Technology for cutting rapeseed oil at low temperature of 120 DEG C

Abstract

The invention discloses a process for cutting rapeseed oil at a low temperature of 120 DEG C, which is used for making scallion and ginger rapeseed oil, and relates to the technical field of compound seasoning manufacturing. A special device with a digital pressure pulse hot processing system is used in a matched manner, ginger and scallion are used for providing moisture, pressure pulses are generated in a flash evaporation manner, and flash evaporation is repeated for 5-7 times at the temperature of 120 DEG C, so that the raw rapeseed oil is obtained. After moisture which contains strong raw rapeseed oil flavor and ginger and scallion flavor and accounts for 80% or above of the total weight of ginger and scallion is discharged, the temperature in the kettle is reduced to 100 DEG C again, the materials are discharged out of the device, oil residues are separated or not separated, and the ginger and scallion rapeseed oil which is very strong in ginger and scallion flavor and cooked rapeseed oil flavor is obtained. According to the invention, only the energy of stir-frying ginger and scallion is utilized, two events of cutting rapeseed oil and stir-frying ginger and scallion are realized at the same time, the efficiency is improved, and the energy is saved. Meanwhile, the food safety, the production safety and the environmental protection safety are substantially improved. The whole process is easy to operate, safe, stable, free of open fire and capable of achieving digital production.

Description

Technical Field

[0001] This invention relates to the field of rapeseed oil production technology, and more specifically to a process technology for low-temperature 120°C quenching rapeseed oil. Background Technology

[0002] Rapeseed oil is beloved by Chinese people for its unique flavor, especially the third or second grade rapeseed oil obtained through traditional pressing or virgin pressing, which has a more distinct and intense flavor. Because raw and cooked rapeseed oil have significantly different flavors, it needs to be heated to remove the raw flavor during cooking, prepared dishes, or compound seasonings. Generally, the temperature needs to exceed the smoke point of rapeseed oil (220°C) to remove the raw flavor and bring out the characteristic oily aroma of cooked rapeseed oil. This has become common knowledge, widely used not only in home cooking but also in the production of compound seasonings and prepared dishes. However, this process presents two problems: first, removing the raw flavor requires a significant amount of energy, which is wasted if the oil is allowed to cool down instead of being heated through processes like stir-frying ginger and scallions; second, such high temperatures pose safety and environmental risks, such as the generation of fumes, the conversion of trans fatty acids, and the risk of fire.

[0003] In fact, directly using rapeseed oil heated above 220°C to sauté ginger, scallions, or other ingredients is excessively hot. The high temperature can cause the oil to violently evaporate moisture from the food, releasing a large amount of volatile oil particles, potentially leading to a "flame-ignition" explosion. This is unsafe and should not be imitated by non-professionals (chefs) in home cooking, and such explosions are strictly prohibited in food production. In production, the temperature for sautéing ginger and scallions in rapeseed oil is generally controlled between 120-150°C, requiring significant heat to evaporate and remove most of the moisture. Freshly sautéed rapeseed oil heated above 220°C needs to be cooled to around 150°C before use, especially if used continuously. Summary of the Invention

[0004] The purpose of this invention is to provide a process for producing rapeseed oil at a low temperature of 120°C in order to solve the above-mentioned technical problems.

[0005] To achieve the above objectives, the present invention specifically adopts the following technical solution: This invention provides a process for producing raw rapeseed oil at a low temperature of 120°C, employing a digital pressure pulse heat processing system for seasoning preparation capable of flash evaporation, comprising the following steps: S1. Raw materials and pretreatment: Pretreatment of rapeseed oil and ginger and scallions; S2. Quantitative feeding: After the rapeseed oil and pre-treated ginger and scallions are measured, they are put into the mixing tank and then into the reaction vessel. Normal pressure feeding or vacuum feeding mode can be used. First, put the ginger and scallions into the mixing tank, and use vacuum feeding to let the material enter the reaction vessel. Then, put in the rapeseed oil to wash the residue on the wall of the mixing tank. Use normal pressure feeding to wash the feed pipe into the reaction vessel. S3. Heating and holding: The material is heated to the preset temperature in the reactor. According to the characteristics of ginger and scallions, the maximum temperature is controlled at 120℃. After the temperature reaches the preset temperature, it is held for 5-10 minutes to allow the pressure inside the reactor to rise to a stable level. S4. Flash Drainage: When the pressure stabilizes, open the cooling water valve of the condenser. The reactor may or may not stop heating. Open the distillation valve on the distillation tube to begin positive pressure closed flash evaporation. The pressure in the reactor will rapidly decrease and match the pressure in the flash tank. Simultaneously, the temperature sensor at the top of the distillation tube will show the distilled steam temperature rising from low to high and then falling back down, indicating the end of positive pressure closed flash evaporation. The vent valve can then be opened to begin open flash evaporation. At this point, the system is connected to the atmosphere, and the pressure gradually decreases to one atmosphere (or even slightly negative pressure), while the temperature drops to 100°C (or even 99°C). Then, open the manifold valve, weigh the pressure tank, and record the weight of the drained water. This completes one full flash evaporation cycle. At this point, the temperature can be increased again to begin the second flash evaporation; repeat this process 5-7 times until the cumulative weight of the removed moisture reaches the expected value, thus ending the flash evaporation process. S5. Cooling and Discharging: After discharging 80%-85% of the total weight of ginger and scallions containing the flavors of raw rapeseed oil and ginger and scallions, the temperature inside the reactor is lowered to 100°C again. The reactor is then connected to circulating cooling water for forced cooling to 80°C. The compound seasoning is discharged through a digital pressure pulse thermal processing system. The oil residue may or may not be separated, resulting in ginger and scallion rapeseed oil that has been completely calcined, has no raw rapeseed oil flavor, and has the aroma of ginger and scallions as well as cooked rapeseed oil.

[0006] In one embodiment, in step S1, the rapeseed oil is grade II or III rapeseed oil, or it can be the "homemade" rapeseed oil commonly known in farmers' markets.

[0007] In one embodiment, in step S1, ginger and scallions refer to fresh old ginger, onions, and scallions. The old ginger is washed, peeled, and processed into granules of about 2-5 mm. The scallions are washed, and rotten skin and leaves are removed and processed into scallion sections of 5-10 mm. The onions are washed, and the heads, roots, and dry skin are removed and processed into granules of about 5-10 mm. 75 g of ginger granules, 75 g of scallion sections, and 75 g of onions are added to every 1 kg of rapeseed oil.

[0008] In one embodiment, in step S2, ginger and scallions can be added to the reactor in either a cold pot, cold oil, and cold material method or a premixed and preheated method. The cold pot, cold oil, and cold material method involves adding the material to the reactor at room temperature. The premixed and preheated method involves adding all or part of the ginger and scallions to the mixing vessel, turning on the first stirring device and the heating function of the mixing vessel, so that the ginger and scallions are premixed and heated. The preheating temperature does not exceed 80°C to prevent disorderly evaporation of moisture.

[0009] In one embodiment, in step S3, controlling the temperature range at 120°C means that after ginger, scallions, and rapeseed oil are added to the reactor, the temperature is rapidly increased from room temperature to the specified temperature of 120°C, and after a holding time of 5-10 minutes, the temperature inside the ginger and scallions is made consistent with the apparent oil temperature. At this time, the pressure inside the reactor will gradually increase and tend to stabilize.

[0010] In one embodiment, in step S4, flash evaporation refers to first sealing the flash evaporator, and after the pressure and temperature inside the reactor drop to a relatively stable state, then opening the flash evaporator. When the temperature inside the reactor drops again to 100°C and the pressure inside the reactor reaches one atmosphere, one flash evaporation is completed. When flash evaporation is started, the heating device is turned off, and when flash evaporation is opened, the weighing pressure tank immediately displays the weight of the water discharged in this flash evaporation.

[0011] Closed flash evaporation refers to the release of pressure inside the reactor into a closed space. Open flash evaporation, on the other hand, involves the pressure inside the reactor being connected to the atmosphere.

[0012] In one implementation, in step S4, repeated flash evaporation refers to the process where, after completing one closed flash evaporation and one open flash evaporation, the temperature drops from 120°C to 100°C and the pressure drops to 1 atmosphere. Then, the steam valve for heating the reactor is opened again to raise the temperature inside the reactor back to 120°C. Once the pressure rises and stabilizes, the heating system is shut off, and the second flash evaporation begins. This process is repeated 5-7 times, starting with closed flash evaporation and then opening flash evaporation. The flash evaporation process ends when the cumulative weight of the discharged moisture reaches the expected value. When the system contains a large amount of water with a high degree of freedom, the pressure increase during heating and holding is significant, resulting in a large flash pressure differential (high flash intensity). This makes it easier for oil to be carried out during flash evaporation. In this case, a complete flash evaporation process can be completed by performing two consecutive closed flash evaporations followed by an open flash evaporation, allowing the system pressure to be released and water drained. Specifically, after the first closed flash evaporation, the distillation valve on the distillation tube is closed, while the manifold valve on the manifold and the vent valve on the weighing pressure tank are opened. At this point, distilled water from the flash tank enters the weighing pressure tank, and the pressure inside the flash tank is released. Once the distilled water weighing display stabilizes, the manifold valve on the manifold is closed, and the distillation valve on the distillation tube is opened to begin the second closed flash evaporation. When there is little water in the system, or when the water has little freedom, the water may be trapped deep inside the tissue or confined by intermolecular forces due to emulsification, making it difficult to drain the water. The temperature inside the vessel rises but the pressure is low. In this case, a closed negative pressure flash evaporation can be used. After using negative pressure flash evaporation, open flash evaporation has no practical significance for drainage. It is equivalent to connecting to the atmosphere and eliminating the vacuum. Therefore, one negative pressure flash evaporation is considered as one complete flash evaporation.

[0013] In one embodiment, the digital thermal processing system for seasoning production capable of flash evaporation includes a batching vessel, a reaction vessel, a buffer tank, a condenser, a flash tank, a weighing pressure tank, a vacuum balancing tank, and a central control system. The discharge port of the batching vessel is connected to the inlet of the reactor through a feed pipe; the distillation port of the reactor is connected to the side wall inlet of the buffer tank through a distillation pipe; the lower discharge port of the buffer tank is connected to the distillation pipe through a spray return pipe; the upper exhaust port of the buffer tank is connected to the inlet of the condenser through a pipe; and the outlet of the condenser is connected to the flash tank through a condenser pipe. The flash tank has two reflux outlets on its side wall, one at the top and one at the bottom. These outlets are connected to the reactor via reflux pipes; the upper outlet is for oil return, and the lower outlet is for water return. A material inlet is located at the bottom of the flash tank, connected to the weighing pressure tank via a manifold and a flexible connector. A level display connector is also connected to the material inlet at the bottom of the flash tank. The top of the flash tank has two upper outlets: one connected to the vacuum balance tank via a vacuum pipe, and the other connected to tap water via a level regulating pipe. The weighing pressure tank is connected to the vacuum balance tank via a flexible connector and a weighing pressure vacuum pipe. The vacuum balance tank is connected to a vacuum pump. The seven components—a batching vessel, a reaction vessel, a buffer tank, a condenser, a flash tank, a weighing pressure tank, and a vacuum balance tank—along with all the pipelines and the automatic valves on all the pipelines, and the corresponding sensors on the seven components, are combined in different ways to form a feeding system, a stirring system, a spray return system, a water-oil fractionation and recovery system, a discharge system, a heating system, a circulating cooling system, a distillation system, and a vacuum system. The central control system connects and controls the feeding system, stirring system, spray return system, water-oil fractionation and recovery system, discharge system, heating system, circulating cooling system, distillation system, vacuum system, automatic valves on pipelines, and corresponding sensors and automatic valves on each component; thereby realizing the heating and cooling of the reactor, high temperature positive pressure, high temperature negative pressure, and flash evaporation process with adjustable intensity and frequency.

[0014] Specifically, the scheme disclosed in this paper differs from the traditional hot processing process of woks or pressure cookers. This scheme is characterized by pressure pulses (flash evaporation) inside the reaction vessel, which significantly improves the extraction and reaction efficiency of the compound seasoning hot processing process.

[0015] Specifically, the batching vessel includes a batching vessel body, a feeding cover installed on top of the batching vessel body, a first stirring device installed inside the batching vessel body, a manual tap water valve installed on top of the feeding cover, a temperature sensor installed on top of the feeding cover, and a bottom valve installed at the discharge port at the bottom of the batching vessel body. The bottom valve is connected to the reaction vessel through a discharge pipe.

[0016] The batching vessel is open with no internal pressure and an external pressure of 0.5 MPa. It has a conical bottom and functions such as heating and stirring. Its volume is comparable to that of the reaction vessel. The bottom of the vessel is connected to the reaction vessel by a bottom valve to supply materials. It should be ensured that the connecting pipe has a large slope and a large diameter so that the materials can flow into the main vessel by gravity in principle. Insulation measures should be taken to reduce ineffective back distillation in the reaction vessel.

[0017] The reactor is designed to withstand internal pressure of ±0.09-0.45 MPa and external pressure of 0.5 MPa. It features the largest possible diameter for the evaporation port, inlet, and outlet. Reactor volumes can be designed in sizes of 10L, 20L, 50L, 200L, 500L, 1000L, 2000L, 3000L, 4000L, 5000L, and 6000L, depending on requirements. The reactor jacket is connected to the steam heating system and the circulating cooling water system. An insulation layer surrounds the jacket, and an insulation shell surrounds the insulation layer. The inner wall of the reactor is typically mirror-polished to minimize material residue.

[0018] This reactor needs to be equipped with temperature, pressure and liquid level sensors. In addition to stirring, heating, constant temperature and forced cooling functions, it must also have functions such as safety valve, venting, compressed air inlet, evaporation and reflux, feeding, discharging and cleaning spray.

[0019] The buffer tank, similar to a cyclone separator, mitigates the impact of flash evaporation. Its inlet pipe's central axis should not be perpendicular to the tank's central axis, but rather installed tangentially to create airflow rotation within the tank. The inlet and top outlet diameters are the same, while the bottom discharge pipe diameter can be relatively smaller. The buffer tank requires insulation and its volume is 1 / 2 to 1 / 4 that of the flash tank.

[0020] The condenser possesses the characteristics of a shell-and-tube condenser, with a heat exchange area 5-15 times that of the reactor's heating area. Its pressure resistance is consistent with the reactor. The condenser's inlet diameter is equal to the evaporator tube diameter, and its outlet diameter is 1 / 2 to 1 / 6 of the inlet diameter. The condenser inlet is connected to the main reactor via an exhaust pipe, buffer tank, and distillation pipe. A pneumatic valve controls the discharge of steam from the main reactor. The condenser outlet is connected to the flash tank inlet. The condenser side is also connected to circulating cooling water, with the lower inlet being the cooling water inlet and the upper outlet.

[0021] The cross-section of the distillation tube determines the evaporation area. Its diameter is taken as the maximum opening size of the space remaining on the reactor head after deducting the space occupied by the stirring device. It needs to be insulated before being connected to the condenser, and a temperature sensor is installed at its highest point.

[0022] The flash tank has the same pressure resistance as the reactor, and its volume is 5-30% of the reactor's volume. The flash tank is equipped with a pressure sensor and connected to a vacuum system and a weighing pressure tank. It also has pipelines for separating distillate oil and water and returning it to the reactor, as well as a level display connecting pipe for observing the liquid level in the flash tank and the liquid level of the oil-water separation returning to the reactor. By pre-injecting or not injecting a certain amount of water, the cavity volume or liquid level of the flash tank can be adjusted within a certain range.

[0023] The weighing pressure tank has the same pressure resistance as the reaction vessel, and its volume is 10-30% of the reaction vessel's volume. Its weighing module accuracy is not less than 0.3%, and the pipeline connected to it must use pressure-resistant flexible connections to ensure that the weighing error is within the required range.

[0024] In one embodiment, the feeding system includes an atmospheric pressure feeding system and a vacuum feeding system; an atmospheric pressure feeding system is used for liquid materials; and a vacuum feeding system is used for semi-solid and solid materials to prevent clogging of the feed pipe. The atmospheric pressure feeding system includes a batching vessel, a reaction vessel, a discharge pipe connecting the batching vessel and the reaction vessel, a discharge valve on the discharge pipe, and a vent valve on the reaction vessel. The specific operation of atmospheric pressure feeding involves first opening the vent valve of the reaction vessel, then opening the discharge valve on the discharge pipe. The material flows from the batching vessel into the reaction vessel by gravity, completing the atmospheric pressure feeding process. The vacuum feeding system includes a vacuum pump and Figure 1 All components and pipes except the weighing pressure tank are included. The specific operation of vacuum feeding is to turn on the vacuum pump to create a certain vacuum state inside the reactor, then close the distillation pneumatic valve on the distillation tube of the reactor to maintain the vacuum inside the reactor, open the bottom valve of the feed tube on the feed pipe, and the material in the batching vessel is sucked into the reactor. The above vacuum feeding operation can be repeated multiple times to complete the vacuum feeding.

[0025] In one embodiment, the water-oil fractionation recovery system includes a buffer tank, a condenser, a flash tank, a level display connecting pipe, and related connecting pipes and valves; the water-oil fractionation recovery system also includes a level regulating pipe, a flow meter installed on the level regulating pipe, and a pneumatic valve for the water supply pipe to achieve quantitative water addition into the flash tank; During operation, the flash tank is observed through the liquid level display connecting pipe. If the fraction in the flash tank contains oil, it is returned to the reactor through the upper oil return pipe of the reflux pipe. The liquid level of the fraction in the flash tank can be pre-adjusted by injecting a metered amount of water through the liquid level regulating pipe. The circulating cooling water on the condenser is turned off, and the distillation valve on the distillation pipe is opened to maintain the same pressure as the reactor for oil return. Alternatively, the lower water return pipe of the reflux pipe can be used to return all the fraction to the reactor for flash evaporation or distillation again.

[0026] The beneficial effects of this invention are as follows: This invention can be used as a compound seasoning or a semi-finished product in pre-cooked dishes where rapeseed oil is used in the formulation, or as a widely applicable ginger and scallion oil product processed from rapeseed oil. This invention utilizes only one unit of energy for stir-frying ginger and scallions, achieving the dual tasks of cooking the rapeseed oil and stir-frying the ginger and scallions, thus saving energy. Simultaneously, it significantly improves food safety, production safety, and environmental safety. The entire process is simple, safe, stable, flameless, and digitally produced. Attached Figure Description

[0027] To more clearly illustrate the technical solutions of the embodiments of the present invention, the accompanying drawings used in the embodiments will be briefly introduced below. It should be understood that the following drawings only show some embodiments of the present invention and should not be regarded as a limitation of the scope. For those skilled in the art, other related drawings can be obtained from these drawings without creative effort.

[0028] Figure 1 This is a schematic diagram of the structure of a digital thermal processing system for the production of compound seasonings according to the present invention; Figure 2 This is a schematic diagram of the mixing tank; Figure 3 This is a schematic diagram of the buffer tank. Figure 4 This is a schematic diagram of the flash tank. Figure 5 This is a temperature curve of the reactor (actual measurement diagram of Example 1). Figure 6 This is a weight curve of the cooling water tank (actual measurement diagram of Example 1). Figure 7 This is the pressure curve of reactor 2 (actual measurement diagram of Example 1); Attached reference numerals: 1. Batching vessel; 2. Reactor; 3. Buffer tank; 4. Condenser; 5. Flash tank; 6. Weighing pressure tank; 7. Vacuum balance tank; 8. Liquid level display connecting pipe; 1.1 First stirring device; 1.2 Manual water valve; 1.3 Feeding cover; 1.4 Temperature sensor; 1.5 Bottom valve of the discharge vessel; 2.1 Second stirring device; 2.2 Safety sensors (temperature sensor, pressure sensor, safety valve); 2.3 Distillation valve; 2.4 First medium inlet and outlet (steam inlet, cooling water outlet); 2.5 Pneumatic valve for reflux tube; 2.6 Vent valve; 2.7 Second medium inlet and outlet (steam inlet, cooling water outlet); 2.8 Bottom valve; 5.1 Water supply pipe pneumatic valve; 5.2 Flow meter; 5.3 Air venting pneumatic valve; 5.4 Pressure sensor; 5.5 Oil return pipe pneumatic valve; 5.6 Recirculation observation glass tube; 5.7 Recirculation pipe pneumatic valve; 5.8 Vacuum tube pneumatic valve; 5.9 Distillation pipe pneumatic valve. Detailed Implementation

[0029] To make the technical problems, technical solutions, and technical effects of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. The components of the embodiments of the present invention described and shown in the accompanying drawings can generally be arranged and designed in various different configurations.

[0030] Therefore, the following detailed description of the embodiments of the invention provided in the accompanying drawings is not intended to limit the scope of the claimed invention, but merely to illustrate selected embodiments of the invention. All other embodiments obtained by those skilled in the art based on the embodiments of the invention without inventive effort are within the scope of protection of the invention.

[0031] It should be noted that similar reference numerals and letters in the following figures indicate similar items; therefore, once an item is defined in one figure, it does not need to be further defined and explained in subsequent figures. Furthermore, the terms "first," "second," etc., are used only to distinguish descriptions and should not be construed as indicating or implying relative importance.

[0032] In the description of the embodiments of the present invention, it should be noted that the terms "inner", "outer", "upper", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, or the orientation or positional relationship in which the product of the invention is usually placed when in use. They are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limiting the present invention.

[0033] Example 1 This embodiment provides a process for producing raw rapeseed oil at a low temperature of 120°C, using a digital thermal processing system capable of flash evaporation for seasoning production. The configuration parameters of this system are as follows: 1) Reactor 2 has a volume of 10L (excluding the upper head), a diameter of 300mm, a length-to-diameter ratio of 1:1, a DN50 feed pipe, a DN50 distillation pipe, a DN50 outlet, a DN15 steam pipe, and a DN15 cooling water pipe. The agitator uses a frame-type design with a scraper. The motor power is 120W, and it uses a cycloidal pinwheel reducer. The maximum internal pressure is 0.4MPa, and the maximum external pressure is 0.5MPa. It has temperature and pressure sensors and can be vented and connected to compressed air. The distillation pipe from the lid to the highest point needs to be insulated.

[0034] 2) The batching vessel 1 has a volume of 10L, a conical bottom, a propeller-type agitator, a 90W cycloidal pinwheel reducer, and is heat-only without cooling. It is connected to tap water and can detect temperature. It can raise and maintain the temperature, and the stirring speed is adjustable.

[0035] 3) Condenser 4 is a shell-and-tube type with a heat exchange area of ​​3.2㎡, a pressure resistance of 0.5MPa, an inlet diameter of DN50, and an outlet pipe diameter of DN20.

[0036] 4) The flash tank 5 has a volume of 4.43L, a pressure resistance of 0.5MPa, and all openings are DN20, equipped with a pressure sensor.

[0037] 5) The weighing pressure tank 6 has a volume of 4.43L and a pressure resistance of 0.5MPa. The weighing module C3 is connected to both the flash tank and the vacuum balance tank via flexible connections.

[0038] 6) The volume of buffer tank 3 is 2.8L, with a conical bottom and a pressure resistance of 0.5MPa. The maximum diameter is the same as that of the flash tank. The air inlet is tangentially inserted, and the air outlet is vertically installed at the top. The bottom return pipe has the same diameter as the air inlet and air outlet pipes, all of which are DN50.

[0039] 7) Reactor 2 and batching vessel 1 must be connected to the steam pipe. The steam pipe should be top-in, bottom-out. The steam inlet pipe must be equipped with a proportional regulating valve, a pneumatic angle seat valve, a pressure sensor, a safety valve, and a shut-off valve. The steam outlet pipe must be equipped with a pneumatic angle seat valve and a steam trap. Spare bypasses should be provided for both the steam inlet and outlet valve assemblies for purposes such as maintenance of important automatic valves and rapid drainage of accumulated water. The circulating cooling water supply pipe to the vessel body should be installed in reverse (bottom-in, top-out) and equipped with an automatic valve for easy switching during forced cooling.

[0040] The process includes the following steps: S1. Raw material pretreatment: rapeseed oil and ginger / scallion pretreatment; the rapeseed oil is grade 2 or 3 pressed rapeseed oil. Grade 1 rapeseed oil has no raw rapeseed oil smell and does not need to be cooked. Ginger and scallions refer to fresh old ginger, onions, and scallions. After washing and peeling, the old ginger is processed into granules of about 2-5mm. After washing and removing rotten skin and leaves, the scallions are processed into scallion sections of 5-10mm. After washing, removing the head and roots, and removing the dry skin, the onions are processed into granules of about 5-10mm. Every 1kg of rapeseed oil is mixed with 75g of ginger granules, 75g of scallion sections, and 75g of onions.

[0041] S2. Quantitative feeding: After pretreatment and metering, rapeseed oil and ginger and scallions are added to the mixing tank 1 and then to the reaction tank 2. Normal pressure feeding or vacuum feeding mode can be used. First, put ginger and scallions into the mixing tank 1 and use vacuum feeding to let the material enter the reaction tank 2. Then, put rapeseed oil in to rinse the residue on the wall of the mixing tank 1 and use normal pressure feeding to rinse the feed pipe into the reaction tank 2. Ginger and scallions can be added to reactor 2 using either a cold pot, cold oil, and cold material method or a premixed and preheated method. The cold pot, cold oil, and cold material method involves adding the material to reactor 2 at room temperature. The premixed and preheated method involves adding all or part of the ginger and scallions to the mixing vessel 1, turning on the first stirring device 1.1 and the heating function of the mixing vessel 1, so that the ginger and scallions are premixed and heated. The preheating temperature does not exceed 80°C to prevent disorderly evaporation of moisture.

[0042] S3. Heating, pressurizing, and heat preservation: The material is heated to the preset temperature in reactor 2. According to the characteristics of ginger and scallions, the temperature range is controlled at 120°C. The temperature range of 120°C means that after ginger, scallions, and rapeseed oil are added to reactor 2, the temperature is rapidly increased from room temperature to the specified temperature of 120°C. After a heat preservation time of 5-10 minutes, the temperature inside the ginger and scallions is consistent with the apparent oil temperature. At this time, the pressure inside reactor 2 will gradually increase and tend to stabilize.

[0043] S4. Flash Drainage: When the pressure stabilizes, open the cooling water valve of condenser 4. The reactor 2 may or may not stop heating. Open the 2.3 distillation valve on the distillation tube to start positive pressure closed flash evaporation. The pressure of reactor 2 drops rapidly and becomes close to the pressure of the flash tank. The positive pressure closed flash evaporation ends, and open flash evaporation begins. At this time, the system is connected to the atmosphere, and the pressure gradually drops to one atmosphere. Then open the distillation valve and weigh the pressure tank 6 to record the weight of the drained water. Repeat flash evaporation 5-7 times. S5. Cooling and Discharging: After discharging water containing 80%-85% of the total weight of ginger and scallions, which contains the flavor of raw rapeseed oil and raw ginger and scallions, the temperature inside reactor 2 is reduced to 100°C again. The material is discharged to meet the requirements of the seasoning processing system. The oil residue is separated or not separated, and the ginger and scallion rapeseed oil that has been completely quenched and has no raw rapeseed oil flavor, and has the flavor of ginger and scallions and cooked rapeseed oil is obtained.

[0044] Specifically, this solution can be used as a compound seasoning or a semi-finished product for self-use in pre-cooked dishes where rapeseed oil is used in the recipe, or as a widely applicable ginger and scallion oil product processed from rapeseed oil. This invention utilizes only one unit of energy for stir-frying ginger and scallions, achieving the dual tasks of cooking the rapeseed oil and stir-frying the ginger and scallions, thus saving energy. Simultaneously, it substantially improves food safety, production safety, and environmental safety. The entire process is simple, safe, stable, flameless, and digitally produced.

[0045] Flash evaporation refers to first sealing the reactor 2 for flash evaporation, and then opening the reactor 2 for flash evaporation after the pressure and temperature inside the reactor 2 have dropped to a relatively stable state. When the temperature inside the reactor 2 drops to 100°C again and the pressure inside the reactor 2 reaches one atmosphere, one flash evaporation is completed. When flash evaporation is started, the heating device is turned off. When flash evaporation is opened, the weighing pressure tank 6 immediately displays the weight of the water discharged in this flash evaporation.

[0046] Repeated flash evaporation refers to the process where, after completing one closed flash evaporation and one open flash evaporation, the temperature drops from 120°C to 100°C and the pressure drops to 1 atmosphere. Then, the steam valve supplying heat to reactor 2 is opened again, raising the temperature inside reactor 2 back to 120°C. Once the pressure rises and stabilizes, the heating system is shut off, and the second flash evaporation begins. This process is repeated 5-7 times, starting with closed flash evaporation and then opening flash evaporation.

[0047] Repeated flashing 5-7 times means that when the cumulative water discharged during each flash evaporation reaches a predetermined value, or when the current maximum temperature of 120°C becomes insufficient to lower the temperature further with closed flash evaporation, and subsequent open flash evaporation can hardly discharge any more water, the flash evaporation process of increasing temperature and accumulating pressure can be stopped. In reality, as a large amount of water is discharged from the system, it becomes increasingly difficult to accumulate pressure during heating, and the peak pressure inside reactor 2 decreases, indicating that drainage has become very difficult. Continued heating may cause the ginger and scallions to darken in color, or even overheat and "caramelize."

[0048] The temperature inside reactor 2 drops to 100°C again, and the material is discharged. This device means that after the final flash evaporation, the material can be discharged when the temperature inside reactor 2 drops to 100°C, thus ending the thermal processing. Since almost no moisture is discharged during the final flash evaporation, it is difficult to quickly cool down to 100°C through flash evaporation. At this time, the circulating cooling water can be switched to force cooling.

[0049] Oil residue separation or non-separation refers to the ability of this product to separate the oil residue using a vibrating circular screen or horizontal centrifuge, depending on the needs of the subsequent application scenario, to obtain ginger and scallion oil and ginger and scallion oil residue products. Alternatively, it can be used without separation to directly obtain ginger and scallion oil products containing residue.

[0050] Figures 5 to 7 A record of the process of making ginger and scallion oil from rapeseed oil by briefly cooking it. Figure 5This is the temperature curve of reactor 2. Figure 6 This is a weight curve of the cooling water tank. Figure 7 This is the pressure curve of reactor 2, and its detailed interpretation is as follows: Figures 5 to 7 The temperature, drainage weight, and time are all absolute values ​​measured by sensors or calculators, but the pressure is a relative value. For example, the initial pressure inside reactor 2 should be one atmosphere, but the graph shows 0.01 MPa, while the peak pressure of the first flash evaporation is shown as 0.12 MPa, but the saturated vapor pressure of water at 120°C should be 0.198 MPa. Therefore, the pressure-time curve can only be interpreted as relative values; the absolute values ​​are meaningless.

[0051] Example 2 This invention provides a digital thermal processing system for the production of compound seasonings, including a batching tank 1, a reaction tank 2, a buffer tank 3, a condenser 4, a flash tank 5, a weighing pressure tank 6, a vacuum balance tank 7, and a central control system. The discharge port of the batching vessel 1 is connected to the inlet of the reaction vessel 2 via a feed pipe; the distillation port of the reaction vessel 2 is connected to the side wall inlet of the buffer tank 3 via a distillation pipe; the lower discharge port of the buffer tank 3 is connected to the distillation pipe via a spray return pipe; the upper exhaust port of the buffer tank 3 is connected to the inlet of the condenser 4 via a pipe; and the outlet of the condenser 4 is connected to the flash tank 5 via a condensation pipe. The flash tank 5 has two reflux outlets on its side wall, one at the top and one at the bottom. These two reflux outlets are connected to the reaction vessel 2 via reflux pipes. The upper reflux pipe is for oil return, and the lower reflux pipe is for water return. The bottom of the flash tank 5 has a material inlet, which is connected to the weighing pressure tank 6 via a manifold and a flexible connection. The material inlet at the bottom of the flash tank 5 is connected to a liquid level display pipe 8. The top of the flash tank 5 has two upper outlets. One upper outlet is connected to a vacuum balance tank 7 via a vacuum pipe, and the other upper outlet is connected to tap water via a liquid level regulating pipe. The weighing pressure tank 6 is connected to the vacuum balance tank 7 via a flexible connection and a weighing pressure vacuum pipe. The vacuum balance tank 7 is connected to a vacuum pump. The seven components—the batching vessel 1, the reaction vessel 2, the buffer tank 3, the condenser 4, the flash tank 5, the weighing pressure tank 6, and the vacuum balance tank 7—along with all the pipes and the automatic valves on all the pipes, and the corresponding sensors on the seven components, are combined in different ways to form a feeding system, a stirring system, a spray return system, a water-oil fractionation and recovery system, a discharge system, a heating system, a circulating cooling system, a distillation system, and a vacuum system. The central control system connects to and controls the feeding system, the stirring system, the spray return system, the water-oil fractionation and recovery system, the discharge system, the heating system, the circulating cooling system, the distillation system, the vacuum system, the automatic valves on the pipelines, and the corresponding sensors and automatic valves on each component; thereby realizing the heating and cooling, high temperature positive pressure, high temperature negative pressure, and the flash evaporation process with adjustable intensity and frequency of the reactor.

[0052] Specifically, the scheme disclosed in this paper differs from the traditional hot processing process of woks or pressure cookers. This scheme is characterized by pressure pulses (flash evaporation) inside the reaction vessel, which significantly improves the extraction and reaction efficiency of the compound seasoning hot processing process.

[0053] Specifically, the batching vessel 1 includes a batching vessel body, a feeding cover 1.3 disposed on the top of the batching vessel body, a first stirring device 1.1 disposed in the batching vessel body, a manual water valve 1.2 disposed on the top of the feeding cover 1.3, a temperature sensor 1.4 disposed on the top of the feeding cover 1.3, and a bottom discharge valve 1.5 disposed at the discharge port at the bottom of the batching vessel body. The bottom discharge valve 1.5 is connected to the reaction vessel 2 through a discharge pipe. Figure 2 As shown.

[0054] The batching vessel 1 is open with no internal pressure and an external pressure of 0.5 MPa. It has a conical bottom and functions such as heating and stirring. Its volume is comparable to that of the reaction vessel. The bottom of the vessel is connected to the reaction vessel 2 via a bottom valve to supply materials to it. It should be ensured that the connecting pipe has a large slope and a large diameter so that the materials can flow into the main vessel by gravity in principle. Insulation measures should be taken to reduce ineffective back distillation in the reaction vessel 2.

[0055] Reactor 2 has an internal pressure resistance of -0.09 to -0.45 MPa and an external pressure of 0.5 MPa. It features the largest possible diameter for its evaporation port, inlet, and outlet. Reactor 2 can be designed with volumes of 10L, 20L, 50L, 200L, 500L, 1000L, 2000L, 3000L, 4000L, 5000L, and 6000L, depending on requirements. The jacket of reactor 2 is connected to the steam heating system and the circulating cooling water system. An insulation layer exists outside the jacket, and an insulation shell surrounds the insulation layer. The inner wall of the reactor is, in principle, mirror-polished to reduce material residue. (The reactor 2 or related pipelines are equipped with the following: 2.1 a second stirring device; 2.2 a safety sensor (temperature sensor, pressure sensor, safety valve); 2.3 a distillation valve; 2.4 a first medium inlet / outlet (steam inlet, cooling water outlet); 2.5 a reflux pipe pneumatic valve; 2.6 a vent valve; 2.7 a second medium inlet / outlet (steam inlet, cooling water outlet); and 2.8 a bottom valve; if...) Figure 3 (As shown).

[0056] This reactor needs to be equipped with temperature, pressure and liquid level sensors. In addition to stirring, heating, constant temperature and forced cooling functions, it must also have functions such as safety valve, venting, compressed air inlet, evaporation and reflux, feeding, discharging and cleaning spray.

[0057] Buffer tank 3 features a cyclone separator-like structure to mitigate the impact of flash evaporation. Its inlet pipe's central axis should not be perpendicular to the tank's central axis, but rather installed tangentially to create airflow rotation within the tank. The inlet and top outlet diameters are the same, while the bottom discharge pipe diameter can be relatively smaller. The buffer tank requires insulation and its volume is 1 / 2 to 1 / 4 that of the flash tank.

[0058] Condenser 4 features a shell-and-tube condenser with a heat exchange area 5-15 times that of the reactor's heating area. Its pressure resistance is identical to that of the reactor. The condenser's inlet diameter is equal to the evaporator tube diameter, and its outlet diameter is 1 / 2 to 1 / 6 of the inlet diameter. The inlet of condenser 4 is connected to the main reactor 2 via an exhaust pipe, buffer tank 3, and distillation pipe. A pneumatic valve 2.3 controls the discharge of steam from the main reactor. The outlet of condenser 4 is connected to the inlet of flash tank 5. Condenser 4 is also connected to circulating cooling water, with the lower inlet being the cooling water inlet and the upper outlet.

[0059] The cross-section of the distillation tube 2.3 determines the evaporation area. Its diameter is taken as the maximum opening size of the space remaining on the reactor head after deducting the space occupied by the stirring device. It needs to be insulated before being connected to the condenser 4, and a temperature sensor is installed at its highest point.

[0060] The flash tank 5 has the same pressure resistance as the reactor 2, and its volume is 5-30% of the reactor volume. The flash tank 5 is equipped with a pressure sensor and is connected to a vacuum system and a weighing pressure tank. It also has pipelines for separating distillate oil and water and returning it to the reactor, as well as a display and connecting pipe 8 for observing the liquid level in the flash tank 5 and the liquid level of the oil-water separation returning to the reactor 2. By pre-injecting or not injecting a fixed amount of water, the cavity volume or liquid level of the flash tank 5 can be adjusted within a certain range. (The flash tank 5 or related pipelines are equipped with a water supply pipe pneumatic valve 5.1, a flow meter 5.2, an air venting pneumatic valve 5.3, a pressure sensor 5.4, an oil return pipe pneumatic valve 5.5, a reflux observation glass tube 5.6, a return distillation pipe pneumatic valve 5.7, a vacuum pipe pneumatic valve 5.8, and a manifold pneumatic valve 5.9, etc.) Figure 4 (As shown).

[0061] The weighing pressure tank 6 has the same pressure resistance as the reaction vessel 2, and its volume is 10-30% of the reaction vessel volume. Its weighing module accuracy is not less than three per thousand, and the pipeline connected to it must use pressure-resistant flexible connection to ensure that the weighing error is within the required range.

[0062] In one embodiment, the feeding system includes an atmospheric pressure feeding system and a vacuum feeding system; an atmospheric pressure feeding system is used for liquid materials; and a vacuum feeding system is used for semi-solid and solid materials to prevent clogging of the feed pipe. The atmospheric pressure feeding system includes a batching vessel 1, a reaction vessel 2, a discharge pipe connecting the batching vessel 1 and the reaction vessel 2, a discharge bottom valve 1.5 installed on the discharge pipe, and a vent valve 2.6 on the reaction vessel 2. The specific operation of atmospheric pressure feeding is as follows: first, open the vent valve 2.6 of the reaction vessel 2, and then open the discharge bottom valve 1.5 on the discharge pipe. The material flows from the batching vessel 1 into the reaction vessel 2 by gravity, completing the atmospheric pressure feeding. The vacuum feeding system includes a vacuum pump and Figure 1 The reactor 2 contains all components and pipes except for the weighing pressure water tank 6. The specific operation of vacuum feeding is as follows: turn on the vacuum pump to create a certain vacuum state inside the reactor 2, then close the distillation pneumatic valve 2.3 on the distillation tube of the reactor 2 to maintain the vacuum inside the reactor 2, and open the bottom valve 1.5 on the discharge pipe. The material in the batching vessel 1 is sucked into the reactor 2. The above vacuum feeding operation can be repeated multiple times to complete the vacuum feeding. In one embodiment, the stirring system includes a first stirring device 1.1 disposed in the batching vessel 1 and a second stirring device 2.1 disposed in the reaction vessel 2. The first stirring device 1.1 is a double-layer inclined blade impeller stirrer, and the second stirring device 2.1 further includes a mechanical seal device, a speed reduction device and a frequency converter. The stirring form of the second stirring device 2.1 is one of frame type, paddle type, ribbon type or scraper type. The stirring speed is controlled by adjusting the frequency of the first stirring device 1.1 and the second stirring device 2.1 through the central control system.

[0063] In one embodiment, the water-oil fractionation and recovery system includes the buffer tank 3, the condenser 4, the flash tank 5, the liquid level display connecting pipe 8, and related connecting pipes and valves; the water-oil fractionation and recovery system also includes a liquid level regulating pipe, a flow meter 5.2 installed on the liquid level regulating pipe, and a water supply pipe pneumatic valve 5.1 to realize the quantitative addition of water to the flash tank 5; During operation, the flash tank 5 is observed through the liquid level display connecting pipe 8. If the fraction in the flash tank 5 contains oil, it is returned to the reactor 2 through the upper oil return pipe of the reflux pipe. The liquid level of the fraction in the flash tank 5 can be pre-adjusted by injecting a metered amount of water through the liquid level regulating pipe. The circulating cooling water on the condenser 4 is turned off, and the distillation valve 2.3 on the distillation pipe is opened to maintain the same pressure as the reactor 2 for oil return. Alternatively, the lower water return pipe of the reflux pipe can be used to return all the fraction to the reactor 2 for flash evaporation or distillation again.

[0064] In one embodiment, the discharge system includes an atmospheric pressure discharge system and a positive pressure discharge system; During normal discharge, the atmospheric pressure discharge system requires that there is no pressure inside the reactor 2. First, open the vent valve 2.6 on the reactor lid, and then open the bottom valve 2.8 to discharge the material. Positive pressure discharge requires the injection of compressed air to maintain the pressure inside the reactor 2 at no more than 0.25 MPa, and the bottom valve 2.8 to be opened to achieve pressurized discharge from the reactor 2.

[0065] In one embodiment, the heating system includes a boiler or steam generator, a temperature sensor on the batching vessel 1, a temperature sensor on the reaction vessel 2, a steam supply pipe and a steam condensate pipe located on the batching vessel 1 and the reaction vessel 2, and a valve assembly and a sensor on the steam supply pipe and the steam condensate pipe. The valve group and the sensor provide the control basis for the central control system and record the temperature changes in the batching tank 1 and the reaction tank 2, so as to realize the heating and heat preservation of the batching tank 1 and the reaction tank 2. The valve assembly includes a steam proportional valve (adjustable steam flow), a pneumatic angle seat valve, a safety valve, and a steam trap (to drain steam condensate from the pipeline). The sensors are a pressure sensor and a temperature sensor.

[0066] In one embodiment, the circulating cooling system includes a forced cooling system for the batching vessel 1 and the reaction vessel 2, and a distillation cooling system within the condenser 4; The circulating cooling system absorbs heat from the batching vessel 1, the reaction vessel 2, and the condenser 4 through pipelines. The heated cooling water is then cooled by a cooling tower and pressurized by a pump before being returned to the jacket of the batching vessel 1, the reaction vessel 2, and the condenser 4 for recycling.

[0067] In one embodiment, the distillation system includes the reaction vessel 2, the buffer tank 3, the condenser 4, the flash tank 5, the weighing pressure tank 6, the vacuum balance tank 7, the vacuum pump, and pipelines connecting the above components. By opening the distillation pneumatic valve 2.3 on the distillation tube, the pressure inside the reaction vessel 2 is instantly released into the closed space of the buffer tank 3, the condenser 4, the flash tank 5 and the weighing pressure tank 6, which is positive pressure closed flash evaporation.

[0068] When the pressure sensor on the reactor 2 shows that it is close to being in equilibrium with the pressure sensor on the flash tank 5, the vent valve 5.3 on the flash tank 5, which is connected to the atmosphere, can be opened, which means that flash evaporation is started; at this time, theoretically the pressure will drop to one atmosphere and the temperature will drop to 100°C.

[0069] Open the valve connecting the vacuum balance tank to create a vacuum in the aforementioned enclosed space. Then, open the distillation pneumatic valve 2.3 on the distillation tube to instantly release the pressure inside the reactor 2 into the enclosed space formed by the buffer tank 3, the condenser 4, the flash tank 5, and the weighing pressure tank 6. This is called negative pressure flash evaporation. As long as the negative pressure in the aforementioned enclosed space is even lower, and the pressure inside the reactor 2 is only one atmosphere or a slight negative pressure, negative pressure (enclosed) flash evaporation can also be performed.

[0070] Specifically, the vent valve 5.3 can be opened beforehand, bypassing the positive pressure closed flash evaporation process, and the distillation valve 2.3 can be opened directly for open flash evaporation. For systems with high temperatures and abundant free water within the reactor 2, direct flash evaporation can easily carry out oil or solid materials. Whether the closed flash evaporation is connected to or not connected to the weighing pressure tank 6 allows adjustment of the closed space size, thereby adjusting the intensity of the closed flash evaporation to suit different types of products.

[0071] In one embodiment, the vacuum system includes a vacuum pump, the vacuum balance tank 7, the weighing pressure tank 6, the flash tank 5, the condenser 4, the buffer tank 3, and the reaction vessel 2; The vacuum balance tank 7 is connected to the weighing pressure tank 6 through the weighing pressure tank vacuum pipe and the flash tank 5 is connected to the flash tank vacuum pipe; thus realizing the functions of vacuum feeding, negative pressure (closed) flash evaporation, (continuous) negative pressure distillation and (closed) high temperature negative pressure of the reactor 2.

[0072] Specifically, the negative pressure (closed) flash evaporation refers to creating a certain degree of vacuum within the flash tank 5, condenser 4, buffer tank 3, and interconnected pipes by drawing a vacuum (detectable by a pressure sensor on the flash tank 5). Then, the condenser's circulating cooling water is turned on, the steam heating system of the closed reaction vessel 2 is turned off, and the distillation valve 2.3 is opened to instantly release the internal pressure of the reaction vessel 2 into the aforementioned negative pressure closed space. Once the decrease in internal pressure of the reaction vessel 2 balances with the increase in pressure in the flash tank 5, the negative pressure (closed) flash evaporation is complete.

[0073] The (continuous) negative pressure distillation refers to the process where, after the pressure inside the reactor 2 returns to normal, the distillation valve 2.3 is opened, a vacuum is opened, and a relatively stable negative pressure is maintained for a certain period of time to heat and distill the system. The (closed) high-temperature negative pressure refers to the process where there is almost no free water and little tissue water in the system of the reactor 2. A high vacuum degree can be formed inside the reactor 2 by drawing a vacuum, and then the distillation valve 2.3 is closed. This forms a heating process of the material system in the reactor 2 under a high vacuum degree in a closed space. The pressure increase and change process (i.e., the process of deep tissue water in the material gradually migrating to the surface and then to the oil phase) can be directly observed or recorded by a pressure sensor.

[0074] In one embodiment, the central control system controls all pneumatic valves, enabling the pneumatic actuators of the valves to be linked to the compressed air solenoid valves for starting and closing, and providing feedback on the closed or open status of the pneumatic valves. The central control system also connects to and controls all sensors. The central control system combines multiple consecutive linked operations with unique functions into a one-button operation. The central control system also automatically records and outputs various process curves, and also enables the copying and recording of manual processes for products with fixed numbers, thereby providing one-button start and automatic execution of the entire product process.

[0075] Specifically, the central control system also connects to and controls all sensors, including pressure sensors, temperature sensors, weighing sensors, liquid flow meters, steam regulating proportional valves, and steam flow meters, and can display, record, and output data from each sensor.

[0076] The central control system can also combine multiple sequentially linked operations with unique functions into a single-button operation. Examples include atmospheric pressure feeding, vacuum feeding, positive pressure closed flash evaporation, open flash evaporation, forced cooling, atmospheric pressure discharge, and pressurized discharge. The stirring speed and heating / holding or forced cooling settings for the batching vessel 1 and the reaction vessel 2 can be preset.

[0077] The central control system can simultaneously and automatically record and output multiple process curves. It can also manually copy and record the process for products with fixed numbers (fixed formulas and fixed processes), thereby providing one-click start and automatic execution of the entire product process.

Claims

1. A process for producing raw rapeseed oil at a low temperature of 120°C, using a digital pressure pulse heat processing system for seasoning preparation capable of flash evaporation, characterized in that, Includes the following steps: S1. Raw materials and pretreatment: Pretreatment of rapeseed oil and ginger and scallions; S2, quantitative feeding: After the rapeseed oil and pre-treated ginger and scallions are measured, they are put into the mixing tank (1) and then into the reaction tank (2). Normal pressure feeding or vacuum feeding mode can be used. First, put the ginger and scallions into the mixing tank (1) and use vacuum feeding to let the material enter the reaction tank (2). Then, put in the rapeseed oil to rinse the residue on the wall of the mixing tank (1) and use normal pressure feeding to rinse the feed pipe into the reaction tank (2). S3. Heating and holding: The material is heated to the preset temperature in the reactor (2). According to the characteristics of ginger and scallion, the maximum temperature is controlled at 120℃. The temperature is raised to the preset temperature and held for 5-10 minutes to make the pressure inside the reactor rise to a stable level. S4, Flash Drainage: When the pressure tends to stabilize, open the cooling water valve of the condenser (4), and the reactor (2) stops or continues heating. Open the distillation valve (2.3) on the distillation tube, and the positive pressure closed flash evaporation begins. The pressure of the reactor (2) drops rapidly and becomes consistent with the pressure of the flash tank. At the same time, when the temperature sensor at the top of the distillation tube shows that the temperature of the distilled steam rises from low to high and then drops from high to low, it indicates that the positive pressure closed flash evaporation is over. The drain valve can be opened to start the open flash evaporation. At this time, the system is connected to the atmosphere, the pressure gradually drops to one atmosphere, and the temperature drops to 100°C. Then open the distillation valve, weigh the pressure tank (6) and record the drainage weight. At this time, a complete flash evaporation is completed. At this point, the temperature can be increased again to begin the second flash evaporation; repeat this process 5-7 times until the cumulative weight of the removed moisture reaches the expected value, thus ending the flash evaporation process. S5. Cooling and Discharging: After multiple flash evaporations to remove 80%-85% of the total weight of ginger and scallions containing the flavors of raw rapeseed oil and raw ginger and scallions, the temperature inside the reactor (2) is reduced to 100°C again. After the reactor is connected to the circulating cooling water and forced to cool down to 80°C, the compound seasoning is discharged. The oil residue is separated or not separated, and ginger and scallion rapeseed oil that has been completely thawed and has no raw rapeseed oil flavor, and has the aroma of cooked ginger and scallions and cooked rapeseed oil is obtained.

2. The process for producing raw rapeseed oil at a low temperature of 120°C according to claim 1, characterized in that, In step S1, the rapeseed oil is grade two or three rapeseed oil, or it can be the "homemade" rapeseed oil commonly known in farmers' markets.

3. The process for producing raw rapeseed oil at a low temperature of 120°C according to claim 1, characterized in that, In step S1, ginger and scallions refer to fresh old ginger, onions, and scallions. After washing and peeling, the old ginger is processed into granules of about 2-5mm. After washing and removing rotten skin and leaves, the scallions are processed into scallion sections of 5-10mm. After washing, removing the head and roots, and removing the dry skin, the onions are processed into granules of about 5-10mm. For every 1kg of rapeseed oil, 75g of ginger granules, 75g of scallion sections, and 75g of onions are added.

4. The process for producing raw rapeseed oil at a low temperature of 120°C according to claim 1, characterized in that, In step S2, ginger and scallions can be added to the reactor (2) in either the cold pot, cold oil and cold material method or the premix and preheating method. The cold pot, cold oil and cold material method means that the material is added to the reactor (2) at room temperature. The premix and preheating method means that all or part of the ginger and scallions are put into the mixing vessel (1), and the heating function of the first stirring device (1.1) and the mixing vessel (1) is turned on so that the ginger and scallions are premixed and heated. The preheating temperature does not exceed 80°C to prevent disorderly evaporation of moisture.

5. The process for producing low-temperature 120°C rapeseed oil according to claim 1, characterized in that, In step S3, the temperature range is controlled at 120°C, which means that after ginger, scallions and rapeseed oil are added to the reaction vessel (2), the temperature is rapidly increased from room temperature to the specified temperature of 120°C, and after a holding time of 5-10 minutes, the temperature of the center of the ginger and scallions is consistent with the apparent oil temperature. At this time, the pressure inside the reaction vessel (2) will gradually increase and tend to stabilize.

6. The process for producing raw rapeseed oil at a low temperature of 120°C according to claim 1, characterized in that, In step S4, flash evaporation refers to first performing closed flash evaporation, and after the pressure and temperature inside the reactor (2) drop to a relatively stable state, then performing open flash evaporation. When the temperature inside the reactor (2) drops again to 100°C and the pressure inside the reactor (2) reaches one atmosphere, one flash evaporation is completed. When flash evaporation is started, the heating device is turned off. When flash evaporation is opened, the weighing pressure tank (6) immediately displays the weight of the water discharged during this flash evaporation. Closed flash evaporation refers to the pressure inside the reactor (2) being released into a closed space, while open flash evaporation is when the pressure inside the reactor (2) is connected to the atmosphere.

7. A process for producing rapeseed oil at a low temperature of 120°C according to claim 1, characterized in that, In step S4, repeated flash evaporation refers to the process where, after completing one closed flash evaporation and one open flash evaporation, the temperature drops from 120°C to 100°C and the pressure drops to one atmosphere. Then, the steam valve for heating the reactor (2) is opened again to raise the temperature inside the reactor (2) back to 120°C. When the pressure rises and becomes relatively stable, the heating system is turned off and the second flash evaporation is started. The process is still to first close the flash evaporation and then open the flash evaporation. This process is repeated 5-7 times. The flash evaporation process ends when the cumulative weight of the discharged water reaches the expected value. When there is a lot of water in the system and the water has a large degree of freedom, the pressure in the system increases significantly during the heating and heat preservation process, and the flash evaporation pressure difference is large. It is easier to carry out oil during flash evaporation. At this time, a complete flash evaporation process can be completed by continuously closing the flash evaporation twice and then opening the flash evaporation, so that the pressure in the system can be released and the water can be drained. That is, after the first closed flash evaporation is completed, the distillation valve (2.3) on the distillation tube is closed, the distillation valve (5.9) on the distillation tube and the vent valve on the weighing pressure tank (6) are opened. At this time, the distilled water in the flash tank enters the weighing pressure tank (6), and the pressure in the flash tank (5) is released. When the distilled water weighing display is stable, the distillation valve (5.9) on the distillation tube can be closed and the distillation valve (2.3) on the distillation tube can be opened to start the second closed flash evaporation.

8. A process for producing rapeseed oil at a low temperature of 120°C according to claim 1, characterized in that, The digital pressure pulse heat treatment system for seasoning production capable of flash evaporation includes a batching vessel (1), a reaction vessel (2), a buffer tank (3), a condenser (4), a flash tank (5), a weighing pressure tank (6), a vacuum balance tank (7), and a central control system. The discharge port of the batching vessel (1) is connected to the inlet of the reaction vessel (2) through a feed pipe; the distillation port of the reaction vessel (2) is connected to the side wall feed port of the buffer tank (3) through a distillation pipe; the lower discharge port of the buffer tank (3) is connected to the distillation pipe through a spray return pipe; the upper exhaust port of the buffer tank (3) is connected to the inlet of the condenser (4) through a pipe; the outlet of the condenser (4) is connected to the flash tank (5) through a condenser pipe. The flash tank (5) has two reflux outlets on its side wall, one above the other. The two reflux outlets are connected to the reactor (2) through reflux pipes, with the upper reflux pipe being the oil return pipe and the lower reflux pipe being the water return pipe. The flash tank (5) has a material inlet at its bottom, which is connected to the weighing pressure tank (6) through a manifold pipe and a flexible connection. The material inlet at the bottom of the flash tank (5) is connected to a liquid level display connecting pipe (8). The flash tank (5) has two upper outlets at its top, one of which is connected to the vacuum balance tank (7) through a vacuum pipe, and the other is connected to tap water through a liquid level regulating pipe. The weighing pressure tank (6) is connected to the vacuum balance tank (7) through a flexible connection and a weighing pressure vacuum pipe. The vacuum balance tank (7) is connected to a vacuum pump. The seven components—the batching vessel (1), the reaction vessel (2), the buffer tank (3), the condenser (4), the flash tank (5), the weighing pressure tank (6), and the vacuum balance tank (7)—along with all the pipes and the automatic valves on all the pipes, and the corresponding sensors on the seven components, are combined in different ways to form a feeding system, a stirring system, a spray return system, a water-oil fractionation and recovery system, a discharge system, a heating system, a circulating cooling system, a distillation system, and a vacuum system. The central control system connects to and controls the feeding system, the stirring system, the spray return system, the water-oil fractionation and recovery system, the discharge system, the heating system, the circulating cooling system, the distillation system, the vacuum system, the automatic valves on the pipelines, and the corresponding sensors and automatic valves on each component; thereby realizing the heating and cooling, high temperature positive pressure, high temperature negative pressure, and the flash evaporation process with adjustable intensity and frequency of the reactor.

9. A process for producing rapeseed oil at a low temperature of 120°C according to claim 1, characterized in that, The feeding system includes an atmospheric pressure feeding system and a vacuum feeding system; an atmospheric pressure feeding system is used for liquid materials; and a vacuum feeding system is used for semi-solid and solid materials. The atmospheric pressure feeding system includes a batching vessel (1), a reaction vessel (2), a discharge pipe connecting the batching vessel (1) and the reaction vessel (2), a discharge vessel bottom valve (1.5) installed on the discharge pipe, and an vent valve (2.6) on the reaction vessel (2). The specific operation of atmospheric pressure feeding is to first open the vent valve (2.6) of the reaction vessel (2), and then open the discharge vessel bottom valve (1.5) on the discharge pipe. The material flows from the batching vessel (1) into the reaction vessel (2) by gravity, thus completing the atmospheric pressure feeding. The vacuum feeding system includes a vacuum pump and all components and pipes except for the weighing pressure water tank (6). The specific operation of the vacuum feeding is to turn on the vacuum pump to form a certain vacuum state in the reactor (2), then close the distillation pneumatic valve (2.3) on the distillation tube of the reactor (2) to maintain the vacuum in the reactor (2), and open the bottom valve (1.5) on the discharge pipe. The material in the batching tank (1) is sucked into the reactor (2). The above vacuum feeding operation can be repeated multiple times to complete the vacuum feeding.

10. A process for producing rapeseed oil at a low temperature of 120°C according to claim 1, characterized in that, The water-oil fractionation and recovery system includes the buffer tank (3), the condenser (4), the flash tank (5), the liquid level display connecting pipe (8), and related connecting pipes and valves; the water-oil fractionation and recovery system also includes a liquid level regulating pipe, a flow meter (5.2) installed on the liquid level regulating pipe, and a water supply pipe pneumatic valve (5.1) to realize the quantitative addition of water to the flash tank (5); During operation, the flash tank (5) is observed through the liquid level display connecting pipe (8). If the fraction in the flash tank (5) contains oil, it is returned to the reactor (2) through the upper oil return pipe of the reflux pipe. The liquid level of the fraction in the flash tank (5) can be pre-adjusted by injecting a quantitative amount of water through the liquid level regulating pipe. The circulating cooling water on the condenser (4) is closed, and the distillation valve (2.3) on the distillation pipe is opened to maintain the same pressure as the reactor (2) for oil return. Alternatively, the lower water return pipe of the reflux pipe can be used to return all the fraction to the reactor (2) for flash evaporation or distillation again.

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