CN215842036U - Separator, circulation heat exchange separation device and treatment system - Google Patents
Separator, circulation heat exchange separation device and treatment system Download PDFInfo
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- CN215842036U CN215842036U CN202121759523.6U CN202121759523U CN215842036U CN 215842036 U CN215842036 U CN 215842036U CN 202121759523 U CN202121759523 U CN 202121759523U CN 215842036 U CN215842036 U CN 215842036U
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Abstract
The utility model relates to the field of separation devices, in particular to a separator, a circulating heat exchange separation device and a treatment system. The separator comprises a shell, a separator body for separating gas and liquid from a gas-liquid mixture and a coalescer for separating a mixed liquid phase obtained by separating the gas and the liquid, wherein the coalescer and the separator body are arranged in the shell and connected with the shell, and the coalescer is communicated with a liquid phase outlet of the separator body. The separator can separate the mixed liquid phase obtained by gas-liquid separation on the basis of realizing gas-liquid separation, can obtain the liquid phase with more single component, and improves the quality of the obtained liquid phase.
Description
Technical Field
The utility model relates to the field of separation devices, in particular to a separator, a circulating heat exchange separation device and a treatment system.
Background
Fischer-Tropsch synthesis, also known as F-T synthesis, is a process for synthesizing liquid hydrocarbons or hydrocarbons (hydrocarbons) from synthesis gas (a mixed gas of carbon monoxide and hydrogen) as a raw material in the presence of a catalyst and under appropriate conditions. In the prior art, heavy oil is separated from a gas phase at an outlet of a Fischer-Tropsch synthesis reactor in a circulating heat exchange separator, and the heavy oil is directly heated by a heavy oil heater, then sent to a stripping tower and sent to a processing workshop. The production process has the problems that the heavy oil separated by the circulating heat exchange separator is entrained with the catalyst and the medium-temperature synthetic water, so that the heavy oil heater is frequently blocked, the qualified delivered heavy oil is brought with water after the heating effect of the heavy oil heater is deteriorated, the heavy oil heater is difficult and frequent to overhaul, and certain hidden troubles exist.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a separator, a circulating heat exchange separation device and a treatment system, wherein the separator can separate a mixed liquid phase obtained by gas-liquid separation on the basis of realizing gas-liquid separation, can obtain a liquid phase with a single component, and can improve the quality of the obtained liquid phase.
The embodiment of the utility model is realized by the following steps:
in a first aspect, the present invention provides a separator for gas-liquid separation, including a housing, a separator body for gas-liquid separation of a gas-liquid mixture, and a coalescer for separating a mixed liquid phase obtained by gas-liquid separation, wherein both the coalescer and the separator body are disposed in the housing and connected to the housing, and the coalescer is communicated with a liquid phase outlet of the separator body.
In an alternative embodiment, the separator includes an accumulation plate that accumulates a mixed liquid phase obtained by gas-liquid separation, the accumulation plate being provided between the coalescer and the liquid phase outlet of the separator body, the accumulation plate being connected to the casing, and a flow passage that communicates the liquid phase to the coalescer being provided between the accumulation plate and the casing.
In an alternative embodiment, the coalescer includes perforated plate and multiunit coalescence subassembly, perforated plate and the above-mentioned coalescence subassembly of multiunit all set up in the casing, and with the casing is connected, perforated plate and multiunit coalescence subassembly are followed the direction of flowing through of mixed liquid phase sets up, makes mixed liquid phase passes through in proper order perforated plate and multiunit coalescence subassembly realizes the liquid-liquid separation.
In an alternative embodiment, a plurality of the coalescing assemblies described above are arranged in a matrix.
In the optional embodiment, every group the coalescence-assembly all includes the polylith coalescence-plate, the polylith the coalescence-plate all set up in the casing, and with the casing is connected, 0 degree < every coalescence-plate with the contained angle between the perforated plate is less than or equal to 90 degrees.
In an alternative embodiment, the shell is provided with a first liquid phase outlet and a second liquid phase outlet, and the height of the first liquid phase outlet from the ground is relatively higher than that of the second liquid phase outlet from the ground in the vertical direction;
and the separator also comprises a boundary meter for controlling the extraction amount of the first liquid phase and the second liquid phase, and the boundary meter is arranged in the shell and is connected with the side wall of the shell.
In a second aspect, the utility model provides a circulating heat exchange separation device, which comprises a heat exchanger and the separator for gas-liquid separation described in any one of the foregoing embodiments, wherein the heat exchanger is connected with the shell and is communicated with the feed inlet of the separator body.
In a third aspect, the utility model provides a treatment system for a fischer-tropsch synthesis product, which comprises a treatment component for medium-temperature synthesis water and the circulating heat exchange separation device of the foregoing embodiment, wherein the circulating heat exchange separation device is connected with the treatment component.
In an alternative embodiment, the treatment assembly comprises a filter and a cooler, the second liquid phase outlet of the circulating heat and exchange separation device is connected with the inlet of the filter, and the outlet of the filter is connected with the inlet of the cooler.
In an alternative embodiment, the treatment system further comprises a heavy oil post-treatment assembly connected to the first liquid phase outlet of the cyclic heat exchange separation device.
The embodiment of the utility model has the beneficial effects that: this embodiment realizes the gas-liquid separation of basis through setting up the separator body, then recycles the coalescer and separates the mixed liquid phase that gas-liquid separation obtained, then can obtain the more single liquid phase of composition, more is favorable to the recovery of liquid, simultaneously, improves the frequent trouble of follow-up equipment that the mixed liquid phase that directly retrieves gas-liquid separation and obtain leads to, quality and does not accord with the scheduling problem.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.
FIG. 1 is a schematic structural view of a separator provided in example 1 of the present invention;
FIG. 2 is a schematic structural view of a coalescer according to example 1 of the present invention;
FIG. 3 is a schematic structural diagram of a circulating heat exchange separation device provided in embodiment 2 of the present invention;
fig. 4 is a schematic structural diagram of a processing system according to embodiment 2 of the present invention.
100-separator; 110-a housing; 111-gas phase outlet; 112-a first liquid phase outlet; 113-a second liquid phase outlet; 120-a separator body; 130-an accumulation plate; 131-a flow channel; 140-a coalescer; 141-a bracket; 142-an expanded pore plate; 143-a coalescing assembly; 144-coalescing plates; 150-a settling zone; 160-interface level meter; 200-a circulating heat exchange separation device; 210-a heat exchanger; 300-a processing system; 310-a processing component; 311-a filter; 312-a cooler; 320-a post-processing component; 321-a heavy oil heater; 322-a stripping column; 330-a deep processing component; 331-an air cooling device; 332-light oil separator; 333-oil water separator; 334-liquid separation tank; 335-a compressor; 340-reactor.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. The components of embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the present invention, presented in the figures, is not intended to limit the scope of the utility model, as claimed, but is merely representative of selected embodiments of the utility model. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings or orientations or positional relationships that the products of the present invention are conventionally placed in use, and are only for convenience of describing the present invention and simplifying the description, but do not indicate or imply that the device or element to which the description refers must have a specific orientation, be constructed in a specific orientation, and be operated, and thus should not be construed as limiting the present invention. Furthermore, the terms "first," "second," "third," and the like are used solely to distinguish one from another and are not to be construed as indicating or implying relative importance.
Furthermore, the terms "horizontal", "vertical" and the like do not imply that the components are required to be absolutely horizontal or pendant, but rather may be slightly inclined. For example, "horizontal" merely means that the direction is more horizontal than "vertical" and does not mean that the structure must be perfectly horizontal, but may be slightly inclined.
In the description of the present invention, it should also be noted that, unless otherwise explicitly specified or limited, the terms "disposed," "mounted," "connected," and "connected" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Example 1
Referring to fig. 1, the present embodiment provides a separator 100 for gas-liquid separation, which includes a housing 110, wherein the housing 110 provides a necessary space for installing the rest of the components. The housing 110 has a vertical structure, but may have a horizontal structure, but the present embodiment will be described by taking a vertical structure as an example. Specifically, one end of the casing 110 relatively close to the ground is a bottom, the other end of the casing 110 opposite to the bottom is a top, the casing 110 is provided with a gas phase outlet 111, a first liquid phase outlet 112 and a second liquid phase outlet 113, in the vertical direction, the height from the gas phase outlet 111 to the ground is relatively higher than the height from the first liquid phase outlet 112 to the ground, and the height from the first liquid phase outlet 112 to the ground is relatively higher than the height from the second liquid phase outlet 113 to the ground; i.e., the gas phase outlet 111, the first liquid phase outlet 112, and the second liquid phase outlet 113 are sequentially disposed in a top-to-bottom direction of the housing 110. The gas phase outlet 111 is configured to output a gas phase obtained by gas-liquid separation, the first liquid phase outlet 112 is configured to output a liquid with a relatively low density in the mixed liquid phase obtained by gas-liquid separation (for example, heavy oil in fischer-tropsch synthesis), and the second liquid phase outlet 113 is configured to output a liquid with a relatively high density in the mixed liquid phase obtained by gas-liquid separation (for example, medium temperature synthesis water in fischer-tropsch synthesis).
Further, the separator 100 includes a separator body 120 for separating a gas-liquid mixture from a liquid mixture, and the separator bodies 120 are disposed in the casing 110 and connected to the casing 110. The gas outlet of the separator body 120 is communicated with the gas phase outlet 111 of the casing 110, that is, the gas separated by the separator body 120 flows out of the separator 100 through the gas phase outlet 111 of the casing 110, and the mixed liquid phase separated by the separator body 120 falls into the casing 110, and then the mixed liquid phase is further separated.
The separator body 120 may adopt a cyclone separator or other separators capable of separating gas and liquid in the prior art, and the number of the separator bodies 120 may be more than 1, 2, 3, 4, etc., as long as the gas outlets of the separator bodies 120 are all communicated with the gas phase outlet 111 of the casing 110. In this embodiment, the separator body 120 includes 4 cyclones, and 4 cyclones set up side by side, and 4 cyclones's gas outlet all communicates with the gaseous phase export 111 of casing, and the cyclone is vertical to be placed, and its liquid phase export faces downwards.
Further, the separator 100 includes an accumulation plate 130 for accumulating the mixed liquid phase obtained by the gas-liquid separation, that is, the mixed liquid phase obtained by the separation by the separator body 120 is accumulated on the accumulation plate 130 and then further separated. Specifically, the accumulation plate 130 is disposed between the coalescer 140 and the liquid phase outlet of the separator body 120, and the accumulation plate 130 is disposed in the casing 110 and connected to the casing 110, that is, the accumulation plate 130 is disposed below the liquid phase outlet of the separator body 120, and then the mixed liquid phase separated by the separator body 120 directly falls on the accumulation plate 130 to be accumulated, and then the subsequent separation is performed.
Further, a flow passage 131 is provided between the accumulator plate 130 and the housing 110 for communicating the liquid phase to the coalescer 140. That is, the area of the cross section of the accumulation plate 130 is smaller than that of the cross section of the casing 110, and one end of the accumulation plate 130 is not connected to the casing 110, and the remaining part of the accumulation plate 130 is connected to the casing 110, and then the flow channel 131 is formed only when the accumulation plate 130 is connected to the casing 110, so that the mixed liquid phase can be directed to flow to the separation means where the phase separation of the mixed liquid is achieved, and the mixed liquid phase is prevented from being directly discharged without passing through the separation means where the phase separation of the mixed liquid is achieved.
Further, referring to fig. 2, the separation device includes a coalescer 140 for separating the mixed liquid phase obtained by gas-liquid separation, the coalescer 140 is disposed in the housing 110 and connected to the housing 110, the coalescer 140 is communicated with the liquid phase outlet of the separator body 120, and then the mixed liquid phase obtained by separation through the separator body 120 can be further separated by the coalescer 140 to obtain a liquid with a more uniform composition.
Specifically, the coalescer 140 includes a support 141, a reaming plate 142 and a plurality of sets of coalescing assemblies 143, the support 141 is disposed in the housing 110 and connected to the housing 110, the support 141 is used for accommodating the plurality of sets of coalescing assemblies 143, so as to fix the coalescing assemblies 143, the coalescing assemblies 143 are arranged in a matrix, so as to increase the throughput of the mixed liquid phase and facilitate accelerating the separation of the mixed liquid phase. The perforated plate and the plurality of groups of coalescing assemblies 143 are arranged along the flow direction of the mixed liquid phase, so that the liquid phase sequentially passes through the perforated plate and the plurality of groups of coalescing assemblies 143 to realize liquid-liquid separation.
Specifically, the perforated plate can be inclined relative to the horizontal plane, as long as it is not completely parallel to the horizontal plane, and is preferably arranged vertically relative to the horizontal plane, so that the action effect of the perforated plate and the mixed liquid phase can be ensured. And the number of perforated plates can be a plurality of, also can be 1, if be a plurality of, can parallel arrangement each other between the perforated plate, do not carry on one's things each other, as long as do not mutually perpendicular can, preferably parallel each other between the perforated plate. The mixed liquid phase is dispersed into the various coalescing assemblies 143 after passing through the perforated plate, and further separation is achieved.
Further, each set of the coalescing assembly 143 includes a plurality of coalescing plates 144, each coalescing plate 144 is connected to the bracket 141, and then connected to the housing 110, and a certain included angle is formed between each coalescing plate 144 and the porous plate, the included angle is greater than 0 degree and less than or equal to 90 degrees, so that the coalescing plates 144 are arranged to enable the mixed liquid phase passing through the porous plate to act on the coalescing plates 144, which is beneficial to the liquid phase separation of different densities in the mixed liquid phase. The coalescing plate 144 is a metal sheet made of alloy or metal, or a thin plate made of other materials.
Further, the separator 100 further includes a level gauge 160 for controlling the amount of the first liquid phase and the second liquid phase drawn out, wherein the level gauge 160 is disposed in the housing 110 and connected to a sidewall of the housing 110. The level gauge 160 is disposed in the settling zone 150, which in turn facilitates control of the outflow of liquid.
Example 2
Referring to fig. 3, the present embodiment provides a cyclic heat exchange separation device 200, which includes a heat exchanger 210 and the separator 100 for gas-liquid separation of embodiment 1, wherein the heat exchanger 210 is connected to the shell 110 and is communicated with the feed inlet of the separator body 120. Namely, the gas-liquid mixture after heat exchange enters the separator body 120 for gas-liquid separation, and then the mixed liquid phase obtained by gas-liquid separation is separated by the coalescer 140.
Referring to fig. 4, the present embodiment further provides a fischer-tropsch synthesis product processing system 300, which includes a medium temperature synthesis water processing assembly 310 and the above-mentioned circulating heat exchange separation device 200, wherein the circulating heat exchange separation device 200 is connected to the processing assembly 310. Namely, the second liquid phase outlet 113, namely the medium temperature synthetic water outlet, of the circulating heat exchange and separation device 200 is connected with the treatment component 310.
In the embodiment, the coalescer 140 is arranged in the circulating heat exchange separation device 200 to separate the heavy oil, the medium-temperature synthetic water and the catalyst through density difference, so that the separated heavy oil does not contain the medium-temperature synthetic water and the catalyst, the frequent blockage problem of a heavy oil heater is further relieved, and the quality of the formed heavy oil is ensured. Meanwhile, the problems that the temperature of the stripping tower is low and the service life of the processed catalyst is influenced by the fact that qualified heavy oil carries water when the heavy oil carries water are solved.
Meanwhile, two different liquid phase outlets are arranged in the circulating heat exchange separation device 200, the first liquid phase outlet 112 is a heavy oil outlet, and the second liquid phase outlet 113 is a medium temperature synthetic water outlet, so that the problem of oil-water separation in the circulating heat exchange separator 100 is solved.
Specifically, the processing assembly 310 comprises a filter 311 and a cooler 312, the second liquid phase outlet 113 of the cyclic heat exchange separation device 200 is connected with an inlet of the filter 311, and an outlet of the filter 311 is connected with an inlet of the cooler 312. The problem of blockage of the heavy oil heater 321 caused by heavy oil entrained catalyst is further improved by arranging the filter 311 to filter the catalyst entrained in the medium-temperature synthetic water.
The filter 311 may be a bag filter or other filter. Similarly, cooler 312 is also a commercially available cooler.
Further, the treatment system 300 further comprises a heavy oil post-treatment assembly 320, and the post-treatment assembly 320 is connected with the first liquid phase outlet 112 of the circulating heat exchange separation device 200.
Specifically, the post-treatment assembly 320 includes a heavy oil heater 321 and a stripper 322, an inlet of the heavy oil heater 321 is connected to the first liquid phase outlet 112, i.e., a heavy oil outlet, and an outlet of the heavy oil heater 321 is communicated with an inlet of the stripper 322.
The treatment system 300 further comprises an advanced treatment assembly 330 for advanced treatment of the gas phase obtained by gas-liquid separation, the advanced treatment assembly 330 is communicated with a gas outlet of the separator body 120, the advanced treatment assembly 330 comprises an air cooling device 331, a light oil separator 332 and an oil-water separator 333, a gas outlet of the separator body 120 is communicated with an inlet of the air cooling device 331, an outlet of the air cooling device 331 is communicated with an inlet of the light oil separator 332, a liquid outlet of the light oil separator 332 is communicated with an inlet of the oil-water separator 333, a water phase outlet of the oil-water separator 333 is connected with a water pump to convey water to a water storage area, and an oil phase outlet of the oil-water separator 333 is connected with an oil pump to convey light oil to a light oil storage area. Meanwhile, the medium-temperature synthetic water cooled by the cooler 312 is also conveyed into the oil-water separator 333 or conveyed to the water storage area by a water pump.
The deep treatment component 330 comprises a liquid separating tank 334 and a compressor 335, the gas phase outlet 111 of the light oil separator 332 is communicated with the liquid separating tank 334, the liquid outlet of the liquid separating tank 334 is connected with the oil-water separator 333, the gas outlet of the liquid separating tank 334 is connected with the compressor 335, and the compressor 335 is connected with the heat exchanger 210 of the circulating heat exchange separation device 200.
The treatment system 300 further comprises a reactor 340, and the reactor 340 is connected with the heat exchanger 210 of the circulating heat exchange separation device 200.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The separator for gas-liquid separation is characterized by comprising a shell, a separator body for performing gas-liquid separation on a gas-liquid mixture and a coalescer for separating a mixed liquid phase obtained by gas-liquid separation again, wherein the coalescer and the separator body are arranged in the shell and connected with the shell, and the coalescer is communicated with a liquid phase outlet of the separator body.
2. The separator for gas-liquid separation according to claim 1, comprising an accumulation plate that accumulates a mixed liquid phase resulting from gas-liquid separation, the accumulation plate being provided between the coalescer and a liquid phase outlet of the separator body, the accumulation plate being connected to the housing, the accumulation plate and the housing having a flow passage therebetween that communicates the liquid phase to the coalescer.
3. The separator according to claim 2, wherein the coalescer includes a perforated plate and a plurality of sets of coalescing assemblies, the perforated plate and the plurality of sets of coalescing assemblies being disposed in the housing and connected to the housing, the perforated plate and the plurality of sets of coalescing assemblies being disposed along a flow direction of the mixed liquid phase, such that the mixed liquid phase sequentially passes through the perforated plate and the plurality of sets of coalescing assemblies to achieve liquid-liquid separation.
4. The separator for gas-liquid separation according to claim 3, wherein a plurality of the coalescing modules are arranged in a matrix.
5. The separator of claim 3, wherein each group of coalescer assemblies comprises a plurality of coalescer plates disposed in the housing and connected thereto, and wherein 0 degrees < the angle between each coalescer plate and the porous plate is 90 degrees or less.
6. The separator for gas-liquid separation according to claim 3, wherein a first liquid phase outlet and a second liquid phase outlet are provided on the housing, and a height of the first liquid phase outlet from the ground is relatively higher than a height of the second liquid phase outlet from the ground in a vertical direction;
and the separator also comprises a boundary meter for controlling the extraction amount of the first liquid phase and the second liquid phase, and the boundary meter is arranged in the shell and is connected with the side wall of the shell.
7. A circulating heat exchange separation device, which is characterized by comprising a heat exchanger and the separator for gas-liquid separation as recited in any one of claims 1 to 6, wherein the heat exchanger is connected with a shell and is communicated with a feed inlet of a separator body.
8. A Fischer-Tropsch synthesis product treatment system, characterized by comprising a medium-temperature synthesis water treatment component and the circulating heat exchange separation device of claim 7, wherein the circulating heat exchange separation device is connected with the treatment component.
9. A Fischer-Tropsch synthesis product processing system according to claim 8, wherein the processing assembly comprises a filter and a cooler, the second liquid phase outlet of the cyclical heat exchange and separation device is connected to an inlet of the filter, and an outlet of the filter is connected to an inlet of the cooler.
10. A Fischer-Tropsch synthesis product processing system according to claim 8, further comprising a heavy oil post-processing assembly, the post-processing assembly being connected to the first liquid phase outlet of the cyclical heat exchange separation device.
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| CN202121759523.6U CN215842036U (en) | 2021-07-30 | 2021-07-30 | Separator, circulation heat exchange separation device and treatment system |
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| CN202121759523.6U CN215842036U (en) | 2021-07-30 | 2021-07-30 | Separator, circulation heat exchange separation device and treatment system |
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