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Cooking Oil Factory
COTTON PRESSING UNIT DIAGRAMME
| 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
CRUDE VEGETABLE OIL EXTRACTION UNIT EQUIPMENTS
| 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 |
| 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 |
| 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 |
| 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
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.
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.
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 |
| 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
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<< PRICE OF FILLING MACHINERY >>
N/A
LABRATORY UNIT
PRICE : €uro 145,000 ( One Hundred and Fourtyfive Thousand Euros )
