TW201100164A - Plasma assisted catalyst reformation apparatus and method - Google Patents

Abstract

A plasma enhanced catalyst recombination apparatus including a feeder, a plasma reactor, a recombination reactor and a pre-heater is provided. A first recombination cavity of the recombination reactor is connected with a plasma cavity of the plasma reactor, and the recombination reactor is disposed inside a pre-heating cavity of the pre-heater. A pre-heating pipe of the pre-heater is connected between a mixing room of the feeder and the plasma cavity, and some portion of the pre-heating pipe is disposed inside the pre-heating cavity. The first recombination cavity is disposed inside a second recombination cavity of the recombination reactor. One end of a recirculation pipe of the recombination reactor is connected with a first recombination opening of the first recombination cavity and is disposed inside the first recombination cavity. Another end of the recirculation pipe is passes through a second recombination outlet of the second recombination cavity and is disposed inside the pre-heating cavity. Besides, a plasma enhanced catalyst recombination method is also provided.

Description

201100164 VI. Description of the Invention: [Technical Field] The present invention relates to a catalyst recombination apparatus and method, and more particularly to a plasma assisted catalyst recombination apparatus and method. [Prior Art] With the advancement of technology, the available energy has also become more diversified, and in particular, the conversion of fossil fuel or biomass fuel into hydrogen fuel can be achieved through catalyst recombination. In general, natural gas, alcohol, decane, butane and other hydrocarbon gases or hydrocarbon liquids can be converted to helium fuel at high temperatures through recombination of the catalyst, which is currently considered to be more environmentally friendly. One of the fuels. The conventional catalyst recombination device must first use an auxiliary burner or an electric heater to heat the catalyst bed first, until the catalyst bed reaches the working temperature, and then the heated hydrogen sulfide gas and the air are subjected to partial oxidation recombination reaction to be converted into Helium, and the heat generated by the partial oxidation recombination reaction to maintain the temperature of the catalytic bed Q, thereby turning off the auxiliary burner or the electric heater. However, auxiliary burners or electric heaters are usually bulky and dangerous components and are only used to heat the catalyst bed first, and there is very little efficiency in use. Another conventional catalyst recombination device is used for the recombination of hydrocarbon liquids, mainly by using a boiler to heat a hydrocarbon liquid and water to vaporize it into a high temperature gas, thereby heating the catalyst bed for recombination reaction, so the catalyst The reconstitution unit must continue to operate the boiler to heat the hydrocarbon liquid and water. However, the efficiency of boiler heating is too low, resulting in a large energy loss, and the boiler is usually a large and dangerous component of the body 201100164. In addition, the conventional technique also proposes an electric-assisted catalyst recombination device, which generates a high-voltage high-frequency alternating current %, thereby generating a discharge to add a gas and air, thereby (4) < carbon argon. The gas and air are heated for 2 beds to cause the catalyst bed to reach the temperate temperature to produce a recombination reaction. When the catalyst::: degree reaches the upper limit value, 'the power of the electropolymer reactor can be cut off, and when the μ degree drops to the lower limit value, the plasma reactor power is restored. In addition, the US 632 The ^ patent, the US sixth, the outline, the 95 = =, the US 6,506, 359 patent is a little more than the aforementioned conventional skills. (However, whether it is for carbon hydride or money (four), all are equipped with heating H has the temperature of the heating catalyst bed to reach the temperature of the maintenance, so that the overall weight of the weight (4) is very large, and it is not dangerous. In addition, the addition and subtraction rate of the heating utility is not ideal, and both are in the process of extinguishing the medium. A lot of energy is wasted. 〇 [Summary] In view of this, the object of the present invention is to provide a plasma-assisted catalyst weight, device, and a high-temperature recombination reactor coated in a preheater, and The blind configuration to guide the heat source can effectively utilize the heat source and greatly reduce the volume of the catalyst recombination device. Further, another object of the present invention is to provide a plasma-assisted catalyst recombination method, which utilizes a mist for a hydrocarbon liquid first. After heating, the hydrocarbon liquid is heated and steamed. Since the atomized hydrocarbon liquid has a large surface area, the heating efficiency can be greatly improved. 201100164 For the above or other purposes, the present invention provides a plasma assisted catalyst recombining device, including a feeder and a plasma. a reactor, a recombination reactor, and a preheating reactor in which the recombination reactor is connected to a plasma reactor. The feeder has a mixing to 'the plasma reactor includes a plasma chamber, a plasma electrode, and a plasma power supply unit, The plasma chamber has a plasma chamber inlet and a plasma chamber outlet, and the plasma power supply unit is coupled to the plasma chamber and the plasma electrode, so as to generate a t (disetoge). The recombination reactor includes A recombination chamber, a recombination chamber, a recirculation tube, a perforated plate, and a first catalyst bed. 1 see that the f group cavity has a first-recombination cavity population, a first-recombination cavity outlet and a first group cavity opening, and the first recombination cavity The inlet is connected to the outlet of the plasma chamber. The cavity is located in the second recombination chamber, and the second recombination chamber has the outlet of the first recombination chamber. The recirculation tube is the inner recirculation tube--the age of the cavity 'And-end is the m' cavity Opening, and the recirculation tube is another: the first recombination chamber outlet passes through the second recombination chamber outlet-first recombination chamber and is adjacent to the first re-nuclear chamber inlet. a cavity and a second recombination cavity. Pre-t7 cavity and a sluice tube, wherein the recombination reaction is located in the pre-chamber cavity... and the preheating cavity has a preheating cavity population and a preheating cavity outlet. In the preheating chamber, and surrounding the recombination reactor, the end is connected to the entrance of the electric chamber, and the other inlet of the preheating tube is connected to the mixing t. The cavity is for the above or other purposes, and the invention further provides a touch The medium recombination method includes the following steps: providing a piezoelectric atomizing unit to supply air; mixing air and atomized carbon = body and water injury, relatively atomized carbon test body and water money; providing electric equipment counter 7 201100164 Exciting the air and the vaporized hydrocarbon liquid and water into a quasi-neutral mixed gas; providing a recombination reactor to recombine the quasi-neutral mixed gas to form a high temperature reaction gas, and recombining the high temperature reaction gas to form a high temperature reformed gas, and High temperature recombination gas suitable for heating fog The hydrocarbon liquid and water are used to vaporize the atomized hydrocarbon liquid and water. In an embodiment of the invention, the air and the hydrocarbon gas are mixed in the mixing chamber and enter the plasma chamber along the preheating tube to become a quasi-neutral mixed gas, and the quasi-neutral mixed gas enters the first recombination chamber. Internally, the first catalyst bed is recombined to form a high-temperature reaction gas, and the high-temperature reaction gas enters the second recombination chamber from the outlet of the first recombination chamber to be recombined in the first catalyst bed to form a high-temperature recombination gas, and the high-temperature recombination gas The gas enters the recirculation tube from the first recombination chamber opening and enters the preheating chamber along the recirculation tube to heat the air and hydrocarbon gas in the preheating tube and exit the preheating chamber from the preheating chamber outlet. In an embodiment of the invention, the feeder may further have a first regulating valve and a second regulating valve, and the first regulating valve and the second regulating valve are connected to the mixing chamber to respectively control air and carbon helium gas. The flow into the mixing chamber. q In one embodiment of the invention, the portion of the recirculation tube described above within the first recombination chamber is, for example, a coil. * In an embodiment of the invention, the direction in which one end of the preheating tube is connected to the inlet of the electro-plasma chamber is, for example, offset from the center of the plasma chamber. In an embodiment of the invention, the preheater may further include a disk-shaped preheating passage disposed in the preheating chamber and connected between one end of the preheating tube and the inlet of the plasma chamber. In an embodiment of the present invention, the recombination reactor may further include a first partition plate and a second partition plate, and the first partition plate is disposed in the first weight 8 201100164 group cavity, and the first The two partition plates are disposed in the second recombination chamber. The first divider can be a cross divider or a ticker. In an embodiment of the present invention, the preheater may further include a third 'dividing plate, and the third dividing plate is disposed in the preheating chamber to distinguish the preheating cavity into a connected one. The first preheating zone and the second preheating zone. Further, the preheating tube is a double-layered recombination reactor along the first preheating zone and the second preheating zone. In addition, the preheater may further include a second catalyst bed, a third catalyst bed and a fourth catalyst bed, wherein the second catalyst bed is located in the first preheating zone, and the third catalyst bed is located in the first preheating zone. At the junction of the hot zone and the second preheating zone, the fourth catalyst bed is located in the second preheating zone. The second catalyst bed may have a high temperature water gas shift catalyst, and the third catalyst bed may have a low temperature water gas shift catalyst, and the fourth catalyst bed may have a carbon monoxide selective oxidation catalyst. In an embodiment of the invention, the feeder is further provided with a piezoelectric atomizing unit, and the piezoelectric atomizing unit is connected to the mixing chamber. The hydrocarbon liquid and water are formed into a mixing chamber by forming an atomized hydrocarbon liquid and water in the piezoelectric atomizing unit, and are mixed with the air entering the mixing chamber to enter the preheating tube, and the mist-hydrogenated hydrocarbon liquid Forming a vaporized carbon crucible liquid and moisture with water in the preheating tube, and entering the plasma chamber along the preheating tube to form a quasi-neutral mixture, and the quasi-neutral mixed gas enters the first recombination chamber Recombining in the first catalyst bed to form a high-spiking reaction gas, and the high-temperature reaction gas is recombined in the first catalyst bed to form a high-temperature recombination gas from the outlet of the first recombination chamber into the second recombination chamber, The high temperature reformed gas enters the recirculation pipe from the opening of the first recombination chamber, and enters the preheating chamber along the recirculation tube to heat the air in the preheating tube, the atomized hydrocarbon liquid and the atomized water, and self preheating The chamber outlet exits the preheating chamber. 9 201100164 In an embodiment of the invention, the hydrocarbon liquid described above is, for example, alcohol or liquefied petroleum gas. In an embodiment of the invention, the feeder may further have a first regulating valve, a third regulating valve and a fourth regulating valve, and the first regulating valve is connected to the mixing chamber to control the air flow, and the third regulating The valve and the fourth regulating valve are connected to the piezoelectric atomizing unit to separately control the flow rate of the carbon dioxide liquid and the water. In an embodiment of the invention, the preheating chamber further has a preheating chamber opening to allow air to enter the preheating chamber from the preheating chamber opening. In addition, the 0 feeder has a fifth regulator valve, and the fifth regulator valve is connected to the preheat chamber opening to control the air flow. In summary, in the plasma assisted catalyst recombination apparatus and method of the present invention, by the arrangement of the recirculation pipe, the temperature of the catalyst bed can be uniformly distributed and the air and the hydrocarbon gas can be uniformly flowed through the porous The catalyst is fully utilized to reduce the volume of the plasma-assisted catalyst recombination device and to increase the efficiency of carbon monoxide gas recombination into hydrogen. The above and other objects, features, and advantages of the present invention will become more apparent from the understanding of the appended claims. 1A is a cross-sectional view of a plasma assisted catalyst recombination apparatus according to an embodiment of the present invention, and FIG. 1B is a cross-sectional view of the plasma assisted catalyst recombination apparatus of FIG. 1A, which is omitted from the first catalyst bed. . Referring to FIGS. 1A to 1B, the plasma assisted catalyst recombination apparatus 1 of the present invention includes a plasma reactor 110, a recombination reactor 120, a preheater 130, and a feeder 140, and these 10 201100164 components are complicated. The connection method is the spirit of the present invention, so as to achieve the purpose of heart recombination efficiency and heat source use efficiency. The following describes the respective components and their connection relationship, and then describes the detailed process of the reorganization of the present invention. The plasma reactor 110 includes a plasma chamber 112, a plasma electrode 114 and a plasma power supply unit 116, wherein the plasma power supply unit 116 is coupled between the plasma chamber 112 and the plasma electrode 114. By supplying high-voltage high-frequency alternating current, an arc discharge can be generated in the plasma chamber 112 to free the gas in the cavity 112 (afterwards) Further, this gas is a mixed gas such as air, hydrocarbon gas or vaporized hydrocarbon liquid). In addition, the plasma chamber 112 has a plasma chamber inlet 112a and an electropolymer chamber outlet 112b', and the aforementioned gas enters the plasma chamber 112 from the plasma chamber inlet i12a, and is discharged from the plasma chamber outlet U2b after being released. Leaving the electropolymerization chamber 112' wherein the electropolymerization reactor no is connected to the recombination reactor 120, and the gas leaving the plasma chamber 112 enters the recombination reactor 120. The recombination reactor 120 includes a first recombination chamber 121, a second recombination chamber Q body 122, a recirculation tube I23, a perforated plate 124, and a first catalyst bed 125, wherein the first recombination chamber 121 is located in the second recombination chamber 122, and the first catalyst bed 125 is disposed in the first recombination cavity 121 and the second recombination cavity 122. In this embodiment, the first recombination cavity 121 and the second recombination cavity 122 are all in the shape of a barrel, and the center lines of the first recombination cavity 121 and the second re-ball cavity 122 are overlapped and aligned. The centerline of the slurry cavity 112 is convenient for assembly operations. However, the present invention does not limit the shape of the first recombination cavity 121 and the second recombination cavity 122. 201100164 (2) m: the recombination cavity 121 has a relative first-recombination cavity inlet, a third weight, and a cavity outlet 121b, and the first heavy-duty inlet 12 is connected to the plasma chamber outlet 112b, with #_工连σ & The free rolling body can be made into the first tongue and groove pure from the first recombination chamber inlet 121a, and the m should be in the virtual chamber inlet 121a and the first catalyst bed (2) is recombined with the first unit bed σ 121b into the f-weight, cavity 122 internal and the first - catalyst bed Π 5 for recombination reaction 0 Ο

That is, according to the flow direction of the gas in the first catalyst bed 125, the first catalyst bed 125 A can be divided into a recombination reaction front stage located in the first-recombination cavity m adjacent to the recombination chamber inlet 121a, and located in the first recombination chamber. The recombination reaction towel segment at the junction of the body κι and the first recombination cavity 122, and the recombination reaction segment located in the second recombination cavity 122 adjacent to a relocation chamber inlet 121& Of course, the process of dividing the first catalyst bed 125 into three sections is for convenience only, and Babe's process of recombination reaction is not different. In order to allow the gas to be evenly distributed from the first recombination chamber inlet 12ia into the first recombination chamber 121, the present invention can dispose the perforated plate 124 within the first recombination chamber 121 and adjacent to the first recombination chamber inlet i2la. As a result, the gas can be uniformly reacted with the first catalyst bed 125 through the porous plate 124 by the diffusion effect of the porous plate 124. Generally speaking, after the gas passes through the perforated plate 4, due to the geometric arrangement of the first recombination cavity 121 and the second recombination cavity 22, the gas still cannot pass the first catalyst bed 125 completely uniformly, but instead The shortest path passes through the first catalyst bed 125 to the first recombination chamber outlet 121b. These phenomena are often referred to as flow-short-circuit or channeling effects, which cause the gas to contact the most catalysts during the flow. In order to solve the above disadvantages, the present invention is in the first recombination chamber 1. The first recombination cavity opening 121C is opened, and the second recombination cavity 122 is opened, and the cavity outlet 122a, wherein the first recombination cavity opening 121c can be opened in the recombination reaction rear section area of the first catalyst bed 125 and the second The recombination chamber outlet, 12 仏 is adjacent to the first recombination chamber outlet 121b, and can be opened in the first catalyst bed 125 = recombination reaction mid-section region.

In response to the above, the recirculation tube 123 is partially located in the first recombination chamber 121 and one end of the recirculation officer 123 is connected to the first recombination chamber opening, and the other end of the circulation official 123 is pierced through the first recombination chamber outlet 121b. The second recombination chamber outlet 122a. The portion of the recirculation tube 123 in the first recombination chamber 121 can be considered an obstacle to prevent gas from passing through the recombination reaction front region of the first catalyst bed 125 in the shortest manner. In this way, the gas passes through the recombination reaction front region of the first catalyst bed 125 in a longer path, thereby contacting more catalyst to improve the efficiency of the recombination reaction. In addition, the portions of the recirculation tube 123 in the first recombination chamber 121 may be arranged in an irregular arrangement for the coil to avoid the aforementioned short-circuit problem of the air flow. Referring to FIGS. 1 to 1B, the preheater 13 includes a preheating chamber Η and a preheating tube 134, wherein the recombination reactor 120 is located in the preheating chamber 132 and the preheating chamber 132 has a preheating chamber. Exit 132b. When the gas flows through the rear reaction region of the first catalyst bed 125, it flows into the recirculation pipe 123 through the first recombination chamber opening 121c, and flows out of the recombination reactor 120 along the recirculation pipe. The gas entering the preheating chamber 132 and finally completing the recombination reaction will fill the entire preheating chamber 132 and exit the preheating chamber 13 201100164. The port 132 is collected and utilized. In addition, the preheating chamber 132 further has a preheating chamber inlet 132a, and the pre-flushing unit f 134 is disposed in the center of the preheating chamber 1 and surrounds the recombination reactor 120. Further, one end of the preheating 134 is connected to the plasma chamber inlet 112a, and the other end of the preheating 134 is a mixing chamber 142 which passes through the preheating chamber inlet U2a to connect the feeder 14'. As a result, the gas is initially mixed in the mixing chamber 142 and enters the electropolymerization chamber 112 via the preheating tube 134 for free reaction. The present invention is that the other end of the recirculation tube 123 can be disposed at any position within the preheating chamber 132 after passing through the second recombination chamber outlet 122a, and in this embodiment t, recirculation The other end of the tube 123 is disposed adjacent to the preheating tube 134 adjacent to the plasma chamber 112, thereby heating the gas in the preheating tube 134. After roughly explaining the complicated configuration between the respective members of the plasma assisted catalyst recombination apparatus 1 of the present invention, the operation flow of the plasma assisted catalyst recombination apparatus 100 will be specifically described below with the hydrocarbon gas of methane. However, the present invention does not limit the type of gas to be destroyed, and hydrocarbon gas such as ethylene, propylene, gas, etc. may also be used. In the process of recombination reaction with a catalyst, if hydrocarbon gas is required to recombine the desired hydrogen or carbon monoxide, the temperature of the catalyst must be higher than the working temperature, and the hydrocarbon gas is subjected to partial oxidation heavy reaction (incomplete Combustion) can be converted to hydrogen or carbon monoxide. In order to make the temperature of the catalyst higher than the working temperature, the present invention firstly introduces a hydrocarbon gas to perform a complete oxidation recombination reaction (complete combustion), thereby releasing a large amount of heat to the first catalyst bed 125 for preheating. . 14 201100164 、 When the temperature of the catalyst is higher than the working temperature, the hydrocarbon gas is changed to a partial oxidation recombination reaction to generate hydrogen, and the key condition for the hydrocarbon gas to undergo partial or partial total oxidation recombination reaction is Adjust the ratio of hydrogen-destroying gas to empty fluorine. In the case of methane, if the ratio of methane to air is lower, it is easier to carry out a complete oxidative recombination reaction. Conversely, if the ratio of a marry to air is higher, the partial oxidation recombination reaction is easier. In this way, the present invention does not require any additional auxiliary heaters, and the first catalyst bed 125 can be directly heated by the above-mentioned equipment to completely burn the hydrocarbon gas, thereby reducing the construction cost. Reduce the overall equipment volume and avoid the danger of setting up the auxiliary heater. Referring again to FIGS. 1A to 1B, the feeder 140 may further have a first regulator 145 and a second regulator 146, and the first regulator 145 and the second regulator 146 are coupled to the mixing chamber 142' to control the air ( The flow rate of entering the mixing chamber with methane (not shown). In the starting (preheating) phase of the embodiment, first, the first regulating valve 145 and the second regulating valve 146 are opened to mix air and decane into the mixing chamber 142, wherein the air to methane flow ratio ❹ is 20 : 1 (that is, the oxygen to carbon ratio is 4.2: 1). Then, air and methane enter the plasma chamber 112 along the preheating tube 134 and are activated by the discharge phenomenon in the plasma chamber 112. In detail, part of the air and methane will be subjected to high-energy electron impact of non-thermal plasma to cause Ionization, Dissociation, Excitation, etc., to form ions (Ion) and electrons. A quasi-neutral mixture of (Electron) and Free Radical (not shown). The aforementioned quasi-neutral mixed gas will enter the first recombination chamber 121 and 15 201100164 to fully burn, and release a large amount of heat to heat the first catalyst bed 12^, thereby making the first catalyst bed 125 The catalyst temperature rises. Although the fire can release the maximum heat when π is fully burned, the combustion occurs when the air is in contact with the first catalyst bed 125, so the heat released by the hospital cannot be completely passed through the gas. The phase (the line and the decane) is transferred to the first catalyst bed 125 by conduction to the solid phase (catalyst). It is worth noting that this embodiment first mixes air with decane and then Ο

Import the first catalyst $ 125. However, if the fired and air are introduced into the first catalyst bed 125, respectively, and then the air and the smoldering are mixed and burned, although the first, the medium bed 125 is composed of a porous catalyst, the porous catalyst = causing poor mixing of the burnt air and air, and the production line is not completely burnt. Generally speaking, the temperature of the first-stage, middle-stage and the middle of the recombination reaction is declining, and when the temperature of the trampoline 125 in the region before the recombination reaction exceeds the lower limit, the air can be adjusted. The ratio is such that methane can be progressively adjusted to be incompletely burned. Taking methane as an example, the temperature at the bottom limit is 550 ° C, and then the flow ratio of the air to the smoldering is 11.9: b. 14.76: 1 or 2 ί, that is, the oxygen to carbon ratio is 2· 5: Bu 3.1:...:D, in order to carry out a series of incomplete combustion of decane with two = gas, and the large amount of heat that is escaping continues to be heated through the gas phase to the solid phase to continuously heat the one-touch bed. 125. Brothers. (^) Since the catalyst temperature in the front region of the recombination reaction has exceeded the lower limit value C, a small portion of the unburned oxygen molecules in the air will partially oxidize and recombine with the methane molecules on the surface, and since this incomplete combustion is 16 201100164 src on the surface of each catalyst, so the heat released by this part will be directly transmitted. The temperature of the catalyst in the recombination reaction area will quickly mediate and make the reorganization of the upper:: empty two other The temperature rises in the area, and the value of the catalyst bed 125 is accelerated by 550. (: Above, the temperature of the catalyst bed 125 is kept at the bottom limit, but the limit is not exceeded by 9 〇〇 °C. _ Ο

The generated heat i:: whole: c-decane is completely burned with air Π5 in the recombination reaction; the catalyst bed 125, and the first media bed is 550. . Above:: If the temperature in the back section reaches the bottom limit, then the ratio of the air to the air will take part of the time to _ more (four) with the air, and consume a longer temperature of 4:::=25 When rising, it is close to, when C, that is, 25 in the front, middle and back regions of the recombination reaction, when the bottom limit is 55 G °C or more, the air and the ratio can be adjusted again to 9.52··1 or 8.57: 1 (that is, the ratio of oxygen to carbon is 2: i 5 2:8: 1), in order to further reduce the air and make the methane carry out different degrees of extraordinary total combustion, and release less heat contained in it to maintain the first The temperature of a catalyst bed 125. Since most of the temperature of the first catalyst bed 125 in the front, middle and rear sections of the recombination reaction is above the operating temperature, most of the oxygen molecules and methane molecules in the air are mostly in the first catalyst bed 125. The single catalyst surface undergoes stable partial oxidation recombination, and the heat released therefrom is directly transferred to each single catalyst to maintain the temperature of the first catalyst bed 125, so that 17 201100164 first catalyst bed 125 The temperature is maintained at 5, c~9 (10). c, that is, in the plasma-assisted catalyst recombination of the present invention, it is necessary to adjust the flow ratio of air to the burnt gas, and in the second gas, only the fuel preheater can make the first-catalyst bed 125 quickly = A large amount of consumption can be used to enable the plasma-assisted catalyst recombination device to complete the start-up (job_bed) process finer than the cost-saving Ο 完成 When the start-up procedure is completed, the following will be described again. Work. π Referring again to FIGS. 1A to 1B', similarly to the foregoing, the first axis is adjusted to the second and the second regulating valve 146 to mix the air with the f: the flow rate of the air and the fire is comparable to 9. Next, the air and the age of The process of heating and heating of the user f 134 will be described later in detail, and the electric heating is carried out along the preheating pipe 134: the body m' is formed by the discharge phenomenon in the plasma cavity 112, Electron and free (four) standard mixed gas (not (four)). In the present embodiment, the direction in which the preheating tube 134 is connected to the electrocavity chamber inlet U2a is, for example, offset from the center of the plasma chamber 112, so that air and nails are burned into the electropolymer chamber 112 to generate a female flow around the (four) electrode 114. Thereby, the air and the smoldering are more uniformly mixed to be activated into a scalloped mixed gas. Then, the quasi-neutral mixed gas enters the first recombination chamber 121' and the free generation molecule and the free oxygen molecule of the quasi-neutral mixed gas towel are in the case where the first-catalyst bed 125 is higher than the working temperature. Partial 〇xidati〇n Reforming reaction is carried out on the surface of the catalyst in the front part of the recombination reaction, and carbon monoxide, carbon dioxide, hydrogen and water are gradually produced. At this time, these carbon monoxide, oxidizing, Hydrogen, water (gaseous), unreacted nitrogen, unreacted formazan molecules and oxygen molecules form a south temperature reaction gas in the region before the recombination reaction of the first catalyst bed 125 (not shown). In response to the above, the high temperature reactive gas will enter the second recombination chamber 122 from the first recombination chamber outlet 121b to continue the reaction. Similarly, the unreacted methane molecules and oxygen molecules in the high temperature reaction gas will be in the middle and rear regions of the recombination reaction. The Partial Oxidation (Reforming) reaction is carried out on the surface of the catalyst to gradually convert the unreacted decane molecules and oxygen molecules into carbon monoxide, carbon dioxide, hydrogen and water (gaseous). As a result, the carbon monoxide, carbon dioxide, hydrogen, water (gaseous), and unreacted nitrogen in the rear region of the first catalyst bed 125 form a south temperature recombination gas (not shown). It is worth noting that the high temperature reaction gas and the high temperature reformed gas are only conceptual differences, and the present invention does not specifically distinguish the exact position where it is located. That is to say, the high-temperature reaction gas is only a general term for the partial oxidation recombination process, and the high-temperature reaction gas is only a general term for the partial oxidation recombination process, and it is easy to understand and not be confused when familiar with the technology. . Then, the still warming gas will enter the recirculation pipe 123 from the first recombination chamber opening 121c. In the foregoing description, the recirculation pipe 23 has a problem of avoiding the occurrence of a short circuit of the air flow, so that the quasi-neutral mixed gas can contact the most catalyst in the region before the recombination reaction through the first catalyst bed 125 to enhance Recombination efficiency and a significant reduction in the volume of the recombination reactor 12〇. In addition, the high temperature reformed gas can absorb the heat in the region of the first reaction bed 125 of the first catalyst bed 125 and transfer the heat to the recombination counter of the first catalyst bed 125. The temperature distribution of the first catalyst bed U5 is made uniform to further enhance the reaction effect of the entire first catalyst bed 125. Then, the high temperature reformed gas enters the preheating chamber 132 along the recirculation pipe 123 to heat the air and methane in the preheating tube 132, and the heated air and methane in the preamplifier tube 132 enter the plasma chamber. After body 112, it is easier to be activated and activated. That is, the present invention utilizes only the residual temperature of the high-temperature reformed gas to heat the air and methane without additionally providing an external heater, thereby reducing the construction cost and reducing the overall size of the apparatus. In this embodiment, the other end of the recirculation pipe 123 passes through the second recombination chamber outlet 122a and is disposed near the preheating tube 134 adjacent to the plasma chamber 112, so that the high temperature recombination gas just leaving the recombination reactor 120 The air and decane in the plasma chamber Π2 can be directly heated to maximize the residual heat of the high-temperature reformed gas. In addition, the portion of the preheating tube 134 in the preheating chamber 132 surrounds the recombination reactor 120', for example, in a double-layered manner to achieve heat absorption of the high temperature recombination gas and heat transfer to the recombination reactor 120. The effect, however, does not limit the manner in which the preheating tube 134 surrounds the recombination reactor 120. In addition, the preheater 130 is a coated recombination reactor 120, and the temperature distribution of the plasma assisted catalyst recombination device 100 can be gradually reduced from the internal high temperature recombination reactor 120 to the peripheral low temperature preheater 130. In order to improve the overall heat utilization rate, and avoid the risk of direct contact with the high temperature recombination reactor 120. Finally, the gradual cooling and hydrogen-rich high-temperature reformed gas will leave the preheating chamber 132 from the preheating chamber outlet 132b and be transported to the downstream device, 20 201100164 := after V treatment to supply fuel cells, internal combustion engines, etc. For the subsequent use 0 j, refer to FIG. 1Α~1Β' In the present embodiment, the recirculation pipes 123, ^ are in the shape of a single irregular coil in the cavity 121, and the Sis is used to prevent the quasi-middle. The mixed gas passes through the recombination reaction front region of the media bed 125 in the shortest manner. However, the present invention does not ::: follow the number and shape of the official 123, and when the number of the recirculation pipe 123 is Ο

::, ,, and strips' then the first recombination chamber ΐ2ι also needs to be re-opened to the first recombination chamber opening 121C. In order to improve the recombination efficiency of the first catalyst bed 125 in one step, the present invention can further provide a partition plate in the first recombination cavity 121 or the second recombination cavity 122. *Description, and for the sake of explanation, the same name and label are still used for the same function. 2A is a cross-sectional view of a plasma assisted catalyst recombination f according to another embodiment of the present invention, and omits the first catalyst bed, the recirculation tube and the first recombination chamber opening, and FIG. 2B is FIG. A top view of the section of the eight-recombination reactor along the AA line. 2A to 2B, the plasma assisted catalyst recombination apparatus 200 of the present embodiment is similar to the plasma assisted catalyst recombination apparatus 1 (shown in FIG. 1A), and the difference is only in the plasma assisted catalyst. The recombination reactor 220 of the reconstitution device further includes a first partitioning plate 226, and the first partitioning plate 226 is disposed in the first recombination cavity 121 to distinguish the first recombination cavity 121 from the plurality of respective recombination chambers 121. Independent first reaction zone S1. In the present embodiment, the first partitioning plate 226 is, for example, a cross partition plate to form four first reaction regions S1, wherein the cross-sectional area of each of the first reaction regions S1 is only the original first recombination cavity 121. 21/24 of the cross-sectional area 201100164 • One, that is, the equivalent diameter of the first reaction zone s 1 of the parent is one-half of the equivalent diameter of the first recombination cavity • 121, so each first reaction In the area S1, the "length to diameter ratio" is twice the length ratio of the first recombination chamber 121. When the airflow quickly passes through a relatively large area of the long diameter, it is easier to form a fully developed turbulence (Fully-developed Turbulence). The different gas components in the turbulent state of the gas flow are extremely easy to achieve complete mixing and uniformly pass through this region at a trapezoidal velocity distribution, so that the completely mixed different gas components are sufficiently contacted with the catalyst in this region. That is, the completely mixed gas component in the quasi-neutral krypton mixed gas of the present embodiment is more in contact with the catalyst in the first reaction zone si, and reacts on the catalyst surface, thereby completely utilizing the first catalyst bed 125. And improve the reaction effect. Incidentally, in order to cooperate with the effect of separating the first partition plates 226, the number of the recirculation pipes 123 may be the same as the number of the first reaction regions S1, so that each of the first reaction regions S1 is provided with one more The circulation tube 123, which is familiar to those skilled in the art, can be easily understood, and will not be described again. Figure 2C is a top plan view of a cross-section of a recombination reactor in accordance with another embodiment of the present invention. Similar to the foregoing, the recombination reactor 220a further includes a second partitioning plate 227' and the second partitioning plate 227 is disposed in the second recombination cavity 122 to distinguish the first recombination cavities 121. The first reaction zone S2. In the present embodiment, the number of the second partitioning plates 227 is, for example, eight, to divide the second recombination cavity 122 into eight symmetrical second reaction regions S2. Similarly to the foregoing, the gas flow in the second reaction zone S2 easily forms a completely developed turbulent flow so that the completely mixed gas component in the high-temperature reaction gas is more sufficiently contacted with the catalyst in the second reaction zone S2 to enhance the reaction effect. Of course, the present invention does not limit the first dividing plate 226 and the second dividing plate 22 201100164

The number and shape of the 227 are also not limited to the shape in which the first reaction region SI or the second reaction region S2 is distinguished. For example, the first divider 226a* can also be a tic-tray separator as shown in the recombination reactor 220b of Figure 2D. 3A is a cross-sectional view of a plasma assisted catalyst recombination apparatus according to another embodiment of the present invention, and the first catalyst bed is omitted, and FIG. 3B is a cross section of the disk-shaped preheating passage of FIG. 3A along the BB line. Top view. Referring to FIG. 3A to FIG. 3B, the plasma assisted catalyst recombining device 300 of the present embodiment is similar to the plasma assisted catalyst recombining device 1 (shown in FIG. 1A), and the difference is only in the case of plasma assisting. The preheater 330 of the catalyst recombining device 300 further includes a disk-shaped preheating passage 336, and the disc-shaped preheating passage 336 is disposed in the preheating chamber 132 and is connected to one end of the preheating tube 134 and the plasma chamber inlet. Between 112a. In response to the above, the disk-shaped preheating passage 336 has an air passage spirally surrounding the plasma chamber 112, and air and decane enter the disk-shaped preheating passage 336 from the preheating pipe 134, and follow the air passage in the disk-shaped preheating passage 336. It circulates inward and eventually enters the plasma chamber 112 via the plasma chamber inlet 112a. Since the high-voltage discharge phenomenon occurs in the plasma chamber 112, the temperature of the electric discharge chamber 112 is also relatively high. By the design of the disk-shaped preheating passage 336, heat in the plasma chamber 112 can be transferred outwardly along the disk-shaped preheating passage 336 to further heat the air and the combustible in the disk-shaped preheating passage 336. In addition, by rapidly absorbing heat by the disk-shaped preheating passage 336, the plasma chamber 112 and the plasma electrode 114 can be quickly cooled, thereby extending the life of the plasma reactor 110.

4 is a cross-sectional view showing a plasma assisted catalyst reassembly according to another embodiment of the present invention. Referring to FIG. 4, the plasma assisted catalyst recombining device 400 of the present embodiment is similar to the plasma assisted catalyst recombining device 100 (FIG. 1A 23 201100164.), and the difference lies only in the plasma assisted catalyst recombination. The pre-heater 430 of the device 400 further includes a third partition plate 438, and the third partition plate is disposed in the preheating chamber nm to distinguish the preheating cavity 132 into a connected pre-, a zone T1 and a preheating zone T2, wherein the preheating pipe 134 surrounds the recombination reactor 120 in a double-layered manner along the first preheating zone T1 and the second preheating zone T2, and the second preheating zone Τ2 is located at the periphery of the first preheating zone τι. In this way, the high temperature of the preheating chamber 132 from the recirculation pipe 123 is heavy, and the gas passes through the first preheating zone T1 and the second preheating zone T2 in sequence, thereby causing the reef gas to be reorganized. The heat is transferred from the periphery. Generally, high-temperature reformed gas still has some carbon monoxide, and carbon monoxide is toxic to humans. Therefore, CO Preferential Oxidation catalyst can be disposed in the first preheating zone T1 and the second preheating zone T2. In order to convert carbon monoxide into carbon dioxide. Of course, the present invention is not limited to which catalyst is disposed in the first preheating zone T1 and the second preheating zone T2. For example, the first preheating zone T1 and the second preheating zone T2 may be further configured with water. Water-gas shifting to convert carbon monoxide in a high temperature reformed gas to carbon dioxide. It should be noted that the present invention does not limit the third partitioning plate 438 to only 'divide the preheating cavity 132 into two regions. Those skilled in the art can use the third dividing plate 438 to advance according to the foregoing. The thermal cavity 132 is divided into three or more connected regions, all of which are still within the scope of the present invention. In the foregoing description, the description of the recombination reaction is mainly carried out by taking hydrocarbon gas as an example, and the plasma assisted catalyst recombination apparatus will be slightly modified as follows to enable it to be applied to the recombination reaction of a hydrocarbon liquid. 5A is a cross-sectional view of a plasma assisted catalyst recombination apparatus according to another embodiment of the present invention, and FIG. 5B is a plasma assisted catalyst recombination apparatus of FIG. 5A for removing a second catalyst bed and a third touch. A schematic cross-sectional view of a media bed and a fourth catalyst bed. Referring to FIGS. 5A-5B, the plasma assisted catalyst recombination apparatus 500 of the present embodiment is similar to the plasma assisted catalyst recombination apparatus 1 (shown in FIG. 1A), and the difference is only in the plasma assisted catalyst. The feeder 540 of the recombining device 500 further has a piezoelectric atomizing unit 544, and the piezoelectric atomizing unit 544 is connected to the mixing chamber 142, and the piezoelectric atomizing unit 544 is used for atomizing the hydrocarbon liquid and the water into fine particles. The mist droplets (the average particle size of the crucibles are smaller than ΙΟμιη) are sent to the mixing chamber 142 and mixed with the air. As a result, the fine droplets in the air behave almost equally, and enter the plasma chamber 112 from the preheating tube 134 for discharge activation. In detail, the feeder 540 has a first regulating valve 145, a third regulating valve 547 and a fourth regulating valve 548, and the first regulating valve 145 is connected to the mixing chamber 142 to control the air flow, and the third regulating valve 547 The piezoelectric atomizing unit 544 is connected to the fourth regulating valve 548 to control the flow rates of the hydrocarbon liquid and the water, respectively. Q Similar to the above, the ratio between the hydrocarbon liquid and the air (or the ratio of oxygen to carbon) can be appropriately adjusted to allow complete combustion (complete oxidation recombination) or incomplete combustion (incomplete oxidation recombination) of the hydrocarbon liquid. In the initial stage, in the embodiment, the first catalyst bed 125 is first burned to the working temperature by decane (hydrocarbon gas), and then the hydrocarbon liquid and water are introduced. Recombination with air for partial oxidation of the hydrocarbon liquid. Of course, in other embodiments, the hydrocarbon phase may be first introduced into the hydrocarbon liquid and air, and the hydrocarbon liquid is completely combusted to heat the first catalyst bed 125 by appropriate proportion distribution, and then the hydrocarbon is gradually adjusted. The ratio of liquid to air is 25 201100164 . The carbon-hydrogen liquid is gradually changed to partial combustion. A similar procedure has been described in detail during the start-up process of the above-mentioned artemisia, and those skilled in the art can easily understand it, and will not repeat them here. In the present embodiment, the hydrocarbon liquid is exemplified by, for example, alcohol, but the present invention does not limit the kind of the hydrocarbon liquid, and the carbon argon liquid may be liquefied petroleum gas or propanol. Incidentally, the third regulating valve 547 and the fourth regulating valve 548 may be externally connected with a piezoelectric pump or a micro pump to inject the alcohol and water into the piezoelectric atomizing unit 544. In addition, the present invention is not limited to the number of piezoelectric atomizing units 544. For example, other embodiments may also provide two piezoelectric atomizing units to atomize alcohol and water, respectively, and then send them to the mixing chamber 142. mixing. When the first catalyst bed 125 has reached the operating temperature and the start-up phase is completed, then the normal operation flow can be entered. Referring again to FIGS. 5A-5B, the first regulator valve 145, the third regulator valve 547, and the fourth regulator valve 548 are first adjusted to mix air, atomized alcohol, and atomized water into the mixing chamber 142. Then, the air, the atomized alcohol and the atomized water will enter the preheating tube 134 for heating, similar to the above, at this time, the preheating chamber 132 is filled with a high temperature gas, and the atomized alcohol and the atomized water The portion will be heated to form a vaporized alcohol and vaporized water. It is worth noting that the average particle diameter of the fine mist droplets is less than 1 Ομιη, so these fine mist droplets have a relatively large surface area, and are very easy to absorb heat and vaporize, which is the first use of the piezoelectric mist in this embodiment. The chemical unit 544 is one of the reasons for atomizing alcohol and moisture. When the air, the vaporized alcohol and the vaporized water enter the plasma chamber 112 along the preheating tube 134, the discharge phenomenon in the plasma chamber 112 is caused. 26 201100164

A quasi-neutral mixed gas containing ions, electrons and radicals is formed (not shown). Then, the quasi-neutral mixed gas enters the first recombination chamber 121, and when the first catalyst bed 125 is higher than the working temperature, the free alcohol molecules and the free oxygen molecules in the quasi-neutral mixed gas are Partial oxidative recombination reactions are carried out on the catalyst surface in the pre-reaction zone to gradually produce carbon monoxide, carbon dioxide, hydrogen and water. At this time, these carbon monoxide, sulphur dioxide, hydrogen, water (gaseous), unreactive nitrogen The unreacted alcohol molecules and oxygen molecules form a high temperature reaction gas (not shown) in the region before the recombination reaction of the first catalyst bed 125. In response to the above, the high temperature reaction gas will continue to react from the first recombination chamber outlet 121b into the second recombination chamber 122. Similarly, the unreacted alcohol molecules and oxygen molecules in the high temperature reaction gas will be in the middle and rear regions of the recombination reaction. The surface of the catalyst is partially oxidized and recombined, and the alcohol molecules and oxygen molecules are completely converted into carbon monoxide, sulphur dioxide, hydrogen and water (gaseous). In this way, the carbon monoxide, carbon dioxide, hydrogen, water damage (gaseous), and *reaction (4) nitrogen in the first catalyst bed 125 and the reaction & region form a high temperature reformed gas (not green) ). The high-temperature recombination gas will enter from the first-recombination off π 121e and then follow the 3^23?' to enter the preheating chamber 132 along the recirculation pipe 123. ...the air in the preheating officer 132, the atomization_and the fog The water is hydrated, and the heated air in the tube 132 and the vaporized alcohol plasma chamber 112 are more easily activated and activated. Reducing the similarity, in order to improve the ammonia gas emitted by the high-temperature heavy city or reduce the content of carbon monoxide in the south temperature recombination gas, this embodiment further 27 201100164 can re-dispose the catalyst in the preheating cavity 132 to make The high temperature reformed gas is further reacted. Referring again to FIG. 5A to 5B, the preheater 530 of the plasma assisted catalyst recombining device 500 of the present embodiment further includes a third partitioning plate 538, and the third dividing plate 538 is configured. In the preheating cavity 132, the first preheating zone τ1 and the second preheating zone Τ2 are connected to the preheating cavity 132=^, wherein the preheating pipe 134 is along the first preheating zone Τ1 and the second Preheating zone Τ2 and surrounded by double layersΟ

The preheating zone 围绕2 around the recombination reactor 12GH is located at the periphery of the first preheating zone Τ1. *''' In addition, the preheater 530 may further include a second catalyst bed 53 and a fourth catalyst bed milk, and the second catalyst bed 531 is positionable; the first preheating zone Τ1, and The third catalyst 543^望-mm-h can be located in the first preheating zone Τ1 and the fourth catalyst bed 535 can be located in the second pre- 孰=2. In this embodiment, the second catalyst bed 531 can be rotated. 533 may have a low temperature water vapor transfer catalyst. The fourth catalyst bed 535 may have a carbon oxide selective oxidation catalyst. As a result, the recombination gas entering the preheating chamber η from the recirculation pipe 123 gradually undergoes the reaction through the first pre-zone, the same, and the same dish 531. T2 ^ milk. In the second catalyst bed 531 j 51, the fourth catalyst bed ^ L 蜩跺 531 and the third catalyst bed 533, the vaporized water in the -temperature recombination gas f is the molecular weight of the gas transfer catalyst surface = = decrease in time - oxygen: carbon content oxygen W ' thereby increasing the hydrogen content, and the external water vapor transfer reaction is an exothermic process, so the released heat of 2011 201100164 can be further transferred to the preheating tube , 34 The air preheated by the preheating pipe 134 is heated, and the alcohol and water are heated to form vaporized alcohol and water, thereby improving the overall heat utilization rate of the plasma auxiliary catalyst recombining device 5〇〇. It should be noted that after the high-temperature moisture conversion catalyst through the second catalyst bed 531, if the concentration of a vaporized carbon in the high-temperature reformed gas can be reduced to around 2% (Vol.), the embodiment may also omit the setting. The low temperature water-gas conversion catalyst of the third catalyst bed 533 is used to reduce the construction cost of the plasma-assisted catalyst recombination device. Ο

After passing through the second catalyst bed and the third catalyst bed, the high temperature heavy gas usually still retains about 2% (v〇1) concentration of carbon monoxide, and gradually lowers the temperature to form a medium temperature reformed gas ( Not shown). In the fourth catalyst bed milk 1: residual - carbon oxide molecules and oxygen molecules in the medium temperature reformed gas will be oxidatively recombined on the surface of the emulsified carbon selective oxidation catalyst to generate carbon dioxide and release heat to heat the preheating tube 134 to increase the overall heat utilization rate of the plasma assisted catalyst recombination device 500. ...the poly-assistance 4===: material' and almost no residue is harmful to the human body:: oxygen:: body hydrogen, the recombination gas is taken from the preheating chamber outlet 132b, and the low-temperature to downstream device is used as fuel. Leaving the preheating chamber 132 finely, it is worth noting that the above-mentioned household body and the low-temperature recombination gas are only the exact recombination gas and the medium-temperature recombination gas to distinguish the exact position where they are located. It is convenient to explain the staged nouns of the concept of oxygen-oxygen, and it is easy to be familiar with this technique = 29 201100164 . Without confusion. In addition, carbon monoxide is also a type of fuel. If it is not desired to remove carbon monoxide, it is also possible to collect the high-temperature recombination gas directly from the preheating chamber outlet 132b without providing the second catalyst bed 531, the third catalyst bed 533 and the fourth catalyst bed 535. In the case of alcohol, it is also a type of biofuel, which in turn reduces the amount of carbon dioxide emissions. Because plants are made into biomass fuels such as alcohol after absorbing carbon atoms from the environment, biofuels such as burning alcohol are only the circulation of carbon atoms in the earth's environment, and do not increase the carbon dioxide in the earth's air environment. The total amount, in turn, can achieve the goal of environmental protection. Referring to FIG. 5A to FIG. 5B, in order to improve the reaction efficiency of the intermediate temperature reformed gas in the fourth catalyst bed 535 to completely remove the residual carbon monoxide, the preheating cavity 132 of the embodiment further has a preheating chamber opening 132c to Air can be introduced into the preheating chamber 132 from the preheating chamber opening 132c, and the oxygen molecules in the air are oxidatively recombined with the residual carbon monoxide on the surface of the carbon monoxide selective oxidation catalyst. Of course, the feeder 540 may further have a fifth regulating valve 549, and the fifth regulating valve 549 is connected to the preheating chamber opening 132c to adjust the flow rate of the air, which can be easily understood by those skilled in the art, and no longer Narration. Although the plasma-assisted catalyst recombination method of the present invention has been described in detail above, for the sake of clarity of the reader, the following description will be further illustrated. Figure 6 is a schematic flow diagram of a plasma assisted catalyst recombination method in accordance with an embodiment of the present invention. Referring to FIG. 6, as shown in steps S61-S64, a piezoelectric atomizing unit is first provided to atomize a hydrocarbon liquid and water, and air is supplied to mix air in the mixing chamber and atomize the hydrocarbon liquid and water. . In accordance with the above, the atomized hydrocarbon liquid and the water are heated in a preheating tube to form a vaporized hydrocarbon liquid and moisture. Then, the air and the vaporized hydrocarbon liquid and the water are excited into a quasi-neutral mixed gas by a plasma reactor, and then the quasi-neutral mixed gas is recombined by the recombination reactor to form a high (warming reaction gas, and then the high temperature reaction is performed). The gas is recombined to form a high temperature reformed gas, wherein the high temperature reformed gas is adapted to heat the atomized carbon argon liquid to vaporize the atomized hydrocarbon liquid and the water. In summary, the plasma assisted touch of the present invention The media recombination device and method have at least the following advantages: First, the recirculation pipe arrangement can avoid the problem of short circuit of the air flow, thereby greatly improving the reaction efficiency of the gas and the catalyst, thereby reducing the volume of the recombination reactor to reduce the manufacturing cost. When the high-temperature reformed gas flows into the recirculation pipe, the heat in the region before the recombination reaction can be taken to the middle portion of the recombination reaction to increase the temperature uniformity of the first catalyst bed, thereby further increasing the recombination efficiency. The flow of hydrogen gas (or hydrocarbon liquid) to the air, so that the carbon helium gas is completely burned to heat the first catalyst bed, thereby making the first The catalyst bed reaches the working temperature to complete the start-up procedure. Therefore, the present invention does not require any additional auxiliary heaters, thereby reducing the construction cost, reducing the overall equipment volume, and avoiding the danger of setting the auxiliary heater. 3. By means of the preheating tube setting, the residual heat of the high temperature recombination gas can be used to heat the air in the preheating tube, the hydrocarbon gas, the atomized hydrocarbon liquid or the atomized water, etc. Initiate the effect of activation. Since there is no need to provide an external heater to preheat air, hydrocarbon gas, atomized hydrocarbon liquid or atomized water, etc., the construction cost can be reduced, and the overall device can be reduced. Dimensions 31 201100164 . Fourth, the preheater is coated with a recombination reactor, so that the temperature distribution of the plasma assisted catalyst recombination device is gradually reduced from the internal high temperature recombination reactor to the peripheral medium and low temperature preheater. In order to improve the overall heat utilization rate, and avoid the risk of direct contact with the high temperature recombination reactor. 5. The gas shape can be formed by the arrangement of the first partition plate and the second partition plate. Fully developed turbulent flow to further improve the efficiency of catalyst recombination conversion. 6. By the arrangement of the disk-shaped preheating channel, the heat in the plasma chamber can be absorbed to prolong the life of the plasma reactor. The second catalyst bed, the third catalyst bed and the fourth catalyst bed are recombined with the high temperature reformed gas, and in addition to increasing the hydrogen content and reducing the carbon monoxide content, the heat released by the recombination reaction can simultaneously heat the preheating tube. Gas or atomized liquid to improve the overall heat utilization rate. 8. When alcohol is used as a hydrocarbon liquid to produce hydrogen fuel, it will not increase the total amount of carbon dioxide in the earth's air environment, thereby achieving environmental protection goals. Although the present invention has been described above by way of a preferred embodiment, it is not intended to limit the invention, and those skilled in the art can make some modifications and refinements without departing from the spirit and scope of the invention. The scope of protection of the present invention is defined by the scope of the appended claims. 32 201100164 BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1A is a schematic cross-sectional view showing a plasma assisted catalyst reassembly according to an embodiment of the present invention. 1B is a schematic cross-sectional view showing the first catalyst bed in the plasma assisted catalyst recombination apparatus of FIG. 1A. 2A is a schematic cross-sectional view of a plasma assisted catalyst recombination apparatus in accordance with another embodiment of the present invention. Figure 2B is a top plan view of the recombination reactor of Figure 2A taken along line AA. 2C to 2D are cross-sectional top views of two recombination reactors in accordance with another embodiment of the present invention. 3A is a cross-sectional view of a plasma-assisted catalyst recombination apparatus according to another embodiment of the present invention. FIG. 3B is a cross-sectional view of the disc-shaped preheating passage of FIG. 3A taken along line BB. 4 is a cross-sectional view showing a plasma assisted catalyst reassembly according to another embodiment of the present invention. Figure 5A is a cross-sectional view showing a plasma assisted catalyst recombination apparatus in accordance with another embodiment of the present invention. Figure 5B is a cross-sectional view showing the second catalyst 'bed, third catalyst bed and fourth catalyst bed removed from the plasma assisted catalyst recombination apparatus of Figure 5A. FIG. 6 is a schematic flow diagram of a plasma assisted catalyst recombination method according to an embodiment of the present invention. [Main component symbol description] 100, 200, 300, 400, 500: plasma assisted catalyst recombination device 33 201100164 110: plasma reactor 112: plasma chamber 112a: plasma chamber inlet 112b: plasma chamber outlet 114 : plasma electrode 116: plasma power supply unit 120, 220, 220a, 220b: recombination reactor 121: first recombination chamber O 121a: first recombination chamber inlet 121b: first recombination chamber outlet 121c: first recombination chamber Opening 122: second recombination chamber 122a: second recombination chamber outlet 123: recirculation tube 124: perforated plate 125: first catalyst bed 130, 330, 430: preheater 132: preheating chamber 132a: pre Hot chamber inlet 132b: preheating chamber outlet 132c: preheating chamber opening 134: preheating tube 140, 540: feeder 142: mixing chamber 145: first regulating valve 34 201100164

146: second regulating valve 226 > 226a: first partitioning plate 227: second partitioning plate 336: disk-shaped preheating passage 438, 538: third partitioning plate 531: second catalyst bed 533: third Catalyst bed 535 : Fourth catalyst bed 544 : Piezoelectric atomization unit 547 : Third regulator valve 548 : Fourth regulator valve 549 : Fifth regulator valve SI : First reaction zone S2 : Second reaction zone ΤΙ : a preheating zone Τ2: second preheating zone S1~S4: step 35

Claims (1)

201100164, VII, the scope of application for patents: 1. A plasma-assisted catalyst recombination device, comprising: _ _ a feeder having a mixing chamber; a plasma reactor comprising: a plasma chamber having an electric a slurry chamber inlet and a plasma chamber outlet; a plasma electrode; a plasma power supply unit coupled to the plasma chamber and the plasma electrode to generate a discharge in the plasma chamber; Connected to the plasma reactor, the recombination reactor comprises: a first recombination chamber having a first recombination chamber inlet, a first recombination chamber outlet and a first recombination chamber opening, and the first recombination chamber The inlet is connected to the plasma chamber outlet; a second recombination chamber, wherein the first recombination chamber is located in the second recombination chamber, and the second recombination chamber has a second recombination chamber outlet; a portion of the first recombination chamber is connected to the first recombination chamber, and the other end of the recirculation tube is pierced through the first recombination chamber outlet. Two recombination chambers out π ; &quot a porous plate disposed in the first recombination chamber adjacent to the first recombination chamber inlet; a first catalyst bed disposed in the first recombination chamber and the second recombination chamber; The preheater comprises: a preheating chamber, wherein the recombination reactor is located in the preheating chamber 36 201100164 . and the preheating chamber has a preheating chamber inlet and a preheating chamber outlet; a preheating tube disposed in the preheating chamber and surrounding the recombination reactor, wherein one end of the preheating tube is connected to the inlet of the plasma chamber, and the other end of the preheating tube is passed through the inlet of the preheating chamber To connect the mixing chamber. 2. The plasma assisted catalyst recombining device of claim 1, wherein an air and a carbon helium gas are mixed in the mixing chamber and enter the plasma chamber along the preheating tube to become a a quasi-neutral mixed gas entering the first recombination chamber and recombining in the first catalyst bed to form a high temperature reaction gas, the high temperature reaction gas entering from the outlet of the first recombination chamber The second recombination chamber is recombined in the first catalyst bed to form a high temperature recombination gas, and the high temperature recombination gas enters the recirculation tube from the first recombination chamber opening, and enters the pretreatment tube along the recirculation tube The hot chamber is configured to heat the air in the preheating tube and the carbon helium gas, and exit the preheating chamber from the preheating chamber outlet. 3. The plasma assisted catalyst reassembly device of claim 1, wherein the feeder further has a first regulating valve and a second regulating valve, and the first regulating valve and the first regulating valve The two regulating valves are connected to the mixing chamber to control the flow rate of an air and a hydrocarbon gas into the mixing chamber, respectively. 4. The plasma assisted catalyst reassembly according to claim 1, wherein the portion of the recirculation tube in the first recombination chamber is a coil. 5. The plasma-assisted catalyst reassembly according to claim 1, wherein a direction of one end of the preheating tube connected to the plasma chamber inlet is offset from a center of the plasma chamber. 6. The plasma-assisted catalyst reassembly according to claim 1, wherein the preheater further comprises a disk-shaped preheating passage disposed in the preheating chamber; Connected between one end of the preheating tube and the inlet of the plasma chamber. 7. The plasma assisted catalyst reassembly according to claim 1, wherein the recombination reactor further comprises a first partition plate disposed in the first recombination chamber. 8. The plasma assisted catalyst reassembly according to claim 7, wherein the first partition is a cross partition or a cross-shaped partition. 9. The plasma assisted catalyst reassembly apparatus of claim 1, wherein the recombination reactor further comprises a second separator disposed in the second recombination chamber. 10. The plasma assisted catalyst recombining device of claim 1, wherein the preheater further comprises a third partitioning plate disposed in the preheating chamber to preheat the cavity It is divided into one of the first preheating zone and the second preheating zone. 11. The plasma assisted catalyst recombination apparatus of claim 10, wherein the preheating tube surrounds the recombination reactor along the first preheating zone and the second preheating zone. 12. The plasma assisted catalyst recombination device of claim 10, wherein the preheater further comprises a second catalyst bed, a third catalyst bed' and a fourth catalyst bed, and The second catalyst bed is located at the first preheating zone, and the third catalyst bed is located at a boundary between the first preheating zone and the second preheating zone, and the fourth catalyst bed is located at the second preheating zone. Hot zone. 13. The plasma assisted catalyst recombination device of claim 12, wherein the second catalyst bed has a high temperature water vapor transfer catalyst, and the third catalyst bed has a low temperature water gas transfer catalyst, and The fourth catalyst bed has an oxidation 38 201100164 . Carbon selective oxidation catalyst. 14. The plasma assisted catalyst reassembly according to claim 1, wherein the feeder further has a piezoelectric atomizing unit connected to the mixing chamber. 15. The plasma assisted catalyst recombining device of claim 14, wherein a hydrocarbon liquid and a water are formed in the piezoelectric atomizing unit to atomize the hydrocarbon liquid and the water. Entering the mixing chamber to enter the preheating tube after being mixed with air entering one of the mixing chambers, atomizing the carbon enthalpy liquid and the water to form a vaporized hydrocarbon liquid and the leeches in the preheating tube And entering the plasma chamber along the preheating tube to form a quasi-neutral mixed gas, the quasi-neutral mixed gas entering the first recombination chamber and being carried out in the first catalyst bed Recombining to form a high temperature reaction gas from the outlet of the first recombination chamber into the second recombination chamber and recombining in the first catalyst bed to form a high temperature recombination gas, the high temperature recombination gas from the first a recombination chamber opening enters the recirculation tube, and enters the preheating chamber along the recirculation tube to heat the air, the atomized carbon crucible liquid and the atomized water in the preheating tube, and self preheating The chamber outlet exits the preheating chamber. The plasma assisted catalyst recombination device of claim 15, wherein the hydrocarbon liquid is alcohol or liquefied petroleum gas. 17. The plasma assisted catalyst recombining device of claim 14, wherein the feeder further has a first regulating valve, a third regulating valve and a fourth regulating valve, and the first regulating The valve is connected to the mixing chamber to control the flow of air into the mixing chamber, and the third regulating valve and the fourth regulating valve are connected to the piezoelectric atomizing unit to respectively control a hydrocarbon liquid and a water inlet. The flow rate of the piezoelectric atomizing unit. 18. The plasma assisted catalyst recombination 39 201100164 as claimed in claim 14, wherein the preheating chamber further has a preheating chamber opening to allow an air to enter the preheating chamber opening. Hot cavity inside. 19. The plasma assisted catalyst recombining apparatus of claim 18, wherein the feeder further has a fifth regulating valve, and the fifth regulating valve is connected to the preheating chamber opening to control the Air flow. 20. A plasma assisted catalyst recombination method comprising: providing a piezoelectric atomization unit to atomize a liquid of hydrogen and one water; providing an air; mixing the air and atomizing the hydrocarbon liquid And the water, and atomizing the carbonized liquid and the water; providing a plasma reactor to excite the air and the vaporized hydrocarbon liquid and the water into a quasi-neutral mixed gas And providing a recombination reactor to recombine the quasi-neutral mixed gas to form a high temperature reaction gas, and recombining the high temperature reaction gas to form a high temperature reformed gas, and the south temperature reformed gas is suitable for heating the atomized carbon The mouse liquid and the water are such that the atomized hydrocarbon liquid is vaporized with the water. 〇 21. The plasma assisted catalyst recombination method of claim 20, wherein the hydrocarbon liquid is alcohol or liquefied petroleum gas. 40