Continuous type Edible Oil Refinery Plant
Continuous Type Oil Refinery Plant is recommended against the batch
refining for higher capacity plants above 30 tons per day and for oils
containing higher FFA content. This process line is bit expensive than
batch process but it provides superior quality refined oil along with
automation system and low processing cost.
Continuous Vegetable Oil Refinery Factory
Unlike batch oil refining process in which oil is processed in measured
batch, in Continuous Vegetable Oil Refinery, crude oil is processed
continuously with a constant stream of flow. During the process,
necessary chemicals and other utility items added continuously in the
measured quantity. There are present foreign impurities such as gums,
mucilage and unfiltered proteinous matter from the seed in the crude oil
extracted from expellers. It also contains gums which makes the oil
unfit for edible purpose.
Basic stages of the process are as below :
Nutralizing
Bleaching
Dewaxing & Deodorizing
The De gumming / Neutralizing System are used as the first step in
chemical refining referred to as Neutralizing. This step will generally
produce oil with lower levels of residual phosphatides and less residual
pigments and therefore require less bleaching earth in bleaching as
well as help generate finished deodorized oil with a lighter colour and
longer shelf life. The Bleaching System is based on treatment with
bleaching earth followed by filtration. The High Efficiency Deodorizing
System can be used for deodorizing of neutralized oils as well as
stripping and deodorizing of high FFA oils as part of physical refining.
Features and specifications:
Water Washing: The residual soap in the de gummed &
neutralized oil is reduced by water washing. In this case the oil from
the separator is heated to about 95 C in the Washing Heater and then
mixed with 10 - 15% soft water in the Wash Mixer.
Vacuum drying: Washed oil is fed continuously to the
Vacuum dryer and sprayed through specially designed nozzles. The vacuum
dryer is kept under a vacuum of 70 torr. The dried oil from the vacuum
chamber is continuously pumped out by pump P105 to intermediate storage
tank (not included).
Bleaching: The feed oil (Acidic treatment, de gummed /
neutralized & washed) enters the Bleacher via a Bleaching heater
where the oil is heated up to Bleaching temperature and discharged into
the slurry mixer. A valve dosing system proportions bleaching earth. The
earth is introduced under the oil spray in the mixing chamber for
improved mixing so that earth does not enter the Bleaching Vacuum
System.
Deodorizing: Bleached oil is continuously pumped from
the Feed Tank by the Deareator Feed Pump. The oil is pre-heated in the
Deaerating Economizer by outgoing deodorized oil followed by the
Deaerating Heater (if necessary) before entering the Deaerator.
Stripping: The hot oil enters the Packed Column, which
is filled with special structured packing so that the oil is distributed
into a thin film and is evenly agitated by stripping steam flowing
counter currently from the bottom of the column.
Deodorizing: The stripped oil from the column flows
into the Deodorizer where it flows through the channels of a series of
vertically stacked compartments (trays) while agitated by stripping
steam. The prolonged thermal action breaks down carotene and other color
bodies, resulting in a lighter oil colour. The stripping steam passes
through the packed column and no separate steam is required in the
stripping column. The maximum retention time in the Deodorizer is 70
minutes.
Dewaxing: After the neutralization the outlet oil
Specification of separator is managed in such a way that it left with
around 3000 to 3500 ppm as soap which acts as seed for the de-waxing .
This oil is first cooled by cooling tower water up o 40 to 45 Deg C.
Then this oil is cooled by outgoing de-waxed oil from the separator.
This oil is then chilled to de-waxing temp and feed to Crystallizers. In
the crystallizer proper residence time is given with maintaining the
temperature of the oil , which results in formation of wax crystals and
residence time will give proper growth to the crystals.
In this a measured quantity of water is added so that the waxes from oil phase moves to water phase with soap stock.
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