Integrated vegetable-oil refining system

Abstract

Disclosed in the present invention is an integrated vegetable-oil refining system. Each work section uses an integrated combined tower, and an integrated combined alkali refining tower is sequentially provided with a water-washing buffer section, a secondary acidification reaction section and an alkali reaction section from top to bottom, an outlet of a degummed oil output pipe being connected to a main inlet of a static acid mixer via a steam heater, an outlet of the static acid mixer being connected to the secondary acidification reaction section, an outlet of the secondary acidification reaction section being connected to a main inlet of a static alkali mixer via a secondary acidified oil transfer pump, an outlet of the static alkali mixer being connected to the alkali reaction section, an outlet of the alkali reaction section being connected to a de-saponification centrifuge via a neutralized oil transfer pump and a steam heater, a light-phase soap-free oil outlet of the de-saponification centrifuge being connected to an upper-end inlet of the water-washing buffer section, a bottom outlet of the water-washing buffer section being connected to an inlet of a water-washing centrifuge, and a light-phase water-washed oil outlet of the water-washing centrifuge being connected to a water-washed oil output pipe. The present invention reduces the equipment cost, saves on installation materials, and decreases the area occupied by the system and the building area.

Description

Integrated vegetable oil refining system Technical Field

[0001] The present invention relates to an oil refining system, in particular to an integrated vegetable oil refining system, and belongs to the technical field of oil refining. Background Art

[0002] The oil refining workshop includes degumming, alkali refining, bleaching, deodorization, and winterization. The degumming process is divided into various routes, including water degumming, acid degumming, super degumming, and enzymatic degumming, depending on the process characteristics. Among them: 1. Water degumming is used to combine the hydrated phospholipids in the oil with process hot water to form a colloid and separate it from the oil. Water degumming is mostly used to produce high-quality phospholipid products; 2. Acid degumming is used to convert some non-hydratable phospholipids in the oil into hydrated phospholipids through an acidification reaction, and combine them with process hot water to form a colloid and separate it from the oil. Acid degumming is often used to reduce the phospholipid content in the oil and improve the frying quality of the oil; 3. Super degumming is used to convert some non-hydratable phospholipids in the oil into hydrated phospholipids through an acidification reaction, and then combine them with light alkaline water to form a colloid and separate it from the oil. Super degumming can remove most of the phospholipids in the oil to obtain high-quality degummed oil; 4. Enzyme degumming is used to react non-hydratable phospholipids in the oil with enzymes. The hydrophilicity of the non-hydratable phospholipids after the reaction is enhanced, and they combine with process hot water to form a colloid and separate it from the oil. Enzyme degumming can remove most of the phospholipids in the oil to obtain high-quality degummed oil while also increasing the oil yield. The above degumming process can be selected according to different process requirements.

[0003] The Chinese invention patent with authorization announcement number CN1042140C discloses a device for continuous hydration and degumming of vegetable oil, including a pump, a heat exchanger, a hot water tank, a multi-layer reaction tank (hydration tank), a separator, a vacuum dryer and other equipment. The above equipment is set separately, and the hydration tank adopts paddle-type mechanical stirring.

[0004] Chinese utility model patent publication number CN211972258U discloses a novel integrated system for enzymatic degumming of oils and fats. The system includes a pump, heat exchanger, mixer, centrifuge, acid storage tank, alkali storage tank, acid reactor, and enzyme reactor. Each of these components is individually configured and uses non-standard containers. The acid and enzyme reactors utilize paddle-type mechanical agitation.

[0005] In addition to pumps, heat exchangers, mixers, centrifuges, and other equipment, the traditional alkali refining process also includes non-standard containers such as acidification tanks, alkali reaction tanks, water wash buffer tanks, vacuum dryers, soft water tanks, and hot water tanks. These tanks are also equipped with mechanical agitators. For example, Chinese utility model patent publication number CN204737934U discloses a fat alkali refining plant comprising a lye tank, water tank, alkali refining pot, centrifuge, oil tank, and saponification pot. These devices are separately installed, with the alkali refining pot and saponification pot utilizing paddle-type mechanical agitators.

[0006] In addition to pumps, heat exchangers, and filters, traditional decolorization processes also include non-standard containers such as pulse dust collectors, decolorant dosing systems, premixing tanks, decolorization towers, and intermediate oil tanks. For example, Chinese utility model patent publication number CN211946944U discloses a grease decolorization system that includes a pre-decolorization tower, a pre-decolorization filter, a decolorization premixing tank, a decolorization tower, a self-cleaning filter, and a decolorization filter, all of which are separately installed.

[0007] The Chinese utility model patent with announcement number CN218642694U discloses a zero-trans fatty acid deodorization system for edible oil. In addition to equipment such as pumps and heat exchangers, it also includes non-standard container equipment such as gas analysis chambers, economizers, falling film heaters, deodorization towers, and fatty acid collectors.

[0008] Traditional vegetable oil refining systems and processes generally have the following problems:

[0009] 1. The process design of each section is complex, with many process equipment, pipes for various media, valves and other installation materials, and a large amount of building space. This significantly increases the project construction cost and the project construction period;

[0010] 2. Due to the large number of pipelines and equipment in each section, it is difficult to drain the internal materials in a timely and effective manner. A large amount of residue in the system can easily cause pipeline blockage and affect product quality.

[0011] 3. Multiple reaction tanks in each section use paddle-type mechanical stirring devices, which have low stirring and mixing efficiency, inadequate reaction process, high consumption of acid and alkali auxiliary materials, high oil loss, and increased maintenance costs;

[0012] 4. In the traditional bleaching process, the bleaching agent is added in batches using an AB valve and a metering cylinder. The clay and oil are mixed by mechanical stirring under vacuum, which results in insufficient mixing of the clay and oil, high consumption of bleaching agent auxiliary materials, high oil loss, and the bleaching agent easily enters the vacuum pipes and vacuum equipment with the vacuum, causing pipe and equipment blockage, affecting normal production, and increasing maintenance costs.

[0013] 5. The energy-saving heat exchange of the oil in the traditional deodorization process and the final heating before deodorization both require a long time. The oil stays at high temperature for a long time, resulting in a large loss of some nutrients in the refined oil, such as vitamin E and sterols, and an increase in the content of harmful substances such as trans fatty acids and glycidyl esters.

[0014] Summary of the Invention

[0015] The purpose of this section is to summarize some aspects of the embodiments of the present invention and briefly introduce some preferred embodiments. Some simplifications or omissions may be made in this section and the abstract and title of this application to avoid obscuring the purpose of this section, the abstract and the title of the invention, and such simplifications or omissions should not be used to limit the scope of the present invention.

[0016] In view of the above problems and / or the problems existing in the prior art, the present invention is proposed.

[0017] The purpose of the present invention is to overcome the problems existing in the prior art and provide an integrated vegetable oil refining system to replace the traditional dispersed process reaction tanks, simplify the refining process, reduce equipment manufacturing costs, save installation materials, and reduce the system footprint and building area.

[0018] In order to solve the above technical problems, the vegetable oil integrated refining system of the present invention includes a degumming section and an alkali refining section, wherein the alkali refining section includes an integrated combined alkali refining tower, wherein the integrated combined alkali refining tower is stacked with a water washing buffer section, a secondary acidification reaction section and an alkali reaction section in sequence from top to bottom, the outlet of the degummed oil output pipe is connected to the cold side inlet of the steam heater C, the cold side outlet of the steam heater C is connected to the main inlet of the static acid mixer B, the outlet of the static acid mixer B is connected to the top inlet of the secondary acidification reaction section, and the bottom outlet of the secondary acidification reaction section is connected to the bottom outlet of the secondary acidification reaction section. The secondary acidification oil delivery pump is connected to the main inlet of the static alkali mixer B, the outlet of the static alkali mixer B is connected to the upper inlet of the alkali reaction section, the bottom outlet of the alkali reaction section is connected to the cold side inlet of the steam heater D through the neutralization oil delivery pump, the cold side outlet of the steam heater D is connected to the inlet of the soap removal centrifuge, the light phase soap removal oil outlet of the soap removal centrifuge is connected to the upper end inlet of the water washing buffer section, the bottom outlet of the water washing buffer section is connected to the inlet of the water washing centrifuge, and the light phase water washing oil outlet of the water washing centrifuge is connected to the water washing oil output pipe.

[0019] Furthermore, the degumming section is a hydration degumming section, and the hydration degumming section includes an integrated combined degumming tower, which is stacked with a hydration reaction section, a degumming vacuum drying section, a hot water tank and a soft water tank in sequence from top to bottom. The outlet of the raw oil pump is connected to the cold side inlet of the steam heater A, the cold side outlet of the steam heater A is connected to the main inlet of the static water mixer, the water inlet of the static water mixer is connected to the outlet of the process hot water pipe, the outlet of the static water mixer is connected to the upper inlet of the hydration reaction section in the integrated combined degumming tower, the lower outlet of the hydration reaction section is connected to the inlet of the degumming centrifuge through a hydration oil delivery pump, the light phase outlet of the degumming centrifuge is connected to the upper inlet of the degumming vacuum drying section, the exhaust port of the degumming vacuum drying section is connected to the degumming vacuum pipe, and the bottom outlet of the degumming vacuum drying section is connected to the degumming oil output pipe through a degumming drying oil delivery pump; the outlet of the hot water tank is connected to the inlet of the process hot water pipe through a hot water pump.

[0020] Furthermore, the degumming section is an acidification degumming section, and the acidification degumming section includes an integrated combined degumming tower, and the integrated combined degumming tower is stacked with a primary acidification reaction section, a hydration reaction section and a degumming vacuum drying section in sequence from top to bottom. The outlet of the raw oil pump is connected to the cold side inlet of the steam heater A, and the cold side outlet of the steam heater A is connected to the main inlet of the static acid mixer A, and the acid inlet of the static acid mixer A is connected to the acid liquid pipe; the outlet of the static acid mixer A is connected to the top inlet of the primary acidification reaction section, and the bottom outlet of the primary acidification reaction section is connected to the primary acidification reaction section through the primary acidification reaction section. The hydration oil delivery pump is connected to the main inlet of the static water mixer, the water inlet of the static water mixer is connected to the outlet of the process hot water pipe, the outlet of the static water mixer is connected to the upper inlet of the hydration reaction section in the integrated combined degumming tower, the lower outlet of the hydration reaction section is connected to the inlet of the degumming centrifuge through the hydration oil delivery pump, the light phase outlet of the degumming centrifuge is connected to the upper inlet of the degumming vacuum drying section, the exhaust port of the degumming vacuum drying section is connected to the degumming vacuum pipe, and the bottom outlet of the degumming vacuum drying section is connected to the degumming oil output pipe through the degumming drying oil delivery pump.

[0021] Furthermore, the outlet of the primary acidified oil delivery pump is connected to the hot side inlet of water cooler A, the hot side outlet of water cooler A is connected to the main inlet of the static water mixer, and the water inlet of the static water mixer is also connected to the alkali liquid pipe; the outlet of the hydrated oil delivery pump is connected to the cold side inlet of steam heater B, and the cold side outlet of steam heater B is connected to the inlet of the degumming centrifuge.

[0022] Furthermore, the degumming section is an enzymatic degumming section, and the enzymatic degumming section includes an integrated combined degumming tower, and the integrated combined degumming tower is sequentially stacked with a primary acidification reaction section, an enzyme reaction section and a vacuum drying section from top to bottom, the outlet of the raw oil pump is connected to the cold side inlet of the steam heater A, the cold side outlet of the steam heater A is connected to the main inlet of the static acid mixer A, the acid inlet of the static acid mixer A is connected to the acid liquid pipe, the outlet of the static acid mixer A is connected to the top inlet of the primary acidification reaction section, the bottom outlet of the primary acidification reaction section is connected to the hot side inlet of the water cooler A through the primary acidification oil delivery pump, and the hot side outlet of the water cooler A is connected to the static alkali The main inlet of the mixer A is connected, the alkali liquid inlet of the static alkali mixer A is connected to the alkali liquid pipe, the outlet of the static alkali mixer A and the outlet of the enzyme preparation pipe are commonly connected to the inlet of the enzyme mixer, the outlet of the enzyme mixer is connected to the upper inlet of the enzyme reaction section, the lower outlet of the enzyme reaction section is connected to the cold side inlet of the steam heater B through the enzyme reaction section oil outlet pump, the cold side outlet of the steam heater B is connected to the inlet of the degumming centrifuge, the light phase outlet of the degumming centrifuge is connected to the upper inlet of the vacuum drying section, the exhaust port of the vacuum drying section is connected to the degumming vacuum pipe, and the bottom outlet of the vacuum drying section is connected to the degumming oil output pipe through the degumming drying oil delivery pump.

[0023] Furthermore, a soft water tank is provided below the hot water tank, the outlet of the soft water tank is connected to the inlet of a soft water pump, and the outlet of the soft water pump is connected to the water supply port of the hot water tank and the flushing port of the degumming centrifuge through a soft water pipe.

[0024] Furthermore, a decolorization section is provided downstream of the alkali refining section, the decolorization section including an integrated combined decolorization tower, the integrated combined decolorization tower sequentially stacked with a pulse dust collector, a decolorant temporary storage tank and a decolorization reaction section from top to bottom, the decolorization reaction section including a static mixing structure located above and a stirring decolorization section located below;

[0025] The inlet of the decolorant temporary storage tank is connected to the outlet of the decolorant delivery pipe, the top outlet of the decolorant temporary storage tank is connected to the inlet of the pulse dust collector, and the top outlet of the pulse dust collector is connected to the atmosphere through a dust removal fan;

[0026] The bottom outlet of the decolorant temporary storage tank is connected to the decolorant inlet of the static mixing structure through a metering rotary valve; the outlet of the alkali refining output pipe is connected to the cold side inlet of the steam heater E, and the cold side outlet of the steam heater E is connected to the oil inlet of the static mixing structure; the bottom outlet of the stirring and decolorizing section is connected to the oil inlet of the decolorizing filter through a filter feeding pump, and the middle oil outlet of the decolorizing filter is connected to the decolorizing oil output pipe.

[0027] Furthermore, an intermediate oil tank is provided at the bottom of the integrated combined decolorization tower, and at least two decolorization filters are provided in parallel. The oil inlet and intermediate oil outlet of each decolorization filter are respectively connected to the dirty oil collection pipe through a valve, and the outlet of the dirty oil collection pipe is connected to the upper inlet of the intermediate oil tank. The bottom outlet of the intermediate oil tank is connected to the upper oil return port of the stirring decolorization section through a siphon return oil pipe.

[0028] Furthermore, the stirring and decolorizing section is a steam stirring and decolorizing section or a jet stirring and decolorizing section.

[0029] Furthermore, the upper side wall exhaust port of the stirring and decolorizing section is connected to the inlet of the gas-liquid separator, the top outlet of the gas-liquid separator is connected to the decolorizing vacuum pipe, and the bottom outlet of the gas-liquid separator is connected to the upper oil return port of the stirring and decolorizing section.

[0030] Furthermore, the upper outlet of each decolorization filter shell is connected to the top flow return oil pipe through a valve, the outlet of the top flow return oil pipe is connected to the upper inlet of the intermediate oil tank, and the top exhaust port of the intermediate oil tank is connected to the decolorization vacuum pipe.

[0031] Furthermore, a deodorization section is provided downstream of the decolorization section, and the deodorization section includes an integrated combined deodorization tower, and the integrated combined deodorization tower is stacked with a fatty acid collector, a post-deacidification tower section, a pre-deacidification tower section and a plate tower stripping section in sequence from top to bottom. The decolorized oil output pipe is connected to the upper inlet of the gas analysis chamber, and the bottom outlet of the gas analysis chamber is connected to the lower shell inlet of the falling film economizer through the gas analysis oil delivery pump. The upper shell outlet of the falling film economizer is connected to the oil inlet of the pre-deacidification tower section, and the bottom of the pre-deacidification tower section is connected to the plate tower stripping section. The upper part of the plate tower stripping section is connected, the bottom oil outlet of the plate tower stripping section is connected to the cold side inlet of the falling film heater through the plate tower oil outlet pump, the cold side outlet of the falling film heater is connected to the upper oil inlet of the post-deacidification tower section, the lower oil outlet of the post-deacidification tower section is connected to the hot side inlet of the falling film economizer, and the hot side outlet of the falling film economizer is connected to the inlet of the deodorizing oil delivery pump; the top gas phase port of the post-deacidification tower section is communicated with the bottom of the fatty acid trap, and the top exhaust port of the fatty acid trap is connected to the deodorization vacuum pipe.

[0032] Furthermore, the bottom liquid outlet of the fatty acid trap is connected to the inlet of the fatty acid circulation pump, the outlet of the fatty acid circulation pump is respectively connected to the fatty acid discharge pipe and the hot side inlet of water cooler B, and the hot side outlet of water cooler B is connected to the top spray port of the fatty acid trap.

[0033] Furthermore, the falling film economizer is built into the central air pump of the plate tower stripping section, and the annular space between the central air pump and the plate tower stripping section cylinder is provided with multiple layers of tower trays, each layer of tower trays is provided with a stripping pump; vent holes are evenly distributed on the circumference of the central air pump so that the gas phase space of the tower trays communicates with the inner cavity of the central air pump;

[0034] The inner cavity of the shell of the falling film economizer is provided with falling film tubes, which run through the upper tube plate and the lower tube plate, and an oil distribution pan is provided above the upper tube plate; the lower end of the shell of the falling film economizer passes through the lower head of the plate tower stripping section and is connected to a deodorized oil buffer tank below the lower tube plate, and a deodorized oil outlet is provided at the bottom of the deodorized oil buffer tank.

[0035] Furthermore, each of the tower plates is provided with a partitioned inner cylinder coaxial with the plate tower stripping section cylinder, the inner side of the partitioned inner cylinder is the inner ring flow channel, and the outer side of the partitioned inner cylinder is the outer ring flow channel; a radial partition is provided between the outer wall of the central vacuum cylinder and the inner wall of the plate tower stripping section cylinder; the outlet of the overflow pipe of the upper tower plate turns to point to the head end of the inner ring flow channel close to the side of the radial partition, and the tail end of the partitioned inner cylinder close to the other side of the radial partition is provided with a notch connected to the head end of the outer ring flow channel.

[0036] Furthermore, the tail end of the outer ring flow channel is provided with a tower plate overflow pipe for overflowing to the head end of the inner ring flow channel of the next layer; or the head end of the inner ring flow channel is provided with a tower plate overflow pipe for overflowing to the tail end of the outer ring flow channel of the next layer; or the tail end of the outer ring flow channel is provided with a tower plate overflow pipe for overflowing to the tail end of the outer ring flow channel of the next layer, and the head end of the inner ring flow channel is provided with a tower plate overflow pipe for overflowing to the head end of the inner ring flow channel of the next layer.

[0037] Furthermore, each of the tower plates is tilted so that it is higher on the outside and lower on the inside, and a tower plate drain pipe is connected to the lowest point of the tower plate. The tower plate drain pipe of each layer extends to the outside of the plate tower stripping section cylinder and is connected to the tower plate reflux port of the lower layer through a drain valve. The tower plate reflux port is located below the liquid level of the outer ring flow channel.

[0038] Furthermore, a reduced diameter section is provided at the lower part of the central vacuum cylinder, the upper end of the reduced diameter section is located below the vent hole of the bottom layer, and a liquid sealing disk is provided at the lower end of the reduced diameter section of the vacuum cylinder, and a drainage hole is provided on the liquid sealing disk.

[0039] Furthermore, an oil distributing cylinder for evenly overflowing toward the oil distribution pan is provided below the inner end of the oil inlet pipe of the falling film energy saver. The oil distribution pan is fixed on the upper tube plate of the falling film energy saver by supporting bolts. The oil distribution pan is evenly distributed with a plurality of oil distribution holes which are narrow at the top and wide at the bottom. The projections of the oil distribution holes are symmetrically distributed in the shape of a right triangle around the upper tube openings of each falling film tube array; air permeable pipes passing through the oil layer are evenly distributed on the oil distribution pan.

[0040] Compared with the existing technology, the present invention has achieved the following beneficial effects: 1. The integrated combined degumming tower is adopted to replace the traditional non-standard container equipment such as hydration tank, acidification tank, enzyme reaction tank, vacuum drying tower, soft water tank, hot water tank, etc., which simplifies the process design of the hydration degumming section, reduces the equipment manufacturing cost, saves installation materials, and reduces the construction area, thereby effectively reducing the project construction cost and shortening the project construction period.

[0041] 2. The hydration reaction section, acidification reaction section and enzyme reaction section of the integrated combined degumming tower adopt a jet stirring device, and combined with an external oil circulation pump, it replaces the traditional blade-type mechanical stirring, improves the reaction efficiency, product quality and equipment operation reliability, reduces the consumption of acid and alkali auxiliary materials and oil loss, shortens the system start-up and shutdown time, and reduces the system inventory.

[0042] 3. The degumming process uses static water mixers, static acid mixers, and static alkali mixers to replace traditional power mixers, which are convenient for direct installation in pipelines and reduce energy consumption.

[0043] 4. The integrated combined alkali refining tower replaces traditional non-standard container equipment such as acidification tanks, alkali reaction tanks, and water washing buffer tanks, which simplifies the process design of the alkali refining section, reduces equipment manufacturing costs, saves installation materials, and reduces construction area, thereby effectively reducing project construction costs and shortening the project construction period.

[0044] 5. The secondary acidification reaction section, alkali reaction section and water washing buffer section of the combined alkali refining tower adopt a jet stirring device, and combined with an external oil circulation pump, it replaces the traditional blade-type mechanical stirring, improves the reaction efficiency, product quality and equipment operation reliability, reduces the consumption of auxiliary materials such as acid, alkali, and water washing water, and grease loss; at the same time, it improves the equipment operation reliability, shortens the system start-up and shutdown time, and reduces the system inventory.

[0045] 6. The integrated combined decolorization tower replaces traditional non-standard container equipment such as decolorant temporary storage tanks, premixing tanks, decolorization towers, and waste oil tanks, which simplifies the process design of the decolorization section, reduces equipment manufacturing costs, saves installation materials, and reduces construction area, thereby effectively reducing project construction costs and shortening the project construction period.

[0046] 7. The metering rotary valve of the integrated combined bleaching tower adopts a continuous metering method to replace the traditional AB valve and metering cylinder. The bleaching reaction section adopts a static mixing structure to replace the traditional mechanical stirring and mixing, which improves the mixing efficiency of the bleaching agent and oil, reduces the consumption of bleaching agent auxiliary materials, and at the same time improves product quality and equipment operation reliability, reduces oil and fat loss, reduces system inventory, and shortens system start-up and shutdown time.

[0047] 8. The integrated combined deodorization tower replaces traditional non-standard container equipment such as fatty acid traps, pre-deacidification towers, post-deacidification towers, plate towers, and gas analysis chambers. This simplifies the process design of the deodorization section, reduces equipment manufacturing costs, saves installation materials, and reduces construction area, thereby effectively reducing project construction costs and shortening the project construction period.

[0048] 9. The falling film heat exchange structure replaces the traditional immersed tube heat exchange or coil heat exchange structure to improve the heat exchange efficiency, significantly reduce the residence time of oil at high temperature, and improve the nutritional quality of refined oil; at the same time, it significantly reduces the amount of material stored in the system and shortens the system start-up and shutdown time;

[0049] 11. For the deodorization section with large production capacity, the space of the central tube in the tower is fully utilized, and the falling film economizer for heat exchange of hot and cold oil is placed in the central exhaust tube of the plate tower stripping section. Further integration makes the falling film economizer have no heat loss and does not require insulation. The deodorized oil in the falling film tube is cooled by the falling film in the vacuum, with high heat exchange efficiency, short residence time, and no mixing back, which effectively avoids the formation of trans acid and harmful polymers.

[0050] 11. The plate stripping section of the integrated combined deodorization tower is in low-temperature mode, taking into account the necessary residence time, so that thermal decomposition, thermal decolorization, trans acid and polymer generation can be controlled. At the same time, the residence time of oil in each layer of the plate stripping section can be adjusted according to process requirements.

[0051] 12. The integrated combined deodorization tower makes full use of the central tube space in the tower and integrates the heat exchange of hot and cold oils into the central gas phase exhaust tube of the plate tower stripping section. There is no heat loss, no need for insulation, and the finished oil in the tube is cooled by vacuum falling film. The heat exchange efficiency is high, the residence time is short, and there is no mixing back, which effectively avoids the formation of trans acids and harmful polymers. After the cold oil is heat exchanged, it directly meets the process requirements of low-temperature deodorization, saving the oil heating device.

[0052] 13. The integrated deodorization tower features a built-in energy-saving heat exchanger, eliminating flange seals on the upper oil pan. This saves manufacturing materials, facilitates assembly and disassembly, and completely eliminates leakage and oxidation of the finished oil from contact with air. The concentric circular oil flow path design on the plate ensures a first-in, first-out system, preventing localized oil stagnation that could affect quality.

[0053] 14. The integrated combined degumming tower, integrated combined alkali refining tower, integrated combined bleaching tower and integrated combined deodorizing tower all adopt a modular design, which saves installation space and floor space, reduces the amount of installation materials, reduces equipment costs, eliminates a large number of pipeline connections, fully utilizes the gravity flow of oil, eliminates unnecessary pump transportation, reduces factory investment and subsequent production and maintenance costs; at the same time, it solves the problems of large fluid resistance along the process, heat loss, and leakage risks of bellows and valves, and can be flexibly configured according to the characteristics of the oil and process index requirements. BRIEF DESCRIPTION OF THE DRAWINGS

[0054] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the following briefly introduces the drawings required for describing the embodiments. Obviously, the drawings described below are only some embodiments of the present invention. Those skilled in the art can also derive other drawings based on these drawings without inventive work. The drawings are provided for reference and explanation only and are not intended to limit the present invention. Among them:

[0055] FIG1 is a flow chart of the hydration degumming section of the present invention;

[0056] FIG2 is a flow chart of the acidification degumming section of the present invention;

[0057] FIG3 is a flow chart of the super degumming section in the present invention;

[0058] FIG4 is a flow chart of the enzymatic degumming process section of the present invention;

[0059] FIG5 is a flow chart of the alkali refining section of the present invention;

[0060] FIG6 is a flow chart of a first embodiment of the decolorization process of the present invention;

[0061] FIG7 is a flow chart of a second embodiment of the decolorization process of the present invention;

[0062] FIG8 is a flow chart of a first embodiment of the deodorization process of the present invention;

[0063] FIG9 is a flow chart of Example 2 of the deodorization section of the present invention;

[0064] FIG10 is a cross-sectional view of an embodiment of the stripping section of the plate tower in FIG9 ;

[0065] FIG11 is a cross-sectional view of the upper end of the falling film economizer in FIG10 ;

[0066] FIG12 is a top view of the upper portion of the falling film economizer in FIG10 ;

[0067] FIG13 is a flow diagram of an embodiment after the partition inner cylinder in the tower tray is separated;

[0068] In the figure: 1. Steam heater A; 2. Static acid mixer A; 2a. Static water mixer;

[0069] 3. Integrated combined degumming tower; 3a. Primary acidification reaction section; 3b. Enzyme reaction section; 3c. Degumming vacuum drying section; 3d. Hot water tank; 3e. Soft water tank; 3f. Hydration reaction section;

[0070] 4. Static alkali mixer A; 5. Degumming centrifuge; 6. Steam heater B; 7. Water cooler A; 8. Enzyme mixer; 9. Steam heater C; 10. Static acid mixer B;

[0071] 11. Integrated combined alkali refining tower; 11a. Secondary acidification reaction section; 11b. Alkali reaction section; 11c. Water washing buffer section; 11d. Alkali refining vacuum drying section;

[0072] 12. Static alkali mixer B; 13. Steam heater D; 14. Soap removal centrifuge; 15. Water washing centrifuge; 16. Steam heater E;

[0073] 17. Integrated combined decolorization tower; 17a. Pulse dust collector; 17b. Decolorant temporary storage tank; 17c. Metering and addition rotary valve; 17d. Decolorization reaction section; 17e. Intermediate oil tank;

[0074] 18. Decolorization filter; 19. Dust removal fan; 20. Gas-liquid separator;

[0075] 21. Integrated combined deodorization tower; 21a. Fatty acid collector; 21b. Post-deacidification tower section; 21c. Pre-deacidification tower section;

[0076] 21d. Plate tower stripping section; 21d1. Partitioned inner cylinder; 21d2. Radial baffle; 21d3. Tray overflow pipe; 21d4. Stripping pump; 21d5. Annular jet pipe in the plate tower stripping section;

[0077] 21e. Gas analysis chamber; 21e1. Decolorized oil inlet; 21e2. Decolorized oil spray pipe; 21e3. Pre-degassing vacuum port; 21e4. Gas analysis chamber oil outlet;

[0078] 22. Falling film economizer; 22a. Oil diffuser; 22b. Oil distribution tray; 22c. Ventilation pipe; 22d. Support bolts; 22e. Upper tube sheet; 22f. Falling film tubes; 22g. Lower shell-side inlet; 22h. Upper shell-side outlet; 22j. Deodorized oil buffer tank; 22k. Deodorized oil outlet;

[0079] 23. Falling film heater; 24. Water cooler B;

[0080] P1. Raw oil pump; P2. Primary acidification oil transfer pump; P2a. Hydration oil transfer pump; P3. Primary acidification oil circulation pump; P3a. Hydration oil circulation pump; P4. Enzyme reaction section oil outlet pump; P5. Enzyme reaction section circulation pump; P6. Degumming and drying oil transfer pump; P7. Hot water pump; P8. Soft water pump; P9. Secondary acidification oil transfer pump; P10. Secondary acidification oil circulation pump; P11. Neutralization oil transfer pump; P12. Neutralization oil circulation pump; P13. Wash oil circulation pump; P14. Alkali refining and drying oil transfer pump; P15. Filtration feed pump; P16. Bleached oil circulation pump; P17. Gasification oil transfer pump; P18. Plate tower oil outlet pump; P19. Deodorized oil transfer pump; P20. Fatty acid circulation pump;

[0081] G1. Raw material pipeline; G2. Acid pipe; G3. Degummed oil output pipe; G4. Steam pipe; G5. Degummed oil vacuum pipe; G6. Process hot water pipe; G7a. Soft water supply pipe; G7b. Soft water supply pipe; G8. Alkali liquid pipe; G9. Enzyme preparation pipe; G10. Alkali refining vacuum pipe; G11. Alkali refining oil output pipe; G12. Decolorant delivery pipe; G13. Filter feed pipe; G14. Decolorization vacuum pipe; G15. Top flow return oil pipe; G16. Intermediate circulation pipe; G17. Waste oil collection pipe; G18. Siphon return oil pipe; G19. Decolorization oil output pipe; G20. Deodorized oil outlet pipe; G21. Fatty acid outlet pipe; G22. Deodorization vacuum pipe. DETAILED DESCRIPTION

[0082] In the following description of the present invention, terms such as "upper," "lower," "front," "back," "left," "right," "inner," and "outer" indicate positions or locations based on the positions shown in the accompanying drawings. These terms are used solely to facilitate description and simplify the present invention and do not necessarily imply that the device must have a specific orientation. All percentages not otherwise specified are by weight.

[0083] In order to make the technical means, creative features, objectives and effects of the present invention easier to understand, the present invention is further described below with reference to specific figures. Obviously, the embodiments described are only part of the embodiments of the present invention, not all of them.

[0084] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by those skilled in the art to which the present invention pertains. The terms used herein in the specification of the present invention are for the purpose of describing specific embodiments only and are not intended to limit the present invention.

[0085] The vegetable oil integrated refining system of the present invention comprises a degumming section, an alkali refining section, a decoloring section and a deodorizing section which are connected in sequence.

[0086] As shown in Figure 1, one of the degumming stages in the present invention is the hydration degumming stage. The principle of hydration degumming is to utilize the hydrophilicity of phospholipids to cause the hydrated phospholipids to absorb water, swell, and condense, and then be separated from the oil by centrifugation. It also absorbs proteins, mucus, and trace metal ions bound to the phospholipids. Hydration degumming can only remove hydrated phospholipids, but it is difficult to remove non-hydratable phospholipids. After hydration degumming, oils and fats generally contain 100-200 ppm of phosphorus. Currently, edible oil processing plants mostly use hydration degumming technology to separate the phospholipids from oils and fats, further purify them, and make them into high-value-added health products to improve the company's economic benefits.

[0087] The hydration degumming section includes a steam heater A 1, a static water mixer 2a, an integrated combined degumming tower 3 and a degumming centrifuge 5. The integrated combined degumming tower 3 includes a hydration reaction section 3f, a degumming vacuum drying section 3c, a hot water tank 3d and a soft water tank 3e stacked in sequence from top to bottom.

[0088] The outlet of the raw material pipeline G1 is connected to the inlet of the raw material oil pump P1, the outlet of the raw material oil pump P1 is connected to the cold side inlet of the steam heater A1, the hot side inlet of the steam heater A1 is connected to the steam pipe G4, the cold side outlet of the steam heater A1 is connected to the main inlet of the static water mixer 2a, the water inlet of the static water mixer 2a is connected to the process hot water pipe G6, the outlet of the static mixer 2 is connected to the top inlet of the hydration reaction section 3f at the top of the integrated combined degumming tower 3, and the hydration reaction section 3f is connected to the main inlet of the static water mixer 2a. The outlet is connected to the inlet of hydrated oil delivery pump P2a, which is in turn connected to the inlet of degumming centrifuge 5. The light phase outlet of degumming centrifuge 5 is connected to the upper inlet of degumming vacuum drying section 3c in integrated combined degumming tower 3. The top exhaust port of degumming vacuum drying section 3c is connected to degumming vacuum pipe G5. The lower outlet of degumming vacuum drying section 3c is connected to the inlet of degumming drying oil delivery pump P6, the outlet of which is connected to degumming oil output pipe G3. Meanwhile, a hot water tank 3d and a soft water tank 3e are located in the lower section of integrated combined degumming tower 3 to supply hot process water and soft water to the degumming section.

[0089] The raw oil from feedstock pipeline G1 is pumped by feedstock pump P1 into the cold side of steam heater A1, where it undergoes heat exchange with steam from the hot side, raising the oil temperature from 30°C to 80-85°C. The oil then enters static water mixer 2a, where it is mixed with a certain proportion of 85-90°C process hot water (1-3% of the oil weight). After mixing, it enters hydration reaction section 3f of integrated combined degumming tower 3 for a hydration reaction lasting approximately 30 minutes. In this hydration reaction section, the hydrophilic colloids in the raw oil combine with water and condense into macromolecular colloidal particles. The hydrated oil is then transported by hydrated oil delivery pump P2a to degumming centrifuge 5. The separated light phase degummed oil, with a moisture content of approximately 0.5%, enters degumming vacuum drying section 3c of integrated combined degumming tower 3 for drying and dehydration. The dehydrated oil has a moisture content of approximately 0.05% and is then transported out of the degumming section via degumming drying oil delivery pump P6 and degummed oil outlet pipe G3.

[0090] The hydration reaction section 3f of the integrated combined degumming tower 3 is internally provided with a multi-stage jet mixer. The hydrated oil discharged from the bottom of the hydration reaction section 3f is transported by the hydrated oil circulation pump P3a and enters the jet mixers at each stage to achieve a sufficient mixing reaction of the hydrated oil.

[0091] In the integrated combined degumming tower 3, the water inlet of the soft water tank 3e is connected to the soft water supply pipe G7a. The bottom outlet of the soft water tank 3e is connected to the inlet of the soft water pump P8. The outlet of the soft water pump P8 is connected to the water inlet of the hot water tank 3d via the soft water supply pipe G7b. This is used to prepare process hot water for the hydration and degumming reaction of the crude oil. The soft water supply pipe G7b is also connected to the clean water inlet of the degumming centrifuge 5 for washing the drum of the degumming centrifuge 5.

[0092] The bottom outlet of hot water tank 3d is connected to the inlet of hot water pump P7, which in turn is connected to process hot water pipe G6. After softened water is injected into hot water tank 3d, it is heated by steam to hot water. Hot water pump P7 then delivers the hot water via process hot water pipe G6 to the inlet of static water mixer 2a and the inlet of degumming centrifuge 5.

[0093] As shown in Figure 2, the second degumming process in the present invention is the acid degumming process. Acid degumming is used to further remove phospholipids from the oil. Typically, organic acids such as citric acid or inorganic acids such as phosphoric acid are added to the feedstock oil to convert the non-hydratable phospholipids in the oil into easily removable hydrated phospholipids. This process also neutralizes the surface charge points of the colloidal dispersed phase particles, causing them to aggregate and settle. It also frees metal ions such as calcium, magnesium, and iron that are bound to the phospholipids and transfers them to the aqueous phase, thereby achieving a degumming effect. Acid degumming technology is the most effective and commonly used method for removing non-hydratable phospholipids from oils and fats. Oils and fats after acid degumming generally contain 20 to 100 ppm of phosphorus.

[0094] The acidification and degumming section includes a steam heater A1, a static acid mixer A2, an integrated combined degumming tower 3, a static water mixer 2a and a degumming centrifuge 5. The integrated combined degumming tower 3 includes a primary acidification reaction section 3a, a hydration reaction section 3f, a degumming vacuum drying section 3c, a hot water tank 3d and a soft water tank 3e stacked in sequence from top to bottom.

[0095] The outlet of the raw material pipeline G1 is connected to the inlet of the raw material oil pump P1, the outlet of the raw material oil pump P1 is connected to the cold side inlet of the steam heater A1, the hot side inlet of the steam heater A1 is connected to the steam pipe G4, the cold side outlet of the steam heater A1 is connected to the main inlet of the static acid mixer A2, and the acid inlet of the static acid mixer A2 is connected to the acid liquid pipe G2; the outlet of the static acid mixer A2 is connected to the top inlet of the primary acidification reaction section 3a at the top of the integrated combined degumming tower 3, the bottom outlet of the primary acidification reaction section 3a is connected to the inlet of the primary acidification oil delivery pump P2, the outlet of the primary acidification oil delivery pump P2 is connected to the main inlet of the static water mixer 2a, and the static water mixer 2 The water inlet of the degumming tower 3a is connected to the process hot water pipe G6. The outlet of the static water mixer 2a is connected to the top inlet of the hydration reaction section 3f in the integrated combined degumming tower 3. The outlet of the hydration reaction section 3f is connected to the inlet of the hydration oil delivery pump P2a. The outlet of the hydration oil delivery pump P2a is connected to the inlet of the degumming centrifuge 5. The light phase outlet of the degumming centrifuge 5 is connected to the upper inlet of the degumming vacuum drying section 3c in the integrated combined degumming tower 3. The top exhaust port of the degumming vacuum drying section 3c is connected to the degumming vacuum pipe G5. The lower outlet of the degumming vacuum drying section 3c is connected to the inlet of the degumming drying oil delivery pump P6. The outlet of the degumming drying oil delivery pump P6 is connected to the degumming oil output pipe G3. Meanwhile, a hot water tank 3d and a soft water tank 3e are located in the lower section of the integrated combined degumming tower 3 to supply hot process water and soft water to the degumming section.

[0096] The raw oil from the raw material pipeline G1 is transported by the raw oil pump P1 to the cold side of the steam heater A1, where it undergoes heat exchange with the steam on the hot side, raising the oil temperature from 30°C to 80°C-85°C. The oil then enters the static acid mixer A2 and is mixed with a certain proportion of acid, usually about 0.05-0.2% of the weight of the oil. The oil then enters the primary acidification reaction section 3a of the integrated combined degumming tower 3 for an acidification reaction of about 60 minutes. The non-hydratable phospholipids in the oil are converted into hydratable phospholipids. The acidified oil after the reaction is subjected to a The sub-acidified oil is pumped out by pump P2 and then enters a static water mixer 2a, where it is mixed with a certain proportion of 85-90°C process hot water (approximately 1-3% of the oil weight). It then enters the hydration reaction section 3f of the integrated combined degumming tower 3 for a hydration reaction lasting approximately 30 minutes. The resulting hydrated oil is then pumped out by pump P2a and enters the degumming centrifuge 5, where the hydrated phospholipids combine with the process hot water to form a colloid and are separated from the oil, reducing the phospholipid content and improving the frying quality of the oil. The light phase degummed oil separated by the degumming centrifuge 5 has a moisture content of approximately 0.5%. It enters the degumming vacuum drying section 3c of the integrated combined degumming tower 3 for drying and dehydration. The dehydrated oil has a moisture content of approximately 0.05% and is then transported out of the degumming section via pump P6 and degummed oil outlet pipe G3.

[0097] The primary acidification reaction section 3a of the integrated combined degumming tower 3 is internally provided with a multi-stage jet mixer. The acidified oil in the primary acidification reaction section 3a is transported by the primary acidification oil circulation pump P3 and enters the jet mixers at each stage to achieve a sufficient mixing reaction of the acidified oil.

[0098] A multi-stage jet mixer is provided inside the hydration reaction section 3f. The hydrated oil discharged from the bottom of the hydration reaction section 3f is sent out by the hydration oil circulation pump P3a and enters the jet mixers at each stage to achieve a full mixing reaction of the hydrated oil.

[0099] In the integrated combined degumming tower 3, the water supply port of the soft water tank 3e is connected to the soft water supply pipe G7a, and the bottom outlet of the soft water tank 3e is connected to the inlet of the soft water pump P8. The outlet of the soft water pump P8 is connected to the water supply port of the hot water tank 3d and the clean water inlet of the degumming centrifuge 5 through the soft water supply pipe G7b, which is used to supply cold process water to the degumming section.

[0100] The bottom outlet of hot water tank 3d is connected to the inlet of hot water pump P7, which in turn is connected to process hot water pipe G6. After softened water is injected into hot water tank 3d, it is heated by steam to hot water. Hot water pump P7 then delivers the hot water via process hot water pipe G6 to the inlet of static water mixer 2a and the inlet of degumming centrifuge 5.

[0101] As shown in Figure 3, the third degumming stage in the present invention is the super degumming stage. Super degumming aims to completely remove the phospholipids from the oil. Typically, organic acids such as citric acid or inorganic acids such as phosphoric acid are added to the feedstock oil to convert non-hydratable phospholipids into easily removable hydrated phospholipids. This process also neutralizes the surface charge of the particles in the colloidal dispersed phase, causing them to aggregate and settle. It also frees metal ions such as calcium, magnesium, and iron bound to the phospholipids and transfers them to the aqueous phase, effectively removing impurities. After acidification and conditioning, the feedstock oil is then hydrated and degummed by adding a certain amount of alkali as a flocculant to further remove the phospholipids. Super degumming technology is one of the most important methods for completely removing colloids such as heavy phospholipids. Oils and fats after super degumming typically contain 5-20 ppm of phosphorus.

[0102] The unspecified parts are the same as the acidification degumming section, with the addition of a static water mixer 2a, a steam heater B 6 and a water cooler A 7.

[0103] The outlet of the primary acidified oil delivery pump P2 is connected to the hot side inlet of water cooler A7, the cold side inlet of water cooler A7 is connected to the cooling water pipe, the hot side outlet of water cooler A7 is connected to the main inlet of static water mixer 2a, and the water inlet of static water mixer 2a is connected to the process hot water pipe G6 and the alkali solution pipe G8.

[0104] The outlet of the hydrated oil delivery pump P2a is connected to the cold side inlet of the steam heater B 6, the hot side of the steam heater B 6 is connected to the steam pipe G4, and the cold side outlet of the steam heater B 6 is connected to the inlet of the degumming centrifuge.

[0105] The raw oil from the raw material pipeline G1 is transported by the raw oil pump P1 to the cold side of the steam heater A1, and heat exchanged with the steam on the hot side. The oil temperature rises from 30°C to 80°C-85°C, and then enters the static acid mixer A2 to be mixed with a certain proportion of acid, and enters the primary acidification reaction section 3a of the integrated combined degumming tower 3 for acidification reaction. The acidification reaction time is about 60 minutes; part of the non-hydratable phospholipids in the oil are converted into hydrated phospholipids. The acidified oil after the reaction is sent out by the primary acidification oil delivery pump P2 and enters the hot side of the water cooler A7, and heat exchanged with the circulating cooling water on the cold side. The oil temperature drops from 80°C to 40°C, which is conducive to the hydration and coagulation of phospholipids; after cooling, it enters the static water mixer 2a and is mixed with the phospholipids. A certain proportion of 85-90°C process hot water is mixed, and a small amount of alkali solution is added, the alkali solution addition ratio is about 1-3% of the oil weight, the alkali solution concentration is 1-2%, and the alkali solution temperature is 85-90°C; after mixing, it enters the hydration reaction section 3f of the integrated combined degumming tower 3 for hydration reaction, the reaction time is about 60 minutes, the hydrated oil after the reaction is sent out by the hydrated oil delivery pump P2a, enters the cold side of the steam heater B 6, and exchanges heat with the hot side steam, the oil temperature rises from 40°C to 80°C, which is conducive to the separation of oil and colloid; then enters the degumming centrifuge 5, the hydrated phospholipids combine with the process hot water to form a colloid and are separated from the oil, thereby reducing the phospholipid content in the oil and improving the frying quality of the oil. The light phase degummed oil separated by the degumming centrifuge 5 has a moisture content of about 0.5%. It enters the degumming vacuum drying section 3c of the integrated combined degumming tower 3 for drying and dehydration. The moisture content of the dehydrated dry oil is about 0.05%. It is transported out of the degumming section through the degumming drying oil delivery pump P6 and the degummed oil output pipe G3.

[0106] As shown in Figure 4, the fourth degumming section of the present invention is an enzymatic degumming section. Enzymatic degumming is a new degumming process, and commonly used enzymes include phospholipase PLA1, PLA2, and PLC. Among them, phospholipase PLA1 and phospholipase PLA2 can specifically hydrolyze the ester bond on the phospholipid glycerol Sn-1 or Sn-2, generating hydrophilic lysophospholipids and free fatty acids, thereby achieving the purpose of dephosphorylation. PLC mainly acts on the glycerophosphate bond at the C3 position of glycerophospholipids, and the hydrolysis products are diacylglycerol (DAG) and organic phosphates (phosphocholine, phosphoethanolamine, phosphoserine, and phosphoinositol, etc.), thereby achieving the purpose of dephosphorylation. The enzymatic degumming process has the advantages of mild operating conditions, thorough dephosphorylation (degummed oil phosphorus content ≤10ppm), low wastewater discharge, and high refined oil yield.

[0107] The enzymatic degumming section includes a steam heater A1, a static acid mixer A2, an integrated combined degumming tower 3, a static alkali mixer A4 and a degumming centrifuge 5. The integrated combined degumming tower 3 includes a primary acidification reaction section 3a, an enzyme reaction section 3b, a degumming vacuum drying section 3c, a hot water tank 3d and a soft water tank 3e stacked in sequence from top to bottom.

[0108] The outlet of the raw material pipeline G1 is connected to the inlet of the raw material oil pump P1, the outlet of the raw material oil pump P1 is connected to the cold side inlet of the steam heater A1, the hot side inlet of the steam heater A1 is connected to the steam pipe G4, the cold side outlet of the steam heater A1 is connected to the main inlet of the static acid mixer A2, the acid inlet of the static acid mixer A2 is connected to the acid pipe G2; the outlet of the static acid mixer A2 is connected to the top inlet of the primary acidification reaction section 3a at the top of the integrated combined degumming tower 3, the primary acidification reaction section 3a The bottom outlet is connected to the inlet of the primary acidified oil delivery pump P2, the outlet of the primary acidified oil delivery pump P2 is connected to the hot side inlet of the water cooler A7, the cold side inlet of the water cooler A7 is connected to the cooling water pipe, the hot side outlet of the water cooler A7 is connected to the main inlet of the static alkali mixer A4, the alkali liquid inlet of the static alkali mixer A4 is connected to the alkali liquid pipe G8, the outlet of the static alkali mixer A4 is connected to the inlet of the enzyme mixer 8, and the inlet of the enzyme mixer 8 is also connected to the enzyme preparation pipe G9 to add the enzyme preparation to the oil. The outlet of the enzyme mixer 8 is connected to the top inlet of the enzyme reaction section 3b in the integrated combined degumming tower 3, the outlet of the enzyme reaction section 3b is connected to the inlet of the enzyme reaction section oil outlet pump P4, the outlet of the enzyme reaction section oil outlet pump P4 is connected to the cold side inlet of steam heater B 6, the hot side of steam heater B 6 is connected to the steam pipe G4, the cold side outlet of steam heater B 6 is connected to the inlet of the degumming centrifuge 5, the light phase outlet of the degumming centrifuge 5 is connected to the upper inlet of the degumming vacuum drying section 3c in the integrated combined degumming tower 3, the top exhaust port of the degumming vacuum drying section 3c is connected to the degumming vacuum pipe G5, the lower outlet of the degumming vacuum drying section 3c is connected to the inlet of the degumming drying oil delivery pump P6, and the outlet of the degumming drying oil delivery pump P6 is connected to the degumming oil output pipe G3. At the same time, a hot water tank 3d and a soft water tank 3e are arranged in the lower section of the integrated combined degumming tower 3 to supply hot process water and soft water to the degumming section.

[0109] The raw oil from the raw material pipeline G1 is transported by the raw oil pump P1 to the cold side of the steam heater A1, where it undergoes heat exchange with the steam on the hot side, raising the oil temperature from 30°C to 80°C-85°C. It then enters the static acid mixer A2 and is mixed with a certain proportion of acid, typically 0.05-0.2% of the oil weight. It then enters the primary acidification reaction section 3a of the integrated combined degumming tower 3 for an acidification reaction, converting some of the non-hydratable phospholipids in the oil into hydrated phospholipids. The reaction time is 60 minutes. The acidified oil after the reaction is sent out through the primary acidified oil delivery pump P2 and enters the hot side of the water cooler A7, where it undergoes heat exchange with the circulating cooling water on the cold side, and the oil temperature drops from 80°C to 55-60°C, which is beneficial to the hydration and coagulation of phospholipids. After cooling, it enters the static alkali mixer A4 and is mixed with a certain proportion of alkali solution. The addition ratio of alkali solution is about 1-3% of the oil weight, the alkali solution concentration is 1-2%, and the alkali solution temperature is 85-90°C. The pH value of the oil is adjusted to 5-6 to create the best process conditions for enzyme-catalyzed hydrolysis. The oil and the enzyme preparation delivered from enzyme preparation pipe G9 then enter enzyme mixer 8 for mixing, with the enzyme preparation added at a ratio of 25-50 ppm. After mixing, the oil enters enzyme reaction section 3b of integrated combined degumming tower 3 for an enzyme reaction, completely converting the remaining non-hydratable phospholipids in the oil into hydrated phospholipids. The degummed oil is then delivered via enzyme reaction section oil outlet pump P4 to the cold side of steam heater B 6, where it undergoes heat exchange with the hot side steam, raising the oil temperature from 40°C to 80°C-85°C, facilitating the separation of the oil and colloid. The degummed oil then enters degumming centrifuge 5 to separate the colloid from the oil, thereby reducing the phospholipid content in the oil and improving its frying quality. The light phase degummed oil separated by degumming centrifuge 5 has a moisture content of approximately 0.5%. It enters degumming vacuum drying section 3c of integrated combined degumming tower 3 for drying and dehydration. The dehydrated oil has a moisture content of approximately 0.05% and is then transported out of the degumming section via degumming dry oil delivery pump P6 and degummed oil outlet pipe G3.

[0110] The primary acidification reaction section 3a of the integrated combined degumming tower 3 is internally provided with a multi-stage jet mixer. The acidified oil in the primary acidification reaction section 3a is transported by the primary acidification oil circulation pump P3 and enters the jet mixers at each stage to achieve a sufficient mixing reaction of the acidified oil.

[0111] A multi-stage jet mixer is provided inside the enzyme reaction section 3b. The degummed oil discharged from the bottom of the enzyme reaction section 3b is sent out through the enzyme reaction section circulation pump P5 and enters the jet mixers at each stage to achieve sufficient mixing reaction.

[0112] In the integrated combined degumming tower 3, the water supply port of the soft water tank 3e is connected to the soft water supply pipe G7a, and the bottom outlet of the soft water tank 3e is connected to the inlet of the soft water pump P8. The outlet of the soft water pump P8 is connected to the water supply port of the hot water tank 3d and the clean water inlet of the degumming centrifuge 5 through the soft water supply pipe G7b, which is used to supply cold process water to the degumming section.

[0113] The bottom outlet of hot water tank 3d is connected to the inlet of hot water pump P7, which in turn is connected to process hot water pipe G6. After softened water is injected into hot water tank 3d, it is heated by steam to hot water. Hot water pump P7 then delivers the hot water via process hot water pipe G6 to the alkali inlet of static alkali mixer 4 and the inlet of degumming centrifuge 5.

[0114] As shown in Figure 5, the alkali refining section of the present invention includes a steam heater C 9, a static acid mixer B 10, an integrated combined alkali refining tower 11, a static alkali mixer B 12, a steam heater D 13, a soap removal centrifuge 14, and a water washing centrifuge 15. The integrated combined alkali refining tower 11 is stacked with a water washing buffer section 11c, a secondary acidification reaction section 11a, and an alkali reaction section 11b from top to bottom.

[0115] The alkali refining process involves neutralizing the free fatty acids in crude oil with a caustic soda solution, forming sodium soap that precipitates in the oil. Centrifugation is then used to separate the soap from the oil, creating a deacidification process. Soapstock has a strong adsorption capacity, absorbing and removing proteins, mucus, pigments, and even mechanical impurities from the crude oil. The alkali solution also saponifies some of the phospholipids in the crude oil, forming a soapstock precipitate.

[0116] The outlet of the degummed oil output pipe G3 is connected to the cold side inlet of the steam heater C 9, the cold side outlet of the steam heater C 9 is connected to the inlet of the static acid mixer B 10, the acid inlet of the static acid mixer B 10 is connected to the acid pipe G2, the outlet of the static acid mixer B 10 is connected to the inlet of the secondary acidification reaction section 11a at the upper part of the integrated combined alkali refining tower 11, the outlet of the secondary acidification reaction section 11a is connected to the inlet of the secondary acidification oil delivery pump P9, the outlet of the secondary acidification oil delivery pump P9 is connected to the inlet of the static alkali mixer B 12, the alkali inlet of the static alkali mixer B 12 is connected to the alkali pipe G8, and the static alkali mixer B 12 is connected to the alkali pipe G8. The outlet of combiner B 12 is connected to the inlet of the alkali reaction section 11b in the upper part of the integrated combined alkali refining tower 11, the outlet of the alkali reaction section 11b is connected to the inlet of the neutralization oil delivery pump P11, the outlet of the neutralization oil delivery pump P11 is connected to the cold side inlet of the steam heater D 13, the cold side outlet of the steam heater D 13 is connected to the inlet of the soap removal centrifuge 14, the light phase soap removal oil outlet of the soap removal centrifuge 14 is connected to the inlet of the water washing buffer section 11c at the top of the alkali refining combined tower 3, the outlet of the water washing buffer section 11c is connected to the inlet of the water washing centrifuge 15, and the light phase water washing oil outlet of the water washing centrifuge 15 is connected to the water washing oil output pipe.

[0117] An alkali refining vacuum drying section 11d is provided below the alkali reaction section 11b of the integrated combined alkali refining tower 11. The outlet of the water-washing oil output pipe is connected to the inlet of the alkali refining vacuum drying section 11d. The top air exhaust port of the alkali refining vacuum drying section 11d is connected to the alkali refining vacuum pipe G10. The outlet of the alkali refining vacuum drying section 11d is connected to the inlet of the alkali refining drying oil delivery pump P14. The outlet of the alkali refining drying oil delivery pump P14 is connected to the alkali refining oil output pipe G11.

[0118] The degummed oil from the degummed oil output pipe G3 enters the cold side of the steam heater C1 and exchanges heat with the steam on the hot side of the steam heater C1, raising the oil temperature from 30°C to 80°C. The oil then enters the static acid mixer B10 and is mixed with a certain proportion of acid, the acid addition ratio of which is usually 0.05-0.2% of the oil weight. The oil then enters the secondary acidification reaction section 11a at the upper part of the integrated combined alkali refining tower 11 for acidification reaction, with a reaction time of 30-60 minutes. The acidified oil after the reaction is transported by the secondary acidification oil delivery pump P9 to the static alkali mixer B12 and mixed with a certain proportion of alkali solution, the alkali solution addition ratio of which is about 1-2% of the oil weight, the alkali solution concentration is 9-12%, and the alkali solution temperature is 85-90°C. The oil then enters the alkali reaction section 11b at the upper middle part of the integrated combined alkali refining tower 11 for acidification reaction. Alkali reaction, the neutralized oil after the reaction is transported by the neutralization oil delivery pump P11 to the cold side of the steam heater D 13, and heat exchanged with the hot side steam. The oil temperature rises from 80°C to 85°C, and then enters the desoaping centrifuge 14. The separated light phase desoaped oil enters the water washing buffer section 11c at the top of the integrated combined alkali refining tower 11 for water washing operation. The addition ratio of water for washing is about 2-5% of the oil weight, and the temperature is 85-90°C. A small amount of acid can also be added according to the situation; then enters the water washing centrifuge 15, and the separated light phase water washing oil has a moisture content of about 0.5%. It enters the alkali refining vacuum drying section 11d in the middle and lower part of the integrated combined alkali refining tower 11 for drying and dehydration. The moisture content of the dehydrated dry oil is about 0.05%, and it is transported out of the alkali refining section by the alkali refining drying oil delivery pump P14.

[0119] A multi-stage jet mixer is provided inside the secondary acidification reaction section 11a at the upper part of the integrated combined alkali refining tower 11. The acidified oil discharged from the bottom of the secondary acidification reaction section 11a is transported by the secondary acidification oil circulation pump P10 and enters the jet mixers at each stage in the secondary acidification reaction section 11a to achieve sufficient mixing reaction of the oil.

[0120] A multi-stage jet mixer is provided inside the alkali reaction section 11b. The hydrated oil discharged from the bottom of the alkali reaction section 11b is transported by the neutralization oil circulation pump P12 and enters the jet mixers at each stage in the alkali reaction section 11b to achieve a full mixing reaction of the neutralization oil.

[0121] The water washing buffer section 11c is internally provided with a multi-stage jet mixer. The water washing oil in the water washing buffer section 11c is transported by the water washing oil circulation pump P13 and enters the jet mixers at each stage in the water washing buffer section 11c to achieve a sufficient mixing reaction of the water washing oil.

[0122] As shown in Figure 6, the decolorization section in the present invention includes a steam heater 16, an integrated combined decolorization tower 17, a decolorization filter 18, a dust removal fan 19 and a gas-liquid separator 20. The integrated combined decolorization tower 17 is stacked with a pulse dust collector 17a, a decolorant temporary storage tank 17b, a metering rotary valve 17c, a decolorization reaction section 17d and an intermediate oil tank 17e from top to bottom. The upper part of the decolorization reaction section 17d is provided with a static mixing structure, and the lower part is provided with a steam stirring decolorization section or a jet stirring decolorization section.

[0123] The principle of the decolorization process is that under certain conditions, certain materials such as activated carbon, bentonite, attapulgite, etc. have a strong selective adsorption effect on pigments and other impurities. Using them to treat oils and fats can achieve the purpose of removing pigments, oxidation products, metal ions, residual soap, residual phosphorus, pesticide residues and polycyclic aromatic hydrocarbons, thereby achieving the purpose of purifying oils and fats.

[0124] The outlet of the decolorant delivery pipe G12 is connected to the inlet of the decolorant temporary storage tank 17b at the top of the integrated combined decolorization tower 17, the top outlet of the decolorant temporary storage tank 17b is connected to the pulse dust collector 17a, the top outlet of the pulse dust collector 17a is connected to the inlet of the dust removal fan 19, and the outlet of the dust removal fan 19 is connected to the atmosphere connecting pipe.

[0125] The bottom outlet of the decolorant temporary storage tank 17b is connected to the inlet of the metering and adding rotary valve 17c, and the lower end outlet of the metering and adding rotary valve 17c is connected to the inlet of the decolorization reaction section 17d.

[0126] The outlet of the alkali refining output pipe G11 is connected to the cold side inlet of the steam heater 16, the cold side outlet of the steam heater 16 is connected to the inlet of the decolorization reaction section 17d of the integrated combined decolorization tower 17, the outlet of the decolorization reaction section 17d is connected to the inlet of the filter feed pump P15, the outlet of the filter feed pump P15 is connected to the inlet of the decolorization filter 18, and the outlet of the decolorization filter 18 is connected to the decolorization oil output pipe G19.

[0127] Furthermore, the vacuum outlet of the decolorization reaction section 17d is connected to the inlet of the gas-liquid separator 20. The top outlet of the gas-liquid separator 20 is connected to the decolorization vacuum line G14, and the bottom outlet of the gas-liquid separator 20 is connected to the oil return line inlet of the decolorization reaction section 17d. Furthermore, an intermediate oil tank 17e is integrated at the bottom of the integrated combined decolorization tower 17 for collecting and reusing waste oil during the decolorization and filtration switching process.

[0128] The alkali-refined oil from the alkali-refining output pipe G11 enters the cold side of the steam heater E16, where it undergoes heat exchange with the steam on the hot side, raising the oil temperature from 90°C to 110°C. The oil then enters the decolorization reaction section 17d in the middle of the integrated combined bleaching tower 17. Under vacuum suction, the raw oil and the decolorant are thoroughly mixed in the static mixing structure at the top of the decolorization reaction section 17d. The decolorant is added in a ratio of 0.5-1.5% by weight of the oil. The static mixing structure at the top of the decolorization reaction section 17d is composed of multiple stages of static baffles to ensure thorough mixing of the oil and the decolorant. The mixture of oil and decolorant then enters the steam-agitation decolorization section of the decolorization reaction section 17d for decolorization. The injection pipe of the steam-agitation decolorization section is connected to the steam pipe G4.

[0129] The decolorized oil is pumped out via filter feed pump P15 and fed through filter feed pipe G13 to one of the decolorization filters 18 for filtration. The filtered oil is then transported to the next stage via decolorization oil output pipe G19. The two decolorization filters operate alternately to achieve continuous production.

[0130] As shown in Figure 7, the steam agitation bleaching section of decolorization reaction section 17d can be replaced with a jet agitation bleaching section. When using the jet agitation bleaching section, a portion of the bleached oil is transported by the bleached oil circulation pump P16 into the multi-stage jet agitation device within the decolorization reaction section 17d for circulated mixing and agitation, ensuring the bleaching process proceeds optimally.

[0131] The decolorant used in the decolorization operation is supplied from the decolorant delivery pipe G12 and, under negative pressure, is first temporarily stored in the decolorant storage tank 17b of the integrated combined decolorization tower 17. The dust-laden gas is then purified and dust-removed by the pulse dust collector 17a, and the clean air is then discharged into the atmosphere via the dust removal blower 19. The decolorant in the decolorant storage tank 17b is metered by a rotary metering valve 17c and continuously fed into the static mixing structure at the top of the decolorization reaction section 17d, where it is thoroughly mixed with the crude oil. The decolorization reaction section 17d operates under vacuum. After exiting the decolorization reaction section 17d, the extracted gas first enters the gas-liquid separator 20 for gas-liquid separation. The gaseous phase discharged from the top of the gas-liquid separator 20 enters the vacuum system via the decolorization vacuum pump G14. The oil droplets separated at the bottom of the gas-liquid separator 20 flow back to the decolorization reaction section 17d under the influence of gravity along the separator's oil return line.

[0132] When the decolorizing filter 18 is working, the decolorizing oil sent by the filter feeding pump P15 enters from the oil inlet of the decolorizing filter 18, and the oil inlet is connected to the side wall of the lower cone of the decolorizing filter 18, gradually filling the decolorizing filter 18 in use, and discharging the gas in the decolorizing filter 18, and extracting it out of the system through the decolorizing vacuum pipe G14 at the top of the intermediate oil tank 17e; until the upper outlet of the shell of the decolorizing filter 18 overflows to the intermediate oil tank 17e through the top flow return oil pipe G15, and the upper outlet of the shell of the decolorizing filter 18 is closed at this time.

[0133] Then the oil filtered by the filter element is discharged from the middle oil outlet of the decolorization filter 18, and returns to the decolorization reaction section 17d through the middle circulation pipe G16 for circulation. After running for a period of time, when a stable filter cake is attached to the outer periphery of the filter element of the decolorization filter 18 and the oil output from the middle oil outlet meets the requirements, the inlet valve of the middle circulation pipe G16 is closed, and the valve of the decolorization oil output pipe G19 is opened. The filtered clear oil is transported to the next section through the decolorization oil output pipe G19.

[0134] When the filter cake intercepted by the outer periphery of the filter element of the decolorizing filter 18 in use is thicker, the filtration pressure difference is larger due to the larger flow resistance. At this time, the spare decolorizing filter 18 is put into use to ensure the continuous operation of the system.

[0135] Open the steam valve at the upper outlet of the shell of the decolorizing filter 18 that is not in use, and use the steam pressure to press the dirty oil out from the middle oil outlet and oil inlet of the decolorizing filter 18, and return it to the intermediate oil tank 17e at the bottom of the integrated combined decolorizing tower 17 through the dirty oil collection pipe G17 for collection. Close the vacuum port on the top of the intermediate oil tank 17e, and the dirty oil in the intermediate oil tank 17e will flow back to the decolorizing reaction section 17d along the siphon return oil pipe G18 under the action of vacuum, and all of it will be recycled.

[0136] Oil deodorization is based on the significant difference in volatility between oils (triglycerides) and substances that affect the oil's flavor, odor, color, and stability. The specific deodorization method employed is physical distillation, which involves injecting steam directly into the oil under high vacuum and high temperature conditions. A high vacuum environment increases the vapor pressure difference between the oil and volatile impurities, while also preventing oxidation of the high-temperature oil and avoiding or minimizing oil hydrolysis. The high temperature of the oil not only increases the vapor pressure difference in the deodorization environment but also destroys pigments such as carotenoids, creating a thermal decolorization effect. The distillation process involves water vapor passing through a layer of high-temperature oil containing odorous components under high vacuum, creating sufficient gas-liquid surface contact. The odorous components in the oil volatilize into the water vapor bubbles and, at a ratio of their partial pressures, escape with the steam into the vacuum system and are discharged, thereby deodorizing the oil.

[0137] As shown in Figure 8, the deodorization section of the present invention includes an integrated combined deodorization tower 21, a falling film economizer 22, a falling film heater 23, and a water cooler B 24. The integrated combined deodorization tower 21 is equipped, from top to bottom, with a fatty acid collector 21a, a post-deacidification tower section 21b, a pre-deacidification tower section 21c, a plate stripping section 21d, and a gas separation chamber 21e. This first embodiment is a low-capacity integrated deodorization section. The diameter of the plate stripping section 21d is relatively small, so the falling film economizer 22 is external.

[0138] The outlet of the decolorized oil output pipe G19 is connected to the decolorized oil inlet of the lower gas analysis chamber 21e of the integrated combined deodorizing tower 21, the bottom oil outlet of the gas analysis chamber 21e is connected to the inlet of the gas analysis oil delivery pump P17, the outlet of the gas analysis oil delivery pump P17 is connected to the lower inlet of the cold side of the falling film economizer 22, the upper outlet of the cold side of the falling film economizer 22 is connected to the upper oil inlet of the pre-deacidification tower section 21c, the lower oil outlet of the pre-deacidification tower section 21c is connected to the upper oil inlet of the plate tower stripping section 21d, and each layer of the plate tower is respectively provided with an annular jet pipe or a stripping pump, and the steam inlet of the annular jet pipe or the stripping pump is respectively connected to the steam pipe G4.

[0139] The lower oil outlet of the plate tower stripping section 21d is connected to the inlet of the plate tower oil delivery pump P18, the outlet of the plate tower oil delivery pump P18 is connected to the oil inlet of the falling film heater 23, the oil outlet of the falling film heater 23 is connected to the upper oil inlet of the post-deacidification tower section 21b, the lower oil outlet of the post-deacidification tower section 21b is connected to the upper inlet of the hot side of the falling film economizer 22, the deodorized oil outlet at the bottom of the falling film economizer 22 is connected to the inlet of the deodorized oil delivery pump P19, and the outlet of the deodorized oil delivery pump P19 is connected to the deodorized oil outlet pipe G20.

[0140] In addition, the top gas phase outlet of the post-deacidification tower section 21b of the integrated combined deodorization tower 21 is connected to the bottom of the fatty acid trap 21a, and the top gas phase outlet of the fatty acid trap 21a is connected to the deodorization vacuum pipe G22, maintaining the negative pressure of the post-deacidification tower section 21b, the pre-deacidification tower section 21c, and the plate tower stripping section 21d in gas phase communication. The upper side wall of the gas analysis chamber 21e is independently connected to the deodorization vacuum pipe G22.

[0141] The fatty acid outlet of the fatty acid collector 21a is connected to the inlet of the fatty acid circulation pump P20. The outlet of the fatty acid circulation pump P20 has two pipelines. One is the circulation pipeline connected to the hot side inlet of the water cooler B 24, and the hot side outlet of the water cooler B 24 is connected to the fatty acid inlet on the upper part of the fatty acid collector 21a; the other is the fatty acid discharge pipe G21, which is connected to the fatty acid tank inlet of the auxiliary tank area.

[0142] The cold oil to be deodorized from the decolorized oil output pipe G19 enters the gas analysis chamber 21e, where the oxygen dissolved in the oil is removed under vacuum. The gasified cold oil is then sent out through the gas analysis oil delivery pump P17 and enters the cold side of the falling film economizer 22, where it undergoes heat exchange with the deodorized hot oil on the hot side and is heated to above 220°C. The gasified oil then enters the pre-deacidification tower section 21c.

[0143] In the pre-deacidification tower section 21c, part of the free fatty acids are distilled and removed under the deodorization vacuum, and then enter the plate tower stripping section 21d under the action of gravity for the final high-temperature stripping and thermal decolorization. The decolorized oil is then sent out through the plate tower oil delivery pump P18 and enters the falling film heater 23 for heating. The oil temperature rises to above 240°C, and then flows by gravity into the post-deacidification tower section 21b. In the post-deacidification tower section 21b, most of the free fatty acids and trace odor components are removed. The deodorized oil then flows by gravity into the hot side of the falling film economizer 22, and exchanges heat with the degassing cold oil on the cold side. The deodorized oil then enters the deodorized oil delivery pump P19 and is output through the deodorized oil outlet pipe G20.

[0144] The gases produced during the deodorization process of the post-deacidification tower section 21b, pre-deacidification tower section 21c, and plate tower stripping section 21d enter the fatty acid trap 21a at the top of the integrated combined deodorization tower 21. The fatty acid trap 21a, fatty acid circulation pump P20, and water cooler B 24 form a fatty acid capture system. The fatty acid circulation pump P20 sends the oil collected at the bottom of the fatty acid trap 21a to the hot side of water cooler B 24 for cooling, and then sends it to the top of the fatty acid trap 21a for circulation spraying, fully capturing the fatty acid gas distilled from the deodorization section. When the total amount of fatty acids in the capture system reaches the set value, some of the fatty acids are sent to the fatty acid tank outside the workshop for storage through the fatty acid discharge pipe G21.

[0145] FIG9 shows a second embodiment of a large-capacity deodorization section. The rest is the same as the first embodiment. Since the diameter of the central vacuum cylinder of the plate tower stripping section 21d is very large, the falling film economizer 22 is built into the central vacuum cylinder of the plate tower stripping section 21d, and the outer insulation layer of the falling film economizer 22 is eliminated.

[0146] As shown in Figure 10, the upper end of the plate tower stripping section cylinder is open, and the lower end of the plate tower stripping section cylinder is sealed with a plate tower stripping section lower head. A partition bottom plate is welded to the lower portion of the plate tower stripping section cavity. The partition bottom plate, the plate tower stripping section lower head, and the plate tower stripping section cylinder together form a gas analysis chamber 21e. A decolorization oil spray pipe 21e2 is provided at the top of the gas analysis chamber 21e. A decolorization oil inlet 21e1 is provided on the upper sidewall of the gas analysis chamber 21e, which is connected to the decolorization oil spray pipe 21e2. A pre-degassing vacuum port 21e3 is also provided on the upper sidewall of the gas analysis chamber 21e, and a gas analysis chamber oil outlet 21e4 is provided at the bottom of the plate tower stripping section lower head.

[0147] The decolorized oil from the previous process enters the gas analysis chamber 21e from the decolorized oil inlet 21e1, and is sprayed out through the decolorized oil spray pipe 21e2 and various nozzles. The entrained air overflows and is extracted and removed from the pre-degassing vacuum port 21e3 to avoid subsequent high-temperature oxidation of the decolorized oil.

[0148] A central air pump is provided upward from the central hole of the compartment bottom plate along the axis of the plate tower stripping section cylinder. The central air pump extends upward to the middle and upper part of the plate tower stripping section cylinder.

[0149] The falling film economizer 22 is located in the inner cavity of the central vacuum cylinder. A plurality of falling film tubes 22f are evenly arranged in the inner cavity of the shell. Each falling film tube 22f runs through the upper tube plate 22e and the lower tube plate. The upper tube mouth of the falling film tube 22f extends from the upper tube plate 22e and is evenly distributed with overflow grooves.

[0150] As shown in Figure 11, the falling film economizer oil inlet pipe is connected to the central sidewall of the plate tower stripping section. The inner end of the falling film economizer oil inlet pipe extends to the axis of the plate tower stripping section, and the outlet end bends downward toward the center of the oil distribution pan 22b. The inner end of the falling film economizer oil inlet pipe is equipped with an oil dispersing tube 22a to facilitate uniform overflow into the oil distribution pan 22b. The oil distribution pan 22b is fixed to the upper tube sheet 22e of the falling film economizer 22 via support bolts 22d and is parallel to the oil distribution pan 22b. The oil distribution pan 22b is evenly distributed with multiple oil distribution holes and evenly distributed with air vents 22c that penetrate the oil layer. The gas phase released from the falling film can enter the central exhaust cylinder above through the air vents 22c.

[0151] As shown in Figure 12, the projections of the oil distribution holes are symmetrically distributed in the shape of a right triangle around the upper tube openings of each falling film tube 22f. The deodorized oil is evenly distributed into the oil distribution pan 22b through the oil inlet pipe of the falling film economizer and the oil dispersion tube 22a. The oil distribution holes are narrow at the top and wide at the bottom to avoid blockage. The oil distribution holes evenly distribute oil to the periphery of the falling film tube 22f, enter the inner wall of the falling film tube 22f from the overflow tooth groove, and flow downward to form a falling film.

[0152] The lower end of the shell of the falling film economizer 22 passes through the gas analysis chamber 21e and the lower head of the plate tower stripping section. The lower tube plate reaches the outside of the lower head of the plate tower stripping section and is connected to a deodorized oil buffer tank 22j below. The deodorized oil buffer tank 22j is located in the inner cavity of the skirt seat, and a deodorized oil outlet 22k is provided at the bottom of the deodorized oil buffer tank 22j.

[0153] The lower part of the shell of the falling film economizer 22 is provided with a shell-side lower inlet 22g, which is connected to the decolorized oil output pipe G19; the upper part of the shell of the falling film economizer 22 is provided with a shell-side upper outlet 22h, which is connected to the oil inlet of the pre-deacidification tower section 21c.

[0154] The pre-degassed decolorized oil flows out of the gasification chamber oil outlet 21e4 in the lower head of the plate tower stripping section and is delivered by the gasification oil delivery pump P17 to the lower shell-side inlet 22g in the lower portion of the falling film economizer housing. It then flows upward along the shell side of the falling film economizer 22, exchanging heat in countercurrent with the deodorized oil film on the tube side. After its temperature drops, the deodorized oil enters the deodorized oil buffer tank 22j for temporary storage before flowing out of the deodorized oil outlet 22k at the bottom of the deodorized oil buffer tank 22j. After this heat exchange, the decolorized oil is preheated and flows out of the upper shell-side outlet 22h in the upper portion of the falling film economizer housing. This upper shell-side outlet 22h is equipped with an expansion joint and extends radially out of the plate tower stripping section.

[0155] The annular space between the central vacuum pump and the plate tower stripping section is equipped with multiple trays, each of which houses a stripping pump 21d4. Above the compartment floor, an annular plate tower stripping section air duct 21d5 is located. The sidewall of the plate tower stripping section is equipped with a plate tower oil outlet. The annular plate tower stripping section air duct 21d5 and the steam inlets of each stripping pump 21d4 are connected to a steam pipe.

[0156] Typically, the tower trays are five layers high. The top of the falling film economizer 22 is flush with the top of the third tray. The central exhaust cylinders in the centers of the upper two trays are disconnected from the lower parts. The upper central exhaust cylinder is slightly smaller, while the lower central exhaust cylinder has a larger inner diameter to accommodate the falling film economizer 22. An annular gas phase passage is reserved around the outer periphery of the falling film economizer 22. The gas phase space of each tray communicates with the inner cavity of the central exhaust cylinder through vents. The vents on each layer are evenly distributed around the circumference of the central exhaust cylinder and are located below the upper tray.

[0157] Each tower plate is provided with a partitioned inner cylinder 21d1 coaxial with the plate tower stripping section cylinder, the inner side of the partitioned inner cylinder 21d1 is the inner ring flow channel, and the outer side of the partitioned inner cylinder 21d1 is the outer ring flow channel; a radial partition 21d2 is provided between the outer wall of the central vacuum cylinder and the inner wall of the plate tower stripping section cylinder, the outlet of the upper tower plate overflow pipe 21d3 points to the head end of the inner ring flow channel close to the radial partition 21d2, the tail end of the partitioned inner cylinder 21d1 close to the other side of the radial partition 21d2 is provided with a notch connected to the head end of the outer ring flow channel, and the tail end of the outer ring flow channel is provided with a tower plate overflow pipe 21d3 for overflowing to the inner ring flow channel of the next layer.

[0158] In Figures 10 and 13, each outer ring flow channel overflows to the inner ring flow channel of the next layer through the tower plate overflow pipe 21d3. The outer ring flow channel of a certain layer overflows to the inner ring flow channel of the next layer, circulates once and enters the outer ring flow channel from the gap, and then overflows to the inner ring flow channel of the next layer. The head end and tail end of each layer remain unchanged.

[0159] The overflow pipes 21d3 of the tower plates of the outer ring flow channel and the inner ring flow channel can also be vertically downward. The first layer of tower plates enters the outer ring flow channel from the gap of the inner ring flow channel, overflows from the outer ring flow channel to the outer ring flow channel of the second layer, enters the inner ring flow channel of this layer at the gap, and then overflows to the inner ring flow channel of the third layer, and enters the outer ring flow channel from the gap of the inner ring flow channel. In this way, the head end and the tail end of each layer alternate in sequence.

[0160] Each inner ring flow channel can also overflow to the outer ring flow channel of the next layer through the tower plate overflow pipe 21d3, and the inner ring flow channel of a certain layer overflows to the outer ring flow channel of the next layer. After a circle of circulation, it enters the inner ring flow channel from the gap and then overflows to the outer ring flow channel of the next layer. The head and tail ends of each layer remain unchanged.

[0161] Multiple groups of stripping pumps 21d4 are installed along the inner and outer ring flow channels, which greatly extends the flow length of the oil on each layer of the tower plate and also extends the residence time, ensuring the first-in-first-out of the oil and avoiding local stagnation of the oil, which affects the quality.

[0162] Each tray is tilted, with the outer tray higher and the inner tray lower. A tray drain pipe is connected to the lowest point of each tray. Each tray drain pipe extends beyond the stripping section of the plate tower and connects to the lower tray's reflux port via a drain valve. The tray reflux port is located below the liquid level in the outer annular flow channel. Because the overflow height of the tray overflow pipe 21d3 cannot be adjusted, the liquid level on each tray is fixed. Under certain process conditions, if the liquid level on the tray is desired to be adjusted, the drain valve can be opened to allow the oil in the upper layer to drain through the tray drain pipe to the next layer.

[0163] A reduced diameter section is provided at the lower part of the central vacuum cylinder, and the upper end of the reduced diameter section is located below the air vent on the bottom layer. The bottom plate of the compartment plays a role similar to a tower plate. Since the liquid level of the upper several layers of tower plates is stable, a stripping pump 21d4 with higher liquid level requirements is set for stripping.

[0164] The bottom compartment floor uses the plate tower stripping section annular jet pipe 21d5 for the final stripping stage, making it easy to adjust the liquid level of this layer. This layer is equipped with a reduced diameter section of the pump to expand the oil storage capacity above the bottom compartment floor and better play a buffering role.

[0165] A liquid seal disc is installed at the lower end of the reduced diameter section of the pump. Condensate from the central pump's gas phase flows directly into the disc under gravity, overflowing downward to form a liquid seal with the gas phase space in the gas separation chamber 21e. The disc is equipped with drainage holes. During normal operation, condensate overflows from the upper end of the disc. When the vehicle is stopped, the drainage holes slowly drain the disc.

[0166] The gaseous material stripped from the bottom plate of each layer of tower tray, including the bottom compartment plate, enters the annular space between the falling film economizer shell and the central vacuum cylinder from the vents on the upper part of each layer, and then moves upward from the edge of the liquid retaining cover of the stripping section of the plate tower.

[0167] The above description is only a preferred embodiment of the present invention, which shows and describes the basic principles, main features and advantages of the present invention, but does not limit the scope of patent protection of the present invention. Those skilled in the art should understand that the present invention is not limited by the above embodiments. In addition to the above embodiments, the present invention may have other implementation modes without departing from the spirit and scope of the present invention. The present invention may also have various changes and improvements, and all technical solutions formed by equivalent replacement or equivalent transformation fall within the scope of protection required by the present invention. The scope of protection required by the present invention is defined by the attached claims and their equivalents. Technical features not described in the present invention can be achieved by or using existing technologies, and will not be described here.

Claims

1. An integrated vegetable oil refining system, comprising a degumming section and an alkali refining section, characterized in that: The alkali refining section comprises an integrated combined alkali refining tower, which is stacked with a water washing buffer section, a secondary acidification reaction section and an alkali reaction section in sequence from top to bottom. The outlet of the degumming oil output pipe is connected to the cold side inlet of the steam heater C, the cold side outlet of the steam heater C is connected to the main inlet of the static acid mixer B, the outlet of the static acid mixer B is connected to the top inlet of the secondary acidification reaction section, the bottom outlet of the secondary acidification reaction section is connected to the main inlet of the static alkali mixer B through a secondary acidification oil delivery pump, the outlet of the static alkali mixer B is connected to the upper inlet of the alkali reaction section, the bottom outlet of the alkali reaction section is connected to the cold side inlet of the steam heater D through a neutralization oil delivery pump, the cold side outlet of the steam heater D is connected to the inlet of a desoaping centrifuge, the light phase desoaping oil outlet of the desoaping centrifuge is connected to the upper end inlet of the water washing buffer section, the bottom outlet of the water washing buffer section is connected to the inlet of the water washing centrifuge, and the light phase water washing oil outlet of the water washing centrifuge is connected to the water washing oil output pipe.

2. The vegetable oil integrated refining system according to claim 1, characterized in that: The degumming section is a hydration degumming section, and the hydration degumming section includes an integrated combined degumming tower, and the integrated combined degumming tower is stacked with a hydration reaction section, a degumming vacuum drying section, a hot water tank and a soft water tank in sequence from top to bottom, the outlet of the raw oil pump is connected to the cold side inlet of the steam heater A, the cold side outlet of the steam heater A is connected to the main inlet of the static water mixer, the water inlet of the static water mixer is connected to the outlet of the process hot water pipe, the outlet of the static water mixer is connected to the upper end inlet of the hydration reaction section in the integrated combined degumming tower, the lower end outlet of the hydration reaction section is connected to the inlet of the degumming centrifuge through a hydration oil delivery pump, the light phase outlet of the degumming centrifuge is connected to the upper end inlet of the degumming vacuum drying section, the exhaust port of the degumming vacuum drying section is connected to the degumming vacuum pipe, and the bottom outlet of the degumming vacuum drying section is connected to the degumming oil output pipe through a degumming drying oil delivery pump; the outlet of the hot water tank is connected to the inlet of the process hot water pipe through a hot water pump.

3. The vegetable oil integrated refining system according to claim 1, characterized in that: The degumming section is an acidification degumming section, and the acidification degumming section includes an integrated combined degumming tower, and the integrated combined degumming tower is stacked with a primary acidification reaction section, a hydration reaction section and a degumming vacuum drying section in sequence from top to bottom. The outlet of the crude oil pump is connected to the cold side inlet of the steam heater A, and the cold side outlet of the steam heater A is connected to the main inlet of the static acid mixer A, and the acid inlet of the static acid mixer A is connected to the acid liquid pipe; the outlet of the static acid mixer A is connected to the top inlet of the primary acidification reaction section, and the bottom outlet of the primary acidification reaction section is connected to the primary acidification oil pump through the primary acidification oil pump. The delivery pump is connected to the main inlet of the static water mixer, the water inlet of the static water mixer is connected to the outlet of the process hot water pipe, the outlet of the static water mixer is connected to the upper inlet of the hydration reaction section in the integrated combined degumming tower, the lower outlet of the hydration reaction section is connected to the inlet of the degumming centrifuge through a hydration oil delivery pump, the light phase outlet of the degumming centrifuge is connected to the upper inlet of the degumming vacuum drying section, the exhaust port of the degumming vacuum drying section is connected to the degumming vacuum pipe, and the bottom outlet of the degumming vacuum drying section is connected to the degumming oil output pipe through a degumming drying oil delivery pump.

4. The vegetable oil integrated refining system according to claim 3, characterized in that: The outlet of the primary acidified oil delivery pump is connected to the hot side inlet of water cooler A, the hot side outlet of water cooler A is connected to the main inlet of the static water mixer, and the water inlet of the static water mixer is also connected to the alkali solution pipe; the outlet of the hydrated oil delivery pump is connected to the cold side inlet of steam heater B, and the cold side outlet of steam heater B is connected to the inlet of the degumming centrifuge.

5. The vegetable oil integrated refining system according to claim 1, characterized in that: The degumming section is an enzymatic degumming section, and the enzymatic degumming section includes an integrated combined degumming tower, and the integrated combined degumming tower is stacked with a primary acidification reaction section, an enzyme reaction section and a vacuum drying section in sequence from top to bottom, the outlet of the raw oil pump is connected to the cold side inlet of the steam heater A, the cold side outlet of the steam heater A is connected to the main inlet of the static acid mixer A, the acid inlet of the static acid mixer A is connected to the acid liquid pipe, the outlet of the static acid mixer A is connected to the top inlet of the primary acidification reaction section, the bottom outlet of the primary acidification reaction section is connected to the hot side inlet of the water cooler A through the primary acidification oil delivery pump, and the hot side outlet of the water cooler A is connected to the static alkali mixer A. The main inlet of the static alkali mixer A is connected, the alkali liquid inlet of the static alkali mixer A is connected to the alkali liquid pipe, the outlet of the static alkali mixer A and the outlet of the enzyme preparation pipe are commonly connected to the inlet of the enzyme mixer, the outlet of the enzyme mixer is connected to the upper inlet of the enzyme reaction section, the lower outlet of the enzyme reaction section is connected to the cold side inlet of the steam heater B through the enzyme reaction section oil outlet pump, the cold side outlet of the steam heater B is connected to the inlet of the degumming centrifuge, the light phase outlet of the degumming centrifuge is connected to the upper inlet of the vacuum drying section, the exhaust port of the vacuum drying section is connected to the degumming vacuum pipe, and the bottom outlet of the vacuum drying section is connected to the degumming oil output pipe through the degumming drying oil delivery pump.

6. The vegetable oil integrated refining system according to any one of claims 2 to 5, characterized in that: A soft water tank is also provided below the hot water tank, the outlet of the soft water tank is connected to the inlet of a soft water pump, and the outlet of the soft water pump is connected to the water replenishment port of the hot water tank and the flushing port of the degumming centrifuge through a soft water pipeline.

7. The vegetable oil integrated refining system according to claim 1, characterized in that: A decolorization section is provided downstream of the alkali refining section, and the decolorization section includes an integrated combined decolorization tower, and the integrated combined decolorization tower is stacked with a pulse dust collector, a decolorant temporary storage tank and a decolorization reaction section in sequence from top to bottom, and the decolorization reaction section includes a static mixing structure located at the top and a stirring decolorization section located at the bottom; The inlet of the decolorant temporary storage tank is connected to the outlet of the decolorant delivery pipe, the top outlet of the decolorant temporary storage tank is connected to the inlet of the pulse dust collector, and the top outlet of the pulse dust collector is connected to the atmosphere through a dust removal fan; The bottom outlet of the decolorant temporary storage tank is connected to the decolorant inlet of the static mixing structure through a metering addition rotary valve; the outlet of the alkali refining output pipe is connected to the cold side inlet of the steam heater E, and the cold side outlet of the steam heater E is connected to the oil inlet of the static mixing structure; the bottom outlet of the stirring and decolorizing section is connected to the oil inlet of the decolorizing filter through a filtering feeding pump, and the middle oil outlet of the decolorizing filter is connected to the decolorizing oil output pipe.

8. The vegetable oil integrated refining system according to claim 7, characterized in that: An intermediate oil tank is provided at the bottom of the integrated combined decolorization tower, and at least two decolorization filters are provided in parallel. The oil inlet and the intermediate oil outlet of each decolorization filter are respectively connected to the dirty oil collection pipe through a valve, and the outlet of the dirty oil collection pipe is connected to the upper inlet of the intermediate oil tank. The bottom outlet of the intermediate oil tank is connected to the upper oil return port of the stirring decolorization section through a siphon oil return pipe.

9. The vegetable oil integrated refining system according to claim 7, characterized in that: The stirring and decolorizing section is a steam stirring and decolorizing section or a jet stirring and decolorizing section.

10. The vegetable oil integrated refining system according to claim 7, characterized in that: The upper side wall suction port of the stirring and bleaching section is connected to the inlet of the gas-liquid separator, the top outlet of the gas-liquid separator is connected to the decolorization vacuum pipe, and the bottom outlet of the gas-liquid separator is connected to the upper oil return port of the stirring and bleaching section.

11. The vegetable oil integrated refining system according to claim 8, characterized in that: The upper shell outlet of each decolorizing filter is connected to the top flow oil return pipe through a valve, the outlet of the top flow oil return pipe is connected to the upper inlet of the intermediate oil tank, and the top exhaust port of the intermediate oil tank is connected to the decolorizing vacuum pipe.

12. The vegetable oil integrated refining system according to claim 7, characterized in that: A deodorizing section is provided downstream of the decolorizing section, and the deodorizing section includes an integrated combined deodorizing tower, and the integrated combined deodorizing tower is stacked with a fatty acid collector, a post-deacidifying tower section, a pre-deacidifying tower section and a plate tower stripping section in sequence from top to bottom, the decolorizing oil output pipe is connected to the upper inlet of the gas analysis chamber, the bottom outlet of the gas analysis chamber is connected to the lower inlet of the shell side of the falling film economizer through a gas analysis oil delivery pump, the upper shell side outlet of the falling film economizer is connected to the oil inlet of the pre-deacidifying tower section, the bottom of the pre-deacidifying tower section is connected to the upper part of the plate tower stripping section The bottom oil outlet of the plate tower stripping section is connected to the cold side inlet of the falling film heater through the plate tower oil outlet delivery pump, the cold side outlet of the falling film heater is connected to the upper oil inlet of the post-acidification tower section, the lower oil outlet of the post-acidification tower section is connected to the hot side inlet of the falling film economizer, and the hot side outlet of the falling film economizer is connected to the inlet of the deodorized oil delivery pump; the top gas phase port of the post-acidification tower section is connected to the bottom of the fatty acid trap, and the top exhaust port of the fatty acid trap is connected to the deodorization vacuum pipe.

13. The vegetable oil integrated refining system according to claim 12, characterized in that: The bottom liquid outlet of the fatty acid trap is connected to the inlet of a fatty acid circulation pump, the outlet of the fatty acid circulation pump is respectively connected to a fatty acid discharge pipe and a hot side inlet of water cooler B, and the hot side outlet of water cooler B is connected to a top spray port of the fatty acid trap.

14. The vegetable oil integrated refining system according to claim 12, characterized in that: The falling film economizer is built into the central vacuum cylinder of the plate tower stripping section. The annular space between the central vacuum cylinder and the plate tower stripping section cylinder is provided with multiple layers of tower plates, and each layer of the tower plates is provided with a stripping pump. Ventilation holes are evenly distributed on the circumference of the central vacuum cylinder to communicate the gas phase space of the tower plates with the inner cavity of the central vacuum cylinder. The inner cavity of the shell of the falling film economizer is provided with falling film tubes, which run through the upper tube plate and the lower tube plate, and an oil distribution pan is provided above the upper tube plate; the lower end of the shell of the falling film economizer passes through the lower head of the plate tower stripping section and a deodorized oil buffer tank is connected below the lower tube plate, and a deodorized oil outlet is provided at the bottom of the deodorized oil buffer tank.

15. The vegetable oil integrated refining system according to claim 14, characterized in that: Each of the tower plates is provided with a partitioned inner cylinder coaxial with the cylinder of the plate tower stripping section, the inner side of the partitioned inner cylinder is the inner ring flow channel, and the outer side of the partitioned inner cylinder is the outer ring flow channel; a radial partition is provided between the outer wall of the central vacuum cylinder and the inner wall of the cylinder of the plate tower stripping section; the outlet of the overflow pipe of the upper tower plate turns to point to the head end of the inner ring flow channel close to the radial partition side, and the tail end of the partitioned inner cylinder close to the other side of the radial partition is provided with a notch connected to the head end of the outer ring flow channel.

16. The vegetable oil integrated refining system according to claim 15, characterized in that: The tail end of the outer ring flow channel is provided with a tower plate overflow pipe for overflowing to the head end of the next inner ring flow channel; or the head end of the inner ring flow channel is provided with a tower plate overflow pipe for overflowing to the tail end of the next outer ring flow channel; or the tail end of the outer ring flow channel is provided with a tower plate overflow pipe for overflowing to the tail end of the next outer ring flow channel, and the head end of the inner ring flow channel is provided with a tower plate overflow pipe for overflowing to the head end of the next inner ring flow channel.

17. The vegetable oil integrated refining system according to claim 14, characterized in that: Each of the tower plates is tilted so as to be higher on the outside and lower on the inside, and a tower plate drain pipe is connected to the lowest point of the tower plate. The tower plate drain pipe of each layer extends to the outside of the cylinder of the plate tower stripping section and is connected to the tower plate reflux port of the lower layer through a drain valve. The tower plate reflux port is located below the liquid level of the outer ring flow channel.

18. The vegetable oil integrated refining system according to claim 14, characterized in that: A reduced diameter section is provided at the lower part of the central vacuum cylinder, the upper end of which is located below the vent hole of the bottom layer, and a liquid sealing disk is provided at the lower end of the reduced diameter section of the vacuum cylinder, on which a drainage hole is provided.

19. The vegetable oil integrated refining system according to claim 14, characterized in that: An oil dispersing cylinder for evenly overflowing toward the oil distribution pan is provided below the inner end of the oil inlet pipe of the falling film economizer. The oil distribution pan is fixed on the upper tube plate of the falling film economizer by supporting bolts. The oil distribution pan is evenly distributed with a plurality of oil distribution holes which are narrow on the top and wide on the bottom. The projections of the oil distribution holes are symmetrically distributed around the upper tube openings of each falling film tube array in the form of an equilateral triangle; the oil distribution pan is evenly distributed with air permeable pipes passing through the oil layer.

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