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Cooking Oil Factory

 

COTTON PRESSING UNIT DIAGRAMME

PRESSING UNIT DIAGRAMME

COTTON PREPERATION SECTION PRESS SECTION
CODE QUANTITY EXPLANATION CODE QUANTITY EXPLANATION
PHE 2 Pneumaric Air Screener HHV1 1 FLAKING MILL
HEF 2 Air Screener Flue System HKT1 2 TOOSTER
KEM 1 Breaker and Screener Machine HMP1 2 PRESS
KFS 1 Breaker Flue System HVE3 1 VIBRATION SCREENER
TKC 1 Twin Tambour Hull Screener HBF6 1 FILTER-PRESS
KFS 1 Hull Circle Flue System HP1 1 PUMP
      HP2 1 PUMP
      HDH3 - VERTICAL HELIX
      HYH3 - HORIZONTAL HELIX
      HAT1 1 UNDERGROUND OIL TANK
      HAT2 1 UNDERGROUND OIL TANK
      HUT1 1 GROUND OIL TANK

CAPACITY OF COTTON PRESSING UNIT : 150 Metric Tonnes / Day

 

CRUDE VEGETABLE OIL EXTRACTION UNIT DIAGRAMME

EXTRACTION UNIT DIAGRAMME

CRUDE VEGETABLE OIL EXTRACTION UNIT EQUIPMENTS

EXTRACTION SUBSIDIARY EQUIPMENT
CODE QUANTITY EXPLANATION CODE QUANTITY EXPLANATION
1D201 1 MOVING CELL EXTRACTOR 1D302 1 SOLVENT WATER SEPERATOR
1E220 7 MISELLA FRONT HEATER 1D312 2 HYDRO CYCLON
1E221 1 SOLVENT FRONT HEATER 1E303 1 CHURN WATER DESOLVENTIZER
1G2101 1 FRESH SOLVENT PUMP 1F301 1 SOLVENT WORK TANK
1G211/217 7 MISELLA PUMP 1F305 1 WHOLE MISELLA TANK
1 G 211.2/271.2 1 WHOLE MISELLA PUMP 1F321 1 CONDENS STEAM TANK
1G261 1 CHAIN CONVEYOR 1G3041 1 WHOLE MISELLA FILTER
1G292 1 COLLECTING CONVEYOR 1G3061 1 WARM WATER PUMP
  1G3071 1 WATERLESS PUMP
      1G3221 1 CONDENS STEAM PUMP
MISELLA DISTILLATION CONDENZATION
CODE QUANTITY EXPLANATION CODE QUANTITY EXPLANATION
1D406 1 FLASH DEPOT (E405 AND MONTAGE) 1E451 1 VACUUM CONDENSOR
1D408 1 DISTILLATION COLON 1E456 1 TOASTER STEAM CONDENSOR
1D410 1 HIGH VACUUM OIL STAGE 1E471 1 EXTRACTION FOR CHURN AIR COOLER
1E403 1 DECLINE FILM EVAPORATOR ECONOMIZER 1G4521 1 SOLVENT CONDENS PUMP
1E405 1 RISING FILM EVAPORATOR 1G461 1 STEAM EJECTOR
1E407 1 OIL HEATER      
1G4011 1 WHOLE MISELLA PUMP      
1G4041 1 INTERLUDE MISELLA PUMP      
1G4091 1 OIL PUMP      
1G4111 1 VACUUM OIL PUMP      
1G412 1 STEAM EJECTOR      
TOASTER-DRYER-COOLER ABSORBTION SYSTEM
CODE QUANTITY EXPLANATION CODE QUANTITY EXPLANATION
1G6511 1 REVOLVING VALVE 1D 7011 1 ABSORPTION COLON
1D652 1 DESOLVENTIZER-TOASTER-DRYER-COOLER 1D 7053 1 VACUUM STRIPPING COLON
1D6541 1 STEAM CONSERVATIVE CYCLON 1E703 1 TEMPERATURE EXCHANGER
1D663 1 CHURN AIR CYCLON 1G 7021 1 MINERAL OIL PUMP
1D672 1 DUST CYCLON 1G 7061 1 MINERAL OIL PUMP
1E6621 1 AIR HEATER 1F722 1 MINERAL OIL TANK
1G6611 1 DRYER AIR FAN      
1G6641 1 REVOLVING VALVE      
1G6711 1 COOLER AIR FAN      
1G6731 1 REVOLVING VALVE      
UNDERGROUND HEXAN STOCK TANKS PIPES, VALVES,ETC FOR ESTABLISHMENT
CODE QUANTITY EXPLANATION CODE QUANTITY EXPLANATION
1G30011 1 SOLVENT PUMP 1H 9511 1 Set AIR FUNNEL
1F3002.1/2 2 UNDERGROUND HEGZANE STOCK TANKS 1H 9521 1 Set VALVES AND SMALL ACCESSORY
      1H 9522 1 Set SEEING GLASS SET
      1K 9531 1 Set LOCAL INSTRUMENTS
      1K 9532 1 Set CONTROL INSTRUMENTS
      1K 9541 1 Set HEXAN DİDECTOR AND WARNING SYSTEM

ELECTRICIAL QUIPMENTS OF CRUDE VEGETABLE OIL EXTRACTION UNIT

CODE QUANTITY EXPLANATION
1N6611 1 Set ELECTRICAL PARTS
1H962 1 MIMIC DIAGRAM CONTROL PANEL
1N963 1 MAIN POWER DISTRIBUTOR PANEL
1 N 964 1 Set ELECTRICAL MOTORS FOR EXTRACTION ESTABLISHMENT
1 N 965 - OBSERVATION LAMBS OF EXTRACTION ESTABLISHMENT MACHINES

 

 

 

 

PROCESS OF CRUDE VEGETABLE OIL EXTRACTION UNIT

1.1 Principal of the Process

This process is related with extraction of liquid element in a matter, namely connected with hard-liquid extraction. The oil is found in the oil cell of the seed is decomposing with using the hexan. This decomposing operation is realizing in the most important part of the establisment, namely in extraction. Following this operation, oil is tranfering from oil-solvent mixture with the distillation of solvent under the vacuum. This process economy based on oil cake in the extraction which is not dropping by any loss and based on compensate in the mixture. Furthermore, benefiting from all the energy. Other economic factors are gaining oil in a considerable degrees, remaining low oil in the oil cakes connected with the design of the equipments and opposite movement extraction principle.

 

1.2 Subsidiary Equipments

 

Gaining solvent from the condensor and esanjor is passing on and collecting in the solvent seperator which is decomposing operation materializing becouse of its' different densities. Pure solvent gravity and solvent_ flowing from the water seperator in to the solvent working tank. Still, water including solvent tracks and it is heating with near 95 celcius in the last churn Desolventizor for remove the solvent tracks. The water is leaving from the solvent removing with the method of boil over and then churn water flow in to the settle hole. Solvent is getting from the working tank and the losses in the extraction process fill again and using. The warm water take away from the last water Desolventisor in to the Sururma silicone with pumps. This water is using as washing liquid in the steam sweeping unit, then it is regain and go in to the Desolventisor. Hexan pieces which is vaporized in the last churn water desolventisor are regain in the kondensation unit which are liquefy.

 

1.3 Distillation and Condensation of the Mixtures

For seperating the oil from the oil, missella mixtures ispassing distillation and it is distilling below the vacuum. Fistly, materials continuosly are passing ofrom hydrosiclon, automatic and self-cleaning filter unit.

1.4 Removing The Solvent Unit in the oil cake ( Desolventizer –Toaster )

 

The food which is seperated from extractor and received its’ oil, includes approximately %32 solvent. Toster feeds with Redler and Desolventisor for removing the Hexan. Desolventisor-Toaster ( D.T.) removing solvent originates from toaster units. Every stages, equip with mixer wings for continuation of oil cakes movement during the solvent removing operation. Solvent removing/Solvent in the oil cake is removing with fresh steam in toaster stages. During the solvent removing operation, food approximately reaches 100/150 celcius . The hexan in the last food which comes from D.T, becomes among %0,005-0,008 dependent on kindof seed which is working its’ contents. Toaster Steams- distilled hexan and steam the last churn water. Seperating from the D.T with the help of sweeping siclon which is cleaned with warm water which comes from desolventisor. The cleaned D.T steams transports to the mixture distillation main evaporator.

1.5 Drying oil cakes and Cooling water

During the removing the solvent in the oil cakes process , the moisture ratio in the oil cake is increasing. According to the international standarts, for obtaning the food which its’ moisture ratio is approximately %10-12 needed drying the food. After the Toaster fry-pans , one drier stages and one coolerstages supply decreasing the moisture ratio approximately %10-12. Fan which is in the Drying stage, stands on air in to the fry-pan in the drier parts and holes on the base of the fry-pan with the help of Air heater with steam heats. This warm air is drying the food which comes from the stages of warm heat toaster. The churn air which is in the drier, is seperating from the dusts before it is given to atmosphere in the siclon. Oil cakes cools in the cooling stages and moisture decreases like kind of drier part . Ambiyant air is passing through the cooling stages with absorbent ventilator. The dusts which are seperating the siclons are emptying in to the revolving valve and oil cake conveyors.  

1.6 Absorbtion Unit- Regaining the solvent
A certain amount of air which remain in the pores of the feeding raw materials are always giving to the extractors. Air is saturated with solvent. Regaining this solvent and for obeying the content of the solvent which is related with churn air rules, this air solvent is removing with transported steam of the partial condansation and absorbtion. The churn air pass through the absorbtion handle after the front cooling approximately 30 celcius and partial condansation of the steams in the front cooler.
Solvent tracks in the churn air are washing with mineral oil in the reverse current flowing. The solvent which absorb with oil dezabsorb with vacuum brushing colon steam brush and front heat in the rising film Evaparotor. The oil is cooling with heat changer with plaque and then pass through the absorbtion column for absorbtion again. Solvent steam which comes from D 705 brushing colons, is concentrating in the E 451 Vacumm condensor.

 

 

CAPACITY OF CRUDE VEGETABLE OIL EXTRACTION UNIT

150 Metric Tonnes / Day

SYSTEM OF CRUDE VEGETABLE OIL EXTRACTION UNIT

 

Continious


STEAM BOILER UNIT

CAPACITY: 6 Metric Tonnes / Hour

SYSTEM : Liquid Fuel



 

 

PROCESS OF REFINERY UNIT OF COOKING OIL FACTORY

NEUTROLISATION DIAGRAMME

WINTERIZING UNIT

When some kind of oil is cooled up to room temperature, it is in turbid color. This the some for sunflower oil and corn oil. Even in lower temperatures, to remain clear, oil should be vinterezed.

( Winterization of Vegerable Oil )

High fusion provides paraffin’s(waxes) to remove, sometimes high fusion also gets stearins remove ,Vinterization is completed in three steps. First step: Oil is in viterizing tank. Second step: Filter helping material is added and oil is cooled slowly. Oil should be waited in a lower temperature in a few hours to obtain a suitable cold testing before oil filtration. Last step: Oil is hold sometime in oil maturer and before filtering to mature After then oil is send to filters to filtrate.

WINTERISATION DIAGRAMME

DEODORIZING UNIT

One of the most important part of the oil refination is the deodorization (removal of the odor) which gives the appropriate value to the oil. The most important fact which the consumer interests mainly about liquid oil is the odor and taste. The oil gains all these specialties in deodorizing agents. That’s why deodorizing agents are very important in oil sector. Every kind of oil has got an odor , that belongs to itself. And
this odor is got rid of, by deodorizing agents

1. Vacuum = To reduce the heat of evaporating ,the atmosphere pressure should be reduced to the lowest level for the materials which give odor , to evaporate .After long studies about this subject, the reducemant is done down to 2 mm Hg in absolute pressure.(2 torr)

2. Temperature = There are two main roles of temperature. On one hand, the pressure in evaporation , of undesired odor material is getting higher related to the reason of high temperature in surrounding , on the other hand it helps oil acids to be distilled easily, providing hydrocarbons with shorter chain structures by exploring oil acid chains to aldehits and ketons. That’s why the temperature is very important factor.

3. Distillation Steam = It is very important to pay attention to the clear steam to be dry and degassed while deodorization process is going on. On one hand, while deodorization process, the steam atomized directly to the oil holds the mission of mixing ,on the other hand it lowers the evaporation pressure as if it is a destilation speciality to provide easy evaporation. It helps oxidised oil acids to be broken into aldehids and katons in high temperatures.

4. Thickness of Oil Layer = By capturing it under vacuum, it gets rid of atmospheric pressure. By this way, a pressure appears at the lowest part of the oil because of its own weight, as if it is remaining a thick level. This increase availability of evaporating pressure of molecules at the bottom level so this natures oils to be remaining in higher levels while removing of odor (deodorazition) process . This is an undesired specialty.

5. Timing : Because it is a destilation process; if prepation of 4 factors, montioned above, is in optimum timing shapes most opropriate position by itself naturally. If those 4 factors can not be manager succesfully deodorization process should be left for timing process. But, as the time passes, the prime cost gets higher.

DEODORISATION DIAGRAMME

 EQUIPMENTS OF REFINERY UNIT OF COOKING OIL FACTORY

NEUTRALIZATION AND BLEACHING UNIT

CODE QUANTITY EXPLANATION
N10T 2 NEUTRALIZATION + BLEACHING TANK
N20S 1 SOAP-STOCK TANK
N30KS 1 ADJUSTED COSTIK + SALTY-WATER TANK
N40P 1 COSTIK PUMP
N20P 1 SOAP-STOCK PUMP
N40T 1 LIQUIED COSTIK STOCK TANK
N50T 1 WASHING WATER AND OIL HOLDER TANK
N60F 1 BLEACHING FILTER
N60P 1 BLEACHING PUMP
N60T 1 BLEACHING OIL TANK
NA10P 1 OIL PUMP
N80V 1 VACUUM PUMP
N70B 1 BAROMETRIC CONDENSOR
N70P 1 WATER CIRCULATION PUMP
  - PNOMATIC LEVEL CONTROLLERS
  - OIL STEAM VALVES – FLOWMETER
  - FLANGES AND BOLTS
DEODORIZING WINTERIZING
CODE QUANTITY EXPLANATION CODE QUANTITY EXPLANATION
D10AT 1 DEODORIZINGTANK V10V 1 WINTERIZING TANK
D10P 1 DEODORİZING OIL PUMP V10M 1 MATURE TANK
D30V 1 VACUUM PUMP V10B 1 BUFFER TANK
D40B 1 BAROMETRIC CONDENSOR V20SG 1 COOLING GROUP
D40P 1 WATER CIRCULATION PUMP V30ST 1 COLD WATER CICULATION TANK
D50S 1 COOLING TANK V30SP 1 COLD WATER CICULATION PUMP
D50P 1 OIL PUMP V40P 1 FILTER FEEDING PUMP
D60PF 1 POLISHING FILTER V50T 1 WINTERIZED OIL TANK
D70P 1 WATER PUMP V50P 1 OIL PUMP
  - PNOMATIC LEVEL CONTROLLERS V60F 1 WINTERIZING FILTER
  - OIL STEAM VALVES – FLOWMETER   - PNOMATIC LEVEL CONTROLLERS
  - FLANGES AND BOLTS   - OIL STEAM VALVES – FLOWMETER
        - FLANGES AND BOLTS

 

 CAPACITY OF REFINERY UNIT OF COOKING OIL FACTORY

50 Metric Tonnes / Day

SYSTEM OF REFINERY UNIT OF COOKING OIL FACTORY

Batch

PRICE OF REFINERY UNIT OF COOKING OIL FACTORY

N/A

+

<< PRICE OF FILLING MACHINERY >>

N/A


LABRATORY UNIT

PRICE : €uro 145,000 ( One Hundred and Fourtyfive Thousand Euros )

RENK, IRK VE DİN KONULARIYLA ASLA İLGİLENMİYORUZ !

 

 

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