Production system for producing tea saponin by taking tea seed cake meal as raw material

Abstract

The utility model relates to a production system for producing tea saponin by taking tea seed cake meal as a raw material, which comprises an annular countercurrent leacher, a soaking type leacher, a tea seed oil extraction system, a tea saponin extraction system, a solvent A recovery system and a solvent B. The annular countercurrent leacher is used for leaching residual tea seed oil in the tea seed cake meal by using a solvent A; a discharge port of the annular countercurrent leacher is communicated with a feed port of the immersion type leacher through a scraper conveyer, degreased tea seed cakes leached by the annular countercurrent leacher are directly fed into the immersion type leacher through the scraper conveyer, the immersion type leacher leaches tea saponin by using a solvent B, the solvent A recovery system realizes recovery and cyclic utilization of the solvent A, and the solvent B recovery system realizes recovery and cyclic utilization of the solvent B; and the solvent B recovery system is used for recovering and recycling the solvent B. According to the device, not only can residual tea seed oil in the tea seed cake be extracted, but also tea saponin can be extracted, and the degreased tea seed cake can be directly used for producing the tea saponin, so that the transfer cost is reduced, the energy consumption is reduced, the energy is saved, and the cost is reduced.

Description

Technical Field

[0001] The utility model relates to the technical field of tea saponin production equipment, in particular to a production system for producing tea saponin by taking tea seed cake as raw material. Background Art

[0002] Tea seed is a unique oil crop in my country, with an annual production of about 600,000 tons of tea seed. Tea seed resources are abundant. Tea oil is produced from tea seeds through pressing and / or extraction. Tea seeds become tea seed cake after being pressed to produce oil, and tea seed meal after being extracted to produce oil. Both tea seed cake and tea seed meal contain 12% to 18% tea saponin and are the main raw materials for producing tea saponin. However, tea seed cake and tea seed meal also contain residual oil. Therefore, when tea seed cake and / or tea seed meal are used to produce tea saponin, they usually need to be defatted. After recovering the residual oil, the defatted tea seed cake and / or tea seed meal are used to produce tea saponin.

[0003] However, at present, the defatting production system of tea seed meal or / and tea seed meal and the production system of tea saponin from defatted tea seed cake or / and tea seed meal are two independent production systems. The defatted tea seed cake or / and tea seed meal produced by the defatting production system needs to be transferred and even temporarily stored before entering the tea saponin production system. The transfer and transportation or temporary storage will cause the defatted tea seed cake or / and tea seed meal to cool down, while the defatted tea seed cake or / and tea seed meal need to be soaked and heated during the production of tea saponin, which leads to a waste of energy. Moreover, the transfer and transportation or temporary storage also requires investment of manpower cost and equipment energy cost, which leads to an increase in the production cost of tea saponin. Utility Model Content

[0004] In view of this, in order to overcome the shortcomings of the existing technical problems, the utility model provides a production system for producing tea saponin using tea seed cake as raw material, which can extract both tea seed oil and tea saponin from the tea seed cake. The defatted tea seed cake after extracting the tea seed oil is directly used to produce tea saponin, thereby reducing transportation costs and reducing the energy consumption required for heating the defatted tea seed cake when producing tea saponin, saving energy and reducing costs.

[0005] In order to achieve the above-mentioned purpose, the technical solution provided by the present utility model is as follows:

[0006] A production system for producing tea saponin using tea seed cake as raw material, characterized by comprising:

[0007] The annular countercurrent extractor has a feed port for feeding tea seed cake, a solvent inlet connected to a solvent A storage tank, a liquid outlet connected to a tea seed oil extraction system, a discharge port connected to a feed port of an immersion extractor via a scraper conveyor, and an air inlet connected to a steam source. The annular countercurrent extractor utilizes solvent A to extract the tea seed oil remaining in the tea seed cake.

[0008] The immersion extractor has a solvent inlet connected to the solvent B storage tank, a liquid outlet connected to the tea saponin extraction system, a material outlet connected to the feed inlet of the degassing machine, and an air inlet connected to the steam source. The immersion extractor uses solvent B to extract tea saponin from the defatted tea seed cake.

[0009] The desolventizer uses steam to remove the solvent from the tea seed meal and dry the desolventized tea seed meal. The air inlet of the desolventizer is connected to the steam source, and the discharge port of the desolventizer is connected to the receiving system.

[0010] Tea seed oil extraction system, including:

[0011] The first separation device has a liquid inlet connected to a liquid outlet of the annular countercurrent extractor, a liquid phase outlet connected to a feed inlet of the evaporation system, and a solid phase outlet connected to a return port of the annular countercurrent extractor.

[0012] The evaporation system includes a first evaporator and a second evaporator connected in series, wherein the feed port of the first evaporator is connected to the liquid phase outlet of the first separation device, the discharge port of the first evaporator is connected to the feed port of the second evaporator, the discharge port of the second evaporator is connected to the feed port of the stripping tower, and the air inlet of the first evaporator and the air inlet of the second evaporator are both connected to a steam source.

[0013] The stripping tower has a discharge port connected to the crude oil storage tank, an air inlet connected to the steam source, and an air outlet connected to the stripping condenser.

[0014] Tea saponin extraction system, including:

[0015] The second separation device has a liquid inlet connected to a liquid outlet of the immersion extractor, a liquid phase outlet of the second separation device connected to a feed inlet of a primary concentration system, and a solid phase outlet of the second separation device connected to a return port of the immersion extractor.

[0016] The primary concentration system includes a third evaporator and a fourth evaporator connected in series, wherein the feed port of the third evaporator is connected to the liquid phase outlet of the second separation device, the discharge port of the third evaporator is connected to the feed port of the fourth evaporator, the discharge port of the fourth evaporator is connected to the feed port of the primary concentration tank, and the air inlet of the third evaporator and the air inlet of the fourth evaporator are both connected to the steam source.

[0017] The concentration system includes multiple evaporators arranged in parallel, the feed ports of the multiple evaporators are all connected to the discharge port of the primary concentration tank, the discharge ports of the multiple evaporators are all connected to the soap liquid pipeline, the soap liquid pipeline is connected to the feed port of the soap liquid storage tank through a pump, the discharge port of the soap liquid storage tank is connected to the tea saponin refining system through a pump and a pipeline, and the air inlet of the evaporator is connected to the steam source.

[0018] Furthermore, it also includes a pretreatment system, which includes a conveying device and a crushing device. The discharge port of the conveying device is connected to the feed port of the crushing device. The tea seed cake enters the crushing device through the conveying device for crushing, and the discharge port of the crushing device is connected to the feed port of the annular countercurrent extractor.

[0019] Furthermore, the invention also includes a solvent A recovery system, wherein the solvent A recovery system includes:

[0020] The evaporative condenser has an air inlet connected to the secondary steam outlet of the first evaporator and the secondary steam outlet of the second evaporator, and the condensate outlet of the evaporative condenser is connected to the solvent A water distribution tank. The evaporative condenser uses cooling water as a medium to condense the secondary steam generated by the first evaporator and the second evaporator. The air outlet of the evaporative condenser is connected to the air inlet of the tail gas condenser.

[0021] The stripping condenser has an air inlet connected to the air outlet of the stripping tower, and a condensate outlet of the stripping condenser is connected to the solvent A water distribution tank. The stripping condenser uses cooling water as a medium to condense the gas containing solvent A flowing out of the stripping tower, and the air outlet of the stripping condenser is connected to the air inlet of the tail gas condenser.

[0022] The solvent A water distribution tank is used to store the recovered condensate of the evaporative condenser and the condensate of the stripping condenser, and to separate solvent A from water. The solvent A water distribution tank has a solvent chamber and a water chamber. The water chamber and the solvent chamber are connected through an overflow. The solvent chamber has a solvent outlet. The solvent outlet is connected to the solvent inlet of the annular countercurrent extractor through a pipeline and a pump. The pipeline is provided with a solvent A heater. The solvent chamber is connected to the solvent A storage tank through a pipeline and a pump.

[0023] Furthermore, the invention also includes a solvent B recovery system, wherein the solvent B recovery system includes:

[0024] The degassing condenser, the air inlet of the degassing condenser is connected to the air outlet of the degassing machine, the condensate outlet of the degassing condenser is connected to the solvent B turnover tank, the degassing condenser uses cooling water as a medium to condense the tail gas containing solvent B discharged from the degassing machine, and the air outlet of the degassing condenser is connected to the air inlet of the tail gas condenser.

[0025] A primary concentrating condenser, wherein the air inlet of the primary concentrating condenser is connected to the secondary steam outlet of the third evaporator and the fourth evaporator, the condensate outlet of the primary concentrating condenser is connected to the solvent B turnover tank, the primary concentrating condenser uses cooling water as a medium to condense the secondary steam discharged from the third evaporator and the fourth evaporator, and the air outlet of the primary concentrating condenser is connected to the air inlet of the tail gas condenser,

[0026] The concentrating condenser has an air inlet connected to the secondary steam outlets of multiple evaporators of the concentrating system, and the condensate outlet of the concentrating condenser is connected to the solvent B recovery tank and the soap liquid pipeline respectively through pipelines. The concentrating condenser uses cooling water to condense the secondary steam discharged from the evaporator of the concentrating system. The liquid outlet of the solvent B recovery tank is connected to the solvent B turnover tank through a pipeline and a pump. The solvent B turnover tank is connected to the solvent B storage tank through a pipeline and a pump. The air outlet of the concentrating condenser is connected to the air inlet of the tail gas condenser.

[0027] Furthermore, the material receiving system includes a cyclone separator, packaging equipment, an air blower, and a dust collector. The feed port of the cyclone separator is connected to the discharge port of the degassing machine, the discharge port of the cyclone separator is connected to the packaging equipment, the air outlet of the cyclone separator is connected to the feed port of the dust collector, the discharge port of the dust collector is connected to the packaging equipment, the air outlet of the dust collector is connected to the air inlet of the air blower, and the air outlet of the air blower is discharged.

[0028] Furthermore, the first separation device and the second separation device both include a hydrocyclone, a filter and a mixed liquid storage tank. The feed port of the hydrocyclone of the first separation device is connected to the liquid outlet of the annular countercurrent extractor, the feed port of the hydrocyclone of the second separation device is connected to the liquid outlet of the immersion extractor, the liquid outlet of the hydrocyclone is connected to the liquid inlet of the filter, the liquid outlet of the filter is connected to the liquid inlet of the mixed liquid storage tank, the liquid outlet of the mixed liquid storage tank of the first separation device is connected to the liquid inlet of the evaporation system, the liquid outlet of the mixed liquid storage tank of the second separation device is connected to the liquid inlet of the primary concentration system, the solid phase outlet of the hydrocyclone of the first separation device, the filter residue outlet of the filter and the residue outlet of the mixed liquid storage tank are connected to the return port of the annular countercurrent extractor, and the solid phase outlet of the hydrocyclone of the second separation device, the filter residue outlet and the residue outlet of the mixed liquid storage tank are connected to the return port of the immersion extractor.

[0029] Furthermore, the first separation device and the second separation device include multiple hydrocyclones, which are connected in parallel or / and in series.

[0030] Furthermore, the tea seed oil extraction system also includes a crude oil cooling device, which is a heat exchanger. The feed port of the crude oil cooling device is connected to the discharge port of the stripping tower through a pipeline and a pump. The discharge port of the crude oil cooling device is connected to the crude oil storage tank. The crude oil cooling device uses cooling water as the medium to cool the crude oil.

[0031] Furthermore, it also includes a tail gas treatment system, the air outlet of the tail gas condenser is connected to the tail gas treatment system, the tail gas condenser uses cooling water as the medium to condense the tail gas, the condensate outlet of the tail gas condenser is connected to the liquid separator, the liquid outlet of the liquid separator is respectively connected to the solvent A water separator and the solvent B turnover tank, the tail gas treatment system includes a paraffin oil absorption tower, a water absorption tower, a paraffin oil cooler, a paraffin oil preheater, a paraffin oil heater and a parsing tower, the air outlet of the tail gas condenser is connected to the air inlet of the paraffin oil absorption tower, the air outlet of the paraffin oil absorption tower is connected to the air inlet of the water absorption tower, the oil inlet of the paraffin oil absorption tower is connected to the oil outlet of the paraffin oil cooler, the oil inlet of the paraffin oil cooler is connected to the hot oil outlet of the paraffin oil preheater, and the paraffin oil preheater is connected to the hot oil outlet of the paraffin oil preheater. The hot oil inlet of the decomposition device is connected to the oil outlet of the decomposition pump, the oil inlet of the decomposition pump is connected to the oil outlet of the decomposition tower, the oil inlet of the decomposition tower is connected to the oil outlet of the paraffin oil heater, the oil inlet of the paraffin oil heater is connected to the cold oil outlet of the paraffin oil preheater, the cold oil inlet of the paraffin oil preheater is connected to the oil outlet of the paraffin oil absorption pump, the oil inlet of the paraffin oil absorption pump is connected to the oil outlet of the paraffin oil absorption tower, the cooling medium inlet of the paraffin oil cooler is connected to the cooling water pipeline, the cooling medium outlet of the paraffin oil cooler is connected to the cooling water tank, the air outlet of the water absorption tower is connected to the exhaust fan, the water inlet of the water absorption tower is connected to the cooling water pipeline, the water outlet of the water absorption tower is connected to the water inlet of the water absorption pump, and the water outlet of the water absorption pump is connected to the circulating water inlet of the water absorption tower.

[0032] Furthermore, it also includes a cooling water system, which includes a cold water tank, a cooling water tower and a cooling water circulation pump. The water outlet of the cooling tower is connected to the return water port of the cooling water tank, and the water outlet of the cooling water tank is connected to the water inlet of the circulation pump. The water outlet of the circulation pump is connected to the cooling medium inlet of the stripping condenser, the cooling medium inlet of the evaporative condenser, the cooling medium inlet of the degassing condenser, the cooling medium inlet of the primary concentrating condenser, the cooling medium inlet of the concentrating condenser, the cooling medium inlet of the tail gas condenser, the cooling medium inlet of the crude oil cooling device and the cooling water pipeline through a pipeline. The cooling medium outlet of the stripping condenser, the cooling medium outlet of the evaporative condenser, the cooling medium outlet of the degassing condenser, the cooling medium outlet of the primary concentrating condenser, the cooling medium outlet of the concentrating condenser, the cooling medium outlet of the tail gas condenser, the cooling medium outlet of the crude oil cooling device and the cooling medium outlet of the paraffin oil cooler are all connected to the return water port of the cooling water tower.

[0033] The beneficial effects of the utility model are:

[0034] 1. The utility model can not only extract residual tea seed oil from tea seed cake, but also extract tea saponin from tea seed cake. The defatted tea seed cake after tea seed oil extraction is directly used to produce tea saponin, thereby reducing transportation costs and reducing the energy consumption required for heating the defatted tea seed cake when producing tea saponin, thus saving energy and reducing costs.

[0035] 2. The utility model has a solvent A recovery system and a solvent B recovery system. The solvent A recovery system is used to realize the recycling and reuse of solvent A, which can effectively reduce the consumption of solvent A. Similarly, the solvent B recovery system is used to realize the recycling and reuse of solvent B, which can effectively reduce the consumption of solvent B, thereby effectively reducing the production cost of tea saponin and tea seed oil.

[0036] 3. The secondary steam generated by the concentration system of the present invention is condensed by a concentration condenser to recover the solvent B and tea saponin carried in the secondary steam. The concentration condenser utilizes the difference between the boiling points of solvent B and tea saponin to condense the secondary steam at different condensation temperatures, thereby recovering the solvent B and tea saponin in the secondary steam respectively. BRIEF DESCRIPTION OF THE DRAWINGS

[0037] Figure 1 It is a structural diagram of the utility model;

[0038] Figure 2 This is a schematic diagram of the structure of the first separation device and the second separation device of the utility model

[0039] Figure 3 This is a schematic structural diagram of the exhaust gas treatment system of the present utility model;

[0040] Figure 4 It is a structural schematic diagram of the cooling water system of the present utility model.

[0041] Reference numerals:

[0042] Annular countercurrent extractor 1, first separation device 2, first evaporator 3, second evaporator 4, stripping tower 5, crude oil cooling device 6, crude oil storage tank 7, stripping condenser 8, evaporative condenser 9, solvent A water tank 10, solvent A storage tank 11, solvent A heater 12, conveying device 13, crushing device 14, scraper conveyor 15, immersion extractor 16, second separation device 17, third evaporator 18, fourth evaporator 19, concentration system 20, soap liquid storage tank 21, concentration condenser 23, primary concentration condenser 24, degassing condenser 25. Degassing machine 26. Cyclone separator 27. Dust collector 28. Air blower 29. Packaging equipment 31. Solvent B heater 30. Solvent B storage tank 32. Solvent B turnover tank 33. Solvent B recovery tank 34. Cooling tower 35. Cooling water tank 36. Atmospheric pressure condenser 37. Tail gas condenser 38. Liquid separator 39. Paraffin oil absorption tower 40. Water absorption tower 41. Tail gas blower 42. Desorption tower 43. Paraffin oil heater 44. Paraffin oil preheater 45. Paraffin oil cooler 46. Hydrocyclone separator 47. Filter 48. Mixed liquid storage tank 49 DETAILED DESCRIPTION

[0043] The present invention is described in further detail below with reference to the accompanying drawings and embodiments:

[0044] like Figure 1 、 Figure 2 、 Figure 3 and Figure 4 As shown, a production system for producing tea saponin using tea seed cake as raw material includes: a pretreatment system, a circular countercurrent extractor 1, an immersion extractor 16, a degassing machine 26, a tea seed oil extraction system, a tea saponin extraction system, a solvent A recovery system, a solvent B recovery system, an exhaust gas treatment system and a cooling water system.

[0045] The pretreatment system includes a conveying device 13 and a crushing device 14. The discharge port of the conveying device 13 is connected to the feed port of the crushing device 14. The tea seed cake enters the crushing device 14 through the conveying device 13 for crushing. The discharge port of the crushing device 14 is connected to the feed port of the annular countercurrent extractor 1. The solvent inlet of the annular countercurrent extractor 1 is connected to the solvent A recovery system. The liquid outlet of the annular countercurrent extractor 1 is connected to the tea seed oil extraction system. The discharge port of the annular countercurrent extractor 1 is connected to the feed port of the immersion extractor 16 through the scraper conveyor 15. The air inlet of the annular countercurrent extractor 1 is connected to the steam source. The annular countercurrent extractor 1 uses solvent A to extract the tea seed oil remaining in the tea seed cake.

[0046] The tea seed oil extraction system includes a first separation device 2, which includes two parallel-arranged hydrocyclones 47, a filter A and a mixed liquid storage tank A. The two parallel-arranged hydrocyclones 47 are respectively a first hydrocyclone and a second hydrocyclone. The feed port of the first hydrocyclone is connected to the liquid outlet of the annular countercurrent extractor 1, and the feed port of the second hydrocyclone is connected to the liquid outlet of the annular countercurrent extractor 1. The liquid phase outlet of the first hydrocyclone and the liquid phase outlet of the second hydrocyclone are both connected to the feed port of the filter A, the liquid phase outlet of the filter A is connected to the feed port of the mixed liquid storage tank A, and the discharge port of the mixed liquid storage tank A is connected to the feed port of the evaporation system. The solid phase outlet of the first hydrocyclone, the solid phase outlet of the second hydrocyclone, the solid phase outlet of the filter A and the slag outlet of the mixed liquid storage tank A are all connected to the return port of the annular countercurrent extractor 1. The evaporation system includes a first evaporator 3 and a second evaporator 4 connected in series. The air inlet of the first evaporator 3 and the air inlet of the second evaporator 4 are both connected to a steam source. The feed inlet of the first evaporator 3 is connected to the discharge outlet of the mixed liquid storage tank A via a pump and a pipeline. The discharge outlet of the first evaporator 3 is connected to the feed inlet of the second evaporator 4 via a pump and a pipeline. The discharge outlet of the second evaporator 4 is connected to the feed inlet of a stripping tower 5 via a pump and a pipeline. The discharge outlet of the stripping tower 5 is connected to the feed inlet of a crude oil cooling device 6 via a pipeline and a pump. The discharge outlet of the crude oil cooling device 6 is connected to a crude oil storage tank 7. The crude oil cooling device 6 is a heat exchanger that uses cooling water as a medium to cool the crude oil. The air inlet of the stripping tower 5 is connected to the steam source, and the air outlet of the stripping tower 5 is connected to the air inlet of a stripping condenser 8.

[0047] The solvent A recovery system includes an evaporative condenser 9, a stripping condenser 8, a solvent A water distribution tank 10 and a solvent A storage tank 11. The air inlet of the evaporative condenser 9 is connected to the secondary steam outlet of the first evaporator 3 and the secondary steam outlet of the second evaporator 4. The condensate outlet of the evaporative condenser 9 is connected to the solvent A water distribution tank 10. The evaporative condenser 9 uses cooling water as a medium to condense the secondary steam generated by the first evaporator 3 and the second evaporator 4. The air outlet of the evaporative condenser 9 is connected to the air inlet of the tail gas condenser 38. The air inlet of the stripping condenser 8 is connected to the air outlet of the stripping tower 5, and the condensate outlet of the stripping condenser 8 is connected to the solvent A water separation tank 10. The stripping condenser 8 uses cooling water as the medium to condense the gas containing solvent A flowing out of the stripping tower 5. The air outlet of the stripping condenser 8 is connected to the air inlet of the tail gas condenser 38. The solvent A water separation tank 10 is used to store the recovered condensate of the evaporative condenser 9 and the condensate of the stripping condenser 8, and to separate solvent A from water. The solvent A water separation tank 10 has a solvent cavity and a water cavity. The water cavity and the solvent cavity are connected through overflow. The solvent cavity has a solvent outlet. The solvent outlet is connected to the solvent inlet of the annular countercurrent extractor 1 through a pipeline and a pump. A solvent A heater 12 is provided on the pipeline. The solvent cavity is connected to the solvent A storage tank 11 through a pipeline and a pump.

[0048] The feed port of the immersion extractor 16 is connected to the discharge port of the annular countercurrent extractor 1 through the scraper conveyor 15, the solvent inlet of the immersion extractor 16 is connected to the solvent B recovery system, the liquid outlet of the immersion extractor 16 is connected to the tea saponin extraction system, the discharge port of the immersion extractor 16 is connected to the feed port of the degassing machine 26 through the lifting and conveying equipment, and the air inlet of the immersion extractor 16 is connected to the steam source. The immersion extractor 16 uses solvent B to extract tea saponin from the defatted tea seed cake, and the degassing machine 26 uses steam to dehumidify the residual solvent in the tea seed cake and dry and desolvate it. The wet tea seed meal is connected to the steam source through the air inlet of the degassing machine 26, and the discharge port of the degassing machine 26 is connected to the receiving system, which includes a cyclone separator 27, a packaging device 31, a blower 29, and a dust collector 28. The feed port of the cyclone separator 27 is connected to the discharge port of the degassing machine 26, the discharge port of the cyclone separator 27 is connected to the packaging device 31, the air outlet of the cyclone separator 27 is connected to the feed port of the dust collector 28, the discharge port of the dust collector 28 is connected to the packaging device 31, the air outlet of the dust collector 28 is connected to the air inlet of the blower 29, and the air outlet of the blower 29 is discharged.

[0049] The tea saponin extraction system includes a second separation device 17, which includes four parallel hydrocyclones 47, a filter B and a mixed liquid storage tank B. The four parallel hydrocyclones 47 are respectively a third hydrocyclone, a fourth hydrocyclone, a fifth hydrocyclone and a sixth hydrocyclone. The feed port of the third hydrocyclone, the feed port of the fourth hydrocyclone, the feed port of the fifth hydrocyclone and the feed port of the sixth hydrocyclone are all connected to the liquid outlet of the immersion extractor 16. The liquid phase outlet of the third hydrocyclone, the liquid phase outlet of the fourth hydrocyclone and the liquid phase outlet of the fifth hydrocyclone are connected to the liquid phase outlet of the sixth hydrocyclone. The liquid phase outlet of the liquid separator, the liquid phase outlet of the fifth hydrocyclone, and the liquid phase outlet of the sixth hydrocyclone are all connected to the feed port of the filter B, the liquid phase outlet of the filter B is connected to the feed port of the mixed liquid storage tank B, and the discharge port of the mixed liquid storage tank B is connected to the feed port of the primary concentration system through a pipeline and a pump. The solid phase outlet of the third hydrocyclone, the solid phase outlet of the fourth hydrocyclone, the solid phase outlet of the fifth hydrocyclone, the solid phase outlet of the sixth hydrocyclone, the solid phase outlet of the filter B and the slag outlet of the mixed liquid storage tank B are all connected to the return port of the immersion extractor 16.

[0050] The primary concentration system includes a third evaporator 18 and a fourth evaporator 19 connected in series. The feed port of the third evaporator 18 is connected to the discharge port of the mixed liquid storage tank B of the second separation device 17 through a pipeline and a pump. The discharge port of the third evaporator 18 is connected to the feed port of the fourth evaporator 19 through a pipeline and a pump. The discharge port of the fourth evaporator 19 is connected to the feed port of the primary concentration tank through a pipeline and a pump. The air inlet of the third evaporator 18 and the air inlet of the fourth evaporator 19 are both connected to the steam source. The concentration system 20 includes a plurality of evaporators arranged in parallel. The feed ports of the plurality of evaporators are all connected to the discharge port of the primary concentration tank. The discharge ports of the plurality of evaporators are all connected to the soap liquid pipeline. The soap liquid pipeline is connected to the feed port of the soap liquid storage tank 21 through a pump. The discharge port of the soap liquid storage tank 21 is connected to the tea saponin refining system 22 through a pump and a pipeline. The air inlet of the evaporator is connected to the steam source. The tea saponin refining system 22 includes an atomizer, a drying tower, a vibrating screen, and a solid tea saponin collecting tank, which are sequentially connected through a pump and a pipeline. The tea saponin refining system 22 is used to atomize and dry the soap liquid in the soap liquid storage tank 21 to produce solid tea saponin.

[0051] The solvent B recovery system includes an evaporative degassing condenser 25, a primary concentrating condenser 24, and a concentrating condenser 23. The air inlet of the evaporative degassing condenser 25 is connected to the air outlet of the evaporative degassing machine 26, and the condensate outlet of the evaporative degassing condenser 25 is connected to the solvent B turnover tank 33. The evaporative degassing condenser 25 uses cooling water as a medium to condense the tail gas containing solvent B discharged from the evaporative degassing machine 26. The air inlet of the primary concentrating condenser 24 is connected to the secondary steam outlets of the third evaporator 18 and the fourth evaporator 19, and the air outlet of the primary concentrating condenser 24 is connected to the air inlet of the tail gas condenser 38. The condensate outlet of the primary concentrating condenser 24 is connected to the solvent B turnover tank 33. The primary concentrating condenser 24 uses cooling water as a medium to condense the secondary steam discharged from the third evaporator 18 and the fourth evaporator 19. The air inlet of the concentrating condenser 23 is connected to the secondary steam outlet of multiple evaporators of the concentrating system 20. The condensate outlet of the concentrating condenser 23 is connected to the solvent B recovery tank 34 and the soap liquid pipeline through pipelines. The concentrating condenser 23 uses cooling water to condense the secondary steam discharged from the evaporator of the concentrating system 20. The liquid outlet of the solvent B recovery tank 34 is connected to the solvent B turnover tank 33 through a pipeline and a pump. The solvent B turnover tank 33 is connected to the solvent B storage tank 32 through a pipeline and a pump.

[0052] The outlet of the tail gas condenser 38 is connected to the tail gas treatment system. The tail gas condenser 38 uses cooling water as the medium to condense the tail gas. The air inlet of the tail gas condenser 38 is connected to the air outlet of the stripping condenser 8, the air outlet of the evaporative condenser 9, the air outlet of the steam stripping condenser 25, the air outlet of the primary concentration condenser 24, the air outlet of the concentration condenser 23 and the air outlet of the atmospheric condenser 37 through a pipeline. The condensate outlet of the tail gas condenser 38 is connected to the solvent A water tank 10. The air outlet of the tail gas condenser 38 is connected to the tail gas treatment system. The system includes a paraffin oil absorption tower 40, a water absorption tower 41, a paraffin oil cooler 46, a paraffin oil preheater 45, a paraffin oil heater 44, a parsing tower 43 and a normal pressure condenser 37. The air outlet of the tail gas condenser 38 is connected to the air inlet of the paraffin oil absorption tower 40, the air outlet of the paraffin oil absorption tower 40 is connected to the air inlet of the water absorption tower 41, the air outlet of the water absorption tower 41 is connected to the tail gas fan 42, the water inlet of the water absorption tower 41 is connected to the cooling water pipeline, the water outlet of the water absorption tower 41 is connected to the water inlet of the water absorption pump, and the water outlet of the water absorption pump is connected to the water absorption pump. The circulating water inlet of the collecting tower 41, the oil inlet of the paraffin oil absorption tower 40 is connected to the oil outlet of the paraffin oil cooler 46, the oil inlet of the paraffin oil cooler 46 is connected to the hot oil outlet of the paraffin oil preheater 45, the hot oil inlet of the paraffin oil preheater 45 is connected to the oil outlet of the analytical pump, the oil inlet of the analytical pump is connected to the oil outlet of the analytical tower 43, the oil inlet of the analytical tower 43 is connected to the oil outlet of the paraffin oil heater 44, the oil return port of the paraffin oil heater 44 is connected to the cold oil outlet of the paraffin oil preheater 45, and the cold oil inlet of the paraffin oil preheater 45 is connected The oil outlet of the paraffin oil absorption pump and the oil inlet of the paraffin oil absorption pump are connected to the oil outlet of the paraffin oil absorption tower 40, the cooling medium inlet of the paraffin oil cooler 46 is connected to the cooling water pipeline, the cooling medium outlet of the paraffin oil cooler 46 is connected to the cooling water tank 36, the air inlet of the decomposition tower 43 is connected to the steam source, the air outlet of the decomposition tower 43 is connected to the air inlet of the normal pressure condenser 37 through a pipeline, the air outlet of the normal pressure condenser 37 is connected to the air inlet of the tail gas condenser 38, and the normal pressure condenser 37 uses cooling water as the cooling medium to condense the decomposition gas discharged from the decomposition tower 43.

[0053] The stripping condenser 8, evaporation condenser 9, evaporation condenser 25, primary concentration condenser 24, concentration condenser 23, tail gas condenser 38, atmospheric condenser 37, crude oil cooling device 6 and paraffin oil cooler 46 all use cooling water as cooling medium. The cooling water system provides cooling water. The cooling water system includes a cold water tank, a cooling water tower 35 and a cooling water circulation pump. The water outlet of the cooling tower is connected to the return water port of the cooling water tank 36. The water outlet of the cooling water tank 36 is connected to the water inlet of the circulation pump. The water outlet of the circulation pump is connected to the cooling medium inlet of the stripping condenser 8, the cooling medium inlet of the evaporation condenser 9, the cooling medium inlet of the evaporation condenser 25, The cooling medium inlet of the primary concentrating condenser 24, the cooling medium inlet of the concentrating condenser 23, the cooling medium inlet of the tail gas condenser 38, the cooling medium inlet of the crude oil cooling device 6, the cooling medium inlet and the cooling water pipeline of the atmospheric condenser 37, the cooling medium outlet of the stripping condenser 8, the cooling medium outlet of the evaporative condenser 9, the cooling medium outlet of the degassing condenser 25, the cooling medium inlet of the primary concentrating condenser 24, the cooling medium outlet of the concentrating condenser 23, the cooling medium outlet of the tail gas condenser 38, the cooling medium outlet of the atmospheric condenser 37, the cooling medium outlet of the crude oil cooling device 6 and the cooling medium outlet of the paraffin oil cooler 46 are all connected to the return water port of the cooling water tower 35.

[0054] During use, the tea seed cake is conveyed to the pulverizing device 14 through the conveying device 13 and pulverized. The pulverized tea seed cake enters the annular countercurrent extractor 1. The solvent A in the solvent A storage tank 11 enters the solvent A heater 12 under the conveying action of the pump. The solvent A is heated by steam in the heater. The heated solvent A enters the annular countercurrent extractor 1. At the same time, steam is added to the annular countercurrent extractor 1. In the annular countercurrent extractor 1, the pulverized tea seed cake is immersed in the solvent A, and the tea seed oil remaining in the tea seed cake is dissolved. The tea seed cake is then fed into the solvent A to become defatted tea seed cake. The defatted tea seed cake is then conveyed to the immersion extractor 16 via a scraper conveyor 15. The solvent A containing tea seed oil enters the first separation device 2 under the action of the pump, and is subjected to solid-liquid separation by the first hydrocyclone and the second hydrocyclone. The separated solid phase material is returned to the annular countercurrent extractor 1, and the liquid phase material at the separation enters the filter A. After being filtered by the filter A, the filtrate enters the mixed liquid storage tank A for temporary storage, and the filter residue is returned to the annular countercurrent extractor 1.

[0055] The filtrate containing tea seed oil in the mixed liquid storage tank A enters the first evaporator 3 under the action of the pump. The steam provided by the steam source enters the first evaporator 3 as a heating medium. The steam heats the filtrate to cause the filtrate to heat up and evaporate. The water in the filtrate heats up and becomes secondary steam. The filtrate is evaporated and concentrated. The filtrate after evaporation and concentration in the first evaporator 3 enters the second evaporator 4 under the action of the pump. The second evaporator 4 uses steam as a heat source to evaporate and concentrate the filtrate again to become a concentrated liquid containing tea seed oil, generating secondary steam. Since the boiling point of tea seed oil is much higher than the boiling point of water and the boiling point of solvent A, the secondary steam generated by the first evaporator 3 and the second evaporator 4 during the evaporation and concentration process contains water vapor and vaporized solvent A. The secondary steam generated by the first evaporator 3 and the second evaporator 4 enters the evaporative condenser 9. The cooling water system provides cooling water as a cooling medium for the evaporative condenser 9. The secondary steam is condensed by the cooling water. Since the boiling point of solvent A is higher than the boiling point of water, most of the condensate flowing out of the condensate outlet of the evaporative condenser 9 is liquid solvent A and a small amount of water. The concentrated liquid containing tea seed oil enters the stripping tower 5, and the concentrated liquid containing tea seed oil is stripped by steam. The residual solvent A in the concentrated liquid is stripped out, and the stripped solvent A enters the stripping condenser 8 in gaseous state. The concentrated liquid after stripping becomes crude oil, which is cooled by the crude oil cooling device 6 and then stored in the crude oil storage tank 7. The gas entering the stripping condenser 8 contains gaseous solvent A and water vapor. Similarly, since the boiling point of solvent A is higher than that of water, the gaseous solvent A in the gas in the stripping condenser 8 is first condensed into liquid. Therefore, the stripping The condensate flowing out of the condensate outlet of the condenser 8 is mostly liquid solvent A and a small amount of water. The condensate of the stripping condenser 8 and the condensate of the evaporative condenser 9 both enter the solvent A water tank 10. The inner cavity of the solvent A water tank 10 is divided into a solvent cavity and a water cavity. The condensate enters the water cavity. Since the specific gravity of solvent A is lower than that of water, solvent A is located in the upper layer. When the overflow port in the water cavity is higher than the overflow port connecting the solvent cavity and the water cavity, the solvent A located in the upper layer enters the solvent cavity first. A drain port can be set at the lower end of the water cavity to discharge excess water. The solvent A entering the solvent cavity enters the solvent A heater 12 under the action of the pump, thereby realizing the recycling and reuse of solvent A, and the solvent A in the solvent A storage tank 11 is connected to the solvent cavity of the solvent A water tank 10 under the action of the pump to replenish solvent A for the system.

[0056] The defatted tea seed cake is conveyed to the immersion extractor 16 via a scraper conveyor 15. Solvent B in the solvent B storage tank 32 is pumped into the solvent B heater 30, where it is heated by steam. The heated solvent B then enters the immersion extractor 16, where steam is simultaneously added. Solvent B then soaks the defatted tea seed cake in the immersion extractor 16, causing the tea saponins in the defatted tea seed cake to dissolve in the solvent B. The defatted tea seed cake, which flows out of the immersion extractor 16, enters the degassing machine 26, where steam is used to degas and dry the tea seed cake to remove the solvent B. The degassing and dried tea seed cake is then conveyed by the air blower 29 to the cyclone separator 27 for collection, packaging, and storage. The exhaust gas then enters the dust collector 28 for dust removal and discharge. This completes the collection of the defatted and tea saponin-extracted tea seed cake.

[0057] The mixed solution flowing out of the liquid outlet of the immersion extractor 16 contains solvent B, water, tea saponin and residue. The mixed solution enters the second separation device 17, and is first separated into solid and liquid by the third hydrocyclone, the fourth hydrocyclone, the fifth hydrocyclone and the sixth hydrocyclone. The separated solid phase material flows back into the immersion extractor 16, and the separated liquid phase material enters the filter B for filtration. The residue filtered out by the filter B flows back into the immersion extractor 16, and the filtered filtrate enters the mixed liquid storage tank B for temporary storage.

[0058] The filtrate containing tea saponin in the mixed liquid storage tank B enters the third evaporator 18 under the action of the pump. The steam provided by the steam source enters the third evaporator 18 as a heating medium. The steam heats the filtrate to cause the filtrate to evaporate. The water in the filtrate is heated to become secondary steam. The filtrate is evaporated and concentrated. The filtrate evaporated and concentrated by the third evaporator 18 enters the fourth evaporator 19 under the action of the pump. The fourth evaporator 19 uses steam as a heat source to evaporate and concentrate the filtrate again to become a primary concentrated liquid containing tea saponin, generating secondary steam. The primary concentrated liquid enters the primary concentration tank for temporary storage under the action of the pump. Since the boiling point of solvent B is lower than that of water, the third evaporator 18 and the fourth evaporator The secondary steam generated by the third and fourth evaporators 19 contains water vapor and vaporized solvent B. The secondary steam generated by the third and fourth evaporators 19 enters the primary concentrator condenser 24. The primary concentrator condenser 24 uses cooling water as the cooling medium to condense the secondary steam. Because the boiling point of solvent B is lower than that of water, the solvent B in the secondary steam is first condensed into liquid. The condensate flowing out of the condensate outlet of the primary concentrator condenser 24 is composed of mostly solvent B and a small amount of water. The condensate enters the solvent B turnover tank 33 for storage and then enters the solvent B heater 30 under the action of a pump. After reheating, it is transported to the immersion extractor 16, thereby realizing the recovery and reuse of solvent B. The solvent B in the solvent B storage tank 32 is used as a supplementary solvent.

[0059] The primary concentrate containing tea saponin in the primary concentration tank enters the concentration system 20, which has multiple evaporators arranged in parallel. The primary concentrate enters each evaporator separately, and steam provided by a steam source enters each evaporator separately. The evaporators use steam as a heat source to heat the primary concentrate, re-concentrating the primary concentrate to form a crude tea saponin solution. The crude tea saponin solution enters the soap liquid storage tank 21 under the action of a pump, and then enters the tea saponin refining system 22 under the action of a pump to produce powdered finished tea saponin. The secondary steam generated by the evaporators in the concentration system 20 enters the concentration evaporator. The secondary steam contains water vapor, tea saponin, and solvent B. Because the boiling point of solvent B is lower than that of water, when the concentration evaporator condenses the secondary steam, the water vapor in the secondary steam first condenses into water, carrying the tea saponin into the soap liquid storage tank 21. The solvent B then condenses into a liquid solvent. The liquid solvent B enters the solvent B recovery tank 34 and then enters the solvent B turnover tank 33 under the action of a pump. This completes the production and extraction of tea saponin.

[0060] The tail gas flowing out of the outlet of the stripping condenser 8, the tail gas flowing out of the outlet of the evaporative condenser 9, the tail gas flowing out of the outlet of the degassing condenser 25, the tail gas flowing out of the outlet of the primary concentration condenser 24, and the tail gas flowing out of the outlet of the concentration condenser 23 all enter the tail gas condenser 38. The tail gas condenser 38 condenses various tail gases, and the condensate enters the separator tank 39. The condensate contains water, a small amount of solvent A and a small amount of solvent B. The inner cavity of the separator tank 39 is divided into three cavities. The different specific gravities of solvent A, solvent B and water are also used to form stratification, and the overflow is used to separate the three. Solvent A enters the solvent A water separation tank 10, and solvent B enters the solvent B turnover tank 33. The gas flowing out of the outlet of the tail gas condenser 38 enters the tail gas treatment system, is first absorbed by paraffin oil and then absorbed by water, and the treated tail gas is discharged into the atmosphere. The paraffin oil after the tail gas absorption enters the decomposition tower 43 for decomposition, and the impurities absorbed enter the atmospheric pressure condenser 37 with the steam instrument for condensation and then re-enter the tail gas condenser 38. The condensate of the atmospheric pressure condenser 37 enters the solvent A water distribution tank 10.

[0061] It should be noted that the above embodiments are illustrative of the technical solutions of the present invention rather than limiting. Equivalent substitutions or other modifications made by ordinary technicians in the relevant technical field based on the existing technology should be included in the scope of rights required by the present invention as long as they do not exceed the concept and scope of the technical solutions of the present invention.

Claims

1. A production system for producing tea saponin using tea seed cake as raw material, characterized by: include: The annular countercurrent extractor (1) has a feed port for feeding tea seed cake, a solvent inlet connected to a solvent A storage tank (11), a liquid outlet connected to a tea seed oil extraction system, a discharge port connected to a feed port of an immersion extractor (16) via a scraper conveyor (15), and an air inlet connected to a steam source. The annular countercurrent extractor (1) utilizes solvent A to extract the tea seed oil remaining in the tea seed cake. The immersion extractor (16) has a solvent inlet connected to the solvent B storage tank (32), a liquid outlet connected to the tea saponin extraction system, a material outlet connected to the feed inlet of the degassing machine (26), and an air inlet connected to the steam source. The immersion extractor (16) uses solvent B to extract tea saponin from the defatted tea seed cake. The desolventizer (26) uses steam to dehumidify the solvent of the tea seed meal and dry the desolventized wet tea seed meal. The air inlet of the desolventizer (26) is connected to the steam source, and the discharge port of the desolventizer (26) is connected to the material receiving system. Tea seed oil extraction system, including: The first separation device (2) has a liquid inlet connected to the liquid outlet of the annular countercurrent extractor (1), a liquid phase outlet of the first separation device (2) connected to the feed inlet of the evaporation system, and a solid phase outlet of the first separation device (2) connected to the return port of the annular countercurrent extractor (1). The evaporation system comprises a first evaporator (3) and a second evaporator (4) connected in series, wherein the feed port of the first evaporator (3) is connected to the liquid phase outlet of the first separation device (2), the discharge port of the first evaporator (3) is connected to the feed port of the second evaporator (4), the discharge port of the second evaporator (4) is connected to the feed port of the stripping tower (5), and the air inlet of the first evaporator (3) and the air inlet of the second evaporator (4) are both connected to a steam source. A stripping tower (5), wherein the discharge port of the stripping tower (5) is connected to the crude oil storage tank (7), the air inlet of the stripping tower (5) is connected to the steam source, and the air outlet of the stripping tower (5) is connected to the stripping condenser (8). Tea saponin extraction system, including: The second separation device (17) has a liquid inlet connected to a liquid outlet of the immersion extractor (16), a liquid phase outlet of the second separation device (17) connected to a feed inlet of the primary concentration system, and a solid phase outlet of the second separation device (17) connected to a return port of the immersion extractor (16). The primary concentration system comprises a third evaporator (18) and a fourth evaporator (19) connected in series, wherein the feed port of the third evaporator (18) is connected to the liquid phase outlet of the second separation device (17), the discharge port of the third evaporator (18) is connected to the feed port of the fourth evaporator (19), the discharge port of the fourth evaporator (19) is connected to the feed port of the primary concentration tank, and the air inlet of the third evaporator (18) and the air inlet of the fourth evaporator (19) are both connected to the steam source. A concentration system (20), wherein the concentration system (20) comprises a plurality of evaporators arranged in parallel, wherein the feed ports of the plurality of evaporators are all connected to the discharge ports of the primary concentration tank, and the discharge ports of the plurality of evaporators are all connected to the soap liquid pipeline, the soap liquid pipeline is connected to the feed port of the soap liquid storage tank (21) through a pump, and the discharge port of the soap liquid storage tank (21) is connected to the tea saponin refining system (22) through a pump and a pipeline, and the air inlet of the evaporator is connected to the steam source.

2. The production system for producing tea saponin using tea seed cake as raw material according to claim 1, characterized in that: The invention also includes a pretreatment system, wherein the pretreatment system includes a conveying device (13) and a crushing device (14), wherein the discharge port of the conveying device (13) is connected to the feed port of the crushing device (14), and the tea seed cake enters the crushing device (14) through the conveying device (13) for crushing, and the discharge port of the crushing device (14) is connected to the feed port of the annular countercurrent extractor (1).

3. The production system for producing tea saponin using tea seed cake as raw material according to claim 1, characterized in that: Also included is a solvent A recovery system, the solvent A recovery system comprising: An evaporative condenser (9), wherein the air inlet of the evaporative condenser (9) is connected to the secondary steam outlet of the first evaporator (3) and the secondary steam outlet of the second evaporator (4), and the condensate outlet of the evaporative condenser (9) is connected to the solvent A water distribution tank (10). The evaporative condenser (9) uses cooling water as a medium to condense the secondary steam generated by the first evaporator (3) and the second evaporator (4). The air outlet of the evaporative condenser (9) is connected to the air inlet of the tail gas condenser (38). The stripping condenser (8) has an air inlet connected to the air outlet of the stripping tower (5), and a condensate outlet of the stripping condenser (8) is connected to the solvent A water distribution tank (10). The stripping condenser (8) uses cooling water as a medium to condense the gas containing solvent A flowing out of the stripping tower (5). The air outlet of the stripping condenser (8) is connected to the air inlet of the tail gas condenser (38). The solvent A water separation tank (10) is used to store the recovered condensate of the evaporation condenser (9) and the condensate of the stripping condenser (8), and to separate the solvent A from water. The solvent A water separation tank (10) has a solvent chamber and a water chamber. The water chamber and the solvent chamber are connected through an overflow. The solvent chamber has a solvent outlet. The solvent outlet is connected to the solvent inlet of the annular countercurrent extractor (1) through a pipeline and a pump. The pipeline is provided with a solvent A heater 12. The solvent chamber is connected to the solvent A storage tank (11) through a pipeline and a pump.

4. The production system for producing tea saponin using tea seed cake as raw material according to claim 1, characterized in that: Also included is a solvent B recovery system, the solvent B recovery system comprising: The degassing condenser (25) has an air inlet connected to the air outlet of the degassing machine (26), and a condensate outlet of the degassing condenser (25) is connected to the solvent B turnover tank (33). The degassing condenser (25) uses cooling water as a medium to condense the tail gas containing solvent B discharged from the degassing machine (26). The air outlet of the degassing condenser (25) is connected to the air inlet of the tail gas condenser (38). A primary concentrating condenser (24), wherein the air inlet of the primary concentrating condenser (24) is connected to the secondary steam outlet of the third evaporator (18) and the fourth evaporator (19), the air outlet of the primary concentrating condenser (24) is connected to the air inlet of the tail gas condenser (38), and the condensate outlet of the primary concentrating condenser (24) is connected to the solvent B turnover tank (33). The primary concentrating condenser (24) uses cooling water as a medium to condense the secondary steam discharged from the third evaporator (18) and the fourth evaporator (19). The concentrating condenser (23) has an air inlet connected to the secondary steam outlets of multiple evaporators of the concentrating system (20), and the condensate outlet of the concentrating condenser (23) is connected to the solvent B recovery tank (34) and the soap liquid pipeline respectively through pipelines. The concentrating condenser (23) uses cooling water to condense the secondary steam discharged from the evaporator of the concentrating system (20). The liquid outlet of the solvent B recovery tank (34) is connected to the solvent B turnover tank (33) through a pipeline and a pump. The solvent B turnover tank (33) is connected to the solvent B storage tank (32) through a pipeline and a pump. The air outlet of the concentrating condenser (23) is connected to the air inlet of the tail gas condenser (38).

5. The production system for producing tea saponin using tea seed cake as raw material according to claim 1, characterized in that: The material receiving system includes a cyclone separator (27), a packaging device (31), an air blower (29), and a dust collector (28). The feed port of the cyclone separator (27) is connected to the discharge port of the degassing machine (26), the discharge port of the cyclone separator (27) is connected to the packaging device (31), the air outlet of the cyclone separator (27) is connected to the feed port of the dust collector (28), the discharge port of the dust collector (28) is connected to the packaging device (31), the air outlet of the dust collector (28) is connected to the air inlet of the air blower (29), and the air outlet of the air blower (29) is emptied.

6. The production system for producing tea saponin using tea seed cake as raw material according to claim 1, characterized in that: The first separation device (2) and the second separation device (17) both include a hydrocyclone (47), a filter (48) and a mixed liquid storage tank (49). The feed port of the hydrocyclone (47) of the first separation device (2) is connected to the liquid outlet of the annular countercurrent extractor (1). The feed port of the hydrocyclone (47) of the second separation device (17) is connected to the liquid outlet of the immersion extractor (16). The liquid outlet of the hydrocyclone (47) is connected to the liquid inlet of the filter (48). The liquid outlet of the filter (48) is connected to the liquid inlet of the mixed liquid storage tank (49). The first separation device (2) The liquid outlet of the mixed liquid storage tank (49) is connected to the liquid inlet of the evaporation system, the liquid outlet of the mixed liquid storage tank (49) of the second separation device (17) is connected to the liquid inlet of the primary concentration system, the solid phase outlet of the hydrocyclone (47) of the first separation device (2), the filter residue outlet of the filter (48) and the residue outlet of the mixed liquid storage tank (49) are connected to the return material port of the annular countercurrent extractor (1), and the solid phase outlet of the hydrocyclone (47) of the second separation device (17), the filter residue outlet of the filter (48) and the residue outlet of the mixed liquid storage tank (49) are connected to the return material port of the immersion extractor (16).

7. The production system for producing tea saponin using tea seed cake as raw material according to claim 6, characterized in that: The number of the hydrocyclones (47) in the first separation device (2) and the second separation device (17) is multiple, and the multiple hydrocyclones (47) are connected in parallel or / and in series.

8. The production system for producing tea saponin using tea seed cake as raw material according to claim 1, characterized in that: The tea seed oil extraction system further comprises a crude oil cooling device (6), which is a heat exchanger. The feed port of the crude oil cooling device (6) is connected to the discharge port of the stripping tower (5) through a pipeline and a pump, and the discharge port of the crude oil cooling device (6) is connected to the crude oil storage tank (7). The crude oil cooling device (6) uses cooling water as a medium to cool the crude oil.

9. The production system for producing tea saponin using tea seed cake as raw material according to any one of claims 1 to 8, characterized in that: The tail gas treatment system is also included. The outlet of the tail gas condenser (38) is connected to the tail gas treatment system. The tail gas condenser (38) uses cooling water as a medium to condense the tail gas. The condensate outlet of the tail gas condenser (38) is connected to the liquid separation box (39). The liquid outlet of the liquid separation box (39) is respectively connected to the solvent A water separation tank (10) and the solvent B turnover tank (33). The tail gas treatment system includes a paraffin oil absorption tower (40), a water absorption tower (41), a paraffin oil cooler (46), paraffin oil preheater (45), paraffin oil heater (44) and analysis tower (43), the air outlet of the tail gas condenser (38) is connected to the air inlet of the paraffin oil absorption tower (40), the air outlet of the paraffin oil absorption tower (40) is connected to the air inlet of the water absorption tower (41), the oil inlet of the paraffin oil absorption tower (40) is connected to the oil outlet of the paraffin oil cooler (46), and the oil inlet of the paraffin oil cooler (46) is connected to the hot oil outlet of the paraffin oil preheater (45). The hot oil inlet of the paraffin oil preheater (45) is connected to the oil outlet of the analytical pump, the oil inlet of the analytical pump is connected to the oil outlet of the analytical tower (43), the oil inlet of the analytical tower (43) is connected to the oil outlet of the paraffin oil heater (44), the oil inlet of the paraffin oil heater (44) is connected to the cold oil outlet of the paraffin oil preheater (45), the cold oil inlet of the paraffin oil preheater (45) is connected to the oil outlet of the paraffin oil absorption pump, and the oil inlet of the paraffin oil absorption pump is connected to the paraffin oil The oil outlet of the absorption tower (40) and the cooling medium inlet of the paraffin oil cooler (46) are connected to the cooling water pipeline, the cooling medium outlet of the paraffin oil cooler (46) is connected to the cooling water tank (36), the air outlet of the water absorption tower (41) is connected to the exhaust fan (42), the water inlet of the water absorption tower (41) is connected to the cooling water pipeline, the water outlet of the water absorption tower (41) is connected to the water inlet of the water absorption pump, and the water outlet of the water absorption pump is connected to the circulating water inlet of the water absorption tower (41).

10. The production system for producing tea saponin using tea seed cake as raw material according to claim 9, characterized in that: The cooling water system includes a cold water tank, a cold water tower (35) and a cooling water circulation pump. The water outlet of the cooling tower is connected to the return water port of the cooling water tank (36). The water outlet of the cooling water tank (36) is connected to the water inlet of the circulation pump. The water outlet of the circulation pump is connected to the cooling medium inlet of the stripping condenser (8), the cooling medium inlet of the evaporation condenser (9), the cooling medium inlet of the degassing condenser (25), the cooling medium inlet of the primary concentration condenser (24), the cooling medium inlet of the concentration condenser (23), and the exhaust gas inlet through a pipeline. The cooling medium inlet of the condenser (38), the cooling medium inlet and cooling water pipeline of the crude oil cooling device (6), the cooling medium outlet of the stripping condenser (8), the cooling medium outlet of the evaporative condenser (9), the cooling medium outlet of the degassing condenser (25), the cooling medium inlet of the primary concentration condenser (24), the cooling medium outlet of the concentration condenser (23), the cooling medium outlet of the tail gas condenser (38), the cooling medium outlet of the crude oil cooling device (6) and the cooling medium outlet of the paraffin oil cooler (46) are all connected to the return water inlet of the cooling tower (35).

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