Membrane separation apparatus and method of conditioning thereof

Abstract

The application discloses a membrane separation equipment and a regulating method thereof. The membrane separation equipment comprises a membrane separation device and a plurality of auxiliary devices for providing membrane separation conditions for the membrane separation device. The membrane separation device comprises a shell and a first membrane core detachably installed in the shell. The first membrane core comprises a plurality of first membrane tubes and a plurality of first heating pipes. The plurality of first membrane tubes are arranged at intervals in the shell and are used for separating materials. The plurality of first heating pipes are arranged in the shell and are located between the plurality of first membrane tubes. The inner wall of the shell, the outer wall of the plurality of first membrane tubes and the outer wall of the plurality of first heating pipes form a first material cavity for the flow of materials. The plurality of first heating pipes are used for heating the materials in the first material cavity. Through such an arrangement, the heating pipes can be flexibly arranged in the first material cavity, so that the uniformity and timeliness of the material heat supplement of the membrane separation device are ensured, and the membrane separation performance of the membrane separation equipment is improved.

Description

Technical Field

[0001] This invention relates to the field of membrane separation technology, and in particular to a membrane separation device and its adjustment method. Background Technology

[0002] Membrane separation generally refers to the process of separating fluid mixtures by utilizing the selective permeation of membranes to different components. Membrane separation technology is widely used in petrochemical, biopharmaceutical, food processing, and environmental engineering fields.

[0003] Since the pervaporation (vapor permeation) separation performance of membranes is closely related to temperature and flow rate, the flux and processing capacity of the membrane will decrease significantly as the temperature and flow rate decrease. Furthermore, the insufficient uniformity and timeliness of heat replenishment and the mismatch of flow cross-sectional area in existing membrane separation devices will affect the membrane separation performance of the membrane separation device. Summary of the Invention

[0004] The purpose of this invention is to propose a membrane separation device and its adjustment method, which aims to solve the problems of insufficient uniformity and timeliness of heat replenishment and unsuitable material flow cross-sectional area in existing membrane separation devices, which affect the membrane separation performance of the membrane separation device.

[0005] In a first aspect, the present invention provides a membrane separation device, the membrane separation device including a membrane separation unit and a plurality of auxiliary devices for providing membrane separation conditions for the membrane separation unit, the membrane separation unit including a housing and a first membrane core detachably installed in the housing;

[0006] The first membrane core includes a plurality of first membrane tubes and a plurality of first heating tubes. The plurality of first membrane tubes are spaced apart from each other in the housing and are used to separate materials. The plurality of first heating tubes are disposed in the housing and located between the plurality of first membrane tubes. The inner wall of the housing, the outer walls of the plurality of first membrane tubes, and the outer walls of the plurality of first heating tubes enclose a first material cavity for material flow. The plurality of first heating tubes are used to heat the material in the first material cavity.

[0007] Secondly, the present invention also provides a method for adjusting a membrane separation device, the method being applied to the membrane separation device of any of the above embodiments, the method comprising the following steps:

[0008] The ratio of the number of the first membrane tubes to the number of the first heating tubes is changed to adjust the membrane separation performance of the membrane separation device for materials.

[0009] By changing the ratio of the first membrane element to the second membrane element, the membrane separation device can be adjusted to meet the dewatering requirements of different material moisture contents and flow rates, thereby achieving optimal equipment performance.

[0010] The embodiments of the present invention have the following beneficial effects:

[0011] The membrane separation device and its adjustment method of the present invention include a first membrane core comprising a plurality of first membrane tubes and a plurality of first heating tubes. The plurality of first heating tubes are disposed within a housing and located between the plurality of first membrane tubes. The inner wall of the housing, the outer walls of the plurality of first membrane tubes, and the outer walls of the plurality of first heating tubes enclose a first material cavity for supplying material flow. This arrangement facilitates the flexible layout of the heating tubes within the first material cavity, thereby ensuring the uniformity and timeliness of the membrane separation device in replenishing the material, and thus improving the membrane separation performance of the membrane separation device.

[0012] The first membrane element is installed in the dewatering section with high material moisture content. As water is removed from the material, the second membrane element is installed in the dewatering section with low material moisture content. This ensures that the requirements for heat replenishment and flow rate are met in different dewatering membrane separation devices, thereby improving the membrane separation performance of the membrane separation equipment. Attached Figure Description

[0013] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0014] in:

[0015] Figure 1 This is a front view of a membrane separation integrated device in one embodiment.

[0016] Figure 2 for Figure 1 The diagram shows a top view of the integrated membrane separation device.

[0017] Figure 3 for Figure 1 The right view of the membrane separation integrated device shown.

[0018] Figure 4 for Figure 1 Left view of the membrane separation integrated device shown.

[0019] Figure 5 This is a schematic diagram of a membrane separation device in one embodiment.

[0020] Figure 6 This is a schematic diagram of the first membrane core in a membrane separation device according to one embodiment.

[0021] Figure 7 for Figure 6 The front view of the first membrane core is shown.

[0022] Figure 8 for Figure 6 The cross-sectional view of the first membrane core is shown.

[0023] Figure 9 This is a schematic diagram of a membrane separation device in one embodiment.

[0024] Figure 10 This is a cross-sectional view of a membrane separation device in one embodiment.

[0025] Figure 11 This is a schematic diagram of a membrane separation device in one embodiment.

[0026] Figure 12 for Figure 11 Cross-section of the first membrane core in the membrane separation device shown. Figure 1 .

[0027] Figure 13 for Figure 11 Cross-section of the first membrane core in the membrane separation device shown. Figure 2 .

[0028] Figure 14 This is a schematic diagram of a membrane separation device in one embodiment.

[0029] Figure 15 For Figure 14 Schematic diagram of the through holes on the first spacer plate in the membrane separation device shown. Figure 1 .

[0030] Figure 16 For Figure 14 Schematic diagram of the through holes on the first spacer plate in the membrane separation device shown. Figure 2 .

[0031] Figure 17 This is a schematic diagram of a membrane separation device in one embodiment.

[0032] Figure 18 This is a flow chart of the molecular sieve membrane dehydration process in one embodiment of the membrane separation integrated device.

[0033] Figure 19 This is a schematic diagram illustrating the effect of material flow rate on membrane dewatering efficiency.

[0034] Figure 20 This is a schematic diagram illustrating the effect of material temperature on membrane dewatering efficiency.

[0035] Figure 21 This is a schematic diagram of a traditional sleeve-type membrane module structure.

[0036] Figure 22 This is a schematic diagram of a traditional baffle-type membrane module structure.

[0037] Reference numerals: 10. Membrane separation device; 11. First material connector; 12. Second material connector; 13. First heating connector; 14. Second heating connector; 20. Preheater; 30. Heater; 21. First heating connector; 22. Second heating connector; 40. Vacuum condenser; 41. First vacuum connector; 42. First cooling connector; 43. Second cooling connector; 50. Connecting pipe; 60. Vaporizer; 71. Feed pump; 72. Filter; 73. Condensate collection tank; 74. Permeate pump; 75. Raw material tank; 76. Product cooler; 77. Product tank; 78. Product pump; 79. Vacuum pump;

[0038] 110. Shell; 111. First shell; 112. Second shell; 114. Separating cavity;

[0039] 120. First membrane tube; 130. First heating tube; 140. First partition plate; 150. Second partition plate; 160. Third partition plate; 170. First membrane shell; 171. Guide rail; 181. First tube body; 182. Second tube body; 190. Connecting hose;

[0040] 201. First material inlet; 202. First material outlet; 203. First vacuum port; 204. First heating inlet; 205. First heating outlet;

[0041] 210. First receiving cavity; 220. First material cavity; 230. First vacuum cavity;

[0042] 320. First partition plate; 321. Adapter channel; 322. First side plate; 323. Second side plate; 324. Sealing plate; 325. First interface; 326. Second interface; 330. Second membrane tube; 340. Second heating tube; 350. Adapter plate; 351. First rotating plate; 352. Second rotating plate; 353. Sealing plate; 360. Adapter pipe; 370. Second partition plate;

[0043] 401. Second heating inlet; 402. Second heating outlet; 403. Second vacuum port; 404. Second material inlet; 405. Second material outlet;

[0044] 410. Second accommodating cavity; 420. Second vacuum cavity; 430. Second material cavity; 440. Second heating cavity. Detailed Implementation

[0045] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0046] It should be noted that all directional indicators (such as up, down, left, right, front, back, etc.) in the embodiments of the present invention are only used to explain the relative positional relationship and movement of each component in a certain specific posture (as shown in the figure). If the specific posture changes, the directional indicators will also change accordingly.

[0047] Furthermore, the use of terms such as "first" and "second" in this invention is for descriptive purposes only and should not be construed as indicating or implying their relative importance or implicitly specifying the number of technical features indicated. Therefore, features defined with "first" and "second" may explicitly or implicitly include at least one of the stated features. Additionally, the technical solutions of the various embodiments can be combined with each other, but only on the basis of being achievable by those skilled in the art. When the combination of technical solutions is contradictory or impossible to implement, such a combination of technical solutions should be considered non-existent and not within the scope of protection claimed by this invention.

[0048] This invention discloses a membrane separation device; please refer to [link / reference]. Figures 1 to 4 The membrane separation equipment includes a membrane separation unit 10 and several auxiliary devices for providing membrane separation conditions for the membrane separation unit 10.

[0049] In this embodiment, the membrane separation device 10 is integrated with several auxiliary devices into a single unit. The auxiliary devices include at least one of a preheater 20, a heater 30, and a vacuum condenser 40, which reduces the pipeline connection length between the auxiliary devices and the membrane separation device 10, reduces the liquid flow resistance in the pipeline, minimizes heat loss, and facilitates the miniaturization of the membrane separation integrated equipment.

[0050] In one embodiment, please refer to Figures 1 to 4The device includes several auxiliary components, including a preheater 20, a heater 30, and a vacuum condenser 40. The preheater 20 is connected to the heater 30 and the material chamber of the membrane separation unit 10, and is used to preheat the material. The heater 30 is connected to the material chamber of the membrane separation unit 10 and is used to heat the material. The vacuum condenser 40 is connected to the vacuum chamber of the membrane separation unit 10 and is used to drive the membrane separation unit 10 to separate the material. The preheater 20 and heater 30 are respectively attached to the outer wall of the membrane separation unit 10, and the permeate side of the membrane separation unit 10 is directly connected to the vacuum condenser 40 as a single unit. The preheater 20, heater 30, and the shell structure of the membrane separation unit 10 are connected in series via a connecting pipe 50, forming a highly efficient integrated membrane separation device.

[0051] Understandably, since the preheater 20 and heater 30 are integrated into the membrane separation device 10, the preheater 20 and heater 30 can use the heat generated by the membrane separation device 10 to preheat or keep the material inside the preheater 20 and heater 30 warm, thus saving energy.

[0052] The vacuum level on the permeate side of the membrane separation unit 10 has a crucial impact on the membrane separation efficiency. The longer the pipeline between the membrane separation unit 10 and the vacuum condenser 40, the worse the vacuum level on the permeate side of the membrane separation unit 10, thus reducing the membrane dehydration efficiency. Since the permeate side of the membrane separation unit 10 is directly connected to the vacuum condenser 40, the travel loss due to pipeline connections can be reduced, ensuring a better vacuum level on the permeate side of the membrane separation unit 10 and avoiding vacuum losses caused by pipeline connections.

[0053] Specifically, the membrane separation device 10 has a first material connector 11 and a second material connector 12 on its shell structure. One of the first material connector 11 and the second material connector 12 is a material inlet and the other is a material outlet. The material passes through the preheater 20, the heater 30, the membrane separation device 10 and the preheater 20 in sequence. The functional modules are connected by a connecting pipe 50. By sharing the shell and reducing the length of the system pipeline connection, the flow loss and heat dissipation of the material in the pipeline are reduced, the heat of the system is fully utilized and the energy consumption of the membrane separation equipment is reduced.

[0054] In this embodiment, the shell structure of the membrane separation device 10 shares an intermediate shell with the preheater 20. The heat energy lost through the shell structure of the membrane separation device 10 is used to heat the raw materials in the preheater 20. At the same time, the heat loss of the membrane separation device 10 and the preheater 20 can be reduced. Furthermore, the shell structure of the membrane separation device 10 is connected to the intermediate shell of the heater 30. The material and the material inside the shell structure of the membrane separation device 10 exchange energy through the intermediate shell, and the energy is not dissipated to the outside. At the same time, the heat loss of the membrane separation device 10 and the heater 30 can be reduced.

[0055] The membrane separation integrated equipment of this embodiment solves the problems of excessive heat dissipation and poor vacuum effect inside the membrane separation integrated equipment system.

[0056] According to the "Design Code for Thermal Insulation Engineering of Industrial Equipment and Pipelines", the allowable heat loss of the insulation layer for equipment and pipelines at 125℃ is 94W / m. 2 That is, the allowable heat loss of the equipment and pipeline insulation layer is 94W / m. 2 The membrane separation unit 10 shares an intermediate shell 1m with the preheater 20. 2 The membrane separation device 10 shares an intermediate shell 1m with the heater 30. 2 The system saves 20m of DN25 pipe; energy consumption savings are calculated as follows:

[0057] Equipment reduces external heat dissipation area: The shell structure of membrane separation unit 10 is reduced by 2m. 2 The preheater 20 and heater 30 are each reduced by 1m. 2 The energy loss is reduced by Q1 = (2 + 1 + 1) × 94 = 376 (W).

[0058] The pipeline reduces the external heat dissipation area: the shell structure of the membrane separation unit 10 is reduced by 3.14 × 34 × 20 × 10 mm. -3 =2.14m 2 The energy loss is reduced by Q2 = 2.14 × 94 = 201.16 (W).

[0059] Based on an annual operating time of 8000 hours, the system can save energy of: (376 + 201.16) × 8000 × 10 -3 =4617.28 (kW.h).

[0060] In this embodiment, the permeate vapor separated by the membrane tube directly enters the vacuum condenser 40 connected to the membrane separation device 10 for cooling. The permeate vapor does not need to be transported through pipelines for direct cooling, which reduces frictional resistance, lowers the energy consumption of the vacuum pump, and improves the vacuum level on the vacuum side of the membrane tube, which is beneficial to the dehydration efficiency of the membrane separation device 10. The remaining permeate vapor after cooling and volume reduction is extracted by the vacuum pump through the first vacuum connector 41.

[0061] According to the basic theory of vacuum technology and experimental data verification, it is shown that the length and cross-sectional area of the vacuum pipeline have an important impact on the pressure difference between the permeating steam and the vacuum condenser 40 at the membrane separation device 10. The explanation is as follows: Generally, the vacuum chamber of the vacuum condenser 40 is connected to the vacuum pump through pipelines. The generation of flow resistance is the result of external friction between gas molecules and the wall surface and internal friction or viscosity between gas molecules. This flow resistance is manifested in the form of pressure difference and volume flow rate or pumping speed loss. In vacuum technology, it is customary to use its reciprocal, the flow conductance L or C of the pipeline, to replace the flow resistance W. The flow conductance has the unit of volume flow rate and is usually expressed in [l s -1 , or [m 3 h -1 . The pressure on the permeation side of membrane pervaporation (vapor permeation) dehydration ranges from 10 to 1000 Pa(A), belonging to low vacuum, mainly viscous flow, also known as continuous flow, and is in a laminar flow state during the normal operation of the device. In the case of laminar flow, the formula for calculating the flow conductance of a circular pipeline is:

[0062] Where: l represents the pipe length [cm]; d represents the pipe diameter [cm]; represents the pressure [Pa]; C represents the flow conductance [l s -1 .

[0063] It can be seen from the above formula that in a vacuum system, both the pipe cross-section and the pipe length greatly affect the flow conductance of the circular pipeline. According to the basic equation of vacuum technology:

[0064] S1 is the pumping speed at the outlet of the evacuated container (ls -1 ), and S2 is the pumping speed at the outlet of the evacuated container (ls -1 ).

[0065] It can be seen from this formula that when the flow conductance is much smaller than the pumping speed of the vacuum pump, that is, U << S2, then S1 ≈ U1, that is, the pumping speed of the container can only be equal to the flow conductance of the pipeline at most. In this case, even using a vacuum pump with a large pumping speed to increase the effective speed is ineffective. Similarly, when the flow conductance is much larger than the pumping speed of the vacuum pump, that is, U >> S2, then S1 ≈ S2. At this time, the pumping speed of the container will be mainly determined by the pumping speed of the vacuum pump. If a vacuum pump with a large pumping speed is used at this time, the effective pumping speed of the container can be significantly increased.

[0066] In summary, by directly connecting the vacuum condenser 40 to the permeation side of the membrane separation device 10, that is, without pipeline connection, the pumping speed of the vacuum pump can be reduced, thereby reducing energy consumption, and at the same time, a better vacuum effect can be obtained on the permeation side of the membrane separation device 10.

[0067] In this embodiment, the membrane separation device 10 is further provided with a first heating joint 13 and a second heating joint 14, one of which is a heating medium inlet and the other is a heating medium outlet. By controlling the flow rate of the heating medium in the first heating joint 13 and the second heating joint 14, the heat replenishment effect within the membrane separation device 10 can be flexibly controlled.

[0068] Furthermore, the heater 30 is provided with a first heating connector 31 and a second heating connector 32. One of the first heating connector 31 and the second heating connector 32 is a heating medium inlet and the other is a heating medium outlet. By controlling the heating medium flow rate of the first heating connector 31 and the second heating connector 32, the initial temperature of the material entering the membrane separation device 10 for dehydration can be flexibly controlled.

[0069] Furthermore, the vacuum condenser 40 is equipped with a first vacuum connector 41, a first cooling connector 42, and a second cooling connector 43. The first vacuum connector 41 is connected to a vacuum pump, and the first cooling connector 42 and the second cooling connector 43 are the inlet and outlet of the cooling medium of the vacuum condenser 40, respectively. By controlling the flow rate of the cooling medium at the first cooling connector 42 and the second cooling connector 43, the vacuum level on the vacuum side of the vacuum condenser 40 can be flexibly controlled, thereby improving the membrane separation effect of the membrane separation device 10.

[0070] In another embodiment, several auxiliary devices include a preheater 20 and a heater 30; the preheater 20 is connected to the heater 30 and is used to preheat the material, and the heater 30 is connected to the material chamber of the membrane separation device 10 and is used to heat the material; wherein the preheater 20 and the heater 30 are respectively attached to the outer wall of the membrane separation device 10.

[0071] Understandably, since the preheater 20 and heater 30 are integrated into the membrane separation device 10, the preheater 20 and heater 30 can use the heat generated by the membrane separation device 10 to preheat or keep the material inside the preheater 20 and heater 30 warm, thus saving energy.

[0072] In this embodiment, the preheater 20 and the heater 30 are respectively attached to the upper and lower or left and right sides of the membrane separation device 10, and share the outer wall plate with the membrane separation device 10. This maximizes the utilization of the heat dissipated by the membrane separation device 10, and also increases the heat preservation effect of the inner cavity of the membrane separation device 10. By making full use of space and sharing the shell through a compact arrangement, the equipment cost is saved.

[0073] In another embodiment, several auxiliary devices include a vacuum condenser 40; the vacuum condenser 40 is connected to the vacuum chamber of the membrane separation device 10 and is used to drive the membrane separation device 10 to separate materials; wherein, the permeate side of the membrane separation device 10 is directly connected to the vacuum condenser 40 as a whole.

[0074] It is understandable that since the permeate side of the membrane separation device 10 is directly connected to the vacuum condenser 40, the stroke loss of the pipeline connection can be reduced, the vacuum degree of the permeate side of the membrane separation device 10 can be better, and the vacuum degree loss caused by the pipeline connection can be avoided.

[0075] In this embodiment, no heater or preheater is required, and it can be used for vaporization permeation projects. After the material is preheated, it passes through an independent vaporizer 60 and then through the membrane separation device 10.

[0076] In another embodiment, several auxiliary devices include a vaporizer 60, a preheater 20, and a vacuum condenser 40; the preheater 20 is connected to the vaporizer 60 and is used to preheat the material; the vaporizer 60 is connected to the material chamber of the membrane separation device 10; the vacuum condenser 40 is connected to the vacuum chamber of the membrane separation device 10 and is used to drive the membrane separation device 10 to separate the material; wherein, the preheater 20 is attached to the outer wall of the membrane separation device 10.

[0077] The membrane separation integrated equipment of this embodiment does not require a heater and can be used in vaporization permeation projects. After the material is preheated, it passes through an independent vaporizer 60 and then into the membrane separation device 10, or the material from the gas phase directly enters the membrane separation device 10.

[0078] Understandably, since the preheater 20 is integrated into the membrane separation device 10, the preheater 20 can use the heat generated by the membrane separation device 10 to preheat or keep the material inside the preheater 20 warm, thus saving energy.

[0079] Since the permeate side of the membrane separation device 10 is directly connected to the vacuum condenser 40, the stroke loss of the pipeline connection can be reduced, the vacuum degree of the permeate side of the membrane separation device 10 can be guaranteed to be good, and the vacuum degree loss caused by the pipeline connection can be avoided.

[0080] Specifically, the preheater 20 is attached to the upper, lower, left, or right side of the membrane separation device 10 and shares the outer wall panel with the membrane separation device 10. This maximizes the utilization of heat dissipated by the membrane separation device 10 and also increases the heat insulation effect of the inner cavity of the membrane separation device 10. Of course, the preheater 20 can also be attached to the left or right side of the membrane separation device 10.

[0081] Figure 18 This is a flow chart of the molecular sieve membrane dehydration process for an integrated membrane separation system. Please refer to it as well. Figure 18The membrane separation integrated equipment also includes a feed pump 71, a filter 72, a condensate collection tank 73, a permeate pump 74, detection instruments, a control device, and a frame structure. The feed pump 71, filter 72, condensate collection tank 73, permeate pump 74, detection instruments, control device, membrane separation device 10, and several auxiliary devices are all installed on the frame structure and integrated into a single unit. The frame structure allows for flexible spatial arrangement of functional components such as the feed pump 71, filter 72, condensate collection tank 73, permeate pump 74, detection instruments, and control device within the membrane separation integrated equipment, facilitating the miniaturization and integrated design of the membrane separation integrated equipment.

[0082] Specifically, the membrane separation integrated equipment also includes a raw material tank 75, a product cooler 76, a product tank 77, a product pump 78, and a vacuum pump 79.

[0083] In one embodiment, please refer to Figures 5 to 13 The membrane separation device 10 includes a housing 110 and a first membrane core detachably installed within the housing 110. The first membrane core includes a plurality of first membrane tubes 120 and a plurality of first heating tubes 130. The plurality of first membrane tubes 120 are spaced apart within the housing 110 and are used for separating materials. The plurality of first heating tubes 130 are disposed within the housing 110 and located between the plurality of first membrane tubes 120. The inner wall of the housing 110, the outer walls of the plurality of first membrane tubes 120, and the outer walls of the plurality of first heating tubes 130 enclose a first material cavity 220 for material flow. The plurality of first heating tubes 130 are used to heat the material within the first material cavity 220. This structural arrangement facilitates the flexible arrangement of the first heating tubes 130 within the first material cavity 220, thereby ensuring the uniformity and timeliness of the material reheating by the membrane separation device 10.

[0084] Understandably, the material can be uniformly and timely heated by a number of flexibly arranged first heating tubes 130, so as to keep the material temperature within the preset range. This eliminates the phenomenon that the material temperature drops as the material consumes heat during dehydration, thus affecting the dehydration rate. At the same time, since the material temperature is kept within the preset range, the membrane separation dehydration can always be kept in the high-efficiency zone.

[0085] Using the membrane separation device of the present invention, the material is in full contact with the first heating tube 130 and the first membrane tube 120 during the flow process, realizing the functions of heat transfer and mass transfer. The number and position of the first heating tube 130 and the first membrane tube 120 can be arranged in a certain proportion according to the heat replenishment requirements of membrane dehydration. The heating medium is introduced into the first heating tube 130 to directly heat the raw material, and they are flexibly arranged in the device according to the process requirements to ensure the uniformity and timeliness of heating.

[0086] In one embodiment, the housing 110 includes a first housing 111 and a plurality of second housings 112 detachably connected to the first housing 111. The first housing 111 is provided with a plurality of partition cavities 114, which are correspondingly arranged with the plurality of second housings 112.

[0087] In this embodiment, the membrane separation device 10 includes a plurality of first membrane cores and a plurality of second membrane cores. One or more of the plurality of first membrane cores and the plurality of second membrane cores are disposed in a one-to-one correspondence within a plurality of partition cavities 114. The structures of the first membrane cores and the second membrane cores are different. By using a plurality of different membrane cores in combination, the membrane separation performance of the membrane separation device 10 can be improved.

[0088] In one embodiment, the first membrane core further includes a first membrane shell 170, within which a first receiving cavity 210 is provided. A plurality of first membrane tubes 120 are spaced apart from each other within the first receiving cavity 210, and a plurality of first heating tubes 130 are disposed within the first receiving cavity 210. The cavity wall of the first receiving cavity 210, together with the outer walls of the plurality of first membrane tubes 120 and the plurality of first heating tubes 130, forms a first material cavity 220 for supplying material flow. This arrangement facilitates the integration of the first membrane tubes 120 and the first heating tubes 130 onto the first membrane shell 170, thereby facilitating the disassembly and replacement of the first membrane core.

[0089] In one embodiment, the first membrane core further includes a first partition plate 140, which is disposed on the first membrane shell 170. The first partition plate 140 and the inner cavity of the second shell 112 enclose a first vacuum cavity 230. The first partition plate 140 is provided with a plurality of perforations. The ends of a plurality of first membrane tubes 120 and the ends of a plurality of first heating tubes 130 are respectively inserted through the plurality of perforations of the first partition plate 140 and extend into the first vacuum cavity 230. The first partition plate 140, the plurality of first membrane tubes 120 and the plurality of first heating tubes 130 constitute a membrane core integrated into one unit.

[0090] In this embodiment, the ratio of the number of inner membrane tubes of the plurality of first membrane cores 120 to the number of first heating tubes 130 is different or the same, and one or more of the plurality of first membrane cores are detachably installed in the plurality of partition cavities 114.

[0091] With this configuration, the ratio of the number of first membrane tubes 120 to the number of first heating tubes 130 can be changed by replacing the membrane core, thereby enabling the membrane separation device 10 to adapt to different scenarios and adjust the membrane separation performance of the membrane separation device 10 on materials.

[0092] Specifically, one end of the first membrane tube 120 is connected to the first vacuum chamber 230, and the other end is provided with a first end seal. With this configuration, a vacuum can be formed inside the first membrane tube 120, and its low-pressure state can drive the membrane layer of the first membrane tube 120 to separate materials. In this embodiment, the first separator 140 can be selected as a porous metal plate.

[0093] The membrane separation device 10 of this embodiment facilitates the disassembly, replacement, and maintenance of the membrane core. In this embodiment, the first heating tube 130 is a U-shaped metal tube.

[0094] Of course, in other embodiments, the membrane separation device 10 may not use a removable membrane core. Instead, the ratio of the number of the first membrane tubes 120 to the number of the first heating tubes 130 can be directly changed by detaching and assembling the first heating tubes 130 and the first membrane tubes 120 on the first partition plate 140. However, compared to the membrane core replacement method, it has a lower cost but takes longer to adjust the working time.

[0095] In one embodiment, the membrane separation device 10 further includes a first tube 181 and a second tube 182. The first tube 181 is connected to a plurality of first heating tubes 130 within a first heating group. A plurality of first tubes 181 are provided, each corresponding to one of the plurality of first heating groups. The second tube 182 is connected to a plurality of first tubes 181 to facilitate the collection and exit of the heating medium. Specifically, both the first tube 181 and the second tube 182 are metal tubes. Specifically, the first tube 181 is detachably connected to the plurality of first heating tubes 130 within the first heating group, and the second tube 182 is detachably connected to a plurality of first tubes 181.

[0096] Optionally, the membrane separation device 10 also includes a connecting hose 190, one end of which is detachably connected to an interface on the second tube body 182, and the other end is detachably connected to a first heating inlet 204 or a first heating outlet 205 on the second shell 112.

[0097] Furthermore, in this embodiment, a first membrane core is provided, and a first material inlet 201 and a first material outlet 202 located away from the first material inlet 201 are provided on the first shell 111. Both the first material inlet 201 and the first material outlet 202 are connected to the first material chamber 220. A first vacuum port 203 connected to the first vacuum chamber 230 is provided on the second shell 112. A heating medium flows in the first heating tube 130, and a first heating inlet 204 and a first heating outlet 205 connected to the first heating tube 130 are also provided on the second shell 112. The first heating inlet 204 and the first heating outlet 205 are both located on the second shell 112 to facilitate the disassembly and replacement of the membrane core.

[0098] After entering the first material chamber 220, the material flows laterally through the first membrane tube 120 and the first heating tube 130 for dehydration and reheating, and is forced to flow back and forth by the second partition plate 150 to enhance the dehydration effect. The first heating inlet 204 and the first heating outlet 205 are connected to the second tube body 182 through flexible hoses, which further facilitates assembly and disassembly.

[0099] Of course, two first membrane cores can be provided and respectively inserted on both sides of the first shell 111. Two second shells 112 are provided and respectively detachably connected to both sides of the first shell 111. The first shell 111 is provided with a first material inlet 201 and a first material outlet 202 located away from the first material inlet 201. The first material inlet 201 and the first material outlet 202 are both connected to the first material chamber 220. Each second shell 112 is provided with a first vacuum port 203 connected to the corresponding first vacuum chamber 230. A heating medium flows in the first heating tube 130. Each second shell 112 is also provided with a first heating inlet 204 and a first heating outlet 205 connected to the first heating tube 130, so as to facilitate the membrane cores to be disassembled and replaced from both sides of the first shell 111. The dual membrane core installation structure further improves the filling density of the membrane separation device 10 and reduces the membrane space density of the device.

[0100] In one embodiment, a plurality of first heating tubes 130 are arranged at intervals along a first direction and all extend along a second direction to form a first heating group, and a plurality of first heating groups are arranged at intervals along a third direction; a plurality of first membrane tubes 120 are arranged in an array along the first direction and the third direction and all extend along the second direction to form a first separation group, and a plurality of first separation groups are disposed between two adjacent first heating groups, so that the ratio of the number of first membrane tubes 120 to the number of first heating tubes 130 on the membrane separation device 10 can be adjusted by adjusting the number of first membrane tubes 120 in the first separation group between two adjacent first heating groups. Figure 6 The direction indicated by the middle arrow X is the first direction, the direction indicated by the arrow Y is the second direction, and the direction indicated by the arrow Z is the third direction.

[0101] In one embodiment, the plurality of first membrane tubes 120 and the plurality of first heating tubes 130 are arranged in an equilateral triangle, a cornered equilateral triangle, a square, or a cornered square, thereby ensuring the uniformity and timeliness of the heating of the material by the first heating tubes 130.

[0102] By setting it up in this way, the flow state of the material can be changed to create favorable operating conditions, improve membrane separation efficiency, and reduce membrane process fouling. Based on the flow direction of the material between the first membrane tube 120 and the first heating tube 130, in order to enhance the mixing of the material during the flow process and reduce temperature polarization and concentration polarization, the first membrane tube 120 and the first heating tube 130 can be arranged in the form of an equilateral triangle, a cornered equilateral triangle, a square, or a cornered square, etc., structurally forcing the material flow to reach a turbulent state.

[0103] Meanwhile, the first membrane core features a flexible segmented design to ensure that the flow velocity of the material on the membrane surface reaches the high-efficiency range for membrane dehydration after entering the first membrane core. To demonstrate the scale-up effect of membrane dehydration on an industrial scale, the concept of "industrial dehydration efficiency" is introduced to evaluate the industrial scale-up effect of membrane dehydration, based on the ratio of dehydration volume of the membrane product under laboratory and industrial chemical conditions. This is defined as the permeate flux of an industrial membrane module per square meter of membrane area (in %) under the same process conditions. The industrial dehydration efficiency can reach 100%.

[0104] In one embodiment, the first membrane core further includes a plurality of second partition plates 150, each of which is provided with a plurality of perforations. A plurality of first membrane tubes 120 and a plurality of first heating tubes 130 are respectively inserted through the perforations of the plurality of second partition plates 150. The plurality of second partition plates 150 are staggered and spaced apart from each other along the second direction within the first accommodating cavity 210 to divide the first material cavity 220 into a serpentine flow channel. The spacing between two adjacent second partition plates 150 within the plurality of first membrane cores may be different or the same in the second direction. By replacing the membrane core, the cross-sectional area of ​​material flow can be changed by altering the spacing between two adjacent second partition plates 150 in the second direction, thereby enabling the membrane separation device 10 to adapt to different scenarios and adjust the membrane separation performance of the membrane separation device 10 for materials.

[0105] Understandably, in the field of membrane separation, pervaporation and vaporization are separation processes involving both mass and heat transfer, resulting in concentration and temperature polarization. Therefore, the flow state of the material (feed liquid) on the membrane surface is a crucial factor affecting the separation process. By using a serpentine flow channel structure, the turbulence of the material flow is increased, reducing the concentration and temperature boundary layers and ensuring a more uniform distribution of the material fluid on the membrane surface. This reduces the impact of concentration and temperature polarization on membrane separation performance.

[0106] In this embodiment, the second partition plate 150 can be selected as a metal plate, PTFE plate, PFA plate, etc. Specifically, the first heating tube 130 and the perforation of the first partition plate 140 are detachably and sealingly connected, and the first membrane tube 120 and the perforation of the first partition plate 140 are detachably and sealingly connected.

[0107] Of course, in other embodiments, the first heating tube 130 and the first partition plate 140 can also be fixedly connected through the perforation. The first heating tube 130 and the first partition plate 140 can be fixedly connected by one or more of the following methods: expansion joint, welding, expansion welding, etc.

[0108] In this embodiment, the membrane separation device 10 is cylindrical. Specifically, the first heating tube 130 can be a metal tube, and the first heating inlet 204 and the first heating outlet 205 are connected to the second tube body 182 via flexible hoses for easy assembly and disassembly.

[0109] Taking the structure of the membrane separation device 10 in this embodiment as an example, the shell 110 of the membrane separation device 10 has a diameter of DN900, that is, the diameter of the shell 110 is 900mm. The minimum arrangement spacing between the first membrane tubes 120 is 19mm. The heating tube has an outer diameter of 14mm and a length of 920mm. The outer diameter of the first membrane tube 120 is ф12mm and the length is 1030mm. In one embodiment, the number of first membrane tubes 120 arranged is 1359, and the number of heating tubes is 456.

[0110] The heat exchange area is: 456 × π × 14 mm × 920 mm = 18.49 m² 2 .

[0111] The membrane area is: 1359 × π ​​× 12 mm × 1030 mm = 52.77 m² 2 .

[0112] Therefore, the compensating density is: 18.49 / 52.77 = 0.35m³. 2 / m 2 .

[0113] The membrane packing density is: 52.77 / (π×450) 2 ×1030mm×10 -9 ) = 80.5m 2 / m 3 .

[0114] In another embodiment, the number of first membrane tubes 120 is 1599, and the number of heating metal tubes is 230.

[0115] The heat exchange area is: 230×π×14mm×920mm=9.31m² 2 .

[0116] The membrane area is: 1599 × π ​​× 12 mm × 1030 mm = 62.09 m² 2 .

[0117] The compensating density is then 9.31 m³. 2 / 62.09m 2 =0.15m2 / m 2 .

[0118] The membrane packing density is: 62.09 / (π×450) 2 ×1030×10 -9 ) = 94.8m 2 / m 3 .

[0119] The above structural analysis shows that, under the premise of meeting the heat compensation density, the membrane packing density of the membrane separation device 10 is relatively high and adjustable.

[0120] In one embodiment, the first membrane core further includes a plurality of third partition plates 160. The first partition plates 140, a plurality of first membrane tubes 120, and a plurality of first heating tubes 130 are integrated and installed on the first membrane shell 170. The first membrane shell 170, together with the outer walls of the first partition plates 140, the plurality of first membrane tubes 120, and the plurality of first heating tubes 130, forms a first material cavity 220 for material flow. The first membrane shell 170 is provided with an inlet and an outlet communicating with the first material cavity 220. The plurality of third partition plates 160 are spaced apart from each other in the first material cavity 220 and are arranged parallel to the plurality of first membrane tubes 120 to divide the first material cavity 220 along a first direction to form a plurality of material sub-cavities. The third partition plates 160 are provided with through holes connecting two adjacent material sub-cavities. By such arrangement, the turbulence of material flow is increased, the concentration boundary layer and temperature boundary layer are reduced, and the fluid is more uniformly distributed on the membrane surface, which can reduce the impact of concentration and temperature polarization on membrane separation performance.

[0121] In this embodiment, the spacing between two adjacent third partition plates 160 within several membrane cores may be different or the same in the first direction. By replacing the membrane cores, the material flow cross-sectional area can be changed by altering the spacing between two adjacent third partition plates 160 in the first direction. This allows the membrane separation device 10 to adapt to different scenarios and adjust its membrane separation performance for materials.

[0122] Specifically, the first membrane shell 170 is provided with an inlet and an outlet communicating with the first material chamber 220; the first shell 111 is provided with a first material inlet 201 and a first material outlet 202 located away from the first material inlet 201, the first material inlet 201 and the first material outlet 202 respectively communicating with the inlet and outlet of the first membrane shell 170; the second shell 112 is provided with a first vacuum port 203 communicating with the first vacuum chamber 230; a heating medium flows inside the first heating tube 130, and the second shell 112 is also provided with a first heating inlet 204 and a first heating outlet 205 communicating with the first heating tube 130. In this embodiment, the first heating tube 130 is a U-shaped metal tube.

[0123] With this configuration, the first partition plate 140, several first membrane tubes 120, and several first heating tubes 130 are all integrated and mounted on the first membrane housing 170, facilitating the integration of the membrane core into one unit. Specifically, the first membrane housing 170 is provided with a first guide rail 171, and the first shell 111 is provided with a needle roller sliding device that cooperates with the first guide rail 171, facilitating the assembly and disassembly of the membrane core.

[0124] In one embodiment, a plurality of partition cavities 114 are provided inside the first shell 111, and a plurality of membrane cores are provided, each corresponding to one of the partition cavities 114. A plurality of second shells 112 are provided, each corresponding to one of the first shells 111 and detachably installed on the first shell 111, and together with a plurality of first partition plates 140, they enclose a plurality of first vacuum cavities 230. This facilitates the flexible arrangement of the membrane cores within the shell 110.

[0125] In one embodiment, the membrane core and the membrane separation device 10 are both rectangular. Compared to the traditional cylindrical structure, the rectangular design ensures that the material flows through uniformly, maintaining a stable and controllable state throughout the flow process, thus fully utilizing the dehydration efficiency of the first membrane tube 120. In this embodiment, the internal chambers of the first shell 111 can be infinitely expanded by increasing the number and arrangement of the partition cavities 114, thereby increasing the number of membrane cores installed in a single membrane separation device 10, improving the membrane module's filling density, and reducing the device's membrane space density.

[0126] In the first membrane core of this embodiment, the ratio of the first membrane tube 120 to the first heating tube 130 inside a single membrane core can be flexibly configured according to process requirements. Based on the heat replenishment requirements, to evaluate the heat replenishment capacity of the membrane module equipment, the concept of "heat replenishment density" is introduced, i.e., heat replenishment area / membrane area (unit: m²). 2 / m 2 The value range is 0.1 to 1.3 m. 2 / m 2 According to process calculations, during liquid-phase dehydration, the permeate flow rate is 3 kg per square meter of membrane area, requiring 1.8 kJ of supplementary heat. Using saturated steam at 0.5 MPa and 150°C as the heat source, the required supplementary heating area is 0.6 m². 2 The heat replenishment density can be flexibly set to meet the heat replenishment requirements.

[0127] In addition, while meeting the heat replenishment requirements, the membrane separation unit 10 can achieve a high "filling density", which is the ratio of membrane area to the volume of the first membrane housing 170 (unit: m³). 2 / m 3 The fill density can reach up to 150m³. 2 / m 2 .

[0128] Furthermore, the membrane separation device 10 in this embodiment uses a first membrane core, achieving a large-scale design for a single membrane separation device 10. The membrane area of ​​the membrane separation device 10 can theoretically be infinitely large. Under the condition of meeting the requirements of conventional road transportation (maximum external dimensions not exceeding 2.5m × 2.5m), the membrane area of ​​one membrane core can reach 42.69m². 2 A single membrane separation unit can accommodate up to 16 membrane cores, with a total membrane area of ​​42.69 m². 2 ×16=683.04m 2 .

[0129] The membrane separation device 10 in this embodiment uses a first membrane core, which solves the problems of large number of devices, large footprint, and difficult maintenance in large membrane separation devices 10. To evaluate the physical space occupied by the membrane separation and dehydration device, the concept of "membrane space density" is introduced, which is the minimum installation volume of the membrane module in the membrane separation device 10 divided by the membrane area (unit: m²). 3 / m 2 ), such as the aforementioned 636.8m 2 Taking membrane area devices as an example, the membrane space density can be as low as 0.05m³. 3 / m 2 .

[0130] In one embodiment, please refer to the following: Figures 14 to 17 The second membrane core includes a second membrane shell, a first spacer 320, a plurality of second membrane tubes 330, and a plurality of second heating tubes 340. The first spacer 320 is disposed on the second membrane shell, and the first spacer 320 and the inner cavity of the second membrane shell enclose a second receiving cavity 410. The first spacer 320 and the inner cavity of the second shell 112 enclose a second vacuum cavity 420. The plurality of second membrane tubes 330 are disposed at intervals in the second receiving cavity 410 and are used to separate materials. The plurality of second heating tubes 340 are disposed in the second receiving cavity 410 and are correspondingly sleeved on the outside of the second membrane tubes 330. The outer wall of the second membrane tubes 330 and the inner wall of the second heating tubes 340 enclose a second material cavity 430 for supplying material flow.

[0131] It is understandable that when the number of second membrane tubes 330 is the same as the number of second heating tubes 340, several second heating tubes 340 are fitted one-to-one on the outside of the second membrane tubes 330. When the second membrane core is also provided with a steel pipe for replacing the second membrane tubes 330, then a portion of several second heating tubes 340 are fitted on the outside of the second membrane tubes 330, and another portion is fitted on the outside of the steel pipe, thereby adjusting the membrane area of ​​the membrane separation device.

[0132] In this embodiment, the first partition plate 320 is provided with a plurality of perforations and a plurality of transition channels 321 connecting the plurality of perforations. The ends of a plurality of second membrane tubes 330 are respectively inserted through the plurality of perforations of the first partition plate 320 and extend into the second vacuum chamber 420. The ends of a plurality of second heating tubes 340 are respectively placed in the plurality of perforations of the first partition plate 320, so that the plurality of second material chambers 430 are connected to the plurality of transition channels 321. By conveying materials through the flow channels in the first partition plate 320, it is not necessary to set up a separate raw material chamber in the housing 110 to convey materials into the second material chambers 430, which can extend the effective length of the second membrane tubes 330 and improve the membrane separation performance of the membrane separation device 10.

[0133] Furthermore, by changing the series or parallel connection relationship between several transfer channels 321, the flow cross-sectional area of ​​the material in the membrane separation device 10 can be adjusted, thereby changing the flow rate of the material and thus adjusting the membrane separation performance of the membrane separation device 10 on the material.

[0134] In one embodiment, the series and parallel connections between the plurality of transition channels 321 on the first spacer 320 within the plurality of second membrane cores are different or the same, and one or more of the plurality of second membrane cores are detachably installed in the plurality of partition cavities 114.

[0135] By replacing the membrane core, the series and parallel connections between several transition channels 321 on the first spacer 320 can be altered, thereby changing the material flow rate and adjusting the membrane separation performance of the membrane separation device 10. In this embodiment, the two sides of the first spacer 320 are detachably connected to the first shell 111 and the second shell 112, respectively.

[0136] In one embodiment, a plurality of transition channels 321 of one or more first spacers 320 in a plurality of membrane cores are connected in series. A first interface 325 and a second interface 326 are provided on the first spacer 320, and the first interface 325 and the second interface 326 are respectively connected to the plurality of transition channels 321.

[0137] A portion of a plurality of transition channels 321 of one or more first spacers 320 in a plurality of membrane cores are connected in series to form a first flow group, and another portion of a plurality of transition channels 321 are connected in series to form a second flow group. The first flow group and the second flow group are arranged in parallel. The first spacer 320 is provided with two first interfaces 325 and two second interfaces 326. One of the two first interfaces 325 is connected to the first flow group and the other is connected to the second flow group. One of the two second interfaces 326 is connected to the first flow group and the other is connected to the second flow group.

[0138] By replacing the membrane core, the series and parallel connection relationships between several transition channels 321 on the first partition plate 320 can be changed, thereby changing the flow rate of the material and adjusting the membrane separation performance of the membrane separation device 10 on the material.

[0139] In one embodiment, a second membrane core is provided, a second heating inlet 401 is provided on the first shell 111, and a second heating outlet 402 is provided away from the second heating inlet 401; a second vacuum port 403 connected to the second vacuum chamber 420 is provided on the second shell 112; a first interface 325 and a second interface 326 are provided on the first partition plate 320, and the first interface 325 and the second interface 326 are respectively connected to a plurality of transfer channels 321, thereby facilitating the integration, disassembly and assembly of the membrane core, and a single membrane core device is adopted.

[0140] Of course, two second membrane cores can also be provided and inserted into both sides of the first shell 111 respectively. Two second shells 112 are provided and detachably connected to both sides of the first shell 111 respectively. Each second shell 112 is provided with a second vacuum port 403 that communicates with the corresponding second vacuum chamber 420. The first partition plate 320 is provided with a first interface 325 and a second interface 326. The first interface 325 and the second interface 326 are respectively connected to several transition channels 321, and a dual-membrane core device is adopted.

[0141] In one embodiment, the first partition plate 320 has several transfer channels 321 divided into several material flow groups, and the transfer channels 321 in each material flow group are connected in series. The first partition plate 320 is provided with several first interfaces 325 and several second interfaces 326, and each first interface 325 and each second interface 326 is connected to each material flow group in a corresponding manner. The membrane separation device 10 also includes several first regulating tubes, one or more of which are detachably connected to several first interfaces 325 and several second interfaces 326 to change the series or parallel relationship between the material flow groups.

[0142] By using the connection control of several first regulating pipes, the series and parallel connection relationship between several transfer channels 321 on the first partition plate 320 is changed, thereby changing the flow rate of the material and adjusting the membrane separation performance of the membrane separation device 10 on the material.

[0143] In one embodiment, the first partition plate 320 has several transfer channels 321 divided into four material flow groups, each material flow group including a first group, a second group, a third group, and a fourth group; the first partition plate 320 is provided with four first interfaces 325 and four second interfaces 326, each first interface 325 including one port connected to the first group, one and two ports connected to the second group, one and three ports connected to the third group, and one and four ports connected to the fourth group, each second interface 326 including two ports connected to the first group, two and two ports connected to the second group, two and three ports connected to the third group, and two and four ports connected to the fourth group; the second shell 112 is provided with a second material inlet 404 and a second material outlet 405.

[0144] Among them, the first detachable connection of the plurality of first regulating pipes is to the second material inlet 404 and the first port; the second detachable connection of the plurality of first regulating pipes is to the second material outlet 405 and the second port 4; the third detachable connection of the plurality of first regulating pipes is to the second port 1 and the second port 2; the fourth detachable connection of the plurality of first regulating pipes is to the second port 2 and the third port 3; and the fifth detachable connection of the plurality of first regulating pipes is to the second port 3 and the fourth port 4.

[0145] Alternatively, the first of a plurality of first regulating tubes is detachably connected to the second material inlet 404 and port 1, the second of a plurality of first regulating tubes is detachably connected to the second material inlet 404 and port 12, the third of a plurality of first regulating tubes is detachably connected to the second material inlet 404 and port 13, and the fourth of a plurality of first regulating tubes is detachably connected to the second material inlet 404 and port 14.

[0146] The fifth of a plurality of first regulating pipes is detachably connected to the second material outlet 405 and the second outlet 21; the sixth of a plurality of first regulating pipes is detachably connected to the second material outlet 405 and the second outlet 22; the seventh of a plurality of first regulating pipes is detachably connected to the second material outlet 405 and the second outlet 23; and the eighth of a plurality of first regulating pipes is detachably connected to the second material outlet 405 and the second outlet 24.

[0147] By using the connection control of several first regulating pipes, the series and parallel connection relationship between several transfer channels 321 on the first partition plate 320 is changed, thereby changing the flow rate of the material and adjusting the membrane separation performance of the membrane separation device 10 on the material.

[0148] In one embodiment, the first spacer 320 is provided with a first interface 325 and a second interface 326, which are respectively connected to a plurality of transfer channels 321; a plurality of second shells 112 are respectively provided with a second material inlet 404 connected to the corresponding first interface 325 and a second material outlet 405 connected to the corresponding second interface 326. This facilitates the flexible arrangement of a plurality of membrane cores within the shell 110.

[0149] The membrane separation device 10 also includes several second regulating pipes, one or more of which are detachably connected to several second material inlets 404 and several second material outlets 405 to change the series or parallel relationship between the membrane cores.

[0150] By using the connection and control of several second regulating pipes, the series and parallel relationships between each membrane core can be changed, thereby changing the flow rate of the material and adjusting the membrane separation performance of the membrane separation device 10.

[0151] In addition to changing the series-parallel relationship of material flow through the second regulating pipe and connecting it with the material flow group in the membrane core, different materials can be input into different membrane cores to meet the need for the same equipment to process multiple materials at the same time.

[0152] In one embodiment, the membrane separation device 10 further includes an adapter plate 350, which is provided with a plurality of fixing holes. One end of a plurality of second heating tubes 340 is placed in a plurality of through holes in the first spacer plate 320, and the other end is placed in a plurality of fixing holes in the adapter plate 350. The adapter plate 350 is also provided with a plurality of connecting channels that connect the plurality of fixing holes, thereby achieving support on the other side of the second membrane tube 330 and the second heating tube 340.

[0153] Of course, in other embodiments, the membrane separation device 10 also includes a transfer tube 360, which is U-shaped and has its two ends connected to two corresponding second heating tubes 340, thereby supporting the other side of the second membrane tube 330 and the second heating tube 340, and transferring materials through the transfer tube 360.

[0154] In one embodiment, the first partition plate 320 includes a first side plate 322 and a second side plate 323 attached to the first side plate 322. The first side plate 322 is provided with a plurality of first holes, and the second side plate 323 is provided with a plurality of second holes corresponding to the plurality of first holes. The first holes and the second holes constitute the perforations of the first partition plate 320. The end of the second membrane tube 330 passes through the first holes and the second holes and extends into the second vacuum chamber 420. The end of the second heating tube 340 is inserted into the first hole. The second side plate 323 is provided with a plurality of transition grooves on the side near the first side plate 322. The plurality of transition grooves and the first side plate 322 surround each other to form a plurality of transition channels 321. By separating the two, the processing and setting of the first partition plate 320 is facilitated, and the cost is low.

[0155] Specifically, both the first side plate 322 and the second side plate 323 are porous metal plates. The second membrane tube 330 and the first spacer 320 can be connected and fixed by one or more methods such as expansion joint, welding, and expansion welding. A sealing plate 324 is also provided between the first side plate 322 and the second side plate 323.

[0156] In one embodiment, the adapter plate 350 includes a first adapter plate 351 and a second adapter plate 352 attached to the first adapter plate 351. The first adapter plate 351 is provided with a plurality of first rotating holes, and the second adapter plate 352 is provided with a plurality of second rotating holes corresponding to the plurality of first rotating holes. The first rotating holes and the second rotating holes constitute the fixing holes of the adapter plate 350. The end of the second membrane tube 330 passes through the first rotating holes and the second rotating holes, and the end of the second heating tube 340 is inserted into the first hole. The second adapter plate 352 is provided with a plurality of connecting grooves on the side near the first adapter plate 351. The plurality of connecting grooves and the first adapter plate 351 enclose a plurality of connecting channels.

[0157] The separate design facilitates the processing and setup of the adapter board 350, resulting in lower costs.

[0158] In one embodiment, one end of a plurality of second membrane tubes 330 extends into the second vacuum chamber 420, and the other end is respectively provided with a plug, thereby facilitating the formation of a vacuum in the second membrane tubes 330. The low pressure and vacuum state can drive the membrane layer of the second membrane tubes 330 to separate materials.

[0159] Of course, in other embodiments, the adapter plate 350 also includes a sealing plate 353, which replaces the sealing. The sealing plate 353 is attached to the side of the second adapter plate 352 away from the first adapter plate 351. The sealing plate 353 has several sealing grooves on the side of the second adapter plate 352. One end of several second membrane tubes 330 extends into the second vacuum chamber 420, and the other end is respectively sealed in several sealing grooves.

[0160] In this embodiment, the cavity wall of the second accommodating cavity 410 and the outer wall of the second heating tube 340 surround each other to form a second heating cavity 440. The housing 110 is provided with a second heating inlet 401 that communicates with the second heating cavity 440 and a second heating outlet 402 that is disposed away from the second heating inlet 401.

[0161] The membrane separation device 10 also includes a second partition plate 370. Each of the second partition plates 370 is provided with a number of perforations. A number of second membrane tubes 330 and a number of second heating tubes 340 are respectively inserted through the number of perforations of the second partition plates 370. The second partition plates 370 are staggered and spaced apart from each other in the second accommodating cavity 410 to divide the second heating cavity 440 into a serpentine flow channel, which facilitates stable and uniform heating of the material.

[0162] In one embodiment, the second shell 112 is provided with a second material inlet 404 and a second material outlet 405, facilitating the detachable installation of the membrane core. Taking the second heating tube 340 as having a specification of ф20×2mm and the second membrane tube 330 having a diameter of 12mm as an example, the internal material flow cross-sectional area corresponding to a single second membrane tube 330 is 88mm². 2 The second heating tube 340 can be connected in parallel, either individually or in multiples, through the upper flow channel of the first partition plate 320, meaning the material flow cross-sectional area can be 88 mm². 2 The length difference between the second heating tube 340 and the second membrane tube 330 is only more than twice the wall thickness of the first partition plate 320. The material feeding chamber and the flow chamber between the two passes are very small, which maximizes the effective utilization length of the second membrane tube 330.

[0163] In one embodiment, the membrane core and the membrane separation device 10 are both rectangular. Compared to the traditional cylindrical structure, the rectangular design ensures that the material flows through uniformly, maintaining a stable and controllable state during flow and fully utilizing the dehydration efficiency of the second membrane tube 330. In this embodiment, the internal chambers of the first shell 111 can be infinitely expanded by increasing the number and arrangement of the partition cavities 314, thereby increasing the number of membrane cores installed in a single membrane separation device 10, improving the membrane module packing density, and reducing the membrane space density of the device.

[0164] The membrane separation device 10 of the present invention employs a second membrane core. The material flows longitudinally through the gap between the second heating tube 340 and the second membrane tube 330. After reaching the first partition plate 320, the flow direction changes in the flow channel on the first partition plate 320 and flows to the next set of second membrane tubes 330. During the back-mixing process, the material is more fully back-mixed, eliminating concentration and temperature differences. At the same time, the heat medium outside the second heating tube 340 provides uniform heating to the material through the heat conduction of the second heating tube 340, so that the material in the membrane separation device 10 is in a temperature controllable state throughout the dehydration process. The temperature of the heat medium can be adjusted according to different dehydration depth requirements to ensure that the material is in a constant temperature state within the membrane module.

[0165] To assess the heat compensation capacity of membrane module equipment based on the required heat compensation, the evaluation parameter "heat compensation density" is introduced. "Heat compensation density" is calculated as heat compensation area / membrane area (unit: m²). 2 / m 2 The compensating density value is ≥1.4m³. 2 / m 2Taking a second heating tube 340 with a specification of ф20×2mm, a second membrane tube 330 with a diameter of 12mm and a length of 1000mm, and a first spacer 320 with a thickness of 30mm as an example, if the number of second membrane tubes 330 and metal tubes is both n, then the heat replenishment density is π×20×(1000-2×30)×n / (π×12×1000×n)=1.57m 2 / m 2 .

[0166] It is understandable that when the membrane separation device 10 uses both the first membrane element and the second membrane element, please refer to [the relevant documentation / reference]. Figures 1 to 4 The first material connector 11, the second material connector 12, the first heating connector 13, and the second heating connector 14 are provided in three sets. When the first membrane core is used, the corresponding first material connector 11 and the second material connector 12 are used as material inlets and outlets, and the corresponding first heating connector 13 and the second heating connector 14 are used as heating inlets and outlets. When the second membrane core is used, the corresponding first material connector 11 and the second material connector 12 are used as heating inlets and outlets, and the corresponding first heating connector 13 and the second heating connector 14 are used as material inlets and outlets, so that the two types of membrane cores can be used simultaneously.

[0167] If the raw material has a high moisture content and needs to be dehydrated to a very low moisture content, two types of membrane cores can be used simultaneously. The first membrane core is used in the front section of the membrane separation device 10, and the second membrane core is connected in series in the rear section. That is, in the chamber where the second membrane core is installed, both sides of the heating tube are material chambers. Since the deep dehydration section requires less heat, the heat of the material on the outside can supplement the material being dehydrated inside, thereby reducing energy loss.

[0168] This invention also discloses a method for adjusting a membrane separation device; please refer to [link / reference]. Figures 1 to 18 The adjustment method is applied to the membrane separation device of any of the above embodiments, and the adjustment method includes the following steps:

[0169] The ratio of the number of first membrane tubes 120 to the number of first heating tubes 130 is changed to adjust the membrane separation performance of the membrane separation device 10 on the material, so that the membrane separation device 10 can adapt to different scenarios and adjust the membrane separation performance of the membrane separation device 10 on the material.

[0170] In one embodiment, the housing 110 includes a first housing 111 and a plurality of second housings 112 detachably connected to the first housing 111. The first housing 111 has a plurality of partition cavities 114, which are correspondingly arranged with the plurality of second housings 112. The membrane separation device 10 includes a plurality of first membrane cores and a plurality of second membrane cores, one or more of which are correspondingly disposed within the plurality of partition cavities 114. The structures of the first membrane cores and the second membrane cores are different. The adjustment method includes the following steps:

[0171] By changing the series or parallel connection between several first membrane cores and several second membrane cores, the flow cross-sectional area of ​​the material in the membrane separation device 10 can be adjusted, thereby changing the flow rate of the material and thus adjusting the membrane separation performance of the membrane separation device for the material.

[0172] The first membrane element is installed in the dewatering section with high material moisture content. As water is removed from the material, the second membrane element is installed in the dewatering section with low material moisture content. This ensures that the requirements for heat replenishment and flow rate are met in different dewatering membrane separation devices, thereby improving the membrane separation performance of the membrane separation equipment.

[0173] Understandably, please refer to Figure 19 and Figure 20 Taking ethanol pervaporation as an example, under the same membrane tube performance conditions, the two factors affecting the dehydration efficiency of the membrane separation device are the material flow rate and the material temperature. Therefore, by controlling the material flow rate and the material temperature, the membrane separation efficiency and dehydration efficiency of the membrane separation device can be adjusted. The material flow rate can be adjusted by adjusting the material flow cross-sectional area, and the material temperature can be adjusted by adjusting the heating efficiency and heat compensation density of the heating tube.

[0174] Comparative Example 1: Please refer to Figure 21 The traditional sleeve-type membrane module structure uses membrane tubes with an outer diameter of ф12mm and a length of 1030mm. Taking a DN900 diameter as an example: the shell diameter is 900mm, and the inner radius of the shell is 450mm. To meet the installation space requirements for the membrane tubes with an outer diameter of ф12mm, the sleeves are selected with an outer diameter of ф20mm × 2mm (i.e., an inner diameter of ф16mm), and the minimum spacing between the sleeves is 26mm. Considering structural design and manufacturing feasibility, the raw material chamber occupies a relatively large space due to the need to accommodate material inlet / outlet and welding space for the shell 110. The raw material chamber is divided into 8 stages by partition plates. Considering the welding operation space between the partition plates and the shell 110 and the first inner tube plate, it is not suitable to add more partition plates. At the same time, adding more partition plates will affect the number of membrane tubes that can be arranged. Each stage has 100 membrane tubes. As shown in the figure, this equipment can arrange a maximum of 800 heat exchange tubes, with 800 membrane tubes, of which the length of the heat exchange tubes is 590mm.

[0175] The heat replenishment area is: 800 × π × 20 × 590 = 29.7 m²2 .

[0176] The membrane area is: 800 × π × 12 × 10³⁰ = 31.06 m² 2 .

[0177] Therefore, the compensating density is: 29.7 / 31.06 = 0.96 m³. 2 / m 2 .

[0178] The membrane packing density is: 31.06 / (π×450) 2 ×1030×10 -9 ) = 47.4m 2 / m 3 .

[0179] Material flow cross-sectional area: 100×∏×(16 2 -12 2 ) / 4 = 8796mm 2 .

[0180] Structural analysis shows that the heat replenishment area of ​​the traditional sleeve-type membrane module structure is not adjustable, the material flow cross-sectional area is not adjustable, and it is not feasible to make it smaller.

[0181] Comparative Example 2: Please refer to Figure 22 The traditional baffle-type membrane module structure uses membrane tubes with an outer diameter of ф12mm and a length of 1030mm. Taking a DN900 diameter as an example: the shell diameter is 900mm, and the inner radius of the shell is 450mm. Considering the sealing and installation space of the membrane tubes, the minimum spacing between the membrane tubes is 19mm, so the number of membrane tubes that can be arranged is approximately 1750. The length of the heat replenishment jacket is limited by the material inlet / outlet and equipment flange fastener installation requirements; the jacket length is 622mm, and the maximum jacket length can be 920mm.

[0182] The heat exchange area is: 622 × π × 900 = 1.5m² 2 Or 920 × π × 900 = 2.6m 2 .

[0183] The membrane area is: 1750 × π × 12 × 10³⁰ = 67.95 m² 2 .

[0184] Therefore, the compensating density is: 1.5 / 67.95 = 0.02m³. 2 / m 2 Or 2.6 / 67.95 = 0.04m 2 / m 2 .

[0185] The membrane packing density is: 67.95 / (π×450) 2 ×1030×10-9 ) = 103.7m 2 / m 3 .

[0186] Structural analysis shows that the heating area of ​​the jacketed baffle membrane module is not adjustable. The material flow cross-sectional area can be adjusted by adjusting the spacing between the baffles, but since the material needs to flow through the entire cross-section of the equipment, it is not feasible to make it too small.

[0187] Example 1: Please refer to Figures 6 to 13 The membrane tube has an outer diameter of ф12mm and a length of 1030mm. The first membrane core is a rectangular membrane core structure that combines heat transfer and mass transfer functions. The distance w between the two third partition plates 160 is adjustable. The number of cavities and partitions A (which must be an even number) formed by the third partition plates 160 are adjustable. The spacing L between the second partition plates 150 is adjustable. The spacing d between the first heating tubes is adjustable. The number of rows B of the first heating tubes is adjustable (which must be an even number). The number m of the first membrane tubes between the first heating tubes depends on the spacing d. The maximum number of membrane tubes n per row and the number of first heating tubes C per row and per partition depends on A. The straight section length of the first heating tube is 1000mm.

[0188] The heat replenishment area is: A×B×C×∏×14×(1000+∏d / 2).

[0189] As shown in the example, 4×6×5×π×14×(1000+π×168 / 2)=6.67m 2 .

[0190] The membrane area is: (mn-[m / 2])(B-1)A×∏×12×1030.

[0191] As shown in the example, (10×6-[10 / 2])×(6-1)×4×π×12×1030=42.69m 2 .

[0192] Therefore, the compensating density is: 6.67 / 42.69 = 0.16 m³. 2 / m 2 .

[0193] The membrane packing density is: 42.69 / (1000×500×1030×10 -9 ) = 82.9m 2 / m 3 .

[0194] The cross-sectional area for material flow is L(w-12×n); as shown in the example, 100×(125-12×6)=5300mm. 2 .

[0195] As can be seen from the structure in the figure and the calculation formula above, changing the d value can change the ratio of the number of the first membrane tube to the number of the first heating tube to adapt to the needs of different dehydration scenarios; changing the L and w values ​​can adjust the cross-sectional area of ​​the material flow to meet the optimal dehydration efficiency for different processing volumes of material, even if the flow velocity of the material on the membrane surface is ≥0.5m / s (pervaporization). That is, the membrane dehydration industrial device eliminates the scale-up effect of conventional chemical equipment and achieves a high efficiency of 100% industrial dehydration efficiency.

[0196] Example 2: Please refer to the following as well. Figures 14 to 17 The membrane separation device adopts a second membrane core structure. The membrane tube has an outer diameter of ф12mm and a length of 1030mm. Taking a DN900 diameter as an example, the sleeve has an outer diameter of ф20×2mm (i.e., an inner diameter of ф16mm), and the minimum spacing between the sleeves is 26mm. Using a multi-inlet single-channel design, four dewatering zones are set up in each of the four quadrants. A1 and A2, B1 and B2, C1 and C2, and D1 and D2 form four inlet / outlet groups. All eight inlets / outlets are detachable, and a total of 980 sleeves are arranged. The straight section length of the heat-replenishing metal pipe is 920mm.

[0197] The heat replenishment area is: 980 × π × 20 × 920 = 56.65 m² 2 .

[0198] The membrane area is: 980 × π × 12 × 10³⁰ = 38.05 m² 2 .

[0199] Therefore, the compensating density is: 56.65 / 38.05 = 1.49 m³. 2 / m 2 .

[0200] The membrane packing density is: 38.05 / (π×450) 2 ×1030×10 -9 ) = 58.1m 2 / m 3 .

[0201] Material flow cross-sectional area: 1×∏×(16) 2 -12 2 ) / 4 = 88mm 2 (Single area)

[0202] Series-parallel connection configuration within a single membrane module: Method 1: After the material enters the membrane housing from the inlet manifold, it simultaneously enters from A1, B1, C1, and D1, and flows out from A2, B2, C2, and D2 to the outlet manifold before exiting the membrane housing. The cross-sectional area of ​​the material is then: 4 × 88 = 352 mm². 2 .

[0203] Method 2: Short pipes connect inlets A2 and B2, and C2 and D2. Material enters the membrane shell from the inlet manifold, then simultaneously enters from A1 and C1, and flows out from B1 and D1 to the outlet manifold before exiting the membrane shell. The cross-sectional area of ​​the material is: 2 × 88 = 196 mm². 2 .

[0204] Method 3: Short pipes connect the inlets A2 and B2, C2 and D2, and B1 and D1. After the material enters the membrane shell from the inlet manifold, it simultaneously enters from A1, flows out from C1, and exits the membrane shell through the outlet manifold. The cross-sectional area of ​​the material is then: 1 × 88 = 88 mm². 2 .

[0205] Method 4: When there are multiple membrane modules or multiple membrane cores, the above three connection methods within a single membrane module can be achieved through series and parallel connections between multiple membrane modules.

[0206] The membrane separation device of this embodiment can control the material flow rate to match the application requirements of different scenarios by selecting one or both of the first membrane core and the second membrane core, so as to achieve the dehydration target with fewer membranes.

[0207] The above description discloses only preferred embodiments of the present invention and should not be construed as limiting the scope of the present invention. Therefore, equivalent variations made in accordance with the claims of the present invention are still within the scope of the present invention.

Claims

1. A membrane separation device, characterized in that, The membrane separation equipment includes a membrane separation device and several auxiliary devices for providing membrane separation conditions for the membrane separation device. The membrane separation device includes a housing and a first membrane core that is detachably installed inside the housing. The first membrane core includes a plurality of first membrane tubes and a plurality of first heating tubes. The plurality of first membrane tubes are spaced apart from each other in the housing and are used to separate materials. The plurality of first heating tubes are disposed in the housing and located between the plurality of first membrane tubes. The inner wall of the housing, the outer walls of the plurality of first membrane tubes, and the outer walls of the plurality of first heating tubes enclose a first material cavity for material flow. The plurality of first heating tubes are used to heat the material in the first material cavity.

2. The membrane separation device according to claim 1, characterized in that, The housing includes a first housing and a plurality of second housings detachably connected to the first housing. The first housing has a plurality of partition cavities, which correspond one-to-one with the plurality of second housings. The membrane separation device includes a plurality of first membrane cores and a plurality of second membrane cores, one or more of the plurality of first membrane cores and a plurality of second membrane cores being disposed in a one-to-one correspondence within a plurality of the separation cavities, wherein the structures of the first membrane cores and the second membrane cores are different.

3. The membrane separation device according to claim 2, characterized in that, The first membrane core further includes a first membrane shell, in which a first receiving cavity is provided, a plurality of first membrane tubes are disposed at intervals in the first receiving cavity, and a plurality of first heating tubes are disposed in the first receiving cavity. The cavity wall of the first receiving cavity, together with the outer walls of the plurality of first membrane tubes and the outer walls of the plurality of first heating tubes, forms a material cavity for supplying material flow.

4. The membrane separation device according to claim 3, characterized in that, The first membrane core further includes a first partition plate, which is disposed on the first membrane shell. One side of the first partition plate and the inner cavity of the first membrane shell form the first receiving cavity, and the other side of the first partition plate and the inner cavity of the second shell form the first vacuum cavity. The first partition plate is provided with a plurality of perforations, and the ends of a plurality of the first membrane tubes and the ends of a plurality of the first heating tubes are respectively inserted through the plurality of perforations of the first partition plate and extend into the first vacuum chamber; The ratio of the number of membrane tubes to the number of heating tubes in a plurality of first membrane cores may be different or the same, and one or more of the plurality of first membrane cores may be detachably installed in a plurality of partition cavities.

5. The membrane separation device according to claim 4, characterized in that, The first membrane core further includes a plurality of second partition plates, each of which is provided with a plurality of perforations. A plurality of first membrane tubes and a plurality of first heating tubes are respectively inserted through the plurality of perforations of the plurality of second partition plates. The plurality of second partition plates are arranged at intervals and staggered with each other in the second direction within the first accommodating cavity to divide the first material cavity into a serpentine flow channel. The spacing between two adjacent second separator plates within a certain first membrane core may be different or the same in the second direction.

6. The membrane separation device according to claim 5, characterized in that, The second membrane core includes: Second membrane shell; A first spacer is disposed on the second membrane shell. The first spacer and the inner cavity of the second membrane shell enclose a second accommodating cavity, and the first spacer and the inner cavity of the second shell enclose a second vacuum cavity. A plurality of second membrane tubes are arranged at intervals within the second accommodating cavity and are used to separate materials; And a plurality of second heating tubes, wherein the plurality of second heating tubes are disposed in the second accommodating cavity and correspondingly sleeved on the outside of the second membrane tube, the outer wall of the second membrane tube and the inner wall of the second heating tube enclose each other to form a second material cavity for supplying material flow; The first spacer plate is provided with a plurality of perforations and a plurality of transition channels connecting the plurality of perforations. The ends of the plurality of second membrane tubes are respectively inserted through the plurality of perforations of the first spacer plate and extend into the second vacuum chamber. The ends of the plurality of second heating tubes are placed one by one in the plurality of perforations of the first spacer plate, so that the plurality of second material chambers are connected to the plurality of transition channels.

7. The membrane separation device according to claim 6, characterized in that, The series or parallel connections between the transfer channels on the first spacer plate within the plurality of second membrane cores may be different or the same, and one or more of the plurality of second membrane cores may be detachably installed in the plurality of the partition cavities.

8. The membrane separation apparatus according to any one of claims 1 to 7, characterized in that, The membrane separation device and several of the auxiliary devices are integrated into a single unit. The auxiliary devices include at least one of a preheater, a heater, and a vacuum condenser.

9. A method for adjusting a membrane separation device, the method being applied to the membrane separation device according to any one of claims 1 to 8, the method comprising the following steps: The ratio of the number of the first membrane tubes to the number of the first heating tubes is changed to adjust the membrane separation performance of the membrane separation device for materials.

10. The adjustment method for the membrane separation equipment according to claim 9, characterized in that, The housing includes a first housing and a plurality of second housings detachably connected to the first housing. The first housing has a plurality of partition cavities, which correspond one-to-one with the plurality of second housings. The membrane separation device includes a plurality of first membrane cores and a plurality of second membrane cores, one or more of the plurality of first membrane cores and a plurality of second membrane cores being disposed in a plurality of the partition cavities in a one-to-one correspondence, and the structures of the first membrane cores and the second membrane cores are different. The adjustment method includes the following steps: By changing the series or parallel connection between a number of the first membrane cores and a number of the second membrane cores, the flow cross-sectional area of ​​the material in the membrane separation device can be adjusted.

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