A complete set of equipment for producing zero trans fatty acid oil

Abstract

The utility model belongs to the technical field of grease processing equipment, concretely relates to a zero trans - fatty acid grease production complete equipment, including raw material oil pretreatment unit, core reaction unit, separation and purification unit and the nitrogen supply unit for providing nitrogen for core reaction unit, raw material oil pretreatment unit includes spiral plate heat exchanger, vacuum dryer and molecular sieve adsorption tower, core reaction unit includes fixed bed enzyme reactor and hydrogenation reaction tower, and fixed bed enzyme reactor and hydrogenation reaction tower all are connected with nitrogen supply unit pipeline, and separation and purification unit includes wiped film evaporator and multistage crystallization separation component. The utility model reconstructs the molecular structure of raw material oil through fixed bed enzyme reactor, makes the reconstructed grease carry out low -temperature low -pressure hydrogenation reaction through hydrogenation reaction tower, eliminates the environmental condition formed by trans - fatty acid, recycles heat energy, reduces production cost, carries out multistage crystallization and accurate separation to different melting point components in material, and obtains zero trans - fatty acid grease.

Description

Technical Field

[0001] This utility model belongs to the technical field of oil processing equipment, specifically relating to a complete set of equipment for producing oils with zero trans fatty acids. Background Technology

[0002] Traditional oil hydrogenation processes use nickel catalysts and high temperatures (>180°C), producing large amounts of trans fatty acids (TFA). TFA has been listed as a harmful substance by the World Health Organization (WHO) and is prone to causing cardiovascular diseases. Therefore, it is essential to produce oils with zero trans fatty acids.

[0003] However, existing zero-trans-fat fatty acid oil production processes have the following drawbacks:

[0004] (1) Production by enzymatic transesterification: low reaction efficiency, high cost, and difficulty in large-scale production;

[0005] (2) The process of full hydrogenation and fractionation is long, energy consumption is high, and the product melting point is not ideal.

[0006] (3) Limitations of existing production equipment: lack of integrated system, unable to simultaneously meet TFA control, continuous production and cost optimization.

[0007] Therefore, it is necessary to provide an integrated, scalable, and continuous production line for zero-trans fatty acid oils that can separate oil components with different melting points. Utility Model Content

[0008] The purpose of this invention is to overcome the shortcomings of the existing technology and provide a complete set of equipment for producing zero trans fatty acid oils.

[0009] To achieve the above objectives, the technical solution adopted by this utility model is: a complete set of equipment for producing zero trans fatty acid oils, including a raw material oil pretreatment unit, a core reaction unit, a separation and purification unit, and a nitrogen supply unit for providing nitrogen to the core reaction unit;

[0010] The feedstock oil pretreatment unit includes a spiral plate heat exchanger, a vacuum dryer, and a molecular sieve adsorption tower. The feedstock oil is introduced into one of the spiral channels of the spiral plate heat exchanger, and its outlet is connected to the feed inlet pipe of the vacuum dryer. The outlet of the vacuum dryer is connected to the feed inlet pipe of the molecular sieve adsorption tower.

[0011] The core reaction unit includes a fixed-bed enzyme reactor and a hydrogenation reaction tower. Both the fixed-bed enzyme reactor and the hydrogenation reaction tower are connected to the nitrogen supply unit pipeline. The feed inlet of the fixed-bed enzyme reactor is connected to the discharge outlet pipeline of the molecular sieve adsorption tower, and the feed inlet of the hydrogenation reaction tower is connected to the discharge outlet pipeline of the fixed-bed enzyme reactor.

[0012] The separation and purification unit includes a scraped film evaporator and a multi-stage crystallization and fractionation assembly. The inlet of the scraped film evaporator is connected to the outlet pipe of the hydrogenation reaction tower. The inlet end of the other spiral channel of the spiral plate heat exchanger is connected to the outlet pipe of the scraped film evaporator, and its outlet end is connected to the pipe of the multi-stage crystallization and fractionation assembly.

[0013] Furthermore, the nitrogen supply unit includes a nitrogen generator and a nitrogen storage tank. The inlet of the nitrogen generator is connected to air, and the outlet of the nitrogen generator is connected to the inlet pipe of the nitrogen storage tank. The fixed-bed enzyme reactor and the hydrogenation reaction tower are both connected to the outlet pipe of the nitrogen storage tank.

[0014] Furthermore, the multi-stage crystallization and fractionation assembly includes a first crystallization tank, a first plate and frame filter, a second crystallization tank, a second plate and frame filter, a third crystallization tank, and a disc centrifuge;

[0015] The inlet of the first crystallizer is connected to the outlet pipe of the spiral channel of the spiral plate heat exchanger, and the outlet of the first crystallizer is connected to the inlet pipe of the first plate and frame filter.

[0016] The inlet of the second crystallizer is connected to the outlet pipe of the first plate and frame filter, and the outlet of the second crystallizer is connected to the inlet pipe of the second plate and frame filter.

[0017] The inlet of the third crystallizer is connected to the outlet pipe of the second plate and frame filter, and the outlet of the third crystallizer is connected to the inlet pipe of the disc centrifuge.

[0018] Furthermore, a first cooling coil is installed on the inner wall of the first crystallization tank.

[0019] Furthermore, a second cooling coil is installed on the inner wall of the second crystallizer.

[0020] Furthermore, a third cooling coil is installed on the inner wall of the third crystallization tank.

[0021] Furthermore, stirring components are installed in the first crystallization tank, the second crystallization tank, and the third crystallization tank.

[0022] Compared with the prior art, the beneficial effects of this utility model are:

[0023] 1. This invention removes water and free fatty acids from the raw oil through a raw oil pretreatment unit, reconstructs the molecular structure of the raw oil through a core reaction unit, and hydrogenates the reconstructed oil to change the molecular structure of the oil and obtain the target product. A nitrogen supply unit provides nitrogen protection to the core reaction unit to prevent side reactions. The core reaction unit utilizes a fixed-bed enzyme reactor for enzymatic pre-structuring combined with a low-temperature and low-pressure hydrogenation reaction in a hydrogenation tower to completely avoid the formation pathway of trans fatty acids. A separation and purification unit deeply removes free fatty acids and volatile substances to avoid the regeneration of trans fatty acids during processing. Multi-level gradient crystallization and separation of components with different melting points in the material are performed to finally obtain a zero-trans fatty acid oil product.

[0024] 2. In this invention, the material discharged from the scraped film evaporator outlet enters one spiral channel of the spiral plate heat exchanger. This not only utilizes the waste heat of the material to preheat the raw material oil in the other spiral channel, but also cools the material. The cooled material then enters the multi-stage crystallization and separation component for separation and purification, enabling the recovery and reuse of heat energy and reducing production costs. Attached Figure Description

[0025] Figure 1 This is a schematic diagram of the complete set of equipment for producing zero trans fatty acid oils according to this utility model.

[0026] In the diagram: Raw material pretreatment unit: 101-spiral plate heat exchanger, 102-vacuum dryer, 103-molecular sieve adsorption tower;

[0027] Core reaction units: 201 - Fixed-bed enzyme reactor, 202 - Hydrogenation reaction tower;

[0028] Separation and purification unit: 301-scraped membrane evaporator, 302-multi-stage crystallization and fractionation assembly, 3021-first crystallization tank, 3022-first plate and frame filter, 3023-second crystallization tank, 3024-second plate and frame filter, 3025-third crystallization tank, 3026-disc centrifuge, 4-first cooling coil, 5-second cooling coil, 6-third cooling coil, 7-stirring component;

[0029] Nitrogen supply unit: 401-Nitrogen generator, 402-Nitrogen storage tank. Detailed Implementation

[0030] The complete set of equipment for producing zero trans fatty acid oils according to this utility model will be described in more detail below with reference to the accompanying drawings and specific embodiments.

[0031] In the description of this utility model, it should be understood that the terms "upper", "lower", "front", "rear", "left", "right", "top", "bottom", "inner", "outer", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this utility model.

[0032] Example 1

[0033] See Figure 1 A complete set of equipment for producing zero trans fatty acid oils includes a raw oil pretreatment unit, a core reaction unit, a separation and purification unit, and a nitrogen supply unit for providing nitrogen to the core reaction unit.

[0034] The feedstock oil pretreatment unit includes a spiral plate heat exchanger 101, a vacuum dryer 102, and a molecular sieve adsorption tower 103;

[0035] The core reaction unit includes a fixed-bed enzyme reactor 201 and a hydrogenation reaction tower 202;

[0036] The nitrogen supply unit includes a nitrogen generator 401 and a nitrogen storage tank 402. The inlet of the nitrogen generator 401 is connected to air, and the outlet of the nitrogen generator 401 is connected to the inlet pipe of the nitrogen storage tank 402. The fixed-bed enzyme reactor 201 and the hydrogenation reaction tower 202 are both connected to the outlet pipe of the nitrogen storage tank 402.

[0037] The separation and purification unit includes a scraped membrane evaporator 301 and a multi-stage crystallization and fractionation assembly 302. The multi-stage crystallization and fractionation assembly 302 includes a first crystallization tank 3021, a first plate and frame filter 3022, a second crystallization tank 3023, a second plate and frame filter 3024, a third crystallization tank 3025, and a disc centrifuge 3026.

[0038] See Figure 1 The raw material oil is introduced into one of the spiral channels of the spiral plate heat exchanger 101, and its outlet end is connected to the feed inlet pipe of the vacuum dryer 102. The inlet end of the other spiral channel of the spiral plate heat exchanger 101 is connected to the discharge outlet pipe of the scraped film evaporator 301, and its outlet end is connected to the feed inlet pipe of the first crystallizer 3021. The raw material oil exchanges heat with the material coming out of the scraped film evaporator 301 through the spiral plate heat exchanger 101 to make full use of the waste heat of the heat source. After preheating, the raw material oil enters the vacuum dryer 102. The vacuum dryer 102 performs vacuum dehydration and deoxygenation on the raw material oil to avoid the influence of moisture and oxygen on the oil in subsequent processing.

[0039] See Figure 1The outlet of the vacuum dryer 102 is connected to the inlet pipe of the molecular sieve adsorption tower 103. The raw oil after vacuum dehydration and deoxygenation enters the molecular sieve adsorption tower 103, where free fatty acids in the raw oil are adsorbed and removed. The inlet of the fixed-bed enzyme reactor 201 is connected to the outlet pipe of the molecular sieve adsorption tower 103. The raw oil after the removal of free fatty acids enters the fixed-bed enzyme reactor 201, which is filled with immobilized lipase. Nitrogen gas is introduced through the nitrogen supply unit. In this device, the immobilized enzyme reconstructs the structure of triglycerides at low temperature. The inlet of the hydrogenation reaction tower 202 is connected to the outlet pipe of the fixed-bed enzyme reactor 201. The reconstructed oil enters the hydrogenation reaction tower 202, where nitrogen gas is introduced through the nitrogen supply unit. Under continuous nitrogen protection, the reconstructed oil is hydrogenated at low temperature and low pressure to eliminate the environmental conditions for the formation of trans fatty acids, thereby changing the molecular structure of the oil to obtain the target product.

[0040] See Figure 1 The feed inlet of the scraped film evaporator 301 is connected to the discharge outlet of the hydrogenation reaction tower 202. The material enters the scraped film evaporator 301 and removes the free fatty acids generated during the reaction through the scraped film evaporator 301. The material discharged from the discharge outlet of the scraped film evaporator 301 enters the spiral plate heat exchanger 101 to exchange heat with the raw material oil and cool down.

[0041] See Figure 1 The inlet of the first crystallization tank 3021 is connected to the spiral channel outlet pipe of the spiral plate heat exchanger 101. The cooled material enters the first crystallization tank 3021. A first cooling coil 4 is installed on the inner wall of the first crystallization tank 3021. Cold ethylene glycol flows through the first cooling coil 4. The material exchanges heat with the cold ethylene glycol in the first cooling coil 4, and the high melting point component in the material crystallizes out. The outlet of the first crystallization tank 3021 is connected to the inlet pipe of the first plate and frame filter 3022. The crystallized material enters the first plate filter for solid-liquid separation. The inlet of the second crystallization tank 3023 is connected to the outlet pipe of the first plate and frame filter 3022. The filtrate enters the second crystallization tank 3023.

[0042] See Figure 1 The inner wall of the second crystallization tank 3023 is equipped with a second cooling coil 5, which is filled with chilled brine. The material entering the second crystallization tank 3023 exchanges heat with the chilled brine in the second cooling coil 5, causing the medium melting point component in the material to crystallize and precipitate. The outlet of the second crystallization tank 3023 is connected to the inlet pipe of the second plate and frame filter 3024. The crystallized material enters the second plate and frame filter for solid-liquid separation. The inlet of the third crystallization tank 3025 is connected to the outlet pipe of the second plate and frame filter 3024, and the filtrate enters the third-stage crystallization tank.

[0043] See Figure 1 The inner wall of the third crystallization tank 3025 is equipped with a third cooling coil 6, which is filled with chilled water. The material entering the third crystallization tank 3025 exchanges heat with the chilled water in the third cooling coil 6, and the low melting point components in the material crystallize out. The crystallized material enters the disc centrifuge 3026 for solid-liquid separation, and the filtrate is the zero trans fatty acid oil product.

[0044] In this embodiment, the material undergoes three-stage non-isothermal gradient crystallization using the cooling medium in the first crystallization tank 3021, the second crystallization tank 3023, and the third crystallization tank 3025. The material is then precisely separated by the first plate and frame filter 3022, the second plate and frame filter 3024, and the disc centrifuge 3026. The solids separated by the first plate and frame filter 3022, the second plate and frame filter 3024, and the disc centrifuge 3026 are solid fats with different melting points, while the oil phase separated by the disc separator is a zero-trans fatty acid fat product.

[0045] Example 2

[0046] See Figure 1 Based on Example 1, stirring components 7 are installed in the first crystallization tank 3021, the second crystallization tank 3023, and the third crystallization tank 3025. The stirring components 7 stir the materials in the first crystallization tank 3021, the second crystallization tank 3023, and the third crystallization tank 3025, so that the cooling medium in the first cooling coil 4, the second cooling coil 5, and the third cooling coil 6 can fully exchange heat with the materials in their respective crystallization tanks, which can effectively improve the crystallization effect and efficiency, and thus improve the quality of zero trans fatty acid oil products.

[0047] Unless otherwise defined, the technical or scientific terms used herein shall have the ordinary meaning as understood by one of ordinary skill in the art to which this invention pertains. The use of terms such as "a" or "an" in this specification and claims does not necessarily indicate a limitation on quantity. Terms such as "comprising" or "including" mean that the element or object preceding the word encompasses the element or object listed following the word and its equivalents, without excluding other elements or objects. Terms such as "connected" or "linked" are not limited to physical or mechanical connections, but may include electrical connections, whether direct or indirect.

[0048] The exemplary embodiments of the present invention have been described in detail above with reference to preferred embodiments. However, those skilled in the art will understand that various modifications and alterations can be made to the above specific embodiments without departing from the concept of the present invention, and various combinations can be made to the various technical features and structures proposed by the present invention without exceeding the protection scope of the present invention.

Claims

1. A complete set of equipment for producing zero trans fatty acid oils, characterized in that: It includes a feedstock pretreatment unit, a core reaction unit, a separation and purification unit, and a nitrogen supply unit for providing nitrogen to the core reaction unit; The feedstock oil pretreatment unit includes a spiral plate heat exchanger, a vacuum dryer, and a molecular sieve adsorption tower. The feedstock oil is introduced into one of the spiral channels of the spiral plate heat exchanger, and its outlet is connected to the feed inlet pipe of the vacuum dryer. The outlet of the vacuum dryer is connected to the feed inlet pipe of the molecular sieve adsorption tower. The core reaction unit includes a fixed-bed enzyme reactor and a hydrogenation reaction tower. Both the fixed-bed enzyme reactor and the hydrogenation reaction tower are connected to the nitrogen supply unit pipeline. The feed inlet of the fixed-bed enzyme reactor is connected to the discharge outlet pipeline of the molecular sieve adsorption tower, and the feed inlet of the hydrogenation reaction tower is connected to the discharge outlet pipeline of the fixed-bed enzyme reactor. The separation and purification unit includes a scraped film evaporator and a multi-stage crystallization and fractionation assembly. The inlet of the scraped film evaporator is connected to the outlet pipe of the hydrogenation reaction tower. The inlet end of the other spiral channel of the spiral plate heat exchanger is connected to the outlet pipe of the scraped film evaporator, and its outlet end is connected to the pipe of the multi-stage crystallization and fractionation assembly.

2. The complete set of equipment for producing zero trans fatty acid oils according to claim 1, characterized in that: The nitrogen supply unit includes a nitrogen generator and a nitrogen storage tank. The inlet of the nitrogen generator is connected to air, and the outlet of the nitrogen generator is connected to the inlet pipe of the nitrogen storage tank. The fixed-bed enzyme reactor and the hydrogenation reaction tower are both connected to the outlet pipe of the nitrogen storage tank.

3. The complete set of equipment for producing zero trans fatty acid oils according to claim 1, characterized in that: The multi-stage crystallization and fractionation assembly includes a first crystallization tank, a first plate and frame filter, a second crystallization tank, a second plate and frame filter, a third crystallization tank, and a disc centrifuge. The inlet of the first crystallizer is connected to the outlet pipe of the spiral channel of the spiral plate heat exchanger, and the outlet of the first crystallizer is connected to the inlet pipe of the first plate and frame filter. The inlet of the second crystallizer is connected to the outlet pipe of the first plate and frame filter, and the outlet of the second crystallizer is connected to the inlet pipe of the second plate and frame filter. The inlet of the third crystallizer is connected to the outlet pipe of the second plate and frame filter, and the outlet of the third crystallizer is connected to the inlet pipe of the disc filter.

4. The complete set of equipment for producing zero trans fatty acid oils according to claim 3, characterized in that: The inner wall of the first crystallization tank is equipped with a first cooling coil.

5. The complete set of equipment for producing zero trans fatty acid oils according to claim 4, characterized in that: The inner wall of the second crystallization tank is equipped with a second cooling coil.

6. The complete set of equipment for producing zero trans fatty acid oils according to claim 5, characterized in that: The inner wall of the third crystallization tank is equipped with a third cooling coil.

7. The complete set of equipment for producing zero trans fatty acid oils according to any one of claims 3 to 6, characterized in that: The first, second, and third crystallization tanks are all equipped with stirring components.

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