Senapati Bapat Marg, Lower Parel (West) Mumbai 400 013, Maharashtra, India, an Indian Company PREAMBLE TO THE DESCRIPTION The following complete specification particularly describes the nature of the invention and the manner in which it is to be performed. FIELD OF INVENTION This invention relates to a process of producing Distilled Fatty Acid (DFA) and a system for manufacturing the same. BACKGROUND OF INVENTION During the last decade, many companies have decided to switch over to distilled fatty acid (DFA) as a main feedstock for manufacturing premium soaps replacing the mix of oils used earlier. In order to meet this increased demand, the installed capacity of DFA plants in the country has been rapidly increasing. Thus the need to make the DFA process more efficient, simple and economical is of vital importance for the industry and the country at large. Conventionally, Distilled Fatty Acid (DFA) is produced from crude split oil by vacuum distillation. Distillation is carried out at low pressure (less than 6 mm Hg) and at about 240 degree Centigrade temperature. A small amount of steam is sparged in the crude split oil to facilitate distillation rate. Steam ejector with barometric condensers system provides the vacuum. Heat for vaporization of Distilled fatty acid is provided by thermic fluid heater and DFA is condensed in surface type water cooled condensers. After vaporization of fatty acids, residue containing mostly degraded oil remains in the distillation still, which is continuously removed, cooled and stored for final disposal. Stainless steel 304L or SS316 is a material of construction for all components of the plant. The conventional process of producing DFA as outlined in Fig 1 comprises of following steps: a. Split oil containing residual oil and free fatty acid having very dark black-red color is continuously fed to distillation column, where the distillation takes place at about 240 degree centigrade b. Distillation column mass is continuously heated in "reboiler", where it is heated by hot thermic fluid to vaporize the free fatty acids at a pressure less than 6 mm Hg. (vacuum of 754-756 mm Hg.), at about 240 degree centigrade c. Fatty acids vaporized are taken to surface type water cooled condensers to condense all the fatty acid. Cooling is done by cooling water obtained from cooling water system. d. Vacuum (pressure of less than 6 mm Hg.) is produced by multi-stage steam -jet ejectors and barometric condenser . Steam is used as motive fluid and cooling water for condensing the steam in barometric condenser to produce the desired vacuum. e. Thermic fluid is heated in thermic fluid boiler system by fuel oil. The hot thermic fluid thus obtained from thermic fluid boiler system is used to provide heat for vaporization of free fatty acids . f. Residue after distillation of free fatty acids is drawn out from distillation column continuously , is cooled and transferred to residue tank for storage. g. DFA condensed in surface cooled condensers is cooled up to 40 degree centigrade by cooling water in separate cooler / heat exchanger and stored In conventional process, distillation is carried out under vacuum because in the presence of oxygen. Fatty acids degrade at high temperature. Due to vacuum, ingress of oxygen is minimized and vaporization can be carried out at lower temperatures .. The conventional process suffers from following limitations: a. It requires large amount of steam and cooling water towards generation of vacuum . b. Material loss in the barometric condensers leads to generation of oily effluent creating effluent and pollution. . c. Fatty Acid Distillation plant with vacuum systems are expensive d. Plant with vacuum system has operating difficulties resulting in downtime on the plant, in case there is a minor leakage. e. Energy consumption is very high. Utilities consumptions in the conventional process are as follows: TABLE 1 Typical Utilities Consumptions for 1000 kg of DFA produced : H P Steam, Kilograms 250 L P Steam, Kilograms 100 Fuel oil, Kilocalories 200,000 Power, Kilowatt hours 30 Cooling Water (in circulation), Cubic Meter 65 Effluent, Cubic Meter 3 OBJECTS OF INVENTION The main object of the invention is to provide a novel process for manufacturing Distilled Fatty Acid (DFA). Another object of the invention is to provide a system for manufacturing DFA with no vacuum requirement for the processing and with less steam and cooling water requirement. Yet another object of the invention is to provide a system for manufacturing DFA, which operates with less fuel consumption. Another object of the invention is to provide a system for manufacturing DFA, which is easy to operate. Yet another object of the invention is to provide a system for manufacturing DFA, which eliminates the risk of frequent downtime of the system. SUMMARY OF THE INVENTION In the present invention, attempt is made to minimize or eliminate the drawbacks of the prior art processes. In the present invention, a new process is provided for manufacturing DFA and a system is provided for manufacturing DFA in accordance with the said new process. In accordance with the present invention, fatty acid distillation is carried out at marginally higher pressure than atmospheric pressure and at temperature equal or less than 260 degree centigrade. In this distillation process, nitrogen is used as carrier gas. Pressure being higher than atmospheric, ingress of oxygen in the system is prevented. DFA is condensed in the water-cooled condensers and nitrogen is recirculated via process blower. Flow rate of nitrogen can be adjusted through speed of process blower to regulate the fatty acid distillation rate. Vacuum system including barometric condenser is not required. Cooling water requirement in the barometric condensers is eliminated and cooling water quantity in the condensers is considerably reduced as re circulated gas and crude split oil is preheated in the condensers Depending on the concentration of free fatty acid in crude split oil, quantity of nitrogen required is varied with the help of process blower. However, all the nitrogen is recycled except the bleed-off, which is required in case of organic non-condensable build-up in the system. Quantity of nitrogen required is to fill up the complete system as initial charge and subsequently, have marginal make-up as required in-lieu-of the bleed-off. Heat for distillation and vaporization of distilled fatty acid is provided by thermic fluid heater. DFA is condensed in water cooled condensers and stored. After vaporization of fatty acids, residue containing mostly degraded oil remains in the distillation still, and is continuously removed, cooled and transferred for storage. STATEMENT OF INVENTION This invention relates to a process for producing distilled fatty acid comprising the steps of feeding pre heated crude split oil and distilling the same in a distillation column in an atmosphere of a carrier gas such as nitrogen, steam or inert gases, said distillation being carried out at a temperature below 260°c and at a pressure marginally above atmospheric pressure condensing the vapours of fatty acids therefrom in at least one condenser, cooling and collecting the condensate (DFA), recycling the carrier gas from the condenser, to the distillation column after heating. This invention also relates to an integrated system for producing distilled fatty acid from crude split oil comprising means for heating crude split oil, a distillation column connected thereto and leading to atleast one condenser, means for supplying a carrier gas such as nitrogen, steam and the like to said distillation column, said condenser means having means for recycling the carrier gas therefrom to said distillation column, means for collecting the condensate and cooling means for cooling the condensers and conventional instrumentation and controls for operating the same. BRIEF DESCRIPTION OF DRAWINGS Fig. 1 - shows the flowchart of conventional system for manufacturing Distilled Fatty Acid Fig.2 - shows the flowchart of the system for manufacturing DFA in accordance with this invention DETAILED DESCRIPTION OF INVENTION Referring to Fig. 2, the system for manufacturing of Distilled Fatty Acid in accordance with new process of this invention, comprises of the following: a. Distillation still b. Re-circulation pump c. Re-boiler d. Crude Split Oil Heater e. Recycled Nitrogen gas heater f. DFA Condenser - 1 g. DFA Condenser - 2 h. DFA Condenser - 3 i. Process blower j. DFA coolers (3 Nos.) k. Residue cooler 1. DFA storage m. Residue Storage n. Nitrogen cylinders connected to system for make-up o. Piping and valves p. Instrumentation and controls and electrical Stream Numbers as given in Fig. 2 , with their flow rates and temperatures for New process of DFA manufacture are given below : Stream Numbers 1 2 3 4 5 6 7 8 9 10 Mass Flow , Kg/h DFA 1000 300 700 15 285 - 15 ~ ~ — Nitrogen 6600 6600 - 6600 -- 6600 - 6600 6600 6600 Temperature (Deg.centigrade) 260 193 40 146 40 130 40 130 245 260 The invention relates to a new process for manufacturing the DFA comprising the following steps: a. All the equipments in the system are filled with nitrogen gas. This is done by purging nitrogen gas from nitrogen gas cylinders after evacuating the system with the help of vacuum pump. This is required only during start-up of the system. After this, vacuum pump is de-linked from the system, as it is no more required. b. Crude split oil from its storage having very dark black-red color is preheated in DFA condenser -2 and further heated in crude split oil heater . Hot crude split oil is then fed to distillation column. c. Distillation column mass is continuously re-circulated by pump through "reboiler", where it is heated by hot thermic fluid. Heated crude split oil is fed back to distillation column, where fatty acid vapors are generated. d. Distillation is facilitated by nitrogen gas which was fed in the system at the start up. Fatty acids vapor with nitrogen gas is taken to condensers system (condenser- 1, condenser-2 & condenser-3), where all DFA condenses. Nitrogen being non- condensable is recycled via process blower. DFA condensed in condensers system is further cooled in DFA coolers and transferred to DFA tank for storage. Recycled Nitrogen is heated through DFA condensers to a higher temperature and further heated by hot thermic fluid in recycled nitrogen heater and is fed to distillation column. e. Thermic fluid is heated in thermic fluid boiler system by means of fuel. Hot thermic fluid is then circulated to this DFA system for heating in crude split oil heater, reboiler, recycled nitrogen heater. f. Cooling water is brought to this DFA system from cooling water system for cooling in DFA condenser-3,DFA coolers , residue coolers . g. After distillation of free fatty acid residue is transferred from distillation column continuously, cooled and stored The novel process for manufacturing DFA as described in claim 1, wherein fatty acid is either rice bran fatty acid or palmitic acid or stearic acid etc. The novel process for manufacturing DFA in accordance with this invention wherein temperature of distillation is less than 260 degree centigrade .. The novel process for manufacturing DFA in accordance with this invention uses steam or nitrogen gas. The new process for manufacturing DFA in accordance with this invention wherein distillation pressure is more than atmospheric pressure. Utilities consumptions in the new process are as follows: TABLE 2 Typical Utilities consumption for 1000 kg of DFA produced in the new process H P Steam, Kilograms NIL L P Steam, Kilograms NIL Fuel oil, KiloCalories 170000 Power, Kilo Watt-hours 10 Cooling Water (in circulation), Cubic Meter 15 Nitrogen Gas, Cubic Meter at 1.25 kg/ sq.cm o.25 Effluent, Cubic Meter 0.5 Quality of DFA Same or Better than in conventional process The foregoing description is a specific embodiment of the present invention. It should be appreciated that this embodiment is described for purpose of illustration only, and the numerous alteration and modifications may be practiced by those skilled in the art without departing from the spirit and the scope of the invention. It is intended that all such modifications and alteration be included in so far as they come within the scope of the invention as claimed or the equivalents thereof. WE CLAIM 1. A process for producing distilled fatty acid comprising the steps of feeding pre heated crude split oil and distilling the same in a distillation column in an atmosphere of a carrier gas such as nitrogen, steam or inert gases, said distillation being carried out at a temperature below 260°c and at a pressure marginally above atmospheric pressure condensing the vapours of fatty acids therefrom in at least one condenser, cooling and collecting the condensate (DFA), recycling the carrier gas from the condenser, to the distillation column after heating. 2. The process as claimed in claim 1 fatty acids like palmitic acid, stearic acid and rice bran fatty acids are distilled from their respective crude split oil. 3. The process as claimed in claims 1 and 2 wherein the distillation and the recycled carrier gases are heated by thermic fluid. 4. An integrated system for producing distilled fatty acid from crude split oil comprising means for heating crude split oil, a distillation column connected thereto and leading to atleast one condenser, means for supplying a carrier gas such as nitrogen, steam and the like to said distillation column, said condenser means having means for recycling the carrier gas therefrom to said distillation column, means for collecting the condensate and cooling means for cooling the condensers and conventional instrumentation and controls for operating the same. 5. A process for producing the distilled fatty acid substantially as herein described. 6. The integrated system for producing distilled fatty acid substantially as herein described with particular reference to Fig 2 of the accompanying drawings. ABSTRACT A Process Of Producing Distilled Fatty Acid And A System Therefor This invention relates to a process for producing distilled fatty acid comprising the steps of feeding pre heated crude split oil and distilling the same in a distillation column in an atmosphere of a carrier gas such as nitrogen, steam or inert gases, said distillation being carried out at a temperature below 260°c and at a pressure marginally above atmospheric pressure condensing the vapours of fatty acids therefrom in at least one condenser, cooling and collecting the condensate (DFA), recycling the carrier gas from the condenser, to the distillation column after heating. This invention also includes a system for carrying out the process described

Full Text

FORM 2
THE PATENTS ACT 1970
(39 of 1970)
&
THE PATENTS RULES, 2003
COMPLETE SPECIFICATION
(See Section 10; rule 13)
TITLE OF THE INVENTION
A Process Of Producing Distilled Fatty Acid And A System Therefor
APPLICANTS
TCE Consulting Engineers Limited,
Matulya Centre A 249 Senapati Bapat Marg,
Lower Parel (West) Mumbai 400 013,
Maharashtra, India, an Indian Company
INVENTOR
Bhaurao M Nichat
an Indian National of
TCE Consulting Engineers Limited,
Matulya Centre A 249 Senapati Bapat Marg,
Lower Parel (West) Mumbai 400 013,
Maharashtra, India, an Indian Company
PREAMBLE TO THE DESCRIPTION
The following complete specification particularly describes the nature
of the invention and the manner in which it is to be performed.

FIELD OF INVENTION
This invention relates to a process of producing Distilled Fatty Acid (DFA) and a system for manufacturing the same.
BACKGROUND OF INVENTION
During the last decade, many companies have decided to switch over to distilled fatty acid (DFA) as a main feedstock for manufacturing premium soaps replacing the mix of oils used earlier. In order to meet this increased demand, the installed capacity of DFA plants in the country has been rapidly increasing. Thus the need to make the DFA process more efficient, simple and economical is of vital importance for the industry and the country at large.
Conventionally, Distilled Fatty Acid (DFA) is produced from crude split oil by vacuum distillation. Distillation is carried out at low pressure (less than 6 mm Hg) and at about 240 degree Centigrade temperature. A small amount of steam is sparged in the crude split oil to facilitate distillation rate. Steam ejector with barometric condensers system provides the vacuum. Heat for vaporization of Distilled fatty acid is provided by thermic fluid heater and DFA is condensed in surface type water cooled condensers. After vaporization of fatty acids, residue containing mostly degraded oil remains in the distillation still, which is continuously removed, cooled and stored for final disposal. Stainless steel 304L or SS316 is a material of construction for all components of the plant.
The conventional process of producing DFA as outlined in Fig 1 comprises of following steps:
a. Split oil containing residual oil and free fatty acid having very dark black-red
color is continuously fed to distillation column, where the distillation takes
place at about 240 degree centigrade

b. Distillation column mass is continuously heated in "reboiler", where it is
heated by hot thermic fluid to vaporize the free fatty acids at a pressure less
than 6 mm Hg. (vacuum of 754-756 mm Hg.), at about 240 degree centigrade
c. Fatty acids vaporized are taken to surface type water cooled condensers to
condense all the fatty acid. Cooling is done by cooling water obtained from
cooling water system.
d. Vacuum (pressure of less than 6 mm Hg.) is produced by multi-stage steam -jet
ejectors and barometric condenser . Steam is used as motive fluid and
cooling water for condensing the steam in barometric condenser to produce the
desired vacuum.
e. Thermic fluid is heated in thermic fluid boiler system by fuel oil. The hot
thermic fluid thus obtained from thermic fluid boiler system is used to provide
heat for vaporization of free fatty acids .
f. Residue after distillation of free fatty acids is drawn out from distillation
column continuously , is cooled and transferred to residue tank for storage.
g. DFA condensed in surface cooled condensers is cooled up to 40 degree
centigrade by cooling water in separate cooler / heat exchanger and stored
In conventional process, distillation is carried out under vacuum because in the presence of oxygen. Fatty acids degrade at high temperature. Due to vacuum, ingress of oxygen is minimized and vaporization can be carried out at lower temperatures ..
The conventional process suffers from following limitations:
a. It requires large amount of steam and cooling water towards generation of
vacuum .
b. Material loss in the barometric condensers leads to generation of oily
effluent creating effluent and pollution. .
c. Fatty Acid Distillation plant with vacuum systems are expensive

d. Plant with vacuum system has operating difficulties resulting in downtime
on the plant, in case there is a minor leakage.
e. Energy consumption is very high.
Utilities consumptions in the conventional process are as follows:
TABLE 1
Typical Utilities Consumptions for 1000 kg of DFA produced :

H P Steam, Kilograms 250
L P Steam, Kilograms 100
Fuel oil, Kilocalories 200,000
Power, Kilowatt hours 30
Cooling Water (in circulation), Cubic Meter 65
Effluent, Cubic Meter 3
OBJECTS OF INVENTION
The main object of the invention is to provide a novel process for manufacturing Distilled Fatty Acid (DFA).
Another object of the invention is to provide a system for manufacturing DFA with no vacuum requirement for the processing and with less steam and cooling water requirement.
Yet another object of the invention is to provide a system for manufacturing DFA, which operates with less fuel consumption.
Another object of the invention is to provide a system for manufacturing DFA, which is easy to operate.

Yet another object of the invention is to provide a system for manufacturing DFA, which eliminates the risk of frequent downtime of the system.
SUMMARY OF THE INVENTION
In the present invention, attempt is made to minimize or eliminate the drawbacks of the prior art processes. In the present invention, a new process is provided for manufacturing DFA and a system is provided for manufacturing DFA in accordance with the said new process.
In accordance with the present invention, fatty acid distillation is carried out at marginally higher pressure than atmospheric pressure and at temperature equal or less than 260 degree centigrade. In this distillation process, nitrogen is used as carrier gas. Pressure being higher than atmospheric, ingress of oxygen in the system is prevented. DFA is condensed in the water-cooled condensers and nitrogen is recirculated via process blower. Flow rate of nitrogen can be adjusted through speed of process blower to regulate the fatty acid distillation rate.
Vacuum system including barometric condenser is not required. Cooling water requirement in the barometric condensers is eliminated and cooling water quantity in the condensers is considerably reduced as re circulated gas and crude split oil is preheated in the condensers
Depending on the concentration of free fatty acid in crude split oil, quantity of nitrogen required is varied with the help of process blower. However, all the nitrogen is recycled except the bleed-off, which is required in case of organic non-condensable build-up in the system.

Quantity of nitrogen required is to fill up the complete system as initial charge and subsequently, have marginal make-up as required in-lieu-of the bleed-off. Heat for distillation and vaporization of distilled fatty acid is provided by thermic fluid heater. DFA is condensed in water cooled condensers and stored. After vaporization of fatty acids, residue containing mostly degraded oil remains in the distillation still, and is continuously removed, cooled and transferred for storage.
STATEMENT OF INVENTION
This invention relates to a process for producing distilled fatty acid comprising the steps of feeding pre heated crude split oil and distilling the same in a distillation column in an atmosphere of a carrier gas such as nitrogen, steam or inert gases, said distillation being carried out at a temperature below 260°c and at a pressure marginally above atmospheric pressure condensing the vapours of fatty acids therefrom in at least one condenser, cooling and collecting the condensate (DFA), recycling the carrier gas from the condenser, to the distillation column after heating.
This invention also relates to an integrated system for producing distilled fatty acid from crude split oil comprising means for heating crude split oil, a distillation column connected thereto and leading to atleast one condenser, means for supplying a carrier gas such as nitrogen, steam and the like to said distillation column, said condenser means having means for recycling the carrier gas therefrom to said distillation column, means for collecting the condensate and cooling means for cooling the condensers and conventional instrumentation and controls for operating the same.
BRIEF DESCRIPTION OF DRAWINGS
Fig. 1 - shows the flowchart of conventional system for manufacturing Distilled Fatty Acid

Fig.2 - shows the flowchart of the system for manufacturing DFA in accordance with this invention
DETAILED DESCRIPTION OF INVENTION
Referring to Fig. 2, the system for manufacturing of Distilled Fatty Acid in accordance with new process of this invention, comprises of the following:
a. Distillation still
b. Re-circulation pump
c. Re-boiler
d. Crude Split Oil Heater
e. Recycled Nitrogen gas heater
f. DFA Condenser - 1
g. DFA Condenser - 2
h. DFA Condenser - 3
i. Process blower
j. DFA coolers (3 Nos.)
k. Residue cooler
1. DFA storage
m. Residue Storage
n. Nitrogen cylinders connected to system for make-up
o. Piping and valves
p. Instrumentation and controls and electrical

Stream Numbers as given in Fig. 2 , with their flow rates and temperatures for New process of DFA manufacture are given below :
Stream Numbers 1 2 3 4 5 6 7 8 9 10
Mass Flow , Kg/h
DFA 1000 300 700 15 285 - 15 ~ ~ —
Nitrogen 6600 6600 - 6600 -- 6600 - 6600 6600 6600
Temperature (Deg.centigrade) 260 193 40 146 40 130 40 130 245 260

The invention relates to a new process for manufacturing the DFA comprising the following steps:
a. All the equipments in the system are filled with nitrogen gas. This is done by
purging nitrogen gas from nitrogen gas cylinders after evacuating the system with
the help of vacuum pump. This is required only during start-up of the system.
After this, vacuum pump is de-linked from the system, as it is no more required.
b. Crude split oil from its storage having very dark black-red color is preheated in
DFA condenser -2 and further heated in crude split oil heater . Hot crude split oil
is then fed to distillation column.
c. Distillation column mass is continuously re-circulated by pump through "reboiler",
where it is heated by hot thermic fluid. Heated crude split oil is fed back to
distillation column, where fatty acid vapors are generated.
d. Distillation is facilitated by nitrogen gas which was fed in the system at the start
up. Fatty acids vapor with nitrogen gas is taken to condensers system (condenser-
1, condenser-2 & condenser-3), where all DFA condenses. Nitrogen being non-
condensable is recycled via process blower. DFA condensed in condensers system

is further cooled in DFA coolers and transferred to DFA tank for storage. Recycled Nitrogen is heated through DFA condensers to a higher temperature and further heated by hot thermic fluid in recycled nitrogen heater and is fed to distillation column.
e. Thermic fluid is heated in thermic fluid boiler system by means of fuel. Hot
thermic fluid is then circulated to this DFA system for heating in crude split oil
heater, reboiler, recycled nitrogen heater.
f. Cooling water is brought to this DFA system from cooling water system for
cooling in DFA condenser-3,DFA coolers , residue coolers .
g. After distillation of free fatty acid residue is transferred from distillation column
continuously, cooled and stored
The novel process for manufacturing DFA as described in claim 1, wherein fatty acid is either rice bran fatty acid or palmitic acid or stearic acid etc.
The novel process for manufacturing DFA in accordance with this invention wherein temperature of distillation is less than 260 degree centigrade ..
The novel process for manufacturing DFA in accordance with this invention uses steam or nitrogen gas.
The new process for manufacturing DFA in accordance with this invention wherein distillation pressure is more than atmospheric pressure.

Utilities consumptions in the new process are as follows:
TABLE 2
Typical Utilities consumption for 1000 kg of DFA produced in the new process

H P Steam, Kilograms NIL
L P Steam, Kilograms NIL
Fuel oil, KiloCalories 170000
Power, Kilo Watt-hours 10
Cooling Water (in circulation), Cubic Meter 15
Nitrogen Gas, Cubic Meter at 1.25 kg/ sq.cm o.25
Effluent, Cubic Meter 0.5
Quality of DFA Same or Better than in conventional process
The foregoing description is a specific embodiment of the present invention. It should be appreciated that this embodiment is described for purpose of illustration only, and the numerous alteration and modifications may be practiced by those skilled in the art without departing from the spirit and the scope of the invention. It is intended that all such modifications and alteration be included in so far as they come within the scope of the invention as claimed or the equivalents thereof.

WE CLAIM
1. A process for producing distilled fatty acid comprising the steps of feeding pre heated crude split oil and distilling the same in a distillation column in an atmosphere of a carrier gas such as nitrogen, steam or inert gases, said distillation being carried out at a temperature below 260°c and at a pressure marginally above atmospheric pressure condensing the vapours of fatty acids therefrom in at least one condenser, cooling and collecting the condensate (DFA), recycling the carrier gas from the condenser, to the distillation column after heating.
2. The process as claimed in claim 1 fatty acids like palmitic acid, stearic acid and rice bran fatty acids are distilled from their respective crude split oil.
3. The process as claimed in claims 1 and 2 wherein the distillation and the recycled carrier gases are heated by thermic fluid.
4. An integrated system for producing distilled fatty acid from crude split oil comprising means for heating crude split oil, a distillation column connected thereto and leading to atleast one condenser, means for supplying a carrier gas such as nitrogen, steam and the like to said distillation column, said condenser means having means for recycling the carrier gas therefrom to said distillation column, means for collecting the condensate and cooling means for cooling the condensers and conventional instrumentation and controls for operating the same.
5. A process for producing the distilled fatty acid substantially as herein described.

6. The integrated system for producing distilled fatty acid substantially as herein described with particular reference to Fig 2 of the accompanying drawings.

ABSTRACT
A Process Of Producing Distilled Fatty Acid And A System Therefor
This invention relates to a process for producing distilled fatty acid comprising the steps of feeding pre heated crude split oil and distilling the same in a distillation column in an atmosphere of a carrier gas such as nitrogen, steam or inert gases, said distillation being carried out at a temperature below 260°c and at a pressure marginally above atmospheric pressure condensing the vapours of fatty acids therefrom in at least one condenser, cooling and collecting the condensate (DFA), recycling the carrier gas from the condenser, to the distillation column after heating. This invention also includes a system for carrying out the process described

Documents:

http://ipindiaonline.gov.in/patentsearch/GrantedSearch/viewdoc.aspx?id=dgwUlB7KKkzXbSJMIH8Pzw==&loc=vsnutRQWHdTHa1EUofPtPQ==

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Patent Number

272526

Indian Patent Application Number

158/MUM/2008

PG Journal Number

15/2016

Publication Date

08-Apr-2016

Grant Date

06-Apr-2016

Date of Filing

23-Jan-2008

Name of Patentee

TATA CONSULTING ENGINEERS LIMITED

Applicant Address

MATULYA CENTRE A 249, SENAPATI BAPAT MARG, LOWER PAREL(WEST), MUMBAI-400013, MAHARASHTRA, INDIA

Inventors:

#	Inventor's Name	Inventor's Address
1	BHAURAO M. NICHAT	MATULYA CENTRE, 'A',249 SENAPATI BAPAT MARG, LOWER PAREL(WEST), MUMBAI-400013.

PCT International Classification Number

C07C209/00

PCT International Application Number

N/A

PCT International Filing date

PCT Conventions:

#	PCT Application Number	Date of Convention	Priority Country
1			NA