УСТРОЙСТВО ДЛЯ ВВОДА ГАЗОВ В ХРОМАТОГРАФ

Устройство для ввода газов в хроматограф, содержащее регулятор адресной подачи потоков рабочего агента, отличающееся тем, что оно снабжено узлом распределения рабочего агента и вводимой пробы, оснащенным двумя пневмораспределителями, блоком управления данным узлом, шприцевой иглой ввода пробы, штуцером ввода газа-носителя и выходным штуцером, при этом оба указанных штуцера соединены с хроматографом, а блок управления соединен электросвязью с пневмораспределителями. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 63 056 (13) U1 (51) МПК G01F 5/00 B01J 12/00 (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ПОЛЕЗНОЙ МОДЕЛИ К ПАТЕНТУ (21), (22) Заявка: 2007101594/22 , 16.01.2007 (24) Дата начала отсчета срока действия патента: 16.01.2007 (45) Опубликовано: 10.05.2007 (72) Автор(ы): Трушин Виктор Борисович (RU) Адрес для переписки: 199004, Санкт-Петербург, В.О. Большой пр-кт, 31, ЗАО НТЦ "Ленхром", В.Д. Красикову U 1 6 3 0 5 6 R U Ñòðàíèöà: 1 U 1 Формула полезной модели Устройство для ввода газов в хроматограф, содержащее регулятор адресной подачи потоков рабочего агента, отличающееся тем, что оно снабжено узлом распределения рабочего агента и вводимой пробы, оснащенным двумя пневмораспределителями, блоком управления данным узлом, шприцевой иглой ввода пробы, штуцером ввода газа-носителя и выходным штуцером, при этом оба указанных штуцера соединены с хроматографом, а блок управления соединен электросвязью с пневмораспределителями. 6 3 0 5 6 (54) УСТРОЙСТВО ДЛЯ ВВОДА ГАЗОВ В ХРОМАТОГРАФ R U (73) Патентообладатель(и): ЗАО НТЦ "Ленхром" (RU) , Трушин Виктор Борисович (RU) U 1 U 1 6 3 0 5 6 6 3 0 5 6 R U R U Ñòðàíèöà: 2 RU 5 10 15 20 25 30 35 40 45 50 63 056 U1 Предложение относится к приборному обеспечению процессов контроля состава жидких углеводородов и может быть использовано в хроматографических методах анализа продуктов разложения изоляции, растворенных в углеводородной среде, в частности, в трансформаторном масле, ...

УСТРОЙСТВО ДЛЯ ПОЛУЧЕНИЯ АЦЕТИЛЕНА ИЗ МЕТАНА И УГЛЕВОДОРОДОВ ЭЛЕКТРОНАГРЕВОМ

Устройство для получения ацетилена из метана и углеводородов, включающее проточный химический реактор, закалочное устройство и нагреватель, отличающееся тем, что химический реактор выполнен в виде графитовой трубки, помещенной внутрь нагревателя из криптола, в котором плотность тока возрастает вблизи этой трубки, а сам нагреватель защищен от контакта с окружающей средой инертным газом, кожухом, керамическим электроизолятором и теплоизолятором из криптола. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 123 408 U1 (51) МПК C07C 2/82 (2006.01) C07C 11/24 (2006.01) B01J 12/00 (2006.01) B01J 19/08 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ПОЛЕЗНОЙ МОДЕЛИ К ПАТЕНТУ 2012120454/04, 17.05.2012 (24) Дата начала отсчета срока действия патента: 17.05.2012 (45) Опубликовано: 27.12.2012 Бюл. № 36 R U 1 2 3 4 0 8 Формула полезной модели Устройство для получения ацетилена из метана и углеводородов, включающее проточный химический реактор, закалочное устройство и нагреватель, отличающееся тем, что химический реактор выполнен в виде графитовой трубки, помещенной внутрь нагревателя из криптола, в котором плотность тока возрастает вблизи этой трубки, а сам нагреватель защищен от контакта с окружающей средой инертным газом, кожухом, керамическим электроизолятором и теплоизолятором из криптола. Стр.: 1 U 1 U 1 (54) УСТРОЙСТВО ДЛЯ ПОЛУЧЕНИЯ АЦЕТИЛЕНА ИЗ МЕТАНА И УГЛЕВОДОРОДОВ ЭЛЕКТРОНАГРЕВОМ 1 2 3 4 0 8 Адрес для переписки: 660036, г.Красноярск, Академгородок, 50, стр.24, Институт химии и химической технологии СО РАН, Л.Г. Вецнер (73) Патентообладатель(и): Федеральное государственное бюджетное учреждение науки Институт химии и химической технологии Сибирского отделения Российской академии наук (ИХХТ СО РАН) (RU) R U Приоритет(ы): (22) Дата подачи заявки: 17.05.2012 (72) Автор(ы): Кухтецкий Сергей Владимирович (RU), Парфенов Олег Григорьевич (RU), Тарабанько Николай Валерьевич (RU) U 1 U 1 1 2 3 4 0 8 1 2 3 4 0 8 R U R U Стр.: 2 RU 5 10 15 20 25 ...

Process and Apparatus for Steam-Methane Reforming

Methane reacts with steam generating carbon monoxide and hydrogen in a first catalytic reactor; the resulting gas mixture undergoes Fischer-Tropsch synthesis in a second catalytic reactor. In the steam/methane reforming, the gas mixture passes through a narrow channel having mean and exit temperatures both in the range of 750° C. to 900° C., residence time less than 0.5 second, and the channel containing a catalyst, so that only reactions having comparatively rapid kinetics will occur. Heat is provided by combustion of methane in adjacent channels. The ratio of steam to methane may be about 1.5. Almost all methane will undergo the reforming reaction, almost entirely forming carbon monoxide. After Fischer-Tropsch synthesis, the remaining hydrogen may be fed back to the combustion channels. The steam for the reforming step may be generated from water generated by the chemical reactions, by condensing products from Fischer-Tropsch synthesis and by condensing water vapor generated in combustion.

BIOMASS GASIFICATION GAS PURIFICATION SYSTEM AND METHOD, AND METHANOL PRODUCTION SYSTEM AND METHOD

A biomass gasification gas purification system has a dust removal apparatus for filtering soot and dust from biomass gasification gas (including tar component) obtained through the gasification of the biomass using a biomass gasification furnace, a desulfurization apparatus for removing sulfur oxide component in the filtered biomass gasification gas, first to third pre-reformation reactors that provide pre-reforming catalyst for reforming the tar component in the biomass gasification gas after desulfurization, and first and second coolers that are interposed between the first to third pre-reformation reactors, and for cooling the reformed gas. 18-. (canceled)9. A biomass gasification gas purification system comprising:a dust removal apparatus for filtering soot and dust from biomass gasification gas obtained through the gasification of the biomass using a biomass gasification furnace;a desulfurization apparatus for removing a sulfur oxide component in the filtered biomass gasification gas;at least two or more pre-reformation reactors for reforming the tar component in the biomass gasification gas after desulfurization;a cooler for cooling a portion of the biomass gasification gas; anda supply line for supplying the cooled biomass gasification gas between the at least two or more pre-reformation reactors.10. A methanol production system comprising:{'claim-ref': {'@idref': 'CLM-00009', 'claim 9'}, 'the biomass gasification gas purification system according to ;'}a booster for boosting the biomass gasification gas after the pre-reforming; anda methanol synthesizer for synthesizing the methanol using the boosted gas after boosting.11. The methanol production system according to claim 10 , further comprising:a reformation reactor for reforming the boosted gas after boosting.13. A methanol production method comprising:{'claim-ref': {'@idref': 'CLM-00012', 'claim 12'}, 'purifying biomass gasification gas using the biomass gasification gas purification method according to ...

APPARATUS FOR PRODUCING TRICHLOROSILANE

An apparatus for producing trichlorosilane in which reacted gas including trichlorosilane and hydrogen chloride is produced by heating raw gas including silicon tetrachloride and hydrogen, the apparatus having: a reaction vessel having a substantially cylindrical shape and being provided with a heated wall forming a gas flow-passage along an axis direction; and a heater heating the heated wall, wherein a folding flow-passage is provided at an uppermost stream of the gas flow-passage and has: an inlet flow-passage in which raw gas is introduced; and a turning part connected to a downstream of the inlet flow-passage in which a flow direction of the raw gas is turned at least once in an opposite direction, the turning part is formed between the inlet flow-passage and the heated wall in the folding flow-passage, and a turning length of the folding flow-passage along the axis direction is smaller than a maximum length of the gas flow-passage along the axis direction. 1. An apparatus for producing trichlorosilane in which reacted gas including trichlorosilane and hydrogen chloride is produced by heating raw gas including silicon tetrachloride and hydrogen , the apparatus comprising:a reaction vessel having a substantially cylindrical shape and being provided with a heated wall forming a gas flow-passage along an axis direction; anda heater heating the heated wall, whereina folding flow-passage is provided at an uppermost stream of the gas flow-passage,the folding flow-passage has: an inlet flow-passage in which raw gas is introduced from outside of the reaction vessel and flows the raw gas along the axis direction; and a turning part connected to a downstream of the inlet flow-passage in which a flow direction of the raw gas is turned at least once in an opposite direction,the turning part is formed between the inlet flow-passage and the heated wall in the folding flow-passage, anda turning length of the folding flow-passage along the axis direction is smaller than a ...

METHOD FOR PRODUCING ISOCYANATE

The invention relates to a process for preparing an isocyanate, which involves contacting fluid streams of amine, phosgene and inert medium in at least one mixing device, such that an inert medium stream is metered at least between one amine stream and one phosgene stream within the mixing device, and then reacting an amine with phosgene in a reaction chamber to form an isocyanate. In this process the inert medium stream is metered such that a point of first contact of the amine and the phosgene occurs at a distance from a surface of the mixing device, and a turbulent flow is present in the reaction chamber. 1. A process for preparing an isocyanate , the process comprising:contacting fluid streams of amine, phosgene and inert medium in at least one mixing device, such that an inert medium stream is metered at least between one amine stream and one phosgene stream within the mixing device; and thenreacting an amine with phosgene in a reaction chamber to form an isocyanate,wherein:the inert medium stream is metered such that a point of first contact of the amine and the phosgene occurs at a distance from a surface of the mixing device; anda turbulent flow is present in the reaction chamber.2. The process according to claim 1 , wherein one inert medium stream is metered in between one amine stream and two phosgene streams.3. The process according to claim 2 , wherein one inert medium stream is metered into the phosgene stream on a side of phosgene stream channels facing the amine stream.4. The process according to claim 2 , wherein theinert medium stream is metered into the amine stream on sides of an amine flow channel facing the phosgene stream.5. The process according to claim 1 , wherein an additional inert medium stream is metered in between a phosgene stream and a wall of the mixing device.6. The process according to claim 1 , wherein the mixing device is an annular gap mixing nozzle.7. The process according to claim 1 , wherein the mixing device is a slot nozzle ...

APPARATUS AND METHOD FOR MANUFACTURING COMPOSITE NANO PARTICLES

Disclosed are an apparatus and a method for manufacturing composite nanoparticles. The apparatus comprises: a first precursor supply unit vaporizing a first precursor and supplying it to a reaction unit; a second precursor supply unit vaporizing a second precursor and supplying it to the reaction unit; the reaction unit producing composite nanoparticles by reacting the vaporized first precursor with the vaporized second precursor; an oxygen supply line supplying an oxygen source to the reaction unit; and a collection unit collecting the composite nanoparticles produced by the reaction unit. Since gas phase synthesis occurs in different stages using the U-shaped reaction chamber, aggregation is prevented and composite nanoparticles of uniform size and high specific surface area can be produced easily. 1. An apparatus for manufacturing composite nanoparticles , comprising:a first precursor supply unit vaporizing a first precursor and supplying it to a reaction unit;a second precursor supply unit vaporizing a second precursor and supplying it to the reaction unit;the reaction unit producing composite nanoparticles by reacting the vaporized first precursor with the vaporized second precursor;an oxygen supply line supplying an oxygen source to the reaction unit; anda collection unit collecting the composite nanoparticles produced by the reaction unit,wherein the reaction unit comprises:a U-shaped reaction chamber having: a first straight flow path wherein nanoparticles are produced from the vaporized first precursor supplied from the first precursor supply unit; a curved flow path which is communicated with the first straight flow path and allows the nanoparticles produced from the first straight flow path to be introduced to a second straight flow path with a curved flow; and the second straight flow path which is communicated with the curved flow path and wherein the composite nanoparticles are produced from the reaction of the nanoparticles of the first precursor ...

UREA PLANT

The invention relates to urea plant with a CO2 and NH3 feed, which comprises a purge line, characterized in that the purge line is connected with a fuel gas input line of a utility plant or an NH3 plant. 1. A urea plant comprising a COand a NHfeed , which further comprises a purge line , wherein the purge line is connected with a fuel gas input line of a utility plant or an NHplant.2. A urea plant according to claim 1 , wherein the purge gas contains oxygen at a concentration in the range of 0-10 mol %.3. A urea plant according to claim 1 , further comprising synthesis equipment and synthesis piping wherein material used for the synthesis equipment and synthesis piping a duplex ferritic-austenitic contains claim 1 , in % by weight:0-0.05 C;0-0.8 Si;0.3-4 Mn;28-35 Cr;3-10 Ni;1.0-4.0 Mo;0.2-0.6 N;0-1.0 Cu;0-2.0 W;0-0.010 S;0-0.2 Ce,the remainder being Fe and normally occurring impurities and additives, having a ferrite content 30-70% by volume.4. A urea plant according to claim 1 , wherein the oxygen concentration in the purge gas is in the range 0-1 mol %.5. A urea plant according to claim 1 , wherein oxygen is essentially absent in the purge gas.6. A urea plant according to claim 1 , wherein the purge stream is directed to the reformer section in an ammonia plant.7. A urea plant according to claim 1 , wherein the purge stream is directed to the fuel gas supply of a steam boiler. In commercial urea processes, urea (NHCONH) is produced by reacting ammonia (NH) and carbon dioxide (CO) at elevated temperature and pressure according to the reactions:2NH+CO→NHCOONHNHCOONH→NHCONH→HOAn overview of commercial processes using this chemistry is given e.g. in Ullmann Encyclopedia, 2005 Wiley-VCH verlag, Weinheim, Germany, chapter Urea. All processes use NHand COas feedstock. These feedstocks, usually both originating from a ammonia plant contain impurities. The impurities do not react in the abovementioned chemistry, and therefore need to be purged from the urea plant in order ...

FLUID SHOCKWAVE REACTOR

The present invention relates to a fluid shockwave reactor. The fluid shockwave reactor introduces laser resonance theory into the field of fluid physics. It consists of a shockwave resonance energy concentration device and at least one set of jet collision device. The shockwave resonance energy concentration device can enhance the shockwave strength produced during jet collisions; strengthen the ultrahigh pressure and cavitation effect of the shockwave field; it can also intensify physical and chemical effects on the processed materials. The fluid shockwave reactor can achieve ultrafine crushing on the fluid materials with lower energy consumption. Under certain technological conditions, the fluid shockwave reactor may also effectively catalytize the chemical reaction process on fluid materials. 1. A fluid shockwave reactor , comprising a shockwave resonance energy concentration device and at least one set of jet collision device ,wherein said jet collision device is composed of two sets of coaxial and opposite nozzle parts, each of said two sets of coaxial and opposite nozzle parts having the same nozzle,wherein said shockwave resonance energy concentration device is a chamber combined with rigid spherical concave surfaces or other rigid convergent surfaces configured to reunite the shockwaves emitted from a focus and converge them back to said focus to produce new shockwaves,wherein said chamber has a jet orifice that holds said nozzle parts and a discharge port that permits outflow of the processed fluid from said chamber,wherein a mid-point between said two nozzles is the location where jet collisions occur and is disposed at a center of said spherical concave surfaces or said focus of all combined convergent surfaces,wherein a sum of the cross-sectional area of said discharge port is greater than a total cross-sectional area of all of said nozzles, and the cross-sectional area of said discharge port and the open position of said discharge port keeps ...

DEVICE AND METHOD FOR PRODUCING SUSPENSIONS OR WET PASTES OF NANOPOWDERS OR ULTRA-FINE POWDERS

A device and a method for producing suspensions or wet pastes of nanoparticles or ultra-fine particles. The method comprises: introducing a flow of particles of nanometric or submicronic size into a first compartment of a chamber having a bulk density between 15 and 100 g/L; forming, in the first compartment, a spray of droplets between 1 and 10 micrometres in size, by injecting a solvent in liquid or gas form into a second compartment of the device and passing said solvent through the filtering means, the solvent being chosen from the solvents which are liquid at ambient temperature and at atmospheric pressure; stopping the formation of the spray when the entire quantity of particles contained in the first compartment forms, as required, with the solvent, a suspension comprising between 80 and 99.9% solvent, if the solvent is introduced into the second compartment in liquid form, or a wet paste comprising between 1 and 10% solvent, if the solvent is introduced into the second compartment in gas form; recovering the suspension or wet paste formed. 1. A device for producing a suspension or a wet paste of particles of nanometric or submicronic size , comprising:a chamber having a first and a second compartment arranged on top of each other;filtering means arranged in the chamber between the first and second compartments, said means being suitable for preventing the-passage of particles of nanometric or submicronic size, while enabling passage of a fluid, from one compartment to the other;means for introducing a flow of particles of nanometric or submicronic size having a bulk density between 15 and 100 g/L, situated in the first compartment;means for discharging gas, situated in the second compartment;means for injecting at least one fluid, situated in the second compartment, suitable for creating a flow from the filtering means, said flow being inverted with respect to the flow created by the means for introducing a gas flow;means for outputting suspension or wet ...

NOZZLE REACTOR AND METHOD OF USE

A nozzle reactor includes a passage having one or more regions with a converging-diverging shape. The nozzle reactor accelerates a reacting fluid to supersonic velocities and mixes it with a feed material. The reacting fluid and the feed material may be pre-heated. The high speed collision between the reacting fluid and the feed material at elevated temperatures causes the materials to react. 1. A nozzle reactor comprising:a main passage including a first region followed by a second region, the first region and the second region each including a convergent section, a throat, and a divergent section;a feed passage in fluid communication with the main passage; anda distributor positioned in the feed passage, the distributor including a plurality of non-circular injection holes configured to annularly distribute flow from the feed passage to the main passage;wherein the distributor distributes flow from the feed passage into the main passage at a location between the throat in the first region and the throat in the second region.2. The nozzle reactor of wherein the main passage expands between the location where the distributor distributes flow into the main passage and the throat in the second region.3. The nozzle reactor of wherein the cross-sectional area of the throat in the second region is at least twice as large as the cross sectional area of the throat in the first region.4. The nozzle reactor of comprising a head portion coupled to a body portion claim 1 , the head portion including the first region and the body portion including the second region.5. The nozzle reactor of wherein the distributor is a physically separate component capable of being removed from the nozzle reactor and replaced.6. The nozzle reactor of comprising a wear ring through which the main passage passes claim 1 , the wear ring being positioned immediately adjacent to and downstream of the location where the distributor distributes flow into the main passage claim 1 , wherein the wear ring ...

Method and Apparatus for Synthetizing Composite Using Simultaneous Vaporization, Vaporizer for Composite Synthesis Apparatus, Vaporizer Heater, and Composite

A composite synthesis method and apparatus, a vaporizer for the composite synthesis apparatus, a vaporizer heater and a composite. In the composite synthesis apparatus using simultaneous vaporization, two or more vaporizers are heated by heaters such that samples vaporized by the vaporizers are supplied into a reactor to synthesize a composite. The apparatus and method may prepare multiple-metal or metal-carbon heterogeneous composites, and may be applied to various metal- and carbon-based adsorbents, absorbents, gas/liquid separation membranes and various catalyst processes. Further, the composite may be applied to various industrial fields through change in metal components or carbon structures. 1. A composite synthesis apparatus using simultaneous vaporization , comprising:a first vaporizer which vaporizes a first sample for synthesis;a second vaporizer which vaporizes a second sample to be synthesized with the first sample;a first heater which heats the first vaporizer;a second heater which heats the second vaporizer; anda reactor to which the first sample and the second sample vaporized by the first vaporizer and the second vaporizer are supplied to synthesize a composite.2. The apparatus according to claim 1 , further comprising:a reaction gas supplier supplying a reaction gas to the reactor for reaction between the first sample and the second sample.3. The apparatus according to claim 1 , further comprising:a recycler returning unreacted gas discharged from the reactor to the reactor.4. The apparatus according to claim 1 , further comprising:a gas supplier supplying gas for vaporizing the first sample and the second sample to the first vaporizer and the second vaporizer.5. The apparatus according to claim 1 , wherein the first vaporizer comprises:a main body receiving the first sample;a sample supply section formed at one side of the main body and supplying the first sample;a gas supply section formed at another side of the main body and supplying gas for ...

PROCESS AND APPARATUS FOR CONVERSION OF SILICON TETRACHLORIDE TO TRICHLOROSILANE

A process for hydrogenating chlorosilanes in a reactor, wherein at least two reactant gas streams are introduced separately from one another into a reaction zone, wherein the first reactant gas stream comprising silicon tetrachloride is conducted via a first heat exchanger unit in which it is heated and is then conducted through a heating unit which heats it to a first temperature before the first reactant gas stream reaches the reaction zone, and wherein the second reactant gas stream comprising hydrogen is heated by a second heat exchanger unit to a second temperature, wherein the first temperature is greater than the second temperature, and then introduced into the reaction zone, such that the mixing temperature of the two reactant gas streams in the reaction zone is between 850° C. and 1300° C., and said reactant gas streams react to give product gases comprising trichlorosilane and hydrogen chloride, wherein the product gases obtained in the reaction are conducted through said at least two heat exchanger units and preheat the reactant gas streams of the reaction by the countercurrent principle, wherein the flow passes first through the first heat exchanger unit and then through the second heat exchanger unit. A reactor for hydrogenating chlorosilanes, comprising two gas inlet devices through which reactant gases can be introduced separately from one another into the reactor, and at least one gas outlet device through which a product gas stream can be conducted, at least two heat exchanger units which are connected to one another and which are suitable for heating reactant gases separately from one another by means of the product gases conducted through the heat exchanger units, and a heating zone which is arranged between a first heat exchanger unit and a reaction zone and in which there is at least one heating element. 1. A process for hydrogenating chlorosilanes in a reactor , wherein at least two reactant gas streams are introduced separately from one ...

Silicon-aluminum mixed oxide powder

Silicon-aluminum mixed oxide powder having a weight ratio of (Al 2 O 3 /SiO 2 ) ttl in the total primary particle of from 0.003 to 0.05, a weight ratio (Al 2 O 3 /SiO 2 ) surface of the primary particles in a surface layer having a thickness of about 5 nm which is less than in the total primary particle and a BET surface area of from 50 to 250 m 2 /g. It is prepared by igniting one or more silicon compounds selected from the group consisting of CH 3 SiCl 3 , (CH 3 ) 2 SiCl 2 , (CH 3 ) 3 SiCl and (n-C 3 H 7 )SiCl 3 , a hydrolysable and oxidizable aluminum compound, at least one fuel gas and air and burning the flame into a reaction chamber, subsequently separating the solid from gaseous materials and subsequently treating the solid with water vapor. The silicon-aluminum mixed oxide powder can be used as catalyst.

NOZZLE REACTOR AND METHOD OF USE

Embodiments of a nozzle reactor of the type useable to inject a first material feed stock and a second material feed stock to cause interaction between the first material feed stock and second material feed stock are described herein. According to some embodiments, the nozzle reactor may crack residual oil produced by other processing units in a refinery process. Furthermore, nozzle reactors may replace traditional processing units of a refinery process, such as cokers, hydrocrackers and deasphalting units. 1. A feed material cracking method comprising:injecting a stream of cracking material through a cracking material injector into a reaction chamber; andinjecting residual oil into the reaction chamber adjacent to the cracking material injector and traverse to the stream of cracking material entering the reaction chamber from the cracking material injector.2. The feed material cracking method as claimed in claim 1 , wherein the residual oil comprises asphaltene.3. The feed material cracking method as claimed in claim 2 , further comprising the step of mixing the asphaltene with a solvent prior to injecting the asphlatene into the reaction chamber.4. The feed material cracking method as claimed in claim 3 , wherein the solvent is selected from the group consisting of toluene claim 3 , Aromatic 100 claim 3 , Aromatic 150 claim 3 , and vacuum gasoil.5. The feed material cracking method as claimed in claim 3 , wherein the asphaltene and solvent are mixed at a asphaltene:solvent ratio of from about 1:2 to about 2:1.6. The feed material cracking method as claimed claim 1 , wherein the residual oil comprises coke.7. The feed material cracking method as claimed in claim 6 , further comprising the steps of:grinding the coke to thereby form up ground coke; andmixing the ground coke with a solvent prior to injecting the ground coke into the reaction chamber.8. The feed material cracking method as claimed in claim 7 , wherein grinding the coke comprises grinding the coke to a ...

APPARATUS FOR LIQUEFACTION OF CARBONACEOUS MATERIAL

A carbonaceous material liquefaction apparatus which uses a nozzle assembly to supply a pressurised liquid towards a carbonaceous material as a high velocity liquid. A supply line () supplies the high pressure liquid to the nozzle assembly (). The high velocity liquid reacts with the carbonaceous material () in a reaction zone () to produce a processed carbonaceous material. A product return line () returns the processed carbonaceous material and entrained liquid to a processing plant. The processing plant comprises a heat exchanger () to transfer heat from the product return line to the supply line, a high pressure pump () to provide the high pressure liquid to the supply line, a separator () in the product return line downstream of the heat exchanger to separate gas () and oil () product from the entrained liquid, at least part of the liquid () being recycled () to the high pressure pump. The reaction can be carried out in-situ or in an above ground reaction chamber (). 1. A carbonaceous material liquefaction apparatus comprising a nozzle assembly to supply a pressurised liquid with superheated or supercritical properties towards a carbonaceous material as a high velocity liquid , a supply line to supply the high pressure liquid to the nozzle assembly , the high velocity liquid reacting with the carbonaceous material to produce an upgraded or liquefied carbonaceous material , a product return line to return the processed carbonaceous material and entrained liquid to a processing plant , the processing plant comprising a heat exchanger to transfer heat from the product return line to the supply line , a high pressure pump to provide the high pressure liquid to the supply line , a separator in the product return line downstream of the heat exchanger to separate gas and oil product from the processed carbonaceous material and entrained liquid , and a recycle line to transfer at least part of the liquid from the separator to the high pressure pump.2. A carbonaceous ...

PLASMA REACTOR GAS DISTRIBUTION PLATE WITH RADIALLY DISTRIBUTED PATH SPLITTING MANIFOLD

In a showerhead assembly, a path splitting manifold comprises a gas supply inlet and a planar floor and plural gas outlets extending axially through the floor and azimuthally distributed about the floor. The path splitting manifold further comprises a plurality of channels comprising plural paths between the inlet and respective ones of the plural outlets. A gas distribution showerhead underlies the floor of the manifold and is open to the plural outlets. In certain embodiments, the plural paths are of equal lengths. 1. A gas distribution showerhead assembly for use in a plasma reactor , comprising:a gas supply lid having a bottom surface, and a gas supply port in said bottom surface;a manifold plate having top and bottom manifold surfaces, said top manifold surface facing said bottom surface of said gas supply lid;a showerhead plate facing said bottom manifold surface and an array of plural gas injection orifices extending through said showerhead plate and distributed in both a radial direction and in an azimuthal direction; (a) plural manifold orifices extending through said manifold plate and located along a radial location;', '(b) plural top surface channels in said top manifold surface and defining plural top paths of generally equal lengths between said gas supply port and respective ones of said manifold orifices;', '(c) plural bottom surface channels formed in said bottom manifold surface and defining plural bottom paths of generally equal lengths between respective ones of said manifold orifices and respective ones of said plural gas injection orifices., 'a gas distribution manifold comprising2. The apparatus of wherein said plural top surface channels constitute a hierarchy of channels recursively coupled at their midpoints to outputs of other channels of said hierarchy.3. The apparatus of wherein said plural bottom surface channels comprise plural arcuate bottom surface channels at respective radial locations and plural radial bottom surface channels ...

DEVICES FOR INJECTION OF GASEOUS STREAMS INTO A BED OF FLUIDIZED SOLIDS

Injection nozzles for use in a gas distribution device are disclosed. In one aspect, the injection nozzle may include: a tube having a fluid inlet and a fluid outlet; wherein the inlet comprises a plurality of flow restriction orifices. In another aspect, embodiments disclosed herein relate to an injection nozzle for use in a gas distribution device, the injection nozzle including: a tube having a fluid inlet and a fluid outlet; wherein the fluid inlet comprises an annular orifice surrounding a flow restriction device. Injection nozzles according to embodiments disclosed herein may be disposed in a gas distribution manifold used in a vessel, for example, for conducting polymerization reactions, spent catalyst regeneration, and coal gasification, among others. 1. A gas distribution apparatus , comprising:a distribution manifold in fluid communication with a gas source and a plurality of injection nozzles;each of the plurality of injection nozzles comprising a fluid inlet disposed within the distribution manifold and a fluid outlet;wherein the fluid inlet comprises a plurality of flow restriction orifices.2. The apparatus of claim 1 , wherein the fluid outlet is proximate an outer circumference of the distribution manifold.3. The apparatus of claim 1 , wherein the tube outlet is external to an outer circumference of the distribution manifold.4. The apparatus of claim 1 , wherein the plurality of flow restriction orifices comprises a plurality of radial flow restriction orifices distributed circumferentially through the tube.5. The apparatus of claim 4 , wherein an axial end of the tube proximate the plurality of radial flow restrictions orifices is capped.6. The apparatus of claim 4 , wherein a ratio of an inner diameter of the tube outlet to a diameter of a radial flow restriction orifice is greater than 2:1.7. The apparatus of claim 4 , wherein the plurality of radial flow restriction orifices are disposed through the tube a length L from an axial end of the tube ...

Apparatus for microdroplet generation via liquid bridge breakup

An apparatus for microdroplet generation via liquid bridge breakup, which can efficiently generate microdroplets using liquid bridge breakup without using a complicated mechanical device. The apparatus includes: two substrate plates having respective hydrophilic surfaces; a protrusion provided on a side surface of either of the two substrate plates so as to maintain a predetermined space between the two substrate plates; and a spacer provided on ends of the two substrate plates and spacing the two substrate plates from each other, thereby inducing liquid bridge breakup.

OZONE GAS SUPPLY SYSTEM

In the present invention, particularly, means for removing moisture contained in a raw material gas is provided in a raw material gas supply part so that the amount of moisture contained in the raw material gas that is supplied to an ozone gas supply system is reduced, and additionally an ozone gas output flow rate management unit is provided that is configured to receive a plurality of ozone gas outputs from a plurality of nitrogen-free ozone generation units and capable of performing an ozone gas output flow rate control for selectively outputting one or a combination of two or more of the plurality of ozone gas outputs to any of a plurality of ozone treatment apparatuses by performing an opening/closing operation on a plurality of ozone gas control valves provided in the ozone gas output flow rate management unit. 1. An ozone gas supply system , configured to supply an ozone gas to each of a plurality of ozone treatment apparatuses while controlling a flow rate and concentration of the gas , the ozone gas supply system comprising:a plurality of nitrogen-free ozone generation units,an ozone gas output flow rate management unit, andan ozone gas output flow rate management unit control part,wherein units of the plurality of nitrogen-free ozone generation units each comprise a nitrogen-free ozone generator suitable for generating an ozone gas and applying a photocatalytic material capable of generating ozone to a discharge surface; an ozone power source suitable for controlling power supplied to the nitrogen-free ozone generator; a mass flow controller (MFC) suitable for controlling a flow rate of a raw material gas inputted to the nitrogen-free ozone generator; an automatic pressure controller (APC) suitable for automatically controlling internal pressure within the nitrogen-free ozone generator; an ozone concentration meter suitable for detecting an ozone concentration value of ozone gas outputted from the nitrogen-free ozone generator; and an ozone control part ...

Sulfur recovery unit and sulfur recovery method

A sulfur recovery unit comprising: a reaction furnace configured to carry out a high-temperature Claus reaction between hydrogen-sulfide-containing gas and oxygen-containing gas introduced to the reaction furnace; a sulfur condenser configured to cool reaction gas discharged from the reaction furnace and condense sulfur contained in the reaction gas; and a pipe that connects the reaction furnace to the sulfur condenser, wherein the reaction furnace is fixed to the ground; and the sulfur condenser and the pipe are arranged so as to be able to move relative to the reaction furnace.

Anti-Soot Reformer

A novel reformer is provided. A gas fuel is guided from a fuel channel. Air and water are guided from a liquid/gas channel. They are mixed together in a mixing space. On mixing them, the temperature of the mixing space is between 150° C. and 300° C. Thus, the reactants are preheated and fully mixed; and a proper temperature is reached to avoid local over-heating and to prevent carbon deposited.

ENERGY PRODUCTION SYSTEMS UTILIZING RUMINANT ANIMAL METHANE EMISSIONS

A process for the utilization of the methane produced by enteric fermentation, specifically to a process that utilizes methane produced by ruminant animals through enteric fermentation as a source of carbon and/or energy for the directed production of methane-based goods or processes is provided. 19.-. (canceled)10. A system configured to simultaneously reduce environmental enteric fermentation methane emissions and produce energy , comprising:(a) one or more ruminant animals; wherein said first gas comprises enteric fermentation-derived methane gas that has been emitted by and collected from said animals,', 'wherein said second gas comprises oxygen and said first gas;, '(b) a first and second gas,'}(c) an energy-generating device that oxidizes methane to produce energy; and(d) a conveyor configured to direct, move, and/or convey said second gas to contact said energy-generating device;wherein introduction of said first gas and said second gas to said device results in oxidation of a portion of said first gas to methanol, water, and/or carbon dioxide, thereby simultaneously reducing environmental enteric fermentation methane emissions and producing energy.11. The system of claim 10 , wherein said second gas further comprises ammonia claim 10 , wherein said energy generated is heat claim 10 , and wherein said energy-generating device comprises an engine.12. The system of claim 10 , wherein said energy-generating device is selected from the group consisting of a fuel cell claim 10 , an engine claim 10 , a culture of microorganisms claim 10 , a reverse-flow reactor claim 10 , a turbine claim 10 , and/or a microturbine.13. The system of claim 10 , wherein said second gas further comprises one or more of air claim 10 , dust claim 10 , nitrogen claim 10 , gases claim 10 , carbon dioxide claim 10 , particulate matter claim 10 , and/or other airborne matter.14. The system of claim 13 , wherein one or more of dust claim 13 , nitrogen claim 13 , gases claim 13 , carbon ...

GAS TREATMENT EQUIPMENT OF NUCLEAR POWER PLANT

At the time of loss of coolant accident, when station blackout occurs, hydrogen, radioactive nuclides, and steam are discharged from a broken portion of a pipe connected to a reactor pressure vessel into the primary containment vessel. A passive autocatalytic hydrogen treatment apparatus installs a catalytic layer and heat exchanger tubes of a heat exchanger in a casing. High-temperature steam including hydrogen and radioactive nuclides is supplied into the heat exchanger tubes and heats gas supplied into the casing . The steam is condensed in the heat exchanger tubes and generates mists. The mists are removed by a mist separator together with the radioactive nuclides. The gas including hydrogen fed from the mist separator in the casing is heated by the aforementioned steam and is introduced into the catalytic layer. Hydrogen is combined with oxygen in the catalytic layer to steam. 1. A gas treatment equipment of a nuclear power plant comprising:a gas treatment apparatus for treating gas components included in gas supplied from a primary containment vessel; and a mist separator,wherein said gas treatment apparatus includes a casing and a gas component treatment member installed in said casing for treating said gas components;wherein a heating device for heating said gas in said casing supplied to said gas component treatment member by heat held by said gas, which includes said steam and gas components, supplied from a primary containment vessel is installed in said casing;wherein said mist separator for removing mists generated by condensation of said steam in said heating device together with a part of said gas components adsorbed to said mists is connected to said heating device; andwherein a pipe path for introducing said gas including said gas components not removed by said mist separator from said mist separator into said casing is installed.2. The gas treatment equipment of a nuclear power plant according to claim 1 , wherein said heating device is disposed on ...

FACILITY AND REACTOR FOR DIRECTLY SYNTHESIZING HYDROCHLORIC ACID FROM HYDROGEN AND CHLORINE WITH HEAT RECOVERY

A reactor for the synthesis of gaseous HCl from chlorine and hydrogen, including a convector and a furnace having in a bottom portion a burner supplied with chlorine and hydrogen in order to form gaseous HCl. The convector is arranged coaxially above the furnace, and includes a plurality of tubes in contact with a heat-transport fluid, the reactive gases of the furnace passing through the tubes. The heat-transport fluid flows in the space between the tubes, with a perforated tubular plate whereon are attached the tubes of the convector being arranged between the furnace and the convector. All of the inner walls of the reactor in contact with the gaseous HCl are made of a metal alloy, and in the furnace, at least one portion of the inner surfaces of the walls in contact with the gaseous HCl is made of an alloy comprising at least 20 wt % nickel. 114-. (canceled)15. A reactor for the synthesis of gaseous HCl , comprising:a furnace having at a bottom portion thereof a burner which is supplied with chlorine and hydrogen in order to form gaseous HCl;a convector coaxially arranged above the furnace and having a plurality of spaced apart convector tubes in contact with a heat-transport fluid, the reactive gases in the furnace flowing through the convector tubes and the heat-transport fluid flowing in the spaces between adjacent tubes;a perforated tubular plate arranged between the furnace and the convector and attached to the convector tubes, the inner walls of the furnace and the convector in contact with the gaseous HCl are made of a metal alloy, and', 'at least one portion of the inner wall surfaces of the furnace walls in contact with the gaseous HCl is made of an alloy comprising at least 30 wt % nickel., 'wherein16. The reactor of claim 15 , wherein all of the inner wall surfaces of the furnace in contact with the gaseous HCl are made from an alloy comprising at least 30 wt % nickel.17. The reactor of claim 16 , wherein the inner wall surfaces made of an alloy ...

METHOD AND APPARATUS FOR PROCESSING OF MATERIALS USING HIGH-TEMPERATURE TORCH

A method and apparatus for reforming carbonaceous material into syngas containing hydrogen and CO gases is disclosed. In one embodiment, a hydrogen rich torch reactor is provided for defining a reaction zone proximate to torch flame. One input of the reactor receives input material to be processed. Further inputs may be provided, such as for example to introduce steam and/or gases such as methane, oxygen, hydrogen, or the like. 1. An apparatus for processing input material , comprising:a reactor vessel defining a combustion zone; the reactor vessel further having at least one input port for receiving the input feedstock, the input feedstock being directed proximally to the at least one flame;', 'the reactor vessel further having an output for discharging a primary reactor output stream;', 'at least one cooler coupled to receive the primary reactor output stream and operable to cool the primary reactor output stream and generate a secondary output stream;, 'the reactor vessel having at least one input for a combustible torch fuel to at least one torch nozzle, the at least one torch nozzle being adapted to generate at least one flame within said reactor;'}a scrubber, coupled to receive the secondary output stream from the cooler/separator, the scrubber being operable to further extract at least one gas from the secondary output stream.2. An apparatus in accordance with claim 1 , wherein the reactor vessel further has an input for receiving a supply of steam.3. An apparatus in accordance with claim 1 , wherein the combustible torch fuel comprises hydrogen.4. An apparatus in accordance with claim 2 , wherein the combustible torch fuel further comprises methane.5. An apparatus in accordance with claim 1 , wherein the combustible torch fuel is combined with oxygen.6. An apparatus in accordance with claim 1 , wherein the combustible torch fuel comprises acetylene.7. An apparatus in accordance with claim 1 , wherein the reactor vessel further having at least one input port ...

CARBONATION DEVICE AND METHOD OF CARBONATION USING THE SAME

Disclosed is a carbonation device including: a storage tank storing a carbonation subject solution; a droplet spray unit spraying the carbonation subject solution from the storage tank as droplets; a carbonation reaction tank disposed with the droplet spray unit and filled with a carbonation gas under a predetermined pressure to provide a slurry by a carbonation reaction of the droplet-sprayed carbonation subject solution with the filled carbonation gas; a carbonation gas supply unit supplying the carbonation gas into the carbonation reaction tank to maintain the carbonation gas in the carbonation reaction tank under the predetermined pressure; and a slurry outlet unit ejecting the slurry from the carbonation reaction tank to maintain the slurry formed in the carbonation reaction tank within a predetermined level, and a method of carbonation using the same. 1. A carbonation device comprising:a storage tank storing a carbonation subject solution;a droplet spray unit spraying the carbonation subject solution from the storage tank in droplets;a carbonation reaction tank disposed with the droplet spray unit and filled with a carbonation gas under a predetermined pressure to provide a slurry by a carbonation reaction of the droplet-sprayed carbonation subject solution with the filled carbonation gas;a carbonation gas supply unit supplying the carbonation gas into the carbonation reaction tank to maintain the carbonation gas in the carbonation reaction tank under the predetermined pressure; anda slurry outlet unit ejecting the slurry from the carbonation reaction tank to maintain the slurry formed in the carbonation reaction tank within a predetermined level.2. The carbonation device of claim 1 , wherein the slurry outlet unit ejecting the slurry formed in the carbonation reaction tank from the carbonation reaction tank to maintain the slurry amount within the predetermined level comprises:a level measurement unit generating a signal to confirm whether the slurry amount ...

Mesofluidic Reactor With Pulsing Ultrasound Frequency

A mesofluidic reactor performs a chemical reaction of a starting material. A liquid phase starting material is introduced into a spraying head equipped with an ultrasound generating piezoelectric crystal unit. An inert/reagent gas feeds into the spraying head, connected to a reactor tube arranged within a thermally insulated multi-zone heating unit. For solid phase, an inert/reagent gas is introduced into a solids container connected to a spraying head equipped with an ultrasound generating piezoelectric crystal unit. The spraying head connects to a reactor tube arranged within a thermally insulated multi-zone heating unit. In either case, a reactor tube outlet connects to a cooled product trap to collect conversed substances. The spraying head generates a particle size distribution with nano and micro sized particles for the liquid phase and nano, micro or larger particles for the solid phase. The inert/reagent gas is preheated over the piezoelectric crystal unit's surface. 1. A mesofluidic reactor to perform a chemical reaction of a starting material , wherein components of the reactor are combined together depending on phase state of the starting material to form said reactor , the mesofluidic reactor comprising:(i) in case of a liquid phase starting material,{'b': 1', '4, 'a container () to store said liquid phase starting material, a high-pressure spraying head () equipped with an ultrasound generating piezoelectric crystal unit and having a nozzle,'}{'b': 3', '1', '4, 'a tubing () to provide fluid communication between the container () and the spraying head (),'}{'b': '12', 'a reactor tube () with an inlet and an outlet,'}{'b': '12', 'claim-text': [{'b': 4', '12, 'the spraying head () is connected to the inlet of the reactor tube (),'}, {'b': 12', '13, 'the outlet of the reactor tube () is connected to a cooled product trap () to collect conversed substances, and'}, {'b': 13', '14', '15, 'the product trap () having an outlet connected to a vacuum tap () and a ...

METHOD FOR PRODUCING CARBAMATE, METHOD FOR PRODUCING ISOCYANATE, CARBAMATE PRODUCTION SYSTEM, AND ISOCYANATE PRODUCTION SYSTEM

A method for producing carbamate including a urea production step; a carbamate-forming step; an ammonia separation step of absorbing the gas with water in the presence of carbonate to produce a gas absorption water, and separating ammonia; an aqueous alcohol solution separation step of separating an aqueous alcohol solution from the gas absorption water; an ammonia/carbon dioxide separation step of separating carbon dioxide gas from the aqueous ammonia solution in the gas absorption water from which the aqueous alcohol solution is separated; an aqueous ammonia solution reusing step of mixing the aqueous ammonia solution and carbonate with the water to be used for production of the gas absorption water. 1. A carbamate production system comprising:a urea production apparatus for producing urea by reaction between ammonia and carbon dioxide gas,a carbamate-forming reaction apparatus for producing carbamate by carbamate-forming reaction between amine, the urea, and alcohol, and by-producing a gas containing alcohol, ammonia, and carbon dioxide,an ammonia separation apparatus for absorbing the gas with water to produce a gas absorption water, and separating ammonia,an aqueous alcohol solution separation apparatus for separating the aqueous alcohol solution from the gas absorption water,an ammonia/carbon dioxide separation apparatus for separating carbon dioxide gas from the aqueous ammonia solution in the gas absorption water from which the aqueous alcohol solution is separated,an aqueous ammonia solution reusing apparatus for using the aqueous ammonia solution along with the water for production of the gas absorption water,an ammonia reusing apparatus for using, in the urea production apparatus, the ammonia separated in the ammonia separation apparatus andan alcohol reusing apparatus for separating alcohol from the aqueous alcohol solution and using the alcohol in the carbamate-forming reaction apparatus.2. A carbamate production system comprising:a urea production ...

A REACTOR FOR OXIDATION OF AMMONIA IN THE PRODUCTION OF NITRIC ACID

A method for the production of nitric acid, comprising a step of oxidation of ammonia in the presence of a catalyst, comprising a step of monitoring the temperature of said catalyst by at least one contactless infrared sensor. 1. A method for the production of nitric acid , comprising a step of oxidation of ammonia in the presence of a catalyst , characterized by comprising a step of monitoring the temperature of said catalyst by at least one contactless infrared sensor.2. The method according to claim 1 , wherein said catalyst is a platinum catalyst or a platinum-rhodium catalyst claim 1 , and said catalyst being preferably the form of a gauze.3. The method according to claim 1 , wherein:said sensor is positioned away from the catalyst and the method comprising the step of switching said sensor between at least a first position wherein the sensor points a first region of the catalyst, and a second position wherein the sensor points a second region of the catalyst, so that the sensor can selectively detect the temperature of said first region and second region of catalyst.4. The method according to claim 1 , comprising the use of a plurality of infrared sensors to monitor the temperature of said catalyst.5. The method according to wherein: an alarm signal is generated when the temperature difference between different regions of catalyst exceeds a predetermined alarm threshold.6. The method according to claim 1 , wherein said step of oxidation is carried out with a ratio of ammonia to an oxidant which is continuously adjusted as a function of the temperature of the catalyst detected by said at least one contactless infrared sensor.7. The reactor for catalytic oxidation of ammonia claim 1 , particularly for subsequent production of nitric acid claim 1 , comprising a pressure vessel and a catalytic basket claim 1 , said catalytic basket containing a catalyst suitable for oxidation of ammonia claim 1 , characterized by comprising at least one infrared sensor arranged to ...

SYSTEM FOR MANUFACTURING FUMED SILICA PARTICLES

The present disclosure provides a system for generating fumed silica particles for manufacturing of an optical fiber preform. The system includes a generator and a plurality of inlets connected with the generator. The generator includes a plurality of burners. The plurality of inlets include a first inlet, a second inlet, a third inlet and a fourth inlet. The first inlet provides passage for flow of a precursor material to the generator. The second inlet provides passage for flow of a first gas to the generator. The third inlet provides passage for flow of a second gas to the generator. The fourth inlet provides passage for flow of a carrier gas to the generator. The plurality of burners enables a chemical reaction between the precursor material, the first gas and the second gas that facilitates the generation of the fumed silica particles. 1. A method for generating fumed silica particles for use in manufacturing an optical fiber preform , the method comprising:receiving a precursor material along with one or more combustion gases, wherein the precursor material along with the make up oxygen is received in the generator;receiving a first gas in the generator;receiving a second gas in the generator;receiving a carrier gas in the generator; andraising the temperature inside the generator to enable a chemical reaction between the precursor material, the first gas and the second gas, wherein the chemical reaction between the precursor material, the first gas and the second gas generates the fumed silica particles of per predefined size.2. The method as recited in claim 1 , wherein the precursor material is at least one of silicon tetrachloride (SiCl) or octamethylcyclotetrasiloxan (OMCTS).3. The method as recited in claim 1 , wherein the first gas is oxygen.4. The method as recited in claim 1 , wherein the second gas is methane CHwhen the precursor material is octamethylcyclotetrasiloxan (OMCTS).5. The method as recited in claim 1 , wherein the combustion gas is make ...

APPARATUS FOR CONVERTING A FEED GAS INTO A PRODUCT GAS

Apparatus for converting feed gas () into a product gas (), comprising at least one reactor () with a reaction chamber () bounded by the inner wall of an outer tube () closed at a first outer end and an inner tube () received coaxially in this outer tube () and provided at both its outer ends with openings, which reactor () is provided with an inlet chamber () and with an outlet chamber (), wherein a first wall () of the outlet chamber () encloses the outer tube () and extends therefrom, and a second wall () of the outlet chamber () lying opposite the first wall () encloses the outer tube () and extends therefrom, and the inlet chamber () is bounded by the second wall () of the outlet chamber () and a third wall () which lies opposite this second wall (), encloses the outer tube () and extends therefrom. 1. An apparatus for converting a feed gas having components for reaction into a product gas , the apparatus comprising:at least one reactor with a reaction chamber which is provided with an inlet opening for feed gas and an outlet opening for product gas and which is bounded by the inner wall of an outer tube closed at a first outer end and the outer wall of an inner tube received coaxially in this outer tube and provided at both its outer ends with openings, which reactor is provided with an inlet chamber which is in open connection with the at least one inlet opening and with an outlet chamber in which the at least one outlet opening debouches, wherein a first wall of the outlet chamber encloses the outer tube and extends therefrom;a second wall of the outlet chamber lying opposite the first wall encloses the outer tube and extends therefrom, whereinthe inlet chamber is bounded by the second wall of the outlet chamber and a third wall which lies opposite this second wall, encloses the outer tube and extends therefrom, wherein the inlet opening is formed in the wall of the outer tube.2. The apparatus as claimed in claim 1 , wherein the outer tube is closed at a ...

ISOBARIC PRESSURE EXCHANGER IN AMINE GAS PROCESSING

A system includes an amine gas processing system that includes a contactor configured to remove an acid gas from an untreated natural gas using an amine in a lean amine stream, output a treated natural gas, and output a rich amine stream. The system also includes a regenerator configured to regenerate the amine in the rich amine stream, output the lean amine stream, and output the acid gas. The system also includes an isobaric pressure exchanger (IPX) configured to transfer the rich amine stream from the contactor to the regenerator and to transfer the lean amine stream from the regenerator to the contactor. 1. A system , comprising: a contactor configured to remove an acid gas from an untreated natural gas using an amine in a lean amine stream, output a treated natural gas, and output a rich amine stream;', 'a regenerator configured to regenerate the amine in the rich amine stream, output the lean amine stream, and output the acid gas; and', 'an isobaric pressure exchanger (IPX) configured to transfer the rich amine stream from the contactor to the regenerator and to transfer the lean amine stream from the regenerator to the contactor., 'an amine gas processing system, comprising2. The system of claim 1 , wherein the IPX comprises at least one of a rotary IPX claim 1 , a non-rotary IPX claim 1 , a reciprocating IPX claim 1 , or a bladder-based IPX claim 1 , or any combination thereof3. The system of claim 1 , wherein the IPX is configured to transfer pressure from the rich amine stream entering the IPX at a first pressure to the lean amine stream leaving the IPX at a second pressure claim 1 , wherein the first pressure is greater than the second pressure.4. The system of claim 1 , wherein an outer housing of the IPX comprises duplex stainless steel.5. The system of claim 1 , wherein the IPX comprises at least one of flanged connectors claim 1 , or threaded connectors claim 1 , or any combination thereof6. The system of claim 1 , wherein the IPX comprises an ...

REACTION SYSTEM AND PROCESS TO PRODUCE FLUORINATED ORGANICS

The invention relates to the use of a liquid-vapor separator such as a de-entrainer to remove an unvaporized portion of a feed, e.g. 1,1,2,3-tetrachloropropene (1230xa), to a catalytic vapor phase fluorination reaction where e.g. 2-chloro-3,3,3,-trifluoropropene (1233xf) is produced. The invention extends the life of the catalyst. 1. A reactor system comprising:a vaporizer;a de-entrainer in fluid communication with said vaporizer, the de-entrainer having a vapor outlet; anda vapor phase reactor in fluid communication with the vapor outlet of the de-entrainer.2. The reactor system of wherein the de-entrainer is a tower claim 1 , a knock out pot claim 1 , a filter claim 1 , or combinations thereof.3. The reactor system of wherein the tower is a packed tower claim 1 , a trayed tower claim 1 , or combinations thereof.4. The reactor system of wherein the de-entrainer further comprises a liquid outlet.5. The reactor system of wherein the knock-out pot further comprises an internal coalescer.6. The reactor system of wherein the internal coalescer comprises packing claim 5 , mesh claim 5 , or combinations thereof.7. The reactor system of wherein the packing comprises Pall rings and the like.8. The reactor system of wherein the de-entrainer comprises a packed tower.9. The reactor system of wherein the packed tower comprises random packing claim 8 , structured packing claim 8 , vane assemblies claim 8 , demisters claim 8 , or combinations thereof.10. A process to prepare 2-chloro-3 claim 8 ,3 claim 8 ,3 claim 8 ,-trifluoropropene (1233xf) comprising:a) providing a starting material comprising liquid 1,1,2,3-tetrachloropropene (1230xa) and vaporous 1230xa;b) separating the vaporous 1230xa from the liquid 1230xa; andc) contacting the vaporous 1230xa with hydrogen fluoride HF under conditions effective to form 1233xf.11. The process of wherein the conditions effective include the presence of a fluorination catalyst.12. The process of wherein the fluorination catalyst is selected ...

LIQUID POLYMER ACTIVATION UNIT WITH IMPROVED HYDRATION CHAMBER

A polymer activation assembly is provided for separating monomer from the oil in which it is suspended in a polymer forming suspension and mixing the monomer with water supplied from another stream. The supply water is supplied through a primary fluid channel extending through the activation assembly and which transitions to a relatively wide rectangular activation channel. A secondary fluid inlet is formed in a side of the activation assembly for injection of the polymer forming suspension therein. A nozzle section of the secondary fluid inlet is formed between an initial section of the inlet and the activation channel. The nozzle section is generally rectangular in cross section and relatively shallow. The distal end of the nozzle section has a width that approximates the width of the activation channel. The nozzle section angles at an acute angle toward the outlet. 1. A polymer activation assembly comprising:a primary fluid channel extending through said polymer activation assembly along a first axis, the primary fluid channel having a primary fluid channel inlet, a primary fluid channel outlet and an activation portion therebetween wherein said activation portion of said primary fluid activation channel is wider than it is deep;a secondary fluid channel having a secondary fluid channel inlet connecting to a nozzle section which intersects the activation portion of the primary fluid channel at an acute angle and which is wider than it is deep.2. The polymer activation assembly as in wherein said activation portion of said primary fluid activation channel is rectangular in cross-section.3. The polymer activation assembly as in wherein a surface of the polymer activation assembly defining said activation portion of said primary fluid activation channel opposite said nozzle is generally planar.4. The polymer activation assembly as in wherein said nozzle section is rectangular in cross-section.5. The polymer activation assembly as in wherein a distal end of said ...

Reactor for a cracking furnace

The invention relates to a reactor for cracking hydrocarbons wherein the reactor has inner wall; characterized in that the inner wall comprises a plurality of concave dimples embedded in a surface of said inner wall.

DEVICE FOR MANUFACTURING POLYSILICON USING HORIZONTAL REACTOR AND METHOD FOR MANUFACTURING SAME

The present invention relates to a polysilicon production apparatus. The apparatus includes: a horizontal reaction tube positioned in an insulated tube and having an inlet port through which gaseous raw materials including silicon-containing reactant gases and a reducing gas are supplied, an outlet port through which residual gases exit, a reaction surface with which the gaseous raw materials come into contact, and a plurality of bottom openings through which molten polysilicon produced by the reactions of the gaseous raw materials is discharged; one or more internal structures placed in the horizontal reaction tube to provide additional reaction surfaces; and first heating means adapted to heat the reaction surface of the horizontal reaction tube. The present invention also relates to a method for the production of polysilicon using the apparatus. 1. A polysilicon production apparatus comprising: a horizontal reaction tube positioned in an insulated tube and having an inlet port through which gaseous raw materials comprising silicon-containing reactant gases and a reducing gas are supplied , an outlet port through which residual gases exit , a reaction surface with which the gaseous raw materials come into contact , and a plurality of bottom openings through which molten polysilicon produced by the reactions of the gaseous raw materials is discharged; one or more internal structures placed in the horizontal reaction tube to provide additional reaction surfaces; and first heating means adapted to heat the reaction surface of the horizontal reaction tube.2. The polysilicon production apparatus according to claim 1 , further comprising second heating means adapted to heat the internal structures placed in the horizontal reaction tube.3. The polysilicon production apparatus according to claim 1 , further comprising a container adapted to collect the molten polysilicon discharged through the bottom openings of the horizontal reaction tube.4. The polysilicon production ...

APPARATUS AND METHODS FOR PRODUCING CHLORINE DIOXIDE

Chlorine dioxide (ClO) is produced by apparatus and methods wherein a ClOgas produced in the apparatus is quickly introduced into a fluid stream to be treated with said gas. To this end, the apparatus has an interior chemical reaction chamber which houses an internal fluid flow tube having a fluid impervious upper section and a porous lower section that respectively define two zones within the interior chemical reaction chamber. 1. An apparatus for producing chlorine dioxide , said apparatus comprising: (a) an upper mixing and/or reaction zone for carrying out a first mixing/chemical reaction operation,', '(b) a lower distribution and reaction zone for carrying out a chlorine dioxide gas producing chemical reaction,', '(c) a first chemical precursor entry port that leads into an internal fluid flow tube housed in the chemical reactor,', '(d) a second chemical precursor entry port that leads into the upper mixing and/or reaction zone,', '(e) a third chemical precursor entry port that also leads into the upper mixing and/or reaction zone, and', '(f) an exit port for discharging fluid from the lower distribution and reaction zone into a fluid flow device;, '(1) a chemical reactor having(2) an internal fluid flow tube having a fluid impervious upper section and a fluid porous lower section, said tube serving to: (a) receive a first chemical precursor, (b) transport that first chemical precursor through the fluid impervious upper section of the internal fluid flow tube and (c) deliver the first chemical precursor into the porous lower section of said internal fluid flow tube whereupon said first chemical precursor is forced through a porous wall region of the porous lower section and into the lower distribution and reaction zone; and(3) a fluid flow device that conducts a portion of a fluid passing through said device into and out of the exit port of the chemical reactor in a manner such that any chlorine dioxide gas produced in the lower distribution and reaction zone ...

SYSTEM AND METHOD FOR PREPARING LIQUID FUELS

Techniques, methods and systems for preparation liquid fuels from hydrocarbon and carbon dioxide are disclosed. The present invention can transform hydrocarbon and carbon dioxide generated from organic feed stocks or other industrial emissions into renewable engineered liquid fuels and store them in a cost-efficient way. The method of the present invention includes: supplying hydrocarbon and carbon dioxide to a heated area of a reaction chamber in controlled volumes; forming carbon monoxide by the energy provided by the heated area; transporting carbon monoxide and hydrogen to a reactor in controlled volumes; supplying additional hydrogen to the reactor; regulating the pressure in the reactor by adjusting the controlled volumes in order to achieve a predetermined object; forming the liquid fuel in the reactor according to the predetermined object; and, storing the liquid fuel in a storage device. 1. A system for preparing a liquid fuel , the system comprising:a reaction chamber;a heated area, located in the reaction chamber, receiving a hydrocarbon in a first controlled volume, and receiving a carbon dioxide in a second controlled volume, wherein the hydrocarbon and the carbon dioxide form a carbon monoxide and a hydrogen by an energy provided by the heated area;a reactor, receiving the carbon monoxide in a third controlled volume, receiving the hydrogen in a fourth controlled volume, and selectively receiving an additional hydrogen in a fifth controlled volume, wherein the reactor forms the liquid fuel from the carbon monoxide and the hydrogen according to a predetermined objecta regulating device, regulating a pressure in the reactor by adjusting the controlled volumes to achieve the predetermined object; anda storage device, storing the liquid fuel.2. The system of claim 1 , wherein the predetermined object includes at least one of a maximum production of the liquid fuel claim 1 , a minimum energy input to the reaction chamber claim 1 , and a longest use duration ...

Radial Flow Process and Apparatus

A flow connector creates a fluid connection between a port in a wall of a reactor vessel and an axial flow path of the reactor vessel. The flow connector has a wall defining a flow path of the flow connector. The flow path terminates in a first end opening and a second end opening. The first end opening is configured to connect to the axial flow path of the reactor vessel, and the second end opening is configured to connect to the port in a wall of the reactor. The flow connector includes a passageway extending through the wall of the flow connector to provide access to the flow path of the flow connector. A cover is dimensioned for sealing the passageway. The passageway may be dimensioned such that a person may traverse the passageway to access the flow path of the flow connector. 1. An apparatus for creating a fluid connection between a port in a wall of a reactor vessel and an axial flow path of the reactor vessel , the apparatus comprising:a flow connector having a wall defining a flow path of the flow connector, the flow path terminating in a first end opening and a second end opening, the first end opening configured to connect to the axial flow path of the reactor vessel, the second end opening configured to connect to the port in a wall of the reactor, the flow connector including a passageway extending through the wall of the flow connector to provide access to the flow path of the flow connector; anda cover dimensioned for sealing the passageway.2. The apparatus of claim 1 , wherein the passageway is dimensioned such that a person may traverse the passageway to access the flow path of the flow connector.3. The apparatus of claim 1 , wherein a first axis of the first end opening and a second axis of the second end opening are substantially perpendicular.4. The apparatus of claim 1 , wherein the first end opening and the passageway are substantially coaxial.5. The apparatus of claim 1 , wherein the flow connector further comprises an interior flange for ...

Ceramic oxygen transport membrane array reactor and reforming method

A commercially viable modular ceramic oxygen transport membrane reforming reactor for producing a synthesis gas that improves the thermal coupling of reactively-driven oxygen transport membrane tubes and catalyst reforming tubes required to efficiently and effectively produce synthesis gas.

REACTOR

An end surface of each first side wall, an end surface of each first middle wall, and an end surface of each first end wall are joined to an adjacent second structure by diffusion bonding, an end surface of each second side wall, an end surface of each second middle wall, and an end surface of each second end wall are joined to an adjacent first structure or a lid structure by diffusion bonding, a thickness of each first side wall is greater than or equal to a thickness of each first middle wall, and a thickness of each second side wall is greater than or equal to a thickness of each second middle wall. 1. A reactor for causing a reaction of a first fluid by a heat exchange between the first fluid and a second fluid to generate a product , the reactor comprising:a plurality of first structures each including: first side walls provided on both sides in a first direction on one surface of a first base plate and extending in a second direction perpendicular to the first direction; a plurality of first middle walls arranged at intervals in the first direction between the paired first side walls on the one surface of the first base plate and extending in the second direction; and first flow channels provided between each first side wall and the adjacent first middle wall and between the respective first middle walls adjacent to each other so that the first fluid flows therethrough;a plurality of second structures coexisting with and stacked on the plural first structures in a third direction perpendicular to the first direction and the second direction, the second structures each including: second side walls provided on both sides in the first direction on one surface of a second base plate and extending in the second direction; a plurality of second middle walls arranged at intervals in the first direction between the paired second side walls on the one surface of the second base plate and extending in the second direction; and second flow channels provided between each ...

REACTOR

A reactor includes: a main reactor core including main reaction flow channels through which the raw material fluid flows, and main temperature control flow channels through which the heat medium flows along a flow direction of the raw material fluid flowing in the main reaction flow channel; and a pre-reactor core including pre-reaction flow channels of which an outlet side connects with an inlet side of the main reaction flow channels and through which the raw material fluid flows, and pre-temperature control flow channels of which an inlet side connects with an outlet side of the main reaction flow channels and through which the product serving as the heat medium flows along a flow direction of the raw material fluid flowing in the pre-reaction flow channel. 1. A reactor for causing a reaction of a raw material fluid by a heat exchange between the raw material fluid and a heat medium to generate a product , the reactor comprising:a main reactor core including a main reaction flow channel through which the raw material fluid flows, and a main temperature control flow channel through which the heat medium flows along a flow direction of the raw material fluid flowing in the main reaction flow channel; anda pre-reactor core including a pre-reaction flow channel of which an outlet side connects with an inlet side of the main reaction flow channel and through which the raw material fluid flows, and a pre-temperature control flow channel of which an inlet side connects with an outlet side of the main reaction flow channel and through which the product serving as the heat medium flows along a flow direction of the raw material fluid flowing in the pre-reaction flow channel.2. The reactor according to claim 1 , further comprising a connection member connecting the outlet side of the pre-reaction flow channel and the inlet side of the main reaction flow channel.3. The reactor according to claim 1 , further comprising a connection member connecting the outlet side of the ...

Gas Processing Device and Method

A methane conversion device comprises a reaction chamber; a sensor for detecting the presence of methane; blowing means for directing external gasses Into the reaction chamber when the sensor detects the presence of methane above a predetermined threshold; conversion means that are configured to oxidise methane; and positioning means for positioning the device on an animal. 1. A methane conversion device comprising:a reaction chamber comprising conversion means that are configured to oxidise methane;a methane retention component;means for causing methane to be released from the methane retention component into the reaction chamber;a sensor that is adapted to detect the presence of methane within gas exterior to the methane conversion device;blowing means configured to drive gas from the exterior of the device onto the methane retention component when the sensor detects the presence of methane above a predetermined threshold; andpositioning means for positioning the device on an animal.2. A device according to claim 1 , wherein the methane retention component comprises a chamber containing a porous material that is configured to reversibly absorb methane.3. A device according to claim 2 , wherein the porous material is provided by a zeolite mineral.4. A device according to any one of the preceding claims claim 2 , wherein a carbon dioxide filter is provided between the blowing means and the methane retention component claim 2 , the carbon dioxide filter being configured to inhibit the passage of carbon dioxide to the methane retention component.5. A device according to any one of the preceding claims claim 2 , wherein the means for causing methane to be released from the methane retention component into the reaction chamber comprises a heating element.6. A methane conversion device comprising:A reaction chamber;A sensor that is adapted to detect the presence of methane within gas exterior to the methane conversion device;Blowing means configured to drive gas from the ...

Device and Method for Heat and Mass-Exchange between Gas and Liquid

A device for heat, mass, and chemical exchange and interaction between gases and liquids. Nozzles feed the gas at angles in different directions to form a gas-liquid mix, swirls, and/or foam above an array of such nozzles. 1. A device for mixing fluids , comprising:a substantially upward path for a first fluid;nozzles forming a substantially two-dimensional grid across the path for the first fluid to pass through the grid; anda means for injecting a second fluid into the path above the grid; to form within the path above the grid for each of the plurality of nozzles at least one jet of the first fluid;', 'for a plurality of the jets to interact to form within the path above the grid non-linear flow of the first fluid; and', 'for the non-linear flow of the first fluid to contact and interact within the path above the grid with the second fluid injected into the path., 'wherein a plurality of nozzles are shaped and positioned within the grid so as for the first fluid passing through the grid'}2. The device of claim 1 , whereinthe non-linear flow of the first fluid comprises at least one substantially upwardly flowing swirl.3. The device of claim 1 , for the first fluid passing through the grid to form within the path above the grid for each of the plurality of nozzles jets of the first fluid;', 'for a plurality of the jets from the plurality of nozzles to interact to form within the path above the grid non-linear flow of the first fluid; and', 'for the non-linear flow of the first fluid to contact and interact within the path above the grid with the second fluid injected into the path., 'wherein the plurality of nozzles are shaped and positioned within the grid so as'}4. The device of claim 3 , whereinthe non-linear flow of the first fluid comprises substantially upwardly flowing swirls.5. The device of claim 4 ,wherein the swirls are rotating in substantially same direction.6. The device of claim 1 , wherein the first fluid is gas.7. The device of claim 1 , wherein ...

APPARATUS AND PROCESS FOR THE CONTINUOUS REACTION OF LIQUIDS WITH GASES

The present invention relates to an apparatus of the loop Venturi reactor type for the continuous reaction of liquids with gases, in particular for hydrogenations, oxidations or acetylations, e.g. for the preparation of toluenediamine by hydrogenation of dinitrotoluene, and a process for the continuous reaction of liquid reactants with gaseous reactants in the apparatus. In the apparatus of the invention, the diversion of an internal circulatory flow in the reactor is effected by means of a diversion pan which is arranged underneath a heat exchanger. 1. An apparatus , comprising:a vertically elongated reactor in which there is a reaction space,at least one heat exchanger which is arranged within the reactor,at least one cooling inlet for introducing the cooling medium into the heat exchanger,{'b': '2', 'at least one cooling outlet for taking the cooling medium off from the heat exchanger (),'}at least one gaseous reactant inlet for introducing the gaseous reactant into the reaction space,at least one liquid reactant inlet for introducing the liquid reactant into the reaction space,at least one mixing chamber,at least one downward-directed driving jet nozzle for introducing the reaction medium, the outlet of which is arranged above the at least one mixing chamber and which is in fluid connection with the reaction space,at least one reaction medium outlet for taking the reaction medium off from the reactor, andat least one diverter arranged below the heat exchanger and below the mixing chamber for diverting the reaction medium flowing downward through the mixing chamber in such a way that the reaction medium once again flows upward through the heat exchanger,wherein the diverter is a diversion pan.2. The apparatus as claimed in claim 1 , wherein the heat exchanger comprises heat exchanger tubes.3. The apparatus as claimed in claim 1 , wherein the heat exchanger comprises heat exchanger tubes and a region surrounding the heat exchanger tubes is in fluid connection with ...

PROCESS FOR CONVERTING ALKANES TO OLEFINS

A process and apparatus for converting an alkane to an olefin. In one embodiment, the process involves oxidative coupling of an alkane, e.g., methane, with an oxidant, such as air, to produce an olefin having twice the number of carbon atoms as the alkane, e.g., ethylene. In another embodiment, the process involves oxidative dehydrogenation of an alkane, e.g., ethane, with an oxidant to form an olefin having the same number of carbon atoms as the alkane, e.g., ethylene. The process involves passing a flow of the oxidant from a first flow passage through a porous medium; diffusing a flow of the alkane from a second flow passage into the porous medium; and contacting the reactant alkane and the oxidant in the presence of a catalyst within the porous medium to produce the olefin. 117-. (canceled)18. A chemical reactor comprising:(a) a first chamber comprising a first inlet and a first flow passage;(b) a second chamber comprising a second inlet and a second flow passage;(c) a porous medium which separates the first flow passage from the second flow passage, the porous medium having an oxidative coupling catalyst or oxidative dehydrogenation catalyst supported therein, wherein the catalyst infills from 40 to 60 percent of a thickness of the porous medium measuring from a side of the porous medium adjacent the second flow passage to a side adjacent the first flow passage; and(d) an outlet from the second chamber.19. (canceled)20. A chemical reactor comprising a non-porous housing having disposed therein a plurality of tubular porous media , such that:(a) in the plurality of tubular porous media, each tubular porous medium provides for a first chamber defining a first flow passage;(b) a plenum bounded by the non-porous housing and the plurality of tubular porous media defines a second chamber providing a second flow passage;(c) each tubular porous medium further comprises a plurality of pores or channels connecting the first flow passage therein to the second flow passage ...

Liquid fuel cpox reformers and methods of cpox reforming

A liquid fuel catalytic partial oxidation (CPOX) reformer can include a plurality or an array of spaced-apart CPOX reactor units, each reactor unit including an elongate tube having a gas-permeable wall with internal and external surfaces, the wall enclosing an open gaseous flow passageway with at least a portion of the wall having CPOX catalyst disposed therein and/or comprising its structure. The catalyst-containing wall structure and open gaseous flow passageway enclosed thereby define a gaseous phase CPOX reaction zone, the catalyst-containing wall section being gas-permeable to allow gaseous CPOX reaction mixture to diffuse therein and hydrogen rich product reformate to diffuse therefrom. At least the exterior surface of the CPOX reaction zone can include a hydrogen barrier. The liquid fuel CPOX reformer can include a vaporizer, one or more igniters, and a source of liquid reformable fuel.

CONVERSION OF GREENHOUSE GASES BY DRY REFORMING

A method for conversion of greenhouse gases comprises: introducing a flow of a dehumidified gaseous source of carbon dioxide into a reaction vessel; introducing a flow of a dehumidified gaseous source of methane into the reaction vessel; and irradiating catalytic material in the reaction vessel with microwave energy. The irradiated catalytic material is heated and catalyzes an endothermic reaction of carbon dioxide and methane that produces hydrogen and carbon monoxide. At least a portion of heat required to maintain a temperature within the reaction vessel is supplied by the microwave energy. A mixture that includes carbon monoxide and hydrogen can undergo catalyzed reactions producing multiple-carbon reaction products in a lower-temperature portion of the reaction vessel. 1. A method for simultaneously consuming carbon dioxide and generating one or more multiple-carbon reaction products in a single reaction vessel , the method comprising:(a) introducing a flow of a dehumidified gaseous source of carbon dioxide into a higher-temperature portion of a reaction vessel;(b) introducing a flow of a dehumidified gaseous source of methane into the higher-temperature portion of the reaction vessel;(c) irradiating first catalytic material in the higher-temperature portion of the reaction vessel with microwave energy so as to heat the first catalytic material and drive an endothermic reaction of the carbon dioxide and the methane, catalyzed by the first catalytic material, that produces hydrogen and carbon monoxide;(d) cooling a lower-temperature portion of the reaction vessel, thereby establishing a temperature gradient within the reaction vessel wherein the irradiated, higher-temperature portion of the reaction vessel exhibits a higher temperature than the cooled, lower-temperature portion of the reaction vessel, wherein at least a portion of heat required to maintain the temperature gradient is supplied by the microwave energy irradiating the first catalytic material in ...

Atomization and Pyrolysis of Resid Cracking Feed

A method and apparatus for conversion of petroleum resid fluid through atomization and pyrolysis, including: generating a stream of atomized resid fluid; and delivering the stream to a plurality of cracking particles, wherein the cracking particles have a temperature from 700° C. to 1200° C. when the stream is delivered. Generating the stream of atomized resid fluid may include: delivering heated resid fluid to a nozzle; and delivering diluent fluid to the nozzle. A method and apparatus includes: a first multi-phase fluid application device configured to generate a first stream of atomized resid fluid; a port configured to guide a plurality of cracking particles to intersect the first stream; and a particle heating component configured to heat the cracking particles before the particles intersect the first stream. 1. A method comprising:delivering heated resid fluid to a nozzle, and also delivering diluent fluid to the nozzle;generating a stream of heated atomized resid fluid through the nozzle, which is a two-phase nozzle, a three-phase nozzle, or a capillary nozzle; and{'b': '225', 'delivering the stream to a plurality of cracking particles having a diameter of from 40 μm to 400 μm, wherein the cracking particles have a temperature from 700° C. to 1200° C. when the stream is delivered.'}2. The method of claim 1 , wherein the nozzle has a temperature of from 700° C. to 1000° C. while the heated resid fluid and the diluent fluid are delivered to the nozzle.3. The method of claim 1 , wherein the heated resid fluid has a temperature of from 50° C. to 300° C. when delivered to the nozzle.4. The method of claim 1 , wherein the heated resid fluid comprises asphaltene or ash content from 500 ppm to 30 wt %.5. The method of claim 1 , wherein the heated resid fluid comprises hydrocarbons having a Conradson carbon residue from 1% to 20%.6. The method of claim 1 , wherein the cracking particles move translationally relative to the nozzle while the stream is delivered to the ...

APPARATUS FOR SYNTHETISING TIN DIOXIDE NANOPARTICLES AND METHOD FOR PRODUCING TIN DIOXIDE NANOPARTICLES

The following invention relates to a novel and efficient nanoparticles synthesis reactor and process production. More particularly, the present invention is applied to the synthesis of nanostructured tin dioxide. The benefits provided by the invention can be seen in various gaseous reactions where occurs the formation of solid and gaseous phases. 1. A nanoparticles synthesis reactor comprising:a tubular section provided with an inlet, a gas distributor, which has a circular shape provided with an inlet, baffles and orifices;said tubular section is provided with a tubular region of reaction, a powder collector which has an outlet;wherein the orifices provide the perpendicular interaction among the reagents flows; {'br': None, 'i': A', 'B', 'C', 'D, '(g)+(g)→(s)+(g).'}, 'wherein the baffles provide means for the optimization of the gas flow around the reactor where the reagents flow, so that the following reaction will occur2. The reactor according to claim 1 , characterized as being used for the tin dioxide nanoparticles synthesis (SnO) using water vapor.3. The reactor according to claim 1 , characterized by the fact that A(g)=SnCl(g); B(g)=HO; C(s)=SnO(s); D(g)=HCl(g).4. The reactor according to claim 2 , characterized as being capable of maintaining the reaction temperature approximately 200° C.5. The reactor according to claim 1 , characterized by the fact that it provides the particle size reduction of the synthesized solids claim 1 , optimizing reaction conversion; temperature and/or reaction time.6. A tin dioxide nanoparticle production process comprising the following steps:(i) providing a distributor with water vapor through an inlet;(ii) optimizing water vapor flow through baffles;(iii) distributing the water vapor flow, uniformly, through orifices around a tubular section where tin tetrachloride gas flows.(iv) providing a tubular section with tin tetrachloride gas through an the inlet;(v) providing a perpendicular interaction between the tin tetrachloride ...

LIQUID FUEL REFORMER INCLUDING A VAPORIZER AND METHOD OF REFORMING LIQUID REFORMABLE FUEL

A liquid fuel reformer includes a fuel vaporizer which utilizes heat from an upstream source of heat, specifically, an electric heater, operable in the start-up mode of the reformer, and therefore independent of the reforming reaction zone of the reformer, to vaporize fuel in a downstream vaporization zone. 118-. (canceled)19. A method of reforming a liquid reformable fuel , the method comprising:introducing an oxygen-containing gas into a conduit for routing fluids toward an inlet of a reformer;heating a stream of the oxygen-containing gas with at least one of a first source of heat comprising an electric heater disposed in the conduit and a second source of heat disposed in the conduit comprising heat of exotherm from the liquid fuel reformer and/or a hydrogen reformate-consuming device external to the liquid fuel reformer to provide a stream of heated oxygen-containing gas;introducing into the stream of heated oxygen-containing gas through or proximate to a vaporizer a liquid reformable fuel to provide a heated gaseous reforming reaction mixture; andreforming the heated gaseous reforming reaction mixture to produce a hydrogen-rich reformate.20. The method of claim 19 , comprising:heating the stream of the oxygen-containing gas and/or the stream of heated oxygen-containing gas with a third source of heat comprising an electric heater disposed in the conduit downstream from the first and second sources of heat and upstream from the vaporizer.21. The method of claim 20 , comprising:discontinuing heating the stream of oxygen-containing gas with the first source of heat; andheating the stream of oxygen-containing gas with the second and third sources of heat.22. The method of comprising adjusting the heat supplied by the second source and/or third source of heat.23. The method of claim 19 , comprising heating the liquid reformable fuel using the second source of heat and/or the third source of heat claim 19 , when present claim 19 , prior to introducing the liquid ...

APPARATUS FOR DECREASING SMR TUBE TEMPERATURE

An apparatus for decreasing steam methane reformer (SMR) tube temperature is provided. The apparatus can include an SMR furnace, a monitoring system in communication with the SMR furnace and a water source in fluid communication with the SMR furnace. The SMR furnace includes a plurality of SMR tubes disposed within the SMR furnace. The monitoring system is configured to monitor the temperature of at least a plurality of SMR tubes and compare the temperature against a first predetermined value, and the water source is configured to introduce water to an SMR tube that has a temperature above the first predetermined value, such that the temperature of the SMR tube is reduced. 1. An apparatus for decreasing steam methane reformer (SMR) tube temperature , the apparatus comprising:an SMR furnace effective for converting a hydrocarbon feed and steam into hydrogen and carbon monoxide under conditions effective for steam reforming;SMR tubes disposed within the SMR furnace, each SMR tube having a feed inlet, a mixing zone, and a reaction zone, the feed inlet configured to receive the hydrocarbon feed, the mixing zone configured to mix the hydrocarbon feed with water, the reaction zone containing a reforming catalyst configured to reform the hydrocarbon feed into hydrogen and carbon monoxide;a monitoring system in communication with at least a plurality of the SMR tubes, wherein the monitoring system is configured to monitor a temperature of at least a plurality of SMR tubes and compare the temperature against a first predetermined value; anda water source containing the water and configured to be in fluid communication with at least a plurality of the SMR tubes, such that the water source is configured to introduce the water to an SMR tube that has a temperature above the first predetermined value.2. The apparatus as claimed in claim 1 , further comprising a header disposed within the SMR furnace and in fluid communication with the water source and at least a portion of the ...

HEAT INTEGRATED REFORMER WITH CATALYTIC COMBUSTION FOR HYDROGEN PRODUCTION

An apparatus for the production of hydrogen from a fuel source includes a combustor configured to receive a combustor fuel and convert the combustor fuel into a combustor heat; a reformer disposed annularly about the combustor, a removable structured catalyst support disposed within the gap and coated with a catalyst to induce combustor fuel combustion reactions that convert the combustor fuel to the combustor heat, and a combustor fuel injection aperture configured for mixing combustion fuel into the combustion catalyst. The combustor fuel injection aperture being disposed along a length of the combustion zone. The reformer and the combustor define a gap therebetween and the reformer is configured to receive the combustor heat. 1. An apparatus for the production of hydrogen from a fuel source , comprising:a combustor configured to receive a combustor fuel and convert the combustor fuel into combustor heat;a reformer disposed annularly about the combustor, wherein the reformer and the combustor define a gap therebetween and the reformer is configured to receive the combustor heat;a removable structured catalyst support disposed within the gap and coated with a catalyst to induce combustor fuel combustion reactions that convert the combustor fuel to the combustor heat, the structured catalyst support being in contact with the combustor and the reformer, forming heat exchange zones where heat is transferred between a feed of the combustor and products of the reformer, and between a feed of the reformer and products of the combustor; anda combustor fuel injection aperture configured for mixing combustion fuel into the combustion catalyst, the combustor fuel injection aperture being disposed along a length of the combustion zone.2. The apparatus of claim 1 , wherein the combustor fuel injection aperture includes an annular ring including injector holes along a perimeter of the annular ring.3. The apparatus of claim 2 , wherein the reformer is configured to receive at ...

MIXING REACTOR FOR HETEROGENEOUS FLUIDS USING HIGH-SPEED EJECTING

A mixing reactor for heterogeneous fluids includes a first inlet part for introducing a first fluid, a first nozzle to eject the first fluid, a fluid chamber having a first space portion and a second space portion having a larger inner diameter than that of the first space portion, a second inlet part for introducing a second fluid, a second nozzle to eject the second fluid, a mixing chamber, and a third nozzle part to eject the second fluid. In the mixing reactor for heterogeneous fluids, two or more fluids are effectively collided with each other to enhance mixing uniformity, reduce side reactions, and thus improve reaction yield and reaction rate, and allow for simple maintenance and reuse. 1. A mixing reactor for heterogeneous fluids using high-speed ejecting , comprising:a first inlet part to which a first fluid is introduced from an outside;a first nozzle coaxially connected to a downstream side of the first inlet part to eject the first fluid;a fluid chamber formed to be coaxially spaced apart from the first nozzle and configured to have a first space portion and a second space portion having a larger inner diameter than that of the first space portion;a second inlet part radially connected to an outer circumferential surface of the fluid chamber and to which a second fluid is introduced from an outside;a second nozzle coaxially connected to a downstream side of the first space portion to eject the second fluid;a mixing chamber formed to be coaxially spaced apart from an inner circumferential surface of the second space portion and coaxially connected to downstream sides of the first nozzle and the second nozzle; anda third nozzle part configured to extend from the inner circumferential surface of the second space portion and radially connected to an outer circumferential surface of the mixing chamber to eject the second fluid.2. The mixing reactor of claim 1 , wherein the mixing chamber comprises an expanded cross section portion and a constant cross section ...

Apparatus for steam-methane reforming

Apparatuses for use in plants for processing methane, the apparatuses comprising a plurality of reaction modules each including a plurality of Fischer-Tropsch reactors operable to convert a gaseous mixture including carbon monoxide and hydrogen to a liquid hydrocarbon. Each module may be disconnected and taken away for servicing while allowing the plant to continue to operate. In some of the apparatuses, each Fischer-Tropsch reactor comprises a plurality of metal sheets arranged as a stack to define first and second flow channels for flow of respective fluids, the channels being arranged alternately to ensure good thermal contact between the fluids in the channels.

METHOD AND SYSTEM FOR PRODUCING METHANOL USING AN INTEGRATED OXYGEN TRANSPORT MEMBRANE BASED REFORMING SYSTEM

A method and system for producing methanol that employs an integrated oxygen transport membrane based reforming system is disclosed. The integrated oxygen transport membrane based reforming system carries out a primary reforming process, a secondary reforming process, and synthesis gas conditioning to produce synthesis gas having a desired module of between about 2.0 and 2.2 for a methanol production process thereby optimizing the efficiency and productivity of the methanol plant. 120-. (canceled)21. A system for producing methanol using an oxygen transport membrane based reforming system comprising:an oxygen transport membrane based reforming system configured to reform a combined feed stream of natural gas and steam to produce a synthesis gas stream, wherein said system comprises at least one reforming reactor and at least one oxygen transport membrane reactor in close proximity to said at least one reforming reactor;a module management system configured to produce a supplemental hydrogen stream from a portion of the produced synthesis gas stream or a portion of a methanol purge stream or both, and wherein a portion of the supplemental hydrogen stream is combined with the produced synthesis gas stream to yield a modified synthesis gas product stream having a module between about 2.0 to 2.2;a methanol synthesis reactor configured to receive the modified synthesis gas product stream and produce crude methanol and the methanol purge stream; anda methanol purification system configured to purify the crude methanol.22. The system of wherein a portion of the supplemental hydrogen stream is combined with the hydrocarbon feed stream.23. The system of wherein the oxygen transport membrane reactor comprises one or more oxygen transport membrane tubes claim 21 , wherein said tubes are configured as multilayered dual phase ceramic tubes capable of conducting oxygen ions at an elevated operational temperature.24. The system of wherein said multilayered dual phase ceramic tubes ...

EXTENDED THERMAL STAGE SULFUR RECOVERY PROCESS

A process for recovering sulfur in a sulfur recovery unit comprising the steps of reacting hydrogen sulfide and oxygen in the reaction furnace at a minimum reaction temperature to produce a reaction effluent; reducing the temperature of the reaction effluent from the minimum reaction temperature to a boiler section outlet temperature to produce a cooled effluent, the cooled effluent comprises hydrogen sulfide, sulfur dioxide, and sulfur-containing contaminants; reacting the hydrogen sulfide, sulfur dioxide, and sulfur-containing contaminants in the catalytic extension to produce a boiler catalytic effluent; reducing the boiler catalytic effluent temperature such that the elemental sulfur condenses to form liquid sulfur and a gases stream; reacting the hydrogen sulfide and sulfur-containing contaminants with the oxygen to produce an oxidizer outlet stream comprises sulfur dioxide; and separating the sulfur dioxide in the scrubbing unit to produce a recycle stream and an effluent gases, the recycle stream comprises sulfur dioxide. 1. An apparatus for recovering sulfur from an acid gas stream , the apparatus comprising:a reaction furnace, the reaction furnace configured to contain a reaction between hydrogen sulfide in the acid gas stream and oxygen in an air feed to produce a reaction effluent, where the reaction furnace operates at a minimum reaction temperature, where the reaction effluent comprises elemental sulfur; a wasteheat stage, the wasteheat stage fluidly connected to the reaction furnace, the wasteheat stage configured to capture heat energy from a reaction effluent to produce a cooled effluent, where the cooled effluent is at a boiler section outlet temperature, and', 'a catalytic extension physically connected to the wasteheat stage, the catalytic extension configured to allow a reaction to convert sulfur compounds to produce a boiler catalytic effluent, where the boiler catalytic effluent comprises elemental sulfur, where the catalytic extension ...

PROCESS FOR MANUFACTURING TETRAFLUOROPROPENE

A process for manufacturing tetrafluoropropene, including, alternately: at least one step of reacting a chlorinated compound with hydrofluoric acid in the gas phase, in the presence of a fluorination catalyst, the proportion of oxygen optionally present being less than 0.05 mol. % relative to the chlorinated compound; a step of regenerating the fluorination catalyst by bringing the fluorination catalyst into contact with a regeneration stream including an oxidizing agent. Also, equipment suitable for carrying out this process. 1. A plant for the manufacture of tetrafluoropropene , comprising at least one gas-phase fluorination reactor comprising a bed of fluorination catalyst , said gas-phase fluorination reactor being configured in order to be fed alternately by:a system for feeding with reaction stream comprising a chlorinated compound and hydrofluoric acid, the proportion of oxygen optionally present in this reaction stream being less than 0.05 mol % with respect to the chlorinated compound; anda system for feeding with regeneration stream comprising an oxidizing agent.2. The plant as claimed in claim 1 , in which the reaction stream is essentially devoid of oxygen.3. The plant as claimed in claim 1 , in which the regeneration stream contains at least 1 mol % of oxygen with respect to the total regeneration stream.4. The plant as claimed in claim 1 , comprising a single reactor configured in order to be fed alternately by the system for feeding with reaction stream and the system for feeding with regeneration stream.5. The plant as claimed in claim 1 , comprising a plurality of reactors claim 1 , each being configured in order to be fed alternately by a system for feeding with reaction stream and a system for feeding with regeneration stream.6. The plant as claimed in claim 5 , configured so that claim 5 , when a reactor is fed by the system for feeding with reaction stream claim 5 , another reactor is fed by the system for feeding with regeneration stream.7. The ...

APPARATUS AND METHOD FOR PREPARING ETHYLENE AND/OR ACETYLENE USING HYDROCARBON

Equipment for producing ethylene and/or acetylene from hydrocarbons, including the reaction chamber (), burner (), common or separate fuel gas inlets () and oxygen inlets (), preheating tubes (), a gas distributor (), cracking gas inlets (), and a reaction product outlet (); the gas distributor (), which has multiple gas inlets and gas outlets, is arranged on the cross section of the reaction chamber (), where the gas inlet is connected to the cracking gas inlet (), and the gas outlet is connected to the preheating tube (). The cracking gas is uniformly distributed through the gas distributor () and passed through the preheating tubes (), which are hollow tubes; the opening at the other end of the hollow tube is close to or inserted into the combustion area of the gaseous fuel and oxygen. After preheating in the hollow tubes, the cracking gas is passed through the combustion area that contains gaseous fuel and oxygen. During the cracking reaction, the reaction product is distributed around the hollow tubes to pre-heat the cracking gas in the tubes. 1. An apparatus for producing ethylene and/or acetylene from hydrocarbon ,{'b': 13', '11', '12', '18', '14', '15', '16', '17, 'the apparatus comprising: a reaction chamber (), a burner (), common or separate gaseous fuel inlets () and oxygen inlets (), preheating tubes (), a gas distributor (), a cracking gas inlet (), and a reaction product outlet ();'}{'b': 13', '11', '12', '18', '16', '17', '14', '15, 'the reaction chamber () being a cavity structure, in which feedstock is reacted; the burner (), the gaseous fuel inlets (), the oxygen inlets (), the cracking gas inlets (), and the reaction product outlet () being set on the wall of the reaction chamber, and the preheating tubes () and the gas distributor () being arranged in the reaction chamber;'}{'b': 12', '13', '18', '13', '11', '17', '13', '16', '13, 'the gaseous fuel inlets () being used to feed gaseous fuel into the reaction chamber (); the oxygen inlets () being ...

Method and system of thermochemical regeneration to provide oxygenated fuel, for example, with fuel-cooled fuel injectors

The present disclosure is directed to integrated injector/igniters providing efficient injection, ignition, and complete combustion of various types of fuels. One example of such an injectors/igniter can include a body having a base portion opposite a nozzle portion. The base portion receives the fuel into the body and the nozzle portion can be positioned adjacent to the combustion chamber. The injector further includes a valve carried by the nozzle portion that is movable between a closed position and an open position to inject the fuel into the combustion chamber. An actuator is coupled the valve and extends longitudinally through the body towards the base portion, and a driver is carried by the body and is movable between a first position and a second position. Thermochemical regeneration of waste heat produced by combustion and associated combustion events is captured and invested in endothermic reactions to improve efficiency of the combustion event. Hydrogen characterized fuel may be used as a heat sink.

SEAL ASSEMBLY FOR CREATING A SEALED FLOW PATH BETWEEN FIRST AND SECOND FLUID DUCTS

A sealing assembly creating a sealed flow path between fluid ducts. The seal assembly comprises a housing and a tubular element within the housing providing a fluid conduit between the fluid ducts. Two sealing elements each have an internal sealing face sealably engaged with the tube and an external face for sealing, in use, with a respective fluid duct. At least one of the sealing elements is slidable with respect to the tubes. A support is slidably retained by the housing, surrounds one end of the tube and supports one of the slidable sealing elements on the side of the sealing element opposite to its external face. A resilient element within the housing biases the support so as to urge the two sealing elements apart. 1. A sealing assembly creating a sealed flow path between first and second fluid ducts , the sealing assembly having a first end facing the first fluid duct and a second end facing the second fluid duct;a housing;a tube within the housing providing a fluid conduit between the fluid ducts;a first sealing element at the first end having an internal sealing face slidably engaged with and slidable with respect to the tube and an external face for sealing, in use, with the first fluid duct;a second sealing element at the second end having an internal sealing face slidably engaged with and slidable with respect to the tube and an external face for sealing, in use, with the second fluid duct;a first support slidably retained by the housing and surrounding one end of the tube and supporting one of the first and second sealing elements on a side of the one of the first and second sealing elements opposite to its external face; anda resilient element within the housing biasing the support so as to urge the first and second sealing elements apart.2. The sealing assembly according to claim 1 , further comprising a second support surrounding an opposite end of the tube and supporting the other one of the first and second sealing elements on a side opposite to the ...

GAS DISTRIBUTOR NOZZLES

Systems and methods for injecting gas into a fluidized bed of particles are provided. The system can include a gas distribution system. The gas distribution system can include a header having a flow passage and a nozzle body coupled to the header. The nozzle body can have an inlet end in fluid communication with the flow passage and an outlet end positioned outside of the header. The nozzle body can have a longitudinal axis that is substantially perpendicular to a direction of flow through the flow passage. The nozzle body can have an orifice positioned between the inlet end and the outlet end. 1. A gas distribution system , comprising:a header having a flow passage; anda nozzle body coupled to the header, wherein the nozzle body has an inlet end in fluid communication with the flow passage and an outlet end positioned outside of the header, wherein the nozzle body has a longitudinal axis that is substantially perpendicular to a direction of flow through the flow passage; and wherein the nozzle body has an orifice positioned between the inlet end and the outlet end.2. The gas distribution system of claim 1 , wherein the inlet end defines an inlet orifice.3. The gas distribution system of claim 2 , wherein the orifice positioned between the inlet end and the outlet end is defined by a wall of the nozzle body.4. The gas distribution system of claim 1 , wherein the orifice positioned between the inlet end and the outlet end is positioned on a downstream side of the nozzle body.5. The gas distribution system of claim 1 , wherein the orifice positioned between the inlet end and the outlet end is positioned within the nozzle body.6. The gas distribution system of claim 5 , wherein a wall of the nozzle body tapers inward from the inlet end to the intermediate orifice.7. The gas distribution system of claim 5 , wherein the inlet end defines an inlet orifice.8. A method for distributing gas comprising:introducing a gas into a header having a flow passage;flowing the gas ...

LIQUID FUEL CPOX REFORMER AND FUEL CELL SYSTEMS, AND METHODS OF PRODUCING ELECTRICITY

Integrated liquid fuel catalytic partial oxidation (CPOX) reformer and fuel cell systems can include a plurality or an array of spaced-apart CPOX reactor units, each reactor unit including an elongate tube having a gas-permeable wall with internal and external surfaces, the wall enclosing an open gaseous flow passageway with at least a portion of the wall having CPOX catalyst disposed therein and/or comprising its structure. The catalyst-containing wall structure and open gaseous flow passageway enclosed thereby define a gaseous phase CPOX reaction zone, the catalyst-containing wall section being gas-permeable to allow gaseous CPOX reaction mixture to diffuse therein and hydrogen rich product reformate to diffuse therefrom. The liquid fuel CPOX reformer also can include a vaporizer, one or more igniters, and a source of liquid reformable fuel. The hydrogen-rich reformate can be converted to electricity within a fuel cell unit integrated with the liquid fuel CPOX reactor unit. 136-. (canceled)37. A reformer comprising:a) at least one partial oxidation reactor unit comprising an inlet for heated gaseous partial oxidation reaction mixture, a partial oxidation reaction zone wherein the heated partial oxidation reaction mixture undergoes partial oxidation reaction mixture to produce hydrogen gas-containing reformate and heat of exotherm, and an outlet for hydrogen gas-containing reformate; and,b) a conduit for separately receiving a flow of oxygen-containing gas, a flow of gaseous reformable fuel and/or a flow of vaporized gaseous reformable fuel, a heat transfer zone for transferring heat of exotherm from the partial oxidation reaction zone of the at least one partial oxidation reactor unit to the oxygen-containing gas flowing in the conduit thereby heating the oxygen-containing gas, a mixing zone for combining heated oxygen-containing gas with gaseous reformable fuel and/or vaporized gaseous reformable fuel flowing in the conduit to provide heated gaseous partial ...

TIN DIOXIDE NANOPARTICLES SYNTHESIS APPARATUS AND TIN DIOXIDE NANOPARTICLES PROCESS PRODUCTION

A new and efficient nanoparticles synthesis apparatus and process production. More particularly, an apparatus and process applied to the synthesis of nanostructured tin dioxide. The benefits provided by the apparatus and process are applied in various gaseous reactions where occurs the formation of solid and gaseous products. 1. A nanoparticle synthesis reactor comprising:a) a reactor inlet;b) a tubular section in which one of at least two reactants flows axially;c) a gas distributor surrounding the tubular section, the gas distributor comprising a distributor inlet, a circular shape, cylindrical baffles providing flow canals, and orifices surrounding the tubular section of the reactor; andd) a powder collector, {'br': None, 'sub': (g)', '(g)', '(s)', '(g), 'A+B→C+D.'}, 'wherein the gas distributor provides an optimized radial interaction among reactant flows through a curtain of at least one of the reactants, providing kinetic enhancement of the following reaction2. The reactor according to claim 1 , wherein:a first of the reactants flows axially through the tubular section; anda second of the reactants enters the gas distributor through the distributor inlet, wherein the second reactant is redirected by the canals provided by the cylindrical baffles and then flows through the orifices that surround the tubular section, meeting the first reactant flow radially, synthesizing nanoparticles.3. The reactor according to claim 1 , wherein:{'sub': (g)', '4(g), 'Ais SnCl;'}{'sub': (g)', '2', '(g), 'Bis HO;'}{'sub': (s)', '2(s), 'Cis SnO;'}{'sub': (g)', '(g), 'Dis HCl; and'}{'sub': '2(s)', 'SnOis in the form of tin dioxide nanoparticles.'}4. The reactor according to claim 3 , wherein the reactor maintains the reaction temperature at approximately 200° C.5. The reactor according to claim 1 , wherein the reactor provides particle size reduction of the synthesized nanoparticles and optimization of at least one of reaction conversion claim 1 , reaction temperature claim 1 , and ...

METHOD AND APPARATUS FOR PRODUCING NANOMATERIAL

A method for producing nanomaterial comprising carbon is disclosed. The method comprises introducing a combination of two or more carbon sources into a synthesis reactor; decomposing at least partially the two or more carbon sources in the synthesis reactor to release carbon from the two or more carbon sources; and synthesizing the nanomaterial comprising carbon from the released carbon in the synthesis reactor. 1. A method for producing nanomaterial comprising carbon , the method comprising:introducing a combination of two or more carbon sources into a synthesis reactor;decomposing at least partially the two or more carbon sources in the synthesis reactor to release carbon from the two or more carbon sources; andsynthesizing the nanomaterial comprising carbon from the released carbon in the synthesis reactor.2. The method of claim 1 , wherein decomposing at least partially the two or more carbon sources in the synthesis reactor to release carbon from the two or more carbon sources is done by providing energy to the synthesis reactor and/or by introducing a decomposing reagent.3. The method of claim 1 , further comprising introducing one or more promoters into the synthesis reactor.4. The method of claim 1 , further comprising introducing one or more catalysts into the synthesis reactor claim 1 , wherein synthesizing the nanomaterial comprising carbon comprises synthesizing the nanomaterial comprising carbon from the released carbon and the one or more catalysts.5. The method of claim 1 , further comprising purifying the synthesized nanomaterial comprising carbon by introducing a purifying reagent.6. The method of claim 1 , further comprising functionalizing the synthesized nanomaterial comprising carbon by introducing a functionalizing reagent.7. The method of claim 1 , wherein at least one of the carbon sources is introduced as a liquid claim 1 , aerosol or gas into the synthesis reactor.8. The method of claim 1 , wherein at least one of the carbon sources is ...

PROCESS FOR MANUFACTURING TETRAFLUOROPROPENE

A process for manufacturing tetrafluoropropene, including, alternately: at least one step of reacting a chlorinated compound with hydrofluoric acid in the gas phase, in the presence of a fluorination catalyst, the proportion of oxygen optionally present being less than 0.05 mol. % relative to the chlorinated compound; a step of regenerating the fluorination catalyst by bringing the fluorination catalyst into contact with a regeneration stream including an oxidizing agent. Also, equipment suitable for carrying out this process. 1. A process for the manufacture of tetrafluoropropene , comprising , alternately:at least one stage of reaction of a chlorinated compound with hydrofluoric acid in the gas phase, in the presence of a fluorination catalyst, the proportion of oxygen optionally present being less than 0.05 mol % with respect to the chlorinated compound;a stage of regeneration of the fluorination catalyst by bringing the fluorination catalyst into contact with a regeneration stream comprising an oxidizing agent.2. The process as claimed in claim 1 , in which the stage of reaction of the chlorinated compound with hydrofluoric acid is carried out essentially in the absence of oxygen.3. The process as claimed in claim 1 , in which the regeneration stream contains at least 1 mol % of oxygen with respect to the total regeneration stream.4. The process as claimed in claim 1 , in which the stage of reaction of the chlorinated compound with hydrofluoric acid is carried out in a single reactor claim 1 , separately in time with respect to the stage of regeneration of the fluorination catalyst.5. The process as claimed in claim 1 , in which the stage of reaction of the chlorinated compound with hydrofluoric acid is carried out in at least one first reactor claim 1 , simultaneously with the implementation of the stage of regeneration of the fluorination catalyst in at least one second reactor.6. The process as claimed in claim 1 , in which the tetrafluoropropene is 2 claim 1 ...

APPARATUS FOR PROCESSING HIGHLY CORROSIVE AGENTS

An apparatus for treating highly corrosive agents comprises a tube bundle () heat exchanger (), structured to carry out a heat exchange between two fluids one of which is highly corrosive and flowing inside of said tube bundle (). 1. An apparatus for treating highly corrosive agents , comprising:a tube bundle heat exchanger, structured to carry out a heat exchange between a first fluid which is highly corrosive and flowing inside of at least one tube bundle, and a second fluid flowing outside of said at least one tube bundle,wherein said at least one tube bundle comprises at least one tube of titanium or titanium alloy, having a layer of zirconium or zirconium alloy bonded to the titanium or titanium alloy tube metallurgically or through welding,wherein said at least one titanium or titanium alloy tube is coated on the inside by said zirconium or zirconium alloy tube, and said zirconium or zirconium alloy layer in contact with said first highly corrosive fluid flowing inside said at least one tube bundle, and said titanium or titanium alloy tube is in contact with at least said second fluid flowing outside said at least one layer bundle,wherein said at least one titanium or titanium alloy tube and said zirconium or zirconium alloy coating layer are bonded together through hot-drawing.2. The apparatus according to claim 1 , wherein said at least one titanium or titanium alloy tube has a thickness between 1.0 and 10 millimeters claim 1 , and in that said zirconium or zirconium alloy coating tube has a thickness between 0.3 and 2.0 millimeters.3. The apparatus according to claim 1 , wherein said at least one titanium or titanium alloy tube is only partially coated with said zirconium or zirconium alloy layer.4. The apparatus according to claim 3 , wherein said zirconium or zirconium alloy layer coats solely an end portion of the at least one titanium or titanium alloy tube.5. The apparatus according to claim 4 , wherein said zirconium or zirconium alloy layer extends ...

SUGAR ALCOHOL SPLIT INJECTION CONVERSION

A method of hydrotreating liquefied biomass feedstock with diesel feedstock to produce alkanes is demonstrated that prevents damage to the reactor catalyst, reduces coke production, and converts nearly all of the polyols to alkanes. In order to mitigate the potential coking issue and to moderate the temperature of the catalyst bed while maintaining high conversion for sugar alcohol to hydrocarbon via a hydrotreating process, a diesel feedstock is fed over the reactor catalyst with multiple injections of polyol feedstock along the reactor. 1. A system for producing renewable fuels , comprising:a) a reactor comprising a first end and a second end and containing a-hydrotreating catalyst;b) a fuel oil feedstock injector operably connected to the first end of the reactor and configured to inject a fuel oil feedstock into the reactor,c) a polyol feedstock injector operably connected at or near the first end of the reactor, and configured to inject a polyol feedstock into the reactord) a second polyol feedstock injectors operably connected to the reactor at a location that is more proximate to the reactor second end than the first polyol feedstock injector, each polyol feedstock injector configured to inject and mix the polyol feedstock with the fuel oil feedstock and the hydrotreating catalyst to generate alkanes.2. The system of claim 1 , further comprising a heater to heat said system fuel oil feedstock to reaction temperature prior to entering said reactor via said fuel oil feedstock injector.3. The system of claim 1 , wherein said polyol feedstock comprises a member of the group consisting of Glycol claim 1 , Glycerol claim 1 , Erythritol claim 1 , Threitol claim 1 , Arabitol claim 1 , Ribitol claim 1 , Xylitol claim 1 , Allitol claim 1 , Dulcitol claim 1 , Galactitol claim 1 , Iditol claim 1 , Mannitol claim 1 , Sorbitol claim 1 , Isomalt claim 1 , Lactitol claim 1 , Maltitol claim 1 , Trehalose and combinations thereof.4. The system of claim 1 , wherein said fuel ...

METHOD FOR PRODUCING HYDROGEN CYANIDE

In a method for producing hydrogen cyanide by passing a feed mixture comprising ammonia and methane through reaction tubes, coated on the inner surface with a catalyst comprising platinum, at a reaction temperature of 1000° C. to 1400° C., operated for a time period of at least 100 h, the concentration difference between the ammonia concentration and the methane concentration in the product gas mixture is maintained in a range of from 1.05 % by volume to 3.0% by volume for at least 80% of the time. 1. A method for producing hydrogen cyanide , comprising passing a feed mixture comprising ammonia and methane through reaction tubes , coated on the inner surface with a catalyst comprising platinum , at a reaction temperature of 1000° C. to 1400° C. to provide a product gas mixture comprising hydrogen cyanide , hydrogen , unreacted ammonia and unreacted methane , the ammonia concentration in said product gas mixture being higher than the methane concentration in said product gas mixture , wherein for a time period of at least 100 h a concentration difference between said ammonia concentration and said methane concentration is maintained in a range of from 1.05% by volume to 3.0% by volume for at least 80% of the time by adjusting the reaction temperature , adjusting the molar ratio of ammonia to carbon in the feed mixture , adjusting a feed rate of said feed mixture , or any combination of said adjustments.2. The method of claim 1 , wherein during said time period said concentration difference is no more than 3.0% by volume for at least 95% of the time.3. The method of claim 1 , wherein for at least 95% of the time said concentration difference is maintained at a constant value in the range of from 1.1% by volume to 2.1% by volume.4. The method of claim 1 , wherein the combined amount of ammonia and methane in said feed mixture is at least 90% by volume.5. The method of claim 1 , wherein said feed mixture comprises less than 4% by volume of oxygen.6. The method of claim ...

PROCESS FOR CONVERTING ALKANES TO OLEFINS

A process and apparatus for converting an alkane to an olefin. In one embodiment, the process involves oxidative coupling of an alkane, e.g., methane, with an oxidant, such as air, to produce an olefin having twice the number of carbon atoms as the alkane, e.g., ethylene. In another embodiment, the process involves oxidative dehydrogenation of an alkane, e.g., ethane, with an oxidant to form an olefin having the same number of carbon atoms as the alkane, e.g., ethylene. The process involves passing a flow of the oxidant from a first flow passage through a porous medium; diffusing a flow of the alkane from a second flow passage into the porous medium; and contacting the reactant alkane and the oxidant in the presence of a catalyst within the porous medium to produce the olefin. 1. A process of oxidative coupling for converting an alkane to an olefin having twice the number of carbon atoms as the alkane , comprising:(a) passing a flow of an oxidant through a first inlet into a first chamber defining a first flow passage;(b) passing a flow of an alkane through a second inlet into a second chamber defining a second flow passage, wherein a porous medium having an oxidative coupling catalyst supported therein separates the first flow passage from the second flow passage;(c) applying a pressure in the first flow passage sufficient to provide a bulk flux of the oxidant through the porous medium into the second chamber;(d) adjusting the flow of the alkane such that a ratio of diffusive flux of the alkane into the porous medium to the bulk flux of the oxidant through the porous medium is greater than 1:1;(e) contacting the oxidant and the alkane at the catalyst within the porous medium under reaction conditions sufficient to produce the olefin, which has twice the number of carbon atoms as the alkane, and which thereafter flows into the second flow passage and exits through an outlet in the second chamber.2. The process of wherein the alkane is a C1-4 alkane selected from ...

Apparatus for Preparing a Material of a Battery Cell

A continuous process for producing a material of a battery cell using a system having a mist generator, a drying chamber, one or more gas-solid separators and a reactor is provided. A mist generated from a liquid mixture of two or more metal precursor compounds in desired ratio is dried inside the drying chamber. Heated air or gas is served as the gas source for forming various gas-solid mixtures and as the energy source for any reactions inside the drying chamber and the reactor. One or more gas-solid separators are used in the system to separate gas-solid mixtures from the drying chamber into solid particles mixed with the metal precursor compounds and continuously feed the solid particles into the reactor for further reaction to obtain final solid material particles with desired crystal structure, particle size, and morphology. 1. A system of producing a material for a battery electrochemical cell , comprising:a mist generator adapted to generate a mist from a liquid mixture;a drying chamber comprising a chamber inlet, a chamber body, and a chamber outlet;a first gas line connected to the drying chamber and adapted to flow a first gas into the drying chamber and form a first mixture with the mist inside the drying chamber; a separator inlet connected to the chamber outlet and adapted to collect one or more products from the chamber outlet of the drying chamber, wherein the first gas-solid separator separates the one or more products into a first type of solid particles and a waste product;', 'a first separator outlet adapted to deliver the first type of solid particles out of the first gas-solid separator; and', 'a second separator outlet adapted to deliver the waste product out of the first gas-solid separator; and, 'a first gas-solid separator, comprising a reactor inlet connected to the first separator outlet to receive the first type of solid particles; and', 'a gas inlet connected to a second gas line to flow a second gas inside the reactor, wherein a second ...

USE OF A PROCESS FOR HYDROGEN PRODUCTION

The present invention relates to the use of a process for hydrogen production in which at least a part of a hydrocarbonaceous feed gas (a) is passed into a reformer (c), wherein the feed gas is contacted in the reformer with a catalyst and the feed gas is converted to hydrogen and solid carbon, for the direct production of a hydrogenous gas at filling stations for sale to a consumer, and also to a reactor (d) for hydrogen production. 2. A device as claimed in claim 1 , wherein the reactor includes a preheating zone claim 1 , adapted to maintain temperatures ranging between 100-900° C.3. A device as claimed in claim 2 , wherein the reactor outlet is in the preheating zone or in the externally heated heating zone.4. A device as claimed in claim 1 , wherein the cooling zone is configured for operating temperatures ranging between 100-600° C. claim 1 , and/or the externally heated heating zone is configured for operating temperatures ranging between 300-1400° C. or 500-1000° C.5. A device as claimed in claim 1 , wherein the outlet for the catalyst and produced carbon are in the cooling zone.6. A device as claimed in claim 1 , wherein the reactor is adapted to provide a gradually decreasing temperature gradient from the externally heated heating zone to the cooling zone during use.7. A device as claimed in claim 1 , wherein the inlet for the catalyst is in the externally heated heating zone or a preheating zone.8. A device as claimed in claim 1 , wherein the externally heated heating zone is less than 50% of a length of the reactor from the feed gas inlet to the reactor gas outlet claim 1 , and/or the cooling zone is less than 50% of a length of the reactor from the feed gas inlet to the reactor gas outlet.9. A device as claimed in claim 1 , comprising a pressure controller on the reactor for an overpressure of 1-500 mbar.10. A device as claimed in claim 1 , adapted to convey catalyst through the reactor in or on a mechanical device during use.11. A device as claimed in ...

PrOx REACTOR AND FUEL CELL ARRANGEMENT COMPRISING PrOx REACTOR

The invention relates to a PrOx reactor (R) comprising a housing that encloses a reaction space and has a first inlet (E) for supply of a hydrogenous first gas (G) to a reaction space, a second inlet (E) for supply of an oxygenous second gas (G) to the reaction space and an outlet (A) for discharge of a third gas (G), wherein there is a multitude of conduits (Kv) extending from the second inlet (E) into the reaction space, each of which comprises at least one opening (O) for supply of the second gas (G) to the reaction space. 111223. A PrOx reactor (R) comprising a housing that surrounds a reaction space and has a first inlet (E) for supply of a hydrogenous first gas (G) to the reaction space , a second inlet (E) for supply of an oxygenous second gas (G) to the reaction space and an outlet (A) for discharge of a third gas (G) ,{'b': 2', '0', '2, 'wherein there is a multitude of conduits (Kv) extending from the second inlet (E) into the reaction space, each of which comprises at least one opening () for supply of the second gas (G) to the reaction space,'}{'b': '2', 'wherein the length and cross section of the conduits (Kv) are designed such that a pressure drop between the second inlet (E) and the end of the respective conduit (Kv) is essentially equal.'}232. The PrOx reactor (R) according to claim 1 , wherein the housing comprises a third inlet (E) for supply of a proportion of the oxygenous second gas (G).3. The PrOx reactor (R) according to claim 1 , wherein each conduit (Kv) comprises a multitude of openings (O).4111. The PrOx reactor (R) according to claim 1 , wherein the first inlet (E) and the outlet (A) are arranged on opposite sides of the housing claim 1 , such that a flow direction of the first gas (G) from the first inlet (E) to the outlet (A) forms a first direction.5. The PrOx reactor (R) according to claim 1 , wherein the PrOx reactor (R) comprises a multitude of plates (P) stacked one on top of another claim 1 , which have preferably been provided ...

ACTIVATION ENERGY REDUCERS FOR CATALYTIC OXIDATION OF GASEOUS MIXTURES

The present invention provides materials for improving the ignition of gaseous reactants in metal catalyzed oxidation reactions comprising a metal catalyst gauze, preferably, a platinum/rhodium catalyst gauze, having in contact therewith, from 0.5 to 1.5 wt. %, based on the weight of the metal catalyst gauze, of one or more pieces of previously used metal catalyst gauze. Further, methods of making the metal catalyst materials comprise shaping the pieces of previously used metal catalyst gauze and placing them equidistant from each other in contact with or on the surface of the metal catalyst gauze. And methods of using the materials comprise feeding into the reactor a gas mixture of oxygen or air and one or more reactant gases, and igniting the gas mixture at the surface of one or more or all of the pieces of previously used metal catalyst. 1. A metal catalyst material comprising a metal catalyst gauze comprising wires or metal threads having a diameter of from 0.007 to 0.25 cm in diameter and having in contact therewith , from 0.5 to 1.5 wt. % , based on the weight of the metal catalyst gauze , of one or more pieces of previously used metal catalyst gauze , that have not been contaminated with iron and that have not been contaminated with foreign debris , hydrocarbons , or oil as tested by visual inspection , the one or more pieces placed equidistant from each other on the surface of the metal catalyst gauze , or , if one piece , placed in contact with or concentrically with the center of the metal catalyst gauze.2. The metal catalyst material as claimed in claim 1 , wherein the one or more pieces of previously used metal catalyst gauze comprise used platinum/rhodium catalyst gauze.3. The metal catalyst material as claimed in claim 1 , wherein the amount of the one or more pieces of previously used metal catalyst gauze ranges from 0.5 to 1.0 wt. % claim 1 , based on the weight of the metal catalyst gauze.4. The metal catalyst material as claimed in claim 1 , ...

EXPERIMENTAL DEVICE FOR SIMULATING EXPLOITATION OF NATURAL GAS HYDRATE IN PERMEABLE BOUNDARY LAYER

A device for simulating exploitation of a natural gas hydrate in a permeable boundary layer includes a high pressure reaction kettle, a formation simulation unit and an aquifer maintaining unit. A water bath jacket externally connected with constant temperature water bath is arranged on the outer wall of the high pressure reaction kettle for providing a necessary temperature condition for the high pressure reaction kettle. A simulative well at the center of the top of the high pressure reaction kettle is connected with liquid injection, gas injection, gas production and water production equipment. An aquifer interface at the bottom of the high pressure reaction kettle is connected to the aquifer maintaining unit through a pipeline. The simulation device simulates the geological environment of a hydrate reservoir, allowing comprehensive evaluation of hydrate exploitation under different formation permeability and different formation pressure gradients. 1. A device for simulating exploitation of a natural gas hydrate in a permeable boundary layer , comprising:a high pressure reaction kettle;a formation simulation unit;an aquifer maintaining unit;a water bath jacket externally connected with a constant temperature water bath and arranged on the outer wall of the high pressure reaction kettle for providing a necessary temperature condition for the high pressure reaction kettle;a simulative well externally connected with a liquid injection, a gas injection, a gas production and a water production equipment and arranged at a center of a top of the high pressure reaction kettle; andan aquifer interface arranged at the bottom of the high pressure reaction kettle, the formation simulation unit being arranged in the high pressure reaction kettle, and the aquifer maintaining unit is connected with the aquifer interface through a pipeline.2. The device for simulating exploitation of the natural gas hydrate in the permeable boundary layer of claim 1 ,wherein an interior of the ...

OPTIMIZED INTRODUCTION OF THE STARTING MATERIALS FOR A PROCESS FOR PREPARING AROMATIC AMINES BY HYDROGENATION OF NITROAROMATICS

The invention relates to a process for preparing aromatic amines by hydrogenation of corresponding nitroaromatics by means of hydrogen, and also an apparatus suitable for this purpose. In particular, the invention relates to a process for preparing toluenediamine (TDA) by hydrogenation of dinitrotoluene (DNT). 117-. (canceled)18. An apparatus , comprising:a reactor,a driving jet nozzle at one end of the reactor, adapted for injecting a reaction mixture from a bottom region of the reactor via an external loop into the bottom region of the reactor,an inlet adapted for a nitroaromatic at one end of the reactor,an inlet adapted for hydrogen, anda measuring device adapted to detect partial or complete blocking of the inlet adapted for the nitroaromatic after improper contact between the inlet adapted for the nitroaromatic and a liquid phase in the reactor,wherein the apparatus is adapted such that, at a correct full height of the reactor, direct physical contact between the inlet adapted for the nitroaromatic and the liquid phase occurs neither in the reactor nor in a pumped circuit, either in an operating state or on shutting down, andwherein the apparatus is adapted to hydrogenate the nitroaromatic with the hydrogen in the reactor in the presence of a suspended catalyst in the liquid phase, thereby obtaining an aromatic amine.19. The apparatus according to claim 18 , wherein the reactor is vertical.20. The apparatus according to claim 18 , further comprising a central plug-in tube in a longitudinal direction of the reactor.21. The apparatus according to claim 18 , further comprising a heat exchanger in an interior of the reactor claim 18 , adapted to allow cooling water to flow and take up part of the heat of reaction.22. The apparatus according to claim 18 , adapted to introduce the hydrogen at a lower end of the reactor.23. The apparatus according to claim 18 , wherein the inlet adapted for the nitroaromatic is distinct from the driving jet nozzle.24. The apparatus ...

Reforming Apparatus and Method

A multiple adiabatic bed reforming apparatus and process are disclosed in which stage-wise combustion, in combination with multiple reforming chambers with catalyst, utilize co-flow and cross-flow under laminar flow conditions, to provide a reformer suitable for smaller production situations as well as large scale production. A passive stage by stage fuel distribution network suitable for low pressure fuel is incorporated and the resistances in successive fuel distribution lines control the amount of fuel delivered to each combustion stage. 1. A gaseous hydrocarbon-steam reforming process comprising:partially combusting the fuel in a first fuel/air mixture stream to heat the fuel/air mixture stream for use during reforming of a gaseous hydrocarbon-steam stream;combusting a second fuel/air mixture stream to heat an air stream for use during reforming of the gaseous hydrocarbon-steam stream; andreforming the gaseous hydrocarbon-steam stream to form a syngas stream and a flue gas stream.2. The process of claim 1 , further comprising:reducing metal dusting and/or coking during the reforming step by heating and pre-reforming the gaseous hydrocarbon-steam stream in multiple pre-reforming stages, prior to reforming the gaseous hydrocarbon-steam stream.3. The process according to claim 2 , wherein heating comprises recovering heat from the flue gas stream into the gaseous hydrocarbon-steam stream in a heat exchanger.4. The process of claim 1 , wherein said reforming comprises at least three stages of:i) heating the gaseous hydrocarbon-steam stream by recovering heat from the heated air stream to form a heated reformer stream and a cooled air stream;ii) reforming at least a portion of the heated reformer stream; andiii) combusting a portion of the partially combusted fuel/air mixture stream in the presence of the cooled air stream to re-heat the cooled air stream.5. The process of claim 4 , wherein an amount of the fuel/air mixture supplied to the combusting step of each of ...

Apparatus and Method for Natural Gas Reformation

An apparatus for the catalytic reaction of gaseous hydrocarbons into synthesis gas by means of oxygen is disclosed. In order to improve the apparatus it is provided for the catalyst chamber containing the gas and the catalyst particle to be separated from the oxygen chamber containing the oxygen by a gas-permeable wall. 1. An apparatus for the catalytic reaction of gaseous hydrocarbons into synthesis gas by means of oxygen , comprising a catalyst chamber containing the gas , wherein catalyst particles are separated from an oxygen chamber containing the oxygen by a gas-permeable wall.2. The apparatus as claimed in claim 1 , wherein the gas-permeable wall is formed by a plurality of tubes.3. The apparatus for the catalytic reaction of gaseous hydrocarbons of claim 2 , wherein the tubes are formed in multiple layers.4. The apparatus for the catalytic reaction of gaseous hydrocarbons of claim 2 , wherein the tubes have a different flow resistance in their longitudinal axis.5. The apparatus for the catalytic reaction of gaseous hydrocarbons of claim 2 , wherein the tubes have a rib structure.6. The apparatus for the catalytic reaction of gaseous hydrocarbons of claim 2 , wherein the catalyst chamber is arranged around the tubes.7. The apparatus for the catalytic reaction of gaseous hydrocarbons of claim 2 , wherein the catalyst chamber is located within the tubes.8. The apparatus for the catalytic reaction of gaseous hydrocarbons of claim 1 , wherein the catalyst particles are provided as a fixed bed.9. The apparatus for the catalytic reaction of gaseous hydrocarbons of claim 1 , wherein the catalyst particles.10. The apparatus for the catalytic reaction of gaseous hydrocarbons of claim 1 , further comprising at least one separation device at an end of the catalyst chamber.11. The apparatus for the catalytic reaction of gaseous hydrocarbons of claim 10 , wherein the separation device is formed as a lamella separator.12. A method for the catalytic reaction of gaseous ...

METHOD OF STEAM METHANE REFORMING

A convectively heated steam/methane reformer having a shell and tube reforming reactor for hydrogen production. A reactor core containing the reactants is convectively heated by hot air flowing through the shell or annulus of the reactor. Heated air is supplied to the reactor through several fluid inlets on the shell side of the reformer. 1. (canceled)2. The method of claim 13 , wherein the plurality of hot fluid inlets further comprise an adjustable valve that opens or closes to maintain temperature stability inside the shell side annulus.3. The method of claim 13 , wherein the adjustable valve may be opened or closed at an angle ranging from 0°-90°.4. The method of claim 13 , wherein the plurality of not fluid inlets are positioned at an angle ranging from 45°-90° to the shell side of the reformer.5. The method of claim 13 , wherein the hot air outlet is positioned on the perimeter of the shell.6. The method of claim 13 , wherein the hot air outlet is positioned on the surface of the shell.7. The method of claim 13 , wherein the shell side annulus is a single zone with no baffles.8. The method of claim 13 , wherein the healing medium is selected front the group consisting of air claim 13 , nitrogen claim 13 , helium claim 13 , and combinations thereof.9. The method of claim 13 , wherein the solid catalyst is nickel and/or magnesium aluminate.10. The method of claim 13 , wherein the plurality of hot fluid inlets are disposed in two groups each spirally positioned to wrap around the circumference of the shell side of the tube and shell reactor.11. The method of claim 10 , wherein the two groups of the plurality of hot fluid inlets are disposed on opposite sides of the shell side of the tube and shell reactor.12. The method of claim 13 , wherein the plurality of hot fluid inlets are tubular extensions from the surface of the shell side of the tube and shell reactor.13. A method for converting methane to hydrogen gas claim 13 , comprising:heating a shell side annulus ...

Apparatus for minimizing bypass in ammonia oxidation burners

A sealing system of a burner basket in an ammonia oxidation burner, wherein the burner basket has a wall that is anchored in the ammonia oxidation burner and the burner basket has a gas-permeable bottom plate, which is placed on further internal fittings of the ammonia oxidation burner and has a peripheral rim, wherein the wall and the gas-permeable bottom plate are not mechanically connected to each other, and so there is a gap between the wall and the peripheral rim of the bottom plate, wherein at the peripheral rim of the bottom plate a rim seal that is made up of individual segments is mounted movably by way of guiding pins and the rim seal projects over the gap between the peripheral rim of the bottom plate to the wall and lies against the wall.

METHOD FOR THE PRODUCTION OF ALKENYL HALOSILANES, AND REACTOR SUITED THEREFOR

Described is a method for producing alkenyl halosilanes by reacting alkenyl halide selected from the group comprising vinyl halide, vinylidene halide, and allyl halide with halosilane selected from the group comprising monohalosilane, dihalosilane, and trihalosilane in the gas phase in a reactor comprising a reaction tube () that has an inlet () at one end and an outlet () at the other end, said reactor further comprising an annular-gap nozzle () that is mounted on the inlet (), extends into the reaction tube (), and has a central supply duct () for one reactant () and a supply duct (), which surrounds the central supply duct (), for the other reactant (). In order to carry out said method, alkenyl halide is injected into the reaction tube () through the central supply duct (), halosilane is injected thereinto through the surrounding supply duct (), and both substances flow through the reaction tube () in the direction of the outlet (). The described method allows alkenyl halosilanes to be produced at a high yield and with great selectivity. The amount of soot formed is significantly lower than in conventional reators. The invention also relates to a reactor for carrying out gas-phase reactions, said reactor being characterized by at least the following elements: A) a reaction tube () that has B) an inlet () at one end, C) an outlet () at the other end, and D) an annular-gap nozzle () which includes a central supply duct () for one reactant () and a supply duct (), which surrounds the central supply duct (), for another reactant (), said nozzle being mounted on the inlet () and extending into the reaction tube (). 11234576582115613. Process for preparing alkenylhalosilanes by reacting alkenyl halide selected from the group of vinyl halide , vinylidene halide and allyl halide with halosilane selected from the group of mono- , di- and trihalosilane in the gas phase in a reactor comprising a reaction tube () equipped with an inlet () at one end of the tube and with an ...

MULTICOMPONENT SYSTEM FOR PRODUCTION OF ALKOXYSILANE-BASED SPRAY FOAMS

Disclosed herein is a multicomponent system comprising at least two separate components A and B, component A containing an alkoxysilane-terminated prepolymer and component B containing a mixture comprising a component B1 containing water and a component B2 containing a polyol having at least two OH-groups and a molar mass from >62 to <500 g/mol, where the proportion of component B2 in component B is from >20% by weight to <80% by weight. Also disclosed herein is a multichamber pressurized can comprising a multicomponent system as disclosed herein, and to a shaped body obtainable by polymerizing the multicomponent system disclosed herein. 1. A multi-component system comprising at least two separate components A and B , wherein component A comprises an alkoxysilane-terminated pre-polymer and component B comprises a mixture comprising a component B1 comprising water , and a component B2 comprising a polyol having at least two OH-groups and a molar mass ≧62 and ≦500 g/mol , wherein the content of component B2 within component B is >20 wt % and ≦80 wt %.2. Multi-component system according to claim 1 , wherein component B1 has a pH-value ≧3.0 and ≦9.0 at 20° C.3. Multi-component system according to claim 1 , wherein component B1 comprises at least one buffer system.4. Multi-component system according to claim 3 , wherein the buffer system is based on at least one organic carboxylic acid and its conjugate base.5. Multi-component system according to claim 4 , wherein the buffer system comprises acetic acid claim 4 , succinic acid claim 4 , tartaric acid claim 4 , malic acid claim 4 , or citric acid claim 4 , or a combination thereof claim 4 , and the respective conjugate base thereof.6. Multi-component system according to claim 3 , wherein the concentration of the buffer system in the component B1 is from 0.001 to 2.0 mol/L.7. Multi-component system according to claim 1 , wherein the polyol of component B2 comprises at least three OH-groups.8. Multi-component system ...

APPARATUS AND PROCESS FOR QUICK COOLING HEAT EXCHANGER IN CARBON BLACK PRODUCTION

Effluent from a carbon black reactor is directly discharged FIG. from the reactor to a quick cooling radiant heat exchanger before, or in some instances after, a reaction-stopping water quench. The cooled reaction quench is then supplied to an air preheater to preheat the carbonaceous feed stock that is supplied to the reactor. The heat exchanger includes a chamber having outside walls formed by heat exchanger tubes which are welded together. If desired, additional cooling capacity is provided by platens formed of heat exchanger tubes which are contained in the chamber to which the reactor effluent is supplied. 1. In a system for the production of carbon black by the furnace process which includes a reactor supplied with a fuel , preheated air and a carbonaceous feed stock , the improvement comprising:a quick cooling radiant heat exchanger located between an effluent discharge outlet of the reactor and an air preheater,said heat exchanger including a reactor effluent inlet in flow communication with the effluent discharge outlet of said reactor and an effluent outlet in flow communication with an effluent inlet of said air preheater,a chamber in said heat exchanger, heat exchanger tubes in said chamber, said heat exchanger tubes being arranged to effect heat transfer primarily by radiation between reactor effluent flowing through said chamber and a cooling medium supplied to said heat exchanger tubes.2. The improvement of wherein said chamber is bounded by said heat exchanger tubes which are welded to each other to form the exterior walls of said chamber.3. The improvement of wherein said chamber is fitted with hanging platens made up of heat exchange tubes claim 1 , said platens defining passages through which reactor effluent flows claim 1 , whereby substantially the entire outer surface of said heat exchanger tubes in said platens is contacted by said reactor effluent.4. The improvement of wherein said chamber includes first and second chamber sections claim 1 , ...

METHODS OF PRODUCING HETERODIAMOND AND APPARATUS THEREFOR

A combinatorial synthesis of a heterodiamond unit cell, which entails a step of reacting a tetrahedranoidal molecule with a heteroatom to form heterodiamond unit cell and then heterodiamond mass. 1. A combinatorial synthesis of a heterodiamond unit cell , which comprises a step of reacting a tetrahedranoidal molecule with a heteroatom.2. The combinatorial synthesis of claim 1 , wherein the tetrahedranoidal molecule is benzvalene claim 1 , 3 claim 1 ,4-diazabenzvalene or 2 claim 1 ,3 claim 1 ,4-methynylcyclobutane.3. The combinatorial synthesis of claim 1 , wherein said heteroatom species is atomic nitrogen.4. The combinatorial synthesis of claim 3 , wherein atomic nitrogen is obtained from a nitrogen-containing species in the vapor phase by exposing said species to a high energy discharge which nitrogen containing species is hydrazine claim 3 , ammonia claim 3 , or dinitrogen.5. The combinatorial synthesis of claim 1 , wherein the heteroatom is atomic boron.6. The combinatorial synthesis of claim 5 , wherein atomic boron is obtained from a boron-containing species in the vapor phase by exposing said species to a high energy discharge which boron containing species is diborane.7. The combinatorial synthesis of claim 1 , wherein a heterodiamond mass is formed from an assembly of a plurality of heterodiamond unit cells.8. The combinatorial synthesis of claim 1 , which is conducted in vapor phase.9. The combinatorial synthesis of claim 1 , which is conducted in solid state.10. The combinatorial synthesis of the heterodiamond unit cell of claim 9 , wherein a homogeneous blend of a tetrahedranoidal molecule and a heteroatom source is subjected to a high energy discharge.11. The combinatorial synthesis of the heterodiamond unit cell of claim 9 , wherein the heteroatom source is hydrazine or ammonia.12. The combinatorial synthesis of claim 1 , which comprises obtaining heteroatoms from a heteroatom source by vaporizing said heteroatom source in an inert carrier gas and ...

LIQUID FUEL CPOX REFORMER AND FUEL CELL SYSTEMS, AND METHODS OF PRODUCING ELECTRICITY

Integrated liquid fuel catalytic partial oxidation (CPOX) reformer and fuel cell systems can include a plurality or an array of spaced-apart CPOX reactor units, each reactor unit including an elongated tube having a gas-permeable wall with internal and external surfaces. The wall encloses an unobstructed gaseous flow passageway. At least a portion of the wall has CPOX catalyst disposed therein and/or comprising its structure. The catalyst-containing wall structure and open gaseous flow passageway enclosed thereby define a gaseous phase CPOX reaction zone, the catalyst-containing wall section being gas-permeable to allow gaseous CPOX reaction mixture to diffuse therein and hydrogen rich product reformate to diffuse therefrom. The liquid fuel CPOX reformer also can include a vaporizer, one or more igniters, and a source of liquid reformable fuel. The hydrogen-rich reformate can be converted to electricity within a fuel cell unit integrated with the CPOX reactor unit. 1. A reformer for the gaseous phase catalytic partial oxidation of a gaseous CPOX reaction mixture of an oxygen-containing gas and a gaseous and/or vaporized liquid CPOX fuel reaction mixture to provide a hydrogen gas product , the reformer comprising:a generally U-shaped open conduit configured to convey a gaseous CPOX reaction mixture of an oxygen-containing gas and a gaseous and/or vaporized liquid CPOX fuel to an inlet of at least one elongate tubular gaseous phase CPOX reactor unit, the reactor unit having a gas permeable wall with an internal surface and an external surface defining a wall thickness therebetween and having at least one CPOX catalyst disposed (i) on at least a portion of an internal surface of the CPOX reactor unit and/or (ii) within the wall thickness thereof, the CPOX-containing portion of the CPOX reactor unit defining a gaseous phase CPOX reaction zone, the CPOX reaction zone adapted to emit a heat of exotherm during a CPOX reaction therein;the U-shaped open conduit comprising a ...

Urea to Ammonia Process

Methods and systems for producing a pressurized ammonia-containing gas stream from aqueous urea. The method comprising pumping an aqueous urea-containing solution to a fluid-tight enclosure at a rate to match the external demand for ammonia-gas, wherein a fluid heat transfer medium is applied to the exterior of the fluid-tight enclosure to transfer heat to the aqueous urea-containing solution sufficient to hydrolyze the solution to an ammonia gaseous product. The systems comprise means for carrying out the methods. 1. A method adapted to provide a pressurized ammonia-containing gas stream from aqueous urea , the method comprising feeding an aqueous urea-containing solution to a fluid-tight enclosure at a rate to match the external demand rate for ammonia-gas , wherein a fluid heat transfer medium is present on the exterior of said fluid-tight enclosure to transfer heat to the aqueous urea-containing solution within the enclosure to hydrolyze the solution and convert the urea-containing solution to an ammonia gaseous product comprising ammonia , carbon dioxide and water vapor , the pressure within said fluid-tight enclosure being maintained by back pressure control to ensure that the ratio of urea and water is maintained independent of the ammonia generation rate , and the urea is converted.2. The method of wherein the fluid-tight enclosure is a tube bundle or coil3. A method adapted to provide a pressurized ammonia-containing gas stream from aqueous urea claim 1 , the method comprising feeding an aqueous urea-containing solution to the tube side of a shell and tube heat exchanger at a rate to match the external demand rate for ammonia-gas claim 1 , wherein a fluid heat transfer medium is present on the shell side to transfer heat to the aqueous urea-containing solution within the tubes sufficient to hydrolyze the solution and convert the urea-containing solution to an ammonia gaseous product comprising ammonia claim 1 , carbon dioxide and water vapor claim 1 , the ...

Induction Heated Reactor

A tube heat exchange reactor for carrying out an endothermic catalytic reaction. The tube heat exchange reactor includes: an outer tube with a first and a second end, where the first end is an inlet end and where the second end is a closed end, an inner tube coaxially arranged within the outer tube and spaced apart from the outer tube, where at least a part of the inner tube holds a bed of catalyst material susceptible for induction heating and where the inner tube has an inlet end and an outlet end, an induction coil placed within the annular space confined between the outer and the inner tube, and a power source arranged to supply alternating current to the induction coil in order to generate an alternating magnetic field within at least a part of the inner tube. 1. A tube heat exchange reactor for carrying out an endothermic catalytic reaction , said tube heat exchange reactor comprising:an outer tube with a first and a second end, where the first end is an inlet end and where the second end is a closed end;an inner tube coaxially arranged within the outer tube and spaced apart from the outer tube, where at least a part of said inner tube holds a bed of catalyst material susceptible for induction heating and where said inner tube has an inlet end and an outlet end;an induction coil placed within an annular space confined between the outer and the inner tube; anda power source arranged to supply alternating current to the induction coil in order to generate an alternating magnetic field within at least a part of said bed of catalyst material within said inner tube,wherein said tube heat exchange reactor is arranged to allow a process gas stream to be led into the inlet end of said outer tube, to flow in the annular space confined between the outer and inner tube towards the second end of the outer tube and subsequently into said inner tube in order to reach said bed of catalyst material and undergo an endothermic reaction resulting in a product gas.2. The tube ...

METHOD FOR DESIGNING MULTI-VALVE UNI-DIRECTION BLOWDOWN SYSTEM FOR A HIGH PRESSURE TUBULAR REACTOR

Provided herein is a unidirectional blow down system for a high-pressure tubular reactor with a hyper that minimizes the tube wall metal temperature during a decomposition event wherein the system prevents the reactor walls from reaching a temperature capable of causing the tube metal to austenize. Also provided are methods of designing and methods of operating a unidirectional blowdown system. 2. The blowdown system of wherein the inner diameter (ID) of the front emergency valve is smaller than the valve ID at the end of the reactor.3. The blowdown system of wherein the front emergency valve has an ID of from about 0.25 to about 0.5 inches.4. The blowdown system of wherein the front emergency valve has an ID of from about 0.3 to about 0.4 inches.5. The blowdown system of wherein the front emergency valve has an ID of 0.375 inches.6. The blowdown system of wherein the valve ID at the end of the reactor is from about 0.375 to about 2 inches.7. The blowdown system of wherein the valve ID at the end of the reactor is from about 1 to about 1.5 inches.8. The blowdown system of wherein the valve ID at the end of the reactor is about 1 inch.9. The blowdown system of wherein there is at least one additional valve between the front emergency valve and the valve at the end of the reactor.10. The blowdown system of wherein there is one additional valve with an ID of about 0.25-0.5 inches between the front emergency valve and the valve at the end of the reactor.11. The blowdown system of wherein the tubes of the tube reactor are low alloy carbon steel.12. The blowdown system of wherein the tubes of the tube reactor are low alloy carbon steel having a carbon content of from about 0.3 to about 0.4% carbon.13. The blowdown system of wherein the tubes of the tube reactor are Grade AISI 4333 tubes.14. The blowdown system of wherein the metal of the tube reactor has an austenization temperature between about 750° C. and about 850° C.15. The blowdown system of wherein the metal of the ...

Chemical Reactor with Integrated Heat Exchanger, Heater, and High Conductance Catalyst Holder

A chemical reactor that combines a pressure vessel, heat exchanger, heater, and catalyst holder into a single device is disclosed. The chemical reactor described herein reduces the cost of the reactor and reduces its parasitic heat losses. The disclosed chemical reactor is suitable for use in ammonia (NH) synthesis. 1. A chemical reactor , comprising:a pressure vessel; a central region;', 'a reactant-in spiral passageway configured to pass reactant from an inlet port of the spiral heat exchanger to the central region; and', 'a reactant-out spiral passageway configured to pass reactant from the central region to an outlet port of the spiral heat exchanger;, 'a spiral heat exchanger disposed within the pressure vessel, the spiral heat exchanger comprisinga heater disposed within the pressure vessel and positioned in the central region of the spiral heat exchanger; anda catalyst holder disposed within the pressure vessel and positioned in the central region of the spiral heat exchanger.2. The chemical reactor of claim 1 , wherein the catalyst holder is an annular catalyst holder and the heater is positioned within the annular catalyst holder.3. The chemical reactor of claim 2 , wherein the annular catalyst holder includes perforated outer and inner walls.4. The chemical reactor of claim 3 , wherein the annular catalyst holder includes tubes extending through the catalyst holder.5. The chemical reactor of claim 1 , wherein the heater is positioned at one axial end of the central region and the catalyst holder is positioned at an opposite axial end of the central region.6. The chemical reactor of claim 5 , wherein an exit end of the reactant-in spiral passageway is located proximate an upstream side of the heater and an entrance end of the reactant-out spiral passageway is located proximate a downstream side of the catalyst holder.7. The chemical reactor of claim 5 , wherein the catalyst holder comprises a sheet metal or foil monolith with a honeycomb-like structure that ...

MULTI-TUBULAR CHEMICAL REACTOR WITH IGNITER FOR INITIATION OF GAS PHASE EXOTHERMIC REACTIONS

A multi-tubular chemical reactor includes an igniter for the initiation of gas phase exothermic reaction within the gas phase reaction zones of the tubular reactor units. 19-. (canceled)10. A method of carrying out a gas phase exothermic reaction within a multi-tubular chemical reactor to produce desired product(s) , the method comprising:introducing gaseous reactants into an inlet of a gaseous flow passageway of a plurality of reactor units, each reactor unit of the plurality comprising an elongate tube having a wall with an internal surface, an external surface, and a wall interior between the internal and external surfaces, at least a portion of the wall interior adapted to function as a gas phase reaction zone, the interior surface of the wall enclosing the gaseous flow passageway having the inlet at one end and an outlet at the opposing end, the interior surface of the wall adapted to permit gas flowing through the passageway to enter the wall interior at the gas phase reaction zone;flowing at least a portion of the gaseous reactants into the as phase reaction zones of the plurality of reactor units;initiating with radiant heat an exothermic reaction of the gaseous reactants within the gas phase reaction zone of at least one of the reactor units, thereby commencing the production of desired product(s) and exothermic heat; andtransferring heat produced by the exothermic reaction occurring within the gas phase reaction zone of the at least one reactor unit to the gas phase reaction zone of one or more adjacent reactor units, thereby initiating an exothermic reaction within the at least one adjacent reactor unit until in such manner an exothermic reaction has been initiated in each of the plurality of spaced-apart reactor units.11. The method of wherein the initiating of the exothermic reaction in the at least one reactor unit comprises heating the at least one reactor unit with at least one igniter claim 10 , the igniter comprising a radiant heat-producing ...

Device for changing nozzles

Vorrichtung zum Wechseln von Düsen an druckbeaufschlagten Behältern (1), bei dem ein Medium (20) mittels Lanze (7) durch eine Düse (8) in den Behälter (1) geleitet wird, wobei an dem Behälter (1) ein Stutzen (2) befestigt ist, der über eine Absperrvorrichtung (3) mit einem Abdichtungsgehäuse (5) zur Aufnahme der Lanze (7) verbunden ist, wobei im Abdichtungsgehäuse (5) Dichtringe (13a, 13b, 13c) angebracht sind, die bei eingeführter Lanze (7) in das Abdichtungsgehäuse (5) die Druckdichtheit zum Behälter (1) und zur Umgebung sicherstellen, und zwischen der Dichtung (13a) und der Absperrvorrichtung (3) mindestens eine Leitung zum Einleiten oder Ablassen einer Sperrflüssigkeit oder einer Gasbeschleierung zur zusätzlichen Dichtheit angebracht ist. contraption for changing nozzles on pressurized containers (1), wherein a medium (20) by means of lance (7) through a nozzle (8) in the container (1), wherein attached to the container (1) a nozzle (2) is that over a shut-off device (3) with a sealing housing (5) for receiving the lance (7) is connected, wherein in the sealing housing (5) sealing rings (13a, 13b, 13c) are mounted, which with inserted lance (7) in the sealing housing (5) the pressure tightness to the container (1) and to ensure the environment, and between the seal (13a) and the shut-off device (3) at least one conduit for introduction or draining a barrier fluid or a Gasbeschleierung attached for additional tightness is.

Reactor for performing endothermic catalytic reactions.

Device for changing nozzles

Die Erfindung betrifft eine Vorrichtung zum Wechseln von Düsen, ohne dass die Druckverhältnisse im zugehörigen Behälter oder Apparat geändert werden müssen. DOLLAR A Erfindungsgemäß wird die Aufgabe bei der eingangs genannten Vorrichtung dadurch gelöst, dass an einem druckbeaufschlagten Behälter (1), bei dem ein Medium (20) mittels Lanze (7) durch eine Düse (8) in den Behälter (1) geleitet wird, ein Stutzen (2) befestigt ist, der über eine Absperrvorrichtung (3) mit einem Abdichtungsgehäuse (5) zur Aufnahme der Lanze (7) verbunden ist und dass im Abdichtungsgehäuse (5) Dichtringe (13a, 13b, 13c) angebracht sind, die bei eingeführter Lanze (7) in das Abdichtungsgehäuse (5) die Druckdichtheit zum Behälter (1) und zur Umgebung sicherstellen. The invention relates to a device for changing nozzles without the pressure conditions in the associated container or apparatus having to be changed. DOLLAR A According to the invention, the object is achieved in the device mentioned at the outset in that on a pressurized container (1) in which a medium (20) is guided into the container (1) through a nozzle (8) through a nozzle (8), a connecting piece (2) is attached, which is connected via a shut-off device (3) to a sealing housing (5) for receiving the lance (7) and that sealing rings (13a, 13b, 13c) are attached to the sealing housing (5) Insert the lance (7) into the sealing housing (5) to ensure pressure tightness to the container (1) and the environment.

Device for changing nozzles

The invention relates to a device which enables nozzles to be changed without changing the pressure conditions in the container or device associated therewith. According to the invention a connector piece support ( 2 ) is fixed to a pressurised container ( 1 ) wherein a medium ( 20 ) is guided into said container through a nozzle ( 8 ) by means of a lance ( 7 ). Said connector piece is connected to a sealing housing ( 5 ) by means of a locking device ( 3 ) in order to receive the lance ( 7 ). Sealing rings ( 13 a, 13 b, 13 c ) are arranged in the sealing housing ( 5 ) thereby ensuring pressure-tightness in relation to the container ( 1 ) and the surrounding area when the lance ( 7 ) is inserted into the sealing housing ( 5 ).

Device for changing nozzles

The invention relates to a device which enables nozzles to be changed without changing the pressure conditions in the container or device associated therewith. According to the invention a connector piece support (2) is fixed to a pressurised container (1) wherein a medium (20) is guided into said container through a nozzle (8) by means of a lance (7). Said connector piece is connected to a sealing housing (5) by means of a locking device (3) in order to receive the lance (7). Sealing rings (13a, 13b, 13c) are arranged in the sealing housing (5) thereby ensuring pressure-tightness in relation to the container (1) and the surrounding area when the lance (7) is inserted into the sealing housing (5).

Device for changing nozzles

Device for replacement of nozzles

The invention relates to the device which enables nozzles to be changed without changing the pressure conditions in the container or device associated therewith. According to the invention a connector piece support (2) is fixed to a pressurized container (1) wherein a medium (20) is guided into said container through a nozzle (8) by means of a lance (7). Said connector piece is connected to a sealing housing (5) by means of a locking device (3) in order to receive the lance (7). Sealing rings (13а, 13b, 13c) are arranged in the sealing housing (5) thereby ensuring pressure-tightness in relation to the container (1) and the surrounding area when the lance (7) is inserted into the sealing housing (5).

Device for changing nozzles

The invention relates to a device which enables nozzles to be changed without changing the pressure conditions in the container or device associated therewith. According to the invention a connector piece support (2) is fixed to a pressurised container (1) wherein a medium (20) is guided into said container through a nozzle (8) by means of a lance (7). Said connector piece is connected to a sealing housing (5) by means of a locking device (3) in order to receive the lance (7). Sealing rings (13a, 13b, 13c) are arranged in the sealing housing (5) thereby ensuring pressure-tightness in relation to the container (1) and the surrounding area when the lance (7) is inserted into the sealing housing (5).

Device for changing nozzles

The invention relates to a device which enables nozzles to be changed without changing the pressure conditions in the container or device associated therewith. According to the invention a connector piece support (2) is fixed to a pressurised container (1) wherein a medium (20) is guided into said container through a nozzle (8) by means of a lance (7). Said connector piece is connected to a sealing housing (5) by means of a locking device (3) in order to receive the lance (7). Sealing rings (13a, 13b, 13c) are arranged in the sealing housing (5) thereby ensuring pressure-tightness in relation to the container (1) and the surrounding area when the lance (7) is inserted into the sealing housing (5).