TWI379710B - Plasma assisted catalyst reformation apparatus and method - Google Patents

Description

1379710 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. [First Shovel Technology] With the advancement of technology, the available energy is also diversified, and the petrochemical fuel or biofuel can be converted into hydrogen fuel, especially through catalyst recombination. In general, natural gas, alcohol, decane: butane and other hydrocarbon gases or hydrocarbon liquids can be converted to hydrogen fuel at high temperatures through the recombination of the catalyst, and hydrogen fuel is currently considered to be more environmentally friendly. ^ One of the fuels. The traditional catalyst heavy-duty device must first use the auxiliary burner to add _ silk first, and the direct-medium bed reaches the temperature. After the heat, the hydrogen gas and the air are partially oxidized and recombined. The auxiliary burner or electric heater is turned off by the heat generated by the partial deuteration recombination reaction to maintain the temperature of the contact = bed. However, auxiliary burners or electric heaters are usually large in size and relatively productive, and they are used in advances to add _ media beds, which are very difficult to make. Another traditional catalyst recombination device is used for hydrocarbon liquids. _ and, if the furnace is used to heat the carbon body and water (4) to vaporize the milk body to recombine by heating the catalyst bed, the catalyst must continue to operate the steel furnace to heat the hydrocarbon (4) and water. Share. However, the efficiency of heating is too low, resulting in a large energy loss, and the boiler is usually also a large and dangerous component. In addition, the prior art also proposes a plasma-assisted catalyst recombination device for generating a high-voltage high-frequency alternating current by using a plasma reactor, thereby generating a discharge to heat the hydrocarbon gas and the air, thereby pulverizing the hydrocarbon gas and the air. The catalyst bed is heated to bring the catalyst bed to operating temperature to produce a recombination reaction. When the temperature of the catalyst bed reaches the upper limit, the power to the plasma reactor can be cut off, and when the temperature of the catalyst bed drops to the lower limit, the plasma reactor power is restored. In addition, U.S. Patent No. 6,702,991, U.S. Patent No. 6,804,950, U.S. Patent No. 6,506,359, the disclosure of which is incorporated herein by reference. However, whether it is for hydrocarbon gas or carbon argon liquid, an additional heater is required to heat the catalyst bed to the operating temperature, making the overall volume of the catalyst recombination unit very bulky and very dangerous. Moreover, the heating efficiency of the heating means is not ideal, and both energy is wasted in the process of heat exchange to the catalyst bed. SUMMARY OF THE INVENTION In view of the above, an object of the present invention is to provide a plasma assisted catalyst recombination device, which comprises a high temperature recombination reactor coated in a preheater and configured by a recirculation pipe to guide a heat source. Effective use of heat sources and drastically reduce the size of the catalyst recombination unit. Further, another object of the present invention is to provide a plasma-assisted catalyst recombination method in which a hydrocarbon liquid is first atomized and then a hydrocarbon liquid is heated and vaporized. Since the atomized hydrocarbon liquid has a large surface area, the heating efficiency can be greatly improved. 6 in order to achieve the above or other (four) 'the invention S out of a electrical auxiliary touch pre-!! device, including the feeder, the plasma reactor, the recombination reactor and the second, wherein the recombination reactor is connected to the plasma reaction Device. The feeding device is active and the electropolymerization reactor comprises an electric cavity, an electric polyelectrode and an electric current to an early element, wherein the plasma cavity has a plasma chamber inlet and a plasma battery to be electrically connected (four) body and electropolymer The electrode 'is in the cavity, the second = ge). The recombination reactor includes a first-recombination weight, a chamber, a recirculation tube, a multiwell plate, and a first catalyst. - Recombination chamber opening /, and the cavity eight, the first - recombination chamber outlet and the first: the chamber is located in the second recombination chamber, and the second recombination chamber has; the chamber outlet. The recirculation pipe is partially located in the first recombination chamber, and one of the recirculation tubes is the one of the recirculation tubes, and the -m ^ is connected to the recombination chamber opening, and the recirculation tube is another one! The second recombination chamber outlet is passed through the first recombination chamber outlet. One = is disposed in the first heavy chamber and adjacent to the first recombination chamber inlet. The first media bed is disposed in the first recombination cavity and the second recombination cavity, the second preheating cavity and the preheating pipe, wherein the recombination reactor is located in the preheating: ^ θ and the preheating cavity has preheating The inlet of the chamber and the outlet of the preheating chamber are pre-twisted, placed in the cavity and surrounded by the recombination reactor, and the end of the preheating tube is connected to the inlet of the plasma chamber, and the other end of the preheating tube is pretreated. The entrance is to connect the mixing chamber. For the above or other purposes, the present invention further provides a plasma assisted catalyst recombination method comprising the steps of: providing a piezoelectric atomizing unit to atomize liquid and moisture; providing air; mixing air and Atomized carbon gas liquid and water, and vaporized atomized hydrocarbon liquid and water; providing plasma anti- 1379710 reactor to excite air and vaporized hydrocarbon liquid and water into 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 the high temperature reformed gas is suitable for heating the atomized hydrocarbon liquid and water to make the mist The hydrocarbon liquid is vaporized with 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 is recombined from the first catalyst chamber into the second recombination chamber to form a high temperature recombination gas, and the high temperature recombination is performed. 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 hydrocarbon gas. The flow into the mixing chamber. In one embodiment of the invention, the portion of the recirculation tube in the first recombination chamber is, for example, a coil. In one embodiment of the invention, the direction in which one end of the preheating tube is connected to the inlet of the 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 1379710 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 partitioning plate, and the third dividing plate is disposed in the preheating cavity to distinguish the preheating cavity into the first connected Preheating zone and 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, and 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 the 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 misty hydrocarbon liquid And the water forms a vaporized hydrocarbon liquid and water in the preheating pipe, and enters the plasma cavity along the preheating pipe to form a quasi-neutral mixed gas, and the quasi-neutral mixed gas enters the first recombination cavity. And recombining in the first catalyst bed to form a high-spiking reaction gas, and the high-temperature reaction gas is recombined from the first recombination chamber into the second recombination chamber to form a high-temperature recombination gas, a high-temperature recombination gas. The first recombination chamber opening enters the recirculation tube, 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 exits from the preheating chamber outlet Preheat the cavity. 1379710 In one 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 hydrocarbon 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 feeder has a fifth regulator, and the fifth regulator is connected to the preheat chamber opening to control 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 recombination of hydrocarbon gas 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 this 10 1379710 is to increase reorganization. Efficiency and heat source use efficiency 2:: The relationship between each component and its connection, and then the electric paddle reaction of the present invention|§ 110 includes ^ 冤 slurry cavity 112, plasma electrode 114 and plasma power supply soap element 116, Gans + 故 & dry u ib, where the plasma power supply is connected to the plasma chamber 112 and the plasma lightning helmet ^ 丄疋 electric water electrode 114, by supplying high voltage and high frequency

The galvanic current can generate an arc discharge in the electropolymerization chamber 112 to free the gas in the body 112 (this gas will be described later as a mixture of air, carbon nitrogen gas or vaporized hydrocarbon liquid). In addition, the 'electric cavity 112 has an electrical cavity inlet 112a and an electrical cavity outlet U2b', and the aforementioned gas enters the electrical cavity 112 from the cavity π 112a and exits the U2b from the plasma cavity after being freed. Leaving the plasma chamber 112, wherein the plasma reactor ι1 is connected to the recombination reactor 12, and the gas leaving the plasma chamber 112 enters the recombination reactor 12A. The recombination reaction 120 includes a first recombination chamber 121, a second recombination chamber 122, a recirculation tube 123, a perforated plate 124, and a first catalyst bed 125, wherein the first recombination chamber U1 is located in the second recombination chamber! 22, 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 both in the shape of a barrel, and the first recombination cavity 21 overlaps with the center line of the second recombination cavity 122 and is aligned with the plasma. The centerline of the cavity 112 is convenient for assembly operations. However, the present invention does not limit the shape of the first recombination cavity 12i and the second recombination cavity 122. 11 1379710 In addition, the first recombination chamber 121 has a first recombination chamber inlet Hla and a first recombination chamber outlet 12lb, and the first recombination chamber population is electrically connected to the outlet chamber mb, so that the free gas can be made by the first weight The electric cavity ^ = 2la enters the first-recombination chamber 〇121a and reacts with the first catalyst bed (2). Then, the gas enters the second recombination chamber 122 from the first recombination chamber outlet 121b to continue the recombination reaction with the first catalyst bed 125.

That is, according to the flow direction of the gas in the first-catalyst bed 125, the first catalyst bed 125 can be roughly divided into a recombination reaction located in the first recombination cavity pi adjacent to a recombination chamber inlet 121a, such as a segment, located in the first recombination chamber. The middle portion of the recombination reaction at the junction of the body κι and the first-recombination cavity 122, and the rear portion of the recombination reaction located in the second recombination chamber 122 adjacent to a recombination chamber inlet 121& Of course, the division of the first catalyst bed 125 into three segments is for convenience only, and the process of substantially performing the recombination reaction is not different. In order to allow the gas to be evenly distributed after entering the first recombination chamber 121 from the first refill chamber inlet i2la, the present invention can dispose the perforated plate 124 within the first recombination chamber 121 and adjacent to the first recombination chamber inlet i21a. In this way, by the diffusion effect of the perforated plate 124, the gas can be uniformly passed through the perforated plate 124 to react with the first catalyst bed 125. In general, after the gas passes through the perforated plate 124, due to the geometric arrangement of the first recombination cavity 121 and the second recombination cavity 122, the gas still cannot pass the first catalyst bed 125 completely uniformly, but will be the shortest. The path passes through the first catalyst bed 125 to the first recombination chamber outlet 121b. These phenomena are often referred to as airflow shorts (0it_.e4iGuit on fl〇w_s) or channeling effect problems, which cause the gas to contact the most 12 (5) 9710, less catalyst during the flow. In order to solve the above disadvantages, the present invention reopens the first recombination cavity opening 12 〖c in the first recombination cavity 121, and opens the second re-nuclear cavity outlet 122a in the second recombination cavity 122, wherein the first recombination cavity opens. 121 (: can be opened in the first touch, the rear reaction region of the bed 125, and the second recombination chamber outlet is adjacent to the first recombination chamber outlet 121b, and can be opened in the middle portion of the recombination reaction of the first catalyst bed 125. In the above, the recirculation pipe 123 is partially located in the first recombination cavity 121, and one end of the recirculation pipe 123 is connected to the first recombination cavity opening 12, and the other end of the recirculation pipe 123 is via the first recombination cavity outlet U1b. The second recombination chamber outlet 122a is passed out. The portion of the recirculation tube 123 in the first recombination chamber 121 can be regarded as an obstacle to prevent the gas from passing through the recombination reaction front region of the first catalyst bed 125 in the shortest manner. As a result, the gas passes through the recombination reaction front region of the first catalyst bed 125 in a longer path, thereby contacting more catalyst to enhance the recombination reaction=efficiency. Further, the recirculation tube 123 is in the first reorganization. Cavity 121 The portion can be arranged in an irregular arrangement for the coil to thereby cause the short-circuit problem of the airflow described above. Referring to Figures ΙΑ1 to 1B, the preheater 13A includes a preheating chamber 132 and a preheating tube 134. The recombination reactor 120 is located in the preheating chamber 132, and the preheating chamber 132 has a preheating chamber outlet 132b. When the gas flows through the rear reaction region of the first catalyst bed 125, it passes through the first The chamber opening 121c is recombined and flows into the recirculation tube 123, and proceeds into the preheating chamber 132 along the recirculation tube 123 ml out of the recombination reactor 12, and the gas which finally completes the recombination reaction fills the entire preheating chamber. 132 is taken from the preheating chamber 13 1379710 port 132. In addition, the ray chamber 132 has a preheating chamber population, and the pre 孰 = 134 is disposed in the preheating chamber 132 and surrounds the recombination reactor η = Bu's preheating officer 134's - end is connected to the Xia cavity population 112 & and preheating officer: 34 the other end is through the preheating chamber inlet ma to connect the feeder _ heart to 142 ° So - the 'gas is initially in the mixing chamber (4) = ' while entering the plasma chamber via the preheating tube 134 112 free for reaction 0

Incidentally, the other end of the recirculation pipe 123 may be disposed at any position within the preheating cavity 132 after passing through the second recombination chamber outlet 122a, and in the present embodiment, The other end of 123 is disposed adjacent to the preheating tube 134 adjacent to the plasma chamber 112 to heat the gas in the preheating tube 134. The operation flow of the plasma assisted catalyst recombination apparatus 100 will be specifically described below with the hydrocarbon gas of decane, after roughly explaining the complicated arrangement between the respective members of the plasma assisted catalyst recombination apparatus 1 of the present invention. However, the present invention is not limited to the type of hydrocarbon gas. It is also applicable to hydrocarbon gas such as ethane, propane or gas. In the process of recombination reaction with a catalyst, if the hydrocarbon gas can be reconstituted into the expected 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 and recombination 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. . 1379710 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 complete oxidation and recombination reaction is to adjust the hydrocarbon. The ratio of gas to air. In the case of methane, for example, 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 sputum to air is higher, the partial oxidative recombination reaction is easier. In this way, the present invention does not require any additional auxiliary heaters to directly burn the first catalyst bed 125 by completely burning the hydrocarbon gas in the aforementioned apparatus, 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 regulating valve 145 and a second regulating valve 146, and the first regulating valve 145 and the second regulating valve 146 are connected to the mixing chamber 142 to respectively control the air ( The flow rate of methane (not shown) entering the mixing chamber is shown. In the start-up phase (preheating) of the present 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 flow ratio of air to methane is 20 : 1 (that is, the oxygen to carbon ratio is 4.2: 1). Next, air and decane enter the plasma chamber 112' along the preheating tube 134 and are activated by the discharge phenomenon in the plasma chamber ip. In detail, the air and decane in the 'speaking' part are subjected to high-energy electron impact of non-thermal plasma to generate free (I〇nizati〇n), dissociation (Excitation), etc., and then form A quasi-neutral mixed gas containing ions (I〇n), electrons (Electron) and free radicals (not shown). The quasi-neutral mixed gas mentioned above enters the first recombination chamber 121 and releases a large amount of heat to heat the first catalyst bed 125, so as to catalyze the catalyst in the catalyst bed 125. The temperature rises. Although the full fuel can be used to ride a "large amount of heat, it depends on the mixed state of the working milk and the Dailang to the first catalyst bed 125, so the f-room can not completely pass the money phase ( The slit air and the burnt gas are transferred to the first catalyst bed 125 by conduction to the solid phase (catalyst). It should be noted that this embodiment first mixes the air with the decane.

Import the first catalyst $ 125. However, if the crucible and the air are separately introduced into the first catalyst bed 125 and then the air is mixed with the crucible, the first catalyst bed 125 is composed of a porous catalyst, but the porous catalyst It still causes poor mixing of the 6 and m, resulting in incomplete combustion. ^ a generally speaking, the temperature of the first catalyst bed 125 in the front, middle and rear regions of the recombination reaction is in a decreasing state, and when the temperature of the first catalyst bed 125 in the region before the recombination reaction exceeds the lower limit value Then, you can start to adjust the ratio of nails to air' so that methane can be gradually adjusted to incomplete combustion. Taking methane as an example, the temperature of the lower limit is 550 ° C, and then the flow ratio of air to decane can be adjusted to be 11.9 : 1, 14.76 : 1 or 9·52 : 1 respectively (that is, the oxygen to carbon ratio is For 2 5 : Bu 3丨:! or 2 :丨), to reduce the air to make a series of incomplete combustion of methane, and release a large amount of heat from the gas phase to the solid phase. The first catalyst bed 125 is continuously heated. At this time, since the catalyst temperature in the region before the recombination reaction has exceeded the limit of 5 5 〇 ° C ', a small portion of the unburned oxygen molecules in the air will undergo partial oxidation recombination with the surface of the decane molecule 4 catalyst, and since this is not Complete combustion is the sound of 16 1379710 born on the surface of each of the Am domains, so this part = the heat released! It is passed directly to each single catalyst: and the catalyst temperature in the front region of the reaction rises rapidly. The reorganization of the field will then accelerate the first touch: the temperature rise of the other areas of the V through the solid phase of the first catalyst bed to the solid phase of the fire and the combustion of the air. Catalyst bed 2: In the bed two values = above, but not exceeding the limit value of 900 〇 C as the principle. It should be noted that 'if it is completely burnt with air and the heat generated, the entire first catalyst bed 125 is heated, so that the temperature of the middle and rear sections of the TV should reach the bottom limit. A lot of hospitals and air, and the temperature of the longer medium-bed 125 rises close to 9 Huan, that is, the temperature of the female 125 in the front, middle and back regions of the recombination reaction is large = the bottom limit is above , you can adjust the air and the accompaniment again: 9.52 : 1 or 8.57 : 1 (that is, the oxygen-to-carbon ratio is 2: 1 ί - enter · ^ to advance - step to reduce 勉 and make the smoldering to different degrees The medium: two temperature ί release less heat f contained to maintain the first-touch due to: the catalyst bed 125 in the front, middle and back sections of the recombination reaction: the half of the dish has been above the working temperature 'so air In most parts of Yin, the knives and the Mt. molecules in the first catalyst bed 125 are mostly oxidized and recombined by the single catalyst 2, and the heat released is directly transmitted to the mother. The catalyst maintains the temperature of the first catalyst bed 125 while maintaining the temperature of the 17 catalyst bed 125 at 55. Between oc and 9 〇〇 ° C. In other words, in the plasma-assisted catalyst recombination device 1 of the present invention, only a large amount of extra heating is required, and the first catalyst can be used. The working temperature X of the bed 125 is rapidly increased, which may cause the plasma-assisted catalyst recombination device to be quickly and cost-effectively, and the method is to start the machine (preheating the catalyst bed) to achieve normal operation. After the 70% starting procedure, the normal operation flow will be described below. Referring again to FIGS. 1A to 1B, similarly to the foregoing, 'the first regulating valve 145 and the second regulating valve 146 are first adjusted to allow air and methane to enter the mixture in the aforementioned ratio. The chamber 142 is mixed, and the flow rate of air to decane is 9.52:丨 or 8.57:1 (that is, the ratio of oxygen to carbon is 2:1 or 丨8:丨, respectively) to the ratio of incomplete combustion. Air and methane will enter the preheating tube 134 for heating (this process of warming by residual heat will be detailed later), and enter the plasma chamber 112 along the preheating tube 134, and through the plasma chamber U2 The discharge phenomenon further forms a quasi-neutral mixed gas containing ions, electrons and radicals (not shown) In the present embodiment, the direction in which the preheating tube 134 is connected to the plasma chamber inlet 112a is, for example, offset from the center of the plasma chamber 112, so that air and nails are burned into the plasma chamber 112 and then generated around the plasma electrode 114. The vortex flows, thereby allowing the air to be more uniformly mixed with the smoldering to be activated as a quasi-neutral mixed gas. Then, the quasi-neutral mixed gas enters the first recombination chamber 121' and is in the first touch When the media bed 125 is higher than the working temperature, the free methane molecules and the free oxygen molecules in the quasi-neutral mixed gas will undergo partial oxidation recombination on the catalyst surface of the recombination reaction zone (partial 〇xidati〇n Reforming). The reaction 'gradually produces carbon monoxide, carbon dioxide, hydrogen and 18 1379710. Water, at this time these carbon monoxide, carbon dioxide, argon, water (gaseous), unreactive nitrogen, unreacted methane molecules and oxygen molecules in the first touch A high temperature reaction gas (not shown) is formed in the front region of the recombination reaction of the media bed 125. The above-mentioned 'hot temperature reaction gas will enter the second recombination cavity 122 from the first recombination chamber outlet 121b to continue the reaction. Similarly, the unreacted decane molecules and oxygen molecules in the high temperature reaction gas will be in the middle and the rear stage of the recombination reaction. The surface of the catalyst is partially oxidized and recombined (Partial 〇xidati〇n • Reforming), and the unreacted methane molecules and oxygen molecules are gradually converted into carbon monoxide, carbon dioxide, hydrogen and water (gaseous). Thus, the carbon monoxide, carbon dioxide, hydrogen, moisture (gaseous), and unreactive nitrogen in the post-recombination reaction zone of the first catalyst bed 125 form a high temperature reformed 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 concept of a partial oxidation recombination process, and the high-temperature reaction gas is only a general term for the concept of a partial oxidation recombination process and is familiar with the art and can be easily understood without being mixed. clear. Next, the high temperature reformed gas enters the recirculation pipe 123 from the first recombination chamber opening 12ic. In the foregoing description, the recirculation pipe 123 has a problem of avoiding 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 improve the recombination efficiency. And greatly reduce the volume of the recombination reactor 12 。. In addition, the 'tempering recombination gas can absorb the heat in the region of the first stage of the recombination reaction of the first catalyst bed 125, and transfer the heat to the middle portion of the recombination reaction of the flute tenth bed of the fleece bed 125. This allows the temperature distribution of the first touch chessboard 'green bed 125' to be uniform to further enhance the reaction effect of the overall first-catalyst bed 125. High: the recombination gas enters the preheating chamber along the recirculation pipe 123 =: the air in the second 132 and the courtyard, and the air in the preheating tube and the burning of the nail into the electropolymer cavity 112 will be more suitable, ^ ^ . Feng invention only uses the residual temperature of the two-temperature recombination gas to heat the air and the courtyard, and the mother needs to provide an external heater, thereby reducing the construction cost and shrinking the overall size. In the present embodiment, the other end of the recirculation pipe 123 passes through the second recombination chamber outlet and is disposed at a temperature adjacent to the "cavity 112" to cause the high temperature recombination gas just leaving the recombination reactor 12G. It is possible to directly enter the air and the smoldering of the electropolymerization chamber 112β, thereby maximizing the residual heat of the high-temperature recombination gas. Further, the preheating tube 134 is preheated, and the inside of the body 132 is preheated. For example, the recombination reaction f 120 is surrounded by a double-layered manner to achieve heat absorption of the high-temperature reformed gas and the effect of the regenerative reactor 120: the heat transfer is not limited to the preheating tube 134. Surrounding the recombination reaction nm. Auxiliary 2: Heavy: ϊϊ: 3〇 is coated with a recombination reactor 120' can be used in 120. The temperature distribution of I set 100 is from the internal high temperature recombination, and the 楹θ Du is gradually reduced to the periphery. The medium and low temperature preheater 130 'borrows the heat utilization rate of the corpus callosum' and avoids the risk of direct contact with high temperature recombination reactions. Hot chamber outlet; 3=1: high temperature recombination gas rich in hydrogen Will leave the preheating chamber 132 from the pre-D and transport it downstream The device, 20 丄 (10) 710 is processed after the step-by-step process to supply the fuel. The battery, the internal combustion engine, etc. are used for the following: Jf test® 1A~1B' In this embodiment, the recirculation pipe 123 recombination chamber The shape i in the body 121 is an irregularity_coil with the obstacle, and the mixed gas of the first-catalyst bed 12" 5 passes through the defined segment area in the shortest way. However, the present invention It is not excessive:: two = quantity and shape, and when the number of recirculation tubes 123 is recombination chamber opening me. (10) body 121 also needs to be opened corresponding to the first one; first: the recombination efficiency of the catalyst bed 125, The recombination cavity 121 of the present invention or the second recombination cavity 122 is provided with a partition #, 4 · will be further exemplified and cooperated with the diagram, and the same name is used for the purpose of explaining the same function. 2A is a schematic cross-sectional view of a plasma assisted catalyst recombination apparatus according to another embodiment of the present invention, and the first catalyst bed, the recirculation tube and the first recombination chamber opening are omitted, and FIG. 2B is FIG. 2A. A top view of the cross section of the recombination reactor along the AA line. Please refer to Figures 2A to 2b, this embodiment The electropolymerization assisted catalyst recombination apparatus 200 is similar to the aforementioned plasma assisted catalyst recombination apparatus 1 (shown in FIG. 1A). The only difference is that the recombination reactor 220 of the plasma assisted catalyst recombination apparatus 2 is more The first partitioning plate 226' is disposed in the first recombination cavity 12i, so that the first recombination cavity m distinguishes a plurality of independent first reaction zones S1. In the example, the first partition 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 si has only the cross section of the original first recombination cavity 121. 21 of the area is 1379710. That is, the equivalent diameter of each first reaction zone S1 is one-half of the equivalent diameter of the first recombination cavity 121, so the length of each first reaction zone S1 The ratio is twice the original length ratio of the first recombination cavity 121. When the airflow quickly passes through a relatively large area of the long diameter, it is easier to form a Fully-developed Turbulence. The different gas components in the turbulent 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 in full contact with the catalyst in this region. That is, the completely mixed gas component in the quasi-neutral Lu mixed gas of the present embodiment is more in contact with the catalyst in the first reaction zone S1, 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. 2C is a cross-sectional view 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 dividing plate 227' and the second dividing plate 227 is disposed in the second recombination cavity 122 to distinguish the second recombination cavity 121 from a plurality of independent stages. The second reaction zone S2 ° In the present embodiment, the number of the second partition plates 227 is, for example, eight, to divide the second recombination cavity 122 into eight symmetrical second reaction zones S2° similar to the foregoing, the second reaction The gas flow in the region S2 is liable to form a fully developed turbulent flow so that the completely mixed gas component in the high temperature reaction gas can more sufficiently contact the catalyst in the second reaction region S2 to enhance the reaction effect. Of course, the present invention does not limit the first partitioning plate 226 and the second partitioning plate 22 I3〆

The number and shape of 2 are not limited to the shape of the first reaction zone SI or the second reaction zone S2. For example, the first divider 226a' is also 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 crucible according to another embodiment of the present invention, and the first catalyst bed is omitted, and FIG. 3B is a cross-sectional view of the disc-shaped preheating passage along the BB. View on the section. Referring to FIG. 3A, the plasma-assisted catalyst recombining device 300 of the present embodiment is similar to the aforementioned electric-meal-catalyst recombining device 100 (shown in FIG. 1A), and the difference is only in the plasma-assisted catalyst. The preheater 330 of the reconstitution device 300 further includes a disk-shaped pre-heating 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 112a. between. In response to the above, the disk-shaped preheating passage 336 has an air passage spirally surrounding the plasma chamber 112, and the air and methane will enter the disk-shaped preheating passage 336 from the preheating pipe 134, and follow the air passage in the disk-shaped preheating passage 336. The inner winding 'and finally 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 chamber 112 is also relatively high. By means of the design of the disk-shaped preheating passage 336, the heat in the plasma chamber 112 can be transferred outward along the disk-shaped preheating passage 336 to further heat the air in the disk-shaped preheating passage 336. Methane. 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 re-leveling device 400 of the present embodiment is similar to the plasma assisted catalyst recombining device 100 (shown in FIG. 23 1379710). The difference is only in the plasma assisted catalyst recombining device. The preheater 430 of 400 further includes a third partitioning plate 438, and the third partitioning plate 438 is disposed in the preheating cavity 132 to distinguish the preheating cavity 132 into the connected first preheating zone T1 and a second 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 T2 is located The periphery of the first preheating zone T1. Thus, the high-temperature reformed gas entering the preheating chamber 132 from the recirculation pipe 123 sequentially passes through the first preheating zone T1 and the second preheating zone T2, thereby causing the high temperature reformed gas to transfer heat to the periphery. Generally, the high temperature reformed gas still has some carbon monoxide, and carbon monoxide is toxic to humans. Therefore, carbon monoxide selective oxidation (CO Preferential Oxidation) can be disposed in the first preheating zone T1 and the second preheating zone T2. The medium is used to convert carbon monoxide into carbon dioxide. Of course, the present invention does not limit 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 reconfigured 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 preheat the third partitioning plate 438 according to the foregoing. The 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. Hereinafter, the electro-hydraulic/assisted catalyst recombination apparatus will be slightly modified so that it can also be applied to the recombination reaction of the hydrogen-trapping liquid. 5A is a schematic 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, A schematic cross-sectional view of a three-catalyst 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 (flat average particle size smaller than ΙΟμιη) are fed to the mixing chamber 142 and mixed with 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. φ 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 the hydrocarbon liquid to be completely burned (completely oxidized and recombined) or not completely burned (incompletely oxidized and recombined). 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 1379710, and the carbon enthalpy liquid is gradually changed to partial combustion. A similar procedure has been described in detail in the start-up process of the aforementioned smoldering, and those skilled in the art can easily understand it, and will not be described again. In the present embodiment, the hydrocarbon liquid is exemplified by, for example, alcohol, but the present invention does not limit the type of the hydrocarbon liquid, and the hydrocarbon 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 into 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. • Next, the air, atomized alcohol and atomized water will enter the preheating tube 134 for heating, similar to the above, at this time, the preheating chamber 132 is filled with high temperature gas, and the atomized alcohol and atomized The water is heated to form a vaporized alcohol and vaporized water. It is worth noting that the average particle size of the fine mist droplets is smaller than ΙΟμιη, 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 piezoelectric atomization in this embodiment. 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 ions, electrons and free radicals are formed by the discharge phenomenon in the plasma chamber 112 26 1379710. Quasi-neutral mixed gas (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 reaction will be carried out on the surface of the catalyst in the front region of the recombination reaction, gradually producing carbon monoxide, carbon dioxide, hydrogen and water. At this time, these carbon monoxide, carbon dioxide, hydrogen, water damage (gaseous), unreactive nitrogen, have not yet The reacted 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 warming reaction gas will continue to react from the first recombination chamber outlet 1211 into the second recombination chamber 122. Similar to the above, the unreacted alcohol molecules and oxygen molecules in the high temperature reaction gas will be in the middle and rear stages of the recombination reaction. The surface of the catalyst is partially oxidized and recombined, and the unreacted alcohol molecules and oxygen molecules are gradually converted into carbon monoxide, oxidizing, hydrogen and water (gaseous). As a result, the carbon monoxide, carbon dioxide, hydrogen, water (gaseous), and unreacted nitrogen in the post-recombination reaction zone of the first catalyst bed 125 form a high temperature reformed gas (not shown). The south temperature reformed gas enters the recirculation tube 123 from the first recombination chamber opening 12ic to enter the preheating chamber 132 along the recirculation tube 123 to heat the air in the preheating tube 132, atomized alcohol and atomization. The moisture, and the heated air and the vaporized alcohol and water in the preheating tube 132 are more easily activated and activated after entering the plasma chamber 112. Similar to the foregoing, in order to further increase the content of hydrogen in the high-temperature reformed gas or reduce the content of carbon monoxide in the temperature-recombinant gas, in this embodiment, 27 1379710 may re-dispose the catalyst in the preheating chamber 132 to recombine the high-temperature recombination gas. Carry out the reaction. Referring to FIG. 5A to FIG. 5B respectively, 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 disposed in the preheating cavity 132. The preheating chamber 丨32 is divided into the first preheating zone T1 and the second preheating zone T2, wherein the preheating pipe 134 is along the first preheating zone T1 and the second preheating zone T2. Layer wrapping

Around the recombination reactor 120, the second preheating zone Τ2 is located at the periphery of the first preheating zone Τ1. In addition, the preheater 530 may further include a second catalyst bed 531, a third catalyst bed 533 and a fourth catalyst bed 535, and the second catalyst bed 531 may be located at: pre=T1' and the third catalyst The bed 533 can be located at the first preheating zone T1 and ί and the fourth catalyst bed 535 can be located in the second preheating

The second catalyst bed 531 may have a high temperature water vapor shift. The fourth catalyst medium may have a low temperature water vapor transfer catalyst, and the niobium may have a carbon monoxide selective oxidation catalyst. In order to use a high-temperature reforming gas in a three-catalyst bed, t C I31 and a third catalyst bed 533, the transfer catalyst and the lower ^7 and the carbon monoxide will generate hydrogen in the high temperature water: Oxygen reduces the amount of carbon monoxide. The helium enthalpy content, and in addition, the gas transfer reaction is an exothermic process, so the released 28 1379710 heat can be further transferred to the preheating pipe 134 to heat the air in the preheating pipe 134 and The atomized alcohol and water are heated to form vaporized alcohol and moisture, thereby increasing the overall heat utilization rate of the plasma assisted catalyst recombination device 500. It should be noted that after the high-temperature water-gas conversion catalyst passing through the second catalyst bed 531, if the concentration of carbon monoxide in the high-temperature reformed gas can be reduced to 2% (Vol.), the third embodiment can also be omitted. The low temperature water gas conversion catalyst of the catalyst bed 533 is used to reduce the construction cost of the plasma auxiliary catalyst recombination device 500. • After passing through the second catalyst bed 531 and the third catalyst bed 533, the high temperature reformed gas usually still retains about 2% (Vol.) concentration of carbon monoxide, and gradually lowers the temperature to form a t-temperature reformed gas (not shown) ). In the fourth catalyst bed 535, residual carbon monoxide molecules and oxygen molecules in the intermediate temperature reformed gas are oxidatively recombined on the surface of the carbon monoxide selective oxidation catalyst to generate carbon dioxide and release heat to heat the preheating tube 134 to The overall heat utilization rate of the plasma assisted catalyst recombination device 500 is increased. After passing through the fourth catalyst bed 535, the intermediate temperature reformed gas gradually lowers the temperature B to form a low temperature reformed gas, wherein the low temperature reformed gas is rich in hydrogen fuel, and there is almost no residual carbon monoxide harmful to the human body. Finally, the cryogenic recombination gas exits the preheating chamber 132 from the preheating chamber outlet 132b and is delivered to the downstream unit as a fuel. It is worth noting that the aforementioned high temperature recombination gas, medium temperature recombination gas and low temperature recombination gas are only conceptual differences, and the present invention does not specifically distinguish the exact position where it is located. That is, high temperature, medium temperature or low temperature reformed gas is only a phased term for the concept of converting carbon monoxide to hydrogen or removing residual carbon monoxide, and familiarity with this technique can be easily understood without confusion. In addition, carbon monoxide is also a kind of mosquito of the fuel, and it is also possible to directly supply the gas from the preheating chamber without providing the second catalyst bed 531 and the catalyst bed 535.

In the case of gasification, it is also a type of biofuel, which in turn reduces the amount of emissions. Because plants are produced from the environment after the absorption of carbon atoms, such as alcohol, such as alcohol, so the burning of alcohol and other raw fuels only ^ the circulation of the earth's environmental carbon atoms, the shirt will increase the secret line environment: the total amount of carbon 'Therefore, the goal of environmental protection can be achieved.

The right does not want to remove the oxidized second catalyst bed 533 and the 132b to collect the high temperature recombination π and refer to the heads 5A to 5B, in order to improve the reaction efficiency of the medium temperature reformed gas in the fourth catalyst 535 to completely remove the residual carbon monoxide, The preheating chamber 132 of the present embodiment further has a preheating chamber opening 132c so that air can enter the preheating chamber 132 from the preheating chamber opening 132c, so that oxygen molecules in the air can be selectively oxidized and oxidized. The surface of the medium is oxidatively recombined with residual carbon monoxide. Of course, the feeder 54 can further have a fifth regulating valve 549, and the fifth regulating valve 549 is connected to the preheating chamber opening 132c to regulate the flow of air. The person skilled in the art can easily understand that, Let me repeat. 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 to 30 ^ 379 710 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 into a high-temperature reaction gas by a recombination reactor, and then the high-temperature reaction gas is subjected to a high-temperature reaction gas. Recombination forms a high temperature reformed gas, wherein the high temperature reformed gas is adapted to heat the atomized hydrocarbon liquid and moisture to vaporize the atomized hydrocarbon liquid and moisture. In summary, the plasma assisted catalyst recombination apparatus and method of the present invention have at least the following advantages: 1. The recirculation pipe is configured to 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 reorganization The volume of the reactor is reduced to reduce manufacturing costs. In addition, when the high-temperature reformed gas flows into the recirculation pipe, the heat in the region before the recombination reaction can be carried to the middle portion of the recombination reaction to increase the temperature uniformity of the first catalyst bed, thereby further increasing the recombination efficiency. 2. The start-up procedure is completed by adjusting the flow rate of the hydrocarbon gas (or hydrocarbon liquid) to the air to cause the hydrocarbon gas to be completely combusted to heat the first catalyst bed, thereby allowing the first catalyst bed to reach the operating temperature. . Therefore, the present invention does not require any additional auxiliary heaters, thereby reducing the cost of construction, reducing the overall equipment volume, and avoiding the danger of providing an auxiliary heater. 3. By means of the preheating tube setting, the residual heat of the high temperature reformed gas can be utilized to heat the air in the preheating tube, the hydrocarbon gas, the atomized hydrocarbon liquid or the atomized water, etc., thereby enhancing the excitation activation. effect. Since it is not necessary 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 size of the device can be reduced. 31 1379710 The preheater is a coated 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, thereby improving the overall heat utilization. Rate and avoid the risk of direct contact with high temperature recombination reactors. 5. By the arrangement of the first partitioning plate and the second dividing plate, the gas can be fully developed turbulent flow to further improve the efficiency of catalytic recombination conversion. 6. By the arrangement of the disk-shaped preheating passage, the heat in the plasma chamber can be absorbed to prolong the life of the plasma reactor. • 7. Using the second catalyst bed, the third catalyst bed and the fourth catalyst bed to recombine with the high temperature reformed gas, in addition to increasing the hydrogen content and reducing the carbon monoxide content, the heat released by the recombination reaction can be simultaneously The gas in the preheating tube or the atomized liquid is heated to increase the overall heat utilization rate. 8. When alcohol is used as a hydrocarbon liquid to produce hydrogen fuel, it will not achieve an increase in the total amount of carbon dioxide in the earth's air environment, thereby achieving environmental protection goals. While the present invention has been described in its preferred embodiments, it is not intended to limit the invention, and the invention may be modified and modified without departing from the spirit and scope of the invention. The scope of the invention is defined by the scope of the appended claims. 32 1379710 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. • Figures 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, the third catalyst bed and the fourth catalyst bed removed from the plasma assisted catalyst recombination apparatus of Figure 5A. FIG. 6 is a schematic flow chart of a plasma assisted catalyst recombination method according to an embodiment of the invention. [Main component symbol description] 100, 200, 300, 400, 500: plasma assisted catalyst recombination device 33 1379710 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 • 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: multi-plate 125: first catalyst bed φ 130, 330, 430: preheater 132: preheating chamber. 132a Preheating chamber inlet 132b: preheating chamber outlet 132c: preheating chamber opening 134: preheating tube 140, 540: feeder 142: mixing chamber 145: first regulating valve 34 1379710 146: second regulating valve 226, 226a : first partition plate 227 : second partition plate 336 : disk-shaped preheating passage 438 , 538 : third partition plate 531 : second catalyst bed 533 : third catalyst bed 535 : fourth catalyst bed • 544: Piezoelectric atomization unit 547: third regulating valve 548: fourth regulating valve 549: fifth regulating valve S1 first reaction zone S2 second Shall preheating zone T2 T1 of the first area of the second preheating zone S1- "S4: Step 35

Claims (1)

1379710 VII. Patent application scope: 1. A plasma auxiliary catalyst recombining device, comprising: a feeder having a mixing chamber; a plasma reactor comprising: a plasma chamber having a plasma 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; • a recombination reactor, connected 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 inlet is connected to the a 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 recirculation tube, a portion Located in the first recombination chamber, one end of the recirculation tube is connected to the first recombination chamber opening, and the other end of the recirculation tube is passed through the second recombination chamber outlet to pass through the second recombination a cavity σ; a porous plate, Disposed in the first recombination chamber and adjacent to the first recombination chamber inlet; a first catalyst bed disposed in the first recombination chamber and the second recombination chamber; a preheater comprising: a preheating chamber, wherein the recombination reactor is located in the preheating chamber 36 1379710, and the preheating chamber has a preheating chamber inlet and a preheating chamber outlet; and a preheating tube disposed at the The preheating chamber is surrounded by the recombination reactor, and 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 out of 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 hydrocarbon 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 hydrocarbon gas, and exit the preheating chamber from the preheating chamber outlet. 3. The plasma assisted catalyst reassembly apparatus according to 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 second regulating valve is 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 catalytic reassembly of the first embodiment of the invention is as follows: 37 u/9710 wherein the preheater further comprises a disk-shaped preheating passage disposed in the preheating chamber and connected to Between the end of the heat pipe and the population of the electricity (four). 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 money assisted catalyst reassembly according to item 7 of the patent scope of the towel, wherein the first partition is a cross partition or a cross-shaped partition. 9. The plasma assisted catalyst reassembly according to claim 4 (4), wherein the recombination reactor further comprises a second partition plate disposed in the first recombination chamber. The plasma-assisted catalytic reassembly of the first aspect of the invention, wherein the preheater further comprises a third partition plate disposed in the preheating chamber to preheat the The cavity is divided into one of the first pre-twisting zones and one of the preheating zones. 8. 11. The electric I assisted catalyst recombination as described in the 1G item of Zhongyi Patent 1 1L. The lining of the lining is to rewind the recombination reactor along the first g-zone preheating zone. 12. The plasma-assisted catalyst recombination as described in paragraph 1 () of the Chinese patent, wherein the preheating 9 further comprises a second catalyst bed, a third catalyst bed ς - a fourth catalyst bed, The second catalyst bed is located in the first preheating zone, and the first catalyst bed is located at the boundary between the first preheating zone and the second preheating zone, and the fourth catalyst bed is located in the second preheating zone. Hot zone. 13. The plasma-assisted catalyst recombination according to claim 12, wherein the second catalyst bed has a high temperature water gas transfer catalyst, and the third medium bed has a low temperature water gas transfer catalyst, and The fourth catalyst bed has a oxidized 38 1379710 carbon selective oxidation catalyst. 14. The plasma assisted catalyst reassembly of claim 1, wherein the feeder further has a piezoelectric atomizing unit coupled 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 mix with air entering one of the mixing chambers and entering the preheating tube, atomizing the hydrocarbon liquid and the water in the preheating tube to form a vaporized hydrocarbon liquid and the water 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, atomized hydrocarbon liquid and atomized water in the preheating tube, and self preheating The chamber outlet exits the preheating chamber. 16. The plasma assisted catalyst recombination device of claim 15, wherein the hydrocarbon liquid is alcohol or liquefied petroleum gas. 17. The plasma assisted catalyst recombination 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 a regulating valve is connected to the mixing chamber to control a flow rate of air entering 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 The flow into the piezoelectric atomizing unit. 18. The plasma assisted catalyst recombination 39 1379710 device of claim 14, wherein the preheating chamber further has a preheating chamber opening to allow an air to enter the preheating from the preheating chamber opening. Inside the cavity. 19. The plasma assisted catalyst recombining device 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 atomizing unit to atomize a hydrocarbon liquid with one water; providing an air; # mixing the air and atomizing the hydrocarbon liquid with The water, and atomizing the atomized hydrocarbon liquid with the water; providing a plasma reactor to excite the air and the vaporized hydrocarbon liquid and the moisture 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 high temperature reformed gas is suitable for heating the atomized hydrocarbon liquid And the moisture to vaporize the atomized hydrocarbon liquid with the water. • 21. The plasma assisted catalyst recombination method of claim 20, wherein the hydrocarbon liquid is alcohol or liquefied petroleum gas. 40