TWM655666U - Mechanical vapor recompression system - Google Patents

Abstract

An embodiment of the present invention provides a mechanical vapor recompression system, which includes a distillation gas-water separation barrel, a gas compressor, a water mist elimination barrel, a main heat exchanger, a waste liquid preheating barrel, and a branch manifold. The mist elimination barrel is fluidly connected between the distillation gas-water separation barrel and the gas compressor, and is used to eliminate a mist from the distillation gas-water separation barrel. The waste liquid preheating barrel includes two regions for containing condensed water and waste liquid. The waste liquid in the waste liquid preheating barrel is heated by the heat energy of the condensed water before its supply to the main heat exchanger. The branch manifold is fluidly connected between the main heat exchanger and the distillation gas-water separation barrel, and is used to separate the steam from the waste liquid.

Description

Mechanical vapor recompression system

The disclosed embodiments relate to a mechanical vapor recompression system, and more particularly to a mechanical vapor recompression system having the characteristic of reducing energy consumption.

As environmental regulations become increasingly stringent, manufacturers are required to upgrade their in-plant water treatment equipment to reduce the total amount of wastewater discharged or even completely avoid wastewater discharge. On the other hand, in order to reduce greenhouse gas emissions and achieve the goal of reducing carbon footprint, manufacturers are also expected to abandon the traditional fossil fuel as an energy source for the above water treatment process and use renewable electricity instead.

Although traditional distillation equipment can reduce wastewater concentration, it consumes a lot of energy. The higher the boiling point of wastewater, the more energy is needed to evaporate it. However, if the boiling point and pressure of wastewater are not increased in order to reduce energy consumption, the boiling liquid will vaporize in the pipeline early, generating water mist and crystals, which will block the pipeline and affect the distillation efficiency.

Mechanical Vapor Recompression System (MVR System) provides a solution for traditional distillation equipment. It returns the heat energy from the steam compressor to produce more steam to reduce energy demand. Manufacturers can use MVR system to treat or recycle industrial high-concentration wastewater (such as nitrate nitrogen) at a lower cost, or use MVR system to desalinate seawater to provide increasingly scarce water resources.

However, in the traditional MVR system, wastewater will generate a large number of floating small water droplets and water mist in the separator. Small water droplets and water mist will form a large number of crystals in the pipeline and steam compressor, causing abnormal operation of the steam compressor. For this reason, the operator needs to shut down the steam compressor frequently for maintenance and cleaning to avoid steam compressor failure and prolongation. This is not only not conducive to improving the efficiency of wastewater treatment, but also increases the operating cost of wastewater treatment. Although reducing the concentration ratio can avoid water mist, it is also not conducive to improving the treatment efficiency.

In view of the shortcomings of the traditional MVR system, the disclosed embodiment proposes a new MVR system, which has at least the advantages of low energy consumption, high durability, high utilization rate, and low maintenance rate compared to the traditional MVR system.

According to an embodiment of the present disclosure, the MVR system includes a distillation gas separation barrel; a gas compressor configured to compress a steam from the distillation gas separation barrel; a water mist elimination barrel, which is fluidly connected between the distillation gas separation barrel and the gas compressor and is configured to eliminate a water mist from the distillation gas separation barrel; a main heat exchanger, which is configured to heat waste water from a waste water source by the pressurized steam from the gas compressor; a waste liquid preheating barrel, which includes a storage barrel and a heat conductive spacer disposed in the storage barrel, the heat conductive spacer The container is divided into at least a first area and a second area, the first area is fluidly connected between the wastewater source and the main heat exchanger and is configured to accommodate the wastewater, the second area is fluidly connected between the main heat exchanger and a drain and is configured to accommodate the condensate generated by the condensation of the steam from the main heat exchanger; and a branch manifold, which includes an inlet pipe fluidly connected to the main heat exchanger and a first outlet pipe and a second outlet pipe connected to the inlet pipe and fluidly connected to different height positions of the distilled gas-water separation barrel.

According to another embodiment of the present disclosure, the MVR system includes a distillation gas separation barrel; a gas compressor configured to compress a steam from the distillation gas separation barrel; a primary heat exchanger configured to heat wastewater from a wastewater source by the pressurized steam from the gas compressor; a waste liquid preheating barrel including a containing barrel and a heat conductive partition disposed in the containing barrel, the heat conductive partition dividing the containing barrel into at least a first area and a second area. The first zone fluid is connected between the wastewater source and the main heat exchanger and is configured to accommodate the wastewater, the second zone fluid is connected between the main heat exchanger and a drain and is configured to accommodate the condensate generated by the condensation of the steam in the main heat exchanger; a heating pipe, whose fluid is connected between the main heat exchanger and the distillation gas-water separation barrel and is configured to heat the wastewater from the main heat exchanger; and a heat source, which is connected to the heating pipe.

According to another embodiment of the present disclosure, the MVR system includes a distillation gas-water separation drum; a gas compressor configured to compress a steam from the distillation gas-water separation drum; a water mist elimination drum, which is fluidly connected between the distillation gas-water separation drum and the gas compressor and is configured to eliminate a water mist from the distillation gas-water separation drum; a primary heat exchanger, which is configured to heat wastewater from a wastewater source by the pressurized steam from the gas compressor; and a secondary heat exchanger, which is fluidly connected to the primary heat exchanger and is configured to allow wastewater supplied to the primary heat exchanger to exchange heat with condensate from the primary heat exchanger.

1, 1a, 1b: Mechanical vapor recompression system

21: Secondary heat exchanger

23: Main heat exchanger

25: Heating pipe

30, 30a, 30b: Waste liquid preheating barrel

31, 31a, 31b: Body

32, 32a, 32b: Thermally conductive spacers

33, 33a, 33b: First area

34, 34a, 34b: Second area

35a: Thermally conductive spacer

40, 40a, 40b: bifurcated manifolds

41, 41a, 41b: First outlet pipe

42, 42a, 42b: Second outlet pipe

43, 43a, 43b: Inlet pipe

50, 50a, 50b: Distillation gas-water separation barrel

51:Entity

54: Connecting tube

55: Storage slot

56, 57: Viewing window

60: Water mist elimination bucket

61:Entity

64: Grid

65: Ring packing

66: Channel

67: Spacer

70: Gas compressor

81: Sources of wastewater

82: Heat source

83: Dryer

84: Condensate storage tank

90: Control equipment

91, 92, 94, 95: Pump

93: Valve

101, 102, 103, 104, 105, 106, 107, 108, 109: pipelines

110, 111, 112, 113, 114, 115, 116, 117, 118, 119: pipelines

510: Bottom

511: Top

512: Side wall

521: First entrance port

522: Second entrance port

523: Export port

550: Bottom

551: Top

552: discharge hole

610: Bottom

611: Top

612: Side

621: Entry Port

622: Export port

623: Drainage outlet

631, 632, 633, 634, 635: Grid panels

651: Ring-shaped body

652: Gap

653:Leaves

6310, 6320: Perforation

6315, 6325, 6335, 6345, 6355: Opening

a1: First angle

a2: Second angle

CL: concentrated waste liquid

D1: Spacing

G1: Heating steam

H1, H2, H3: Height difference

HG: High pressure steam

L1, L2, L3, L4, L5: condensate

LV: Height line

T0, T1, T2, T4: long axis

W0, W1, W2, W3, W4, W10, W11: Wastewater

W5, W8, W9, W13: Steam

W6, W7, W12: compound airflow

The embodiments of the present disclosure are best understood by reading the following [Implementation Method] in conjunction with the drawings. It should be noted that, in accordance with standard industry practice, the various structures are not drawn to scale. In fact, the sizes of the various structures may be arbitrarily increased or decreased for clarity of discussion.

FIG1 shows a schematic diagram of a mechanical vapor recompression system according to a first embodiment of the present disclosure.

Figures 2A, 2B, and 2C show top views of the waste liquid preheating barrel according to some embodiments of the present disclosure.

FIG. 3A is a schematic diagram showing some components of a mechanical vapor recompression system according to some embodiments of the present disclosure.

FIG3B shows a schematic diagram of a bifurcated manifold according to some embodiments of the present disclosure.

FIG3C shows a schematic diagram of a bifurcated manifold according to some embodiments of the present disclosure.

FIG4 shows a schematic diagram of a distillation gas-water separation barrel according to some embodiments of the present disclosure.

FIG5 shows a schematic cross-sectional view of a distillation gas-water separation barrel according to some embodiments of the present disclosure.

FIG6A shows a schematic diagram of a heating tube according to some embodiments of the present disclosure.

FIG6B shows a schematic cross-sectional view of a heating tube according to some embodiments of the present disclosure.

FIG7 shows a schematic cross-sectional view of a water mist elimination barrel according to some embodiments of the present disclosure.

FIG8 shows a schematic cross-sectional view of a plurality of grid plates according to some embodiments of the present disclosure.

FIG9 shows a schematic diagram of a Bower ring according to some embodiments of the present disclosure.

FIG10 shows a schematic diagram of a mechanical vapor recompression system according to a second embodiment of the present disclosure.

FIG11 shows a schematic diagram of a mechanical vapor recompression system according to a third embodiment of the present disclosure.

The following disclosure provides a number of different embodiments or examples for implementing different features of the subject matter provided. Specific examples of components and configurations will be described below to simplify the disclosure. Of course, these are merely examples and are not intended to be limiting. For example, in the following description, forming a first component above or on a second component may include embodiments in which the first component and the second component are formed in direct contact, and may also include embodiments in which additional components may be formed between the first component and the second component so that the first component and the second component may not be in direct contact. In addition, the disclosure may repeat component symbols and/or letters in various examples. This repetition is for simplicity and clarity and does not in itself indicate a relationship between the various embodiments and/or configurations discussed.

Additionally, for ease of description, spatially relative terms (such as "below," "beneath," "below," "above," "over," "on," "on," and the like) may be used herein to describe the relationship of one element or component to another element or components, as depicted in the figures. Spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. The device may be oriented in other ways (rotated 90 degrees or in other orientations), and the spatially relative descriptors used herein may be interpreted accordingly.

As used herein, terms such as "first", "second", and "third" describe various elements, components, regions, layers, and/or sections, which should not be limited by these terms. These terms may only be used to distinguish elements, components, regions, layers, or sections from each other. Unless the context clearly indicates otherwise, terms such as "first", "second", and "third" used herein do not imply a sequence or order.

As used herein, the terms "approximately," "substantially," "substantial," and "about" are used to describe and take into account small variations. When used in conjunction with an event or circumstance, the terms may refer to instances where the event or circumstance occurred exactly as well as instances where the event or circumstance occurred very approximately.

As used herein, the terms "pipeline", "tubing", "flow channel" and "conduit" are used interchangeably and refer to any type, size or configuration of flow conduits commonly used in the art for transporting liquid and/or gaseous materials and combinations thereof.

FIG1 shows a schematic diagram of a mechanical vapor recompression system 1 according to a partial embodiment of the present disclosure. The mechanical vapor recompression system 1 includes a secondary heat exchanger 21, a main heat exchanger 23, a heating pipe 25, a waste liquid preheating barrel 30, a branching manifold 40, a distillation gas-water separation barrel 50, a water mist elimination barrel 60, a gas compressor 70 and a control device 90. The components of the mechanical vapor recompression system 1 can be increased or decreased according to demand, and are not limited to the embodiment shown in FIG1.

The secondary heat exchanger 21, the primary heat exchanger 23 and the waste liquid preheating drum 30 are configured to heat the waste liquid from a waste liquid source 81 so that the waste liquid becomes boiling when entering the distillation gas-water separation drum 50. In an exemplary embodiment, the waste liquid source 81 is a scrubber for cleaning combustion exhaust gas. The waste liquid W0 from the scrubber can first be removed from heavy metal impurities by a heavy metal filter, and then transported to the secondary heat exchanger 21 through a pipeline 101 and a pump 91 (e.g., an electric pump).

The step of heating the waste liquid by using the secondary heat exchanger 21, the primary heat exchanger 23 and the waste liquid preheating barrel 30 includes: (1) heating the waste liquid W0 in the secondary heat exchanger 21 by using the heat energy of the condensate L2 from the waste liquid preheating barrel 30 to make it into waste liquid W1 having a first elevated temperature (e.g., 60-98°C, the value of the end point of the interval will change with the operating pressure); (2) supplying the waste liquid W1 to the waste liquid preheating barrel 30 through the pipeline 102, and heating it by using the heat energy of the condensate L1 contained in the waste liquid preheating barrel 30 to make it into a waste liquid W1 having a second elevated temperature. (3) supplying the waste liquid W2 from the waste liquid preheating drum 30 to the main heat exchanger 23 through the pipeline 103 and the pump 92 (e.g., pneumatic pump), and heating it by the heat energy of the high-pressure steam HG in the main heat exchanger 23 to become the (steam-containing) waste liquid W3 with a boiling temperature (e.g., 62~130℃, the value of the end point of the interval will change with the operating pressure), so as to facilitate the separation of the steam therein from the waste liquid in the distillation gas-water separation drum 50.

In some embodiments, as shown in FIG. 1 , the waste liquid preheating barrel 30 includes a hollow storage barrel 31 and a heat conductive spacer 32. The heat conductive spacer 32 can be made of a material with a high thermal conductivity coefficient (e.g., aluminum). The heat conductive spacer 32 is disposed in the storage barrel 31 and extends vertically from the top surface 311 of the storage barrel 31 to the bottom surface 310 of the storage barrel 31 to divide the storage barrel 31 into a first area 33 and a second area 34. The first area 33 and the second area 34 are independent of each other and are not connected to each other.

One end of the first region 33 relative to the top surface 311 of the storage barrel 31 is connected to the secondary heat exchanger 21 through the pipeline 102. One end of the first region 33 relative to the bottom surface 310 of the storage barrel 31 is connected to the main heat exchanger 23 through the pipeline 103. One end of the second region 34 relative to the top surface 311 of the storage barrel 31 is connected to the main heat exchanger 23 through the pipeline. One end of the second region 34 relative to the bottom surface 310 of the storage barrel 31 is connected to the secondary heat exchanger 21 through the pipeline 111. When the mechanical vapor recompression system 1 is in operation, the waste liquid W1 from the secondary heat exchanger 21 and the condensate L1 from the main heat exchanger 23 are respectively supplied to the first region 33 and the second region 34, and heat exchange is performed through the heat conductive spacer 32. In this way, the heat energy of the condensate L1 will be further utilized, thereby reducing the energy required to heat the waste liquid W1.

In some embodiments, the waste liquid and condensate stored in the waste liquid preheating barrel 30 are supplied to the waste liquid preheating barrel 30 at a fixed flow rate and discharged from the waste liquid preheating barrel 30 at a fixed flow rate (i.e., the waste liquid and condensate are not statically stored in the waste liquid preheating barrel 30). In other embodiments, the waste liquid and condensate supplied into the waste liquid preheating barrel 30 are statically stored in the waste liquid preheating barrel 30 for a predetermined time, and are discharged from the waste liquid preheating barrel 30 after the predetermined time. The above flow rate can be calculated based on parameters such as the temperature of the condensate, the temperature of the waste liquid, the volume of the waste liquid preheating barrel 30, and the heat transfer efficiency of the heat conductive spacer 32. In some embodiments, the secondary heat exchanger 21 is omitted, and the waste liquid reaches a desired temperature by heat exchange with the condensate in the waste liquid preheating barrel 30.

In some embodiments, as shown in FIG. 2A , a heat conductive spacer 32 is disposed at the center of the storage barrel 31 of the waste liquid preheating barrel 30 to equally separate the first area 33 and the second area 34. However, the configuration of the waste liquid preheating barrel is not limited to this, and the heat conductive spacer can be disposed in the hollow body in other ways. For example, as shown in FIG. 2B , the waste liquid preheating barrel 30a includes a storage barrel 31a and two heat conductive spacers 32a and 35a. The heat conductive spacers 32a and 35a are located in the storage barrel 31a and are disposed perpendicularly to each other to separate the two first areas 33a and the two second areas 34a. In the circumferential direction of the storage barrel 31a, the first area 33a and the second area 34a are disposed alternately. Alternatively, as shown in FIG. 2C , the waste liquid preheating barrel 30b includes a containing barrel 31b and an annular heat-conducting spacer 32b. The heat-conducting spacer 32b is concentrically disposed in the containing barrel 31b to separate a first area 33b and a second area 34b. The second area 34b is located at the center of the containing barrel 31b, and the first area 33b is annularly disposed around the second area 34b.

The cross-section of the spacers in the above-mentioned embodiments may be wavy, sawtooth, or fin-shaped to increase the contact area between the spacers and the liquid, thereby improving the heat exchange efficiency. The spacers may be made of materials with high heat conductivity and corrosion resistance to the waste liquid to be received (e.g., steel-aluminum composite plates) to increase the service life of the spacers.

In a conventional MVR system, the waste liquid passing through the secondary heat exchanger 21 and the condensate from the primary heat exchanger 23 are stored in two barrels for subsequent processing. Since the two barrels are separated, the temperature of the waste liquid and the condensate will decrease with the increase of storage time, which is not conducive to heat recovery. Compared with the design of the conventional MVR system, the waste liquid preheating barrel 30 of the disclosed embodiment can fully recover the heat energy of the condensate to heat the waste liquid, so as to reduce the heat loss caused by heating the waste liquid in the primary heat exchanger. In addition, compared with the conventional two-barrel configuration, the waste liquid preheating barrel 30 of the disclosed embodiment has the advantage of reducing the equipment usage area.

Referring again to FIG. 1 , in some embodiments, the waste liquid W3 passing through the main heat exchanger 23 enters the distillation gas-water separation barrel 50 through the bifurcated manifold 40. In some embodiments, the bifurcated manifold 40 includes a first outlet pipe 41, a second outlet pipe 42, and an inlet pipe 43. One end of the inlet pipe 43 is fluidly connected to the outlet of the main heat exchanger, and the other end of the inlet pipe 43 is coupled to the first outlet pipe 41 and the second outlet pipe 42. The opposite ends of the first outlet pipe 41 and the second outlet pipe 42 connected to the inlet pipe 43 are fluidly connected to the first inlet port 521 and the second inlet port 522 located at different heights on the distillation gas-water separation barrel 50, respectively. In some embodiments, as shown in FIG. 3A , the bifurcated manifold 40 has a substantially Y-shaped structure, wherein the long axis T1 of the first outlet pipe 41 and the long axis T0 of the inlet pipe 43 are arranged at a first angle a1, and the long axis T2 of the second outlet pipe 42 and the long axis T0 of the inlet pipe 43 are arranged at a second angle a2. However, it should be understood that many variations and modifications may be made to the embodiments disclosed herein. In some other embodiments, as shown in FIG. 3B , the second outlet pipe 42a of the bifurcated manifold 40a is not directly coupled to the inlet pipe 43a, but is coupled to the upper side of the first outlet pipe 41a. The long axis T1 of the first outlet pipe 41a and the long axis T0 of the inlet pipe 43a are arranged at a first angle a1, and the long axis T2 of the second outlet pipe 42a and the long axis T1 of the first outlet pipe 41a are arranged at a second angle a2. In some other embodiments, as shown in FIG. 3C , the first outlet pipe 41b and the second outlet pipe 42b of the bifurcated manifold 40b do not intersect. The intersection of the first outlet pipe 41b and the inlet pipe 43b is closer to or farther from the main heat exchanger (i.e., the inlet of the inlet pipe 43b) than the intersection of the second outlet pipe 42b and the inlet pipe 43b.

The first angle a1 may be between about 15 degrees and about 70 degrees. For example, the first angle a1 may be selected from any of 15 degrees, 20 degrees, 25 degrees, 30 degrees, 35 degrees, 40 degrees, 45 degrees, 50 degrees, 55 degrees, 60 degrees, 65 degrees or 70 degrees. By providing the first outlet pipe 41, the waste liquid W3 from the main heat exchanger 23, after the steam (all or part) is removed, forms the waste liquid W4, which will move downward along the inner wall of the first outlet pipe 41 by gravity, and enter the distillation gas-water separation barrel 50 (FIG. 1) through the first inlet port 521 (FIG. 1). Since the waste liquid W4 is not directly supplied to the distillation gas-water separation barrel 50 using a pipeline perpendicular to the side wall 512 of the distillation gas-water separation barrel 50, the suspended matter or tiny droplets caused by the waste liquid W4 splashing in the distillation gas-water separation barrel 50 can be reduced or avoided. Therefore, the risk of the gas compressor being damaged due to crystallization of the waste liquid can be further reduced. In an exemplary embodiment, the first angle a1 is set to 45 degrees to facilitate the waste liquid W4 to smoothly enter the first outlet pipe 41.

The second angle a2 may be between about 15 degrees and about 90 degrees. For example, the second angle a2 may be selected from any of 15 degrees, 20 degrees, 25 degrees, 30 degrees, 35 degrees, 40 degrees, 45 degrees, 50 degrees, 55 degrees, 60 degrees, 65 degrees, 70 degrees, 75 degrees, 80 degrees, 85 degrees or 90 degrees. The steam W5 in the waste liquid W3 from the main heat exchanger 23 will enter the second outlet pipe 42 upward due to its lighter specific gravity, and enter the distillation gas-water separation barrel 50 (FIG. 1) through the second inlet port 522 (FIG. 1). Since the steam W5 and the waste liquid W4 are separated before entering the distillation gas-water separation barrel 50 (Figure 1), the steam in the distillation gas-water separation barrel 50 is reduced or avoided from being mixed with water mist or fine droplets. Therefore, the risk of the gas compressor being damaged by crystallization of the waste liquid can be further reduced. In an exemplary embodiment, the second angle a2 is set to 45 degrees to facilitate the steam W5 to smoothly enter the second outlet pipe 42.

FIG. 4 shows a schematic diagram of a distillation gas-water separation barrel 50 according to some embodiments of the present disclosure. The distillation gas-water separation barrel 50 is configured to separate the steam in the waste liquid W4 from the remaining waste liquid. In some embodiments, the distillation gas-water separation barrel 50 includes a separation tank 51, a connecting pipe 54, and a storage tank 55. The separation tank 51 is a hollow cylindrical structure with a predetermined height. The first inlet port 521 and the second inlet port 522 of the distillation gas-water separation barrel 50 are respectively formed on the side wall 512 of the separation tank 51 and are separated by a height difference H1 in the vertical direction. The height difference H1 can be appropriately selected to minimize the possibility of the steam W5 being contaminated by suspended matter or fine droplets in the waste liquid W4, but will not prevent the steam separated from the waste liquid W4 from leaving the distillation gas-water separation barrel 50 through the outlet port 523.

The connecting pipe 54 is connected between the bottom surface 510 of the separation tank 51 and the top surface 551 of the storage tank 55. The concentrated waste liquid CL from which the steam has been removed in the separation tank 51 will be pulled by gravity and enter the storage tank 55 through the connecting pipe 54, and will be discharged through the discharge hole 552 formed on the bottom surface 550 of the storage tank 55. As shown in FIG1 , the concentrated waste liquid CL discharged from the storage tank 55 can be discharged to the dryer 83 through the pipeline 106 for further treatment, and a large amount of water in the concentrated waste liquid is removed to form wet sludge, so as to achieve the goal of zero wastewater discharge. Alternatively, after entering the storage tank 55, the concentrated waste liquid CL can be resupplied to the main heat exchanger 23 through the pipeline 114 and the pump 94 (e.g., a pneumatic pump) to mix with the waste liquid W2.

Referring to Figures 4 and 5, in some embodiments, the first inlet port 521 and the second inlet port 522 of the distillation gas-water separation barrel 50 are eccentrically arranged relative to the center C of the separation tank 51. For example, as shown in Figure 5, the first inlet port 521 is connected to the side wall 512 of the separation tank 51, wherein the outer wall of the first inlet port 521 is tangent to the outer wall of the separation tank 51, and the long axis T4 of the first inlet port 521 extends perpendicular to the radial direction of the separation tank 51 and is separated from the center C of the separation tank 51 by a distance D1. The second inlet port 522 can be connected to the separation tank 51 in a manner similar to the first inlet port 521.

As shown in FIG. 4 , since the first inlet port 521 and the second inlet port 522 are disposed eccentrically, the waste liquid W4 passing through the first inlet port 521 and the steam W5 passing through the second inlet port 522 will enter the separation tank 51 in a swirling manner. In this way, the waste liquid W4 can be prevented from splashing in the separation tank 51, thereby reducing or avoiding the concern of water mist or liquid droplets entering the steam. On the other hand, through the swirling movement of the steam W5, most of the water mist in the steam W5 will be removed from the steam W5 by the centrifugal force. In some embodiments, the steam W5 in the separation tank 51 and the steam separated from the waste liquid W4 will mix to form a composite gas flow W6, and will be discharged from the distillation gas-water separation barrel 50 through an outlet port 523 formed on the top surface 511 of the separation tank 51. The outlet port 523 can be set in a tilted manner relative to the top surface 511 of the separation tank 51 to facilitate the discharge of the rotating composite gas flow W6. In some embodiments, the distillation gas-water separation barrel 50 may further include one or more inspection windows 56, 57 for the operator to inspect the conditions in the separation tank 51 and the storage tank 55.

Referring again to FIG. 1 , in some embodiments, after the waste liquid W4 leaves the branch manifold 40 and before entering the distillation gas-water separation barrel 50, the waste liquid W4 is further heated by the heating pipe 25. In some embodiments, as shown in FIGS. 6A and 6B , the heating pipe includes a shell 26, a fluid inlet 27, a fluid outlet 28, and a plurality of flow channels 29. The shell 26 has a side wall 261 and two end surfaces 262 and 263 located at both ends of the side wall 261. The shell 26 is a hollow structure, the upper end of which is connected to the fluid inlet 27, and the lower end is connected to the fluid outlet 28. The flow channel 29 is a tubular structure having openings at both ends and extending parallel to the side wall 261. One end of the flow channel 29 located on the end surface 262 is connected to the first outlet pipe 41 of the branch manifold 40 (Figure 1), and the other end of the flow channel 29 located on the end surface 263 is connected to the first inlet port 521 of the distillation gas-water separation barrel 50 (Figure 1). When heating the waste liquid W4, as shown in Figure 6B, the heated steam G1 enters the shell 26 through the fluid inlet 27, and after flowing through the outer surface of the flow channel 29, it is discharged from the shell 26 through the fluid outlet 28.

In some embodiments, as shown in FIG. 1 , the heating pipe 25 can be fluidly connected to a heat source 82 via a valve 93 to receive heated steam from the heat source 82. Furthermore, the heating pipe 25 can be fluidly connected to the second outlet pipe 42 via a pipeline 105 to discharge the heated steam into the distillation gas-water separation barrel 50 via the second outlet pipe 42. In an exemplary embodiment, the heat source 82 is high-temperature steam discharged from a factory equipment (not shown), so the carbon footprint generated by the operation of the mechanical steam recompression system 1 can be reduced. In some embodiments, the heating process of the waste liquid W4 is only performed when the mechanical steam recompression system 1 is started, and stops when the waste liquid W4 reaches a predetermined temperature. In other embodiments, the heating process of the waste liquid W4 is automatically executed when the temperature of the waste liquid W4 is lower than a predetermined temperature. In still other embodiments, the heating process of the waste liquid W4 is continuously executed during the operation of the mechanical vapor recompression system 1.

The traditional MVR system uses a heater installed in the separation tank to directly heat the waste liquid, and the heater will vibrate during the heating process. This vibration will generate waste liquid droplets in the separation tank, and the droplets will adhere to the gas compressor with the steam. Heating the waste liquid by the heating pipe of the embodiment of the present disclosure can effectively avoid the above-mentioned shortcomings of the traditional MVR system. In addition, since the high-temperature steam heats the waste liquid W4 through the outer surface of the flow channel 29 instead of directly heating the waste liquid W4, the generation of water mist and droplets can be further reduced.

FIG7 shows a schematic cross-sectional view of a water mist elimination barrel 60 according to some embodiments of the present disclosure. According to some embodiments, the water mist elimination barrel 60 includes a body 61, an inlet port 621, an outlet port 622, a plurality of grid plates 631, 632, 633, 634, 635, a grid frame 64, a plurality of annular fillers 65, and a channel 66.

The body 61 has a hollow cylindrical structure. The inlet port 621 is disposed on the side surface 612 of the body 61 and adjacent to the top surface 611 of the body 61. The inlet port 621 is configured to receive the composite airflow W6 delivered from the separation tank 51 via the pipeline 107 (FIG. 1). In some embodiments, similar to the arrangement of the first inlet port 521 shown in FIG. 5, the inlet port 621 of the mist elimination barrel 60 is eccentrically arranged relative to the center of the body 61. In this way, the composite airflow W6 passing through the inlet port 621 will enter the body 61 in a swirling manner.

The outlet port 622 is disposed at the center of the top surface 611 of the body 61. The channel 66 is a hollow tube. The upper end of the channel 66 is connected to the outlet port 622 and extends to the lower end thereof in a direction away from the outlet port 622 and toward the bottom surface 610 of the body 61. The lower end of the channel 66 is separated from the bottom surface 610 of the body 61 by a height difference H2 and does not directly contact the bottom surface 610 of the body 61.

A plurality of grid plates 631, 632, 633, 634, 635 are disposed in the body 61 and below the inlet port 621. The grid plates 631, 632, 633, 634, 635 each have an annular structure, the outer circumference of which abuts against the inner wall surface of the body 61, and the inner circumference of which abuts against the outer surface of the channel 66. Specifically, as shown in FIG8 , the inner circumference of the grid plates 631, 632, 633, 634, 635 each defines an opening 6315, 6325, 6335, 6345, 6355. The channel 66 penetrates the openings 6315, 6325, 6335, 6345, 6355 and abuts against the inner edge thereof. Adjacent grid plates 631, 632, 633, 634, 635 are separated by spacers 67 disposed therebetween and are spaced apart from each other.

In some embodiments, the grid plates 631, 632, 633, 634, 635 further include perforations for allowing fluid to pass through, wherein the perforations of two of the adjacently arranged grid plates 631, 632, 633, 634, 635 are arranged alternately with each other. For example, as shown in FIG8, the grid plates 631 and 632 each include a plurality of perforations 6310 and 6320, wherein the perforations 6310 on the grid plate 631 are arranged alternately with the perforations 6320 on the grid plate 632. That is, when viewed in the direction of the parallel channel 66, the perforations 6310 on the grid plate 631 and the perforations 6320 on the grid plate 632 do not overlap.

Referring again to FIG. 7 and FIG. 9 , the grid 64 has an annular structure and is configured to allow fluid to pass through. In some embodiments, the grid 64 is disposed in the body 61, with its outer circumference abutting against the inner wall surface of the body 61 and its inner circumference abutting against the outer surface of the channel 66. The grid 64 is separated from the bottom surface 610 of the body 61 by a height difference H3. In an exemplary embodiment, the height difference H3 is greater than the height difference H2 (i.e., the lower end of the channel 66 is closer to the bottom surface 610 of the body 61 than the grid 64). A plurality of annular fillers 65 are distributed on the grid 64. The annular fillers 65 can be respectively a Bower ring, which is configured to remove water mist in the airflow. In some embodiments, as shown in FIG. 9 , the annular filler 65 includes an annular body 651, wherein a plurality of notches 652 are formed on the annular body 651, and an edge of each notch 652 is connected to an inwardly bent blade 653.

The method of eliminating water mist in the water mist elimination barrel 60 is described as follows: First, after the composite airflow W6 enters the body 61 through the inlet port 621, the composite airflow W6 enters the separation tank 51 in a swirling manner, so the water mist with a larger mass in the composite airflow W6 will be removed from the composite airflow W6 by the centrifugal force. In addition, when the composite airflow W6 passes through the perforations of the grid plates 631, 632, 633, 634, and 635, the grid plates 631, 632, 633, 634, and 635 will remove the water mist with a smaller mass in the composite airflow W6 due to the staggered arrangement of the perforations, thereby forming a composite airflow W7 with very little water mist content. Furthermore, when the composite airflow W7 passes through the annular filler 65, the annular filler 65 will remove most of the water mist in the composite airflow W7 due to the structural characteristics of the annular filler 65, and form steam W8 without water mist or almost without water mist. After passing through the annular filler 65 and the grid 64, the steam W8 will leave the water mist elimination barrel 60 through the channel 66 and the outlet port 622. However, it should be understood that the configuration of the water mist elimination barrel 60 disclosed in the present disclosure is not limited to the above-mentioned embodiments. In some embodiments, one or two of the three mechanisms for removing water mist in the water mist elimination barrel 60 (i.e., swirling airflow, grid plate, annular filler) can be selectively omitted.

The water mist elimination barrel 60 of the disclosed embodiment is designed to remove water mist in the composite gas flow by a variety of different mechanisms, providing at least the following technical advantages: (1) Since the water mist elimination barrel 60 can reduce the water mist content in the steam W8 supplied to the gas compressor 70 to a minimum or even completely remove it, the gas compressor 70 will not be easily damaged by crystallization caused by the water mist, so the gas compressor 70 will not be damaged by crystallization caused by the water mist. 0 can be extended and the gas compressor 70 does not need to be frequently maintained; (2) Since the ring packing 65, which is expensive to manufacture, is used to process the composite gas flow W7 having a lower water mist content and passing through the grid plates 631, 632, 633, 634, 635, the service life of the ring packing 65 can be extended and the ring packing 65 does not need to be frequently replaced.

Referring again to FIG. 1 , after steam W8 leaves the water mist elimination barrel 60, it is supplied to the gas compressor 70 via the pipeline 108. The gas compressor 70 compresses the steam W8 to increase its pressure and temperature and convert it into high-pressure steam HG. The high-pressure steam HG is transported from the gas compressor 70 to the main heat exchanger 23 via the pipeline 109, and heat is exchanged with the waste liquid W2 in the main heat exchanger 23. The high-pressure steam HG is condensed in the main heat exchanger 23 to form a condensate L1. The condensate L1 is then transported to the second region 34 of the waste liquid preheating barrel 30 via the pipeline 110 and the pump 95 (e.g., a pneumatic pump) to perform heat exchange with the waste liquid W1 in the first region 33 of the waste liquid preheating barrel 30 and is converted into the condensate L2 with a lower temperature. The condensate L2 is then transported to the secondary heat exchanger 21 via the pipeline 111 to perform heat exchange with the waste liquid W0 and is converted into the condensate L3 with a lower temperature. The condensate L3 is then transported to the condensate storage tank 84 via the pipeline 112 for storage. Since the source of the condensate (i.e., the high-pressure steam HG) no longer contains waste liquid mist (or contains only very little mist), the water quality of the condensate produced by the mechanical steam recompression system 1 of the disclosed embodiment is also better than the water quality of the condensate produced by the traditional distillation system.

Referring again to FIG. 1 and FIG. 9 , in some embodiments, the water mist elimination barrel 60 further includes a drain port 623 (FIG. 9) and an exhaust hole 624 (FIG. 9). The drain port 623 is disposed on the bottom surface 610 of the body 61 of the water mist elimination barrel 60 and is configured to discharge the waste liquid collected by the water mist in the water mist elimination barrel 60 from the water mist elimination barrel 60. The waste liquid from the water mist elimination barrel 60 will be discharged to the first area 33 of the waste liquid preheating barrel 30 through the pipeline 113, and will be mixed with the waste liquid W1 and then distilled again.

In some embodiments, at least some components of the mechanical vapor recompression system 1 are arranged at different heights, thereby reducing the area required for installing the mechanical vapor recompression system 1. For example, as shown in FIG1 , the water mist elimination barrel 60 and the gas compressor 70 of the mechanical vapor recompression system 1 are arranged above the height line LV, and the remaining components of the mechanical vapor recompression system 1 can be arranged below the height line LV, thereby reducing the space occupied by the mechanical vapor recompression system 1. The height line LV can be composed of an elevated platform (not shown).

The control device 90 is configured to control the operation of the electronic components of the mechanical vapor recompression system 1. For example, the control device 90 is set according to a predetermined program to control the operation of pumps 91, 92, 94, 95, valve 93 and gas compressor 70. The control device 90 can be a computer and include a processor, a memory, an input/output interface, a communication interface, a system bus and other components. The control device 90 can selectively open the valve 93 according to a detector (such as a thermometer provided at the first inlet port 521) provided in the mechanical vapor recompression system 1 to supply steam into the heating pipe 25.

Table 1 shows the energy consumption and cost comparison table of the mechanical vapor recompression system 1 of the disclosed embodiment and the traditional distillation equipment.

The data shown in Table 1 can prove that the mechanical steam recompression system 1 of the disclosed embodiment has excellent energy-saving performance compared with the traditional distillation equipment. Therefore, the mechanical steam recompression system 1 of the disclosed embodiment can effectively reduce carbon emissions and save the cost of treating waste liquid.

FIG. 10 shows a schematic diagram of a mechanical vapor recompression system 1a according to another embodiment of the present disclosure. The same or similar components of the mechanical vapor recompression system 1a and the mechanical vapor recompression system 1 are given similar symbols, and their features will not be described again. In some embodiments, the difference between the mechanical vapor recompression system 1a and the mechanical vapor recompression system 1 includes that the mechanical vapor recompression system 1a omits the branch manifold 40 and the water mist elimination barrel 60. The waste liquid W3 from the main heat exchanger 23 is directly transported to the first inlet port 521 through the pipeline 115, and is heated by the heating pipe 25 to maintain it in a boiling state. Therefore, when the waste liquid W3 enters the separation tank 51 of the distillation gas-water separation barrel 50a, the steam W9 generated by the heating of the waste liquid W3 will be separated from the concentrated waste liquid CL and transported to the gas compressor 70 through the pipeline 116 for compression. Since the waste liquid W3 is not heated by the heater installed in the separation tank 51, there will be no water mist of the waste liquid in the steam W9 (or only very little water mist), which will not cause negative impact on the gas compressor 70.

In the embodiment where the first inlet port 521 is eccentrically disposed relative to the center C of the separation tank 51, since the steam W9 swirls in the separation tank 51, most of the water mist in the steam W9 will be further subjected to the centrifugal force and discharged from the steam W9. Therefore, even if the water mist elimination barrel 60 is omitted, the concern that the gas compressor 70 is damaged by the crystallization of water mist can be avoided or reduced. In other embodiments, the mechanical vapor recompression system 1 only reduces the installation of one of the branch manifold 40 and the water mist elimination barrel 60, but retains the other of the branch manifold 40 and the water mist elimination barrel 60, which can still avoid or reduce the concern that the gas compressor 70 is damaged by the crystallization of water mist.

FIG. 11 shows a schematic diagram of a mechanical vapor recompression system 1b according to another embodiment of the present disclosure. The same or similar components of the mechanical vapor recompression system 1b and the mechanical vapor recompression system 1 are given similar symbols, and their features will not be described again. In some embodiments, the difference between the mechanical vapor recompression system 1b and the mechanical vapor recompression system 1 includes that the mechanical vapor recompression system 1b omits the waste liquid preheating barrel 30 and the branching manifold 40. During operation, the waste liquid W10 from the secondary heat exchanger 21 is directly transported to the primary heat exchanger 23 through the pipeline 117. Furthermore, the waste liquid W11 from the main heat exchanger 23 is directly transported to the first inlet port 521 through the pipeline 119. After entering the separation tank 51, the waste liquid W11 swirls in the separation tank 51 to remove most of the water mist and liquid and form a composite gas flow W12 to be discharged from the distillation gas-water separation barrel 50b. The composite gas flow W12 from the distillation gas-water separation barrel 50b is then supplied to the water mist elimination barrel 60, and after eliminating the water mist, steam W13 that does not contain water mist is formed. The steam W13 is then supplied to the gas compressor 70 for compression. Since there is no water mist of waste liquid in the steam W13, there will be no negative impact on the gas compressor 70. In other embodiments, the mechanical steam recompression system 1 only reduces the installation of one of the waste liquid preheating barrel 30 and the branch manifold 40, but retains the other of the waste liquid preheating barrel 30 and the branch manifold 40, which can still avoid or reduce the concern of the gas compressor 70 being damaged by the crystallization of water mist.

The gas compressor 70 compresses the steam W13 to increase its pressure and temperature and convert it into high-pressure steam HG. The high-pressure steam HG is transported from the gas compressor 70 to the main heat exchanger 23 via the pipeline 109, and heat exchanges with the waste liquid W10 in the main heat exchanger 23. The high-pressure steam HG forms a condensate L4 due to condensation in the main heat exchanger 23. The condensate L4 is then transported to the secondary heat exchanger 21 via the pipeline 118 and the pump 95 (e.g., a gas pressure pump) to exchange heat with the waste liquid W0 and convert it into a condensate L5 with a lower temperature. The condensate L5 is then transported to the condensate storage tank 84 via the pipeline 112 for storage. Since the source of the condensate (i.e., the high-pressure steam HG) no longer contains waste liquid mist (or contains only very little mist), the water quality of the condensate produced by the mechanical steam recompression system 1b of the disclosed embodiment is also better than the water quality of the condensate produced by the traditional distillation system.

The above has summarized the structures of several embodiments so that those with ordinary knowledge in the art can better understand the state of the embodiments disclosed herein. Those with ordinary knowledge in the art should understand that they can easily use this disclosure as a basis for designing or modifying other processes and structures to implement the same purpose and/or achieve the same advantages of the embodiments introduced in this article. Those with ordinary knowledge in the art should also realize that such equivalent constructions should not deviate from the spirit and scope of this disclosure, and that they can make various changes, substitutions and modifications to this article without departing from the spirit and scope of this disclosure.

50: Distillation gas-water separation barrel

51:Entity

510: Bottom

511: Top

512: Side wall

521: First entrance port

522: Second entrance port

523: Export port

54: Connecting tube

55: Storage slot

550: Bottom

551: Top

552: discharge hole

56, 57: Viewing window

CL: concentrated waste liquid

H1: Height difference

W4: Wastewater

W5: Steam

W6: Compound airflow

Claims (20)

A mechanical steam recompression system comprises: a distillate gas separation drum; a gas compressor configured to compress a steam from the distillate gas separation drum; a water mist elimination drum, which fluidly connects the distillate gas separation drum and the gas compressor and is configured to eliminate a water mist from the distillate gas separation drum; a main heat exchanger, which is configured to heat wastewater from a wastewater source by the pressurized steam from the gas compressor; A waste liquid preheating barrel, comprising a containing barrel and a heat conductive partition disposed in the containing barrel, the heat conductive partition dividing the containing barrel into at least a first area and a second area, the first area fluidly connected between the waste water source and the main heat exchanger and configured to contain the waste water, the second area fluidly connected between the main heat exchanger and a drain outlet and configured to contain condensate generated from the main heat exchanger after the steam condenses; and a branch manifold, comprising an inlet pipe fluidly connected to the main heat exchanger and a first outlet pipe and a second outlet pipe connected to the inlet pipe and fluidly connected to different height positions of the distilled gas-water separation barrel. A mechanical vapor recompression system as described in claim 1, wherein the water mist elimination barrel comprises: a body; an outlet port located at the bottom of the body; a channel extending from the outlet port toward the bottom of the body to an air inlet end; an inlet port connected to the body; a plurality of grid plates arranged in sequence below the inlet port and arranged around the channel; and a plurality of annular fillers arranged between the plurality of grid plates and the air inlet end of the channel. A mechanical vapor recompression system as described in claim 2, wherein each of the grid plates includes a plurality of perforations, and the perforations of two of the adjacently arranged grid plates are arranged alternately with each other. A mechanical vapor recompression system as described in claim 2, wherein the inlet port is connected to the body and is offset from the center of the body. A mechanical vapor recompression system as described in claim 1, wherein the first outlet pipe fluid of the branch manifold is connected to a first inlet port of the distilled gas-water separation barrel, and the second outlet pipe fluid of the branch manifold is connected to a second inlet port of the distilled gas-water separation barrel, the first inlet port is located below the second inlet port, and the angle between the inlet pipe and the first outlet pipe is between about 15 degrees and about 70 degrees. A mechanical vapor recompression system as described in claim 5, wherein the angle between the inlet pipe and the second outlet pipe is between about 15 degrees and about 90 degrees. The mechanical vapor recompression system as described in claim 5 further includes a heating pipe, which includes: a shell having a side wall and two end faces located at both ends of the side wall; a plurality of flow channels extending parallel to the side wall between the two end faces and fluidly connected between the first outlet pipe of the branch manifold and the first inlet port of the distilled gas-water separation barrel; and a fluid inlet and a fluid outlet, respectively connected to the side wall of the shell, wherein a high-temperature fluid enters the interior of the shell from the fluid inlet and is discharged from the shell through the fluid outlet after flowing through the outer surfaces of the flow channels to heat the waste water from the main heat exchanger transported to the distilled gas-water separation barrel through the flow channels. A mechanical vapor recompression system as described in claim 7, wherein the fluid outlet of the heating tube is fluidly connected to the second outlet pipe, and the high-temperature fluid is discharged from the fluid outlet of the heating tube and then enters the distillation gas-water separation barrel through the second outlet pipe and the second inlet port. A mechanical vapor recompression system as described in claim 1, wherein the first outlet pipe fluid of the branch manifold is connected to a first inlet port of the distilled gas-water separation barrel, and the second outlet pipe fluid of the branch manifold is connected to a second inlet port of the distilled gas-water separation barrel, wherein at least one of the first inlet port and the second inlet port is offset from the center of the distilled gas-water separation barrel. A mechanical steam recompression system comprises: a distillate separation drum; a gas compressor configured to compress a steam from the distillate separation drum; a primary heat exchanger configured to heat wastewater from a wastewater source by the pressurized steam from the gas compressor; A waste liquid preheating barrel, comprising a containing barrel and a heat conductive partition disposed in the containing barrel, the heat conductive partition divides the containing barrel into at least a first area and a second area, the first area fluid is connected between the waste water source and the main heat exchanger and is configured to contain the waste water, the second area fluid is connected between the main heat exchanger and a drain outlet and is configured to contain condensate generated by condensation of the steam in the main heat exchanger; A heating pipe, whose fluid is connected between the main heat exchanger and the distillation gas-water separation barrel and is configured to heat the waste water from the main heat exchanger; and A heat source, which is connected to the heating pipe. A mechanical steam recompression system as described in claim 10, wherein the heat source is high-temperature steam exhausted from a factory equipment. A mechanical vapor recompression system as described in claim 10, wherein the heating pipe comprises: a shell having a side wall and two end faces located at both ends of the side wall; a plurality of flow channels extending parallel to the side wall between the two end faces and fluidly connected between the main heat exchanger and the distillation gas-water separation barrel; and a fluid inlet and a fluid outlet, respectively connected to the side wall of the shell, wherein a high-temperature fluid from the heat source enters the interior of the shell from the fluid inlet, and after flowing through the outer surfaces of the flow channels, is discharged from the shell through the fluid outlet to heat the waste water from the main heat exchanger transported to the distillation gas-water separation barrel through the flow channels. The mechanical vapor recompression system as described in claim 12 further includes: A branch manifold, which includes an inlet pipe fluidly connected to the main heat exchanger and a first outlet pipe and a second outlet pipe connected to the inlet pipe and fluidly connected to different height positions of the distillate gas-water separation barrel, wherein the first outlet pipe is located below the second outlet pipe, and the heating pipe is fluidly connected between the first outlet pipe and the distillate gas-water separation barrel. The mechanical vapor recompression system as described in claim 10 further includes: A water mist elimination barrel, which is fluidly connected between the distillation gas-water separation barrel and the gas compressor and is configured to eliminate a water mist from the distillation gas-water separation barrel. The mechanical steam recompression system as described in claim 1 or 10 further includes: A secondary heat exchanger, the fluid of which connects the first zone and the second zone of the waste liquid preheating barrel and is configured to allow the waste water supplied to the first zone to exchange heat with the condensate from the second zone. A mechanical vapor recompression system as described in claim 1 or 10, wherein the distilled gas-water separation drum comprises: a separation tank; a storage tank located below the separation tank; and a connecting pipe connected to the separation tank and the storage tank, wherein the pipe diameter of the connecting pipe is smaller than the width of the separation tank and smaller than the width of the storage tank. A mechanical steam recompression system includes: a distillate gas-water separation drum; a gas compressor configured to compress a steam from the distillate gas-water separation drum; a water mist elimination drum, which is fluidly connected between the distillate gas-water separation drum and the gas compressor and is configured to eliminate a water mist from the distillate gas-water separation drum; a primary heat exchanger, which is configured to heat waste water from a waste water source by the pressurized steam from the gas compressor; and a secondary heat exchanger, which is fluidly connected to the primary heat exchanger and is configured to allow the waste water supplied to the primary heat exchanger to exchange heat with the condensate from the primary heat exchanger. A mechanical vapor recompression system as described in claim 17, wherein the water mist elimination barrel comprises: a body; an outlet port located at the bottom of the body; a channel extending from the outlet port toward the bottom of the body to an air inlet end; an inlet port connected to the body; a plurality of grid plates arranged in sequence below the inlet port and arranged around the channel; and a plurality of annular fillers arranged between the plurality of grid plates and the air inlet end of the channel. The mechanical steam recompression system as described in claim 17 further comprises: A waste liquid preheating barrel, which comprises a containing barrel and a heat conductive partition disposed in the containing barrel, the heat conductive partition divides the containing barrel into at least a first area and a second area, the first area fluid is connected between the secondary heat exchanger and the primary heat exchanger and is configured to contain the waste water, the second area fluid is connected between the primary heat exchanger and the secondary heat exchanger and is configured to contain the condensate generated by the condensation of the steam in the primary heat exchanger. The mechanical vapor recompression system as described in claim 17 further includes: A branch manifold including an inlet pipe fluidly connected to the main heat exchanger and a first outlet pipe and a second outlet pipe connected to the inlet pipe and fluidly connected to different height positions of the distillation gas-water separation drum.

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