Complete Process Flow of 100TPD Solvent Extraction Workshop
Date:Jan 2nd, 2026
Our solvent extraction system is designed to separate pretreated oilseeds into crude oil and high-protein meal with high efficiency. By applying a multi-stage counterflow extraction process using industrial-grade hexane, the system maximizes oil recovery. After extraction, the meal undergoes solvent removal treatment, while the oil–solvent mixture (miscella) is transferred to the distillation unit for solvent separation and purification.
Today we will introduce the negative-pressure evaporation extraction process flow of a 100 TPD solvent extraction workshop, which includes five main sections: solvent extraction, wet meal desolventizing, miscella distillation, solvent vapor recovery, and exhaust gas absorption.
1. Solvent Extraction Section
Raw materials are conveyed into the drag-chain extractor by a scraper conveyor and come into countercurrent contact with fresh solvent (n-hexane), which is the most commonly used liquid solvent in oil extraction. After contact, miscella is formed. The miscella is pumped and sprayed onto incoming materials to reduce solvent consumption and operating costs. After multiple washing stages, the concentrated miscella is discharged from the second oil compartment and transferred by the miscella pump to the hydrocyclone and filter for solid removal. The separated solids are returned to the first oil compartment for further extraction, while the filtered miscella is sent to the miscella tank.
2, Miscella Distillation Section
The miscella is pumped by the first-stage feed pump into the pre-evaporator, where the temperature is maintained at 60–70°C, and then flows into the first flash tank. Next, the miscella is delivered by the second-stage feed pump to a heat exchanger for preheating, and then enters the second evaporator, operating at about 90°C, followed by the second flash tank.
After that, the miscella is sent by the stripping feed pump to the stripping tower, where the temperature reaches approximately 110°C, enabling more efficient evaporation of the n-hexane solvent. The stripped oil is then discharged by the stripping outlet pump to the oil-to-oil heat exchanger. After heat exchange, the crude oil is transferred to the crude oil tank and finally pumped to the refining workshop for further processing.
Since this is a negative-pressure evaporation extraction system, the miscella evaporation section operates under vacuum conditions, which are maintained by a steam jet ejector system.
3. Wet Meal Desolventizing Section
The main purpose of this section is to remove residual solvent from the wet meal and reduce its moisture content and temperature to acceptable levels. After the extraction process, both miscella and wet meal are obtained. The wet meal is conveyed by a scraper conveyor into the DTDC desolventizer-toaster-dryer-cooler system. It passes through the desolventizing stage (60–70°C), toasting stage (around 90°C), drying stage (about 110°C), and cooling stage to produce finished dry meal. The final meal is then transported by a scraper conveyor to the meal storage silo.
4. Solvent Recovery Section
During the wet meal desolventizing and miscella evaporation processes, solvent vapors are generated and collected. These solvent vapors are then directed to the desolventizing condenser and stripping condenser. In the condensers, the vapor is cooled and converted into liquid solvent and water, which are discharged into the combined water separator tank.
Since water has a higher density than solvent, the solvent layer floats on top. When the water level reaches the set point, the recovered solvent flows into the solvent tank and is pumped by the fresh solvent pump through the solvent heater back to the extractor for reuse, reducing solvent consumption and operating costs.
Because solvent vapors from different sections have different pressure levels, some vapors may not be fully captured by the main condensers. These uncondensed vapors are first balanced in a pressure equalization tank and then sent to the nearest condenser for further condensation and recovery.
5. Exhaust Gas Absorption Section
Some solvent vapors cannot be condensed by the condensers and are referred to as exhaust gas. These gases are recovered based on the principle of solubility in paraffin oil. First, the free gas enters the paraffin oil absorption tower. A small portion of the exhaust gas that cannot be absorbed is discharged through the exhaust fan.
The absorbed solvent gas is pumped by the rich oil pump to the paraffin oil heat exchanger for heat recovery, then sent to the heater and fed into the paraffin oil stripping tower. Under high-temperature conditions, the solvent is separated from the paraffin oil. The recovered solvent vapor passes through the economizer and flows into the combined water separator tank, while the regenerated paraffin oil is returned to the paraffin oil tank for reuse.
Key Benefits of our solvent extraction system
High Performance
Optimized extraction technology delivers higher oil recovery rates and consistent output quality.
Economic Efficiency
Reduced operating and maintenance expenses help lower total production costs and improve profitability.
Energy Saving
Lower energy consumption in downstream processing minimizes overall power demand and improves energy utilization.
Smart Control
Integrated automation and centralized monitoring enable stable operation and easier process management.
With proven solvent extraction technology, stable system performance, and efficient energy-saving design, our solutions help customers achieve higher oil yield and lower operating costs. If you are planning to build or upgrade your extraction plant, feel free to contact us. Our engineering team is ready to provide customized solutions and professional technical support.
For more information, please contact us:
Call: +86-159 3716 3029
Email:company@dingmachinery.com
Visit: http://www.dsoilpress.com
Today we will introduce the negative-pressure evaporation extraction process flow of a 100 TPD solvent extraction workshop, which includes five main sections: solvent extraction, wet meal desolventizing, miscella distillation, solvent vapor recovery, and exhaust gas absorption.
1. Solvent Extraction Section
Raw materials are conveyed into the drag-chain extractor by a scraper conveyor and come into countercurrent contact with fresh solvent (n-hexane), which is the most commonly used liquid solvent in oil extraction. After contact, miscella is formed. The miscella is pumped and sprayed onto incoming materials to reduce solvent consumption and operating costs. After multiple washing stages, the concentrated miscella is discharged from the second oil compartment and transferred by the miscella pump to the hydrocyclone and filter for solid removal. The separated solids are returned to the first oil compartment for further extraction, while the filtered miscella is sent to the miscella tank.
2, Miscella Distillation Section
The miscella is pumped by the first-stage feed pump into the pre-evaporator, where the temperature is maintained at 60–70°C, and then flows into the first flash tank. Next, the miscella is delivered by the second-stage feed pump to a heat exchanger for preheating, and then enters the second evaporator, operating at about 90°C, followed by the second flash tank.
After that, the miscella is sent by the stripping feed pump to the stripping tower, where the temperature reaches approximately 110°C, enabling more efficient evaporation of the n-hexane solvent. The stripped oil is then discharged by the stripping outlet pump to the oil-to-oil heat exchanger. After heat exchange, the crude oil is transferred to the crude oil tank and finally pumped to the refining workshop for further processing.
Since this is a negative-pressure evaporation extraction system, the miscella evaporation section operates under vacuum conditions, which are maintained by a steam jet ejector system.
3. Wet Meal Desolventizing Section
The main purpose of this section is to remove residual solvent from the wet meal and reduce its moisture content and temperature to acceptable levels. After the extraction process, both miscella and wet meal are obtained. The wet meal is conveyed by a scraper conveyor into the DTDC desolventizer-toaster-dryer-cooler system. It passes through the desolventizing stage (60–70°C), toasting stage (around 90°C), drying stage (about 110°C), and cooling stage to produce finished dry meal. The final meal is then transported by a scraper conveyor to the meal storage silo.
4. Solvent Recovery Section
During the wet meal desolventizing and miscella evaporation processes, solvent vapors are generated and collected. These solvent vapors are then directed to the desolventizing condenser and stripping condenser. In the condensers, the vapor is cooled and converted into liquid solvent and water, which are discharged into the combined water separator tank.
Since water has a higher density than solvent, the solvent layer floats on top. When the water level reaches the set point, the recovered solvent flows into the solvent tank and is pumped by the fresh solvent pump through the solvent heater back to the extractor for reuse, reducing solvent consumption and operating costs.
Because solvent vapors from different sections have different pressure levels, some vapors may not be fully captured by the main condensers. These uncondensed vapors are first balanced in a pressure equalization tank and then sent to the nearest condenser for further condensation and recovery.
5. Exhaust Gas Absorption Section
Some solvent vapors cannot be condensed by the condensers and are referred to as exhaust gas. These gases are recovered based on the principle of solubility in paraffin oil. First, the free gas enters the paraffin oil absorption tower. A small portion of the exhaust gas that cannot be absorbed is discharged through the exhaust fan.
The absorbed solvent gas is pumped by the rich oil pump to the paraffin oil heat exchanger for heat recovery, then sent to the heater and fed into the paraffin oil stripping tower. Under high-temperature conditions, the solvent is separated from the paraffin oil. The recovered solvent vapor passes through the economizer and flows into the combined water separator tank, while the regenerated paraffin oil is returned to the paraffin oil tank for reuse.
Key Benefits of our solvent extraction system
High Performance
Optimized extraction technology delivers higher oil recovery rates and consistent output quality.
Economic Efficiency
Reduced operating and maintenance expenses help lower total production costs and improve profitability.
Energy Saving
Lower energy consumption in downstream processing minimizes overall power demand and improves energy utilization.
Smart Control
Integrated automation and centralized monitoring enable stable operation and easier process management.
With proven solvent extraction technology, stable system performance, and efficient energy-saving design, our solutions help customers achieve higher oil yield and lower operating costs. If you are planning to build or upgrade your extraction plant, feel free to contact us. Our engineering team is ready to provide customized solutions and professional technical support.
For more information, please contact us:
Call: +86-159 3716 3029
Email:company@dingmachinery.com
Visit: http://www.dsoilpress.com
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