Hollow fiber type gas membrane separator
By using a double-stage membrane separator and a fiber tube with a sandwich structure in the hollow fiber gas membrane separator, the problems of poor mechanical properties and poor pollution resistance are solved, and the effect of high-purity gas separation and extending the membrane life is achieved.
Patent Information
- Application Number
- CN202510373725.3
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2025-03-27
- Publication Date
- 2025-05-13
AI Technical Summary
The supporting layer and membrane layer distribution structure of the existing hollow fiber membrane separator leads to poor mechanical properties, poor pollution resistance and high permeability attenuation of the membrane material.
Using a double-stage gas membrane separator, the raw gas is first passed through a high permeability membrane material, and then separated by a high selective membrane material. Combined with the sandwich structure of the intermediate membrane layer of the inner and outer support layer, the mechanical properties and pollution resistance of the fiber tube are enhanced.
It improves the purity of the gas, extends the service life of the film material, enhances the mechanical strength and pollution resistance of the fiber wire, and reduces the permeability attenuation speed.
Smart Images
Figure CN119971777A_ABST
Abstract
Description
Technical Field
[0001] The invention relates to the technical field of separators, and in particular to a hollow fiber gas membrane separator. Background Art
[0002] Hollow fiber membrane is a microporous tubular structure with a separation layer (such as a dense polymer membrane or a ceramic membrane) coated on the inner or outer wall. / When mixed gas is driven by pressure, different components of the mixed gas have different speeds of passing through the membrane due to differences in molecular size and diffusion rate, forming The "quick breath" and The "slow breath" It penetrates into the hollow fiber tube and is enriched at one end of the separator to form permeate gas. The non-permeate gas is enriched in the boundary area between the hollow fiber tube and the shell.
[0003] The hollow fiber membrane separators currently on the market use a hollow fiber tube with a support layer and a membrane layer. The internal and external distribution of the support layer and the membrane layer are adjusted according to whether it is internal pressure or external pressure to separate the mixed raw gas. The mechanical properties are poor, and the anti-pollution performance of the hollow fiber tube is not good. In addition, as the use time increases, the permeability attenuation of the membrane material is likely to increase, and the recovery rate after cleaning is not good enough. Summary of the invention
[0004] The present invention provides a hollow fiber gas membrane separator to solve the defects in the prior art that the supporting layer and membrane layer distribution structure easily lead to poor mechanical properties of the hollow fiber tube, poor anti-pollution and high permeability attenuation of the membrane material.
[0005] The present invention provides a hollow fiber gas membrane separator, comprising: A mounting base, wherein connecting supports are arranged on both sides of the upper end of the mounting base, and a cooler is arranged on the rear side of the upper end of the mounting base; a separation assembly, wherein the separation assembly comprises a primary membrane separator and a secondary membrane separator arranged on the front side of the upper end of the mounting base, and the membrane separators are respectively connected to the mounting base through the connecting supports on both sides; a conveying pipeline assembly, wherein the conveying pipeline assembly comprises a plurality of pipelines arranged between the primary membrane separator and the secondary membrane separator; a pipeline control component, wherein the pipeline control component comprises a check valve, a temperature control valve and a high differential pressure interlock arranged on the conveying pipeline assembly.
[0006] Optionally, the membrane separator includes a shell, the outside of the shell is fixedly connected to a connecting support, a plurality of hollow fiber filaments are arranged inside the shell, and the hollow fiber filaments are neatly arranged and fully sealed at one end with epoxy resin, and the other end is sealed with epoxy resin for gaps therebetween, and the hollow fiber filaments are sealed and connected to the shell through sealing rubber rings provided at the sealing end and the sealing end.
[0007] Optionally, the hollow fiber filament includes an innermost internal support layer, a separation membrane layer is arranged outside the internal support layer, an external support layer is arranged outside the separation membrane layer, and the pore size of the external support layer is larger than the pore size of the internal support layer, the separation membrane layer inside the first-level membrane separator is a high permeability membrane, and the separation membrane layer inside the second-level membrane separator is a high selectivity membrane.
[0008] Optionally, a raw gas inlet pipe is provided on the side of the shell outside close to the sealing end of the hollow fiber filament, and a non-permeate gas outlet pipe is provided on the side of the shell outside close to the sealing end of the hollow fiber filament. The raw gas inlet pipe and the non-permeate gas outlet pipe are located on opposite sides of the shell, and a permeate gas outlet pipe is provided on the top end of the shell outside.
[0009] Optionally, the delivery pipeline assembly includes a high-temperature gas delivery pipe arranged on the rear side of the first-level membrane separator, one end of the high-temperature gas delivery pipe is connected to the air inlet of the cooler, the check valve is connected to the other end of the high-temperature gas delivery pipe, a secondary gas delivery pipe is arranged on the rear side of the second-level membrane separator, the rear end of the secondary gas delivery pipe is connected to the air outlet of the cooler, and a permeate gas collection and discharge pipe is arranged at the upper end of the membrane separator.
[0010] Optionally, the check valve is connected to the non-permeate gas outlet pipe of the primary membrane separator, the front end of the secondary gas delivery pipe is connected to the raw gas inlet pipe of the secondary membrane separator, and a pressure gauge is provided on the high-temperature gas delivery pipe.
[0011] Optionally, a high differential pressure interlock is provided on the high-temperature gas delivery pipe, and a pressure gauge is located between the check valve and the high differential pressure interlock, and a temperature control valve is provided on the secondary gas delivery pipe.
[0012] Optionally, when the temperature of the gas introduced into the secondary gas delivery pipe is lower than 40° C., the temperature control valve is opened, and when the temperature of the gas introduced into the secondary gas delivery pipe is higher than 40° C., the temperature control valve is closed.
[0013] Optionally, the feed gas introduced into the primary membrane separator is preheated, and the gas pressure inside the secondary membrane separator is lower than that of the primary membrane separator.
[0014] The hollow fiber gas membrane separator provided by the present invention has the following technical effects or advantages: 1. The raw gas is separated by a two-stage gas membrane separator. The raw gas is preheated before entering the first-stage membrane separator to make the temperature of the raw gas higher than the dew point to prevent the liquid from condensing on the fiber surface of the membrane separator when the raw gas passes through the surface of the subsequent membrane material, affecting the separation effect of the membrane. The raw gas first passes through the high-permeability membrane material and then the non-permeated gas produced passes through the high-selectivity membrane material to permeate in the form of lower pressure to extract high-purity gas; the check valve and high differential pressure interlock are used to provide further protection for the membrane inside the high-pressure gas membrane separator to prevent the membrane from being subjected to reverse pressure difference.
[0015] 2. The fiber tube adopts a sandwich structure of inner and outer support layers and an intermediate membrane layer. The gap on the surface of the outer support layer is larger than that of the inner support layer. The double support increases the mechanical properties of the hollow fiber tube and reduces the permeability attenuation of the membrane material inside the hollow fiber tube, thereby extending the service life of the membrane material and increasing the anti-pollution property of the fiber. BRIEF DESCRIPTION OF THE DRAWINGS
[0016] In order to more clearly illustrate the technical solutions in the present invention or the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.
[0017] Figure 1 A three-dimensional schematic diagram of a hollow fiber gas membrane separator provided by an embodiment of the present invention Figure 1 ; Figure 2 The hollow fiber gas membrane separator of the present invention is a three-dimensional schematic diagram Figure 2 ; Figure 3 The hollow fiber gas membrane separator of the present invention is a three-dimensional schematic diagram Figure 3 ; Figure 4 It is a three-dimensional enlarged schematic diagram of the gas membrane separator of the present invention; Figure 5 It is an enlarged schematic diagram of the cross section of the internal structure of the gas membrane separator of the present invention; Figure 6 It is an enlarged schematic diagram of the cross section of the hollow fiber inside the gas membrane separator of the present invention; Figure 7 yes Figure 6 Magnified view of area A.
[0018] Reference numerals: 1. Install the chassis; 2. Separation assembly; 201. Primary membrane separator; 202. Secondary membrane separator; 203. Shell; 204. Hollow fiber filaments; 2041. Internal support layer; 2042. Separation membrane layer; 2043. External support layer; 205. Sealing rubber ring; 206. Raw gas inlet pipe; 207. Non-permeable gas outlet pipe; 208. Permeable gas outlet pipe; 3. Delivery pipeline assembly; 301. High-temperature gas delivery pipe; 302. Secondary gas delivery pipe; 303. Permeable gas collection and discharge pipe; 4. Pipeline control component; 401. Check valve; 402. Temperature control valve; 403. High differential pressure interlock; 5. Connecting support; 6. Cooler. DETAILED DESCRIPTION
[0019] In order to make the purpose, technical solution and advantages of the present invention clearer, the technical solution of the present invention will be clearly and completely described below in conjunction with the drawings of the present invention. Obviously, the described embodiments are part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.
[0020] As mentioned above, the current hollow fiber membrane separator uses a hollow fiber tube with a support layer and a membrane layer. The internal and external distribution of the support layer and the membrane layer is adjusted according to the internal pressure or external pressure type to separate the mixed raw gas. The mechanical properties are poor, and the anti-pollution performance of the hollow fiber tube is not good. In addition, as the use time increases, the permeability attenuation of the membrane material is likely to increase, and the recovery rate after cleaning is not good enough.
[0021] In view of this, the present invention provides a hollow fiber gas membrane separator, which can be used for and For separation, the raw gas first passes through a high permeability membrane material, and then the non-permeated gas produced passes through a high selectivity membrane material to permeate at a lower pressure, thereby improving The fiber tube adopts a sandwich structure of inner and outer support layers and an intermediate membrane layer. The gap on the surface of the outer support layer 2043 is larger than that of the inner support layer 2041, which prolongs the service life of the membrane material and increases the mechanical strength and anti-pollution property of the fiber.
[0022] Combine the following Figure 1 to Figure 7 The present invention is described in detail.
[0023] Embodiment 1: like Figure 1 to Figure 7As shown, the present invention provides a gas membrane separator, in particular, a hollow fiber gas membrane separator. In this embodiment, the separator is mainly composed of four parts: a mounting base 1, a separation assembly 2, a delivery pipeline assembly 3, and a pipeline control component 4. Connecting supports 5 are fixedly connected to both sides of the upper end of the mounting base 1. The separation assembly 2 is arranged on the front side of the upper end of the mounting base 1, and the separation assembly 2 is connected through the delivery pipeline assembly 3, and the raw gas is transported to the interior of the separation assembly 2 for separation treatment, and the pipeline control component 4 on the delivery pipeline assembly 3 is used to control the opening and closing of each pipeline of the delivery pipeline assembly 3.
[0024] like Figure 1~Figure 3 As shown, in the present invention, a mounting base 1 is used as a mounting base, and connecting supports 5 are arranged at both sides of the upper end of the mounting base 1, and the connecting supports 5 are used to fix the separation assembly 2 on the mounting base 1. Among them, the separation assembly 2 is composed of two separators, namely, a primary membrane separator 201 and a secondary membrane separator 202, and both separators are composed of a shell 203, a plurality of hollow fiber filaments 204, and a sealing rubber ring 205 arranged at both ends of the hollow fiber filaments 204. In this application, the shell 203 is supported by stainless steel material and has a strong pressure resistance. After the two ends of the plurality of hollow fiber filaments 204 are aligned, epoxy resin is used to seal the entire end at one end, and epoxy resin is only used to seal the gap between the fiber filaments 204 at the other end of the arranged plurality of hollow fiber filaments 204 to make a membrane core. The sealing rubber ring 205 and the inside of the shell 203 are used to seal and partition at both ends of the membrane core, and the hollow fiber filaments 204 are fixed. A shell pass is formed between the hollow fiber filaments 204 and the shell 203 , and the co-feed gas enters and permeates inside the hollow fiber filaments 204 .
[0025] The hollow fiber filaments 204 used in the present invention are all composed of a three-layer structure, such as Figure 7 As shown, the innermost is the internal support layer 2041, the middle is the separation membrane layer 2042, and the outermost is the external support layer 2043. The inner and outer support layers are used to support the membrane in the middle. The pore size of the air holes on the surface of the external support layer 2043 is larger than the pore size of the air holes on the surface of the internal support layer 2041. When the raw gas penetrates from the shell side to the inside of the hollow fiber tube, the mass transfer resistance of a certain gas passing through the external support layer 2043 can be reduced, thereby achieving rapid gas conduction. The smaller pore size of the air holes on the surface of the internal support layer 2041 can reduce the damage to the membrane caused by excessive external pressure. After the raw gas enters the primary membrane separator 201, the (hydrogen) and (carbon monoxide) to separate, As "fast gas", it quickly penetrates into the separation membrane layer 2042 of the primary membrane separator 201. The rate of permeation into the separation membrane layer 2042 is slow, which is called "slow gas". The selectivity of the separation membrane layer 2042 is used to and Separation, and as non-permeate gas Then enter the interior of the secondary membrane separator 202, A small amount of internal The water permeates again and enters the separation membrane layer 2042 inside the secondary membrane separator 202 .
[0026] In order to improve the separation Purity, the separation membrane layer 2042 inside the secondary membrane separator 202 needs to use a highly selective separation membrane, and in order to reduce In order to reduce the resistance when penetrating into the first membrane separator 201 and reduce the impact of the transported raw gas on the life of the compressor, the separation membrane layer 2042 inside the first membrane separator 201 needs to use a high permeability separation membrane. The gas pressure entering the shell side of the first membrane separator 201 is lower than the gas pressure entering the shell side of the second membrane separator 202, ensuring that the second membrane separator 202 is and Selection and separation of two gases, improving non-permeation gas purity.
[0027] The present invention sets a raw gas inlet pipe 206 outside the shell 203, and sets a non-permeate gas outlet pipe 207 on the side of the outer side of the shell 203 away from the raw gas inlet pipe 206. The gas selected by the separation membrane layer 2042 is transported from the inside of the hollow fiber tube upward from the permeate gas outlet pipe 208 at the upper end of the outer shell 203 to the outside of the shell side 203. The permeate gas collection and discharge pipe 303 in the shape of a three-way is used to collect the permeate gas at the upper ends of the two separators and transport them outward. A high-temperature gas delivery pipe 301 is set at the rear side of the non-permeate gas outlet pipe 207 of the first-level membrane separator 201, and a check valve 401 is set at the connection between the high-temperature gas delivery pipe 301 and the non-permeate gas outlet pipe 207 of the first-level membrane separator 201, and a pressure gauge and a high differential pressure interlock 403 are set on the high-temperature gas delivery pipe 301 to ensure that no reverse pressure difference is caused to the membrane inside the separator.
[0028] In addition, a cooler 6 is provided at the rear side of the upper end of the mounting frame 1. The cooling temperature of the cooler 6 is set to 40°C. The other end of the high-temperature gas delivery pipe 301 connected to the check valve 401 is connected to the air inlet of the cooler 6. (Contains a small amount ), enters the interior of the cooler 6, and is cooled to below 40°C. The present invention connects a secondary gas delivery pipe 302 to the gas outlet of the cooler 6, and the other end of the secondary gas delivery pipe 302 is connected to the raw gas inlet pipe 206 of the secondary membrane separator 202, in order to ensure that the cooling temperature reaches below 40°C. A temperature control valve 402 is set on the secondary gas delivery pipe 302. If the temperature is lower than 40°C, the temperature control valve 402 opens to allow gas to be transported to the interior of the secondary membrane separator 202. If the gas temperature is higher than 40°C, the temperature control valve 402 closes, and the gas cannot flow into the secondary membrane separator 202. Controlling the temperature below 40°C is one way to increase and The first is to reduce the difference in diffusion rates between the two membranes to improve the separation selectivity, and the second is to ensure the long-term and efficient operation of the membrane.
[0029] The raw gas is filtered and preheated and transported to the first-stage membrane separator 201 through a compressor, and then enters the shell side of the first-stage membrane separator 201. The penetration rate is higher than , through the pressure difference inside and outside the hollow fiber filament 204, Enter the interior of the hollow fiber filament 204. The gas has a low permeability and is enriched through the shell between the hollow fiber filaments 204 and the shell 203, and is transported from the inside of the non-permeated gas outlet pipe 207 to the inside of the high-temperature gas delivery pipe 301. If the pressure on the high-temperature gas delivery pipe 301 is higher than the gas pressure inside the primary membrane separator 201, the check valve 401 will be closed, and the high differential pressure interlock 403 will be locked to close the high-temperature gas delivery pipe 301 to prevent the membrane inside the primary membrane separator 201 from being subjected to a reverse pressure difference.
[0030] Enriched Then it is cooled to below 40℃ by cooler 6 to reduce The thermal movement rate increases and The selectivity of The interception rate. A small amount of residue Then, it is separated by the secondary membrane separator 202. The gas is discharged from the permeate outlet pipe 208 of the secondary membrane separator 202 and discharged through the permeate collection outlet pipe 303 and the permeate outlet pipe 208 of the primary membrane separator 201. Gather and discharge them together for collection.
[0031] In this embodiment, the hollow fiber filament 204 inside the primary membrane separator 201, the separation membrane layer 2042 can be a PDMS membrane with a permeability of 500 GPU, a selectivity of 15, and a rapid recovery rate. , reducing the load of subsequent processing. The temperature of the raw gas preheated and transported into the first-stage membrane separator 201 is 80°C and the pressure is 3MPa. The use of low-pressure steam or hot water to heat the transported raw gas can make the temperature of the raw gas higher than the dew point, preventing the liquid from condensing on the fiber surface of the separator when the raw gas passes through the surface of the subsequent membrane material, thereby affecting the separation effect of the membrane.
[0032] The dew point is and The mixed raw gas is cooled under a certain pressure to a temperature where liquid water begins to condense. Heating is used to prevent liquid water from precipitating and to prevent blockage in the hollow fiber tube. Generally, the higher the humidity of the gas, the higher the dew point temperature. The dew point temperature is calculated using the Antoine equation, as follows: ,in, is the water vapor partial pressure (here and Total pressure of the mixed gas), is temperature, A, B, and C are constants (when the temperature range is 1~100℃, A is 6.12, B is 7.59, and C is 240.73).
[0033] Therefore, the dew point temperature of the raw gas can be inferred from the Antoine equation: ; is the dew point temperature of the mixed gas.
[0034] The separation membrane layer 2042 of the secondary membrane separator 202 can be a polyimide membrane, with a selectivity of 50 and a permeability of 25 GPU, an operating temperature of 40°C, and a non-permeation gas pressure of 0.8 MPa entering the secondary membrane separator 202. and For separation, the porosity of the two supporting layers of the hollow fiber filaments 204 should be no less than 60% to reduce the gas flow resistance. In this embodiment, the outer supporting layer 2043 can be made of polysulfone material with a thickness of 80 to 100 , aperture is 0.3~0.5 The thickness of the separation membrane layer 2042 can be 8 to 15 The internal support layer 2041 can be made of polyethersulfone material with a thickness of 70~90 , the aperture can be 0.1~0.2 .
[0035] The internal single-support (single-layer external pressure type) separation membrane, the external single-support (single-layer internal pressure type) separation membrane and the internal and external double-support (sandwich type) separation membrane were tested for anti-pollution and operating life.
[0036] Comparative Example 1: Single-layer external pressure type; Comparative Example 2: Single-layer internal pressure type; This solution: Sandwich type. A high-pressure membrane separation test platform (maximum pressure 10MPa, temperature controllable 0~100℃), scanning electron microscope (for membrane structure characterization), gas chromatograph (for gas composition analysis), dynamic mechanical analyzer (mechanical performance test) and dust pollution simulator (including Particles, particle size 1~5 ).
[0037] Raw gas / (volume ratio is 1:1), pressure is 3MPa, temperature is 40℃. Penetration rate (GPU), / Separation factor (α) and Each experiment was repeated three times and the average value was taken.
[0038] When conducting mechanical property tests, the tensile strength of the single filament was tested. DMA was used to measure the breaking strength of the fiber (in units of ) and elongation at break (%), and under a pressure of 5 bar, run continuously for 1000 hours, record the decay rate of permeability, and perform compression test.
[0039] When conducting dust pollution test for pollution resistance, / Mixed gas (containing 0.1wt% Particles, pressure at 2.5 , temperature is 50℃), the membrane permeability change before and after pollution was analyzed by SEM+EDS, and when the permeability dropped by 20%, it was backwashed with deionized water and the recovery rate was recorded.
[0040] When conducting anti-aging tests under long-term operation, the pressure is controlled at 5 , the temperature is 80℃, the raw gas contains 1% , used to simulate acidic environment, monitor the corresponding membrane permeation attenuation curve, chemical structure changes of membrane layer (FTIR analysis) and The fluctuation of purity lasted for about 8 months.
[0041] Table 1 Test results of mechanical properties of fibers with different support layers and membrane layers
[0042] It can be seen from the test results that the fiber filaments with inner and outer support layers and a membrane layer in the middle have higher mechanical properties.
[0043] Table 2 Test results of anti-pollution properties of fibers of various structures after 100 hours of pollution
[0044] From the test results, it can be seen that the fiber filaments with inner and outer support layers and a membrane layer in the middle have higher anti-pollution performance when polluted for 100 hours.
[0045] Table 3 Anti-pollution test results of fibers of various structures after 500 hours of pollution
[0046] From the test results, it can be seen that the fiber filaments with inner and outer support layers and a membrane layer in the middle have higher anti-pollution performance when polluted for 500 hours.
[0047] Table 4 Long-term life performance test results of fiber filaments of various structures at 0 hours of operation
[0048] It can be seen from the test results that the fiber filaments with inner and outer support layers and a membrane layer in the middle have a longer long-term service life when not in use.
[0049] Table 5 Long-term life performance test results of fiber filaments of various structures after 3000 hours of operation
[0050] The test results show that the fiber filaments with inner and outer support layers and a membrane layer in the middle have a longer long-term service life when running for 3000 hours.
[0051] Table 6 Long-term life performance test results of fiber filaments of various structures after 6000 hours of operation
[0052] The test results show that the fiber filaments with inner and outer support layers and a membrane layer in the middle have a longer long-term service life when running for 6000 hours.
[0053] Therefore, the tensile strength of the sandwich structure single fiber is 41% higher than that of the single layer, the elongation at break is increased by 33%, and the permeability attenuation in the compression test is only 1 / 3 of that of the single layer structure; under dusty conditions, the permeability attenuation rate of the sandwich structure is reduced by 60%, and the recovery rate after cleaning is 7 percentage points higher than that of the single layer; the accelerated aging experiment shows that the life of the sandwich structure is more than twice that of the single layer. Better purity retention ability.
[0054] In summary, the hollow fiber gas membrane separator of the present invention has the following advantages: 1. Use double-stage gas membrane separator and For separation, the raw gas is preheated before entering the primary membrane separator 201 to make the temperature of the raw gas higher than the dew point, to prevent the liquid from condensing on the fiber surface of the membrane separator when the raw gas passes through the subsequent membrane material surface, affecting the separation effect of the membrane, and the raw gas first passes through the high permeability membrane material and then the non-permeated gas produced passes through the high selectivity membrane material to permeate in the form of lower pressure, thereby improving purity.
[0055] 2. The fiber tube adopts a sandwich structure of inner and outer support layers and an intermediate membrane layer. The gap on the surface of the outer support layer 2043 is larger than that of the inner support layer 2041, which prolongs the service life of the membrane material, increases the mechanical strength and anti-pollution property of the fiber filaments, and cooperates with the check valve and high differential pressure interlock to provide further protection for the membrane inside the high-pressure gas membrane separator to prevent reverse pressure difference from being caused to the membrane.
[0056] The check valve, temperature control valve and high differential pressure interlock used to control the opening and closing of the pipeline in the equipment are all existing technologies, which are common knowledge in the field and are not the improved technical points of this case, so they will not be elaborated here.
[0057] In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inside", "outside" and the like indicate positions or positional relationships based on the positions or positional relationships shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific position, be constructed and operated in a specific position, and therefore cannot be understood as limiting the present invention; the terms "primary" and "secondary" are only used for descriptive purposes, and cannot be understood as indicating or implying relative importance. In addition, unless otherwise clearly specified and limited, the terms "installed", "connected" and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be an indirect connection through an intermediate medium, or it can be a connection between the two elements. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.
[0058] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit it. Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the aforementioned embodiments, or make equivalent replacements for some of the technical features therein. However, these modifications or replacements do not deviate the essence of the corresponding technical solutions from the spirit and scope of the technical solutions of the embodiments of the present invention.
Claims
1. A hollow fiber gas membrane separator, characterized in that: include: A mounting base (1), wherein connecting supports (5) are provided on both sides of the upper end of the mounting base (1), and a cooler (6) is provided on the rear side of the upper end of the mounting base (1); A separation assembly (2), the separation assembly (2) comprising a primary membrane separator (201) and a secondary membrane separator (202) arranged on the front side of the upper end of the mounting frame (1), and the membrane separators are connected to the mounting frame (1) via connecting supports (5) on both sides respectively; A transport pipeline assembly (3), the transport pipeline assembly (3) comprising a plurality of pipelines arranged between the primary membrane separator (201) and the secondary membrane separator (202); A pipeline control component (4), the pipeline control component (4) comprising a check valve (401), a temperature control valve (402) and a high differential pressure interlock (403) arranged on the delivery pipeline assembly (3).
2. The hollow fiber gas membrane separator according to claim 1, characterized in that: The membrane separator comprises a shell (203), the exterior of the shell (203) being fixedly connected to a connection support (5), a plurality of hollow fiber filaments (204) being arranged inside the shell (203), one end of the hollow fiber filaments (204) being neatly arranged and fully sealed with epoxy resin, and the other end of the hollow fiber filaments (204) being sealed with epoxy resin at their gaps, and the hollow fiber filaments (204) being sealed and connected to the shell (203) via sealing rubber rings (205) provided at the sealing ends and the sealing ends.
3. The hollow fiber gas membrane separator according to claim 2, characterized in that: The hollow fiber filament (204) includes an innermost internal support layer (2041), a separation membrane layer (2042) is arranged outside the internal support layer (2041), an external support layer (2043) is arranged outside the separation membrane layer (2042), and the pore size of the external support layer (2043) is larger than the pore size of the internal support layer (2041), the separation membrane layer (2042) inside the primary membrane separator (201) is a high permeability membrane, and the separation membrane layer (2042) inside the secondary membrane separator (202) is a high selectivity membrane.
4. The hollow fiber gas membrane separator according to claim 2, characterized in that: A raw gas inlet pipe (206) is arranged on the side of the shell (203) outside close to the sealed end of the hollow fiber filament (204), and a non-permeate gas outlet pipe (207) is arranged on the side of the shell (203) outside close to the sealed end of the hollow fiber filament (204). The raw gas inlet pipe (206) and the non-permeate gas outlet pipe (207) are located on different sides of the shell (203), and a permeate gas outlet pipe (208) is arranged on the top end of the shell (203).
5. The hollow fiber gas membrane separator according to claim 1, characterized in that: The delivery pipeline assembly (3) comprises a high-temperature gas delivery pipe (301) arranged at the rear side of the first-stage membrane separator (201), one end of the high-temperature gas delivery pipe (301) being connected to the air inlet of the cooler (6), the check valve (401) being connected to the other end of the high-temperature gas delivery pipe (301), a second-stage gas delivery pipe (302) being arranged at the rear side of the second-stage membrane separator (202), the rear end of the second-stage gas delivery pipe (302) being connected to the air outlet of the cooler (6), and a permeate gas collection discharge pipe (303) being arranged at the upper end of the membrane separator.
6. The hollow fiber gas membrane separator according to claim 4 or 5, characterized in that: The check valve (401) is connected to the non-permeate gas outlet pipe (207) of the primary membrane separator (201), the front end of the secondary gas delivery pipe (302) is connected to the raw gas inlet pipe (206) of the secondary membrane separator (202), and a pressure gauge is provided on the high-temperature gas delivery pipe (301).
7. The hollow fiber gas membrane separator according to claim 5, characterized in that: The high differential pressure interlock (403) is arranged on the high-temperature gas delivery pipe (301), and the pressure gauge is located between the check valve (401) and the high differential pressure interlock (403), and the temperature control valve (402) is arranged on the secondary gas delivery pipe (302).
8. The hollow fiber gas membrane separator according to claim 5, characterized in that: When the temperature of the gas introduced into the secondary gas delivery pipe (302) is lower than 40° C., the temperature control valve (402) opens; when the temperature of the gas introduced into the secondary gas delivery pipe (302) is higher than 40° C., the temperature control valve (402) closes.
9. The hollow fiber gas membrane separator according to claim 1, characterized in that: The raw gas introduced into the first-stage membrane separator (201) is preheated, and the gas pressure inside the second-stage membrane separator (202) is lower than that of the first-stage membrane separator (201).