A continuous crystallization production device for glutamine

Abstract

The utility model discloses a kind of glutamine continuous crystallization production devices, belong to biological chemical equipment technical field.It include stock solution feed pump, the outlet of stock solution feed pump is connected with the inlet of feed preheating unit, and the discharge of feed preheating unit is connected with multiple-effect evaporation concentration unit and flash crystallization unit in turn;The feed preheating unit includes evaporative condensate preheater, steam condensate preheater and one-effect steam preheater connected in turn by pipeline, for carrying out multistage preheating to stock solution;The multiple-effect evaporation concentration unit includes one-effect falling-film evaporation system, two-effect forced circulation evaporation system and three-effect forced circulation evaporation system connected in series in turn;The flash crystallization unit includes OSLO flash crystallization ware.This glutamine continuous crystallization production device not only can improve system overall processing capacity, reduce operation and maintenance difficulty, but also can further improve material conversion rate, improve product quality.

Description

Technical Field

[0001] This utility model relates to a flash crystallization system, and more particularly to a continuous crystallization production device for glutamine, belonging to the field of biochemical equipment technology. Background Technology

[0002] Glutamine is the most abundant free amino acid in the human body. Although classified as a "non-essential amino acid" (because the body can synthesize it), under physiological stress (such as severe illness, trauma, or after strenuous exercise), it transforms into a "conditionally essential amino acid," meaning it must be supplemented externally. In recent years, with the increasing health awareness of consumers and the continuous expansion of the sports nutrition market, the global production of glutamine has been steadily increasing. Currently, most finished glutamine products are produced using a combination of vacuum concentration and intermittent cooling crystallization. However, vacuum concentration is time-consuming and inefficient, while intermittent cooling crystallization requires more equipment and has higher labor costs, indirectly leading to lower production efficiency.

[0003] Chinese utility model patent CN219795689U discloses a "membrane concentration and separation device for transglutaminase processing," comprising a base cabinet, mounting plate, shock-absorbing components, the main body of the concentration and separation device, a centrifugal pump and concentration tank, a support frame, a separation tank, and fixing holes. This technical solution utilizes the elasticity of a first spring to move the support plate up and down. The up-and-down movement of the support plate drives the movement of a rotating rod, which in turn drives the movement of a second spring. The movement of the second spring stabilizes the rotation of the rotating rod. The shock absorber reduces spring rebound, thus reducing force. This structure solves the problem of centrifugal force generated by the impeller causing vibration in the centrifugal pump, which could lead to loosening of connections in the membrane concentration and separation device during long-term use. However, its drawbacks include: poor adaptability to feed solutions and limited adaptability to overall temperature and chemical composition; the inability to achieve high output concentrations due to inherent limitations; high cost of membrane replacement after scaling; and difficulty in large-scale continuous production. These limitations make it unsuitable for large-scale production. Utility Model Content

[0004] 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.

[0005] In view of the problems existing in the above and / or prior art, this utility model is proposed.

[0006] The purpose of this invention is to overcome the problems of low efficiency, high cost, and inability to produce continuously in the existing technology, and to provide a continuous crystallization production device for glutamine, which can not only increase the overall processing capacity of the system and reduce the difficulty of operation and maintenance, but also further improve the material conversion rate and improve product quality.

[0007] To solve the above technical problems, this utility model provides a continuous crystallization production device for glutamine, including a raw liquid feed pump, the outlet of which is connected to the inlet of the feed preheating unit, and the outlet of the feed preheating unit is sequentially connected to a multi-effect evaporation concentration unit and a flash crystallization unit. The feed preheating unit includes an evaporation condensate preheater, a steam condensate preheater, and a single-effect steam preheater connected in sequence by pipelines, for multi-stage preheating of the raw liquid. The multi-effect evaporation and concentration unit includes a first-effect falling film evaporation system, a second-effect forced circulation evaporation system, and a third-effect forced circulation evaporation system connected in series; the flash crystallization unit includes an OSLO flash crystallizer.

[0008] Furthermore, the single-effect falling film evaporation system includes a single-effect falling film evaporator and a single-effect falling film separator. The sidewall of the single-effect falling film separator is connected to the lower part of the tube side of the single-effect falling film evaporator. The lower part of the tube side of the single-effect falling film evaporator and the bottom of the single-effect falling film separator are both connected to the inlet of the single-effect transfer pump. The outlet of the single-effect transfer pump is connected to the double-effect forced circulation evaporation system through the single-effect transfer pipe.

[0009] Furthermore, the double-effect forced circulation evaporation system includes a double-effect forced crystallizer, a double-effect forced evaporator, and a double-effect forced circulation pump; the bottom outlet of the double-effect forced crystallizer is connected to the inlet of the double-effect forced circulation pump, the outlet of the double-effect forced circulation pump is connected to the tube-side inlet of the double-effect forced evaporator, and the tube-side outlet of the double-effect forced evaporator is connected to the circulating liquid inlet of the double-effect forced crystallizer; the outlet of the double-effect forced circulation pump is also connected to the triple-effect forced circulation evaporation system through a double-effect transfer pipe.

[0010] Furthermore, the triple-effect forced circulation evaporation system includes a triple-effect forced crystallizer, a triple-effect forced evaporator, and a triple-effect forced circulation pump; the bottom outlet of the triple-effect forced crystallizer is connected to the inlet of the triple-effect forced circulation pump, the outlet of the triple-effect forced circulation pump is connected to the tube-side inlet of the triple-effect forced evaporator, and the tube-side outlet of the triple-effect forced evaporator is connected to the circulating liquid inlet of the triple-effect forced crystallizer; the bottom of the triple-effect forced crystallizer is also connected to the flash crystallization unit via a triple-effect transfer pump and a triple-effect transfer pipe.

[0011] Furthermore, the flash crystallization unit also includes a flash forced circulation pump and a flash discharge pump; the lower circulating liquid outlet of the flash crystallizer is connected to the inlet of the flash forced circulation pump, and the outlet of the flash forced circulation pump is connected to the upper circulating liquid inlet of the flash crystallizer; the bottom crystal slurry outlet of the flash crystallizer is connected to the flash discharge pipe through the flash discharge pump.

[0012] Furthermore, the shell-side inlet of the first-effect steam preheater is connected to the live steam pipe and the shell-side inlet of the first-effect falling film evaporator, and its shell-side condensate outlet is connected to the shell side of the first-effect falling film evaporator; the shell-side condensate outlet of the first-effect falling film evaporator is connected to the steam condensate tank, and the outlet of the steam condensate tank is connected to the shell-side inlet of the steam condensate preheater through a steam condensate pump.

[0013] Furthermore, the top secondary steam outlet of the first-effect falling film separator is connected to the shell-side inlet of the second-effect forced evaporator via a first-effect secondary steam pipe; the top secondary steam outlet of the second-effect forced crystallizer is connected to the shell-side inlet of the third-effect forced evaporator via a second-effect secondary steam pipe; and the top secondary steam outlet of the third-effect forced crystallizer is connected to the air inlet of a composite air cooler via a third-effect secondary steam pipe.

[0014] Furthermore, the exhaust port of the composite air cooler is connected to the inlet of the evaporation vacuum pump through an evaporation system vacuum regulating valve and an evaporation vacuum manifold.

[0015] Furthermore, the shell-side inlet of the evaporative condensate preheater is connected to the outlet of an evaporative condensate tank, and the inlet of the evaporative condensate tank is connected to the shell-side condensate outlet of the triple-effect forced evaporator.

[0016] Furthermore, the flash crystallization unit also includes a flash condenser and a flash vacuum pump; the top secondary steam outlet of the flash crystallizer is connected to the shell-side inlet of the flash condenser through a flash secondary steam pipe, and the shell-side vacuum port of the flash condenser is connected to the inlet of the flash vacuum pump.

[0017] Compared with the prior art, the advantages or beneficial effects of this utility model include at least the following: 1. The evaporation section adopts a triple-effect evaporation method, which combines falling film evaporation and forced circulation evaporation to achieve evaporation concentration. The triple-effect evaporation mode can further reduce steam consumption and realize multi-stage utilization of steam. The combination of falling film and forced circulation evaporation can improve the overall heat transfer efficiency in the falling film stage and avoid the problem of tube blockage caused by too much dry matter in the forced circulation stage, thus ensuring continuous production and improving production efficiency for customers.

[0018] 2. The glutamine solution first undergoes preheating via the system's evaporation condensate to raise its feed temperature. It then undergoes further preheating with the system's steam condensate, again raising the feed temperature. Finally, it exchanges heat with the steam from the first-effect falling film evaporator, further increasing the feed temperature. Ultimately, the feed temperature is brought close to the first-effect evaporation temperature. This three-stage preheating reduces the heat load required for the material to enter the system for evaporation and concentration. The condensate generated by the system heats the material while simultaneously recovering heat from the system's condensate, thus also preheating the feed.

[0019] 3. The evaporation section employs a falling film evaporation combined with forced circulation evaporation, enabling continuous feeding and discharging during the evaporation and concentration of the glutamine solution. When the material concentration and dry matter content are relatively low, falling film evaporation provides high heat transfer efficiency and a short material residence time. When the material concentration and dry matter content are relatively high, forced circulation evaporation is used. This meets the system's evaporation requirements while reducing the risk of scaling and extending the system's continuous operating time. Furthermore, the combination of these two evaporation methods has minimal impact on the composition of the glutamine solution, resulting in a significant improvement in the evaporation and concentration efficiency of the glutamine solution.

[0020] 4. The flash crystallization section uses an OSLO crystallizer. The unique structure and working principle of the OSLO crystallizer make it excellent in crystal production during flash crystallization. On the one hand, it can produce large and uniform finished products with a low secondary nucleation rate. On the other hand, the flash evaporation method eliminates the need for physical heat exchange surfaces, fundamentally eliminating the heat exchanger clogging problems of previous operations. This not only allows for continuous feeding and discharging but also extends the cleaning cycle and improves overall production efficiency.

[0021] 5. The system vacuum is adjusted by interlocking the opening of the non-condensable steam pneumatic valve. Through stable, precise and effective control logic, the overall system vacuum stability is achieved. On the one hand, automated control can make the system adjustment more precise, and on the other hand, it reduces the possibility of manual intervention errors or inaccurate manual adjustments on site.

[0022] 6. The secondary steam from the final effect of evaporation and concentration is cooled by a composite air cooler, which not only has a very high water saving rate and greatly reduces the customer's initial investment in public utility facilities, but also has lower operating and maintenance costs and can ensure a better vacuum degree during operation. 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: Figure 1 This is a flowchart of the continuous crystallization production apparatus for glutamine according to this utility model; Figure reference numerals: 1. Evaporative condensate preheater; 2. Steam condensate preheater; 3. Steam condensate tank; 4. Parallel preheater; 5. Single-effect falling film evaporator; 6. Single-effect falling film separator; 7. Double-effect forced crystallizer; 8. Double-effect forced evaporator; 9. Triple-effect forced crystallizer; 10. Triple-effect forced evaporator; 11. Evaporative condensate tank; 12. OSLO flash crystallizer; 13. Flash condenser; 14. Flash condensate tank P1. Raw material feed pump; P2. Steam condensate pump; P3. Single-effect transfer pump; P4. Double-effect forced circulation pump; P5. Triple-effect transfer pump; P6. Triple-effect forced circulation pump; P7. Evaporation condensate pump; P8. Flash forced circulation pump; P9. Flash discharge pump; P10. Flash condensate pump; P11. Evaporation vacuum pump; P12. Flash vacuum pump; C1. Composite air cooler; V1. Vacuum regulating valve for evaporation system; G1. Raw liquid feed pipe; G2. Live steam pipe; G3. Secondary steam pipe for first effect; G4. Transfer pipe for first effect; G5. Secondary steam pipe for second effect; G6. Transfer pipe for second effect; G7. Secondary steam pipe for third effect; G8. Transfer pipe for third effect; G9. Flash secondary steam pipe; G10. Flash discharge pipe; G11. Evaporation vacuum main pipe. Detailed Implementation

[0024] In the following description of this utility model, the terms "upper", "lower", "front", "rear", "left", "right", "inner", "outer", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, and are only for the convenience of describing this utility model and simplifying the description, and do not mean that the device must have a specific orientation.

[0025] 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.

[0026] 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.

[0027] like Figure 1 As shown, the continuous glutamine crystallization production device of this utility model includes an evaporation condensate preheater 1, a steam condensate preheater 2, a steam condensate tank 3, a side-by-side preheater 4, a first-effect falling film evaporator 5, a first-effect falling film separator 6, a second-effect forced crystallizer 7, a second-effect forced evaporator 8, a third-effect forced crystallizer 9, a third-effect forced evaporator 10, an evaporation condensate tank 11, an OSLO flash crystallizer 12, a flash condenser 13, and a flash condensate tank 14.

[0028] The outlet of the feed pipe G1 is connected to the inlet of the feed pump P1. The outlet of the feed pump P1 is connected to the tube-side inlet of the evaporative condensate preheater 1. The tube-side outlet of the evaporative condensate preheater 1 is connected to the tube-side inlet of the steam condensate preheater 2. The tube-side outlet of the steam condensate preheater 2 is connected to the tube-side inlet of the parallel preheater 4. The tube-side outlet of the parallel preheater 4 is connected to the top tube-side inlet of the first-effect falling film evaporator 5. The lower part of the tube-side of the first-effect falling film evaporator 5 is connected to the first-effect falling film separator 6. The bottom outlet of the tube side of the device 5 and the bottom outlet of the first-effect falling film separator 6 are both connected to the inlet of the first-effect transfer pump P3. The outlet of the first-effect transfer pump P3 is connected to the second-effect circulation pipe through the first-effect transfer pipe G4. The bottom circulation liquid outlet of the second-effect forced crystallizer 7 is connected to the inlet of the second-effect forced circulation pump P4 through the second-effect circulation pipe. The outlet of the second-effect forced circulation pump P4 is connected to the lower inlet of the tube side of the second-effect forced evaporator 8. The upper outlet of the tube side of the second-effect forced evaporator 8 is connected to the side wall circulation liquid inlet of the second-effect forced crystallizer 7.

[0029] The outlet of the second-effect forced circulation pump P4 is also connected to the third-effect circulation pipe through the second-effect transfer pipe G6. The bottom circulation liquid outlet of the third-effect forced crystallizer 9 is connected to the inlet of the third-effect forced circulation pump P6 through the third-effect circulation pipe. The outlet of the third-effect forced circulation pump P6 is connected to the lower inlet of the tube side of the third-effect forced evaporator 10. The upper outlet of the tube side of the third-effect forced evaporator 10 is connected to the side wall circulation liquid inlet of the third-effect forced crystallizer 9.

[0030] The triple-effect circulation pipe is also connected to the inlet of the triple-effect transfer pump P5. The outlet of the triple-effect transfer pump P5 is connected to the flash forced circulation pipe via the triple-effect transfer pipe G8, and then both are connected to the upper circulation liquid inlet of the OSLO flash crystallizer 12. The lower circulation liquid outlet of the OSLO flash crystallizer 12 is connected to the inlet of the flash forced circulation pump P8. The bottom crystal slurry outlet of the OSLO flash crystallizer 12 is connected to the inlet of the flash discharge pump P9 via the flash discharge pipe G10. The outlet of the flash discharge pump P9 is connected to the next stage.

[0031] The live steam pipe G2 is connected to the shell-side inlet of the first-effect falling film evaporator 5. The shell-side inlet of the parallel preheater 4 is connected to the shell-side inlet of the first-effect falling film evaporator 5. The shell-side condensate outlet of the first-effect falling film evaporator 5 is connected to the inlet of the steam condensate tank 3 through a water trap. The outlet of the steam condensate tank 3 is connected to the inlet of the steam condensate pump P2. The outlet of the steam condensate pump P2 is connected to the shell-side inlet of the steam condensate preheater 2. The shell-side outlet of the steam condensate preheater 2 is connected to the common condensate tank.

[0032] The top secondary steam outlet of the first-effect falling film separator 6 is connected to the shell-side inlet of the second-effect forced evaporator 8 via the first-effect secondary steam pipe G3. The shell-side vacuum port of the first-effect falling film evaporator 5 is also connected to the first-effect secondary steam pipe G3. The top secondary steam outlet of the second-effect forced crystallizer 7 is connected to the shell-side steam inlet of the third-effect forced evaporator 10 via the second-effect secondary steam pipe G5. The shell-side vacuum port of the second-effect forced evaporator 8 is also connected to the second-effect secondary steam pipe G5. The shell-side condensate outlet of the second-effect forced evaporator 8 is connected to the condensate inlet at the bottom of the shell side of the third-effect forced evaporator 10 via a water trap. The shell-side condensate outlet of the third-effect forced evaporator 10 is connected to the evaporative condensate tank 11 via a water trap. The outlet of the evaporative condensate tank 11 is connected to the inlet of the evaporative condensate pump P7. The outlet of the evaporative condensate pump P7 is connected to the shell-side inlet of the evaporative condensate preheater 1. The shell-side outlet of the evaporative condensate preheater 1 is connected to the common condensate tank.

[0033] The top secondary steam outlet of the triple-effect forced crystallizer 9 is connected to the inlet of the composite air cooler C1 through the triple-effect secondary steam pipe G7. The exhaust port of the composite air cooler C1 is connected to the inlet of the evaporation vacuum pump P11 through the evaporation vacuum main pipe G11 and the evaporation system vacuum regulating valve V1. The outlet of the evaporation vacuum pump P11 is open to the atmosphere.

[0034] The top secondary steam outlet of the OSLO flash crystallizer 12 is connected to the shell-side inlet of the flash condenser 13 via flash secondary steam pipe G9. The shell-side vacuum of the flash condenser 13 is connected to the inlet of the flash vacuum pump P12, and the outlet of the flash vacuum pump P12 is open to the atmosphere. The shell-side condensate outlet of the flash condenser 13 is connected to the inlet of the flash condensate tank 14 via a water trap. The outlet of the flash condensate tank 14 is connected to the inlet of the flash condensate pump P10, and the outlet of the flash condensate pump P10 is connected to a common condensate tank.

[0035] The glutamine solution from the feed pipe G1 has a concentration of 6% and a temperature of 30°C. It is fed into the tube side of the evaporative condensate preheater 1 by the feed pump P1 and preheated to about 44.3°C. The heat source medium for the shell side of the evaporative condensate preheater 1 is the condensate pump P7. After exchanging heat with the glutamine feed solution, the condensate enters the common condensate tank.

[0036] The glutamine solution, after being preheated by the evaporating condensate, is sent to the tube side of the steam condensate preheater 2 and preheated to approximately 53°C. The heat source medium for the shell side of the steam condensate preheater 2 is the condensate pumped by the steam condensate pump P2. After exchanging heat with the glutamine stock solution, the condensate enters the common condensate tank.

[0037] The glutamine solution, after being preheated by the evaporation condensate, is then sent to the tube side of the parallel preheater 4 and preheated to approximately 58.6°C. The heat source medium for the shell side of the parallel preheater 4 is the live steam from the shell side of the first-effect falling film evaporator 5. After exchanging heat with the material, the steam condenses into condensate and flows by gravity into the shell side of the first-effect falling film evaporator 5.

[0038] After the above three-stage preheating, the glutamine solution at approximately 58.6°C enters the tube side of the first-effect falling film evaporator 5 for evaporation. The heat source medium for the shell side of the first-effect falling film evaporator 5 is the live steam pipe G2 from the common area. After heat exchange with the tube side material, the live steam in the shell side of the first-effect falling film evaporator 5 condenses into condensate, which flows by gravity into the steam condensate tank 3 and is then pumped out by the steam condensate pump P2.

[0039] After the material undergoes first-effect evaporation, the outlet temperature of the first-effect falling film evaporator 5 is approximately 69°C. The glutamine concentrate is then pumped into the second-effect forced crystallizer 7 via the first-effect falling film transfer pump P3 and the first-effect transfer pipe G4.

[0040] The glutamine concentrate at approximately 69°C enters the tube side of the double-effect forced evaporator 8 for heating, and then circulates in the double-effect forced crystallizer 7. After a certain period of evaporation and concentration, the secondary concentrate is pumped into the triple-effect circulation pipe by the double-effect forced circulation pump P4 through the double-effect transfer pipe G6. The outlet temperature of the secondary concentrate is approximately 58.7°C.

[0041] Under the delivery of the triple-effect forced circulation pump P6, the secondary glutamine concentrate at approximately 58.7°C enters the tube side of the triple-effect forced evaporator 10 for heating, and then enters the triple-effect forced crystallizer 9. After a certain period of evaporation and concentration, the tertiary concentrate is pumped into the flash forced circulation tube by the triple-effect transfer pump P5 through the triple-effect transfer pipe G8. The outlet temperature of the tertiary concentrate is approximately 47.7°C.

[0042] The tertiary glutamine concentrate at approximately 47.7°C enters the OSLO flash crystallizer 12. The concentrate is continuously circulated by the flash forced circulation pump P8 for flash evaporation. As the temperature of the glutamine concentrate continues to decrease, the supersaturation of the solution increases. When the solution reaches the set temperature and residence time, the material is pumped out of the system through the flash discharge pipe G10 by the flash discharge pump P9 and enters the next stage. The flash discharge temperature is approximately 17°C.

[0043] The secondary steam generated after the glutamine solution is evaporated in the first-effect falling film evaporator 5 has a temperature of approximately 68°C. It first passes through the first-effect falling film separator 6 for vapor-liquid separation, and the separated liquid is discharged from the bottom of the first-effect falling film separator 6. The secondary steam evaporated in the first effect enters the shell-side heat source inlet of the second-effect forced evaporator 8 through the first-effect secondary steam pipe G3 as the heating heat source for the second-effect forced evaporator 8.

[0044] After heat exchange with the material in the tubes of the first-effect falling film evaporator 5, the live steam condenses into water, which is discharged from the shell-side condensate outlet of the first-effect falling film evaporator 5 and flows by gravity into the steam condensate tank 3. The condensate in the steam condensate tank 3 is sent to the hot side of the steam condensate preheater 2 by the steam condensate pump P2.

[0045] The secondary steam generated by the second-effect forced evaporator 8 has a temperature of approximately 56.5℃. It first undergoes gas-liquid separation in the second-effect forced crystallizer 7. The separated secondary steam enters the shell-side heat source inlet of the third-effect forced evaporator 10 through the second-effect secondary steam pipe G5, serving as the heating source for the third-effect forced evaporator 10. After heat exchange with the material in the tubes of the second-effect forced evaporator 8, the first-effect secondary steam condenses into water, which is discharged from the shell-side condensate outlet of the second-effect forced evaporator 8 and flows by gravity into the shell side of the third-effect forced circulating evaporator 10.

[0046] The secondary steam generated by the triple-effect forced evaporator 10 has a temperature of approximately 47.7℃. It first undergoes gas-liquid separation in the triple-effect forced crystallizer 9. The separated secondary steam enters the combined air cooler C1 through the triple-effect secondary steam pipe G7 for cooling. The cooled condensate flows by gravity into the evaporation condensate tank 11 through the drain pipe of the combined air cooler C1. The secondary steam from the second effect condenses into water after heat exchange with the material in the tubes of the triple-effect forced evaporator 10. This water is discharged from the shell-side condensate outlet of the triple-effect forced evaporator 10 and flows by gravity into the evaporation condensate tank 11. The condensate in the evaporation condensate tank 11 is then pumped to the hot side of the evaporation condensate preheater 1 by the evaporation condensate pump P7.

[0047] The secondary steam generated in the OSLO flash crystallizer 12 enters the flash condenser 13 through the flash secondary steam pipe G9 and exchanges heat with the cold water from the circulating cold water main pipe G11. The condensed water flows into the flash condensate tank 14 through the shell side drain pipe of the flash condenser 13. The condensate in the flash condensate tank 14 is pumped into the common condensate tank by the flash condensate pump P10.

[0048] The multi-effect evaporation system mainly uses different vacuum levels in each effect for evaporation. The overall vacuum of the system is controlled by the vacuum regulating valve V1 and the evaporation vacuum manifold G11. The vacuum port of the flash condenser 13 is evacuated to the outside by the flash vacuum pump P12. The flash vacuum pump P12 can maintain the negative pressure in the flash evaporation system, ensuring stable and continuous flash evaporation.

[0049] 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. A continuous crystallization production apparatus for glutamine, comprising a feed pump (P1), characterized in that, The outlet of the raw liquid feed pump (P1) is connected to the inlet of the feed preheating unit, and the outlet of the feed preheating unit is connected in sequence to the multi-effect evaporation concentration unit and the flash crystallization unit. The feed preheating unit includes an evaporation condensate preheater (1), a steam condensate preheater (2) and a single-effect steam preheater connected in sequence by pipelines, for multi-stage preheating of the raw liquid; The multi-effect evaporation and concentration unit includes a first-effect falling film evaporation system, a second-effect forced circulation evaporation system, and a third-effect forced circulation evaporation system connected in series; the flash crystallization unit includes an OSLO flash crystallizer (12).

2. The continuous glutamine crystallization production apparatus according to claim 1, characterized in that: The single-effect falling film evaporation system includes a single-effect falling film evaporator (5) and a single-effect falling film separator (6). The side wall of the single-effect falling film separator (6) is connected to the lower part of the tube side of the single-effect falling film evaporator (5). The lower part of the tube side of the single-effect falling film evaporator (5) and the bottom of the single-effect falling film separator (6) are both connected to the inlet of the single-effect transfer pump (P3). The outlet of the single-effect transfer pump (P3) is connected to the double-effect forced circulation evaporation system through the single-effect transfer pipe (G4).

3. The continuous glutamine crystallization production apparatus according to claim 2, characterized in that: The double-effect forced circulation evaporation system includes a double-effect forced crystallizer (7), a double-effect forced evaporator (8), and a double-effect forced circulation pump (P4); the bottom outlet of the double-effect forced crystallizer (7) is connected to the inlet of the double-effect forced circulation pump (P4), the outlet of the double-effect forced circulation pump (P4) is connected to the tube-side inlet of the double-effect forced evaporator (8), and the tube-side outlet of the double-effect forced evaporator (8) is connected to the circulating liquid inlet of the double-effect forced crystallizer (7); the outlet of the double-effect forced circulation pump (P4) is also connected to the triple-effect forced circulation evaporation system through a double-effect transfer pipe (G6).

4. The continuous glutamine crystallization production apparatus according to claim 3, characterized in that, The triple-effect forced circulation evaporation system includes a triple-effect forced crystallizer (9), a triple-effect forced evaporator (10), and a triple-effect forced circulation pump (P6); the bottom outlet of the triple-effect forced crystallizer (9) is connected to the inlet of the triple-effect forced circulation pump (P6), the outlet of the triple-effect forced circulation pump (P6) is connected to the tube-side inlet of the triple-effect forced evaporator (10), and the tube-side outlet of the triple-effect forced evaporator (10) is connected to the circulating liquid inlet of the triple-effect forced crystallizer (9); the bottom of the triple-effect forced crystallizer (9) is also connected to the flash crystallization unit through a triple-effect transfer pump (P5) and a triple-effect transfer pipe (G8).

5. The continuous glutamine crystallization production apparatus according to claim 1, characterized in that, The flash crystallization unit also includes a flash forced circulation pump (P8) and a flash discharge pump (P9); the lower circulating liquid outlet of the flash crystallizer (12) is connected to the inlet of the flash forced circulation pump (P8), and the outlet of the flash forced circulation pump (P8) is connected to the upper circulating liquid inlet of the flash crystallizer (12); the bottom crystal slurry outlet of the flash crystallizer (12) is connected to the flash discharge pipe (G10) through the flash discharge pump (P9).

6. The continuous glutamine crystallization production apparatus according to claim 1, characterized in that, The shell-side inlet of the first-effect steam preheater is connected to the live steam pipe (G2) and the shell-side inlet of the first-effect falling film evaporator (5), and its shell-side condensate outlet is connected to the shell side of the first-effect falling film evaporator (5); the shell-side condensate outlet of the first-effect falling film evaporator (5) is connected to the steam condensate tank (3), and the outlet of the steam condensate tank (3) is connected to the shell-side inlet of the steam condensate preheater (2) through the steam condensate pump (P2).

7. The continuous glutamine crystallization production apparatus according to claim 4, characterized in that, The top secondary steam outlet of the first-effect falling film separator (6) is connected to the shell-side inlet of the second-effect forced evaporator (8) via the first-effect secondary steam pipe (G3); the top secondary steam outlet of the second-effect forced crystallizer (7) is connected to the shell-side inlet of the third-effect forced evaporator (10) via the second-effect secondary steam pipe (G5); and the top secondary steam outlet of the third-effect forced crystallizer (9) is connected to the air inlet of a composite air cooler (C1) via the third-effect secondary steam pipe (G7).

8. The continuous glutamine crystallization production apparatus according to claim 7, characterized in that, The exhaust port of the composite air cooler (C1) is connected to the inlet of the evaporation vacuum pump (P11) through an evaporation system vacuum regulating valve (V1) and an evaporation vacuum manifold (G11).

9. The continuous glutamine crystallization production apparatus according to claim 4, characterized in that, The shell-side inlet of the evaporative condensate preheater (1) is connected to the outlet of an evaporative condensate tank (11), and the inlet of the evaporative condensate tank (11) is connected to the shell-side condensate outlet of the triple-effect forced evaporator (10).

10. The continuous glutamine crystallization production apparatus according to any one of claims 1 to 9, characterized in that, The flash crystallization unit also includes a flash condenser (13) and a flash vacuum pump (P12); the top secondary steam outlet of the flash crystallizer (12) is connected to the shell-side inlet of the flash condenser (13) through a flash secondary steam pipe (G9), and the shell-side vacuum port of the flash condenser (13) is connected to the inlet of the flash vacuum pump (P12).

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