STAND-ALONE SELF-SUSTAINING HEAT EXCHANGER TYPE MODULAR REFORMER

The present invention hereinafter with reference to the attached drawing more detailed as follows. However technical idea of the present invention is appended drawing contents of easily account for example ranging only, the technical range of the present invention is defined or changed are not correct. In addition, based on the technical idea of the present invention various modifications and alteration within range of this example vertical one skilled will of course may be permitted.

In addition, the specification range and claim defining the terms or word sense and subsequent analysis or a pre-conventional don't be not, its own invention best method described in the invention for most general outline of a term that technical idea of the present invention to appropriately define a predicated principle to meet the interpreted semantics and general outline must substrate. One embodiment of the present invention most preferred embodiment example specification if a technical idea of the present invention will not replace both example only and since, the application time to replace these various examples can be modified with equal negative accomplishing for understanding.

Figure 1 shows a type of heat exchanger of the present invention also self-standing it stands the stay [ning modular reformer configuration are disclosed.

One reactant at an end (110); said predetermined reaction conditions in an incoming reactant to react catalyst layer (120); said catalyst produced product discharged through the discharge end (130); a reactor including number 1 (100); said unreacted steam in order to cool the cooling trap (200); and said unreacted water passed through a cooling trap reservoir storing a stand-alone number (300); characterized in that a self-supporting modular liposomes including self-it stands the stay [ning heat exchanger type of monomeric units disclosed. Modifying its reactants entering the number not one specifically for example. Methane, naphthenic, fly pin, naphthenic, such as paraffin oil refinery gas, heavy oil, crude water vapor with implementation being. Said catalyst a predetermined reaction conditions using contact modification required number is not one specifically if the reaction conditions in the progress. In 900 °C to 50 °C implementation being 60atm 1atm temperature conditions. Preferably 850 °C temperature conditions in implementation being 10atm 1atm to 400 °C. More preferably 650 °C to 750 °C temperature conditions in 1atm implementation being 2atm.

If greater or lesser than said reaction conditions, catalyst and reactants and reaction away active changing rate is lowered, the silicon products are lower.

Said number 1 reactor catalyst forms can be greatly number one if not. Continuation [kyo anti-tank reaction, tubular reactor, an improved barrier stack flow reactors, implementation being in a fixed bed reactor. Preferably tubular reactor among others.

Said catalyst layer of the catalyst catalyst can be specially number one if not. Platinum-based, cobalt-based, iron-based, nickel-based. Implementation being based catalysts. Preferably the nickel-based catalyst are disclosed.

Said catalyst layer is constructed catalyst the catalyst supports can be specially if not one number. Silicon oxides, alumina, tin oxide, titanium oxide, indium oxide and implementation being. Preferably gamma alumina are disclosed.

Said catalyst layer on the dielectric layer than the reaction catalyst housing specially number one if not. Preferably be a porous metal foam. Said porous metal is made out of aluminum, iron, stainless steel, nickel, iron - chromium - aluminum alloy (Fecralloy), nickel - chromium alloy, copper, copper - nickel alloy selected from heat transfer layer including one or more be a.

Said inlet, catalyst layer, discharge, number 1 reactor, cooling trap, reservoir number in the reaction conditions in the valve, temperature sensor, pressure sensor, flow meter and the like the same number of nontrivial disclosed.

One or more gas supply 2 number 1 feeder (410); water tank for storing water (420); said water tank for supplying water to the pump number 1 (430); water vaporizers for vapor phase change chamber comprises said number 1 (440); and said combustible gas and said water is mixed with said combustible gas and said number 1 pump power supply modules are fed to the evaporation mixer (450) including a reaction water unit (400); can be further comprises.

Is said water tank can be a variety of types of supplies water. Additionally additive may have. In the form of a presence of pure, fresh water, odd, brine, or alcohol and water mixed aqueous solvent such as aliphatic hydrocarbons such as the continuing operation of the cyclohexane; benzene, toluene, xylene, aromatic hydrocarbons such as methyl naphthalene; quinoline, pyridine such as complex ring compounds; acetone, methyl ethyl ketone, cyclohexanone of ketones; acetic acid methyl, methyl acrylic acid such as esters; d ethylene tree amine, N, N - dimethylamino-propyl amine such as amines; d ethyl ether, propylene oxide, ether such as tetrahydrofuran (THF): N - methylpyrrolidone (NMP), dimethyl formamide, dimethyl acetamide amides such as; methyl gun [su selling america [tu process, a process for an aprotic polar solvent such as dimethyl with an organic-based solvent may be one or 2 or more.

Said number 1 said pump water supply to provide said one achieves the purpose particularly number could not. Centrifugal pump, hydraulic pump, drain pump, upon, motor pump, implementation being underwater pump. In the volute pump, axial flow pump, diagonal flow [...] turbo pump, pump concrete pump truck, Washington pump, bucket pump reciprocating pumps, gear pump, screw pump bucket pump implementation being.

The vapor phase water on said evaporator can be supplied one specially number if not. Said evaporator dry, anti-just misfortune, only misfortune, implementation being misfortune circulation. Said implementation being heat exchanger evaporator.

Said exhaust gas after said heat exchanger can possibly combined the exothermic heat reaction heat.

Water unit further comprises a cooler for cooling said reaction reactants can be.

Said mixer for mixing fluids particularly number 2 or more can be one if not. Rotary mixer, fixed mixer, and cold interspersion, fluidized bed mixer implementation being.

An exothermic reaction fuel supplier (510); said fuel reacts with the oxide number feeder (520); said exothermic reaction of fuel with an igniter for disclosure number (530); and said exothermic reaction having such a (540); including a exothermic heat supplier (500) further includes a, said one end of the reactor and the heat exchange chamber said number 1 can be contiguous.

Heating said combustion reaction, partial oxidation reaction gas can be reactions are.

Said fuel supply may comprise one exothermic reaction for a fuel fuel if not specially number. Solid, liquid, vapor be a fossil fuel. Preferably vapor fossil fuel implementation being. More preferably can be methane.

Said oxidation number supply fuel and said oxygen can react if not one specifically number including compounds. Preferably air, oxygen, carbon monoxide implementation being. More preferably implementation being oxygen.

Said igniter reaction can be disclosure if not specially number one. File [los burner, plasma point firearm, spark point firearm, implementation being resistor.

Therefore it stands the stay [ning Figure 2 shows a type of heat exchanger according to one embodiment of the invention self-standing modular reformer configuration are disclosed.

Linked with said solvent and said reservoir products flow through flowmeter (610); said composition of product for measuring analyzer (620); and said mechanical separating and product for capturing number device (630); including a post-processor (600) can be further comprises.

Figure 3 shows a comparison of the present invention also towing compact type reformer configuration are disclosed.

Said compact type the reformer using said self-standing it stands the stay [ning module type reformer alternative electric heater supplied Dichlorethane.

Figure 4 the steam methane reforming and burner operating conditions reactant GSHV according to according to one embodiment of the invention are disclosed.

Figure 5 a according to one embodiment of the invention 15 wt % of Ni / γ provided Al₂ O₃ Compact gas-phase reactor reaction yield graph are disclosed.

According to one embodiment of the invention 20 wt % Ni / γ provided Al of Figure 6 the₂ O₃ Compact gas-phase reactor reaction yield graph are disclosed.

Figure 7 the according to one embodiment of the invention 20 wt % of Ni / γ provided Al₂ O₃ Gas-phase reactor reaction yield graph form heat exchanger are disclosed.

In the embodiment of Figure 8 the reaction of catalyst in a reactor in heat exchanger form reactant GSHV graph are disclosed.

In addition, the present invention refers to said methane and said gas supply ratio 1:1 to 10:1 supply ratio supplied steam reaction with methane may have. Preferably 1. Supply ratio 5:1 to 5:1 may have. More preferably 2:1 to 4:1 may have supply ratio. All said supply ratio, according to reforming reaction can be hard.

In addition, the present invention refers to said reaction with 100 °C to 400 °C supplied steam is directed, to 40 mpa 100kPa implementation being. Preferably 100 °C to 300 °C, to 20 mpa 100kPa implementation being. More preferably 100 °C to 200 °C, to 10 mpa 100kPa implementation being. Said reactants into said out additional Dichlorethane should lower circular metal plate increases and can be dog qualitative reactivity.

In addition, the present invention refers to said catalyst layer in catalyst german silver methane 1L/min, 60g 10g to implementation being. Preferably methane in 1L/min, to 40g 15g implementation being. More preferably methane in 1L/min, 20g to 30g implementation being.

In addition, a catalytic amount of an adhesive composition comprising a hydrocarbon compound the present invention refers to said contrast ratio 1 to 6 g/mol implementation being. Preferably 1. 5 To implementation being 4g/mol. More preferably 2 to implementation being 3g/mol.

In addition, 1 to 6 carbon atoms of said hydrocarbon compound are alkanes, alkyne, can be alkene compounds. Preferably 1 to 3 carbon atoms of alkanes, alkyne, can be alkene compounds. More preferably can be methane.

In addition, the present invention refers to said catalyst layer nickel nitrate aqueous solution catalyst alumina support may be impregnated with disclosed.

In addition, the present invention refers to said catalyst in the form of pores of the porous metal foam structure [...] catalyst sheet (sheet) a constant catalyst is worked into a shape by pressing the porous metal foam catalyst structure by thrusting means for filling the unit number after tank housing, wherein the housing unit is porous metal foam is manufactured catalyst structure, said catalyst diameter 0. 1 - 10 Mm sphere or pellet form and, in a sheet form said porous metal foam structure has a thickness of 1 - 10 mm, pore size 0. 1 - 10 Mm, said direct contact with said porous metal foam structure each pore is the surface of the catalyst part and the extent to which the quantity of charged, which is filled with the porous metal foam catalyst structure housing said catalyst porosity is implementation being 10 - 75%.

In addition, the present invention refers to said exothermic reaction of said fuel and said oxidation number where the combustion or partial oxidation, said catalyst layer temperature remains capable of producing 500 °C to 900 °C for overload apparatus and for supplying the exothermic heat actuator disclosed.

In addition, the present invention refers to said target flow rate and composition conditions said flowmeter and analyzer products drive the water flow rate and composition said reaction unit, said number 1 reactor, said number for the exothermic heat insulation number violations (700) can be further comprise.

In addition, an exhaust gas discharged after heat exchange reactor through said evaporator said insulation the exothermic heat said number 1 be a protruded on the first planes.

(In the embodiment)

The experiments using nickel-functional aliphatic dicarboxylic acid 20 wt % and 15 wt % Ni / γ provided Al filled liposomes compact₂ O₃ Catalyst was utilized.

15 Wt % and 20 wt % Ni / γ provided Al filled₂ O₃ The catalyst Ni nitrate hexahydrate (Ni (NO₃ )₂ 6H₂ O, Aldrich) precursor and γ-a Al₂ O₃ A support bead (UOP) was prepared by Incipient wetness method. First, surface adsorbed impurities for a stand-alone number γ provided Al₂ O₃ Support 400 °C 8hr calcination processing in his embodiment. An appropriate amount of Ni nitrate hexahydrate (Ni (NO₃ )₂ 6H₂ An aqueous solution which has been pretreated γ provided Al O₂ O₃ Support 20 wt % and 15 wt % nickel to be packed Incipient wetness method to the support impregnated using chains. After drying the impregnated catalyst in 120 °C 24hr, 800 °C 8hr was in firing.

Finally, the catalyst average particle diameter 0. Is grinding to 15 mm inner diffusion reduction have been reduced. 200 Ml/min flow rate using a catalyst prepared by the number 800 °C 24hr hydrogen was in before experiment.

Heat exchanger type reformer and supplying modular the reformer burner of Figure 2 Dichlorethane, week burner ignition increased pilot burner flame layer comprises three portions formed backwashing. Methane and a process air supply ratio 1:10 supplied fuel air feed rate of supply of methane gas composition 5 respectively. 00 And 50. Has 0 L/min. Temperature 850 °C monomer which, for steam reforming reaction into the reaction gas to a level below 850 °C 700 °C in resulting in temperature. To increase the reaction temperature in the catalyst layer is methane burner air dose rate 6. In 69 99 L/min. 9 L/min to the raise. 798 °C final catalyst layer temperature is under or over.

Figure 7 steam methane injection ratio 3:1 (18. 5L/min: 6. 17L/min), GHSV=6, 300h^-1 , 20 Wt % of Ni / γ provided Al₂ O₃ Catalyst 167. 9G, 798 °C reaction temperature, pressure 1atm result in reforming characteristics are disclosed. The methane conversion 99. 7% And, H₂ , CO, CO₂ Each composition ratio (drying conditions) 74. 7%, 15. 9%, 7. 76% Are disclosed. H₂ The amount of 1. 21 Nm³ /Hr raised up each other. Said high methane conversion such as due to high reaction temperature to the clip thereto.

H₂ Unit mole of methane as fuel molar ratio 0. 65 Said burner conditions and the conditions are the same. Said fuel demand for refrigeration cycle is provided to convert Cu-a Cl or larger than the value of source, the amount of formed on the methane and air supplied to the burner, the reforming reaction temperature is 650 °C down fuel requirement can be reduced. In this case methane conversion rate is 90. To 6%, H₂ The coating amount is 3% degree expected to substrate.

The process of modular operating system designs required the entire article reduced in surface tackiness such heat exchanger type liposomes can reduce the amount of energy it will rain. In addition utilizing gas heat exchanger type modular the reformer standing five or accomplished in a deep sea environment can be independently onto. The distributed for manufacturing hydrogen will is inserted into the facility.

Reactants GHSV (Gas hourly space velocity) is e.g. increased, increased steam methane gun [ming endothermic heat of reaction. The GHSV 5,000 - 20,000 h^-1 Relayed to which number, 5,000 h^-1 Hereinafter supplied reactant insertion in hydrogen generation amount is too large and corrosion, 20,000 h^-1 In reactant feed rate went low hydrogen generation amount exothermic heat supply two large reaction conversion is too less. An electric heater in general GHSV reactants under control cannot, methane combustion reactor surface and catalyst metal foam heat exchanger type modular liposomes efficacious article reduced in surface tackiness to supply high endothermic heat of reaction can be known. Additionally heat exchanger type modular the reformer reactant flow tube side due to the pore metal in high reactants and a pipe free even GHSV reactant stream according to channel 3.

Figure 8 heat exchanger type modular liposomes that reactants in 10, 000h GHSV is 6,300 GHSV oligomers reactants table^-1 Result of increases up are disclosed. Various GHSV conditions liposomes reaction temperature is methane heat exchanger type modular units: air ratio is 10:1 to at the time of supply while maintaining methane 6. 99, 7. 99 And 10. 9 L/min while under [e been number increases. In accordance with the reactant GHSV methane conversion 99. In reduced to 98% or 7%, hydrogen concentration 75. 5% Being maintained substantially constant. GHSW 6,300 and 8,000 h^-1 798 °C and 760 °C revealing the secret key in each reaction equilibrium reaction temperature to determine the other. GHSW 10,000 h^-1 The reaction temperature is 98% or more and up to 745 °C in methane conversion. The amount of the hydrogen 6,300 h^-1 In 1. 21 Nm³ In 10,000 h/hr^-1 In 1. 97 Nm³ Been increased up/hr.

(Comparison example 1)

Hydrogen 1 nm³ The amount of hydroxy-functional catalytic properties of Figure 3 is for obtaining 2/h of his experiment using compact liposomes. The reformer general electric heater using the air.

15 Wt % of Ni / γ provided Al₂ O₃ 90% Or more methane conversion german silver catalyst loading conditions, hydrogen 1 nm³ In 655 °C/h of 167. 8G are disclosed. Steam methane injection ratio is 3:1. Catalyst bulk density 0. 72 G/mL when, 1 inch diameter, length of a hydroxy-functional 613 mm liposomes using the air. Methane and steam are turned each flow rate is 6. 17L/min, 18. 5L/min are disclosed.

External heat exchange while maintaining the temperature of the catalyst layer 800 °C nitrogen flushed-gate. Reaction has a low methane and steam mixture supplied, the reaction temperature is 701 °C until the movement of the other. Then, a 691 °C to 692 °C holds the temperature during the reaction.

Figure 5 steam methane injection ratio 3:1 (18. 5L/min: 6. 17L/min), catalyst 167. 9G, 692 °C reaction temperature, pressure 1atm result in reforming characteristics are disclosed.

Hydrogen 1 nm³ 2/H or more production flow shown to exhibit a stable reaction time can be found. The methane conversion 94. To the 4%, hydrogen concentration 73. 4% And to an identified, 692 °C maximum production flow rate is 1 in hydrogen. 19 Nm³ /H up to.

(Comparison example 2)

Hydrogen 1 nm³ The amount of hydroxy-functional catalytic properties of Figure 3 is for obtaining 2/h of his experiment using compact liposomes. The reformer general electric heater using the air.

20 Wt % of Ni / γ provided Al₂ O₃ 90% Or more methane conversion german silver catalyst loading conditions, hydrogen 1 nm³ In 655 °C/h of 167. 8G are disclosed. Steam methane injection ratio is 3:1. Catalyst bulk density 0. 72 G/mL when, 1 inch diameter, length of a hydroxy-functional 613 mm liposomes using the air. Methane and steam are turned each flow rate is 6. 17L/min, 18. 5L/min are disclosed.

External heat exchange while maintaining the temperature of the catalyst layer 850 °C nitrogen flushed-gate. Reaction has a low methane and steam mixture supplied, the reaction temperature is maintained after said unloaded to the movement of the up 738 °C.

Figure 6 steam methane injection ratio 3:1 (18. 5L/min: 6. 17L/min), catalyst 167. 9G, 738 °C reaction temperature, pressure 1atm result in reforming characteristics are disclosed.

Hydrogen 1 nm³ 2/H or more production flow shown to exhibit a stable reaction time can be found. The methane conversion 97. To the 9%, 75% and hydrogen concentration to an identified, 692 °C maximum production flow rate is 1 in hydrogen. 22 Nm³ /H up to.

20 Wt % of Ni / γ provided Al₂ O₃ Catalyst according to comparison example 1 example 2 Ni / γ provided Al difference compared result of high activity₂ O₃ Catalyst γ provided Al₂ O₃ Support higher ratio dispersed nickel particles due water are repeated.

The present invention is drawing the mixture of the fuel, such as in the embodiment described together but, this is the subject matter of invention including a one of the one in the embodiment are in various embodiment and, in the embodiment hereinafter art person with skill in the art is to be used for and, in the embodiment described the present invention refers to said only that are not limited by a alluding to him. Thus, the range of the present invention scope of protection for the new device must be interpreted by fee so as to prevent, the subject matter of invention within a range not out change in, substituted, and feature of the present invention is replaced by equivalent in a range will all rights range.

In addition, some of the drawings is to a configuration has the reduced number or a chamber presents a number of wanting to account for these other ancestor.