Method for treating carotenoid wash water

Abstract

The present application relates to a kind of carotenoid cleaning water processing method.The processing method described in the present application includes: carotenoid cleaning water is mixed with dichloromethane, under the shearing action of linear velocity 10m / s-20m / s, obtain carotenoid coarse emulsion;The first mixed liquor and pretreated carotenoid cleaning water are obtained by separating the carotenoid coarse emulsion;The first mixed liquor is recycled to obtain carotenoid recovery product.The processing method described in the present application significantly improves the recovery rate of carotenoid, and the amount of dichloromethane is less, and the recovery process is simple and efficient, and the quality of carotenoid prepared is high.

Description

Technical Field

[0001] This invention relates to the field of food industry technology, and in particular to a method for treating carotenoid washing water. Background Technology

[0002] Carotenoids mainly include β-carotene, lutein, lycopene, astaxanthin, canthaxanthin, and aconitine. Carotenoids are widely used in food processing technology and are extremely important pigments and dietary supplements. As an important food-grade pigment, carotenoids generally possess highly recognizable characteristic colors. When switching production lines for carotenoid formulations, a thorough cleaning of the entire production line is required to prevent residual carotenoids from contaminating subsequent products. Due to the strong coloring power of carotenoids, a large amount of cleaning water is generated during cleaning, and this water is very dark in color, placing a heavy burden on wastewater treatment plants.

[0003] Carotenoid washing water is typically treated using the following methods: 1. Directly send the carotenoid washing water to a wastewater treatment plant for conventional treatment methods such as anaerobic and aerobic processes; 2. Add an extractant to extract the carotenoids from the washing water, and then send the extracted carotenoid washing water to a wastewater treatment plant for further treatment; 3. Add a metal catalyst to the carotenoid washing water to catalytically oxidize and destroy the carotenoids before sending it to a wastewater treatment plant for further treatment; 4. Use a combination of the above methods to treat the carotenoid washing water.

[0004] The above methods have the following problems when treating carotenoid washing water: a) Carotenoids in the washing water are not utilized or the recovery rate is low; b) When using solvent extraction, since the total amount of carotenoid washing water is generally 1 to 5 times the total volume of the equipment being cleaned, the amount of extractant used is extremely large, the extraction equipment is huge, and the recovery cost is high. Summary of the Invention

[0005] Therefore, it is necessary to provide a method for treating carotenoid washing water to address the above problems; the treatment method significantly improves the recovery rate of carotenoids, uses less dichloromethane, has a simple and efficient recovery process, and produces high-quality carotenoids.

[0006] A method for treating carotenoid washing water includes the following steps:

[0007] Carotenoid washing water was mixed with dichloromethane and subjected to shearing at a linear velocity of 10 m / s-20 m / s to obtain a crude carotenoid emulsion.

[0008] The crude carotenoid emulsion was separated to obtain a first mixture and pretreated carotenoid washing water;

[0009] The first mixture is recycled to obtain carotenoid recovery product.

[0010] In one embodiment, in the step of mixing the carotenoid washing water with dichloromethane, the mass ratio of the dichloromethane to the carotenoid in the carotenoid washing water is 10:1-30:1.

[0011] In one embodiment, during the shearing process with a linear velocity of 10 m / s to 20 m / s, the temperature is 15°C to 40°C.

[0012] In one embodiment, the method for separating the crude carotenoid emulsion is selected from centrifugal separation, with a centrifugation factor of 500-1500.

[0013] In one embodiment, activated carbon is used to adsorb the pretreated carotenoid washing water, and dichloromethane is used to desorb the adsorbed activated carbon to obtain a second mixture. The second mixture is then recycled to obtain a carotenoid recovery product.

[0014] In one embodiment, the mass ratio of the activated carbon to the pretreated carotenoid washing water is 0.001:1 to 0.005:1.

[0015] In one embodiment, in the step of desorbing the adsorbed activated carbon with dichloromethane, the mass ratio of dichloromethane to the adsorbed activated carbon is 5:1-20:1.

[0016] In one embodiment, the desorbed activated carbon is recycled to adsorb the pretreated carotenoid washing water.

[0017] In one embodiment, the first mixture and the second mixture are combined for recycling.

[0018] In one embodiment, the recycling process includes: mixing the first mixture, the second mixture, and water, and then distilling to obtain dichloromethane and carotenoid recoveries.

[0019] In one embodiment, the mass of the water is 0.1 to 2.0 times the total mass of the first mixture and the second mixture.

[0020] In one embodiment, dichloromethane obtained by distillation is recycled for use in the shearing step and / or desorption step.

[0021] The processing method described in this invention, by strictly controlling the mixing shear velocity of carotenoid washing water and dichloromethane to 10 m / s-20 m / s, completely disrupts the original 0.15 μm-2 μm microparticle oil-in-water emulsion system in the carotenoid washing water. This allows dichloromethane to extract the carotenoid microparticles from the original oil-in-water emulsion system. The carotenoid microparticles dissolve in dichloromethane or are suspended in dichloromethane saturated oil droplets, forming a new 5 μm-10 μm large-particle-size crude oil-in-water emulsion system. Simultaneously, it prevents the dichloromethane and the original oil-in-water emulsion system from being re-sheared into an emulsion system with an emulsion particle size of 0.15 μm-2 μm, ensuring efficient extraction. Thus, separating the crude carotenoid emulsion yields a first dichloromethane mixture with a carotenoid content as high as approximately 10 g / L-50 g / L. This first mixture can then be recycled to obtain high-quality, high-recovery-rate carotenoids.

[0022] Therefore, the treatment method described in this invention significantly improves the recovery rate of carotenoids, uses less dichloromethane, has a simple and efficient recovery process, and produces high-quality carotenoids, thus realizing the resource recovery and utilization of carotenoids in carotenoid washing water. Attached Figure Description

[0023] Figure 1 This is a flowchart illustrating one embodiment of the present invention. Detailed Implementation

[0024] To facilitate understanding of the present invention, it will be described in more detail below. However, it should be understood that the present invention can be implemented in many different forms and is not limited to the embodiments or examples described herein. Rather, these embodiments or examples are provided to make the disclosure of the present invention more thorough and complete.

[0025] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention pertains. The terminology used herein in the description of the invention is for the purpose of describing particular embodiments or examples only and is not intended to be limiting of the invention.

[0026] It should be noted that the carotenoid content in the washing water is generally 1.0 g / L-30.0 g / L. The washing water also contains other substances such as gelatin, sodium OSA starch, gum arabic, and dextrin. The carotenoids in the washing water typically exist as tiny particles of 0.15 μm-2 μm. These tiny particles are coated with aqueous solutions of gelatin, sodium OSA starch, and gum arabic, forming a stable, oil-in-water (O / W) emulsion. Therefore, solvent extraction to extract carotenoids from the washing water presents challenges beyond the extremely large amount of extractant required. These challenges include the low solubility of carotenoids in various solvents and the difficulty in extracting O / W carotenoids. Even adding 100-200 times the total amount of extractant to the washing water is insufficient to completely extract the carotenoids and achieve a near-colorless state.

[0027] Based on the above issues, combined with Figure 1 As shown, this invention provides a method for treating carotenoid washing water, comprising the following steps:

[0028] S1, carotenoid washing water is mixed with dichloromethane and subjected to shearing at a linear velocity of 10m / s-20m / s to obtain a crude carotenoid emulsion;

[0029] S2, the crude carotenoid emulsion is separated to obtain a first mixture and pretreated carotenoid washing water;

[0030] S3, the first mixture is recycled to obtain carotenoid recovery product.

[0031] In step S1, by strictly controlling the mixing shear velocity of the carotenoid washing water and dichloromethane to 10m / s-20m / s, the original 0.15μm-2μm microparticle oil-in-water emulsion system in the carotenoid washing water can be completely destroyed. This allows dichloromethane to extract the carotenoid microparticles from the original oil-in-water emulsion system. The carotenoid microparticles dissolve in dichloromethane or are suspended in dichloromethane saturated oil droplets, forming a new 5μm-10μm large-particle-size crude oil-in-water emulsion system. At the same time, this avoids the dichloromethane and the original oil-in-water emulsion system from being re-sheared into an emulsion system with an emulsion particle size of 0.15μm-2μm, ensuring that the extraction process is carried out efficiently.

[0032] Preferably, the mass ratio of dichloromethane to carotenoids in the carotenoid washing water is 10:1-30:1. Under shearing conditions at an online velocity of 10m / s-20m / s, this is more conducive to the efficient extraction of carotenoids and promotes the formation of a water-in-oil crude emulsion system with a large particle size of 5μm-10μm.

[0033] Preferably, during the shearing process with a linear velocity of 10m / s-20m / s, the temperature is 15℃-40℃, which not only helps to improve the solubility of carotenoids in dichloromethane, but also avoids violent boiling of dichloromethane, ensuring sufficient dichloromethane during the emulsification extraction process, thereby improving the extraction efficiency.

[0034] In step S2, by separating the crude carotenoid emulsion, a first mixed solution of dichloromethane with a carotenoid content of approximately 10 g / L to 50 g / L can be obtained. Preferably, the separation method of the crude carotenoid emulsion is centrifugation with a centrifugation factor of 500-1500. This ensures that the dichloromethane containing carotenoids is separated from the washing solution while preventing trace amounts of insoluble substances such as gelatin, sodium OSA starch, and gum arabic in the carotenoid washing water from being separated. This allows the centrifuge to discharge slag smoothly and operate normally, thereby improving the extraction efficiency and the quality of the obtained carotenoids.

[0035] Considering that the carotenoid content in the pretreated carotenoid washing water is approximately 0.1 g / L-1.0 g / L, it is preferable to use activated carbon to adsorb the pretreated carotenoid washing water, and then use dichloromethane to desorb the adsorbed activated carbon to obtain a second mixture. The second mixture is then recycled to obtain a carotenoid recovered product. By combining dichloromethane extraction under a specific linear velocity shear with activated carbon adsorption treatment, the recovery rate of carotenoids in the carotenoid washing water can be further improved.

[0036] Preferably, the mass ratio of activated carbon to pretreated carotenoid washing water is 0.001:1-0.005:1, which is beneficial for fully adsorbing carotenoids in the carotenoid washing water, so that the treated washing water reaches a near-colorless and clear state, and then the treated washing water is sent to the wastewater treatment plant, which can greatly reduce the treatment load of the wastewater treatment plant.

[0037] Preferably, in the step of desorbing the adsorbed activated carbon with dichloromethane, the mass ratio of dichloromethane to the adsorbed activated carbon is 5:1-20:1. This ensures that the carotenoids adsorbed in the activated carbon can be fully dissolved in the dichloromethane, which not only helps to improve the recovery rate of carotenoids, but also allows the desorbed activated carbon to be reused.

[0038] Further optimization involves recycling the desorbed activated carbon to adsorb the pretreated carotenoid washing water, thus realizing the recycling of activated carbon and reducing treatment costs.

[0039] Preferably, the first mixture and the second mixture are combined for recycling, which simplifies the processing steps and makes the recycling process simple and efficient.

[0040] In one embodiment, the recycling process includes: mixing the first mixture, the second mixture, and water, and distilling to obtain dichloromethane and carotenoid recovered products. Preferably, the mass of water is 0.1 to 2.0 times the total mass of the first and second mixtures. This not only avoids the deterioration of carotenoids when the dichloromethane is evaporated, but also allows crystals to gradually precipitate in the two phases, resulting in better crystal form of the carotenoids and further improving their quality.

[0041] Preferably, the dichloromethane obtained by distillation is recycled for use in the shearing and / or desorption steps, thereby realizing the recycling of dichloromethane, greatly reducing the amount of dichloromethane used, and lowering the processing cost.

[0042] Therefore, the treatment method described in this invention significantly improves the recovery rate of carotenoids, uses less dichloromethane, has a simple and efficient recovery process, and produces high-quality carotenoids, thus realizing the resource recovery and utilization of carotenoids in carotenoid washing water.

[0043] The following specific embodiments will further illustrate the treatment method of the carotenoid washing water.

[0044] Example 1

[0045] 1200L of cleaning water from the β-carotene production line was added to a 2000L emulsification kettle equipped with a stator-rotor shearing device. The β-carotene content in the cleaning water was measured to be approximately 2.03g / L, equivalent to a total β-carotene volume of approximately 2.436kg. 60kg of dichloromethane was added to the cleaning water, and the emulsification kettle jacket was circulated with 25℃ cooling water for insulation. The stator-rotor shearing device was then activated, with a set rotation speed of approximately 1500r / min and a rotor impeller linear velocity of approximately 14.7m / s. After shearing for 30 minutes, the shearing device was shut off, yielding a crude carotenoid emulsion.

[0046] Adjust the speed of the disc centrifuge to approximately 4800 r / min and the centrifugation factor to approximately 1200. Slowly place the sheared crude carotenoid emulsion into the disc centrifuge for centrifugation. Collect the first mixture separated by centrifugation into the recovery vessel, and collect the pretreated carotenoid washing solution into the adsorption vessel.

[0047] After centrifugation, 3 kg of activated carbon was added to the adsorption vessel containing 1183 kg of pretreated carotenoid washing solution, and adsorption was carried out for 30 min with stirring. After adsorption was complete, the solution was filtered to obtain colorless washing water, with a β-carotene content of approximately 0.13 g / L, which was sent to a wastewater treatment plant. The filtered filter cake was added to a desorption vessel, and 25 kg of dichloromethane was added. Desorption was carried out with stirring for 1.0 h. After desorption was complete, the activated carbon and the second mixture were filtered and recycled for use in the adsorption process.

[0048] A total of 83 kg of the first mixture obtained from centrifugation and the second mixture obtained from desorption were added to a recovery vessel. 20 kg of drinking water was added to the vessel, and hot water was circulated through the vessel jacket for heating. After dichloromethane recovery was complete, the mixture was cooled, and the recovered dichloromethane was recycled for use in the shearing and desorption processes. The material in the vessel was cooled and then filtered. The filter cake contained the recovered β-carotene, and approximately 2.38 kg of dried β-carotene was obtained. The all-trans content was approximately 85.7%, the cis content was approximately 10.1%, and the β-carotene recovery rate was approximately 93.6%.

[0049] Example 2

[0050] The difference between Example 2 and Example 1 is that the rotational speed of the shearing device is set to approximately 1000 r / min and the impeller linear velocity is approximately 10 m / s.

[0051] The final recovered β-carotene, after drying, weighed approximately 2.27 kg. The all-trans content was approximately 85.3%, the cis content was approximately 10.2%, and the β-carotene recovery rate was approximately 89.0%.

[0052] Example 3

[0053] The difference between Example 3 and Example 1 is that the rotational speed of the shearing device is set to approximately 2000 r / min and the impeller linear velocity is approximately 20 m / s.

[0054] The final recovered β-carotene, after drying, weighed approximately 2.41 kg. The all-trans content was approximately 83.8%, the cis content was approximately 12.1%, and the β-carotene recovery rate was approximately 94.9%.

[0055] Example 4

[0056] The difference between Example 4 and Example 1 is that the speed of the disc centrifuge is adjusted to approximately 3100 r / min, and the centrifugal separation factor is approximately 500.

[0057] The final recovered β-carotene, after drying, weighed approximately 2.22 kg. The all-trans content was approximately 84.8%, the cis content was approximately 10.2%, and the β-carotene recovery rate was approximately 86.6%.

[0058] Example 5

[0059] The difference between Example 5 and Example 1 is that the speed of the disc centrifuge is adjusted to approximately 5400 r / min, and the centrifugal separation factor is approximately 1500.

[0060] The final recovered β-carotene, after drying, weighed approximately 2.39 kg. The all-trans content was approximately 84.2%, the cis content was approximately 9.1%, and the β-carotene recovery rate was approximately 91.5%.

[0061] Example 6

[0062] The difference between Example 6 and Example 1 is that the speed of the disc centrifuge is adjusted to approximately 6200 r / min, and the centrifugal separation factor is approximately 2000.

[0063] The final recovered β-carotene, after drying, weighed approximately 2.87 kg. The all-trans content was approximately 73.7%, the cis content was approximately 8.3%, and the β-carotene recovery rate was approximately 96.6%.

[0064] Example 7

[0065] 1200L of cleaning water from the β-carotene production line was added to a 2000L emulsification kettle equipped with a stator-rotor shearing device. The β-carotene content in the cleaning water was measured to be approximately 2.03g / L, equivalent to a total β-carotene volume of approximately 2.436kg. 25kg of dichloromethane was added to the cleaning water, and the emulsification kettle jacket was kept warm by circulating 20℃ cooling water. The stator-rotor shearing device was then activated, with a set rotation speed of approximately 1300r / min and a rotor impeller linear velocity of approximately 12.5m / s. After shearing for 30 minutes, the shearing device was shut off, yielding a crude carotenoid emulsion.

[0066] Adjust the speed of the disc centrifuge to approximately 4800 r / min and the centrifugation factor to approximately 1200. Slowly place the sheared crude carotenoid emulsion into the disc centrifuge for centrifugation. Collect the first mixture separated by centrifugation into the recovery vessel, and collect the pretreated carotenoid washing solution into the adsorption vessel.

[0067] After centrifugation, 1.5 kg of activated carbon was added to the adsorption vessel containing 1185 kg of pretreated carotenoid washing solution, and adsorption was carried out by stirring for 30 min. After adsorption was complete, the solution was filtered to obtain colorless washing water, with a β-carotene content of approximately 0.27 g / L, which was sent to a wastewater treatment plant. The filtered filter cake was added to a desorption vessel, and 25 kg of dichloromethane was added. Desorption was carried out by stirring for 1.0 h. After desorption was complete, the activated carbon and the second mixture were filtered and recycled for use in the adsorption process.

[0068] A total of 49 kg of the first mixture obtained from centrifugation and the second mixture obtained from desorption were added to a recovery vessel. 20 kg of drinking water was added to the vessel, and hot water was circulated through the vessel jacket for heating. After dichloromethane recovery was complete, the mixture was cooled, and the recovered dichloromethane was recycled for use in the shearing and desorption processes. The material in the vessel was cooled and then filtered; the filter cake contained the recovered β-carotene, and approximately 2.19 kg of dried β-carotene was obtained. The all-trans content was approximately 83.5%, the cis content was approximately 12.6%, and the β-carotene recovery rate was approximately 86.4%.

[0069] Example 8

[0070] 1200L of cleaning water from the β-carotene production line was added to a 2000L emulsification kettle equipped with a stator-rotor shearing device. The β-carotene content in the cleaning water was measured to be approximately 2.03g / L, equivalent to a total β-carotene volume of approximately 2.436kg. 50kg of dichloromethane was added to the cleaning water, and the emulsification kettle jacket was circulated with 35℃ cooling water for insulation. The stator-rotor shearing device was then activated, with a set rotation speed of approximately 1400r / min and a rotor impeller linear velocity of approximately 13.9m / s. After shearing for 30 minutes, the shearing device was shut off, yielding a crude carotenoid emulsion.

[0071] Adjust the speed of the disc centrifuge to approximately 4800 r / min and the centrifugation factor to approximately 1200. Slowly place the sheared crude carotenoid emulsion into the disc centrifuge for centrifugation. Collect the first mixture separated by centrifugation into the recovery vessel, and collect the pretreated carotenoid washing solution into the adsorption vessel.

[0072] After centrifugation, 5 kg of activated carbon was added to the adsorption vessel containing 1187 kg of pretreated carotenoid washing solution, and adsorption was carried out by stirring for 30 min. After adsorption was complete, the solution was filtered to obtain colorless washing water, with a β-carotene content of approximately 0.078 g / L, which was sent to a wastewater treatment plant. The filtered filter cake was added to a desorption vessel, and 30 kg of dichloromethane was added. The solution was stirred and desorbed for 1.0 h. After desorption was complete, the activated carbon and the second mixture were filtered and recycled for use in the adsorption process.

[0073] A total of 78 kg of the first mixture obtained from centrifugation and the second mixture obtained from desorption were added to a recovery vessel. 20 kg of drinking water was added to the vessel, and hot water was circulated through the vessel jacket for heating. After dichloromethane recovery was complete, the mixture was cooled, and the recovered dichloromethane was recycled for use in the shearing and desorption processes. The material in the vessel was cooled and then filtered; the filter cake contained the recovered β-carotene, and approximately 2.56 kg of dried β-carotene was obtained. The all-trans content was approximately 82.2%, the cis content was approximately 9.3%, and the β-carotene recovery rate was approximately 96.2%.

[0074] Example 9

[0075] The difference between Example 9 and Example 1 is that the first mixture separated by centrifugation is directly mixed with 20 kg of drinking water for recycling, and the pretreated carotenoid washing solution is sent to the wastewater treatment plant.

[0076] The final recovered β-carotene, after drying, weighed approximately 2.06 kg. The all-trans content was approximately 82.5%, the cis content was approximately 12.4%, and the β-carotene recovery rate was approximately 80.3%.

[0077] Comparative Example 1

[0078] 1200L of cleaning water from the β-carotene production line was added to a 2000L extraction vessel. The β-carotene content in the cleaning water was measured to be approximately 2.03g / L, equivalent to a total β-carotene content of approximately 2.436kg. 200kg of dichloromethane was added to the cleaning water, and the mixture was stirred and extracted for 1 hour. After standing for 30 minutes, the first mixture was separated. Another 200kg of dichloromethane was added to the extraction vessel, and the mixture was stirred and extracted for 1 hour. After standing for 30 minutes, the first mixture was separated again.

[0079] After separation, 3 kg of activated carbon was added to the extraction vessel, and adsorption was carried out with stirring for 30 minutes. After adsorption was complete, the mixture was filtered to obtain colorless washing water, which was sent to a wastewater treatment plant. The filtered filter cake was added to a desorption vessel, and 25 kg of dichloromethane was added. The mixture was stirred and desorbed for 1.0 h. After desorption was complete, the activated carbon and the second mixture were filtered and recycled for use in the adsorption process.

[0080] A total of 422 kg of the first mixture obtained from extraction and the second mixture obtained from desorption were added to a recovery vessel. 20 kg of drinking water was added to the vessel, and hot water was circulated through the vessel jacket for heating. After dichloromethane recovery was complete, the mixture was cooled, and the recovered dichloromethane was recycled for use in the shearing and desorption processes. The material in the vessel was cooled and then filtered. The filter cake contained the recovered β-carotene, and approximately 1.65 kg of dried β-carotene was obtained. The all-trans content was approximately 84.7%, the cis content was approximately 9.3%, and the β-carotene recovery rate was approximately 63.7%.

[0081] Comparative Example 2

[0082] The difference between Comparative Example 2 and Example 1 is that the rotational speed of the shearing device is set to approximately 2900 r / min and the impeller linear velocity is approximately 28.8 m / s.

[0083] The final recovered β-carotene, after drying, weighed approximately 1.81 kg. The all-trans content was approximately 87.2%, the cis content approximately 9.4%, and the β-carotene recovery rate was approximately 71.8%.

[0084] Comparative Example 3

[0085] The difference between Comparative Example 3 and Example 1 is that the rotational speed of the shearing device is set to approximately 800 r / min and the impeller linear velocity is approximately 8.2 m / s.

[0086] The final recovered β-carotene, after drying, weighed approximately 3.25 kg. The all-trans content was approximately 47.3%, the cis content was approximately 5.4%, and the β-carotene recovery rate was approximately 70.3%.

[0087] The technical features of the above embodiments can be combined in any way. For the sake of brevity, not all possible combinations of the technical features in the above embodiments are described. However, as long as there is no contradiction in the combination of these technical features, they should be considered to be within the scope of this specification.

[0088] The embodiments described above are merely illustrative of several implementations of the present invention, and while the descriptions are relatively specific and detailed, they should not be construed as limiting the scope of the invention patent. It should be noted that those skilled in the art can make various modifications and improvements without departing from the concept of the present invention, and these all fall within the protection scope of the present invention. Therefore, the protection scope of this invention patent should be determined by the appended claims.

Claims

1. A method for treating carotenoid-containing washing water, characterized in that, Includes the following steps: Carotenoid washing water was mixed with dichloromethane and subjected to shearing at a linear velocity of 10 m / s-20 m / s in a shearing device to obtain a crude oil-in-water emulsion of carotenoids with a large particle size of 5 μm-10 μm. The mass ratio of dichloromethane to carotenoids in the carotenoid washing water was 10:1-30:

1. During the shearing process at a linear velocity of 10 m / s-20 m / s, the temperature was 15℃-40℃. The crude carotenoid emulsion was separated to obtain a first mixture and pretreated carotenoid washing water; The first mixture is recycled to obtain carotenoid recovery product.

2. The method for treating carotenoid washing water according to claim 1, characterized in that, The separation method for the crude carotenoid emulsion is selected from centrifugal separation, with a centrifugation separation factor of 500-1500.

3. The method for treating carotenoid washing water according to claim 1 or claim 2, characterized in that, The pretreated carotenoid washing water is adsorbed by activated carbon, and the adsorbed activated carbon is desorbed by dichloromethane to obtain a second mixture. The second mixture is then recycled to obtain the carotenoid recovered product.

4. The method for treating carotenoid washing water according to claim 3, characterized in that, The mass ratio of activated carbon to the pretreated carotenoid washing water is 0.001:1-0.005:

1.

5. The method for treating carotenoid washing water according to claim 3, characterized in that, In the step of desorbing the adsorbed activated carbon with dichloromethane, the mass ratio of dichloromethane to the adsorbed activated carbon is 5:1-20:

1.

6. The method for treating carotenoid washing water according to claim 3, characterized in that, The desorbed activated carbon is recycled to adsorb the pretreated carotenoid washing water.

7. The method for treating carotenoid washing water according to claim 3, characterized in that, The first mixture and the second mixture are combined for recycling.

8. The method for treating carotenoid washing water according to claim 7, characterized in that, The recycling process includes: mixing the first mixture, the second mixture, and water, and then distilling to obtain dichloromethane and carotenoid recovered products.

9. The method for treating carotenoid washing water according to claim 8, characterized in that, The mass of the water is 0.1 to 2.0 times the total mass of the first mixture and the second mixture.

10. The method for treating carotenoid washing water according to claim 8, characterized in that, Dichloromethane obtained by distillation is recycled for use in the shearing and / or desorption steps.

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