A reactor that converts dimethyl ether into hydrogen

Abstract

[0003] Methods, apparatus, and systems for a reactor for converting dimethyl ether to hydrogen are described. The reactor includes an outer tube configured to contain heat. The reactor includes an inner tube nested within the outer tube, the inner tube configured to conduct the heat contained in the outer tube. The inner tube forms a reaction chamber between first and second ends of the plurality of inner tubes. The reactor includes a feed line connected to one end of the plurality of inner tubes. The feed line is configured to pass dimethyl ether and steam through the inner tube. The reactor includes a reactor outlet configured to collect hydrogen from the inner tube and discharge the hydrogen.

Description

[Technical Field]

[0001] (Cross-reference to application) This application claims the benefit of and priority to U.S. Patent Application No. 18 / 063,989, entitled "Reactor for Converting Dimethyl Ether to Hydrogen," filed December 9, 2022. This application also claims the benefit of and priority to U.S. Provisional Application No. 63 / 413,136, entitled "Reactor for Converting Dimethyl Ether to Hydrogen," filed October 4, 2022. The disclosures of these applications are incorporated herein by reference in their entireties.

[0002] The present disclosure relates generally to energy conversion, and more particularly to a reactor that converts dimethyl ether to hydrogen. [Background technology]

[0003] Hydrocarbon fuels are widely used in energy consumption devices and energy production. Many devices and systems that utilize hydrocarbon fuels, such as fuel cells, require the fuel to be reformed to produce hydrogen (H2). For example, fuel cell vehicles require high-purity hydrogen as a fuel for propulsion. Currently, low-temperature electrolysis and steam methane reforming are used to produce hydrogen from water and hydrocarbon fuels, respectively. In low-temperature electrolysis, hydrogen is generated from water in an electrolyzer. This process is highly inefficient due to the large power consumption required for low-temperature electrolysis.

[0004] Additionally, conventional technologies for producing hydrogen from natural gas and other fuels suffer from inefficient conversion of methane and carbon monoxide to hydrogen, resulting in excessive carbon dioxide emissions. For example, conventional hydrogen production and separation systems using steam methane reformers suffer from high operating temperatures, requiring large amounts of natural gas fuel, and from inability to convert all of the methane to hydrogen. As a result, a significant amount of the input energy is converted into heat. This heat generation leads to further inefficiencies. To make matters worse, conventional technologies consume fossil fuels, require external fuel to drive the reaction, and do not utilize waste heat from other sources to improve efficiency.

[0005] Furthermore, these conventional systems suffer from reduced efficiency and increased costs when scaled down from the currently typical 500,000 kilograms per day systems. Furthermore, conventional systems typically produce significant amounts of NOx in addition to high carbon dioxide emissions. This makes it difficult to obtain permits to install and operate these conventional systems, especially in non-industrial areas. In the case of renewable fuels, such systems operate at even lower efficiency due to the need for carbon dioxide-diluted fuel and compression of the fuel stream. Therefore, improved technologies / processes and reactors for producing hydrogen are needed to meet the demand for clean, efficient, sustainable, and mass-producible green / renewable hydrogen.

[0006] Adapting these currently available processes to generate hydrogen on-site at hydrogen fueling stations or hydrogen fueling transportation hubs is not easy. These processes require transporting hydrogen from the production facility to the hydrogen station, which is highly inefficient and costly. The proposed process technology and reactor design described below overcome these hurdles and challenges. Summary of the Invention

[0007] The present disclosure relates generally to energy conversion, and more particularly to a reactor that converts dimethyl ether to hydrogen.

[0008] In one aspect, the present specification discloses an apparatus for a reactor. The reactor includes an outer tube configured to contain heat. The outer tube has an outer tube diameter. The reactor includes an inner tube nested inside the outer tube. The inner tube is configured to conduct the heat contained in the outer tube, has an inner tube diameter smaller than the outer tube diameter, has a first end and a second end, and forms a reaction chamber between the first end and the second end. The reactor includes a feed line connected to the first end of the inner tube. The feed line is configured to pass dimethyl ether and steam through the inner tube. The reactor includes a reactor outlet adjacent the second end of the inner tube. The reactor outlet is configured to collect hydrogen from the inner tube and discharge the hydrogen.

[0009] In some variations, the reaction chamber is configured to house a catalyst, the catalyst configured to receive heat housed in the outer tube, the heat housed in the outer tube having a uniform temperature along the length of the outer tube. Furthermore, the reaction chamber produces hydrogen based on a cooperative reaction of dimethyl ether and steam with the catalyst heated by the heat housed in the outer tube. Furthermore, the catalyst includes an acid catalyst and a reforming catalyst. Furthermore, methanol is produced by hydrolysis of dimethyl ether over the acid catalyst, and steam reforming of methanol is produced over the reforming catalyst.

[0010] In some variations, the heat contained in the outer tube is steam heat, and the inner tube is configured to conduct the heat contained in the outer tube. Furthermore, the outer tube and the inner tube are oriented vertically. Furthermore, the outer tube further comprises a steam inlet for the outer tube and a steam condensate outlet for the outer tube. Furthermore, a space between the outer tube and the inner tube allows steam to circulate and condense within the outer tube.

[0011] In another aspect, disclosed herein is an apparatus for a reactor. The reactor includes a casing configured to contain heat. The reactor includes a plurality of tubes nested within the casing. The plurality of tubes are configured to conduct heat contained within the casing. Each of the plurality of tubes has a first end and a second end, forming a reaction chamber between the first end and the second end. The reactor includes a supply line connected to each of the first ends of the plurality of tubes. The supply line is configured to pass dimethyl ether and steam through the plurality of tubes. The reactor includes a reactor outlet adjacent each of the second ends of the plurality of tubes. The reactor outlet is configured to collect hydrogen from the plurality of tubes and discharge the hydrogen.

[0012] In some variations, the heat is generated by a plurality of electric heating elements inside the casing and outside the plurality of tubes, the plurality of tubes being configured to conduct heat contained in the casing, the casing further comprising a refractory surface along an interior portion of the casing, and a layer of insulation between the refractory surface and an exterior portion of each of the plurality of tubes.

[0013] In yet another variation, another reactor apparatus is disclosed herein. The reactor includes a shell configured to contain heat. The reactor includes a plurality of tubes nested within the shell. The plurality of tubes are configured to conduct heat from the heat contained within the shell. Each of the plurality of tubes has a first end and a second end, forming a reaction chamber between the first end and the second end. The reactor includes a supply line connected to each of the first ends of the plurality of tubes. The supply line is configured to receive dimethyl ether and steam. The reactor includes a reactor outlet adjacent each of the second ends of the plurality of tubes. The reactor outlet is configured to discharge hydrogen.

[0014] In some variations, the reactor further comprises a plurality of burners configured to generate heat housed inside the shell. The reactor further comprises a shell outlet configured to discharge fuel gas. Further, the plurality of burners are configured to be turned on simultaneously to maintain a uniform temperature. The shell is a fire box.

[0015] In yet another variation, another reactor apparatus is disclosed herein. The reactor includes a shell configured to contain heat. The reactor includes an upper tube plate connected to an upper portion of the shell. The upper tube plate has a plurality of upper tube plate openings. The reactor includes a lower tube plate connected to a lower portion of the shell. The lower tube plate has a plurality of lower tube plate openings. The reactor includes a plurality of tubes configured to extend between the upper tube plate and the lower tube plate. Each of the plurality of tubes is configured to be inserted inside an upper tube plate opening of the plurality of upper tube plate openings and a lower tube plate opening of the plurality of lower tube plate openings. Each of the plurality of tubes is configured to conduct heat from heat contained inside the shell, forming a reaction chamber between the upper tube plate and the lower tube plate. The reactor includes a feed line adjacent to an upper portion of the shell. The feed line is configured to pass dimethyl ether and steam through the plurality of tubes. The reactor includes a reactor outlet adjacent to a lower portion of the shell. The reactor outlet is configured to collect hydrogen from the plurality of tubes and discharge the hydrogen.

[0016] In some variations, the reaction chamber is configured to contain a catalyst. The catalyst is configured to receive heat contained in the plurality of tubes. The heat contained in the shell has a uniform temperature between the upper tube plate and the lower tube plate. Furthermore, the shell and the plurality of tubes are vertically oriented. Furthermore, the shell further comprises an inlet for heating the plurality of tubes with at least one of steam or heating oil and an outlet for draining condensate from inside the shell. Furthermore, a space between the shell and the plurality of tubes allows at least one of steam or heating oil to circulate inside the plurality of tubes.

[0017] In yet another variation, another reactor apparatus is disclosed herein. The reactor includes a shell having a reaction chamber. The reaction chamber is configured to contain a fluidized catalytic reaction bed. The reactor includes a heat source configured to extend from an upper portion of the reaction chamber to a lower portion of the reaction chamber. The heat source is configured to heat the fluidized catalytic reaction bed. The reactor includes a feed line proximate to a lower portion of the reaction chamber. The feed line has a plurality of feed line openings. Each feed line opening of the plurality of feed line openings is configured to pass dimethyl ether and steam to the reaction chamber. The reactor includes a reactor outlet proximate to a top of the shell. The reactor outlet is configured to collect hydrogen from the reaction chamber and discharge the hydrogen.

[0018] In some variations, the shell is oriented vertically, and the fluidized catalytic reaction bed is configured to circulate within the reaction chamber. Furthermore, the heat source is at least one of an electric coil or a tube containing steam, winding in alternating directions within the reaction chamber, and the fluidized catalytic reaction bed is configured to conduct heat from the at least one of the electric coil or the tube containing steam. Furthermore, the reaction chamber produces hydrogen based on a cooperative reaction of dimethyl ether and steam with the fluidized catalytic reaction bed heated by the heat source. Furthermore, the shell further includes a dimethyl ether vapor outlet connected to the supply line. The dimethyl ether vapor outlet is configured to discharge excess dimethyl ether and steam from the reaction chamber to the supply line, thereby recycling the excess dimethyl ether and steam.

[0019] In yet another variation, the present specification discloses a system for measuring a reaction. The reaction measurement system also includes a supply line valve configured to control flow of dimethyl ether and steam into an inner tube. The inner tube is nested within an outer tube and configured to conduct heat contained in the outer tube, the inner tube having an inner tube diameter smaller than the outer tube diameter, forming a reaction chamber. The system also includes a thermal sensor configured to determine a temperature of the heat contained in the outer tube. The system also includes a controller communicatively connected to the supply line valve and the thermal sensor. The controller is configured to determine the temperature of the heat contained in the outer tube based on the thermal sensor and adjust the supply flow rate through the supply line valve in response to the temperature of the heat satisfying a temperature threshold.

[0020] In some variations, the reaction measurement system includes a vapor dimethyl ether ratio sensor configured to output a vapor dimethyl ether ratio measurement representative of the vapor dimethyl ether ratio in the reaction chamber, a controller communicatively coupled to the vapor dimethyl ether ratio sensor and configured to determine the vapor dimethyl ether ratio measurement based on the vapor carbon ratio sensor, compare the vapor dimethyl ether ratio measurement to the vapor carbon ratio, and adjust the feed flow rate at the feed line valve in response to the comparison.

[0021] In some variations, the system further includes a pressure sensor configured to output a pressure measurement representative of an outlet pressure in the outlet line and a backpressure valve in the outlet line configured to control the outlet pressure in the outlet line, and a controller communicatively coupled to the pressure sensor and the backpressure valve and configured to determine the pressure measurement in the outlet line based on the pressure sensor and adjust the outlet pressure with the backpressure valve in the outlet line in response to the pressure measurement meeting the outlet pressure threshold.

[0022] In some variations, the system includes at least one carbon monoxide sensor or carbon dioxide sensor configured to output at least one carbon monoxide measurement or carbon dioxide measurement representative of at least one of carbon monoxide or carbon dioxide in the reaction chamber, and a controller communicatively coupled to the at least one carbon monoxide sensor or carbon dioxide sensor and configured to determine the at least one of carbon monoxide or carbon dioxide in the reaction chamber based on the at least one carbon monoxide sensor or carbon dioxide sensor, and adjust the supply flow rate at the supply line valve in response to the at least one carbon monoxide measurement or carbon dioxide measurement meeting at least one carbon monoxide threshold or carbon dioxide threshold.

[0023] In some variations, the system includes a hydrogen sensor configured to output a hydrogen sensor measurement representative of hydrogen at a reactor outlet adjacent one end of the inner tube, the hydrogen sensor measurement being indicative of a cooperative reaction of the catalyst in the reaction chamber with dimethyl ether and steam. A controller is communicatively coupled to the hydrogen sensor and configured to determine the hydrogen sensor measurement at the reactor outlet adjacent one end of the inner tube based on the hydrogen sensor, and adjust the feed flow rate with the feed line valve in response to the hydrogen sensor measurement satisfying a hydrogen threshold. [Brief explanation of the drawings]

[0024] The embodiments herein may be better understood by reference to the following description in conjunction with the accompanying drawings, where like reference numbers indicate identical or functionally similar elements and in which:

[0025] [Figure 1] FIG. 1 illustrates an example of a steam-heated reactor comprising an inner tube nested within an outer tube configured to contain steam. [Figure 2A] FIG. 1 illustrates an example of an electrically heated reactor comprising tubes nested within a casing configured to contain heat generated by a heating element. [Figure 2B]FIG. 1 illustrates an example cross section of an electrically heated reactor comprising tubes nested within a casing configured to contain heat generated from a heating element. [Figure 3] FIG. 1 illustrates an example of a burner-heated reactor comprising multiple tubes nested within a shell configured to contain heat generated from a fuel-fired burner. [Figure 4] FIG. 1 shows an example of a double plate reactor with multiple tubes extending between an upper tube plate and a lower tube plate. [Figure 5] FIG. 1 illustrates a fluidized catalytic reactor comprising a fluidized catalytic reaction bed nested within a reaction chamber configured to accommodate a heat source extending from the bottom of the reaction chamber to the top of the heat chamber. [Figure 6A] 1 is a table showing exemplary specifications for dimethyl ether fed to a feed line to a reactor that converts dimethyl ether to hydrogen. [Figure 6B] 1 is a table showing exemplary specifications for steam supplied to a feed line to a reactor that converts dimethyl ether to hydrogen. [Figure 6C] 1 is an example of a table showing exemplary product compositions expected from a reactor. [Figure 6D] 1 is an example table showing exemplary specifications for purified hydrogen exiting a pressure swing adsorption system after a reactor converts dimethyl ether to hydrogen. [Figure 7] FIG. 1 is an example of a block diagram showing the overall process flow for converting dimethyl ether and steam to hydrogen. [Figure 8] FIG. 1 is an example block diagram showing a DME vapor supply process flow for converting dimethyl ether into hydrogen. [Figure 9] FIG. 1 is an example of a block diagram illustrating a hydrogen purification process. [Figure 10] FIG. 1 is an example of a block diagram including a controller configured to send instructions to reactor hardware based on reactor sensors. [Figure 11] FIG. 1 is a block diagram illustrating a computing system consistent with embodiments of the present subject matter. DETAILED DESCRIPTION OF THE INVENTION

[0026] The methods, systems, and apparatus described herein are for a reactor that converts dimethyl ether to hydrogen. In the following detailed description, reference is made to the accompanying drawings, which form a part of this specification. In the drawings, like numerals generally refer to like elements unless the context dictates otherwise. The exemplary alternatives described in the detailed description, drawings, and claims are not meant to be limiting. Other alternatives may be utilized and other changes may be made without departing from the spirit or scope of the subject matter presented herein. It will be readily understood that the aspects as generally described herein and illustrated in the figures may be arranged, substituted, combined, and designed in a wide variety of different configurations, all of which are expressly contemplated and made a part of this application.

[0027] The reactor described herein is configured to convert dimethyl ether into hydrogen. Unlike conventional systems, the reactor described herein is clean, efficient, and suitable for mass production of hydrogen by using renewable dimethyl ether (DME) as a feedstock to produce renewable hydrogen. A feed line delivers mixed steam and dimethyl ether to the reactor. The feed line passes the mixed steam and dimethyl ether to a reaction chamber. The reaction chamber contains a catalyst configured to receive heat for converting the steam and dimethyl ether to hydrogen. The reaction chamber produces hydrogen based on a cooperative reaction between the dimethyl ether and steam mixture and the catalyst in response to the catalyst and reactants being heated.

[0028] The reactors described herein may be of isothermal design. An isothermal design may allow for a thermodynamic process in which the temperature of the reactor system remains fairly constant. Heat transfer into the system occurs at a rate that maintains thermal equilibrium. Unlike conventional systems, the reactor can be at a constant temperature by using saturated steam at a constant pressure. In some embodiments, the reactor design may be a multi-tube reactor, with each tube packed with catalyst. Steam may be supplied to each tube to maintain a constant reaction temperature within the inner tube. The latent heat from condensation of the steam can provide the necessary heat for the reactor and maintain a constant temperature.

[0029] The isothermal design and heat source of the reactor are a significant improvement over conventional systems that require significantly higher temperatures for operation. The isothermal design of the reactor described herein allows for an operating temperature of 225-300°C, as opposed to operating temperatures in excess of 1000°C in conventional systems. Furthermore, the operating pressure of the reactor described herein is between 8-17 bar, and the steam-to-dimethyl ether molar ratio is between 2-4.

[0030] Unlike conventional systems for producing hydrogen, a catalyst may be heated to induce the reaction from dimethyl ether to hydrogen. Dimethyl ether can be reacted (or reformed) with water in the form of steam to produce hydrogen using a catalyst based on Gibbs free energy and theoretical thermodynamic reaction equations. Understanding Gibbs free energy requires the use of specific catalysts to drive the necessary reactions and inhibit which reactions. Acid catalysts and copper-zinc catalysts (reforming catalysts) may also be used to convert dimethyl ether to hydrogen.

[0031] The catalyst requires heat to produce hydrogen. The conversion reaction from dimethyl ether to hydrogen is an endothermic reaction and requires a heat supply for the reaction. More specifically, the catalyst and reactants require heat to carry out a cooperative reaction between the dimethyl ether and steam mixture to produce hydrogen. Heat passes through the reaction chamber. The heat passing through the reaction chamber may be contained in an inner tube, a shell, a casing, an outer tube, etc. The heat may be generated by steam, an electric heating element, fuel combustion, heated oil, and / or the like. In one example, the heat is contained in an outer tube with a nested inner tube. The inner tube may be configured to conduct heat contained in the outer tube. The space between the outer and inner tubes allows heat (e.g., steam) to circulate and condense within the outer tube. One feature of the reactor is its ability to adjust the heat demand for generating the reaction and its ability to supply the required heat from a heating medium.

[0032] In some embodiments, the tubes are configured to produce 50 kg or more of hydrogen per day. The outer dimensions of the tubes control the dimensions of the reaction chamber, which are selected based on the reactivity of the components, heat transfer to the catalyst within the reaction chamber, and the required gas hourly space velocity. That is, balanced reactivity of the components being converted to hydrogen must be coordinated with heat transfer between the catalyst and the mixture of dimethyl ether and steam. Timing reactions and actions must be coordinated and balanced. If the reaction and heat transfer are not synchronized, inefficient hydrogen conversion will result in excessive non-reaction of the components. That is, improper temperatures will result in unbalanced heat transfer and incomplete reactions. Incomplete reactions lead to waste, excessive emissions, and reduced energy efficiency.

[0033] To increase the likelihood that the reaction and heat transfer are coordinated within the reactor, a two-stage process for producing hydrogen from dimethyl ether via steam reforming is based on reaction kinetics and the Gibbs free energy principle. First, dimethyl ether can be hydrolyzed to produce methanol over an acid catalyst, and then the methanol can be steam reformed over a copper-zinc catalyst. The dimethyl ether steam reforming reaction can be endothermic. In the process of producing hydrogen, the hydrolysis reaction of dimethyl ether to methanol is the limiting reaction. The catalyst can promote the reaction that produces hydrogen. Methanol is an intermediate product of the dimethyl ether steam reforming process. A catalyst containing copper and zinc oxide promotes the production of both hydrogen and methanol.

[0034] Carbon dioxide and carbon monoxide are by-products of the two-stage process. However, these by-products can be minimized by appropriate process operating conditions, and optionally by a water-gas shift reaction. The mole fraction of carbon monoxide increases with increasing temperature for a given steam-dimethyl ether ratio and decreases with increasing steam-dimethyl ether ratio at a given temperature. To minimize carbon monoxide and optimize hydrogen production, a relatively low temperature range and a relatively high steam-dimethyl ether ratio may be applied within the reaction chamber. Furthermore, reducing the operating pressure improves hydrogen production efficiency based on Le Châtelier's principle.

[0035] Based on the above thermodynamics, the ideal catalyst is a bifunctional catalyst, which may be a physical mixture of an acid catalyst for DME hydrolysis and a copper-zinc catalyst for methanol steam reforming.

[0036] The catalyst may include an acid catalyst and a reforming catalyst. Methanol is produced by hydrolyzing dimethyl ether over the acid catalyst, and hydrogen is produced by steam reforming of methanol over the reforming catalyst. In some embodiments, one-third of the catalyst is an acid catalyst, and two-thirds of the catalyst is a mixture of reforming catalysts (copper-zinc). The acid catalyst may be a hydrolysis catalyst. The acid catalyst can convert or hydrolyze a sufficient amount of dimethyl ether to methanol.

[0037] Reaction thermodynamics suggests that the conversion reaction from dimethyl ether to hydrogen is carried out based on the reaction temperature, reaction pressure, catalyst properties, and steam-dimethyl ether ratio. In some embodiments, the reactor operating temperature is between 225°C and 300°C, the reactor operating pressure is between 8-17 bar, the steam-dimethyl ether molar ratio is between 2 and 4, and saturated high-pressure steam (used as a heating medium) is between 4.0-10 MPa (580-1450 PSIG). The gas hourly space velocity for designing the reactor mainly depends on the physical and chemical properties of the catalyst and various operating conditions (e.g., temperature, pressure, steam-dimethyl ether ratio).

[0038] Based on thermodynamic simulations, a maximum hydrogen conversion efficiency of about 97% is obtained when the steam to dimethyl ether ratio is 2, the temperature is 200° C., and the absolute pressure is 1 atm.

[0039] Dimethyl ether and steam can be converted to hydrogen using one of five different reactors. One type of reactor has an inner tube nested within an outer tube, with steam circulating between the inner and outer tubes to induce a heat-based reaction within the inner tube. Multiple combinations of these reactors may be used depending on the hydrogen production capacity. Another type of reactor has tubes nested within a casing with an electric heating element for heating the tubes and inducing a heat-based reaction within the tubes. Multiple combinations of these reactors may be used depending on the hydrogen production capacity. Yet another type of reactor has tubes nested within a shell (furnace), with heat from a burner circulating within the shell to induce a heat-based reaction within the tubes. Yet another type of reactor has tubes extending between tube plates within the shell, with heat circulating within the shell to induce a heat-based reaction within the tubes. Yet another type of reactor comprises a fluidized catalytic reaction bed nested within a reaction chamber with a heat source extending from the bottom of the reaction chamber to the top of a heating chamber to induce a heat-based reaction in the fluidized catalytic reaction bed. In some embodiments, features of one type of reactor may be combined with another type of reactor.

[0040] FIG. 1 shows an example of a steam-heated reactor 100 including an inner tube 120 nested within an outer tube 110 configured to receive steam. The steam-heated reactor 100 includes the outer tube 110, the inner tube 120 nested within the outer tube 110, a supply line 130 connected to one end of the inner tube 120, and a reactor outlet 140 connected to the other end of the inner tube 120. The hydrogen production capacity of the multiple steam-heated reactors 100 is, for example, 1,000 kg / day or more. The steam-heated reactor 100 can produce hydrogen by utilizing the reaction of dimethyl ether with water vapor (steam). This reaction can also be defined as the reforming of dimethyl ether to hydrogen.

[0041] The reactor includes an outer tube 110. The outer tube 110 is configured to contain heat. The outer tube 110 has a diameter. In some embodiments, the diameter of the outer tube 110 is 3 to 4 inches. The outer tube 110 is configured to contain steam or heated oil. The heat contained in the outer tube 110 has a uniform temperature along the length of the outer tube. In some embodiments, the outer tube 110 extends a length of 10 to 25 feet.

[0042] The steam-heated reactor 100 includes an inner tube 120 nested inside an outer tube 110. The inner tube 120 is configured to transfer heat contained in the outer tube 110. The inner tube 120 has a diameter smaller than the diameter of the outer tube 110. The inner tube 120 has a first end and a second end. The inner tube 120 has a reaction chamber 190 between the ends. The inner tube 120 contains the reaction chamber 190. In some embodiments, the diameter of the inner tube 120 is between 1 1 / 4 inches and 2 inches. The inner tube 120 contains a catalyst 127 within the reaction chamber 190 for the reaction of dimethyl ether with hydrogen. In some embodiments, the combination of the steam-heated reactor 100 with the inner tube nested within the outer tube extends in length from 10 feet to 25 feet to produce 1000 kg / day or more of hydrogen.

[0043] The outer tube 110 and the inner tube 120 may be the same length. In some embodiments, the length of the outer tube 110 is the same length as the inner tube 120. The outer tube 110 and the inner tube 120 form a steam-heated reactor 100 that converts dimethyl ether and steam into hydrogen. The inner tube 120 is filled with a catalyst 127. The space 115 between the outer tube 110 and the inner tube 120 allows steam to circulate and condense within the outer tube 110. In some embodiments, the steam circulating within the space 115 between the outer tube 110 and the inner tube 120 can be at a temperature of 245 to 310 degrees Celsius. The inner tube 120 conducts heat to heat the catalyst 127 and the reactants. As the steam condenses, the heat conducted by the inner tube 120 is transferred to the catalyst 127 and the reactants. The number and length of the outer tubes, including the inner tube with the reaction chamber, may be varied to meet capacity and engineering requirements.

[0044] In some embodiments, the outer tube 110 and the inner tube 120 are vertically oriented with a first end adjacent the top of the outer tube 110 and a second end adjacent the bottom of the outer tube 110. The outer tube 110 has a steam inlet 150 and a steam condensate outlet 152. The steam inlet 150 receives steam, and the steam condensate outlet 152 discharges condensate. The temperature inside the outer tube 110 can be uniform throughout the length of the inner tube 120. In some embodiments, the uniform temperature of the outer tube 110 is the condensation temperature of the steam. In some embodiments, the steam can condense at only one temperature to increase the likelihood that the steam temperature is uniform throughout the outer tube 110. Steam can be an advantageous heat source because the condensation rate can indicate the rate at which the inner tube 120 absorbs heat and the reaction rate.

[0045] The outer tube 110 with the inner tube 120 with catalyst 127 may be arranged with multiple steam-heated reactors having outer tubes with ring-shaped or box-shaped inner tubes. In some embodiments, the outer tubes of multiple steam-heated reactors are arranged inside a cylindrical, square, or rectangular box. The cylindrical, square, or rectangular box has a steam inlet for receiving heating steam and a steam outlet for discharging steam condensate. The cylindrical, square, or rectangular box may be a casing, shell, housing, and / or the like.

[0046] The steam-heated reactor 100 has a supply line 130 for supplying dimethyl ether and steam to the reaction chamber within the inner tube 120. The supply line 130 is connected to a first end of the inner tube 120. A single supply line 130 may be connected to a first end of each of the inner tubes 120 in a case where multiple steam-heated reactors are present. The first end of the inner tube 120 may be the upper end of the inner tube 120. The supply line 130 is configured to deliver dimethyl ether and steam to the inner tube 120.

[0047] The steam-heated reactor 100 has a reactor outlet 140 adjacent to the second end of the inner tube 120. The reactor outlet 140 collects hydrogen from the inner tube 120 and discharges the hydrogen. The second end of the inner tube 120 may be the lower end of the inner tube 120.

[0048] The reaction chamber in the inner tube 120 is configured to house a catalyst 127. The catalyst 127 is configured to receive the heat housed in the outer tube 110. The reaction chamber 190 can produce hydrogen based on a cooperative reaction between the catalyst 127 heated by the heat housed in the outer tube 110, dimethyl ether, and steam.

[0049] FIG. 2A illustrates an example of an electrically heated reactor 200 including tubes 220 nested within an outer casing 210 configured to contain heat generated by an electric heating element 270. The electrically heated reactor 200 includes the outer casing 210, the tubes 220 nested within the casing, a supply line 130 connected to one end of the tubes 220, and a reactor outlet 140 connected to the other end of the tubes 220. The hydrogen production capacity of multiple electrically heated reactors can be 1,000 kg / day or more. The electrically heated reactor 200 can produce hydrogen using the reaction of dimethyl ether and steam. This reaction can also be defined as the reforming of dimethyl ether to hydrogen.

[0050] The electrically heated reactor 200 includes an outer casing 210. The outer casing 210 is configured with an insulating layer 250 and an inner refractory layer 260. The inner refractory layer 260 is configured with a tube 220 and an electric heating element 270. Heat within the inner refractory layer 260 is generated by the electric heating element 270. The electric heating element 270 is embedded inside the inner refractory layer 260 in the space 115 between the tube 220 and the outer wall of the inner refractory layer 260. The electric heating element 270 may be an electric coil. The heat contained in the casing may have a uniform temperature along the length of the casing. In some embodiments, the outer casing 210 has a refractory surface along an inner portion of the outer casing 210. The outer casing 210 includes an insulating layer 250 between the inner refractory layer 260 and the inner portion of the outer casing 210. The insulating layer 250 can prevent heat leakage to the outside of the casing. In some embodiments, the outer casing 210 with the telescoping tubes 220 extends in length from 10 feet to 40 feet.

[0051] The electrically heated reactor 200 includes a tube 220 nested within an outer casing 210. The tube 220 is configured to conduct heat contained within the outer casing 210. The tube 220 has a smaller tube diameter than the outer casing 210. The tube 220 is configured to conduct heat contained within the outer casing 210. The tube has a first end and a second end. Between the ends, the tube 220 contains a reaction chamber 190. The tube 220 contains the reaction chamber 190. In some embodiments, the diameter of the tube is between 1 1 / 2 inches and 4 inches. The tube contains a catalyst 127 within the reaction chamber 190 for the reaction of dimethyl ether to hydrogen. In some embodiments, the electrically heated reactor combination with an inner tube nested within the outer casing extends in length from 10 feet to 25 feet to produce 1,000 kg / day or more of hydrogen.

[0052] In multiple electrically heated reactors, each tube has the same length. In some embodiments, the length of the outer casing is the same as the length of the tubes. The outer casing 210 and the tubes 220 form a reaction chamber 190 that converts dimethyl ether and steam into hydrogen. The tubes 220 are filled with a catalyst 127. In some embodiments, an electric heating element 270 heats the tubes to between 245 and 310 degrees Celsius. The tubes 220 conduct heat to heat the catalyst 127 and the reactants. The number and length of the outer casing with the inner tubes containing the reaction chamber may be varied to meet capacity and engineering needs.

[0053] In some embodiments, the tube 220 is vertically oriented with a first tube end adjacent the top of the outer casing 210 and a second tube end adjacent the bottom of the outer casing 210. The temperature within the casing can be uniform along the length of the tube. The uniform temperature of the casing is controlled by an electric heating element 270. The electric heating element 270 can be one or more electric coils.

[0054] The outer casings, each containing a plurality of tubes with catalyst 127, may be arranged in a ring or box shape. In some embodiments, the outer casings are arranged inside a cylindrical, square, or rectangular box. The cylindrical, square, or rectangular box may house a power cable with a switch for the electrical coil. The cylindrical, square, or rectangular box may be a casing, shell, housing, and / or the like.

[0055] The electrically heated reactor 200 includes a supply line 130 for supplying dimethyl ether and steam to the reaction chamber within the tube. The supply line 130 is connected to a first end of the tube. Additionally and / or alternatively, a single supply line 130 may be connected to each first end of the inner tube in which multiple electrically heated reactors reside. The first end of the tube may be the upper end of the tube 220. The supply line 130 may be configured to deliver dimethyl ether and steam to the tube 220.

[0056] The electrically heated reactor 200 includes a reactor outlet 140 adjacent the second end of the tube 220. The reactor outlet 140 collects and discharges hydrogen from the tube 220. The second end of the tube 220 may be the lower end of the tube 220.

[0057] 2B illustrates an example cross-section of an electrically heated reactor 200 within a tube 220 nested within an outer casing 210 configured to contain heat generated by a heating element 270. The electrically heated reactor 200 includes an outer casing 210 and a tube 220 nested within the outer casing 210. An insulating layer 250 is disposed between the inside of the outer casing 210 and the tube 220 nested within the outer casing 210. An inner refractory layer 260 includes an electric heating element 270 and is disposed between the insulating layer 250 and the tube 220. The tube 220 includes a catalyst 127.

[0058] FIG. 3 illustrates an example of a burner-heated reactor 300 including multiple nested tubes 320 nested within a shell 310 configured to contain heat generated by the combustion of fuel. The burner-heated reactor 300 includes the shell 310, the multiple nested tubes 320 within the shell 310, a fuel burner 340, a supply line 130 connected to one end of each of the tubes, and a reactor outlet 140 connected to the other end of each of the tubes. The shell 310 may be a firebox or a cylindrical shell. The hydrogen production capacity of the burner-heated reactor 300 is, for example, 1,000 kg / day or more. The burner-heated reactor 300 can produce hydrogen by reacting dimethyl ether with water vapor (steam). This reaction can also be defined as the reforming of dimethyl ether to hydrogen.

[0059] Burner-heated reactor 300 includes a shell 310. Shell 310 is configured to contain heat. A plurality of nested tubes 320 containing catalyst 127 are inside shell 310. Shell 310 contains a hot flue gas heating medium from a fuel burner 340. Shell 310 may be a fire box, cylindrical shell, square box, or rectangular box containing hot flue gas from the combustion of fuel. Shell 310 has a fuel gas inlet 350 and a fuel gas outlet 352 that receive fuel and air, respectively, for the fuel burner. The box or cylinder may also be a casing, shell, housing, and / or the like. Shell 310 is configured to contain the heat generated by burning fuel.

[0060] The interior of shell 310 has a refractory surface 325. Shell 310 is constructed of refractory material to retain heat at high temperatures. A fuel burner 340 is configured to generate heat contained within shell 310. Fuel burner 340 is located on the top of shell 310 and oriented downward for vertical combustion. Additionally and / or alternatively, in some embodiments, fuel burner 340 is located on a vertical wall of shell 310 for horizontal combustion. The fuel burners can be controlled independently of the other fuel burners. In some embodiments, fuel burners 340 are configured to be turned on simultaneously to maintain a uniform temperature within shell 310. This heat is generated by the combustion of fuel by the ambient air within fuel burner 340 and heat dissipation from refractory surface 325. Fuel gas and ambient air enter fuel burner 340 through fuel gas inlet 350. Hot fuel gas produced by the combustion of fuel can exit shell 310 through fuel gas outlet 360. Hot fuel gas circulates within the space 115 between the tubes within the shell 310 and the interior wall of the shell 310. Radiant heat contained in the refractory surface 325 of the shell 310 and heat contained in the hot fuel gas can maintain a uniform temperature along the length of the multiple nested tubes 320. In some embodiments, the shell 310 includes an insulating layer on an exterior portion of the shell 310. The insulating layer can prevent heat leakage outside the shell 310. In some embodiments, the shell 310 extends vertically to a height of 10 to 40 feet to accommodate the multiple nested tubes 320.

[0061] Burner-heated reactor 300 includes a plurality of nested tubes 320 inside a shell 310. The plurality of nested tubes 320 are configured to conduct heat contained within shell 310. The plurality of nested tubes 320 have a first end and a second end. Between the ends, the plurality of nested tubes 320 house a reaction chamber 190. In some embodiments, the diameter of the plurality of nested tubes 320 is between 1.5 inches and 4 inches. The plurality of nested tubes 320 contains a catalyst 127 within reaction chamber 190 for the reaction of dimethyl ether with hydrogen. The plurality of nested tubes 320 extend in length from 10 feet to 40 feet to produce 1,000 kg / day or more of hydrogen.

[0062] The multiple nested tubes 320 may be the same length. In some embodiments, the length of the shell 310 is the same length as the multiple nested tubes 320. The shell 310 and the multiple nested tubes 320 form a reaction chamber for converting dimethyl ether and steam into hydrogen. The multiple nested tubes 320 may be filled with a catalyst 127. The space 115 between the shell 310 and the multiple nested tubes 320 allows heat from the hot fuel gas and radiant heat from the refractory surface 325 to heat the multiple nested tubes 320, the catalyst 127, and the reactants. The fuel gas can exit the shell 310 through a fuel gas outlet 352. In some embodiments, the heat circulating within the space 115 between the shell 310 and the multiple nested tubes 320 is greater than 300 degrees Celsius. The multiple nested tubes 320 conduct heat to heat the catalyst 127 and the reactants. In some embodiments, a fuel burner 340 is positioned near the refractory surface 325 of the shell 310. The number and length of the multiple nested tubes 320 containing the reaction chambers may be varied to meet capacity and engineering needs.

[0063] In some embodiments, the plurality of nested tubes 320 are vertically oriented with a first tube end adjacent the top of the shell 310 and a second tube end adjacent the bottom of the shell 310. The temperature within the shell 310 can be uniform across the length of the plurality of nested tubes 320. In some embodiments, the uniform temperature of the shell 310 can be due to the hot fuel gas and radiant heat from the refractory surface 325.

[0064] The burner-heated reactor 300 includes a set of supply lines for supplying dimethyl ether and steam to the reaction chambers within the tubes. The set of supply lines are connected to first ends of the plurality of nested tubes 320. Additionally and / or alternatively, a single supply line 130 may be connected to each of the first ends of the plurality of nested tubes 320. The first ends of the plurality of nested tubes 320 may be upper ends of the plurality of nested tubes 320. The supply lines may be configured to deliver dimethyl ether and steam to the plurality of nested tubes 320.

[0065] The burner-heated reactor 300 has a reactor outlet 140 adjacent to the second ends of the plurality of nested tubes 320. The reactor outlet 140 collects and discharges hydrogen from the plurality of nested tubes 320. The second ends of the plurality of nested tubes 320 may be the lower ends of the plurality of nested tubes 320.

[0066] The reaction chamber 190 within the plurality of nested tubes 320 is configured to house a catalyst 127. The catalyst 127 is configured to receive heat housed in the shell 310. The reaction chamber can produce hydrogen based on a cooperative reaction between the catalyst 127 heated by the heat housed in the shell 310, dimethyl ether, and steam.

[0067] FIG. 4 illustrates an example of a dual-plate reactor 400 including multiple tubes extending between an upper tube plate 410 and a lower tube plate 415. The dual-plate reactor 400 includes a cylindrical shell 405, an upper tube plate 410, a lower tube plate 415, an upper dish end 420, a lower dish end 425, multiple nested tubes 320 extending between the upper tube plate 410 and the lower tube plate 415, a feed line 130 adjacent to the upper dish end 420 of the cylindrical shell 405, and a reactor outlet 140 adjacent to the lower dish end 425 of the cylindrical shell 405. The dual-plate reactor 400 can produce hydrogen at a rate of, for example, 1,000 kg / day or more. The dual-plate reactor 400 can produce hydrogen by reacting dimethyl ether with steam. This reaction can also be defined as the reforming of dimethyl ether to hydrogen. The dual plate reactor 400, comprising a plurality of nested tubes 320 extending between an upper tube plate 410 and a lower tube plate 415, may be in either a horizontal or vertical configuration.

[0068] The dual-plate reactor 400 includes a cylindrical shell 405. The cylindrical shell 405 includes a plurality of tubes containing a catalyst 127. The cylindrical shell 405 contains a common heating medium, such as steam or hot oil, surrounding the tubes. In some embodiments, the dual-plate reactor 400 does not include an individual heated steam jacket or hot oil jacket. The cylindrical shell 405 includes a first inlet 450 for receiving steam or hot oil and a first outlet 452 for discharging condensate or hot oil. The cylindrical shell 405 includes a feed line 130, a reactor outlet 140 for delivering the dimethyl ether mixture, and a hydrogen product outlet. The cylindrical shell 405 may be a casing, shell, housing, or the like. The cylindrical shell 405 may be configured to contain heat.

[0069] The cylindrical shell 405 is configured with an upper tube plate 410 connected to an upper dish end 420 of the cylindrical shell 405 and a lower tube plate 415 connected to a lower dish end 425 of the cylindrical shell 405. The upper tube plate 410 has an opening therein. The lower tube plate 415 has an opening therein. The cylindrical shell 405 is configured to contain steam or heated oil. Heat circulates within the space 115 between the tubes within the cylindrical shell 405 and the interior wall within the cylindrical shell 405. The heat contained within the cylindrical shell 405 can have a uniform temperature along the length of the cylindrical shell 405. In some embodiments, the cylindrical shell 405 extends a length of 10 to 25 feet.

[0070] The double-plate reactor 400 includes a plurality of nested tubes 320 within a cylindrical shell 405. The nested tubes 320 are configured to conduct heat within the cylindrical shell 405. The nested tubes 320 have a first end and a second end. The first end of the nested tubes 320 is configured to be inserted into an opening in the upper tube plate 410. The second end of the nested tubes 320 is configured to be inserted into an opening in the lower tube plate 415. Between the ends, the nested tubes 320 include a reaction chamber 190. The tubes house the reaction chamber 190. In some embodiments, the diameter of the tubes is between 1 1 / 4 inches and 2 inches. The nested tubes 320 contain a catalyst 127 within the reaction chamber 190 for reacting dimethyl ether with hydrogen. The nested tubes 320 extend in a length of 10 to 25 feet to produce 1,000 kg or more of hydrogen per day.

[0071] The multiple nested tubes 320 may have the same length. In some embodiments, the length of the cylindrical shell 405 is the same length as the multiple nested tubes 320. The cylindrical shell 405 and the multiple nested tubes 320 form a dual-plate reactor 400 for converting dimethyl ether and steam into hydrogen. The multiple nested tubes 320 are filled with a catalyst 127. The space 115 between the cylindrical shell 405 and the multiple nested tubes 320 allows steam to circulate and condense within the cylindrical shell 405. In some embodiments, the heat circulating within the space 115 between the cylindrical shell 405 and the tubes can be between 245 and 310 degrees Celsius. The multiple nested tubes 320 conduct heat to heat the catalyst 127. The steam condenses, and the heat conducted by the tubes is transferred to the catalyst 127 and the reactants. The number and length of the multiple nested tubes 320 may be varied to meet capacity and engineering requirements.

[0072] In some embodiments, the plurality of nested tubes 320 are vertically oriented with a first tube end adjacent the top of the cylindrical shell 405 and a second tube end adjacent the bottom of the cylindrical shell 405. The temperature within the cylindrical shell 405 can be made uniform throughout the length of the tube by circulating heated oil or steam. In some embodiments, the uniform temperature of the cylindrical shell 405 is the condensation temperature of the steam. In some embodiments, the steam can condense at only one temperature to increase the likelihood of a uniform steam temperature throughout the cylindrical shell 405. Steam can be an advantageous heat source because the condensation rate can indicate the heat absorption rate of the tube.

[0073] The double-plate reactor 400 includes a feed line 130 that supplies dimethyl ether and steam to an upper dish end 420 of the cylindrical shell 405 and distributes the dimethyl ether and steam to reaction chambers within the plurality of nested tubes 320. The feed line 130 is connected to the upper dish end 420 of the cylindrical shell 405. A first end of the plurality of nested tubes 320 may be an upper end of the plurality of nested tubes 320. The feed line 130 is configured to pass the dimethyl ether and steam through the plurality of nested tubes 320.

[0074] The double-plate reactor 400 has a reactor outlet 140 adjacent to a second end of the plurality of nested tubes 320. The reactor outlet 140 collects hydrogen from the plurality of nested tubes 320 and discharges the hydrogen.

[0075] The reaction chamber 190 within the plurality of nested tubes 320 is configured to house a catalyst 127. The catalyst 127 is configured to receive heat housed in the cylindrical shell 405. The reaction chamber 190 can produce hydrogen based on a cooperative reaction between the catalyst 127 heated by the heat housed in the cylindrical shell 405, dimethyl ether, and steam.

[0076] In some embodiments, the dual-plate reactor 400 is oriented horizontally, with the upper and lower dish ends 420 and 425 corresponding to the left and right dish ends, the upper tube plate 410 corresponding to the left tube plate, the lower tube plate 415 corresponding to the right tube plate, multiple nested tubes 320 extending between the left and right tube plates, the supply line 130 adjacent to the left dish portion of the cylindrical shell 405, and the reactor outlet 140 adjacent to the right dish portion of the cylindrical shell 405.

[0077] FIG. 5 illustrates a fluidized catalytic reactor 500 including a fluidized catalytic reactor bed 520 nested within a heating chamber 590 configured to accommodate a heat source 550 extending from the bottom of the heating chamber 590 to the top of the heating chamber 590. The fluidized catalytic reactor 500 includes a shell 310, a heat source within the shell 310, a feed line 130 adjacent to the bottom of the shell 310, and a reactor outlet 140 adjacent to the top of the shell 310. The hydrogen production capacity of the fluidized catalytic reactor 500 is, for example, 1,000 kg / day or more. The fluidized catalytic reactor 500 can produce hydrogen by reacting dimethyl ether with steam. This reaction can also be defined as the reforming of dimethyl ether to hydrogen.

[0078] The fluidized catalytic reactor 500 includes a shell 310. The shell 310 is configured to accommodate heat. The shell 310 is configured to have a heating chamber 590. The heating chamber 590 is configured to accommodate a fluidized catalytic reaction bed 520. The fluidized catalytic reaction bed 520 extends from the top of the shell 310 to the bottom of the shell 310. The fluidized catalytic reaction bed 520 also extends from one side of the shell 310 to the opposite side of the shell 310. The fluidized catalytic reaction bed 520 is configured to receive the heat accommodated in the shell 310. The reaction chamber can produce hydrogen based on the cooperative reaction of dimethyl ether and steam with a fluidized catalyst 127 heated by the heat accommodated in the shell 310. The fluidized catalyst 127 may include a fluidized acid catalyst and a fluidized reforming catalyst. Methanol is produced by hydrolyzing dimethyl ether over the fluidized acid catalyst, and methanol is produced by steam reforming over the fluidized reforming catalyst. In some embodiments, one-third of the fluid catalyst is a fluid acid catalyst and two-thirds of the fluid catalyst is a fluid reforming catalyst (copper zinc) mixture. The fluid acid catalyst may be a hydrolysis catalyst. The fluid acid catalyst is capable of converting a sufficient amount of dimethyl ether to methanol. The fluid hydrolysis catalyst is capable of hydrolyzing dimethyl ether to methanol.

[0079] The fluidized catalytic reactor 500 includes a heat source 550 extending from the top of the heating chamber 590 to the bottom of the heating chamber 590. The heat source 550 may be a heating coil configured to heat the fluidized catalytic reactor bed 520. The heat source 550 may be steam or heated oil in a tube or coil. Additionally and / or alternatively, the heat source 550 may be an electrically powered heating element configured to generate heat. The heat source 550 may extend from the top of the heating chamber 590 to the bottom of the heating chamber 590 by extending in alternating opposite directions, vertically or horizontally, in a zigzag or coil pattern. In some embodiments, the heat source 550 extends across the shell 310 in a first horizontal direction until it reaches a first side of the shell 310, extends vertically, and then extends across the shell 310 in a second horizontal direction opposite the first horizontal direction until it reaches a second side of the shell 310. In some embodiments, the power source extends across the shell 310 in a first vertical direction until it reaches the top or bottom of the shell 310, extends vertically, and then extends across the shell 310 in a second vertical direction opposite the first vertical direction until it reaches the opposite end of the shell 310. The heat contained in the heating chamber 590 within the shell 310 and the fluidized catalytic reaction bed 520 can result in a uniform temperature throughout the fluidized catalytic reaction bed 520. In some embodiments, the shell 310 extends in a length between 10 feet and 25 feet.

[0080] Fluidized catalytic reactor 500 includes a fluidized catalytic reactor bed 520 nested within shell 310. Fluidized catalytic reactor bed 520 is configured to transfer heat contained in heat source 550. Fluidized catalytic reactor bed 520 is a reaction chamber for reacting dimethyl ether into hydrogen.

[0081] The shell 310, heat source 550, and fluidized catalytic reactor bed 520 form a fluidized catalytic reactor 500 that converts dimethyl ether and steam into hydrogen. A space 115 between the heating coils / tubes of the heat source 550 and the fluidized catalytic reactor bed 520 allows heat to circulate and condense in the shell 310. In some embodiments, the heat source 550 can be between 245 and 310°C. Heat from the tubes / coils of the heat source 550 can be transferred to the fluidized catalyst 127 and the reactants. The temperature within the shell 310 and the fluidized catalytic reactor bed 520 is uniform.

[0082] Fluidized catalytic reactor 500 includes a feed line 130 for supplying dimethyl ether and steam to heating chamber 590. Feed line 130 is adjacent to the bottom of shell 310. Feed line 130 is configured to pass dimethyl ether and steam through shell 310. Feed line 130 includes a diffuser 530 having a series of openings configured to evenly distribute the dimethyl ether and steam within heating chamber 590.

[0083] The fluidized catalytic reactor 500 has a reactor outlet 140 adjacent the top of the shell 310. The reactor outlet 140 collects hydrogen from the reaction chamber and discharges the hydrogen. In some embodiments, a filter is disposed between the reaction chamber and the reactor outlet 140.

[0084] Referring to FIG. 6A, a table showing exemplary specifications for dimethyl ether fed into a feed line to a reactor that converts dimethyl ether to hydrogen is shown.

[0085] Referring to FIG. 6B, a table showing exemplary specifications for steam supplied to the feed line to the reactor that converts dimethyl ether to hydrogen is shown.

[0086] Referring to FIG. 6C, an example table showing an exemplary expected product composition from the reactor is shown.

[0087] Referring to FIG. 6D, an example table is shown showing exemplary specifications for purified hydrogen exiting the pressure swing adsorption system after the reactor converts dimethyl ether to hydrogen.

[0088] Referring to Figure 7, an example block diagram illustrating a process flow for converting dimethyl ether and steam into hydrogen is shown. The process includes receiving dimethyl ether from a storage tank 720, utilizing a heat exchanger 730 to increase the temperature of the dimethyl ether, mixing steam from a steam boiler 710 with the dimethyl ether, and entering the heated dimethyl ether and steam mixture into a reactor 790. The steam from the steam boiler 710 may be mixed with the dimethyl ether and also entered into the reactor 790 to heat the catalyst 127. The hydrogen produced by the reactor 790 passes through a heat exchanger 730 to cool the hydrogen while simultaneously heating the dimethyl ether, and then passes through a hydrogen purification system 750 comprising a pressure swing adsorption system 752. The hydrogen purification system 750 may include a reactor product cooling system, a water wash column, and a carbon dioxide removal system.

[0089] The dimethyl ether is delivered to the site and stored in a storage tank 720, such as a pressurized vessel. The dimethyl ether is pumped from the storage tank 720 and heated by a heat exchanger. The heat exchanger is configured to perform a heat exchange process that utilizes heat from the recycled steam to heat the dimethyl ether. In some embodiments, the dimethyl ether is heated using heat recovered from the reactor 790.

[0090] Steam for heating reactor 790 may be generated by high-pressure boiler 710. In some embodiments, high-pressure boiler 710 is fueled by exhaust gas from pressure swing adsorption system 752 and supplemented with dimethyl ether from storage tank 720 to boil water into steam. The exhaust gas that fuels high-pressure boiler 710 may be supplied from an exhaust gas drum. For example, the exhaust gas used as fuel for high-pressure boiler 710 may be unconverted reactants and carbon monoxide produced by reactor 790, which is then separated from the high-pressure hydrogen product by pressure swing adsorption system 752. In some embodiments, the exhaust gas from pressure swing adsorption system 752 contains some unrecovered hydrogen and is supplemented with a small amount of dimethyl ether for use as fuel for high-pressure boiler 710. The exhaust gas may be a purge gas for pressure swing adsorption system 752.

[0091] Steam from the high-pressure boiler 710 can be mixed with dimethyl ether to produce a mixture of steam and dimethyl ether. The mixture of steam and dimethyl ether is further heated by heat exchanger 730 until it reaches a reaction temperature threshold of reactor 790. The reaction temperature threshold corresponds to the temperature required for the combination of dimethyl ether and steam to react with catalyst 127 in reactor 790. The mixed dimethyl ether and steam enter reactor 790 from the top of reactor 790. Additionally, steam from boiler 710 may be split to provide heat to reactor 790 and to provide steam for mixing with dimethyl ether entering reactor 790. For example, steam from boiler 710 may be configured to heat the outer tube or shell of reactor 790. The steam from boiler 710 may meet the reaction temperature threshold to induce a reaction between the catalyst 127 and the mixture of steam and dimethyl ether in the reaction chamber. In some embodiments, the reaction of dimethyl ether, steam, and catalyst 127 in reactor 790 is carried out at a reaction temperature that meets a reaction temperature threshold and a reaction pressure that meets a reaction pressure threshold. The steam from high-pressure boiler 710 may be adjusted in flow rate, pressure, and temperature to meet reaction requirements, balance the temperature of the steam, and adjust the formation of condensation in reactor 790.

[0092] In some embodiments, the reactor product passes through a hydrogen purification system 750. The hydrogen purification system 750 may include cooling the reactor product in a water-cooled exchanger. The hydrogen purification system 750 may include removing condensate and methanol from the cooled reactor product using a high-temperature condensate drum. The removed condensate (water and methanol) is pumped by a condensate pump and sent to the reactor 790 via a condensate vaporizer. Unconverted methanol is recycled to the inlet of the reactor 790 for further conversion. Once the high-temperature condensate drum has removed most of the water and methanol, the hydrogen-rich gas flows to a water wash column and a carbon dioxide removal process before being sent to a pressure swing adsorption system 752 to purify the hydrogen.

[0093] Pressure swing adsorption system 752 includes multiple pressure adsorption vessels, product filters, and automatic switching valves managed by a cycle controller. Pressure swing adsorption system 752 is configured to remove impurities from the reactor product (e.g., crude hydrogen 905). The impurities include carbon monoxide, carbon dioxide, steam condensate, and trace amounts of unconverted methanol and dimethyl ether. The purified hydrogen from pressure swing adsorption system 752 is further compressed and stored in compressed hydrogen storage tanks or hydrogen cylinders. The purified hydrogen product from pressure swing adsorption system 752 may be further compressed by a product hydrogen compressor. The compressed hydrogen is stored or transported for consumption. The tail gas from pressure swing adsorption system 752 (containing the impurities in the raw reactor product) is sent to a tail gas drum and then to boiler 710 for use as fuel gas. In some embodiments, the pure water and steam condensate are sent to a degasser to remove oxygen. Oxygen removers and pH-adjusting chemicals may be added to the treated water. The treated water is pumped out by a boiler feed pump and sent to the boiler 710. The boiler 710 is equipped with a boiler feed pump.

[0094] 8, an example block diagram illustrating a process flow for converting dimethyl ether to hydrogen is shown. The process includes receiving dimethyl ether, increasing the temperature of the dimethyl ether using a heat exchanger, mixing steam from a steam boiler 710 with the dimethyl ether, and entering the heated dimethyl ether and steam mixture into a reactor 790.

[0095] The dimethyl ether enters first heat exchanger 810 and is vaporized. First heat exchanger 810 is configured to use vapor condensate from reactor 790 to heat and vaporize the dimethyl ether. In some embodiments, the dimethyl ether entering first heat exchanger 810 is heated by the reactor product exiting reactor 790.

[0096] In the second heat exchanger 820, the dimethyl ether is further heated to meet a temperature threshold related to the temperature requirement for mixing the dimethyl ether with steam. Once the dimethyl ether meets the threshold temperature related to the temperature requirement for mixing the dimethyl ether with steam, the dimethyl ether enters the mixer 830. The mixer 830 is configured to mix the dimethyl ether and steam. The steam entering the mixer 830 is received from the steam boiler 710. Following the mixing process of the dimethyl ether and steam, the mixed dimethyl ether and steam enters the third heat exchanger 840.

[0097] In the third exchanger 840, the dimethyl ether is further heated to meet a reaction temperature threshold. The reaction temperature threshold corresponds to the temperature required for the combination of dimethyl ether and steam to react with the catalyst 127 in the reaction chamber. In some embodiments, the third heat exchanger 840 is heated by steam supplied directly from the boiler 710. The temperature of the steam from the boiler 710 meets the reaction temperature threshold for the combination of dimethyl ether and steam to reach the reaction temperature threshold. Once the mixture of dimethyl ether and steam meets the reaction temperature threshold, the dimethyl ether and steam enter the reactor 790.

[0098] The steam used to heat the reactor 790 at a uniform temperature forms a steam condensate. The condensate rapidly flows into a high-pressure condensate drum to generate low-pressure steam, which is then fed to the reactor along with dimethyl ether. Additional steam may be required to meet the steam-to-dimethyl ether ratio of the reactor feed, which can be supplemented with steam from the boiler 710. The reactor product from the reactor 790 is used to heat the condensate from the high-temperature condensate drum in the fourth heat exchanger 860, the first heat exchanger 810, and the second heat exchanger 820. The first heat exchanger 810, the second heat exchanger 820, and the third heat exchanger 850 may be heated using steam condensate from the reactor system. The steam previously used to heat the reaction chamber condenses.

[0099] Steam from the boiler 710 is used to heat a reaction chamber to produce hydrogen. More specifically, the steam from the boiler 710 is used to induce a reaction between the catalyst 127 in the reaction chamber and a combination of dimethyl ether and steam to produce hydrogen. Condensate from the heating of the reaction chamber exits the reaction chamber and enters a high-pressure condensate drum. Steam condensate from the high-pressure condensate drum is configured to enter a degasser. In some embodiments, the condensate in the degasser is configured to return to the boiler 710.

[0100] 9, an example block diagram illustrating a hydrogen purification process is shown. The purification process includes cooling the reactor product (e.g., crude hydrogen 905), removing water from the hydrogen, scrubbing the reactor product with a cold water wash, removing carbon dioxide from the reactor 790, and purifying the hydrogen in a pressure swing adsorption system 752.

[0101] The crude hydrogen 905 from reactor 790 enters a cooler 910. Cooler 910 is configured to aid in converting steam within the crude hydrogen 905 into water. The crude hydrogen 905 enters a condenser drum 930 with water condensed from the crude hydrogen 905. The gaseous output of condenser drum 930 enters a water wash column, then passes through a carbon dioxide removal system, and on to pressure swing adsorption system 752.

[0102] Pressure swing adsorption system 752 is configured to remove carbon dioxide and carbon monoxide from crude hydrogen 905. Pressure swing adsorption system 752 includes adsorbent beds 954 for collecting and removing methane, carbon dioxide, carbon monoxide, and trace amounts of unconverted methanol and dimethyl ether. Pressure swing adsorption system 752 is configured to receive crude hydrogen 905 and remove condensate, carbon monoxide, methane, and carbon dioxide from crude hydrogen 905 using adsorbent beds 954 through a pressurization and depressurization process. The pressurization and depressurization process is controlled by a cycle controller 958 communicatively connected to each pressure swing adsorption unit in pressure swing adsorption system 752. Pressure swing adsorption system 752 outputs purified hydrogen. In some embodiments, the adsorbent is selected based on the type of impurities present in the feed stream. For example, silica gel or alumina may be added to remove water, activated carbon may be added to remove carbon dioxide, or zeolites may be added to remove methane, carbon monoxide, and nitrogen. Adsorption of impurities occurs at relatively high pressures (typically 20-50 bar). Additionally, adsorption of impurities occurs at relatively high temperatures, such as approximately 50-60°C (120-140°F). The operating pressure is 200 PSIG, and the target PSA hydrogen recovery is 80-85%. The tail gas from pressure swing adsorption system 752 (including the impurities in the reactor product) is sent to tail gas drum 940 and then to boiler 710 for use as fuel gas. The purified hydrogen passes through final filter 960 before being further compressed and stored or shipped for consumption.

[0103] FIG. 10 shows an example block diagram including a controller 1010 configured to send instructions to reactor hardware 1030 based on reactor sensors 1020. The reactor includes temperature sensors located at the steam inlet and / or steam outlet. The temperature of the steam used to heat the reaction is monitored before entering the reactor. The temperature sensors are used to determine whether heat transfer to the reaction chamber is sufficient for an efficient reaction without excessive by-products. The reactor includes a pressure sensor in the reaction chamber configured to measure the pressure within the reaction chamber. The pressure sensor is located in the supply line 130 and configured to determine the flow rate of dimethyl ether. The reactor may include a steam dimethyl ether sensor to determine the ratio of steam to dimethyl ether. The reactor may also include sensors to detect carbon dioxide and / or carbon monoxide.

[0104] In some embodiments, reactor hardware 1030 includes a supply line valve configured to control the flow of dimethyl ether and steam into the reactor or inner tube. Reactor sensor 1020 includes a thermal sensor configured to determine the temperature of the heat contained in the outer tube. Controller 1010 is communicatively connected to the supply line valve and the thermal sensor. Controller 1010 may be configured to determine the temperature of the heat contained in the outer tube based on the thermal sensor. Controller 1010 may be configured to adjust the supply flow rate at the supply line valve depending on whether the temperature of the heat meets a temperature threshold.

[0105] In some embodiments, reactor hardware 1030 includes a steam dimethyl ether ratio sensor configured to output a steam dimethyl ether ratio measurement indicative of the ratio of steam to methyl ether in the reaction chamber. Controller 1010 is communicatively coupled to the steam dimethyl ether ratio sensor. Controller 1010 is configured to determine the steam dimethyl ether ratio measurement based on the steam dimethyl ether ratio sensor. Controller 1010 may be configured to compare the steam dimethyl ether ratio measurement to the steam carbon ratio. Controller 1010 may be configured to adjust the feed flow rate at a valve in feed line 130 in response to the comparison.

[0106] In some embodiments, reactor sensor 1020 includes a pressure sensor configured to output a pressure measurement representative of the discharge pressure in the outlet line. The outlet line includes a backpressure valve configured to control the outlet pressure of the outlet line. Controller 1010 is communicatively connected to the pressure sensor and the backpressure valve. Controller 1010 is configured to determine the pressure measurement in the outlet line based on the pressure sensor. Controller 1010 is configured to adjust the outlet pressure with the backpressure valve in the outlet line in response to the pressure measurement meeting the outlet pressure threshold. The pressure in the reactor and the pressure swing adsorption system must be maintained at a constant pressure value. The backpressure valve is located at the rear end of the pressure swing adsorption unit, where the hydrogen product pressure is maintained. The vapor pressure within the reactor itself is fixed by the hydrogen product backpressure. The vapor pressure is controlled by condensing drum 930. The vapor pressure is adjusted as needed to maintain the vapor pressure and temperature for heating the reactants in reactor 790.

[0107] In some embodiments, the reactor sensor 1020 comprises at least one carbon monoxide sensor or carbon dioxide sensor configured to output at least one carbon monoxide measurement or carbon dioxide measurement representative of at least one of the carbon monoxide or carbon dioxide in the reaction chamber. The controller 1010 is communicatively coupled to the at least one carbon monoxide sensor or carbon dioxide sensor. The controller 1010 is configured to determine the at least one of the carbon monoxide or carbon dioxide in the reaction chamber based on the at least one carbon monoxide sensor or carbon dioxide sensor. The controller 1010 is configured to adjust the feed flow rate at the valve in the feed line 130 in response to the at least one of the carbon monoxide measurement or the carbon dioxide measurement meeting at least one of the carbon monoxide threshold or the carbon dioxide threshold.

[0108] In some embodiments, the reactor sensor 1020 comprises a hydrogen sensor configured to output a hydrogen measurement representative of hydrogen at the reactor outlet 140 adjacent one end of the inner tube. The hydrogen sensor measurement is indicative of a cooperative reaction of the catalyst 127 in the reaction chamber with dimethyl ether and steam. The controller 1010 is communicatively coupled to the hydrogen sensor. The controller 1010 is configured to determine the hydrogen measurement at the reactor outlet adjacent one end of the inner tube based on the hydrogen sensor. The controller 1010 is configured to adjust the feed flow rate at a valve in the feed line in response to the hydrogen measurement meeting a hydrogen threshold value.

[0109] Referring to FIG. 11 , a computing system 1100 includes a processor 1110, a memory 1120, a storage medium 1130, and an input / output device 1140. The processor 1110, the memory 1120, the storage medium 1130, and the input / output device 1140 are interconnected via a system bus 1150. The processor 1110 can process instructions for execution within the computing system 1100. The instructions thus executed may, for example, execute one or more components of reactor hardware for converting dimethyl ether to hydrogen. In some exemplary embodiments, the processor 1110 is a single-threaded processor. Alternatively, the processor 1110 may be a multi-threaded processor. The processor 1110 can process instructions stored in the memory 1120 and / or the storage medium 1130 to display graphical information for a user interface provided via the input / output device 1140.

[0110] Memory 1120 is a non-transitory computer-readable medium that stores information within computing system 1100. Memory 1120 is configured to store, for example, data structures representing a configuration object database. Storage medium 1130 can provide persistent storage for computing system 1100. Storage medium 1130 may be a floppy disk drive, hard disk drive, optical disk drive, tape drive, or other suitable persistent storage device. Input / output devices 1140 provide input / output operations to computing system 1100. In some exemplary embodiments, input / output devices 1140 include a keyboard and / or a pointing device. In various embodiments, input / output devices 1140 include a display unit for displaying a graphical user interface.

[0111] According to some exemplary embodiments, input / output device 1140 provides input / output operations for network devices. For example, input / output device 1140 may include an Ethernet port or other network port for communicating with one or more wired and / or wireless networks (e.g., a local area network (LAN), a wide area network (WAN), the Internet, a public land mobile network (PLMN), etc.).

[0112] In some exemplary embodiments, computing system 1100 is used to execute various interactive computer software applications used to organize, analyze, and / or store data in various formats. Computing system 1100 may also be used to execute any type of software application. These applications may be used to perform various functions, such as planning functions (e.g., creating, managing, and editing spreadsheet documents, word processing documents, and other objects), computing functions, and communication functions. Applications may have various add-in features. Applications may also be standalone computing items or functions. When activated within an application, the features are used to generate a user interface that is presented via input / output devices 1140. The user interface is generated by computing system 1100 and presented to a user (e.g., on a computer screen monitor).

[0113] The terms used herein are for the purpose of describing particular embodiments only and are not intended to limit the embodiments. As used herein, the singular forms "a," "an," and "the" include the plural forms unless the context clearly dictates otherwise. Furthermore, as used herein, the terms "comprises" and / or "comprising" specify the presence of stated features, integers, steps, operations, elements, and / or components, but are understood not to exclude the presence or addition of one or more other features, integers, steps, operations, elements, components, and / or groups thereof. As used herein, the term "and / or" includes any and all combinations of one or more of the associated listed items.

[0114] Unless otherwise specified or clear from the context, the term "about" as used herein is understood to mean within a normal range of tolerance in the art, for example, within two standard deviations of the mean. "About" is understood to mean within 10%, 9%, 8%, 7%, 6%, 5%, 4%, 3%, 2%, 1%, 0.5%, 0.1%, 0.05%, or 0.01% of the stated value. Unless otherwise specified from the context, all numerical values ​​provided herein are modified by the term "about."

[0115] The many features and advantages of the present disclosure are apparent from the detailed specification, and the appended claims are intended to cover all such features and advantages of the present disclosure that fall within the true spirit and scope of the present disclosure. Further, because numerous modifications and changes will readily occur to those skilled in the art, it is not desired to limit the disclosure to the exact construction and operation shown and described, but rather to employ all suitable modifications and equivalents within the scope of the present disclosure.

[0116] In the above description and in the claims, phrases such as "at least one" or "one or more" may be used following a conjunctive list of elements or features. The term "and / or" also appears in lists of two or more elements or functions. Unless implicitly or explicitly contradicted by the context, such phrases are intended to refer to any of the listed elements or functions individually, or any of the listed elements or functions in combination with any of the other listed elements or functions. For example, the phrases "at least one of A and B," "one or more of A and B," and "A and / or B" mean "A only, B only, or both A and B," respectively. A similar interpretation applies to lists containing more than two items. For example, the phrases "at least one of A, B, and C," "one or more of A, B, and C," and "A, B, and / or C" mean "A only, B only, C only, both A and B, both A and C, both B and C, or both A, B, and C," respectively. Use of the term "based on" above and in the claims is intended to mean "based at least in part on," allowing for unrecited features or elements.

[0117] The examples set forth in the foregoing description do not represent all examples consistent with the subject matter described herein. Rather, they are merely examples consistent with aspects related to the described subject matter. While several variations have been described in detail herein, other modifications and additions are possible. In particular, additional features and / or variations may be provided in addition to those described herein. For example, the above-described examples are directed to various combinations and subcombinations of the disclosed features, and / or combinations and subcombinations of one or more features in addition to those disclosed herein. Furthermore, the logic flow depicted in the accompanying figures or described herein does not necessarily require the particular order shown, or sequential order, to achieve desirable results. Other examples or embodiments are within the scope of the following claims.

[0118] The Abstract of the Disclosure is provided to allow the reader to quickly ascertain the nature of the technical disclosure. It is submitted with the understanding that it will not be used to interpret or limit the scope or meaning of the claims. Moreover, in the foregoing Detailed Description, it can be seen that various features are grouped together in a single embodiment for the purpose of streamlining the disclosure. This method of disclosure is not to be interpreted as reflecting an intention that the claimed embodiments require more features than are expressly recited in each claim. Rather, as the following claims reflect, inventive subject matter lies in less than all features of a single disclosed embodiment. Accordingly, the following claims are incorporated into the Detailed Description, with each claim standing on its own as a separate embodiment.

[0119] While the foregoing is directed to embodiments of the present disclosure, other and further embodiments of the disclosure may be devised without departing from the basic scope thereof, which scope is determined by the following claims.

Claims

1. an outer tube configured to contain heat, the outer tube having an outer tube diameter; an inner tube nested within the outer tube, the inner tube configured to conduct heat contained in the outer tube, the inner tube having an inner tube diameter smaller than the outer tube diameter, the inner tube having a first end and a second end, and defining a reaction chamber between the first end and the second end; a supply line connected to a first end of the inner tube, the supply line configured to pass dimethyl ether and steam through the inner tube; a reactor outlet adjacent the second end of the inner tube configured to collect hydrogen from the inner tube and discharge the hydrogen; A reactor comprising:

2. 10. The reactor of claim 1, wherein the reaction chamber is configured to contain a catalyst, the catalyst is configured to receive heat contained in the outer tube, and the heat contained in the outer tube has a uniform temperature along a length of the outer tube.

3. 3. The reactor according to claim 2, wherein the reaction chamber produces hydrogen based on a cooperative reaction between the catalyst heated by heat contained in the outer tube, dimethyl ether, and steam.

4. The reactor according to any one of claims 2 to 3, wherein the catalyst comprises an acid catalyst and a reforming catalyst.

5. 5. The reactor of claim 4, wherein methanol is produced by hydrolysis of dimethyl ether over the acidic catalyst and steam reforming of the methanol is produced over a reforming catalyst.

6. The reactor according to any one of claims 1 to 6, wherein the heat accommodated in the outer tube is steam heat, and the inner tube is configured to conduct the heat accommodated in the outer tube.

7. 7. The reactor of claim 6, wherein the outer tube and the inner tube are oriented vertically.

8. The reactor of any one of claims 6 to 7, wherein the outer tube further comprises a steam inlet for the outer tube and a steam condensate outlet for the outer tube.

9. 9. The reactor of claim 8, wherein a space between the outer tube and the inner tube allows the vapor to circulate and condense within the outer tube.

10. a casing configured to contain heat; a plurality of tubes nested within the casing, the plurality of tubes configured to conduct heat contained within the casing, each of the plurality of tubes having a first end and a second end, the plurality of tubes defining a reaction chamber between the first end and the second end; a supply line connected to each of the first ends of the plurality of tubes, the supply line configured to pass dimethyl ether and steam through the plurality of tubes; a reactor outlet adjacent each of the plurality of tube second ends configured to collect hydrogen from the plurality of tubes and discharge the hydrogen; A reactor comprising:

11. 11. The reactor of claim 10, wherein the heat is generated by a plurality of electric heating elements inside the casing and outside the plurality of tubes, the plurality of tubes being configured to conduct heat contained within the casing.

12. 12. The reactor of claim 10, wherein the casing further comprises a refractory surface along an interior portion of the casing and a layer of insulation located between the refractory surface and an exterior portion of each of the plurality of tubes.

13. a shell configured to contain heat; a plurality of tubes nested within the shell, the plurality of tubes configured to conduct heat from a heat source contained within the shell, each of the plurality of tubes having a first end and a second end, the plurality of tubes defining a reaction chamber between the first end and the second end; a supply line connected to each of the first ends of the plurality of tubes, the supply line configured to receive dimethyl ether and steam; a reactor outlet adjacent each of the plurality of tube second ends, the reactor outlet configured to discharge hydrogen; A reactor comprising:

14. a plurality of burners disposed inside the shell and configured to generate heat contained inside the shell; a shell outlet configured to discharge fuel gas; The reactor of claim 13 comprising:

15. 15. The reactor of claim 14, wherein the burners are configured to be turned on simultaneously to maintain a uniform temperature, and the shell is a firebox.

16. a shell configured to contain heat; an upper tube plate connected to an upper portion of the shell, the upper tube plate having a plurality of upper tube plate openings; a lower tube plate connected to a lower portion of the shell, the lower tube plate having a plurality of lower tube plate openings; a plurality of tubes configured to extend between the upper tube plate and the lower tube plate, each of the plurality of tubes configured to be inserted inside one of the plurality of upper tube plate openings and one of the plurality of lower tube plate openings, configured to conduct heat from heat contained within the shell, and forming a reaction chamber between the upper tube plate and the lower tube plate; a feed line adjacent to a top of the shell, the feed line configured to pass dimethyl ether and steam through the plurality of tubes; a reactor outlet adjacent a lower portion of the shell configured to collect hydrogen from the plurality of tubes and discharge the hydrogen; A reactor comprising:

17. 17. The reactor of claim 16, wherein the reaction chamber is configured to contain a catalyst, the catalyst is configured to receive heat contained in the plurality of tubes, and the heat contained in the shell has a uniform temperature between the upper tube plate and the lower tube plate.

18. 20. The reactor of claim 17, wherein the shell and the plurality of tubes are vertically oriented.

19. 19. The reactor of any one of claims 17 to 18, wherein the shell further comprises an inlet for heating the plurality of tubes with at least one of steam or heating oil, and an outlet for draining condensate from inside the shell.

20. 20. The reactor of any one of claims 17 to 19, wherein a space between the shell and the plurality of tubes allows at least one of steam or heating oil to circulate inside the plurality of tubes.

21. a shell having a reaction chamber configured to house a fluidized catalytic reaction bed; a heat source configured to extend from an upper portion of the reaction chamber to a lower portion of the reaction chamber, the heat source configured to heat the fluidized catalytic reaction bed; a feed line proximate a lower portion of the reaction chamber, the feed line having a plurality of feed line openings, each feed line opening of the plurality of feed line openings configured to pass dimethyl ether and vapor into the reaction chamber; a reactor outlet adjacent a top of the shell configured to collect hydrogen from the reaction chamber and discharge the hydrogen; A reactor comprising:

22. 22. The reactor of claim 21, wherein the shell is vertically oriented and the fluidized catalytic reactor bed is configured to circulate within the reaction chamber.

23. 23. The reactor of any one of claims 21 to 22, wherein the heat source is at least one of an electric coil or a tube containing steam that winds around the reaction chamber in alternating directions, and the fluidized catalytic reaction bed is configured to conduct heat from the at least one of the electric coil or the tube containing steam.

24. 24. The reactor of claim 21, wherein the reaction chamber produces hydrogen based on a cooperative reaction between the fluidized catalytic reaction bed heated by the heat source, the dimethyl ether, and steam.

25. 25. The reactor of any one of claims 21 to 24, wherein the shell further comprises a dimethyl ether vapor outlet connected to the supply line, the dimethyl ether vapor outlet configured to discharge excess dimethyl ether and vapor from the reaction chamber to the supply line to recycle the excess dimethyl ether and vapor.

26. a supply line valve configured to control dimethyl ether and steam flowing into an inner tube, the inner tube being telescopically received within an outer tube and configured to conduct heat contained in the outer tube, the inner tube having an inner tube diameter smaller than the outer tube diameter, forming a reaction chamber; a thermal sensor configured to determine the temperature of the heat contained in the outer envelope; a controller communicatively connected to the supply line valve and the thermal sensor; Equipped with The controller determining a temperature of the heat contained in the outer tube based on the thermal sensor; adjusting the supply flow rate at the supply line valve in response to the temperature of the heat satisfying a temperature threshold; A reaction measurement system configured as follows.

27. a vapor dimethyl ether ratio sensor configured to output a vapor dimethyl ether ratio measurement representative of the vapor dimethyl ether ratio in the reaction chamber; The controller communicatively coupled to the vapor dimethyl ether ratio sensor; determining a measurement of the vapor dimethyl ether ratio based on a vapor carbon ratio sensor; comparing the measured vapor dimethyl ether ratio to a vapor carbon ratio; adjusting the supply flow rate at the supply line valve in response to the comparison; The reaction measurement system according to claim 26, configured as follows:

28. a pressure sensor configured to output a pressure measurement representative of an outlet pressure of the outlet line; a back pressure valve in the outlet line configured to control an outlet pressure of the outlet line; Further provided with The controller communicatively connected to the pressure sensor and the back pressure valve; determining a pressure measurement in the outlet line based on the pressure sensor; adjusting the outlet pressure with the back pressure valve in the outlet line in response to the pressure measurement meeting an outlet pressure threshold. The reaction measurement system according to any one of claims 26 to 27, configured as described above.

29. at least one of a carbon monoxide sensor or a carbon dioxide sensor configured to emit at least one of a carbon monoxide measurement or a carbon dioxide measurement indicative of at least one of carbon monoxide or carbon dioxide in the reaction chamber; The controller communicatively coupled to at least one of the carbon monoxide sensor or the carbon dioxide sensor; determining at least one of carbon monoxide or carbon dioxide in the reaction chamber based on at least one of the carbon monoxide sensor or the carbon dioxide sensor; adjusting the supply flow rate with the supply line valve in response to at least one of the carbon monoxide measurement or the carbon dioxide measurement meeting at least one of a carbon monoxide threshold or a carbon dioxide threshold. The reaction measurement system according to any one of claims 26 to 28, configured as described above.

30. a hydrogen sensor configured to output a hydrogen sensor measurement representative of hydrogen at a reactor outlet proximate one end of the inner tube, the hydrogen sensor measurement indicating a cooperative reaction of the dimethyl ether and the steam with a catalyst in the reaction chamber; The controller communicatively connected to the hydrogen sensor; determining a measurement value of the hydrogen sensor at the reactor outlet adjacent one end of the inner tube based on the hydrogen sensor; adjusting the supply flow rate with the supply line valve in response to the measurement value of the hydrogen sensor satisfying a hydrogen threshold value; The reaction measurement system according to any one of claims 26 to 29, configured as described above.

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