Evaporation and concentration device for honeysuckle mixed liquid

Abstract

The utility model discloses an evaporation and concentration device for honeysuckle mixed liquor, which is characterized in that an outlet of a feeding pump is connected with a cold side inlet of a first-stage plate-type evaporator through cold sides of a condensate water preheater and a non-condensable steam preheater, and a cold side outlet of the first-stage plate-type evaporator is connected with a middle inlet of a first-stage evaporation separator; the bottom of the first-stage evaporation separator is connected with a cold side inlet of the second-stage plate-type evaporator through a first-stage discharging pump, a cold side outlet of the second-stage plate-type evaporator is connected with a middle inlet of the second-stage evaporation separator, and a bottom outlet of the second-stage evaporation separator is connected with a top tube pass inlet of the falling-film evaporator through a second-stage discharging pump; the lower part of the falling-film evaporator is connected with a falling-film separator, bottom outlets of the falling-film evaporator and the falling-film separator are connected with an inlet of a TVR discharge pump, and an outlet of the TVR discharge pump is connected with a system discharge pipe. The device is high in energy utilization rate and small in occupied area and discharging density fluctuation.

Description

Technical Field

[0001] This utility model relates to an evaporation and concentration device, and more particularly to an evaporation and concentration device for honeysuckle mixture, belonging to the technical field of evaporation and purification equipment. Background Technology

[0002] The study of traditional Chinese medicine has a history of thousands of years in my country, and through exploration and research, a complete production system has been formed. In recent years, traditional Chinese medicine has become increasingly popular among consumers due to its natural medicinal properties and the absence of side effects.

[0003] Concentration of traditional Chinese medicine (TCM) has always been an essential step in the production process. Currently, most TCM concentration methods employ multi-effect evaporation or MVR falling film evaporation. Multi-effect evaporation is not only energy-intensive but also bulky and heavily reliant on external steam. Furthermore, the high steam temperature generated by multi-effect evaporation can negatively impact the properties of the active ingredients, especially for heat-sensitive materials like TCM. The production process also consumes large amounts of steam and circulating cooling water, increasing production costs and placing high demands on the steam supply, resulting in energy waste. MVR falling film evaporation technology offers advantages such as recycling secondary steam, reducing energy consumption, and lower operating costs. However, as the concentration ratio increases, insufficient secondary steam makes it difficult to further increase the solution concentration.

[0004] Chinese utility model patent CN 218166007U discloses an automatic high-efficiency concentration system, comprising a heater, an evaporator, a condenser, and a collection tank connected sequentially by pipes. The top and bottom of the heater are connected to the evaporator via a first pipe and a second pipe, respectively. The first pipe is tangential to the evaporator, improving gas-liquid separation at the point of entry from the heater to the evaporator. A primary distillation column and a secondary distillation column are sequentially connected between the evaporator and the condenser via pipes, representing the structure of similar products. This technical solution employs a multi-effect evaporation concentration scheme, resulting in a large system footprint and high steam consumption. Furthermore, the high-temperature steam may cause irreversible damage to the components of the traditional Chinese medicine.

[0005] Chinese utility model patent CN 217015360U discloses a balanced multi-effect concentrator for traditional Chinese medicine extracts, comprising an extract inlet, heater I, evaporation chamber I, heater II, evaporation chamber II, heater III, evaporation chamber III, and a finished product outlet. Heater I is connected to gas-liquid separator I, gas-liquid separator II is connected to gas-liquid separator I, gas-liquid separator III is connected to heater II, gas-liquid separator IV is connected to gas-liquid separator III, and gas-liquid separator V is connected to heater III and a condensate outlet. Gas-liquid separator II is connected to heater II and gas-liquid separator IV, and gas-liquid separator IV is connected to heater III and a condensate outlet, representing the structure of similar products. This technical solution employs a multi-effect evaporation and concentration scheme. During system operation, it still requires a large amount of steam and circulating cooling water. Furthermore, the lack of a preheating system for the feed material results in a prolonged time from heating to evaporation, further exacerbating steam consumption. Meanwhile, the heat from condensate and non-condensable steam is not fully utilized, leading to energy waste.

[0006] Chinese utility model patent CN 202120072309.7 discloses an MVR evaporation device for alcohol extraction of traditional Chinese medicine, comprising: a feed pump connected by pipelines, a primary preheater, a secondary preheater, a cooling component, and an evaporation component, which is the structure of similar products. This technical solution adopts a single-pass falling film evaporation and concentration scheme, but the single-pass falling film evaporator requires a large floor space and has a high overall investment cost. Furthermore, the single-pass MVR falling film concentration process cannot guarantee the range of fluctuations in the output concentration. Utility Model Content

[0007] The purpose of this section is to outline some aspects of embodiments of the present invention and to briefly describe some preferred embodiments. Simplifications or omissions may be made in this section, as well as in the abstract and title of this application, and such simplifications or omissions should not be construed as limiting the scope of the present invention.

[0008] In view of the problems existing in the above and / or prior art, this utility model is proposed.

[0009] The purpose of this invention is to overcome the problems existing in the prior art and provide an evaporation and concentration device for honeysuckle mixed solution. While achieving effective evaporation and concentration of honeysuckle mixed solution, it improves the system heat utilization rate, reduces the overall equipment area, reduces the difficulty of operation and maintenance, and reduces the fluctuation of output density while reducing the overall energy consumption of the system.

[0010] To solve the above technical problems, this utility model provides an evaporation and concentration device for honeysuckle mixture, including a honeysuckle mixture feed pipe. The outlet of the honeysuckle mixture feed pipe is connected to the cold side inlet of a condensate preheater via a feed pump. The cold side outlet of the condensate preheater is connected to the cold side inlet of a non-condensable steam preheater. The cold side outlet of the non-condensable steam preheater is connected to the cold side inlet of a primary plate evaporator. The cold side outlet of the primary plate evaporator is connected to the middle inlet of a primary evaporator separator. The bottom of the primary evaporator separator is connected to the inlet of a primary discharge pump. The outlet of the primary discharge pump is connected to the cold side inlet of a secondary plate evaporator. The cold side outlet of the secondary plate evaporator is connected to the middle inlet of the secondary evaporator separator. The bottom outlet of the secondary evaporator separator is connected to the inlet of a secondary discharge pump. The outlet of the secondary discharge pump is connected to the top tube side inlet of a falling film evaporator. A falling film separator is connected to the lower part of the falling film evaporator. The bottom outlets of both the falling film evaporator and the falling film separator are connected to the inlet of a TVR discharge pump. The outlet of the TVR discharge pump is connected to the system discharge pipe.

[0011] As an improvement of this utility model, the top outlets of the primary evaporator and the secondary evaporator are both connected to the inlet of the steam compressor. The outlet of the steam compressor is connected to the hot-side inlet of the primary plate evaporator and the secondary plate evaporator through a compressed steam pipe. The hot-side outlet of the primary plate evaporator is connected to the inlet of the primary gas-liquid separator. The bottom drain of the primary gas-liquid separator is connected to the inlet of the primary condensate tank. The bottom outlet of the primary condensate tank is connected to the condensate main pipe through a primary condensate pump. The outlet of the condensate main pipe is connected to the hot-side inlet of the condensate preheater. The hot-side outlet of the condensate preheater is connected to the condensate drain pipe.

[0012] As a further improvement of this utility model, the condensate drain pipe is connected to the compressed steam desuperheating water inlet of the steam compressor.

[0013] As a further improvement of this utility model, the hot-side outlet of the secondary plate evaporator is connected to the inlet of the secondary gas-liquid separator, the bottom drain of the secondary gas-liquid separator is connected to the inlet of the secondary condensate tank, and the bottom outlet of the secondary condensate tank is connected to the condensate main pipe through a secondary condensate pump.

[0014] As a further improvement of this utility model, the top exhaust port of the falling film separator is connected to the middle air inlet of the steam jet pump, and the live steam pipe is connected to the power steam inlet of the steam jet pump through a live steam regulating valve. The outlet of the steam jet pump is connected to the shell-side steam inlet of the falling film evaporator, the shell-side condensate outlet of the falling film evaporator is connected to the inlet of the TVR condensate tank, and the bottom outlet of the TVR condensate tank is connected to the condensate main pipe through a TVR condensate pump.

[0015] As a further improvement of this utility model, the top exhaust port of the falling film separator is also connected to the shell-side air inlet of the TVR condenser, and the shell-side exhaust port of the falling film evaporator is connected to the shell-side air inlet of the TVR condenser. The shell-side condensate outlet of the TVR condenser is connected to the inlet of the TVR condensate tank through a water trap.

[0016] As a further improvement of this utility model, the top exhaust port of the TVR condensate tank is also connected to the shell-side air inlet of the falling film evaporator.

[0017] As a further improvement of this utility model, the exhaust port of the first-stage gas-liquid separator is connected to the non-condensable steam main pipe through a first-stage plate evaporation vacuum regulating valve, the exhaust port of the second-stage gas-liquid separator is connected to the non-condensable steam main pipe through a second-stage plate evaporation vacuum regulating valve, the shell-side exhaust port of the TVR condenser is connected to the non-condensable steam main pipe through a TVR evaporation system vacuum regulating valve, the outlet of the non-condensable steam main pipe is connected to the hot-side inlet of the non-condensable steam preheater, the hot-side outlet of the non-condensable steam preheater is connected to the hot-side inlet of the surface cooler, the hot-side outlet of the surface cooler is connected to the middle inlet of the third-stage gas-liquid separator, the bottom drain port of the third-stage gas-liquid separator is connected to the inlet of the first-stage condensate tank, and the exhaust port of the third-stage gas-liquid separator is vented to the atmosphere through a vacuum pump.

[0018] Compared with existing technologies, this utility model achieves the following beneficial effects: 1. The MVR system abandons the multi-effect falling film evaporator and replaces it with a two-stage plate evaporator. Firstly, in terms of layout, it greatly reduces the overall longitudinal footprint of the system, significantly reducing the investment cost of concrete and steel structures. Secondly, compared with the steam consumption per ton of water evaporated by traditional processes, the MVR system consumes little steam except during startup and other special circumstances. The steam consumption is significantly reduced, resulting in a significant reduction in production and operating costs. The evaporation mode combining plate evaporators and falling film evaporators allows for continuous feeding and discharging during the evaporation and concentration of the honeysuckle mixed solution. With short heating time, high evaporation efficiency, and minimal impact on the composition of the honeysuckle solution, this process significantly improves the evaporation efficiency of the honeysuckle mixed solution.

[0019] 2. The honeysuckle mixture first undergoes two stages of preheating to raise the feed temperature, making the feed temperature basically equal to the system evaporation temperature. This reduces the heat load required for the material to enter the system for evaporation and concentration. The primary preheating heat source is the condensate generated by the system, which heats the material in the first stage while recovering the heat from the condensate. The secondary preheating heat source is the non-condensable steam generated by the system, which further utilizes the heat from the non-condensable steam to perform secondary preheating of the feed.

[0020] 3. Traditional falling film evaporators have a large footprint, and uneven liquid feeding may occur in the top feed distribution tray. In this device, the preheated honeysuckle mixed solution first enters the first-stage plate evaporator for evaporation, then passes through a first-stage discharge pump to the second-stage plate evaporator for further evaporation. The concentrated liquid then passes through a second-stage discharge pump to the TVR system for further concentration, and finally is discharged from the system by the TVR discharge pump. MVR evaporation uses plate evaporators, which have high heat transfer efficiency, low heat loss, and are easy to clean. This combined plate evaporation and falling film evaporation process solves the problems of large footprint, high cost, and difficult operation and maintenance associated with traditional multi-effect Chinese medicine evaporation and concentration equipment, ensuring improved production efficiency for customers.

[0021] 4. The system employs MVR+TVR evaporation. After concentration via MVR, the material is pumped into the TVR falling film evaporator via a two-stage discharge pump. Due to the increased boiling point temperature, a single steam compressor is insufficient for production; therefore, a steam jet pump provides the heat source for the TVR system. The MVR section ensures basic steam recycling and energy saving, while the TVR system uses high-pressure, high-temperature steam as the driving force to draw in some low-temperature secondary steam, forming a medium-pressure, medium-temperature mixed steam, providing an additional heat source for the evaporator. This combination further recovers and utilizes more secondary steam energy, resulting in higher energy efficiency and better energy savings compared to a standalone MVR system.

[0022] 5. This process utilizes a vacuum pump, compressor, and steam jet pump in coordination to maintain negative pressure in the overall evaporation system, enabling low-temperature evaporation and minimizing damage to the honeysuckle mixture. Low-temperature evaporation not only reduces the occurrence of unintended chemical reactions but also effectively preserves nutrients and flavor compounds. Attached Figure Description

[0023] To more clearly illustrate the technical solutions of the embodiments of this utility model, the drawings used in the description of the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort. The drawings are provided for reference and illustration only and are not intended to limit this utility model. Wherein:

[0024] Figure 1 The flowchart shows the evaporation and concentration device for the honeysuckle mixture of this utility model.

[0025] In the diagram: 1. First-stage plate evaporator; 2. Second-stage plate evaporator; 3. Falling film evaporator; 4. First-stage evaporator separator; 5. Second-stage evaporator separator; 6. Falling film separator; 7. Condensate preheater; 8. Non-condensable steam preheater; 9. First-stage condensate tank; 10. Second-stage condensate tank; 11. TVR condenser; 12. TVR condensate tank; 13. Liquid accumulator; 14. Surface cooler;

[0026] H1. Steam compressor; H2. Steam jet pump;

[0027] F1. Primary gas-liquid separator; F2. Secondary gas-liquid separator; F3. Tertiary gas-liquid separator;

[0028] P1. Feed pump; P2. Primary condensate pump; P3. Primary discharge pump; P4. Secondary condensate pump; P5. Secondary discharge pump; P6. TVR discharge pump; P7. TVR condensate pump; P8. Liquid collection pump; P9. Vacuum pump;

[0029] V1. Primary plate-type evaporator vacuum regulating valve; V2. Secondary plate-type evaporator vacuum regulating valve; V3. TVR evaporator system vacuum regulating valve; V4. Live steam regulating valve;

[0030] ZT1. Mass flow meter;

[0031] G1. Honeysuckle mixture feed pipe; G2. Condensate main pipe; G3. Condensate drain pipe; G4. Live steam pipe; G5. Compressed steam pipe; G6. Non-condensable steam main pipe; G7. Circulating cooling water pipe; G8. System discharge pipe. Detailed Implementation

[0032] To make the technical means, creative features, achieved objectives and effects of this utility model easier to understand, the present utility model will be further described below with reference to specific illustrations. Obviously, the described embodiments are only some embodiments of this utility model, and not all embodiments.

[0033] 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 is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention.

[0034] like Figure 1 As shown, the evaporation and concentration device for honeysuckle mixed liquid of this utility model includes a primary plate evaporator 1, a secondary plate evaporator 2, a falling film evaporator 3, a primary evaporator separator 4, a secondary evaporator separator 5, a falling film separator 6, a condensate preheater 7, a non-condensable steam preheater 8, a primary condensate tank 9, a secondary condensate tank 10, a TVR condenser 11, a TVR condensate tank 12, a liquid accumulation tank 13, and a surface cooler 14.

[0035] The outlet of the honeysuckle mixture feed pipe G1 is connected to the inlet of the feed pump P1. The outlet of the feed pump P1 is connected to the cold-side inlet of the condensate preheater 7. The cold-side outlet of the condensate preheater 7 is connected to the cold-side inlet of the non-condensable steam preheater 8. The cold-side outlet of the non-condensable steam preheater 8 is connected to the cold-side inlet of the first-stage plate evaporator 1. The cold-side outlet of the first-stage plate evaporator 1 is connected to the middle inlet of the first-stage evaporator separator 4. The bottom of the first-stage evaporator separator 4 is connected to the inlet of the first-stage discharge pump P3. The outlet of the first-stage discharge pump P3 is connected to the cold-side inlet of the second-stage plate evaporator 2. The side inlet is connected, the cold side outlet of the secondary plate evaporator 2 is connected to the middle inlet of the secondary evaporator separator 5, the bottom outlet of the secondary evaporator separator 5 is connected to the inlet of the secondary discharge pump P5, the outlet of the secondary discharge pump P5 is connected to the top tube inlet of the falling film evaporator 3, the lower part of the falling film evaporator 3 is connected to the falling film separator 6, the bottom outlets of the falling film evaporator 3 and the falling film separator 6 are both connected to the inlet of the TVR discharge pump P6, the outlet of the TVR discharge pump P6 is connected to the system discharge pipe G8, and the system discharge pipe G8 is equipped with a mass flow meter ZT1.

[0036] The top outlets of the primary evaporator separator 4 and the secondary evaporator separator 5 are both connected to the inlet of the steam compressor H1. The outlet of the steam compressor H1 is connected to the hot-side inlet of the primary plate evaporator 1 and the secondary plate evaporator 2 via the compressed steam pipe G5. The hot-side outlet of the primary plate evaporator 1 is connected to the inlet of the primary gas-liquid separator F1. The bottom drain of the primary gas-liquid separator F1 is connected to the inlet of the primary condensate tank 9 via a water trap. The bottom outlet of the primary condensate tank 9 is connected to the inlet of the primary condensate pump P2. The outlet of the primary condensate pump P2 is connected to the condensate main pipe G2. The outlet of the condensate main pipe G2 is connected to the hot-side inlet of the condensate preheater 7. The hot-side outlet of the condensate preheater 7 is connected to the condensate drain pipe G3. The condensate drain pipe G3 is connected to the condensate reuse system and the compressed steam desuperheating water supply port of the steam compressor H1.

[0037] The hot side outlet of the secondary plate evaporator 2 is connected to the inlet of the secondary gas-liquid separator F2. The bottom drain of the secondary gas-liquid separator F2 is connected to the inlet of the secondary condensate tank 10 through a water trap. The bottom outlet of the secondary condensate tank 10 is connected to the inlet of the secondary condensate pump P4. The outlet of the secondary condensate pump P4 is also connected to the condensate main pipe G2.

[0038] The hot-side inlets of the primary plate evaporator 1 and the secondary plate evaporator 2 are also connected to the live steam pipe G4. When the unit is started, the live steam pipe G4 provides a heat source to the hot side of the primary plate evaporator 1.

[0039] The bottom drain of the steam compressor H1 is connected to the inlet of the condensate tank 13. The condensate in the secondary steam of the first-stage evaporator separator 4 and the second-stage evaporator separator 5 also enters the condensate tank 13. The bottom outlet of the condensate tank 13 is connected to the inlet of the condensate pump P8, and the outlet of the condensate pump P8 is connected to the inlet of the first-stage condensate tank 9.

[0040] The top exhaust port of the falling film separator 6 is connected to the middle air inlet of the steam jet pump H2. The live steam pipe G4 is connected to the power steam inlet of the steam jet pump H2 through the live steam regulating valve V4. The exhaust port of the steam jet pump H2 is connected to the shell-side steam inlet of the falling film evaporator 3. The shell-side condensate outlet of the falling film evaporator 3 is connected to the inlet of the TVR condensate tank 12 through a water trap.

[0041] The top exhaust port of the falling film separator 6 is also connected to the shell-side air inlet of the TVR condenser 11, and the shell-side exhaust port of the falling film evaporator 3 is connected to the shell-side air inlet of the TVR condenser 11. The tube side of the TVR condenser 11 is connected to the circulating cooling water pipe G7. The shell-side condensate outlet of the TVR condenser 11 is connected to the inlet of the TVR condensate tank 12 through a water trap. The bottom outlet of the TVR condensate tank 12 is connected to the inlet of the TVR condensate pump P7. The outlet of the TVR condensate pump P7 is also connected to the hot-side inlet of the non-condensable steam preheater 8 through the condensate main pipe G2.

[0042] The top vent of the TVR condensate tank 12 is also connected to the shell-side inlet of the falling film evaporator 3.

[0043] The exhaust port of the first-stage gas-liquid separator F1 is connected to the non-condensable steam main G6 through the first-stage plate evaporation vacuum regulating valve V1. The exhaust port of the second-stage gas-liquid separator F2 is connected to the non-condensable steam main G6 through the second-stage plate evaporation vacuum regulating valve V2. The shell-side exhaust port of the TVR condenser 11 is connected to the non-condensable steam main G6 through the TVR evaporation system vacuum regulating valve V3. The outlet of the non-condensable steam main G6 is connected to the hot-side inlet of the non-condensable steam preheater 8. The hot-side outlet of the non-condensable steam preheater 8 is connected to the hot-side inlet of the surface cooler 14. The hot-side outlet of the surface cooler 14 is connected to the middle inlet of the third-stage gas-liquid separator F3. The bottom drain port of the third-stage gas-liquid separator F3 is connected to the inlet of the first-stage condensate tank 9 through a water trap. The exhaust port of the third-stage gas-liquid separator F3 is vented to the atmosphere through the vacuum pump P9.

[0044] The raw liquid from the honeysuckle mixture feed pipe G1 is fed into the cold side of the condensate preheater 7 by the feed pump P1 for primary preheating, raising the temperature of the raw liquid from 48℃ to 57℃. After primary preheating, the liquid then enters the cold side of the non-condensable steam preheater 8 for secondary preheating to approximately 60℃. After two stages of preheating, the 60℃ honeysuckle mixture enters the cold side of the primary plate evaporator 1 for evaporation. The hot side medium of the primary plate evaporator 1 is secondary steam compressed by the steam compressor H1. The condensate after heat exchange enters the primary gas-liquid separator F1 for separation. The condensate discharged from the bottom of the primary gas-liquid separator F1 flows into the primary condensate tank 9 by gravity through a water trap. The gas phase from the primary gas-liquid separator F1 flows through the primary plate evaporator vacuum regulating valve V1 and the primary non-condensable steam pipe into the non-condensable steam main G6, and then enters the hot side of the non-condensable steam preheater 8 as a heat source.

[0045] After evaporation, the honeysuckle mixture reaches an outlet temperature of approximately 62°C in the primary plate evaporator 1. It then enters the primary evaporator separator 4 for vapor-liquid separation. The separated primary concentrate is discharged from the bottom of the primary evaporator separator 4 and pumped by the primary discharge pump P3 into the cold side of the secondary plate evaporator 2 for further evaporation. It first undergoes vapor-liquid separation in the secondary evaporator separator 5, with an outlet temperature of approximately 63°C. The heat source medium for the secondary plate evaporator 2 is secondary steam compressed by the steam compressor H1. The condensate after heat exchange enters the secondary gas-liquid separator F2 for further separation. The condensate discharged from the bottom of the secondary gas-liquid separator F2 flows by gravity into the secondary condensate tank 10 through a water trap. The gas phase from the secondary gas-liquid separator F2 flows through the secondary plate evaporator vacuum regulating valve V2 and the secondary non-condensable steam pipe into the non-condensable steam main pipe G6, and then enters the hot side of the non-condensable steam preheater 8 as a heat source.

[0046] The secondary steam discharged from the top of the primary evaporator separator 4 and the secondary evaporator separator 5 is heated to 70°C by the compressor H1. After the secondary steam is heated, it enters the hot side of the primary plate evaporator 1 and the secondary plate evaporator 2 through the compressed steam pipe G5 as a heating source medium.

[0047] The secondary concentrate discharged from the bottom of the secondary evaporator separator 5 is sent to the tube side of the falling film evaporator 3 by the secondary discharge pump P5 for evaporation. The discharge temperature of the falling film evaporator 3 is about 65°C. The concentrate is then pumped into the downstream process section for further processing by the TVR discharge pump P6 through the system discharge pipe G8 and the mass flow meter ZT1.

[0048] The secondary steam generated by the falling film evaporator 3 has a temperature of approximately 60°C. It first undergoes gas-liquid separation in the falling film separator 6. The separated liquid is discharged from the bottom of the separator 6 to the discharge pipe. A portion of the secondary steam separated by the separator 6 enters the steam jet pump H2 and mixes with the live steam from the live steam pipe G4 to form mixed secondary steam, which then re-enters the shell side of the falling film evaporator 3 as a heating medium. After heat exchange with the material, the mixed secondary steam condenses into water, which flows by gravity into the TVR condensate tank 12.

[0049] Another portion of the secondary steam separated by the falling film separator 6 enters the TVR condenser 11 to exchange heat with the circulating water and condense into condensate. The condensate then flows by gravity through the outlet of the TVR condenser 11 to the TVR condensate tank 12.

[0050] The condensate produced by the steam compressor H1 flows by gravity into the liquid collection tank 13, and is then pumped into the primary condensate tank 9 by the liquid collection pump P8.

[0051] The exhaust gas from the top of the TVR condensate tank 12 also enters the shell side of the falling film evaporator 3. The shell side exhaust gas from the falling film evaporator 3 enters the shell side of the TVR condenser 11 for condensation. The shell side exhaust gas from the TVR condenser 11 flows through the TVR evaporation system vacuum regulating valve V3 and the TVR non-condensable steam pipe into the non-condensable steam main pipe G6, and then enters the hot side of the non-condensable steam preheater 8 as a heat source. The non-condensable steam discharged from the hot side of the non-condensable steam preheater 8 enters the hot side of the surface cooler 14 for condensation, and the circulating cooling water from the circulating cooling water pipe G7 enters the cold side of the surface cooler 14 for cooling. The exhaust gas from the hot side of the surface cooler 14 enters the three-stage gas-liquid separator F3 for separation, and the bottom drainage of the three-stage gas-liquid separator F3 enters the first-stage condensate tank 9 for collection. The top of the three-stage gas-liquid separator F3 is evacuated by the vacuum pump P9.

[0052] The secondary steam generated by evaporation contains a certain amount of non-condensable gases. After heat exchange and condensation in the primary plate evaporator 1, the secondary plate evaporator 2, and the falling film evaporator 3, the remaining gas is all non-condensable and is finally extracted and discharged by vacuum pump P9. Furthermore, vacuum pump P9 maintains negative pressure within the system, ensuring stable low-temperature evaporation. The system vacuum is regulated by interlocking the opening of pneumatic valves. Stable, precise, and effective control logic ensures the stability of the overall system vacuum. Simultaneously, automated control allows for more precise system adjustment and reduces operational errors or inaccurate manual adjustments by personnel on-site.

[0053] The condensate in the primary condensate tank 9 is pumped into the condensate main pipe G2 by the primary condensate pump P2. The condensate in the secondary condensate tank 10 is pumped into the condensate main pipe G2 by the secondary condensate pump P4. The condensate in the TVR condensate tank 12 is pumped into the condensate main pipe G2 by the TVR condensate pump P7. The condensate collected in the condensate main pipe G2 enters the hot side of the condensate preheater 7 as a heat source, and is then discharged through the condensate drain pipe G3. Part of it is used as desuperheating water for the steam compressor H1.

[0054] By interlocking the live steam regulating valve V4 at the power port of the steam jet pump H2 with the discharge density, the discharge density is automatically adjusted, achieving precise control of the system's discharge density. This meets customers' needs for different discharge densities and also improves the overall system's production efficiency.

[0055] Compared to traditional processes, this device requires fewer consumables and is easier to maintain. With these advantages, it is highly adaptable to concentrated honeysuckle mixed solutions and can meet the production needs of enterprises of different sizes.

[0056] The above description is merely a preferred embodiment of the present utility model, showing and describing the basic principles, main features, and advantages of the present utility model. It is not intended to limit the scope of patent protection of the present utility model. Those skilled in the art should understand that the present utility model is not limited to the above embodiments. In addition to the above embodiments, the present utility model may have other implementations without departing from the spirit and scope of the present utility model. Various changes and improvements to the present utility model are also possible. All technical solutions formed by equivalent substitutions or equivalent transformations fall within the scope of protection claimed by the present utility model. The scope of protection claimed by the present utility model is defined by the appended claims and their equivalents. Technical features not described in the present utility model can be implemented by or using existing technology, and will not be elaborated here.

Claims

1. An evaporation and concentration device for honeysuckle mixture, comprising a honeysuckle mixture feed pipe, characterized in that: The outlet of the honeysuckle mixture feed pipe is connected to the cold-side inlet of the condensate preheater via a feed pump. The cold-side outlet of the condensate preheater is connected to the cold-side inlet of the non-condensable steam preheater. The cold-side outlet of the non-condensable steam preheater is connected to the cold-side inlet of the first-stage plate evaporator. The cold-side outlet of the first-stage plate evaporator is connected to the middle inlet of the first-stage evaporator separator. The bottom of the first-stage evaporator separator is connected to the inlet of the first-stage discharge pump. The outlet of the first-stage discharge pump is connected to the cold-side inlet of the second-stage plate evaporator. The cold-side outlet of the second-stage plate evaporator is connected to the middle inlet of the second-stage evaporator separator. The bottom outlet of the second-stage evaporator separator is connected to the inlet of the second-stage discharge pump. The outlet of the second-stage discharge pump is connected to the top tube-side inlet of the falling film evaporator. A falling film separator is connected to the lower part of the falling film evaporator. The bottom outlets of both the falling film evaporator and the falling film separator are connected to the inlet of the TVR discharge pump. The outlet of the TVR discharge pump is connected to the system discharge pipe.

2. The evaporation and concentration apparatus for honeysuckle mixture according to claim 1, characterized in that: The top outlets of both the primary and secondary evaporator separators are connected to the inlet of the steam compressor. The outlet of the steam compressor is connected to the hot-side inlet of both the primary and secondary plate evaporators via a compressed steam pipe. The hot-side outlet of the primary plate evaporator is connected to the inlet of the primary gas-liquid separator. The bottom drain of the primary gas-liquid separator is connected to the inlet of the primary condensate tank. The bottom outlet of the primary condensate tank is connected to the condensate main pipe via a primary condensate pump. The outlet of the condensate main pipe is connected to the hot-side inlet of the condensate preheater. The hot-side outlet of the condensate preheater is connected to the condensate drain pipe.

3. The evaporation and concentration apparatus for honeysuckle mixture according to claim 2, characterized in that: The condensate drain pipe is connected to the compressed steam desuperheating water inlet of the steam compressor.

4. The evaporation and concentration apparatus for honeysuckle mixture according to claim 2, characterized in that: The hot-side outlet of the secondary plate evaporator is connected to the inlet of the secondary gas-liquid separator, the bottom drain outlet of the secondary gas-liquid separator is connected to the inlet of the secondary condensate tank, and the bottom outlet of the secondary condensate tank is connected to the condensate main pipe through the secondary condensate pump.

5. The evaporation and concentration apparatus for honeysuckle mixture according to claim 4, characterized in that: The top exhaust port of the falling film separator is connected to the middle air inlet of the steam jet pump. The live steam pipe is connected to the power steam inlet of the steam jet pump through a live steam regulating valve. The exhaust port of the steam jet pump is connected to the shell-side steam inlet of the falling film evaporator. The shell-side condensate outlet of the falling film evaporator is connected to the inlet of the TVR condensate tank. The bottom outlet of the TVR condensate tank is connected to the condensate main pipe through a TVR condensate pump.

6. The evaporation and concentration apparatus for honeysuckle mixture according to claim 5, characterized in that: The top exhaust port of the falling film separator is also connected to the shell-side air inlet of the TVR condenser, and the shell-side exhaust port of the falling film evaporator is connected to the shell-side air inlet of the TVR condenser. The shell-side condensate outlet of the TVR condenser is connected to the inlet of the TVR condensate tank through a water trap.

7. The evaporation and concentration apparatus for honeysuckle mixture according to claim 5, characterized in that: The top exhaust port of the TVR condensate tank is also connected to the shell-side air inlet of the falling film evaporator.

8. The evaporation and concentration apparatus for honeysuckle mixture according to claim 6, characterized in that: The exhaust port of the first-stage gas-liquid separator is connected to the non-condensable steam main pipe through a first-stage plate evaporation vacuum regulating valve. The exhaust port of the second-stage gas-liquid separator is connected to the non-condensable steam main pipe through a second-stage plate evaporation vacuum regulating valve. The shell-side exhaust port of the TVR condenser is connected to the non-condensable steam main pipe through a TVR evaporation system vacuum regulating valve. The outlet of the non-condensable steam main pipe is connected to the hot-side inlet of the non-condensable steam preheater. The hot-side outlet of the non-condensable steam preheater is connected to the hot-side inlet of the surface cooler. The hot-side outlet of the surface cooler is connected to the middle inlet of the third-stage gas-liquid separator. The bottom drain port of the third-stage gas-liquid separator is connected to the inlet of the first-stage condensate tank. The exhaust port of the third-stage gas-liquid separator is vented to the atmosphere through a vacuum pump.

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