Oxidation tower for oxidizing and demethanizing flue gas of dual-fuel engine of ship

Abstract

The utility model discloses a ship dual-fuel engine flue gas oxidation and demethanization oxidation tower, and relates to the technical field of flue gas treatment.The oxidation tower comprises a tower body and further comprises a flue gas input pipe and a flue gas output pipe; the first reactor is arranged in the tower body and is communicated with the flue gas input pipe, and a first output end is arranged at the bottom of the first reactor; the second reactor is arranged in the tower body and sleeves the periphery of the first reactor, a second output end is arranged at the bottom of the second reactor, the first output end extends out of the second output end, the top of the second reactor is communicated with the flue gas output pipe, and a flue gas inlet pipe is further arranged on the side wall of the second reactor; the first spraying assembly is used for conveying an oxidizing solution into the first reactor; and the second spraying assembly is used for conveying an oxidizing solution to the outside of the second reactor. The oxidation tower disclosed by the utility model can efficiently decompose escape methane in flue gas.

Description

Technical Field

[0001] The present application relates to the technical field of flue gas treatment, and in particular to a flue gas oxidation demethanization tower for a ship dual-fuel engine. Background Art

[0002] With increasingly stringent environmental protection requirements and adjustments to the energy structure, the shipping industry has gradually adopted dual-fuel engines, such as the mixed use of liquefied natural gas (LNG) and traditional fuels, to reduce greenhouse gas emissions. Although dual-fuel engines can significantly reduce carbon dioxide and nitrogen oxide emissions during operation, there is still a certain amount of escaped methane (CH4) in the flue gas, which is a potent greenhouse gas with a global warming potential (GWP) much higher than carbon dioxide.

[0003] Therefore, how to efficiently decompose the escaped methane in the flue gas has become a technical problem that needs to be solved urgently in the shipping industry. Utility Model Content

[0004] The technical problem actually solved by the technical solution of this application is how to efficiently decompose the escaped methane in the flue gas.

[0005] In order to solve the above-mentioned technical problems, the technical solution of the present application provides a ship dual-fuel engine flue gas oxidation demethanization oxidation tower, including a tower body, the oxidation tower also including: a flue gas input pipe and a flue gas output pipe; a first reactor, which is arranged in the tower body and is connected to the flue gas input pipe, and has a first output end at the bottom; a second reactor, which is arranged in the tower body and is sleeved on the outer periphery of the first reactor, wherein the first output end extends out of the second output end, the top of the second reactor is connected to the flue gas output pipe, and the side wall of the second reactor is also provided with a flue gas inlet pipe; a first spray assembly, which is used to transport an oxidizing solution to the interior of the first reactor; and a second spray assembly, which is used to transport an oxidizing solution to the outside of the second reactor.

[0006] In some embodiments, the first reactor comprises a first cylindrical section, a first conical section, and a second cylindrical section which are smoothly connected in sequence, wherein the inner diameter of the first cylindrical section is greater than the inner diameter of the second cylindrical section.

[0007] In some embodiments, the first output end of the first reactor includes at least two air ducts, and the air outlets at the ends of each of the air ducts are bent in a clockwise or counterclockwise direction.

[0008] In some embodiments, the second reactor comprises a third cylindrical section, a second conical section, and a fourth cylindrical section which are smoothly connected in sequence, wherein the inner diameter of the third cylindrical section is greater than the inner diameter of the fourth cylindrical section.

[0009] In some embodiments, the first spray assembly includes: a first spray head, disposed on the top of the first reactor; and a first spray head pipe, one end of which is connected to the first spray head and the other end of which extends out of the tower body.

[0010] In some embodiments, the second spray assembly includes: at least one second nozzle pipe, and the second nozzle pipe includes: an annular pipe section surrounding the outer circumference of the second reactor, and the annular pipe section is evenly provided with a plurality of second nozzles, wherein the input end of the second nozzle pipe extends out of the tower body.

[0011] In some embodiments, the oxidation tower further includes: a first catalyst packing layer, which is disposed in the tower body, located at the outer periphery of the second reactor, and located below the flue gas inlet pipe.

[0012] In some embodiments, the oxidation tower further includes: a heat exchange coil, which is disposed in the tower body, sleeved on the outer periphery of the second reactor, and located below the flue gas inlet pipe.

[0013] In some embodiments, the number of the flue gas input pipes is two, and the two flue gas input pipes are symmetrically arranged relative to the axis center of the first reactor.

[0014] In some embodiments, the number of the flue gas inlet pipes is two, and the two flue gas inlet pipes are symmetrically arranged relative to the axis center of the second reactor.

[0015] In some embodiments, the oxidation tower also includes: a third spray assembly for conveying an oxidizing solution into the second reactor, and the third spray assembly includes: a third nozzle, disposed on the inner wall of the second reactor and located above the flue gas inlet pipe; a third nozzle pipe, one end of which is connected to the third nozzle and the other end extends out of the tower body.

[0016] Compared with the prior art, the ship dual-fuel engine flue gas oxidation demethanization oxidation tower of the technical solution of the present application has the following beneficial effects:

[0017] The marine dual-fuel engine flue gas oxidation demethanization oxidation tower of the present application can achieve gas-vapor contact between flue gas and oxides. Compared with the gas-liquid contact method of the traditional scrubber, it can greatly increase the contact probability between flue gas and oxides, thereby significantly improving the oxidation decomposition efficiency of flue gas, and can also reduce the amount of oxidizing solution, thereby achieving efficient decomposition of escaped methane in flue gas. At the same time, the waste heat of flue gas can directly vaporize the oxidizing solution without the need for an external heat source, which can not only avoid the energy consumption of external heating, but also reduce the manufacturing cost and maintenance difficulty of the equipment.

[0018] Furthermore, the first output end of the first reactor includes at least two air ducts, and the air outlets at the end of each air duct are bent together in a clockwise or counterclockwise direction, so that a vortex wind field can be formed at the bottom of the tower body. This can not only increase the mixing and contact probability of the flue gas and the oxidizing solution, but also increase the residence time of the flue gas in the tower body, thereby further improving the oxidation efficiency.

[0019] Furthermore, by arranging the flue gas input pipe symmetrically with respect to the axis center of the first reactor, the input flue gas can form a cyclonic wind field in the first reactor, which is beneficial for the flue gas and oxidizing steam to swirl downward in the first reactor.

[0020] Furthermore, the flue gas inlet pipe is arranged symmetrically with respect to the axis center of the second reactor, so that the flue gas entering the second reactor forms a cyclonic wind field, thereby improving the gas-liquid separation effect. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] The following drawings describe in detail the exemplary embodiments disclosed in this application. The same reference numerals represent similar structures in several views of the drawings. Those skilled in the art will understand that these embodiments are non-limiting, exemplary embodiments, and the drawings are only for the purpose of illustration and description, and are not intended to limit the scope of this application. Other embodiments may also accomplish the intentions in this application. It should be understood that the drawings are not drawn to scale. Among them:

[0022] Figure 1 This is a schematic structural diagram of a flue gas oxidation demethanization tower for a ship dual-fuel engine according to an embodiment of the present application;

[0023] Figure 2 This is a schematic diagram of the structure of the first reactor and the second reactor of the flue gas oxidation demethanization oxidation tower of the ship dual-fuel engine according to an embodiment of the present application;

[0024] Figure 3 This is a schematic diagram of the top view of the structure of the flue gas oxidation demethanization oxidation tower of a ship dual-fuel engine according to an embodiment of the present application;

[0025] Figure 4 This is a schematic diagram of the structure of the air guide duct according to an embodiment of the present application;

[0026] Figure 5 This is a cross-sectional schematic diagram of the first catalyst packing layer of an embodiment of the present application;

[0027] Figure 6 This is a schematic structural diagram of a flue gas oxidation demethanization system for a ship dual-fuel engine according to an embodiment of the present application;

[0028] Figure 7 This is a schematic structural diagram of another ship dual-fuel engine flue gas oxidation demethanization system according to an embodiment of the present application;

[0029] The meanings of the reference numerals are as follows:

[0030] 1- oxidation tower; 2- oxidizing solution recovery device; 3- liquid replenishment device; 4- oxidation dehydration device; 5- first heat exchange device; 6- second heat exchange device; 7- pH detection device; 8- circulation pump; 9- supplementary pump; 10- tower body; 11- smoke inlet pipe; 12- smoke outlet pipe; 13- smoke inlet pipe;

[0031] 41-oxidation and dehydration chamber; 42-second catalyst packing layer; 43-fourth spray assembly; 44-demist assembly;

[0032] 100-first reactor; 101-first cylindrical section; 102-first conical section; 103-second cylindrical section; 104-air duct;

[0033] 200 - second reactor; 201 - third cylindrical section, 202 - second conical section; 203 - fourth cylindrical section;

[0034] 300-first spray assembly; 301-first spray head; 302-first spray head pipeline;

[0035] 400-second spray assembly; 401-second spray head pipeline; 402-second spray head;

[0036] 500-first catalyst packing layer; 600-heat exchange coil;

[0037] 700 - the third spray assembly; 701 - the third spray head; 702 - the third spray head pipeline. DETAILED DESCRIPTION

[0038] The following description provides specific application scenarios and requirements of the present application, with the purpose of enabling those skilled in the art to make and use the contents of the present application. Various local modifications to the disclosed embodiments are obvious to those skilled in the art, and the general principles defined herein may be applied to other embodiments and applications without departing from the spirit and scope of the present application. Therefore, the present application is not limited to the embodiments shown, but to the widest scope consistent with the claims. The ship dual-fuel engine flue gas oxidation demethanization oxidation tower (hereinafter referred to as the oxidation tower) of the embodiment of the present application is described in detail below in conjunction with the accompanying drawings.

[0039] The oxidation tower of the embodiment of the present application can perform oxidation treatment on the input gas, and can be applied to the demethanization treatment of the flue gas of the ship LNG dual-fuel engine.

[0040] Combination Figure 1 and Figure 2The oxidation tower 1 of the embodiment of the present application includes a tower body 10, a flue gas input pipe 11, a flue gas output pipe 12, a first reactor 100, a second reactor 200, a first spray assembly 300 and a second spray assembly 400.

[0041] The first reactor 100 is disposed in the tower body 10 and is connected to the smoke inlet pipe 11, and has a first output end at the bottom. The smoke inlet pipe 11 is used to transport smoke into the first reactor 100. In some embodiments, the smoke inlet pipe 11 can be disposed on the side wall of the first reactor 100, and the first end of the smoke inlet pipe 11 is connected to the first reactor 100, and the second end of the smoke inlet pipe 11 extends out of the tower body 10.

[0042] The number of the flue gas input pipe 11 is at least one. In some preferred embodiments, the number of the flue gas input pipe 11 is at least two, and the two flue gas input pipes 11 are configured so that the input flue gas can form a cyclonic wind field in the first reactor 100, and the cyclonic wind field can make the flue gas, oxidizing steam and unvaporized oxidizing solution continuously swirl toward the bottom of the first reactor 100 and flow out from the first output end. In some specific embodiments, such as Figure 3 As shown, the number of the flue gas input pipes 11 is two, and the two flue gas input pipes 11 are symmetrically arranged relative to the axis center of the first reactor 100 .

[0043] The first spray assembly 300 is used to transport the oxidizing solution into the first reactor 100. Since the temperature of the flue gas is usually high and higher than the vaporization temperature of the oxidizing solution, the oxidizing solution is vaporized into oxidizing steam, thereby realizing a gas-steam contact oxidation method. Compared with the traditional gas-liquid contact oxidation method, the contact probability between the flue gas and the oxidizing steam is greatly improved, thereby significantly improving the oxidation decomposition efficiency of methane.

[0044] In some specific embodiments, the first spray assembly 300 includes: a first spray head 301 and a first spray head pipe 302, wherein the first spray head 301 is disposed at the top of the first reactor 100, a first end of the first spray head pipe 302 is connected to the first spray head 301, and a second end of the first spray head pipe 302 extends out of the tower body 10. The flue gas input pipe 11 is disposed close to the first spray head 301 to increase the contact probability between the flue gas and the oxidizing solution, thereby improving the vaporization efficiency of the oxidizing solution and the oxidative decomposition efficiency of the flue gas.

[0045] In some embodiments, the first output end of the first reactor 100 includes at least two air ducts 104, and is configured to form a cyclone wind field at the bottom of the tower body 10 for the output flue gas and oxidizing steam. On the one hand, the cyclone wind field can increase the probability of mixing and contacting the flue gas with the oxidizing solution, thereby improving the oxidation decomposition efficiency; on the other hand, the cyclone wind field can increase the flow of the flue gas in the horizontal direction, thereby increasing the residence time of the flue gas in the tower body 10, thereby improving the oxidation decomposition efficiency.

[0046] In some embodiments, the air outlets at the ends of each of the air guide pipes 104 are bent together in a clockwise or counterclockwise direction to form a swirl wind field. Figure 4 As shown, there are four air ducts 104, and the air outlets at the ends of each air duct 104 are bent clockwise or counterclockwise. More specifically, two adjacent air ducts 104 are perpendicular to each other, and the air outlets at the ends of each air duct 104 are bent 90 degrees counterclockwise.

[0047] In some specific embodiments, the first reactor 100 includes a first cylindrical section 101, a first conical section 102, and a second cylindrical section 103, which are smoothly connected in sequence from the top to the bottom of the first reactor 100, wherein the inner diameter of the first cylindrical section 101 is greater than the inner diameter of the second cylindrical section 103.

[0048] The second reactor 200 is arranged in the tower body 10 and is sleeved on the outer circumference of the first reactor 100, and has a second output end at the bottom, wherein the first output end of the first reactor 100 extends out of the second output end of the second reactor 200 to prevent the flue gas and oxidizing steam outputted from the first reactor 100 from rising and entering the second reactor 200. The top of the second reactor 200 is connected to the flue gas output pipe 12, and the side wall of the second reactor 200 is also provided with a flue gas inlet pipe 13.

[0049] In some specific embodiments, the first end of the flue gas output pipe 12 is in communication with the top of the second reactor 200, and the second end of the flue gas output pipe 12 extends out of the tower body 10, and is used to output the flue gas to the outside of the tower body 10. The first end of the flue gas inlet pipe 13 is in communication with the side wall of the second reactor 200, and the second end of the flue gas inlet pipe 13 is in communication with the interior of the tower body 10, and is used to transport the flue gas after oxidation decomposition in the tower body 10 to the second reactor 200. Since the oxidation decomposition products of methane in the flue gas are carbon dioxide and water, the flue gas after oxidation decomposition is a gas-liquid mixture, which enters the second reactor 200 through the flue gas inlet pipe 13 for gas-liquid separation, and the separated gas phase will be output from the tower body 10 through the flue gas output pipe 12, and the separated liquid phase will flow out from the second output end of the second reactor 200.

[0050] The number of the flue gas inlet pipe 13 is at least one. In some preferred embodiments, the number of the flue gas inlet pipe 13 is at least two, and is configured so that the input flue gas after oxidation and decomposition forms a cyclonic wind field in the second reactor 200 to improve the gas-liquid separation effect. Figure 3 As shown, the number of the flue gas inlet pipes 13 is two, and they are symmetrically arranged relative to the axis center of the second reactor 200.

[0051] In some specific embodiments, the second reactor 200 includes a third cylindrical section 201, a second conical section 202 and a fourth cylindrical section 203, which are smoothly connected in sequence from the top to the bottom of the second reactor 200, wherein the inner diameter of the third cylindrical section 201 is greater than the inner diameter of the fourth cylindrical section 203.

[0052] The second spray assembly 400 is used to transport the oxidizing solution to the outside of the second reactor 200. The waste heat of the flue gas output from the first output end of the first reactor 100 can vaporize the oxidizing solution, thereby increasing the concentration of the oxidizing steam and further improving the oxidative decomposition efficiency of methane.

[0053] In some specific embodiments, the second spray assembly 400 includes: at least one second nozzle pipe 401, and the second nozzle pipe 401 includes: an annular pipe section surrounding the outer circumference of the second reactor 200, and the annular pipe section is evenly provided with a plurality of second nozzles 402, wherein the input end of the second nozzle pipe 401 extends out of the tower body 10.

[0054] In order to accelerate the oxidative decomposition process of the flue gas and make the escaped methane decompose more thoroughly, a first catalyst packing layer 500 can be provided inside the tower body 10, and the first catalyst packing layer 500 is located at the periphery of the second reactor 200 and below the flue gas inlet pipe 13. In some embodiments, the first catalyst packing layer 500 is located between the flue gas inlet pipe 13 and the second spray assembly 400. Figure 5 The cross-sectional view of a first catalyst filler layer 500 is shown. The first catalyst filler layer 500 may include conventional catalyst fillers as long as they can play a catalytic role. As an example, the catalyst filler is an oxide filler of metals such as manganese, copper, and titanium.

[0055] In some embodiments, the oxidation tower further comprises: a heat exchange coil 600, which is arranged in the tower body 10, and is sleeved on the outer periphery of the second reactor 200, and is located below the flue gas inlet pipe 13. In some embodiments, the heat exchange coil 600 is also located below the first catalyst packing layer 500. The heat exchange coil 600 is used to absorb the waste heat of flue gas and oxidizing steam, wherein the oxidizing steam will produce a temperature drop after absorbing heat, and then precipitate small droplets, which will fall to the bottom of the tower body 10. When the heat exchange coil 600 is working, a waste heat recovery medium such as cold water is input at the input end of the heat exchange coil 600, and the waste heat recovery medium flows in the heat exchange coil 600, absorbs the waste heat to form hot water or steam, and is discharged from the tower body 10 at the output end of the heat exchange coil 600.

[0056] In some embodiments, the oxidation tower further includes: a third spray assembly 700 for conveying an oxidizing solution into the second reactor 200, which can oxidize the flue gas input into the second reactor 200 again, thereby improving the oxidation treatment effect of the oxidation tower.

[0057] In some specific embodiments, the third spray assembly 700 includes: a third spray head 701 and a third spray head pipe 702, wherein the third spray head 701 is disposed on the inner side wall of the second reactor 200 and is located above the flue gas inlet pipe 13. A first end of the third spray head pipe 702 is connected to the third spray head 701, and a second end of the third spray head pipe 702 extends out of the tower body 10.

[0058] In some specific embodiments, the input ends of the first nozzle pipe 302 of the first spray assembly 300 , the second nozzle pipe 401 of the second spray assembly 400 , and the third nozzle pipe 702 of the third spray assembly 700 are connected to a delivery pipe for the oxidizing liquid outside the tower body 10 .

[0059] The overall operation process of the oxidation tower of the embodiment of the present application will be further described below.

[0060] The flue gas is input into the first reactor 100 through the flue gas input pipe 11, and the oxidizing solution is transported into the first reactor 100 through the first spray assembly 300. The high temperature of the flue gas causes the oxidizing solution to vaporize and undergo an oxidation reaction. The formed gas-liquid vapor is output through the first output end of the first reactor 100, and the liquid phase drips to the bottom of the tower body 10. The gas phase contacts the oxidizing solution sprayed by the second spray assembly 400 to vaporize and undergo an oxidation reaction. The liquid phase generated in this process drips to the bottom of the tower body 10, and the oxidizing solution in the flue gas is removed. The concentration of the steam is further increased, and the steam enters the first catalyst packing layer 500 to undergo a catalytic oxidation reaction, oxidizing and decomposing the methane in the flue gas. The output gas-liquid mixture enters the second reactor 200 through the flue gas inlet pipe 13 for gas-liquid separation, and the oxidizing solution is transported into the second reactor 200 through the third spray assembly 700 to oxidize the flue gas again. The separated gas phase is discharged from the tower body 10 through the flue gas output pipe 12, and the separated liquid phase is output through the second output end of the second reactor 200 and drips to the bottom of the tower body 10. In this way, efficient decomposition of escaping methane in the flue gas is achieved.

[0061] The oxidation tower of the embodiment of the present application can be applied to the flue gas oxidation demethanization system of a ship dual-fuel engine.

[0062] In some embodiments, reference Figure 6 The system includes: an oxidation tower 1, an oxidizing solution recovery device 2 and a liquid replenishing device 3, wherein the oxidation tower 1 is used to input flue gas and oxidizing solution, and output treated flue gas and unreacted oxidizing solution, and its structure can refer to the oxidation tower of the aforementioned embodiment. The oxidizing solution recovery device 2 is used to recover unreacted oxidizing solution and transport the unreacted oxidizing solution to the oxidation tower 1 to complete the recovery and reuse of the oxidizing solution. The liquid replenishing device 3 is used to replenish the oxidizing solution to the oxidation tower 1.

[0063] Combination Figure 1 , Figure 6 and Figure 7 The oxidizing solution recovery device 2 includes a liquid inlet and a liquid outlet, and the liquid inlet is connected to the outlet at the bottom of the tower body 10, and the liquid outlet is connected to the first spray assembly 300 and the second spray assembly 400. Specifically, the liquid outlet is connected to the first spray head pipeline 302 of the first spray assembly 300 and the second spray head pipeline 401 of the second spray assembly 400.

[0064] In some embodiments, the system further includes an oxidation dehydration device 4 for oxidizing and dehydrating the treated flue gas output from the oxidation tower 1. The oxidation dehydration device 4 may include: an oxidation dehydration chamber 41, a second catalyst packing layer 42, a fourth spray assembly 43, and a demisting assembly 44.

[0065] The side wall of the oxidation dehydration chamber 41 is provided with a smoke inlet, the top is provided with a smoke outlet, and the bottom is provided with a liquid outlet, wherein the smoke inlet is connected to the smoke output pipe 12, and is used to input treated smoke into the interior of the oxidation dehydration chamber 41, and the smoke outlet is used to output clean smoke, that is, demethanized smoke, and the liquid outlet is connected to the liquid outlet end of the oxidizing solution recovery device 2, and is used to output the liquid output by the oxidation dehydration device 4 to the liquid outlet end of the oxidizing solution recovery device 2.

[0066] The second catalyst packing layer 42 is arranged inside the oxidation dehydration cavity 41 and above the smoke inlet. The second catalyst packing layer 42 may include a conventional catalyst packing, which may be the same or different from the material of the first catalyst packing layer 500 as long as it can play a catalytic role. As an example, the catalyst packing is an oxide packing of metals such as manganese, copper, and titanium. The structure of the second catalyst packing layer 42 may refer to the first catalyst packing layer 500.

[0067] The fourth spray assembly 43 is used to spray the oxidizing solution above the second catalyst packing layer 42. The fourth spray assembly 43 may include a fourth nozzle pipeline and a fourth nozzle, wherein the first end of the fourth nozzle pipeline is connected to the liquid outlet of the oxidizing solution recovery device 2, and the second end of the fourth nozzle pipeline is connected to the fourth nozzle.

[0068] The demisting assembly 44 is arranged inside the oxidation dehydration chamber 41 and close to the smoke outlet for dehydrating the smoke. The specific structure of the demisting assembly 44 is not required, as long as it can play a dehydrating role.

[0069] After the treated flue gas is transported to the interior of the oxidative dehydration chamber 41, it enters the second catalyst packing layer 42. At the same time, the oxidizing solution is sprayed into the second catalyst packing layer 42 through the fourth spray assembly 43. The flue gas and the oxidizing solution are in countercurrent contact in the second catalyst packing layer 42. The oxidizing solution can catalytically oxidize the remaining methane, thereby improving the methane removal rate of the flue gas.

[0070] The unreacted oxidizing solution in the oxidation and dehydration chamber 41 will be output to the liquid outlet of the oxidizing solution recovery device 2 through the liquid outlet of the oxidation and dehydration chamber 41, and after merging with the unreacted oxidizing solution output from the liquid outlet of the oxidizing solution recovery device 2, it will be output to the first spray component 300, the second spray component 400, the third spray component 700 and the fourth spray component 43 to achieve the recovery and reuse of the oxidizing solution.

[0071] In some embodiments, the system further includes a first heat exchange device 5 and a second heat exchange device 6. The first end of the first heat exchange device 5 is connected to the flue gas output pipe 12, and the second end is connected to the smoke inlet of the oxidation dehydration chamber 41, and is used to cool the flue gas supplied to the inside of the oxidation dehydration chamber 41 to a first target temperature. The first end of the second heat exchange device 6 is connected to the liquid outlet of the oxidizing solution recovery device 2, and the second end is connected to the fourth spray assembly 43, and is used to cool the oxidizing solution supplied to the fourth spray assembly 43 to a second target temperature. As an example, the first target temperature and the second target temperature are 25~35°C.

[0072] In some specific embodiments, the first heat exchange device 5 and the second heat exchange device 6 are both seawater heat exchangers, and low-temperature seawater is transported to the first heat exchange device 5 and the second heat exchange device 6 by a seawater pump to absorb heat, and the formed high-temperature seawater will be discharged.

[0073] The rehydration device 3 is connected to the tower body 10 and is used to replenish the oxidizing solution into the tower body 10. In some embodiments, when it is detected that the pH value of the oxidizing solution at the liquid outlet of the oxidizing solution recovery device 2 decreases and increases, it means that the oxidizing property of the oxidizing solution in the system decreases, and it is necessary to replenish new oxidizing solution into the tower body 10 through the rehydration device 3. In some embodiments, the system further includes a pH detection device 7 for monitoring the pH value of the oxidizing solution at the liquid outlet of the oxidizing solution recovery device 2.

[0074] In some specific embodiments, a circulation pump 8 is further provided at the liquid outlet of the oxidizing solution recovery device 2, and the circulation pump 8 is used to transport the unreacted oxidizing solution. The liquid replenishing device 3 is connected to the tower body 10 through a supplementary pump 9, and the supplementary pump 9 is used to input the oxidizing solution in the liquid replenishing device 3 into the tower body 10.

[0075] The following combination Figure 1 and Figure 7 The overall operation process of the ship dual-fuel engine flue gas oxidation demethanization system is further described.

[0076] The flue gas is input into the first reactor 100 through the flue gas input pipe 11, and the oxidizing solution is transported into the first reactor 100 through the first spray assembly 300. The high temperature of the flue gas causes the oxidizing solution to vaporize and undergo an oxidation reaction. The formed gas-liquid vapor is output through the first output end of the first reactor 100, and the liquid phase drips to the bottom of the tower body 10 and is output to the oxidizing solution recovery device 2. The gas phase contacts the oxidizing solution sprayed by the second spray assembly 400 to vaporize and undergo an oxidation reaction. The liquid phase generated in this process drips to the bottom of the tower body 10 and is output to the oxidizing solution recovery device 2. The concentration of the oxidizing vapor in the flue gas is further increased, and enters the first catalyst packing layer 500 to undergo catalysis. Oxidation reaction, oxidatively decomposes the methane in the flue gas, and the output gas-liquid mixture enters the second reactor 200 through the flue gas inlet pipe 13 for gas-liquid separation, and the oxidizing solution is transported to the second reactor 200 through the third spray assembly 700 to oxidize the flue gas again. The separated liquid phase is output through the second output end of the second reactor 200, drips to the bottom of the tower body 10, and is output to the oxidizing solution recovery device 2. The separated gas phase is discharged from the tower body 10 through the flue gas output pipe 12, and after being cooled to the first target temperature by the first heat exchange device 5, enters the oxidation and dehydration chamber 41 for oxidation and dehydration treatment, and outputs demethanized flue gas, thereby realizing the demethanization treatment of the flue gas of the ship LNG dual-fuel engine. The liquid generated by oxidation and dehydration is output to the liquid outlet of the oxidizing solution recovery device 2, and after merging with the unreacted oxidizing solution output from the liquid outlet of the oxidizing solution recovery device 2, it is output to the first spray assembly 300, the second spray assembly 400, the third spray assembly 700 and the fourth spray assembly 43. Before being transported to the fourth spray assembly 43, it is cooled to the second target temperature by the second heat exchange device 6 to achieve the recovery and reuse of the oxidizing solution. During the above oxidation treatment process, the pH value of the oxidizing solution at the liquid outlet of the oxidizing solution recovery device 2 is monitored by the pH detection device 7. When the pH value is detected to increase or decrease, the new oxidizing solution is added to the tower body 10 by the liquid replenishment device 3.

[0077] It should be noted that different embodiments may produce different beneficial effects. In different embodiments, the beneficial effects that may be produced may be any one or a combination of the above, or any other beneficial effects that may be obtained.

[0078] The basic concepts have been described above. Obviously, for those skilled in the art, the above detailed disclosure is only for example and does not constitute a limitation of this specification. Although not explicitly stated here, those skilled in the art may make various modifications, improvements and corrections to this application. Such modifications, improvements and corrections are suggested in this specification, so such modifications, improvements and corrections still belong to the spirit and scope of the exemplary embodiments of this application.

[0079] It should be noted that in the description of this application, unless otherwise clearly specified and limited, the terms "installation", "connection", "connected", "connection", and "fixation" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a rotational connection or a sliding connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the internal connection of two elements or the interaction relationship between two elements. For ordinary technicians in this field, the specific meanings of the above terms in this application can be understood in combination with specific circumstances.

[0080] In addition, when terms such as "first", "second", and "third" are used in the specification of this application to describe various features, these terms are only used to distinguish these features and cannot be understood as indicating or implying the relationship between the features, the relative importance, or implicitly indicating the number of features indicated.

[0081] In addition, the present specification describes exemplary embodiments by reference to idealized exemplary cross-sectional views and / or plan views and / or stereograms. Therefore, differences from the illustrated shapes due to, for example, manufacturing techniques and / or tolerances are foreseeable. Therefore, the exemplary embodiments should not be interpreted as being limited to the shapes of the regions shown herein, but should include deviations in shapes caused by, for example, manufacturing. Therefore, the regions shown in the figures are schematic in nature, and their shapes are not intended to illustrate the actual shapes of the regions of the device nor to limit the scope of the exemplary embodiments.

[0082] At the same time, the present application uses specific words to describe the embodiments of this specification. For example, "one embodiment", "an embodiment", and / or "some embodiments" refer to a certain feature, structure or characteristic related to at least one embodiment of the present application. Therefore, it should be emphasized and noted that "one embodiment" or "an embodiment" or "an alternative embodiment" mentioned twice or more in different positions in the present application does not necessarily refer to the same embodiment. In addition, some features, structures or characteristics in one or more embodiments of the present application can be appropriately combined.

[0083] Similarly, it should be noted that in order to simplify the description disclosed in this application and thus help understand one or more embodiments, in the above description of the embodiments of this application, multiple features are sometimes combined into one embodiment, figure or description thereof. However, this disclosure method does not mean that the features required by the object of this application are more than the features mentioned in the claims. In fact, the features of the embodiments are less than all the features of the single embodiment disclosed above.

[0084] Finally, it should be understood that the embodiments described in this application are only used to illustrate the principles of the embodiments of the present application. Other variations may also fall within the scope of the present application. Therefore, as an example and not a limitation, the alternative configurations of the embodiments of the present application may be considered to be consistent with the teachings of the present application. Accordingly, the embodiments of the present application are not limited to the embodiments explicitly introduced and described in the present application.

Claims

1. A ship dual-fuel engine flue gas oxidation demethanization oxidation tower, comprising a tower body (10), characterized in that: The oxidation tower also includes: A smoke inlet pipe (11) and a smoke outlet pipe (12); A first reactor (100) is disposed in the tower body (10) and is connected to the flue gas input pipe (11), and has a first output end at the bottom; A second reactor (200) is arranged in the tower body (10) and is sleeved on the outer circumference of the first reactor (100), and has a second output end at the bottom, wherein the first output end extends out of the second output end, the top of the second reactor (200) is connected to the smoke output pipe (12), and a smoke inlet pipe (13) is also provided on the side wall of the second reactor; A first spray assembly (300) is used to transport an oxidizing solution into the interior of the first reactor (100); The second spray assembly (400) is used to transport the oxidizing solution to the outside of the second reactor (200).

2. The ship dual-fuel engine flue gas oxidation demethanization oxidation tower according to claim 1, characterized in that: The first reactor (100) comprises a first cylindrical section (101), a first conical section (102) and a second cylindrical section (103) which are smoothly connected in sequence, wherein the inner diameter of the first cylindrical section (101) is greater than the inner diameter of the second cylindrical section (103).

3. The ship dual-fuel engine flue gas oxidation demethanization oxidation tower according to claim 1, characterized in that: The first output end of the first reactor (100) comprises at least two air guide pipes (104), and the air outlets at the ends of each of the air guide pipes (104) are bent together in a clockwise or counterclockwise direction.

4. The ship dual-fuel engine flue gas oxidation demethanization oxidation tower according to claim 1, characterized in that: The second reactor (200) comprises a third cylindrical section (201), a second conical section (202) and a fourth cylindrical section (203) which are smoothly connected in sequence, wherein the inner diameter of the third cylindrical section (201) is greater than the inner diameter of the fourth cylindrical section (203).

5. The ship dual-fuel engine flue gas oxidation demethanization oxidation tower according to claim 1, characterized in that: The first spray assembly (300) comprises: A first nozzle (301) is disposed on the top of the first reactor (100); A first nozzle pipe (302) has one end connected to the first nozzle (301) and the other end extending out of the tower body (10).

6. The ship dual-fuel engine flue gas oxidation demethanization oxidation tower according to claim 1, characterized in that: The second spray assembly (400) comprises: at least one second spray head pipe (401), and the second spray head pipe (401) comprises: an annular pipe section surrounding the outer circumference of the second reactor (200), and the annular pipe section is evenly provided with a plurality of second spray heads (402), wherein the input end of the second spray head pipe (401) extends out of the tower body (10).

7. The ship dual-fuel engine flue gas oxidation demethanization oxidation tower according to claim 1, characterized in that: The oxidation tower further comprises: a first catalyst packing layer (500) disposed in the tower body (10), located on the outer periphery of the second reactor (200), and located below the flue gas inlet pipe (13).

8. The ship dual-fuel engine flue gas oxidation demethanization oxidation tower according to claim 1, characterized in that: The oxidation tower further comprises: a heat exchange coil (600), which is arranged in the tower body (10), sleeved on the outer periphery of the second reactor (200), and located below the flue gas inlet pipe (13).

9. The ship dual-fuel engine flue gas oxidation demethanization oxidation tower according to claim 1, characterized in that: The number of the flue gas input pipes (11) is two, and the two flue gas input pipes (11) are symmetrically arranged relative to the center of the axis of the first reactor (100); And / or, the number of the flue gas inlet pipes (13) is two, and the two flue gas inlet pipes (13) are symmetrically arranged relative to the axis center of the second reactor (200).

10. The ship dual-fuel engine flue gas oxidation demethanization oxidation tower according to claim 1, characterized in that: The oxidation tower further comprises: a third spray assembly (700) for conveying an oxidizing solution into the second reactor (200), and the third spray assembly (700) comprises: a third nozzle (701) disposed on the inner wall of the second reactor (200) and located above the flue gas inlet pipe (13); A third nozzle pipe (702) has one end connected to the third nozzle (701) and the other end extending out of the tower body (10).

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