A deep gas purification device and method based on momentum defoaming

Abstract

The application discloses a kind of momentum defoaming based deep gas purification device and method, it is related to chemical equipment technical field, including tank, dynamic distributor, with several momentum defoaming ware momentum defoaming module, fiber condensation module and rotary liquid removal module, tank is equipped with oil gas inlet, liquid phase outlet, gas phase outlet, oil gas inlet is connected dynamic distributor by pipeline, dynamic distributor end is connected with momentum defoaming module;Momentum defoaming module top is equipped with fiber module and rotary liquid removal module in sequence.This application utilizes the momentum of gas-liquid mixture and the baffle in momentum defoaming ware to collide, break up foam liquid drop, and make liquid drop move to the edge of baffle, under the driving of subsequent airflow, discharge, realize the elimination of foam liquid drop;The remaining micro liquid drop is coalesced and grown into larger droplet by fiber condensation module, finally enters rotary liquid removal module, realizes the efficient separation of liquid drop and gas under the action of centrifugal field, reaches the effect of gas deep purification.

Description

Technical Field

[0001] This invention relates to the field of chemical equipment technology, and in particular to a deep gas purification device and method based on momentum defoaming. Background Technology

[0002] With the continuous progress of society and the development of the petrochemical industry, the quality of various petroleum products is also improving. Light oils, due to their high cleanliness, high combustion efficiency, large market demand, and ease of storage, provide strong support for achieving low-carbon economy and sustainable development goals. To further refine petroleum products into C3, C4, and C5 light oils through hydrogenation, smaller bubbles are typically needed to achieve liquid-phase hydrogenation. However, smaller bubbles can easily cause some of the distillate after the reaction to escape as a foamy gas-liquid mixture or droplets under the entrainment of high-speed gas flow, resulting in oil waste and even impacting subsequent refining processes. Therefore, adopting appropriate and efficient defoaming devices can prevent the escape of certain light oil components by high-speed gas flow, thus avoiding resource waste and increased energy consumption.

[0003] In actual processes, the liquid phase entrainment in the gas phase needs to be controlled below a suitable value to meet the quality requirements of the desired product. If the circulating hydrogen contains an oil phase, it will have a toxic effect on the catalyst, potentially neutralizing or poisoning it, reducing catalytic activity, and slowing down or hindering the reaction rate. Furthermore, oil droplets or foamy gas-liquid mixtures may deposit in the reactor and pipelines, causing equipment blockage and corrosion, and even potentially leading to equipment wear and damage. This may require frequent maintenance and cleaning, increasing production costs.

[0004] In traditional industrial production processes, defoaming is typically achieved using devices such as wire mesh demisters, which offer advantages such as simple structure, ease of installation and maintenance, and high economic efficiency. However, their defoaming efficiency is not high when handling high flow rates, high temperatures, high pressures, or extreme foaming conditions. Therefore, there is a need to develop a deep gas purification device with defoaming capabilities to address the problem of high foam and droplet content in the circulating hydrogen gas from hydrogenation reactions.

[0005] To address the aforementioned technical challenges, some solutions already exist within existing technologies:

[0006] CN116574542A discloses a high-efficiency cyclone defoaming oil-gas separator, including a tank with a medium inlet, an oil outlet, and a natural gas outlet. A cyclone defoaming component to improve the defoaming rate is installed inside the medium inlet, and a wire mesh demister to defoam micro-foams is installed inside the natural gas outlet. Forced defoaming is achieved using cyclone flow and a hypergravity field, which improves defoaming efficiency to some extent. However, when applied to this process, the foam entrained by the high-speed airflow causes instability in the cyclone flow field structure, resulting in a certain amount of foam remaining at the gas phase outlet inside the cyclone separator, thus affecting the defoaming efficiency.

[0007] CN220003436U discloses a gas-liquid separation device and a gas-liquid separation system. The gas-liquid separation device includes a separation tank, an exhaust port on the upper side of the separation tank, a drain port on the lower side of the separation tank, an air inlet on the separation tank, and a liquid collection mechanism. The separation tank contains at least one layer of baffles above the air inlet. Each baffle has at least one receiving cavity with an open bottom and a fiber coalescing unit located within the receiving cavity. The sidewall of the receiving cavity has through holes to allow liquid-containing gas entering the separation tank from the air inlet to undergo gas-liquid separation via the fiber coalescing unit. The separated gas is discharged through the exhaust port, and the separated liquid is transported to the drain port by the liquid collection mechanism and discharged. This gas-liquid separation device can perform gas-liquid separation of liquid-containing gas and liquid, with high separation efficiency and a simple structure, and can efficiently coalesce fine droplets. However, in this process, large-volume foam can easily clog the fiber layer, making airflow difficult and resulting in a certain degree of efficiency reduction.

[0008] In other words, for hydrogen recirculation reactions where the inlet is a gas-liquid mixture mixed with a certain amount of foam phase, existing technologies can directly use swirl or coalescence to cause problems such as unstable swirl flow field and fiber blockage due to the foam phase. Summary of the Invention

[0009] The purpose of this invention is to address the shortcomings of existing technologies by proposing a deep gas purification device and method based on momentum defoaming. The aim is to eliminate oil phase foam and droplets in the hydrogenation reaction cycle based on momentum, while using coalescing fibers and cyclone devices to eliminate fine oil droplets, thereby achieving the function of deep gas purification and solving the problem of foamy gas-liquid mixture appearing at the gas outlet.

[0010] To achieve the above objectives, the present invention adopts the following technical solution:

[0011] A deep gas purification device based on momentum defoaming includes a tank, a dynamic distributor, a momentum defoaming module with several momentum defoamers, a fiber coagulation module, and a rotary dehydration module, wherein:

[0012] The tank has an oil and gas inlet in the middle of its side wall, a gas outlet at the top and a liquid outlet at the bottom. 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 and dried hydrogen, and the liquid outlet is used to discharge the separated liquid phase.

[0013] The oil and gas inlet is connected to the dynamic distributor via a pipeline. The dynamic distributor is equipped with a feed chamber with multiple independent chambers. Each set of independent chambers is connected to the momentum defoamer via a distribution pipe.

[0014] The momentum defoamer is a tower-shaped structure, comprising a straight cylindrical section and a conical section connected from bottom to top. The straight cylindrical section is used for initial defoaming, and the conical section is used for deep momentum defoaming.

[0015] The momentum defoaming module extends from the top and consists of a fiber coagulation module, a rotary dehydration module, and a gas phase outlet. The rotary dehydration module and the fiber coagulation module are provided with overflow channels at both ends for discharging the separated liquid phase. The overflow channels are connected to the liquid collection area at the bottom of the tank.

[0016] Furthermore, the dynamic distributor has a built-in spiral guide vane, and several partitions arranged at equal angles are provided below the spiral guide vane. The partitions divide the feed chamber into multiple independent chambers, and the distribution pipe is connected to the outside of each independent chamber. The spiral angle of the spiral guide vane is 30-45°, and the number of partitions is 2-8.

[0017] Furthermore, the momentum defoamer has a metal mesh formed by intersecting metal wires installed inside the straight section, the intersecting angle of the metal wires being 30-90°, and the metal mesh being covered with barbs.

[0018] Furthermore, the inner wall of the momentum defoamer cone section is provided with several annular baffles arranged at equal intervals along its vertical direction. The inclination angle between the annular baffles and the horizontal plane is between 30 and 45°, and the distance between two vertically adjacent sets of annular baffles is 0.15 to 0.2 times the total vertical distance of the cone section; the outlet diameter of the cone section is 0.2 to 0.4 times the diameter of the straight section.

[0019] Furthermore, the momentum defoaming module also includes an upper partition and a lower partition located above and below the multiple sets of momentum defoamers, and the top of the cone section is connected to an overflow pipe, which passes through the upper partition.

[0020] Furthermore, the fiber coagulation module includes several fiber beds spaced apart, wherein the fiber beds are made of modified polymer fibers woven at a certain angle, the weaving angle being 45-90°, the diameter of the modified polymer fibers being 50-250μm; the porosity of the fiber beds is 0.65-0.85 and decreases upward in the direction of the incoming flow, the thickness of the fiber beds is between 0.3-0.5m, and the number of fiber beds is 1-3.

[0021] Furthermore, the rotary dehydration module is composed of multiple cyclone core tubes arranged in a ring;

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

[0023] The cyclone core tube is arranged in the form of inner and outer sleeves, which are fixed together by a fixing plate, and a drainage chamber is formed between the inner and outer sleeves for discharging the separated liquid.

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

[0025] S1. The oil and gas are introduced into the tank through the oil and gas inlet. 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 defoaming module, and defoaming is carried out by the momentum defoamer.

[0026] S2. The defoamed oil and gas flow upward through the fiber condensation module, where the cross fibers in the fiber condensation module capture and coalesce the small droplets entrained in the airflow.

[0027] S3. After agglomeration, the oil and gas continue to flow upward through the cyclone separation module, and the liquid droplets entrained in the oil and gas are separated by high-speed rotational flow in the cyclone separation unit.

[0028] S4. The droplets are discharged through the drain chamber 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 and dehydration purification, are discharged through the gas phase outlet at the top of the separator tank.

[0030] Furthermore, in S1, the momentum defoamer defoaming method is as follows: the oil and gas are initially defoamed and then defoamed by momentum depth by using the metal mesh with barbs in the straight section and the annular baffle with multiple conical sections in the conical section. The oil and gas flow moves into the conical section under the action of high-speed airflow. The high momentum foam droplets in the oil and gas flow collide with the annular baffle, and the liquid film is continuously broken and eventually annihilated into fine droplets.

[0031] Furthermore, both the momentum defoaming module and the rotary dehydration module are used in parallel in multiple sets, evenly distributed across the flow cross-section of the separator, wherein:

[0032] The single-unit processing capacity of the momentum defoamer is 50-500 m³. 3 / h.

[0033] The single-unit processing capacity of the cyclone separator module is 100-1000m³. 3 / h.

[0034] Compared with the prior art, the beneficial effects of the present invention are:

[0035] (1) This invention proposes a deep purification device based on gas momentum defoaming. The hydrogen gas in the hydrogenation reaction cycle, which is a gas-liquid mixture at the inlet and contains a certain amount of foam phase, is evenly distributed to the momentum defoamer through a dynamic distributor. This avoids problems such as unstable swirling flow field and fiber blockage caused by foam phase caused by direct swirling or coalescence. Furthermore, the momentum defoamer utilizes the momentum collision between the gas itself and the wall surface to eliminate the entrained foam droplets and reduce relative energy loss, thereby achieving the purpose of efficient defoaming.

[0036] (2) Based on the momentum defoaming module, this invention proposes a deep gas purification method. On the basis of the momentum defoaming module eliminating most of the foamy droplets, a step-by-step enhanced micro-droplet separation method is proposed. The fiber coagulation module is used to realize the collision, aggregation and growth of micro-droplets into larger droplets. After passing through the momentum defoamer, the smaller foam is less likely to cause blockage of the fiber bed. Finally, it is further removed in the cyclone core tube in the rotary desliming module, realizing the efficient removal of micro-droplets and greatly improving the separation efficiency. Attached Figure Description

[0037] Figure 1 This is a schematic diagram of the overall structure of the present invention;

[0038] Figure 2 This is a schematic diagram of the overall structure of the dynamic allocator in this invention;

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

[0040] Figure 4 This is a schematic diagram of the momentum defoamer in the momentum defoaming module of the present invention;

[0041] Figure 5 This is a schematic diagram of the cyclone core tube in the rotary dehydration module of the present invention;

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

[0043] Figure 7 This is a schematic diagram illustrating the principle of how the momentum defoaming module in this invention eliminates foamy droplets.

[0044] In the diagram: 1. Oil and gas import;

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

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

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

[0048] 6. Swirl core tube; 601. Core tube partition; 602. Core tube center column; 603. Single spiral blade; 604. Exhaust pipe; 605. Fixing plate; 606. Drainage chamber;

[0049] 7. Level gauge; 8. Liquid phase outlet; 9. Overflow channel. Detailed Implementation

[0050] The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings of the embodiments of the present invention. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments.

[0051] Example 1

[0052] A deep gas purification device based on momentum defoaming, such as Figure 1As shown, the system includes a tank (not shown) and a dynamic distributor 2, a momentum defoaming module with several momentum defoamers 3, a fiber condensation module 4, and a rotary dehydration module with several swirl core tubes 6, all housed within the tank. The tank inlet is connected to the momentum defoaming module via the dynamic distributor 2, and the fiber condensation module 4 and the rotary dehydration module are sequentially arranged above the momentum defoaming module. Oil and gas enter the tank and are evenly distributed by the dynamic distributor 2 to the momentum defoaming module for defoaming. The oil and gas then rise to the fiber condensation module 4 and the rotary dehydration module to remove droplets, and finally, the defoamed and dehydrated gas is discharged from the tank.

[0053] Specifically, see Figure 1 The tank has a vertical cylindrical structure. An oil / gas inlet 1 is located in the middle of the side wall of the tank, used to receive the gas and liquid phases to be purified. A gas outlet 5 is located at the top of the tank, and a liquid outlet 8 is located at the bottom. Gas outlet 5 is used to discharge the separated, dried hydrogen gas, and liquid outlet 8 is used to discharge the separated liquid phase. The bottom of the tank is divided into a liquid collection area, and a level gauge 7 is also installed on the tank. The detection end of level gauge 7 is located in the liquid collection area to detect the liquid level in the collection area.

[0054] See Figure 1 Simultaneously combined Figure 2-3 The oil and gas inlet 1 on the tank is connected to the dynamic distributor 2 via a pipeline. The dynamic distributor 2 is equipped with a feed chamber 201 with multiple independent chambers 205, which uniformly discharges the gas-liquid mixture in the independent chambers 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 several 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 via a pipe, and the feed chamber 201 has a cylindrical structure.

[0056] A central column 203 is fixed at the 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 times the diameter De of the dynamic distributor 2.

[0057] Multiple sets of spiral guide vanes 202 are installed 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 in place. Preferably, the angle of the spiral guide vane 202 is 30-45°.

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

[0059] Each set of independent chambers 205 is externally connected to a distribution pipe 206 for conveying the feed into the independent chamber 205. Each distribution pipe 206 is evenly distributed on the outer wall of the feed chamber 201 near the bottom and communicates with the independent chamber 205. Preferably, the inner wall of the distribution pipe 206 is tangential 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 its shape is cylindrical or square.

[0060] See Figure 1 Simultaneously combined Figure 4 The momentum defoaming module includes multiple sets of momentum defoamers 3, which are vertically oriented and evenly arranged around the dynamic distributor 2. Each set of momentum defoamers 3 is connected to an independent chamber 205 via a distribution pipe 206 on the dynamic distributor 2.

[0061] The momentum defoamer 3 is a cylindrical tower-shaped structure. It consists of a straight cylindrical section 302 and a conical section 306 connected from bottom to top. The straight cylindrical section 302 is used for initial defoaming, and the conical section 306 is used for deep momentum defoaming. Specifically, the lower part of the momentum defoamer 3 is the straight cylindrical section 302, with a constant diameter; the upper part is the conical section 306, with a diameter gradually decreasing from bottom to top. Preferably, the outlet diameter of the conical section 306 is 0.2-0.4 times the diameter of the straight cylindrical section 302.

[0062] The straight section 302 of the momentum defoamer 3 is externally 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. 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 treated.

[0063] The momentum defoamer 3 has a grid structure inside its straight cylindrical section 302, located near the top. The grid structure includes a metal mesh 303 and barbs (not shown in the figure). The metal mesh 303 is horizontally placed and adapted to the diameter of the inner wall of the straight cylindrical section 302. The metal mesh 303 is formed by intersecting metal wires at an angle of 30-90°. The metal mesh 303 is used to break up larger bubbles in the mixed phase, thus avoiding problems such as channel blockage caused by incomplete defoaming of large bubbles. The barbs are fixed to the metal mesh 303 and are used to puncture some of the larger bubbles in the gas-liquid mixture.

[0064] An annular baffle 304 is installed inside the conical section 306 of the momentum defoamer 3. Multiple sets of annular baffles 304 are arranged vertically along the cylinder. These sets of annular baffles 304 are evenly spaced along the inner wall of the conical section 306 of the momentum defoamer 3. The inclination angle between each set of annular baffles 304 and the horizontal plane is between 30° and 45°. Preferably, the distance between two vertically adjacent sets of annular baffles 304 is 0.15-0.2 times the total vertical distance of the conical section 306. The annular baffles 304 are used to prevent the high-momentum foam from rising further with the airflow. After the high-momentum foam impacts the wall, the liquid film continuously ruptures, eventually forming a certain amount of fine droplets. These droplets are then discharged from the momentum defoamer 3 under the entrainment effect of the high-speed airflow, achieving the purpose of momentum defoaming.

[0065] The momentum defoamer 3 also includes an upper baffle and a lower baffle (not shown in the figure), which are located above and below each set of momentum defoamers 3 and dynamic distributors 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 there is a certain space between the lower baffle and the bottom of the momentum defoamer 3.

[0066] The top outlet of the cone section 306 is connected to an overflow pipe 305, which passes through the upper baffle and connects to the coalescing buffer zone. The defoamed oil and gas rises to the coalescing buffer zone through the overflow pipe 305.

[0067] In addition, a support rod is fixed inside the tank, and 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 the fixing plate is connected and fixed to the longitudinal and transverse mounting plates of the support rod, thereby installing and fixing the momentum defoaming module and its connected dynamic distributor 2 inside the tank (not shown in the figure).

[0068] Back Figure 1 The top of the momentum defoaming module extends vertically upwards and is successively configured as a fiber coagulation module 4 and a rotary dehydration module. A vortex buffer zone exists between the fiber coagulation module 4 and the rotary dehydration module, and an exhaust buffer zone (not shown in the figure) is located above the rotary dehydration module.

[0069] The fiber coagulation module 4 includes several fiber beds spaced apart, wherein the fiber beds are made of modified polymer fibers woven at a certain angle, the weaving angle being 45-90°, and the diameter of the modified polymer fibers being 50-250μm. Within this range, the fiber's ability to capture droplets is optimal; the fiber material should be oleophilic fibers such as polytetrafluoroethylene and polyester.

[0070] The porosity of the fiber bed is 0.65-0.85 with a decreasing gradient in the upward direction of the inflow. The thickness of the fiber bed is between 0.3-0.5m. The number of fiber beds is determined according to the gas-liquid mixed phase flow rate, preferably 1-3, so that small droplets can be fully captured. This is beneficial for the accumulation and aggregation of droplets in the hydrophilic 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 composed of multiple cyclone core tubes 6 arranged in a ring, and the number of cyclone core tubes 6 required is determined according to the flow rate of the gas-liquid mixture to be treated.

[0072] The bottom of the cyclone core tube 6 is the inlet end. A core tube center column 602 is located at the center of the inlet end of the cyclone core tube 6. Each cyclone core tube 6 has multiple core tube partitions 601 at its bottom, which are evenly fixed to the core tube center column 602. The core tube partitions 601 divide the bottom into multiple independent chambers, and each chamber is equipped with a single spiral blade 603, which is fixed to the core tube center column 602. Preferably, there are three core tube partitions 601, and three corresponding spiral blades. Furthermore, preferably, the spiral angle of the single spiral blade 603 is 30-45°.

[0073] The cyclone core tube 6 is arranged in the form of an inner and outer sleeve, which are fixed together by a number of evenly arranged fixing plates 605. A drainage chamber 606 is formed between the inner and outer sleeves for discharging the separated liquid. Preferably, there are 4-6 fixing plates 605. 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 times the diameter of the inner sleeve. The lighter gas phase in the gas-liquid mixture passing 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 centrifugal force, and finally discharged from the core tube along the drainage chamber 606, achieving deep purification of the gas.

[0074] Furthermore, both ends of the rotary desliming module and the fiber coagulation module 4 are equipped with overflow channels 9 for discharging the separated liquid phase, see... Figure 1 Simultaneously combined Figure 5The overflow channel 9 is connected from the side of the rotating dehydration module to the liquid collection area at the bottom of the tank. After the liquid level on the fiber bed and the platform of the cyclone core tube 6 reaches a certain height, it is discharged along the overflow channel 9 into the liquid collection chamber at the bottom of the tank. The liquid level in the tank is monitored in real time by the liquid level gauge 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 dehydration module are used in multiple parallel connections, as follows:

[0076] The single-unit processing capacity of the tower-shaped momentum defoamer 3 is 50-500m³. 3 / h, which are used in parallel by being evenly distributed across the flow cross section of the separator, preferably in a ring arrangement.

[0077] The single-tube throughput of the cyclone separator 6 is 100-1000m³. 3 / h, which are used in parallel by being evenly distributed across the flow cross section of the separator, preferably in a ring arrangement.

[0078] Example 2

[0079] A deep gas purification method based on momentum defoaming, employing the aforementioned deep gas purification device.

[0080] Since the circulating hydrogen gas coming out of the reactor contains a certain amount of oil phase, which exists in the form of foam-like droplets and micro-droplets, forming a gas-liquid mixture (i.e., oil-gas), the gas purity is insufficient, affecting subsequent processes. Therefore, this gas-liquid mixture is introduced into the deep gas purification device of this application to achieve efficient, rapid, and low-cost agglomeration and separation of foam-like droplets and micro-droplets.

[0081] The methods specifically include:

[0082] Oil and gas are introduced into the tank through the oil and gas inlet 1 in the middle of the tank. 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 flow to each momentum defoamer 3 on the momentum defoaming module, and defoaming is performed by the momentum defoamer 3. In the momentum defoamer 3, the gas-liquid mixture first moves vertically upward along the straight section 302. When it moves to the metal mesh 303, under the action of the metal mesh 303 and its attached barbs, the large foam droplets are broken into several small foam droplets. Under the action of the high-speed airflow, it moves into the conical section 306. The high momentum foam droplets collide with the annular baffle 304, and the liquid film is continuously broken, eventually annihilating into fine droplets. Under the entrainment of the airflow, it moves into the overflow pipe 305 and is discharged from the momentum defoamer 3.

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

[0084] After defoaming, the oil and gas flow upward through the fiber condensation module 4. The cross-fibers in the fiber condensation module 4 capture and coalesce the small droplets entrained in the airflow. When the gas enters the fiber condensation module 4, due to the significant difference in affinity between the fiber materials and the oil and gas phases, the liquid is captured by the fiber materials and remains on the material surface and in the pores, forming an oil film. When the oil film grows to a certain thickness, it falls off and merges into larger droplets under the action of gravity and other forces. This achieves the coalescence of micro-droplets into larger droplets, which are then discharged from the fiber condensation module 4 by the entrainment effect of the high-speed airflow. The remaining very small amount of incompletely treated foam droplets are also turned into micro-droplets under the shearing action of the fibers, achieving complete elimination.

[0085] The gas discharged from the fiber condensation module 4 contains only a certain amount of larger droplets.

[0086] The oil and gas then continue to flow upwards through the cyclone separation module, where high-speed rotational flow separates the entrained droplets. Within the rotary desliming module, larger droplets settle faster or are thrown off the cyclone path due to inertia compared to smaller, untreated droplets, making them easier to separate and eliminate within the cyclone core tube 6. When the gas enters the cyclone core tube 6 vertically, it is first evenly distributed into multiple streams by the core tube partition 601. Each stream, under the action of its corresponding spiral blades, forms a further vortex. A low-pressure zone is generated in the central region of the turbulent rotation, and its centrifugal field and pressure gradient field cause all the gas in the feed to converge towards the center, thus forming an air column in the center of the cyclone core tube 6. Under the superposition of the vortex field and the gravitational field, the liquid then moves towards the sidewall. When the liquid reaches a certain height, it is discharged from the core tube through the drain cavity 606 between the inner and outer sleeves, while the gas is discharged through the gas phase outlet at the top, achieving deep purification of the gas. The liquid separated from the coalescing fiber module and the rotary dehydration module is discharged into the collection area through the overflow channels 9 on both sides of the tank, and finally discharged from the separator through the liquid phase outlet 8. At the same time, the oil and gas purified by defoaming and dehydration are discharged through the gas phase outlet device at the top of the separator tank.

[0087] In the above method, the inlet flow velocity of the gas deep purification device is 3-7 m / s, the inlet liquid volume is 5-8%, and the droplet size in the gas discharged by the automatic defoaming module is generally around 0.1-70 μm. After being agglomerated by the fiber coagulation module 4, the droplet size is generally between 30-500 μm. Using the deep purification device based on momentum defoaming function of this invention, the defoaming rate can reach ≥99.9%, the size of the entrained droplets at the gas phase outlet 5 is ≤1 μm, the size of the foamy droplets is ≤10 μm, and the frequency of their occurrence is extremely low.

[0088] Comparative Example 1

[0089] A petrochemical plant uses the deep purification device based on gas momentum defoaming function as described in Example 1. The reaction environment conditions and 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-to-gas ratio 0.1 0.1 reactor pressure 3Mpa 3Mpa Volumetric flow rate <![CDATA[50m 3 / h]]> <![CDATA[50m 3 / h]]> Defoaming efficiency 65.2％ 98.7％ Average droplet size at gas exit 40μm 2.7μm Frequency of foam droplet occurrence 180 pieces / min 2 times / min

[0092] As can be seen from the data in Table 1, 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 foamy droplets is reduced to 2 per min.

[0093] Comparative Example 2

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

[0095] Table 2

[0096] Original device Example 1 reaction temperature 275 275 Liquid-to-gas ratio 0.1 0.1 reactor pressure 3Mpa 3Mpa Volumetric flow rate <![CDATA[50m 3 / h]]> <![CDATA[50m 3 / h]]> Defoaming efficiency 62.2％ 97.3％ Average droplet size at gas exit 17μm 4.2μm Frequency of foam droplet occurrence 120 pieces / min 4 times / min

[0097] As can be seen from the data in Table 2, compared with Application Example 1, the gas-liquid separation efficiency of Application Example 1 is increased 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 reduced to 4 per min, and there is no blockage in the fiber bed. The overall effect is good.

[0098] The above description is only a preferred embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any equivalent substitutions or modifications made by those skilled in the art within the scope of the technology disclosed in the present invention, based on the technical solution and inventive concept of the present invention, should be covered within the scope of protection of the present invention.

Claims

1. A deep gas purification device based on momentum defoaming, characterized in that, It includes a tank, a dynamic distributor, a momentum defoaming module with several momentum defoamers, a fiber coagulation module, and a rotary dehydration module, wherein: The tank body has an oil and gas inlet in the middle of its side wall. The oil and gas inlet is connected to the dynamic distributor via a pipeline. The dynamic distributor has a feeding chamber with multiple independent chambers. Each set of independent chambers is connected to the momentum defoamer via a distribution pipe. The momentum defoamer is a tower-shaped structure, comprising a straight cylindrical section and a conical section connected from bottom to top. The straight cylindrical section is used for initial defoaming, and the conical section is used for deep momentum defoaming. The momentum defoaming module extends from the top and consists of a fiber condensation module, a rotary desliming module, and a gas phase outlet. The rotary desliming module and the fiber condensation module are provided with overflow channels at both ends for discharging the separated liquid phase. The overflow channels are connected to the liquid collection area at the bottom of the tank. The dynamic distributor has a built-in spiral guide vane, and the momentum defoamer cone section is provided with several annular baffles.

2. The deep gas purification device based on momentum defoaming according to claim 1, characterized in that, Below the spiral guide vane are several baffles arranged at equal angles, which divide the feed chamber into multiple independent chambers. Each independent chamber is connected to the distribution pipe. The spiral angle of the spiral guide vane is 30-45°, and the number of baffles is 2-8.

3. The deep gas purification device based on momentum defoaming according to claim 1, characterized in that, The momentum defoamer has a metal mesh formed by intersecting metal wires installed inside its straight cylindrical section. The intersecting angle of the metal wires is 30-90°, and the metal mesh is covered with barbs.

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

5. The deep gas purification device based on momentum defoaming according to claim 1, characterized in that, The momentum defoaming module also includes an upper partition and a lower partition located above and below multiple momentum defoamers. The top of the conical section is connected to an overflow pipe, which passes through the upper partition.

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

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

8. A deep gas purification method based on momentum defoaming, characterized in that, The method using the deep gas purification device as described in any one of claims 1-7 comprises: S1. The oil and gas are introduced into the tank through the oil and gas inlet. 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 defoaming module, and defoaming is carried out by the momentum defoamer. S2. The defoamed oil and gas flow upward through the fiber condensation module, where the cross fibers in the fiber condensation module capture and coalesce the small droplets entrained in the airflow. S3. After aggregation, the oil and gas continue to flow upward through the rotary dehydration module, where high-speed rotational flow separates the liquid droplets entrained in the oil and gas. S4. The droplets are discharged through the draining chamber of the rotary dehydration module and flow to the liquid collection area at the bottom of the tank via the overflow channel; S5. The oil and gas, after defoaming and dehydration purification, are discharged through the gas phase outlet at the top of the separator tank.

9. The deep gas purification method based on momentum defoaming according to claim 8, characterized in that, In S1, the momentum defoamer defoaming method is as follows: the oil and gas are initially defoamed and then defoamed by momentum depth by using the metal mesh with barbs in the straight section and the annular baffle with multiple conical sections in the conical section. The oil and gas flow moves into the conical section under the action of high-speed airflow. The high momentum foam droplets in the oil and gas flow collide with the annular baffle, and the liquid film is continuously broken and eventually annihilated into fine droplets.

10. The deep gas purification method based on momentum defoaming according to claim 8, characterized in that, Both the momentum defoaming module and the rotary dehydration module are used in parallel in a uniformly distributed manner along the flow cross section of the separator, wherein: The single-unit processing capacity of the momentum defoamer is 50-500 m³. 3 / h; The single-unit processing capacity of the cyclone separator module is 100-1000m³. 3 / h.

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