Deep gas purification device based on momentum defoaming

Abstract

The utility model discloses a deep gas purification device based on momentum defoaming, which relates to the technical field of chemical equipment and comprises a tank body, a dynamic distributor, a momentum defoaming module with a plurality of momentum defoamers, a fiber condensation module and a rotary liquid removal module. The oil-gas inlet is communicated with a dynamic distributor through a pipeline; the tail end of the dynamic distributor is connected with a momentum defoaming module; a fiber module and a rotary liquid removal module are sequentially arranged at the top end of the momentum defoaming module. The momentum of the gas-liquid mixture is utilized to collide with the baffle in the momentum defoaming device to crush foamed liquid drops, and the liquid drops move to the edge of the baffle and are discharged under the driving of subsequent airflow, so that the foamed liquid drops are eliminated; and the remaining fine liquid drops are aggregated by the fiber aggregation module and grow into larger liquid drops, and finally the larger liquid drops enter the rotary liquid removal module, so that efficient separation of the liquid drops and the gas is realized under the action of a centrifugal force field, and the effect of deep purification of the gas is achieved.

Description

Technical Field

[0001] The utility model relates to the technical field of chemical equipment, in particular to a deep gas purification device based on momentum defoaming. Background Art

[0002] The development of light oil provides strong support for the realization of low-carbon economy and sustainable development goals due to its advantages such as high cleanliness, high combustion efficiency, large market demand and easy storage. In order to further refine oil products into light oils such as C3, C4, and C5 through hydrogenation reactions, smaller bubbles are usually required to achieve liquid-phase hydrogenation reactions. However, smaller-sized bubbles easily cause part of the distillate after the reaction to be discharged in the form of a foamy gas-liquid mixture or droplets under the entrainment of high-speed airflow along with the circulating hydrogen, thereby causing waste of oil products and even causing certain impacts on subsequent refining projects. Therefore, the use of appropriate and efficient defoaming devices can prevent the waste of resources and increased energy consumption caused by the escape of certain light oil components after being entrained by high-speed airflow.

[0003] In the actual process, the liquid content entrained in the gas phase needs to be controlled below an appropriate value to meet the quality requirements of the desired product. If the circulating hydrogen is entrained with oil phase, on the one hand, it will have a toxic effect on the catalyst, which may neutralize or poison the catalyst, reduce the catalytic activity, slow down or hinder the reaction rate; on the other hand, oil phase droplets or foamy gas-liquid mixtures may be deposited in the reactor and pipelines, causing equipment blockage and corrosion, and may even cause equipment wear and damage, which may require frequent maintenance and cleaning, increasing production costs.

[0004] In traditional industrial production processes, wire mesh defoamers and other devices are usually used for defoaming, which has the advantages of simple structure, easy installation and maintenance, and high economy; however, the defoaming efficiency is not high when dealing with high flow, high temperature, high pressure or extreme foaming conditions. Therefore, it is necessary to develop a gas deep purification device with defoaming function to solve the problems of high foam and droplet content in hydrogen in the hydrogenation reaction cycle.

[0005] In view of the above technical difficulties, some solutions have been found in existing technologies:

[0006] CN116574542A discloses a high-efficiency cyclone defoaming oil-gas separation device, including a tank body, and the tank body includes a medium inlet, an oil outlet and a natural gas outlet. A cyclone defoaming component for improving the defoaming rate is installed on the inner side of the medium inlet, and a wire mesh defoamer for defoaming tiny bubbles is arranged on the inner side of the natural gas outlet. The cyclone and super gravity field are used for forced defoaming, which improves the defoaming efficiency to a certain extent. However, when applied to this process, the foam entrained by the high-speed airflow causes the instability of the cyclone flow field structure to a certain extent, so that a certain amount of foam still exists at the gas phase outlet in the cyclone, thereby affecting the defoaming efficiency.

[0007] CN220003436U discloses a gas-liquid separation device and a gas-liquid separation system. The gas-liquid separation device comprises a separation tank body, an exhaust port located on the upper side of the separation tank body, a liquid discharge port located on the lower side of the separation tank body, an air inlet located on the separation tank body, and a liquid collecting mechanism. The separation tank body is provided with at least one layer of partitions located above the air inlet, each partition is provided with at least one accommodating cavity with an open bottom and a fiber agglomeration unit located in the accommodating cavity, and a through hole is provided on the side wall of the accommodating cavity, so that the liquid-containing gas entering the separation tank body from the air inlet can be separated from the gas and liquid by the fiber agglomeration unit, the gas obtained by the gas-liquid separation is discharged through the exhaust port, and the liquid obtained by the gas-liquid separation is transported to the liquid discharge port through the liquid collecting mechanism for discharge. The gas-liquid separation device can perform gas-liquid separation treatment on liquid-containing gas and liquid, has high separation efficiency and simple device structure, and can efficiently aggregate and treat fine droplets. However, in this process, the relatively large volume of foam easily blocks the fiber layer, making it difficult for the airflow to pass through, thereby causing a certain degree of efficiency reduction.

[0008] That is to say, for the hydrogen circulating in the hydrogenation reaction which is a gas-liquid mixed phase at the inlet and is mixed with a certain amount of foam phase, if the existing technology directly passes through the swirl or coalescence of the foam phase, it will cause problems such as unstable swirl flow field and fiber blockage. Utility Model Content

[0009] The purpose of the utility model is to solve the shortcomings existing in the prior art, and to propose a deep gas purification device based on momentum defoaming, the purpose of which is to eliminate oil phase foam and droplets in the hydrogen gas in the hydrogenation reaction cycle based on momentum, and to use coalescing fibers and cyclone devices to eliminate fine oil droplets, thereby achieving the function of deep gas purification and solving the phenomenon of foamy gas-liquid mixture appearing at the gas outlet.

[0010] In order to achieve the above purpose, the utility model adopts the following technical solutions:

[0011] A deep gas purification device based on momentum defoaming comprises a tank body, a dynamic distributor, a momentum defoaming module with a plurality of momentum defoamers, a fiber coagulation module and a rotary deliquescence module, wherein:

[0012] The middle part of the side wall of the tank body is provided with an oil and gas inlet, the top of the tank body is provided with a gas outlet, and the bottom of the tank body is provided with a liquid phase outlet. The oil and gas inlet is used to receive the gas and liquid phases to be purified, the gas outlet is used to discharge the separated dry hydrogen, and the liquid phase outlet is used to discharge the separated liquid phase.

[0013] The oil and gas inlet is connected to the dynamic distributor through a pipeline, and a feed chamber with multiple groups of independent chambers is provided in the dynamic distributor, and each group of independent chambers is connected to the momentum defoamer through a distribution pipe;

[0014] The momentum defoamer is a tower-shaped structure, including a straight section and a conical section connected from bottom to top, the straight section is used for preliminary defoaming; the conical section is used for momentum deep defoaming;

[0015] The momentum defoaming module extends along the top to include a fiber condensation module, a rotary dehydration module and a gas phase outlet in sequence, and overflow channels for discharging the separated liquid phase are provided at both ends of the rotary dehydration module and the fiber condensation module, and the overflow channels are connected to the liquid collecting area at the bottom of the tank body.

[0016] Furthermore, the dynamic distributor is equipped with a spiral guide vane, and a plurality of partitions arranged at equal angles are provided below the spiral guide vane. The plurality of partitions divide the feed chamber into a plurality of independent chambers, and each group of independent chambers is correspondingly connected to the distribution pipe, wherein the spiral angle of the spiral guide vane is 30-45°, and the number of partitions is 2-8.

[0017] Furthermore, a metal grid formed by crossing metal wires is installed in the straight section of the momentum defoamer, the crossing angle of the metal wires is 30-90°, and the metal grid is covered with barbs.

[0018] Furthermore, a plurality of equally spaced annular baffles are vertically arranged on the inner wall of the conical cylinder section of the momentum defoamer, the inclination angle between the annular baffles and the horizontal plane is between 30-45°, and the distance between two vertically adjacent groups of annular baffles is 0.15-0.2 times the total vertical distance of the conical cylinder section; the outlet diameter of the conical cylinder section is 0.2-0.4 times the diameter of the straight cylinder section.

[0019] Furthermore, the momentum defoamer module also includes an upper baffle and a lower baffle located at the upper and lower parts of the multiple groups of momentum defoamers. The top of the conical cylinder section is connected to an overflow pipe, and the overflow pipe passes through the upper baffle.

[0020] Furthermore, the fiber coagulation module includes a plurality of fiber bed layers arranged at intervals, wherein the fiber bed layers are woven from modified polymer fibers at a certain angle, the weaving angle is 45-90°, and the diameter of the modified polymer fibers is 50-250 μm; the porosity of the fiber bed layer is 0.65-0.85 and the gradient decreases upward in the direction of the flow, the thickness of the fiber bed layer is between 0.3-0.5 m, and the number of fiber bed layers is 1-3.

[0021] Furthermore, the rotary dehydration module is formed by a plurality of cyclone core tubes arranged in a ring shape;

[0022] Each cyclone core tube has a plurality of independent chambers at the bottom, and each chamber is equipped with an independent spiral blade, which is fixed on the core tube center column in the center of the cyclone core tube, and the spiral angle of the spiral blade is 30-45°;

[0023] The cyclone core tube is arranged in the form of an inner and outer sleeve, the inner and outer sleeves are fixed by a fixing plate, and a liquid discharge cavity for discharging separated liquid is formed between the inner and outer sleeves.

[0024] A deep gas purification method based on momentum defoaming, using the deep gas purification device, the method comprising:

[0025] S1. The oil and gas are introduced into the tank from the oil and gas inlet, and the oil and gas enter the dynamic distributor through the feed pipe for distribution. The dynamic separator evenly distributes the oil and gas flow to each momentum defoamer on the momentum defoamer module, and defoaming is performed in the momentum defoamer;

[0026] S2, the defoamed oil and gas flow flows upward through the fiber condensation module, and the small droplets entrained in the air flow are captured and aggregated by the cross fibers in the fiber condensation module;

[0027] S3, the oil and gas after being coalesced continue to flow upward through the cyclone separation module, and high-speed rotation flow is performed in the cyclone separation unit to separate the droplets entrained in the oil and gas;

[0028] S4, the liquid droplets are discharged from the liquid discharge cavity of the cyclone separation module and flow to the liquid collection area at the bottom of the tank through the overflow channel;

[0029] S5. The oil and gas after defoaming, deliquescence and purification are discharged from the gas phase outlet at the top of the separator tank.

[0030] Furthermore, in S1, the momentum defoamer defoams in the following manner: a metal grid with barbed hooks in the straight cylinder section and an annular baffle of multiple conical sections in the conical cylinder section are used to perform preliminary defoaming and momentum deep defoaming on the oil and gas in sequence, wherein the oil and gas airflow moves into the conical cylinder section under the action of high-speed airflow, and high-momentum foam droplets in the oil and gas airflow collide with the annular baffle, and the liquid film is continuously broken and finally annihilated into fine droplets.

[0031] Furthermore, the momentum defoaming module and the rotary deliquescence module are used in parallel in multiple groups in a uniformly distributed manner on the flow cross section of the separator, wherein:

[0032] The processing capacity of a single kinetic defoamer is 50-500m 3 / h.

[0033] The processing capacity of a single cyclone separation module is 100-1000m 3 / h.

[0034] Compared with the prior art, the beneficial effects of the utility model are:

[0035] (1) The utility model proposes a deep purification device based on gas momentum defoaming, which distributes the hydrogen gas of the hydrogenation reaction cycle, which is a gas-liquid mixed phase at the inlet and mixed with a certain amount of foam phase, to the momentum defoamer evenly through a dynamic distributor, thereby avoiding the problems of unstable swirl flow field and fiber blockage caused by the foam phase directly through swirl or coalescence, and utilizing the momentum collision between the gas itself and the wall in the momentum defoamer to eliminate the entrained foam droplets and reduce the relative energy loss, thereby achieving the purpose of efficient defoaming;

[0036] (2) The utility model utilizes the momentum defoaming module. On the basis of eliminating most of the foam droplets in the momentum defoaming module, it combines the fiber coagulation module with the rotary dehydration module to achieve step-by-step enhanced separation of fine droplets. The fiber coagulation module is used to achieve the collision, aggregation, and growth of fine droplets into larger droplets. After passing through the momentum defoamer, the smaller bubbles are not easy to cause clogging of the fiber bed. Finally, they are further removed in the cyclone core tube in the rotary dehydration module, thereby achieving efficient removal of fine droplets and greatly improving the separation efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0037] Figure 1 It is a schematic diagram of the overall structure of the utility model;

[0038] Figure 2 It is a schematic diagram of the overall structure of the dynamic distributor in the utility model;

[0039] Figure 3 This is a top view of the structure of the dynamic distributor in the utility model, showing the overall arrangement of the gas-liquid distribution pipes;

[0040] Figure 4 This is a schematic structural diagram of a momentum defoamer in a momentum defoamer module of the utility model;

[0041] Figure 5 It is a structural schematic diagram of the cyclone core tube in the rotary dehydration module of the utility model;

[0042] Figure 6 This is a top view of the fiber coagulation module and the rotary deliquidation module in the utility model, showing the drainage direction and the location of the overflow channel;

[0043] Figure 7 It is a schematic diagram of the principle of eliminating foam droplets by the momentum defoaming module in the utility model.

[0044] In the figure: 1. Oil and gas imports;

[0045] 2. Dynamic distributor; 201. Feed chamber; 202. Spiral guide vane; 203. Center column; 204. Baffle; 205. Independent chamber; 206. Distribution pipe;

[0046] 3. Momentum defoamer; 301. Feed pipe; 302. Straight section; 303. Metal grid; 304. Annular baffle; 305. Overflow pipe; 306. Conical section;

[0047] 4. Fiber coagulation module; 5. Gas outlet;

[0048] 6. Cyclone core tube; 601. Core tube partition; 602. Core tube center column; 603. Spiral blade single piece; 604. Exhaust pipe; 605. Fixed plate; 606. Drainage chamber;

[0049] 7. Liquid level meter; 8. Liquid phase outlet; 9. Overflow channel. DETAILED DESCRIPTION

[0050] The technical solutions in the embodiments of the present invention will be described clearly and completely below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, rather than all of the embodiments.

[0051] Example 1

[0052] A deep gas purification device based on momentum defoaming, such as Figure 1As shown, it includes a tank body (not shown in the figure) and a dynamic distributor 2 arranged in the tank body, a momentum defoaming module with a plurality of momentum defoamers 3, a fiber coagulation module 4 and a rotary deliquation module with a plurality of cyclone core tubes 6. The inlet of the tank body is connected to the momentum defoaming module through the dynamic distributor 2, and the fiber coagulation module 4 and the rotary deliquation module are arranged in sequence above the momentum defoaming module. The oil and gas enter the tank body, and are evenly diverted to the momentum defoaming module through the dynamic distributor 2 for defoaming, and then the oil and gas rise to the fiber coagulation module 4 and the rotary deliquation module to remove droplets, and finally the gas after defoaming and deliquation is discharged from the tank body.

[0053] Specifically, see Figure 1 The tank body is set as a vertical cylindrical structure, and an oil and gas inlet 1 is provided in the middle of the side wall of the tank body. The oil and gas inlet 1 is used to receive the gas and liquid phases to be purified. The top of the tank body is provided with a gas outlet 5 and the bottom of the tank body is provided with a liquid phase outlet 8. The gas outlet 5 is used to discharge the separated dry hydrogen, and the liquid phase outlet 8 is used to discharge the separated liquid phase. The bottom end of the tank body is divided into a liquid collection area. The tank body is also provided with a liquid level gauge 7. The detection end of the liquid level gauge 7 is located in the liquid collection area, which is used to detect the liquid level in the liquid collection area.

[0054] See Figure 1 Combined with Figure 2-3 The oil and gas inlet 1 on the tank body is connected to the dynamic distributor 2 through a pipeline. The dynamic distributor 2 is provided with a feed chamber 201 with multiple groups of independent chambers 205, and the gas-liquid mixed phase in the independent chambers is uniformly discharged into the momentum defoaming module.

[0055] Specifically, the dynamic distributor 2 is located above the liquid collection area and installed at the center of the tank. The dynamic distributor 2 includes a feed chamber 201 and a plurality of distribution pipes 206 connected to the bottom of the feed chamber 201. The feed chamber 201 is connected to the oil and gas inlet 1 through a pipeline, and the feed chamber 201 is a cylindrical structure.

[0056] A central column 203 is fixed at the inner center of the feed chamber 201 on the dynamic distributor 2. Preferably, the diameter Da of the central column 203 is 0.3-0.4 of the diameter De of the dynamic distributor 2.

[0057] A plurality of groups of spiral guide vanes 202 are mounted on the central column 203. Specifically, the central column 203 is connected to the edge of the spiral guide vane 202, thereby fixing the spiral guide vane 202. Preferably, the angle of the spiral guide vane 202 is 30-45°.

[0058] The bottom of the feed chamber 201 of the dynamic distributor 2 is provided with a plurality of partitions 204 arranged at equal intervals in a circle, and the plurality of partitions 204 are located below the spiral guide vane 202. The plurality of partitions 204 are used to divide the feed chamber 201 at the bottom of the spiral guide vane 202 into a plurality of evenly distributed independent chambers 205, and evenly distribute the gas-liquid mixed phase (i.e., oil and gas) to be separated through each evenly distributed independent chamber 205 to ensure a consistent flow rate at the outlet. Preferably, the number of partitions 204 is 2-8.

[0059] Each group of independent chambers 205 is connected to a distribution pipe 206 for conveying the feed in the independent chamber 205. Each distribution pipe 206 is evenly distributed on the outer wall of the feed chamber 201 cylinder near the bottom and communicates with the independent chamber 205, and the inner wall of the distribution pipe 206 is preferably tangent to the outer wall of the feed chamber 201. The diameter of the distribution pipe 206 is determined according to the flow rate to be processed, and the shape is cylindrical or square.

[0060] See Figure 1 Combined with Figure 4 The momentum defoamer module includes a plurality of groups of momentum defoamers 3, which are vertical structures and are evenly arranged around the dynamic distributor 2. Each group of momentum defoamers 3 is connected to a group of independent chambers 205 through a distribution pipe 206 on the dynamic distributor 2.

[0061] The momentum defoamer 3 is a cylindrical tower structure; the momentum defoamer 3 is composed of a straight section 302 and a conical section 306 connected from bottom to top, wherein the straight section 302 is used for preliminary defoaming; the conical section 306 is used for momentum depth defoaming. Specifically, the lower part of the momentum defoamer 3 is the straight section 302, the diameter of which remains unchanged; the upper part is the conical section 306, the diameter of which gradually decreases from bottom to top. Preferably, the outlet diameter of the conical section 306 is 0.2-0.4 times the diameter of the straight section 302.

[0062] The straight section 302 of the momentum defoamer 3 is connected to the feed pipe 301, the distribution pipe 206 of the dynamic distributor 2 is connected to the feed pipe 301 of the momentum defoamer 3, and the momentum defoamer 3 is connected to the oil and gas inlet 1 through the distribution pipe 206 of the dynamic distributor 2 to achieve the purpose of receiving the mixed phase to be processed.

[0063] The straight section 302 of the momentum defoamer 3 is equipped with a grid structure, which is located near the top of the straight section 302. The grid structure includes a metal grid 303 and a barbed hook (not shown in the figure), wherein the metal grid 303 is placed horizontally and matches the inner wall diameter of the straight section 302, and the metal grid 303 is formed by crossing metal wires, and the crossing angle of the metal wires is 30-90°. The metal grid 303 is used to divide the larger foam in the mixed phase, thereby avoiding the problems of passage blockage caused by incomplete defoaming of the subsequent large foam; the barbed hook is fixed on the metal grid 303, and the barbed hook is used to pierce some larger bubbles in the gas-liquid mixed phase.

[0064] An annular baffle 304 is installed in the conical cylinder section 306 of the momentum defoamer 3. Multiple groups of annular baffles 304 are arranged along the vertical direction of the cylinder. Multiple groups of annular baffles 304 are arranged at equal intervals along the inner wall of the conical cylinder section 306 of the momentum defoamer 3. The inclination angle between each group of annular baffles 304 and the horizontal plane is between 30-45°, and preferably, the distance between two vertically adjacent groups of annular baffles 304 is 0.15-0.2 times the total vertical distance of the conical cylinder section 306. The annular baffle 304 is used to prevent the high momentum foam group from further rising with the airflow. After the high momentum foam hits the wall, the liquid film continues to break, and finally a certain amount of fine droplets are formed, which are discharged from the momentum defoamer 3 under the entrainment of the high-speed airflow, thereby achieving the purpose of momentum defoaming.

[0065] The momentum defoamer 3 further includes an upper baffle and a lower baffle (not shown in the figure), which are located at the upper and lower parts of each group of momentum defoamers 3 and the dynamic distributor 2. Above the upper baffle is a coalescence buffer zone (not shown in the figure), preferably, the distance between the upper baffle and the top outlet of the cone section 306 is about 10-30 cm, and the lower baffle is separated from the bottom of the momentum defoamer 3 by a certain space.

[0066] The top outlet of the conical cylinder section 306 is connected to an overflow pipe 305, and the overflow pipe 305 passes through the upper partition plate and is connected to the coalescence buffer zone. The defoamed oil and gas rise to the coalescence buffer zone through the overflow pipe 305.

[0067] In addition, a support rod is fixed inside the tank body, and a longitudinal and transverse mounting plates are provided on the support rod. A fixing plate is provided on the outer wall of the momentum defoaming module, and is connected and fixed to the longitudinal and transverse mounting plates of the support rod through the fixing plate, so that the momentum defoaming module and the dynamic distributor 2 connected thereto are installed and fixed in the tank body (not shown in the figure).

[0068] Back to Figure 1 The top of the momentum defoaming module extends upward in the vertical direction and is sequentially provided with a fiber coagulation module 4 and a rotary dehydration module. Among them, there is a swirl buffer between the fiber coagulation module 4 and the rotary dehydration module, and there is an exhaust buffer above the rotary dehydration module (not shown in the figure).

[0069] The fiber coagulation module 4 includes a plurality of fiber bed layers arranged at intervals, wherein the fiber bed layers are woven from modified polymer fibers at a certain angle of 45-90°, and the diameter of the modified polymer fibers is 50-250 μm. Within this range, the fiber has the best ability to capture droplets; wherein, the fiber material should be lipophilic fibers such as polytetrafluoroethylene, polyester ethylene, etc.

[0070] The porosity of the fiber bed layer is 0.65-0.85 and its gradient decreases upward in the direction of the flow. The thickness of the fiber bed layer is between 0.3-0.5m, and the number of fiber bed layers is determined according to the flow rate of the gas-liquid mixed phase, preferably 1-3 so that small droplets can be fully captured, which is conducive to the accumulation and aggregation of droplets in the lyophilic fiber bed, providing a basis for further liquid removal by the subsequent rotary dehydration module.

[0071] Combination Figure 5 As shown, the rotary dehydration module is formed by a plurality of cyclone core tubes 6 arranged in a ring, and the number of cyclone core tubes 6 required to be arranged is determined according to the flow rate of the gas-liquid mixture to be processed.

[0072] The bottom of the cyclone core tube 6 is the inlet end. A core tube central column 602 is provided at the center of the inlet end of the cyclone core tube 6. A plurality of core tube partitions 601 are provided at the bottom of each cyclone core tube 6. The core tube partitions 601 are evenly fixed on the core tube central column 602. The bottom is divided into a plurality of independent chambers by the core tube partitions 601. A spiral blade monolith 603 is installed on each chamber. The spiral blade monolith 603 is fixed on the core tube central column 602. Preferably, the core tube partition 601 is set to 3 pieces, and the corresponding spiral blades are set to 3 pieces. And preferably, the spiral angle of the spiral blade monolith 603 is 30-45°.

[0073] The cyclone core tube 6 is arranged in the form of an inner and outer sleeve, respectively an inner sleeve and an outer sleeve, and the inner and outer sleeves are fixed by a number of evenly arranged fixing plates 605, and a drainage cavity 606 for discharging the separated liquid is formed between the inner and outer sleeves. Preferably, the number of fixing plates 605 is 4-6. An exhaust pipe 604 is provided at the top of the inner sleeve. Preferably, the diameter of the exhaust pipe 604 (i.e., the gas phase overflow outlet) of the adaptive cyclone core tube 6 is 0.6-0.7 of the diameter of the inner sleeve. The lighter gas phase in the gas-liquid mixture through the spiral blades is discharged along the exhaust pipe 604, while the relatively heavier liquid phase is discharged along the wall under the action of the centrifugal field, and finally discharged from the core tube along the drainage cavity 606, thereby achieving deep purification of the gas.

[0074] The two ends of the rotary deliquescence module and the fiber coagulation module 4 are provided with overflow channels 9 for discharging the separated liquid phase. Figure 1 Combined with Figure 5The overflow channel 9 is connected from the side of the rotary deliquidation module to the liquid collecting area at the bottom of the tank. When the liquid level on the fiber bed and the cyclone core tube 6 platform reaches a certain height, it is discharged into the liquid collecting cavity at the bottom of the tank along the overflow channel 9. The liquid level in the tank is monitored in real time by the liquid level meter 7. When the liquid level reaches the preset value, it is discharged from the tank through the liquid phase outlet 8.

[0075] In addition, the momentum defoaming module and the rotary deliquescence module are used in multiple groups in parallel, as follows:

[0076] The processing capacity of a single tower kinetic defoamer 3 is 50-500m 3 / h, and are used in parallel in a uniformly distributed manner on the flow cross-section of the separator, preferably in an annular arrangement.

[0077] The processing capacity of a single cyclone separation core tube 6 is 100-1000m 3 / h, and are used in parallel in a uniformly distributed manner on the flow cross-section of the separator, preferably in an annular arrangement.

[0078] Example 2

[0079] A deep gas purification method based on momentum defoaming adopts the above-mentioned deep gas purification device.

[0080] Since the circulating hydrogen coming out of the reactor contains a certain amount of oil phase, wherein the oil phase exists in the form of foamy droplets and fine droplets, a gas-liquid mixture (i.e., oil and gas) is formed, which results in insufficient gas purity and affects subsequent processes; therefore, the gas-liquid mixture is introduced into the deep gas purification device of the present application to achieve efficient, rapid, and low-cost aggregation and separation of foamy droplets and fine droplets.

[0081] The methods specifically include:

[0082] The oil and gas are introduced into the tank from the oil and gas inlet 1 in the middle of the tank body, and the oil and gas enter the dynamic distributor 2 through the pipeline for distribution. The distribution pipe 206 of the dynamic separator evenly distributes the oil and gas airflow to each momentum defoamer 3 on the momentum defoamer module, and defoaming is performed in the momentum defoamer 3; in the momentum defoamer 3, the gas-liquid mixture first moves vertically upward along the straight cylinder section 302, and when it moves to the metal grid 303, under the action of the metal grid 303 and its attached barbed hooks, the large foam droplets are divided and broken into several small foam droplets, and move to the conical cylinder section 306 under the action of high-speed airflow, and the high-momentum foam droplets collide with the annular baffle 304, and the liquid film is continuously broken, and finally annihilated into fine droplets, which move to the overflow pipe 305 under the entrainment of the airflow, and are then discharged from the momentum defoamer 3.

[0083] The gas discharged from the automatic defoamer 3 still contains a large number of fine droplets that have not been processed in the kinetic defoamer module and a very small amount of incompletely processed foam droplets.

[0084] The defoamed oil and gas airflow flows upward through the fiber condensation module 4, and the small droplets entrained in the airflow are captured and aggregated by the cross fibers in the fiber condensation module 4; when the gas enters the fiber condensation module 4, due to the large difference in the affinity of the fiber material to the oil and gas phases, the liquid is captured by the fiber material and retained on the surface and in the gaps of the material to form an oil film; when the oil film increases to a certain thickness, the oil film falls off and merges into larger droplets under the action of gravity, thereby achieving the aggregation of fine droplets into larger droplets, and finally discharged from the fiber condensation module 4 through the entrainment of high-speed airflow, and the remaining very small amount of untreated foamy droplets also become fine droplets under the shearing action of the fibers, achieving complete elimination.

[0085] The gas discharged from the fiber agglomeration module 4 contains only a certain amount of relatively large droplets.

[0086] Then the oil and gas continue to flow upward through the cyclone separation module, and the high-speed rotation flow in the cyclone separation unit separates the droplets entrained in the oil and gas; in the rotary deliquidation module, compared with the untreated smaller fine droplets, the larger droplets settle faster or are thrown away from the cyclone path due to inertia, so that they are more easily separated and eliminated in the cyclone core tube 6. When the gas enters the cyclone core tube 6 in the vertical direction, it is first evenly distributed into multiple streams under the action of the core tube partition 601, and each air flow forms a further cyclone under the action of the corresponding spiral blades. A low-pressure area is generated in the central area of ​​the rotating turbulent flow, and its centrifugal field and pressure gradient field make all the gas in the feed gather toward the center, so that an air column is formed in the center of the cyclone core tube 6. Under the superposition of the cyclone field and the gravity field, the liquid moves toward the side wall. When the liquid converges to a certain height, it is discharged from the core tube along the drainage cavity 606 between the inner and outer sleeves, and the gas is discharged along the gas phase outlet at the top, so as to achieve deep purification of the gas. The liquid separated from the coalescing fiber module and the rotary deliquidation module is discharged into the liquid collecting area along the overflow channels 9 on both sides of the tank body, and finally discharged from the separator along the liquid phase outlet 8. At the same time, in this process, the oil and gas purified by defoaming and deliquidation are discharged from the device through the gas phase outlet at the top of the separator tank body.

[0087] In the above method, the inlet flow rate of the gas deep purification device is 3-7m / s, the inlet liquid volume is 5-8%, the droplet size in the gas discharged by the automatic defoaming module is generally about 0.1-70μm, and the droplet size after being coalesced by the fiber condensation module 4 is generally between 30-500μm. With the deep purification device based on the momentum defoaming function of the utility model, the defoaming rate can reach ≥99.9%, the size of the entrained droplets at the gas phase outlet 5 is ≤1μm, the size of the foam droplets is ≤10μm, and the frequency of occurrence is extremely low.

[0088] Comparative Example 1

[0089] A petrochemical plant uses the deep purification device based on the gas momentum defoaming function of Example 1. The reaction environment conditions and the product properties of Example 1 and the original device using multiple built-in cyclones are shown in Table 1.

[0090] Table 1

[0091] Original device Example 1 Reaction temperature 260 260 Liquid-gas ratio 0.1 0.1 Reactor pressure 3Mpa 3Mpa Volume flow <![CDATA[50m 3 / h]]> <![CDATA[50m 3 / h]]> Defoaming efficiency 65.2％ 98.7％ Average droplet size at gas phase outlet 40μm 2.7μm Frequency of foam droplets 180 pieces / min 2 times / min

[0092] From the data in Table 1, it can be seen that the gas-liquid separation efficiency of this application example 1 is improved by 33.9% compared with the original device, the average droplet size at the gas phase outlet is reduced by about 38 μm, and the frequency of foam droplets is also reduced to 2 / min.

[0093] Comparative Example 2

[0094] A petrochemical plant uses the deep purification device based on the gas momentum defoaming function of Example 1. The reaction environment conditions and the product properties of Example 1 and the original device with multiple fiber layers are shown in Table 2.

[0095] Table 2

[0096] Original device Example 1 Reaction temperature 275 275 Liquid-gas ratio 0.1 0.1 Reactor pressure 3Mpa 3Mpa Volume flow <![CDATA[50m 3 / h]]> <![CDATA[50m 3 / h]]> Defoaming efficiency 62.2％ 97.3％ Average droplet size at gas phase outlet 17μm 4.2μm Frequency of foam droplets 120 pieces / min 4 times / min

[0097] It can be seen from the data in Table 2 that compared with Application Example 1, the gas-liquid separation efficiency of Application Example 1 is improved by 36% compared with the original device, the average droplet size at the gas phase outlet is reduced by about 13 μm, the frequency of foam droplets is also reduced to 4 / min, and the fiber bed is not blocked, and the overall effect is good.

[0098] The above description is only a preferred specific implementation manner of the present invention, but the protection scope of the present invention is not limited thereto. Any technician familiar with the technical field can make equivalent replacements or changes within the technical scope disclosed by the present invention according to the technical scheme and the utility model concept of the present invention, which should be covered by the protection scope of the present invention.

Claims

1. A deep gas purification device based on momentum defoaming, characterized in that: The invention comprises a tank, a dynamic distributor, a kinetic defoaming module having a plurality of kinetic defoamers, a fiber coagulation module and a rotary deliquescence module, wherein: An oil and gas inlet is provided in the middle of the side wall of the tank body, and the oil and gas inlet is connected to the dynamic distributor through a pipeline. A feed chamber with multiple groups of independent chambers is provided in the dynamic distributor, and each group of independent chambers is connected to the momentum defoamer through a distribution pipe. The momentum defoamer is a tower-shaped structure, including a straight section and a conical section connected from bottom to top, wherein the straight section is used for preliminary defoaming; and the conical section is used for momentum deep defoaming; The momentum defoaming module extends along the top to include a fiber condensation module, a rotary dehydration module and a gas phase outlet in sequence, and overflow channels for discharging the separated liquid phase are provided at both ends of the rotary dehydration module and the fiber condensation module, and the overflow channels are connected to the liquid collecting area at the bottom of the tank body.

2. The deep gas purification device based on momentum defoaming according to claim 1 is characterized in that: The dynamic distributor is equipped with a spiral guide vane, and a plurality of partitions arranged at equal angles are provided below the spiral guide vane. The plurality of partitions divide the feed chamber into a plurality of independent chambers, and each group of independent chambers is correspondingly connected to the distribution pipe. The spiral angle of the spiral guide vane is 30-45°, and the number of the partitions is 2-8.

3. The deep gas purification device based on momentum defoaming according to claim 1 is characterized in that: A metal grid formed by crossing metal wires is installed in the straight section of the momentum defoamer, the crossing angle of the metal wires is 30-90 degrees, and the metal grid is covered with barbs.

4. The deep gas purification device based on momentum defoaming according to claim 1 is characterized in that: The inner wall of the cone section of the momentum defoamer is provided with a plurality of annular baffles arranged at equal distances along its vertical direction, the inclination angle between the annular baffles and the horizontal plane is between 30-45°, and the distance between two vertically adjacent groups of annular baffles is 0.15-0.2 times the total vertical distance of the cone section; the outlet diameter of the cone section is 0.2-0.4 times the diameter of the straight section.

5. The deep gas purification device based on momentum defoaming according to claim 1 is characterized in that: The momentum defoamer module also includes an upper baffle and a lower baffle located at the upper and lower parts of the multiple groups of momentum defoamers. The top of the cone section is connected to an overflow pipe, and the overflow pipe passes through the upper baffle.

6. The deep gas purification device based on momentum defoaming according to claim 1 is characterized in that: The fiber coagulation module includes a plurality of fiber bed layers arranged at intervals, wherein the fiber bed layers are woven from modified polymer fibers at a certain angle of 45-90°, and the diameter of the modified polymer fibers is 50-250 μm; the porosity of the fiber bed layers is 0.65-0.85 and the gradient decreases upward in the direction of the flow, the thickness of the fiber bed layers is between 0.3-0.5 m, and the number of the fiber bed layers is 1-3.

7. The deep gas purification device based on momentum defoaming according to claim 1 is characterized in that: The rotary dehydration module is formed by a plurality of cyclone core tubes arranged in a ring shape; Each cyclone core tube has a plurality of independent chambers at the bottom, and each chamber is equipped with an independent spiral blade, which is fixed on the core tube center column in the center of the cyclone core tube, and the spiral angle of the spiral blade is 30-45°; The cyclone core tube is arranged in the form of an inner and outer sleeve, the inner and outer sleeves are fixed by a fixing plate, and a liquid discharge cavity for discharging separated liquid is formed between the inner and outer sleeves.

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