Vapor-liquid separation energy-saving device for vegetable oil processing

Abstract

The utility model relates to a vegetable oil processing vapor-liquid separation energy-saving device, which comprises an energy saver, an evaporative condenser, a steam stripping condenser and a solvent water distribution box, and a mixed steam inlet is arranged on the side wall of the energy saver close to the bottom of the energy saver; the bottom of the energy saver is communicated with the top of the solvent water distribution box through a pipeline I, the bottom of the solvent water distribution box is communicated with the top of the energy saver through a pipeline II, and a water distribution pump is fixedly mounted on the pipeline II; the first connector is used for communicating with the second evaporator. The second connector communicates with the top of the solvent water distribution box through a third pipeline. The interface V is communicated with a stripping tower, and the interface VI is communicated with the top of the solvent water distribution box through a pipeline IV. The device has the beneficial effects that the structure is simple, the design is reasonable, the complementary energy of mixed steam in production is recovered, the cyclic utilization of a solvent is realized, the energy consumption is saved, and the cost is reduced.

Description

Technical Field

[0001] The utility model relates to the technical field of vegetable oil processing, in particular to a gas-liquid separation energy-saving device for vegetable oil processing. Background Art

[0002] The extraction method is to apply the principle of extraction, select a certain organic solvent that can dissolve oil, and make it contact with the pre-treated oil - soak or spray, so that the oil in the oil is dissolved. This method makes the solvent and the oil it dissolves form a solution, which is called mixed oil. Taking advantage of the different boiling points of the selected solvent and the oil, the mixed oil is evaporated and stripped, the solvent is evaporated, the oil is left, and the crude oil is obtained. The evaporated solvent vapor is recovered by condensation and recycled.

[0003] In the above process, the condensate of the evaporative condenser and the stripping condenser is collected in the liquid collecting tank, and the condensate in the liquid collecting tank is pumped into the economizer through the liquid collecting pump. The above process has the following disadvantages: In actual production, the water distribution pump is constantly distributing water; the condensate of the evaporative condenser and the stripping condenser must be collected in the liquid collecting tank before it can be collected and used. In order to save energy, the liquid collecting pump must also rotate continuously during the vapor-liquid contact process, which consumes a lot of energy and has a high cost. Utility Model Content

[0004] The utility model provides a gas-liquid separation energy-saving device for vegetable oil processing, aiming to solve the problems in the prior art.

[0005] The technical solution of the utility model to solve the above technical problems is as follows:

[0006] A plant oil processing vapor-liquid separation energy-saving device comprises an economizer, an evaporative condenser, a stripping condenser and a solvent water separation tank, wherein a mixed steam inlet is arranged at a portion of a side wall of the economizer near its bottom; the bottom of the economizer is connected to the top of the solvent water separation tank through a first pipeline, the bottom of the solvent water separation tank is connected to the top of the economizer through a second pipeline, and a water separation pump is fixedly installed on the second pipeline;

[0007] The evaporative condenser is provided with an interface 1 and an interface 2 which are interconnected, as well as an interface 3 and an interface 4 which are interconnected; the stripping condenser is provided with an interface 5 and an interface 6 which are interconnected, as well as an interface 7 and an interface 8 which are interconnected; the interface 1 is used to connect to the second evaporator, and the interface 2 is connected to the top of the solvent water distribution tank through pipeline 3; the interface 5 is used to connect to the stripping tower, and the interface 6 is connected to the top of the solvent water distribution tank through pipeline 4.

[0008] The utility model has the following beneficial effects: during the processing, the mixed steam formed by treating the oil cake with the degassing machine enters the shell side of the pre-evaporator to exchange heat with the mixed oil to be treated, the mixed steam releases heat and partially condenses to become a mixed liquid of solvent and water, the mixed oil absorbs heat to make part of the solvent in the mixed oil volatilize into gas and enter the evaporative condenser for condensation; the uncondensed mixed steam after passing through the shell side of the pre-evaporator enters the economizer, and contacts the liquid condensed by the evaporative condenser and the stripping condenser, the condensate absorbs the heat of the mixed steam, and flows into the solvent water separation tank for water separation and recycling; the mixed steam releases heat after contacting the condensate, and the partially liquefied mixed steam liquid enters the solvent water separation tank together with the condensate from the evaporative condenser after absorbing heat.

[0009] The utility model has a simple structure and a reasonable design, and can recover the residual energy of the mixed steam in production, realize the recycling of the solvent, save energy consumption and reduce costs.

[0010] On the basis of the above technical solution, the present invention can also be improved as follows.

[0011] Furthermore, a plurality of annular nozzles are horizontally fixedly installed at even intervals from top to bottom in the energy saver, and the plurality of annular nozzles are respectively connected to the pipeline 2, and a plurality of injection holes are respectively evenly spaced on the upper and lower sides thereof; at least one flow plate is obliquely fixedly installed in the area between two adjacent annular nozzles in the energy saver.

[0012] The beneficial effect of adopting the above further scheme is that the structure of the economizer is reasonably designed, the mixed steam after heat release freely escapes into the vapor-liquid contactor (economizer) from bottom to top, and contacts with the mixed liquid pumped from the solvent chamber in the solvent water separation tank (the mixed liquid forms a multi-stage spray mist curtain from top to bottom) in countercurrent infinite stages, and the heated mixed liquid flows into the water separation chamber of the solvent water separation tank by gravity; the cooled mixed steam freely escapes into the atmospheric condenser (shell side), and is cooled by cooling water (in the condenser tube side) pumped from the cooling tower of the leaching workshop, and the condensate of the mixed steam cooled by water (the mixed steam becomes a mixed solution) freely flows into the water separation chamber of the solvent water separation tank; the mixed solution entering the water separation chamber in the solvent water separation tank is automatically separated by using the density difference between the solvent and water.

[0013] Furthermore, the internal space of the solvent water distribution tank is divided into a mutually independent primary separation chamber, a secondary water chamber, a secondary solvent chamber, a tertiary solvent chamber and a tertiary water chamber by multiple partitions. The primary separation chamber is connected to the secondary water chamber and the secondary solvent chamber, the secondary water chamber and the tertiary water chamber, and the secondary solvent chamber and the tertiary solvent chamber respectively through overflow pipes, and the primary separation chamber is connected to one end of the pipeline.

[0014] The beneficial effect of adopting the above further solution is that the structure design of the solvent water separation tank is reasonable, and multi-stage separation of water and solvent is achieved, and the separation is more thorough.

[0015] Furthermore, it includes a normal pressure condenser, on which are provided an interface nine and an interface ten which are interconnected, and an interface eleven and an interface twelve which are interconnected; the top of the economizer, the interface nine, the interface ten and the pipeline three are sequentially connected through pipelines; the interface seven, the interface eight, the interface three, the interface four, the interface eleven and the interface twelve are sequentially connected through condensate pipelines, and the interface seven and the interface twelve are respectively used for connecting to a condensate supply tank.

[0016] The beneficial effects of adopting the above further scheme are simple structure and reasonable design. The mixed steam releases heat after contacting the condensate, and the partially liquefied mixed steam liquid enters the solvent water separation tank together with the condensate from the condenser after absorbing heat. The uncondensed mixed steam enters the atmospheric pressure condenser and is further cooled and liquefied by circulating water, thereby further improving the recovery effect.

[0017] Furthermore, it also includes a pre-evaporator, on which are provided an interface thirteen and an interface fourteen that are interconnected, as well as an interface fifteen and an interface sixteen that are interconnected; the interface sixteen is connected to the mixed steam inlet on the economizer through a pipeline, and the interface fifteen is used to connect to the mixed steam outlet of the degassing machine; the interface thirteen is used to connect to the mixed oil outlet of the extractor, and the interface fourteen is used to connect to the second evaporator.

[0018] The beneficial effect of adopting the above further scheme is that during the processing, the mixed steam formed by treating the oil cake in the degassing machine enters the shell side of the pre-evaporator to exchange heat with the mixed oil to be treated, the mixed steam releases heat and partially condenses to become a mixed liquid of solvent and water, the mixed oil absorbs heat to make part of the solvent in the mixed oil evaporate into gas and enter the evaporative condenser for condensation; the uncondensed mixed gas after passing through the shell side of the pre-evaporator enters the economizer, and contacts the liquid condensed by the evaporative condenser and the stripping condenser, and the condensate absorbs the heat of the mixed steam and flows into the solvent water separation tank by gravity for water separation and recycling.

[0019] Furthermore, the top of the pre-evaporator is also connected to the area connected to the interface three and the interface four through a pipeline.

[0020] The beneficial effects of adopting the above further scheme are simple structure and reasonable design. All solvent vapor enters the evaporative condenser for condensation treatment, and the separated solvent can be directly recovered into the solvent water separation tank.

[0021] Furthermore, the pre-evaporator is also provided with a mixed steam-liquid outlet connected to the area connected to the interface fifteen and the interface sixteen, and the mixed steam-liquid outlet is connected to the pipeline one through a pipeline.

[0022] The beneficial effects of adopting the above further scheme are simple structure and reasonable design. The mixed steam and liquid discharged from the pre-evaporator directly enter the solvent water separation tank through pipeline 1, which is convenient for recovery.

[0023] Furthermore, one end of the pipeline three is connected to the pipeline one, and one end of the pipeline four is connected to the pipeline three.

[0024] The beneficial effects of adopting the above further solution are simple structure, reasonable pipeline distribution and reduced cost.

[0025] Furthermore, the top of the solvent water distribution tank is also connected to one end of a solvent supply pipeline, the other end of the solvent supply pipeline is used to connect to a solvent reservoir, and a solvent supply pump is fixedly installed on the solvent supply pipeline.

[0026] The beneficial effects of adopting the above further solution are simple structure and reasonable design. The solvent in the solvent reservoir can be regularly replenished into the entire system by using a solvent supply pump to ensure sufficient solvent to enable the normal operation of the entire system.

[0027] Furthermore, the bottom of the solvent water distribution tank is connected through one end of a solvent circulation pipeline, the other end of the solvent circulation pipeline is used to connect to an extractor, and a solvent circulation pump and a solvent heater are fixedly installed at intervals on the solvent circulation pipeline along the direction of solvent flow.

[0028] The beneficial effects of adopting the above further scheme are simple structure and reasonable design. The solvent separated by the solvent water separation tank can be sent back to the extractor for recycling by the solvent circulation pump, thereby realizing the recycling of the solvent, saving energy consumption and reducing costs. In addition, the solvent heater can heat the recovered solvent to meet production needs. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] Figure 1 It is a schematic diagram of the overall structure of the utility model;

[0030] Figure 2 It is a structural schematic diagram of the energy saver in the utility model;

[0031] Figure 3 It is a structural schematic diagram of the annular nozzle in the utility model;

[0032] Figure 4 It is a structural schematic diagram of the flow plate in the utility model;

[0033] Figure 5It is a structural schematic diagram of the solvent water distribution tank in the utility model.

[0034] In the accompanying drawings, the components represented by the reference numerals are listed as follows:

[0035] 1. Economizer; 2. Evaporative condenser; 3. Stripping condenser; 4. Solvent water distribution tank; 5. Water distribution pump; 6. Annular nozzle; 7. Flow plate; 8. Primary separation chamber; 9. Secondary water chamber; 10. Secondary solvent chamber; 11. Tertiary solvent chamber; 12. Tertiary water chamber; 13. Overflow pipe; 14. Atmospheric pressure condenser; 15. Pre-evaporator; 16. Solvent supply pump; 17. Solvent circulation pump; 18. Inlet nozzle; 19. Mixed oil supply pump; 20. Solvent heater; 21. Liquid storage tank. DETAILED DESCRIPTION

[0036] It should be noted that, in the absence of conflict, the embodiments of the present invention and the features in the embodiments can be combined with each other.

[0037] In the description of the present utility model, it should be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside" and the like indicate positions or positional relationships based on the positions or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present utility model and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present utility model. In addition, the terms "first", "second", etc. are only used for descriptive purposes, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Therefore, features defined as "first", "second", etc. may explicitly or implicitly include one or more of the features. In the description of the present utility model, unless otherwise specified, "multiple" means two or more.

[0038] In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, the terms "installation", "connection" and "connection" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be an indirect connection through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood by specific circumstances.

[0039] The present invention will be described in detail below with reference to the accompanying drawings and in combination with embodiments.

[0040] Example 1

[0041] like Figures 1 to 5 As shown, this embodiment provides a gas-liquid separation energy-saving device for vegetable oil processing, comprising an economizer 1, an evaporative condenser 2, a stripping condenser 3 and a solvent water separation tank 4, wherein a mixed steam inlet is provided at a portion of the side wall of the economizer 1 near its bottom; the bottom of the economizer 1 is connected to the top of the solvent water separation tank 4 through a pipeline 1, and the bottom of the solvent water separation tank 4 is connected to the top of the economizer 1 through a pipeline 2, and a water separation pump 5 is fixedly installed on the pipeline 2;

[0042] The evaporative condenser 2 is provided with an interface 1 and an interface 2 which are interconnected, as well as an interface 3 and an interface 4 which are interconnected; the stripping condenser 3 is provided with an interface 5 and an interface 6 which are interconnected, as well as an interface 7 and an interface 8 which are interconnected; the interface 1 is used to connect to the second evaporator, and the interface 2 is connected to the top of the solvent water distribution tank 4 through a pipeline 3; the interface 5 is used to connect to the stripping tower, and the interface 6 is connected to the top of the solvent water distribution tank 4 through a pipeline 4.

[0043] During the processing, the mixed steam formed by treating the oil cake in the degassing machine enters the shell side of the pre-evaporator to exchange heat with the mixed oil to be treated. The mixed steam releases heat and partially condenses to become a mixed liquid of solvent and water. The mixed oil absorbs heat to make part of the solvent in the mixed oil evaporate into gas and enter the evaporative condenser for condensation; the uncondensed mixed steam after passing through the shell side of the pre-evaporator enters the economizer and contacts with the liquid condensed by the evaporative condenser and the stripping condenser. After the condensate absorbs the heat of the mixed steam, it flows into the solvent water separation tank by gravity for water separation and recycling; the mixed steam releases heat after contacting the condensate, and the partially liquefied mixed steam liquid enters the solvent water separation tank together with the condensate from the evaporative condenser after absorbing heat.

[0044] Preferably, in this embodiment, the water diversion pump 5 is preferably a booster pump.

[0045] It should be noted that the above-mentioned evaporative condenser 2, stripping condenser 3 and water diversion pump 5 respectively adopt existing technologies, and their specific structures and principles are not described in detail here.

[0046] This embodiment has a simple structure and a reasonable design, and can recover the residual energy of the mixed steam in production, realize the recycling of the solvent, save energy consumption, and reduce costs.

[0047] Example 2

[0048] On the basis of Example 1, in this embodiment, a plurality of annular nozzles 6 are horizontally fixedly installed at even intervals from top to bottom in the energy saver 1, and the plurality of annular nozzles 6 are respectively connected to the pipeline 2 through branch pipelines, and a plurality of injection holes are evenly spaced on the upper and lower sides thereof; at least one flow plate 7 is obliquely fixedly installed in the area corresponding to the area between two adjacent annular nozzles 6 in the energy saver 1.

[0049] The structure of the economizer 1 is reasonably designed. The mixed steam after heat release freely escapes into the vapor-liquid contactor (economizer) from bottom to top, and contacts with the mixed liquid pumped from the solvent chamber in the solvent water separation tank (the mixed liquid forms a multi-stage spray mist curtain from top to bottom) in countercurrent infinite stages, and the heated mixed liquid flows into the water separation chamber of the solvent water separation tank by gravity; the cooled mixed steam freely escapes into the atmospheric condenser (shell side), and is cooled by cooling water (in the condenser tube side) pumped by the cooling tower of the leaching workshop, and the condensate of the mixed steam cooled by water (the mixed steam becomes a mixed solution) freely flows into the water separation chamber of the solvent water separation tank; the mixed solution entering the water separation chamber in the solvent water separation tank is automatically separated by using the density difference between the solvent and water.

[0050] Alternatively, the annular nozzle 6 located at the bottom can also be replaced by the inlet nozzle 18.

[0051] Based on the above solution, the parts above and below the multiple annular nozzles 6 in the economizer 1 are also inclinedly provided with flow plates 7 respectively.

[0052] In addition, one flow plate 7 or two flow plates 7 may be provided between two adjacent annular nozzles 6, and the specific number of flow plates 7 may be designed according to requirements.

[0053] Example 3

[0054] On the basis of the above embodiments, in this embodiment, the internal space of the solvent water distribution tank 4 is divided into a mutually independent primary separation chamber 8, a secondary water chamber 9, a secondary solvent chamber 10, a tertiary solvent chamber 11 and a tertiary water chamber 12 by multiple partitions, and the primary separation chamber 8 is connected to the secondary water chamber 9 and the secondary solvent chamber 10, the secondary water chamber 9 and the tertiary water chamber 12, and the secondary solvent chamber 10 and the tertiary solvent chamber 11 through an overflow pipe 13, and the primary separation chamber 8 is connected to one end of the pipeline.

[0055] The structure design of the solvent water separation tank 4 is reasonable, and the multi-stage separation of water and solvent is realized, and the separation is more thorough.

[0056] Example 4

[0057] On the basis of the above embodiments, the present embodiment also includes a normal pressure condenser 14, and the normal pressure evaporator 14 is provided with an interface nine and an interface ten which are interconnected, and an interface eleven and an interface twelve which are interconnected, and the top of the economizer 1, the interface nine, the interface ten and the pipeline three are connected in sequence through pipelines; the interface seven, the interface eight, the interface three, the interface four, the interface eleven and the interface twelve are connected in sequence through condensate pipelines, and the interface seven and the interface twelve are respectively used to connect to the condensate supply tank.

[0058] This solution has a simple structure and a reasonable design. The mixed steam releases heat after contacting the condensate. The partially liquefied mixed steam liquid enters the solvent water separation tank together with the condensate from the condenser that has absorbed heat. The uncondensed mixed steam enters the atmospheric pressure condenser 14 and is further cooled and liquefied by circulating water, thereby further improving the recovery effect.

[0059] It should be noted that the above-mentioned atmospheric pressure condenser 14 adopts the existing technology, and its specific structure and principle are not described in detail here.

[0060] Example 5

[0061] On the basis of the above embodiments, the present embodiment further includes a pre-evaporator 15, on which the pre-evaporator 15 is provided with an interface thirteen and an interface fourteen which are interconnected, and an interface fifteen and an interface sixteen which are interconnected; the interface sixteen is connected to the mixed steam inlet on the economizer through a pipeline, and the interface fifteen is used to connect to the mixed steam outlet of the degassing machine; the interface thirteen is used to connect to the mixed oil outlet of the extractor, and the interface fourteen is used to connect to the second evaporator.

[0062] During the processing, the mixed steam formed by treating the oil cake in the degassing machine enters the shell side of the pre-evaporator to exchange heat with the mixed oil to be treated. The mixed steam releases heat and partially condenses to become a mixed liquid of solvent and water. The mixed oil absorbs heat to make part of the solvent in the mixed oil evaporate into gas and enter the evaporative condenser for condensation; the uncondensed mixed gas after passing through the shell side of the pre-evaporator enters the economizer and contacts the liquid condensed by the evaporative condenser and the stripping condenser. After the condensate absorbs the heat of the mixed steam, it flows into the solvent water separation tank by gravity for water separation and recycling.

[0063] Based on the above scheme, a liquid storage tank 21 is also fixedly installed on the pipeline connecting the above interface thirteen and the mixed oil outlet of the extractor, and a mixed oil supply pump 19 is fixedly installed on the pipeline connecting the liquid storage tank 21 and the interface thirteen. The mixed oil produced by the extractor is stored in the above liquid storage tank 21, and the mixed oil in the liquid storage tank 21 is delivered to the pre-evaporator 15 by the mixed oil supply pump 19.

[0064] In addition, the interface 15 on the pre-evaporator 15 is connected to the DTDC desiccant evaporator, which is used to process the oil meal produced by the extractor, and the mixed steam outlet generated by the oil meal processing is connected to the interface 15 on the pre-evaporator.

[0065] It should be noted that the above-mentioned pre-evaporator 15, DTDC degassing machine and mixed oil supply pump 19 respectively adopt the existing technology, and their specific structures and principles are not described in detail here.

[0066] Example 6

[0067] On the basis of Example 5, in this example, the top of the pre-evaporator 15 is also connected to the area connected to the interface three and the interface four through a pipeline.

[0068] The scheme has a simple structure and a reasonable design. All solvent vapors enter the evaporative condenser for condensation treatment, and the separated solvent can be directly recovered into the solvent water separation tank.

[0069] Example 7

[0070] On the basis of any one of Examples 5 to 6, in this embodiment, the pre-evaporator 15 is further provided with a mixed steam-liquid outlet connected to the area connected to the interface fifteen and the interface sixteen, and the mixed steam-liquid outlet is connected to the pipeline one through a pipeline.

[0071] This solution has a simple structure and a reasonable design. The mixed steam and liquid discharged from the pre-evaporator 15 directly enter the solvent water separation tank 4 through the pipeline 1, which is convenient for recovery.

[0072] Example 8

[0073] On the basis of the above embodiments, in this embodiment, one end of the pipeline three is connected to the pipeline one, and one end of the pipeline four is connected to the pipeline three.

[0074] The solution has a simple structure, reasonable pipeline distribution and reduced costs.

[0075] Alternatively, the above pipeline three and pipeline four may also be directly connected to the solvent water distribution tank 4, but this solution has more pipelines, and the pipeline distribution is complex, the equipment occupies a large space, and the cost is high.

[0076] Example 9

[0077] On the basis of the above embodiments, in this embodiment, the top of the solvent water distribution tank 4 is also connected to one end of the solvent supply pipeline, the other end of the solvent supply pipeline is used to connect to the solvent reservoir, and a solvent supply pump 16 is fixedly installed on the solvent supply pipeline.

[0078] This solution has a simple structure and a reasonable design. The solvent supply pump 16 can be used to regularly replenish the solvent in the solvent reservoir into the entire system to ensure that the solvent amount is sufficient so that the entire system can operate normally.

[0079] It should be noted that the above-mentioned solvent supply pump 16 adopts the existing technology, and its specific structure and principle are not described in detail here.

[0080] Example 10

[0081] On the basis of the above embodiments, in this embodiment, the bottom of the solvent water distribution tank 4 is connected through one end of the solvent circulation pipeline, the other end of the solvent circulation pipeline is used to connect to the extractor, and the solvent circulation pump 17 and the solvent heater 20 are fixedly installed at intervals along the direction of solvent flow on the solvent circulation pipeline.

[0082] This solution has a simple structure and a reasonable design. The solvent separated by the solvent water separation tank 4 can be sent back to the extractor for recycling by the solvent circulation pump 17, thereby realizing the recycling of the solvent, saving energy consumption and reducing costs. In addition, the solvent heater 20 can heat the recovered solvent to meet production needs.

[0083] It should be noted that the above-mentioned solvent circulation pump 17 and solvent heater 20 respectively adopt the existing technology, and their specific structures and principles are not described in detail here.

[0084] The working principle of the utility model is as follows:

[0085] The superheated steam from the steam cylinder enters the desolventizing layer of the DTDC desolventizer, and the dry steam contacts the defatted white meal from the extractor (the white meal flows from top to bottom) in reverse direction from bottom to top;

[0086] The solvent in the white meal absorbs the heat of steam and vaporizes, combining with water vapor to form mixed steam. The mixed steam carries heat and continues to rise, and contacts with the white meal that continuously enters the degassing machine in an infinite countercurrent manner. After contact, the proportion of solvent contained in the mixed steam continues to increase, and the temperature of the mixed steam continues to decrease, and then naturally escapes from the top of the DTDC degassing machine.

[0087] The temperature of the mixed steam escaping from the DTDC is still as high as over 70°C. It passes through a softened hot water layer over 90°C for purification while absorbing the heat of the hot water.

[0088] The mixed steam after absorbing the heat of hot water automatically escapes into the shell side of the first evaporator (i.e., pre-evaporator), and performs countercurrent heat exchange with the mixed oil at about 50°C from the extractor (the mixed oil enters the tube side of the first evaporator from bottom to top, and the mixed steam enters the shell side of the first evaporator from top to bottom, and the two exchange heat through thin-walled stainless steel tubes).

[0089] The mixed steam after releasing heat escapes freely from bottom to top into the vapor-liquid contactor (economizer), and contacts with the mixed liquid pumped from the solvent cavity in the solvent water separation tank (the mixed liquid forms a multi-stage spray mist curtain from top to bottom) in countercurrent infinite stages, and the heated mixed liquid flows into the water separation cavity of the solvent water separation tank.

[0090] The cooled mixed steam escapes freely into the atmospheric condenser (shell side), and is cooled by cooling water (in the condenser tube side) from the cooling tower pump in the leaching workshop. The condensate of the mixed steam after water cooling (the mixed steam becomes a mixed solution) flows freely into the water separation chamber of the solvent water separation tank.

[0091] The mixed solution entering the water separation chamber in the solvent water separation tank is automatically separated by using the density difference between the solvent and water:

[0092] The separated softened water automatically flows into the cooking tank and is further heated to above 90°C to further separate the solvent contained in the water. The heated hot soft water is circulated and pumped to the scrubber by a hot water pump to wash the mixed steam escaping from the top of the DTDC. The excess hot soft water (containing no more than 100ppm of solvent) is purified and sent to other processes to further utilize its heat and soft water resources.

[0093] The separated solvent enters the solvent chamber after multi-stage separation of the water contained therein. The hot solvent (normal production temperature is above 40°C) entering the solvent chamber is pumped into the extractor by a special stainless steel solvent circulation pump for circulation extraction and degreasing of the impregnated material.

[0094] In order to prevent water in the solvent from entering the extractor, a stainless steel water distribution pump is installed at the bottom of the solvent chamber (304 stainless steel is used to prevent rust and iron slag), and the pumped solvent is continuously pumped into the economizer for direct contact heat exchange with the continuously flowing mixed steam.

[0095] In the solvent chamber, two outlets are set, one for the water separation pump and the other for the circulating solvent pump. In order to ensure the continuous flow of the mixed liquid in the water separation pump, the pump outlet is often about 200mm lower than the mixed solvent pump; but about 50mm higher than the bottom of the solvent chamber to prevent impurities such as rust from entering the water separation pump.

[0096] The equipment and pipelines used in the utility model are all made of 304 stainless steel to improve their operating efficiency.

[0097] It should be noted that all electronic components involved in the present invention adopt the existing technology, and the above-mentioned components are electrically connected to the controller, and the control circuit between the controller and each component is the existing technology.

[0098] It is obvious to those skilled in the art that the present invention is not limited to the details of the exemplary embodiments described above, and that the present invention can be implemented in other specific forms without departing from the spirit or essential features of the present invention. Therefore, the embodiments should be regarded as exemplary and non-restrictive from any point of view, and the scope of the present invention is defined by the appended claims rather than the above description, and it is intended that all changes falling within the meaning and scope of the equivalent elements of the claims be included in the present invention. Any reference numeral in a claim should not be regarded as limiting the claim to which it relates.

[0099] In addition, it should be understood that although the present specification is described according to implementation modes, not every implementation mode contains only one independent technical solution. This description of the specification is only for the sake of clarity. Those skilled in the art should regard the specification as a whole. The technical solutions in each embodiment may also be appropriately combined to form other implementation modes that can be understood by those skilled in the art.

[0100] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A gas-liquid separation energy-saving device for vegetable oil processing, characterized in that: The invention comprises an economizer (1), an evaporative condenser (2), a stripping condenser (3) and a solvent water separation tank (4); a mixed steam inlet is provided at a portion of a side wall of the economizer (1) near its bottom; the bottom of the economizer (1) is connected to the top of the solvent water separation tank (4) through a first pipeline; the bottom of the solvent water separation tank (4) is connected to the top of the economizer (1) through a second pipeline; a water separation pump (5) is fixedly installed on the second pipeline; The evaporative condenser (2) is provided with an interface 1 and an interface 2 which are interconnected, and an interface 3 and an interface 4 which are interconnected; the stripping condenser (3) is provided with an interface 5 and an interface 6 which are interconnected, and an interface 7 and an interface 8 which are interconnected; the interface 1 is used to connect to the second evaporator, and the interface 2 is connected to the top of the solvent water separation tank (4) through a pipeline 3; the interface 5 is used to connect to the stripping tower, and the interface 6 is connected to the top of the solvent water separation tank (4) through a pipeline 4.

2. The plant oil processing gas-liquid separation energy-saving device according to claim 1, characterized in that: A plurality of annular nozzles (6) are evenly spaced and fixedly installed horizontally from top to bottom in the energy saver (1), and the plurality of annular nozzles (6) are respectively connected to the second pipeline, and a plurality of injection holes are evenly spaced on the upper and lower sides thereof; at least one flow plate (7) is obliquely fixedly installed in the region between two adjacent annular nozzles (6) in the energy saver (1).

3. The gas-liquid separation energy-saving device for vegetable oil processing according to claim 1, characterized in that: The internal space of the solvent water separation box (4) is divided into mutually independent primary separation chambers (8), secondary water chambers (9), secondary solvent chambers (10), tertiary solvent chambers (11) and tertiary water chambers (12) by a plurality of partitions; the primary separation chamber (8) is connected to the secondary water chamber (9) and the secondary solvent chamber (10); the secondary water chamber (9) is connected to the tertiary water chamber (12); and the secondary solvent chamber (10) is connected to the tertiary solvent chamber (11) via overflow pipes (13); the primary separation chamber (8) is connected to one end of the pipeline.

4. The gas-liquid separation energy-saving device for vegetable oil processing according to any one of claims 1 to 3, characterized in that: It also includes a normal pressure condenser (14), on which are provided an interface nine and an interface ten that are interconnected, and an interface eleven and an interface twelve that are interconnected; the top of the economizer (1), the interface nine, the interface ten, and the pipeline three are sequentially connected through pipelines; the interface seven, the interface eight, the interface three, the interface four, the interface eleven, and the interface twelve are sequentially connected through condensate pipelines, and the interface seven and the interface twelve are respectively used to connect to a condensate supply tank.

5. The gas-liquid separation energy-saving device for vegetable oil processing according to any one of claims 1 to 3, characterized in that: The invention also comprises a pre-evaporator (15), on which are provided an interface 13 and an interface 14 which are interconnected, and an interface 15 and an interface 16 which are interconnected; the interface 16 is connected to the mixed steam inlet on the economizer (1) through a pipeline, and the interface 15 is used to connect to the mixed steam outlet of the degassing machine; the interface 13 is used to connect to the mixed oil outlet of the extractor, and the interface 14 is used to connect to the second evaporator.

6. The gas-liquid separation energy-saving device for vegetable oil processing according to claim 5, characterized in that: The top of the pre-evaporator (15) is also connected to the area where the interface three and the interface four are connected through a pipeline.

7. The gas-liquid separation energy-saving device for vegetable oil processing according to claim 5, characterized in that: The pre-evaporator (15) is also provided with a mixed steam-liquid outlet connected to the area connected to the interface fifteen and the interface sixteen, and the mixed steam-liquid outlet is connected to the pipeline one through a pipeline.

8. The gas-liquid separation energy-saving device for vegetable oil processing according to any one of claims 1 to 3, characterized in that: One end of the pipeline three is connected to the pipeline one, and one end of the pipeline four is connected to the pipeline three.

9. The gas-liquid separation energy-saving device for vegetable oil processing according to any one of claims 1 to 3, characterized in that: The top of the solvent water distribution tank (4) is also connected to one end of a solvent supply pipeline, the other end of the solvent supply pipeline is used to connect to a solvent reservoir, and a solvent supply pump (16) is fixedly installed on the solvent supply pipeline.

10. The gas-liquid separation energy-saving device for vegetable oil processing according to any one of claims 1 to 3, characterized in that: The bottom of the solvent water distribution tank (4) is connected via one end of a solvent circulation pipeline, the other end of which is used to connect to an extractor, and a solvent circulation pump (17) and a solvent heater (20) are fixedly installed at intervals along the direction of solvent flow on the solvent circulation pipeline.

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