Single Layer Gas Processing

A process for converting carbon dioxide (CO2) gas into a medium BTU gas is disclosed. The CO2 gas may be injected into a reactor alone or simultaneously with a hydrocarbon gas and converted into a gas product suitable for further processing. The conversion process may include molten layers of iron and reactive slag in an upwardly flowing reactor operated under oxygen lean conditions.

METHOD AND APPLIANCE FOR SEPARATING A MIXTURE CONTAINING CARBON DIOXIDE BY CRYOGENIC DISTILLATION

In a method for separating at least one lighter impurity of a gaseous mixture containing at least 30% mol of carbon dioxide, a liquid () enriched with carbon dioxide is drawn off into a vat of a distillation column (), at least part () of the liquid enriched with carbon dioxide is vapourised and then heated to a first temperature higher than the boiling temperature thereof in the exchanger and leaves the exchanger at the hot end thereof, and at least part of the vapourised and heated liquid is sent from the hot end of the exchanger at the first temperature, without being cooled in the exchanger and without having been compressed, to the lower part of the distillation column, where it participates in the distillation while enriching itself. 110.-. (canceled)11. A method for separating at least one lighter impurity of a gaseous mixture containing at least 30% mol of carbon dioxide comprising:i) cooling the gaseous mixture in a heat exchanger, the heat exchanger comprising a hot end, the gaseous mixture entering the heat exchanger at the hot end, and the cooled gaseous mixture or a fluid derived from the gaseous mixture, this fluid containing at least 60% carbon dioxide, being separated by a distillation column, the distillation column having a head and a bottom part,ii) removing a liquid enriched in carbon dioxide from the distillation column and introduced into a tank,iii) drawing off a gas depleted in carbon dioxide and enriched in at least one lighter impurity at the head of the column and reheated in the heat exchanger,iv) sending at least a part of the liquid enriched in carbon dioxide the exchanger wherein at least one part of the liquid sent to the exchanger is vaporized and then heated to a first temperature higher than its boiling point in the exchanger and leaves from the exchanger at the hot end thereof, and at least a part of the vaporized and heated liquid is sent from the hot end of the exchanger at the first temperature, without being cooled in the ...

METHOD FOR DRYING CATALYTIC OXIDATION FURNACE

A method for drying a catalytic oxidation furnace, the method including: 1) charging a feed gas including oxygen and natural gas, and a temperature control gas to a catalytic oxidation furnace loaded with a catalyst; 2) preheating a mixed gas including the feed gas and the temperature control gas to increase the temperature of the mixed gas, and stopping the preheating when the temperature of the mixed gas achieves a temperature adapted to trigger the oxidation reaction of the mixed gas; and 3) within the molar ratio of the temperature control gas to the feed gas being 0.1-7:1.3-1.6, reducing the molar ratio of the temperature control gas to the feed gas such that the rise of the temperature of the mixed gas conforms to the temperature rising rate of the drying-out curve of a heat insulation refractory material of the catalytic oxidation furnace. 1. A method for drying a catalytic oxidation furnace , the method comprising:1) charging a feed gas comprising oxygen and natural gas, and a temperature control gas capable of reducing a reaction temperature rising rate to a catalytic oxidation furnace loaded with a catalyst, wherein a molar ratio of the oxygen to the natural gas in the feed gas is 0.3-0.6:1, and a molar ratio of the temperature control gas to the feed gas is 0.1-7:1.3-1.6;2) preheating a mixed gas comprising the feed gas and the temperature control gas to increase a temperature of the mixed gas, and stopping the preheating when the temperature of the mixed gas achieves a temperature adapted to trigger an oxidation reaction of the mixed gas; and3) within the molar ratio of the temperature control gas to the feed gas being 0.1-7:1.3-1.6, reducing the molar ratio of the temperature control gas to the feed gas so that a rise of the temperature of the mixed gas conforms to a temperature rising rate of a drying-out curve of a heat insulation refractory material of the catalytic oxidation furnace, and stopping charging the temperature control gas when the ...

Processing methane for syngas production with reduced co2 emissions

A method for processing methane includes processing methane in presence of a carbon dioxide stream, whereby a synthesis gas including carbon monoxide and hydrogen is produced. The synthesis gas is contacted with a carbon monoxide-absorbing solution, thereby removing at least a portion of the carbon monoxide and producing a final synthesis gas having an increased ratio of hydrogen to carbon monoxide.

CARBON DIOXIDE REDUCTION SYSTEM AND CARBON DIOXIDE REDUCTION METHOD

A carbon dioxide reduction system comprises a transport path that transports carbon dioxide and a reduction apparatus that reduces heated carbon dioxide introduced through the transport path wherein the carbon dioxide is heated in the transport path by at least one of recycled energy and exhaust heat. 1. A carbon dioxide reduction system comprising:a reduction apparatus that reduces carbon dioxide; anda transport path that transports carbon dioxide to the reduction apparatus, wherein the carbon dioxide is heated in the transport path by at least one of recycled energy and exhaust heat.2. The carbon dioxide reduction system according to claim 1 , wherein the recycled energy is produced by at least one selected from the group consisting of solar power generation claim 1 , wind power generation claim 1 , hydraulic power generation claim 1 , wave power generation claim 1 , tidal power generation claim 1 , biomass power generation claim 1 , geothermal power generation claim 1 , solar heat claim 1 , and underground heat.3. The carbon dioxide reduction system according to claim 1 , wherein the exhaust heat is heat generated in a combustion furnace.4. The carbon dioxide reduction system according to claim 1 , further comprising:a carbon dioxide separation apparatus,wherein the carbon dioxide in the transport path is carbon dioxide separated from an exhaust gas containing carbon dioxide by the carbon dioxide separation apparatus.5. The carbon dioxide reduction system according to claim 4 , further comprising:a combustion furnace,wherein the exhaust gas is exhaust gas generated in the combustion furnace, and the transport path is a circulation path that circulates the carbon dioxide so that the carbon dioxide is heated by the heat generated in the combustion furnace.6. The carbon dioxide reduction system according to claim 5 , further comprising:a heat exchanger that cools the exhaust gas containing carbon dioxide generated in the combustion furnace,wherein the circulation ...

SYSTEMS AND METHODS FOR CARBON MONOXIDE PRODUCTION BY REDUCTION OF CARBON DIOXIDE WITH ELEMENTAL SULFUR

Thermoneutral systems and methods for producing carbon monoxide (CO) and sulfur dioxide (SO) are disclosed. The systems can include a first reaction zone and a second reaction zone, where heat generated in the first reaction zone is sufficient to drive a carbon dioxide gas (CO(g)) and elemental sulfur gas (S(g)) reaction to produce a product stream that includes CO(g) and SO(g). 1. A system for producing carbon monoxide (CO) and sulfur dioxide (SO) , the system comprising:(a) a first reaction zone configured to produce heat from an exothermic reaction of a first reaction mixture and a first product stream;{'sub': 2', '2, '(b) a second reaction zone comprising a gaseous reaction mixture of carbon dioxide (CO(g)) and elemental sulfur and configured to receive the produced heat from the first reaction zone in an amount sufficient to heat the gaseous reaction mixture and produce a second product stream comprising CO and SO;'}(c) a first outlet in fluid communication with the first reaction zone and configured to remove the first product stream from the first reaction zone; and{'sub': '2', '(d) a second outlet in fluid communication with the second reaction zone and configured to remove the second product stream comprising CO and SOfrom the second reaction zone.'}2. The system of claim 1 , wherein exothermic first reaction mixture comprises carbonyl sulfide (COS) and oxygen source oxygen (O) and the first product stream comprises COand SO.3. The system of claim 1 , wherein the second reaction zone encompasses the first reaction zone.4. The system of claim 3 , wherein the first reaction zone and the second reaction zone form a concentric reactor claim 3 , and wherein the first reaction zone is the annulus of the concentric reactor.5. The system of claim 1 , wherein the first product stream absorbs heat from the exothermic reaction claim 1 , and the system further comprises a heat exchanging unit in fluid communication with the first outlet and the second reaction zone and ...

PROCESS FOR PURIFYING A SYNTHESIS GAS

The present invention provides for a pressure swing adsorption (PSA) process for the substantial removal of HO and COfrom a synthesis gas to obtain a multicomponent product gas substantially free of HO and COwith high recovery of the product gas. Further, the present invention provides an integrated process that achieves sufficiently high Hand CO recoveries such that compression and recycling of the syngas purification PSA tailgas is not necessary to be economically advantageous compared to the conventional processes. 1. An integrated process for the individual recovery of at least a purified H-rich gas and a purified CO-rich gas from a hydrocarbon feedstock comprising:{'sub': 2', '4', '2', '2, 'a. introducing a hydrocarbon feedstock into a syngas generating unit and generating a superatmospheric pressure syngas stream consisting essentially of at least H, CO, CH, CO, and HO;'}{'sub': 2', '2, 'b. feeding the generated superatmospheric pressure syngas stream to a pressure swing adsorption (PSA)-based purification process unit to produce a superatmospheric pressure syngas stream substantially free of HO and CO,'}{'sub': 2', '2', '2, 'c. routing the superatmospheric pressure syngas stream substantially free of HO and COto a separation system producing at least a H-rich stream and a CO-rich stream; and'}{'sub': 2', '2', '2', '2, 'd. wherein the PSA-based purification process unit is purged with high-purity Nstream for a first portion of a purge phase and with H-containing gas substantially free of HO and COfor a second portion of the purge phase.'}2. The integrated process of claim 1 , wherein the syngas generation system is selected from a steam reformer claim 1 , an autothermal reformer claim 1 , or a partial oxidation reactor.3. The integrated process of claim 1 , wherein the hydrocarbon feedstock is natural gas.4. The integrated process of claim 1 , wherein the high-purity Na stream used during the first portion of the purge phase is generated by a cryogenic air ...

ELECTROLYTIC CELL AND ELECTROLYTIC DEVICE

An electrolytic cell capable of simply electrolyzing carbon dioxide into carbon monoxide and oxygen with low activation energy, and an electrolytic device. The carbon dioxide electrolytic cell includes a cathode, an anode, and a solid electrolyte having oxide ion conductivity. The cathode is the following (A) or (B); (A) a metal and a first mayenite-type compound are included therein or (B) a metal and a second mayenite-type compound are included therein, said second mayenite type compound including a mayenite type compound having electron conductivity. 1. A electrolytic cell comprising:a cathode,an anode, anda solid electrolyte having oxide ion conductivity;whereinthe cathode is following (A) or (B):(A) the cathode comprises a metal and a first mayenite-type compound, or(B) the cathode comprises a metal and a second mayenite-type compound, wherein the second mayenite-type compound comprises a mayenite-type compound having electronic conductivity;{'sub': 2', '3, 'each of the first mayenite-type compound and the second mayenite-type compound is a mayenite-type compound having a representative composition represented by 12CaO.7AlO;'}the first mayenite-type compound and the second mayenite-type compound are the same or different; and{'sub': 2', '3, 'the mayenite-type compound comprises Al and at least one element selected from the group consisting of Ca and Sr, and a molar ratio of a sum of CaO and SrO to AlOin terms of oxides is 12.6:6.4 to 11.7:7.3.'}2. The electrolytic cell according to claim 1 ,wherein the mayenite-type compound comprises:(i) at least one element selected from the group consisting of B, Si and Ge, and total amount thereof is 0 to 17 mol % in terms of oxides with respect to the mayenite-type compound;(ii) at least one element selected from the group consisting of Li, Na, and K, and total amount thereof is 0 to 5 mol % in terms of oxides with respect to the mayenite-type compound;(iii) at least one element selected from the group consisting of Mg and ...

Carrier for synthesis gas production catalyst, method of manufacturing the same, synthesis gas production catalyst, method of manufacturing the same and method of producing synthesis gas

This invention provides a carrier for a synthesis gas production catalyst that can suppress carbon depositions and allows to efficiently produce synthesis gas on a stable basis for a long duration of time when producing synthesis gas by carbon dioxide reforming. It is a carrier to be used for producing synthesis gas containing carbon monoxide and hydrogen from source gas containing methane-containing light hydrocarbons and carbon dioxide. The carrier contains magnesium oxide grains and calcium oxide existing on the surfaces of magnesium oxide grains. The calcium oxide content thereof is between 0.005 mass % and 1.5 mass % in terms of Ca.

A PROCESS AND REACTOR FOR CONVERTING CARBON DIOXIDE INTO CARBON MONOXIDE

A process for converting carbon dioxide and hydrogen into a product stream comprising carbon monoxide, water and hydrogen by introducing carbon dioxide, hydrogen and oxygen into a reaction vessel, and performing a reverse water gas shift reaction at elevated temperature, wherein 1. A process for converting carbon dioxide and hydrogen into a product stream comprising carbon monoxide , water and hydrogen , the process comprising introducing carbon dioxide , hydrogen and oxygen into a reaction vessel , and performing a reverse water gas shift reaction at elevated temperature , wherein(a) no catalyst is present in the reaction vessel, and(b) at least a gas stream comprising carbon dioxide, a hydrogen rich gas stream and an oxygen rich gas stream are introduced into the reaction vessel in separate feed streams, wherein the hydrogen rich gas stream is introduced into the reaction vessel at a temperature between 15 and 450° C.,(c) the hydrogen rich gas stream and oxygen rich gas stream being introduced in close vicinity of each other, wherein at least the hydrogen rich gas stream and the oxygen rich gas stream are introduced into the reaction vessel via a burner comprising coaxial channels for the separate introduction of the different gas streams, the burner being located at the top of the reaction vessel, wherein the hydrogen and oxygen in the hydrogen rich gas stream and oxygen rich gas stream undergo a combustion reaction upon entering the reaction vessel, thereby providing the heating energy required for the reverse water-gas shift reaction; and(d) the temperature in the reaction vessel is maintained in the range of 1000 to 1500° C. by varying the molar ratio of hydrogen to oxygen, which are introduced into the reaction vessel in the hydrogen rich gas stream and oxygen rich gas stream, respectively.2. The process according to claim 1 , wherein in step (c) the hydrogen rich gas stream and oxygen rich gas stream are introduced into the reaction vessel in close vicinity ...

PROCESS AND APPARATUS FOR THE CRYOGENIC SEPARATION OF A MIXTURE OF CARBON MONOXIDE, HYDROGEN AND METHANE FOR THE PRODUCTION OF CH4

In a process of the separation of a mixture of carbon monoxide, hydrogen and methane, the mixture is sent to a scrubbing column, a bottom liquid withdrawn at the bottom of the scrubbing column is depleted in hydrogen with respect to the mixture and is sent to a stripping column, a bottom liquid from the stripping column is sent to a separation column and a liquid enriched in methane withdrawn from the bottom of the separation column is vaporized in order to form a final product. 1. A process for the separation of a mixture of carbon monoxide , hydrogen and methane , the process comprising the steps of:i) sending the mixture or a fluid derived from this mixture, after cooling to a cryogenic temperature in a heat exchanger, to a scrubbing column fed at the top with a liquid containing at least 80 mol % of carbon monoxide or to at least one phase separator;ii) withdrawing a bottom liquid at the bottom of the scrubbing column or of the phase separator or of one of the phase separators is depleted in hydrogen with respect to the mixture and is sent to a stripping column;iii) withdrawing a gas at the top of the stripping column;iv) sending a bottom liquid from the stripping column to a separation column; andv) withdrawing a liquid enriched in methane from the bottom of the separation column and vaporized in the heat exchanger in order to form a final product,wherein the vaporized liquid enriched in methane is compressed in a compressor and a part of the compressed gas is returned at the bottom of the separation column for separation therein.2. The process according to claim 1 , in which the part of the compressed gas is at a lower pressure than that of the compressed final product.3. The process according to claim 1 , in which the scrubbing column is fed at the top with a liquid originating from a condenser where at least a part of the gas from the top of the scrubbing column or originating from the top of the separation column or originating from a cycle for ...

METHOD AND APPARATUS FOR SEPARATION OF 13C16O FROM NATURAL CO

Method and Apparatus for separating at least one CO isotope compound, especially isotope compound 13C16O, from natural CO, comprising: 1. Method for separating at least one CO isotope compound , especially isotope compound 13C16O , from natural CO , comprising:{'b': 110', '112', '114', '116', '118', '120', '112, 'i': 'b', 'operating a rectification column system (), comprising a plurality of rectification sections (,,,,) arranged adjacent to one another in a chain-like manner, including an upper rectification section and a plurality of lower rectification sections, wherein maintaining evaporation of liquid present in the rectification column is achieved by heating the liquid by heating means provided in each rectification section, wherein the heating of at least one of the plurality of rectification sections is provided by heating means comprising a heat pump cycle (), wherein preferably the heating at the least one further one of the plurality of rectification sections is provided by means comprising an electrical heater.'}2132112122112. Method according to claim 1 , wherein the heating in the upper rectification section is provided to utilize a heat pump cycle connecting a reboiler () of the upper rectification section () and a condenser () associated with upper rectification section ().3. Method according to claim 1 , wherein pressures within the rectification column system range from 0.5 bar abs in the upper rectification section to around 3 bar abs in a lowermost rectification section.4. Method according to claim 1 , wherein temperatures within the rectification column system range from 77K in the upper rectification section to around 95 K in a lowermost rectification section.5122210220. Method according to claim 1 , wherein the liquefied working fluid of the heat pump cycle is supplied to the condenser () using at least one pump ( claim 1 ,).6. Method according to claim 1 , wherein the working fluid of the heat pump cycle is nitrogen.7. Method according to ...

Fe-N-C CATALYST, METHOD OF PREPARATION AND USES THEREOF

The invention relates to single-atom Fe catalysts useful for the electrochemical reduction of carbon dioxide, method of preparation as uses thereof. In particular, the invention relates to a method of preparation of Fe(II) doped Zn-ZIF precursor material and use thereof in the preparation of a catalyst containing Fe single atoms on N doped carbon matrix derived from the pyrolysis of this Fe(II) doped Zn-ZIF precursor material. 121-. (canceled)22. A method for the electroreduction of COto CO comprising electroreducing COin the presence of a catalyst material containing Fe single atom on N doped carbon matrix prepared from a Fe(II)-doped Zn-zeolitic imidazole framework (ZIF).23. The method according to claim 22 , wherein the catalyst material is obtained from the pyrolysis of a Fe(II)doped-Zn-ZIF-8.24. The method according to claim 22 , wherein said catalyst material contains Fe single atom on N doped carbon matrix.25. The method according to claim 22 , wherein said Fe(II)-doped Zn-ZIF is has a crystal structure of Zn-ZIF-8 wherein some Zn(II) ions are substituted by Fe(II) ions.26. A method for the preparation of a catalyst material comprising the steps of:a) providing a Fe(II)-doped Zn-zeolitic imidazole framework (ZIF) in dried form under inert atmosphere;b) subjecting said Fe(II)-doped Zn-ZIF to a pyrolysis under inert atmosphere during about 2 to about 24 hours, typically 3 hours; andc) collecting the obtained pyrolysis product as a catalyst material.27. The method according to claim 26 , wherein the pyrolysis under step b) is carried out at a temperature between about 800 and 950° C.28. The method according to claim 26 , wherein the pyrolysis under step b) is carried out through the ramping of temperature at a rate of about 3 to 10° C. mid′.29. The method according to claim 26 , wherein the inert atmosphere is provided by a Nflow.30. The method according to claim 26 , wherein said Fe(II)-doped Zn-ZIF has a crystal structure of Zn-ZIF-8 wherein some Zn(II) ions ...

METHOD AND APPARATUS FOR PRODUCING ORGANIC SUBSTANCES

It is an object of the present invention to convert COto CO by bringing about a reverse shift reaction in a relatively low-temperature condition, and thereby enhancing efficiency of generating organic substances, such as ethanol. A raw material gas g containing COand His subjected to a reverse shift reaction in a reverse shift reactor Organic substances are generated from a raw material gas g after the reverse shift reaction in an organic substance generator In the subjecting step, the raw material gas g is brought into contact with a reverse shift reaction catalyst The reverse shift reaction catalyst includes a support and a catalyst metal supported by the support The catalyst metal includes a transition metal. The catalyst metal is preferably composed of Fe with at least one kind of metal from among Al, Ga, In, Cu, Ag, Au, Pd and Mn added thereto. 1. A method for producing organic substances from a raw material gas containing COand H , the method comprising steps of:subjecting the raw material gas to a reverse shift reaction; andgenerating organic substances from the raw material gas after the reverse shift reaction, wherein:the raw material gas is contacted with a reverse shift reaction catalyst in the subjecting step;the reverse shift reaction catalyst includes a support and a catalyst metal supported by the support; andthe catalyst metal includes a transition metal.2. The method according to claim 1 , wherein the catalyst metal includes Fe with at least one kind of metal selected from a group of Al claim 1 , Ga claim 1 , In claim 1 , Cu claim 1 , Ag claim 1 , Au claim 1 , Pd claim 1 , and Mn added thereto.3. The method according to claim 1 , wherein the catalyst metal includes Fe with Pd added thereto.4. The method according to claim 1 , wherein a temperature condition in the subjecting step is from 150 degrees C. to 500 degrees C.5. The method according to claim 1 , wherein an offgas generated in the generating step is mixed with the raw material gas before ...

DEVICES, SYSTEMS, FACILITIES, AND PROCESSES FOR LIQUEFIED NATURAL GAS PRODUCTION

Devices, systems, and methods for liquefied natural gas production facilities are disclosed herein. A liquefied natural gas (LNG) production facility includes a liquefaction unit and a gas turbine. The liquefaction unit condenses natural gas vapor into liquefied natural gas. Fuel to the gas turbine contains at least about 90% hydrogen by volume.

PD-CATALYZED DECOMPOSITION OF FORMIC ACID

Process for Pd-catalyzed decomposition of formic acid 2. Process according to claim 1 ,wherein the compound in process step b) is selected from:{'sub': 2', '2', '3', '3', '2', '2', '3', '2, 'Pd(acac), PdCl, Pd(dba)*CHCl (dba=dibenzylideneacetone), Pd(OAc), Pd(TFA), Pd(CHCN)Cl.'}3. Process according to claim 1 ,{'sub': '2', 'wherein the compound in process step b) is Pd(OAc).'}4. Process according to claim 1 ,wherein the process comprises additional process step f):f) addition of an acid.5. Process according to claim 4 ,{'sub': 2', '4', '3', '3', '3', '3, 'wherein the acid in process step f) is selected from: HSO, CHSOH, CFSOH, PTSA.'}6. Process according to claim 4 ,wherein the acid in process step f) is PTSA.7. Process according to claim 1 ,{'sup': 1', '2', '3', '4, 'sub': 1', '12', '1', '12', '4', '14', '4', '14', '1', '12', '1', '12', '3', '14', '3', '14', '2, 'wherein R, R, R, Rare each independently selected from: —(C-C)-alkyl, —O—(C-C)-alkyl, —(C-C)-aryl, —O—(C-C)-aryl, cycloalkyl, —(C-C)-heteroalkyl, —O—(C-C)-heteroalkyl, —(C-C)-heteroaryl, —O—(C-C)-heteroaryl, —COO-alkyl, —COO-aryl, —C—O-alkyl, —C—O-aryl, NH, halogen and the residues are also capable of forming a larger condensed ring;'}wherein the recited alkyl groups, aryl groups, cycloalkyl, heteroalkyl groups, heteroaryl groups may be substituted as follows:{'sub': 1', '12', '1', '12, '—(C-C)-alkyl, —O—(C-C)-alkyl, halogen;'}{'sup': 1', '2', '3', '4, 'and at least one of the radicals R, R, R, Rdoes not represent phenyl.'}8. Process according to claim 1 ,{'sup': 1', '2', '3', '4, 'sub': 1', '12', '4', '14', '1', '12', '3', '14, 'wherein R, R, R, Rare each independently selected from: —(C-C)-alkyl, —(C-C)-aryl, cycloalkyl, —(C-C)-heteroalkyl, —(C-C)-heteroaryl, halogen and the residues are also capable of forming a larger condensed ring;'}wherein the recited alkyl groups, aryl groups, cycloalkyl, heteroalkyl groups, heteroaryl groups may be substituted as follows:{'sub': 1', '12', '1', '12, '—(C-C)-alkyl, ...

METHOD AND APPLIANCE FOR SEPARATING A SYNTHESIS GAS BY CRYOGENIC DISTILLATION

The invention relates to a method for separating a synthesis gas comprising hydrogen and carbon monoxide by cryogenic distillation, according to which the synthesis gas () is cleaned and cooled to a cryogenic temperature, the cooled synthesis gas is separated by a first means () in order to produce a hydrogen-depleted liquid (), the hydrogen-depleted liquid is introduced into the upper part of a stripping column () and a hydrogen-enriched gas () is drawn off at the head of the stripping column, at least partially condensed and sent back to the upper part of the stripping column. 1. A process for the separation of a synthesis gas comprising hydrogen , carbon monoxide and methane , and possibly nitrogen , by cryogenic distillation , in which:{'b': 1', '5, 'i) the synthesis gas (, ) is purified and cooled down to a cryogenic temperature,'}{'b': 9', '15', '91', '15, 'ii) the cooled synthesis gas is separated by a first means (, ) in order to produce a liquid depleted in hydrogen (), the separation carried out by the first means consists of a stage of scrubbing in a scrubbing column () with at least a part of the liquid enriched in methane withdrawn from a column for the separation of carbon monoxide and methane having an overhead condenser, the condenser being cooled by a carbon monoxide cycle, and'}{'b': '25', 'iii) the liquid depleted in hydrogen is introduced into the upper part of a stripping column () which also comprises a lower part,'}{'b': 27', '29, 'iv) a gas enriched in hydrogen (, ) is withdrawn at the top of the stripping column,'}{'b': 33', '45', '43', '77', '29, 'v) a liquid () is withdrawn at the bottom of the stripping column and sent to the separation column (), a gas () enriched in carbon monoxide and depleted in methane is withdrawn at the top of the separation column, a liquid () depleted in carbon monoxide and enriched in methane is withdrawn at the bottom of the separation column and the gas enriched in carbon monoxide is heated by heat exchange ...

CARBON DIOXIDE PHOTO-REACTOR

According to the inventive concept, a carbon dioxide photo-reactor includes a body having a closed interior space, provided with a photocatalytic material in the interior space, and that generates a reaction gas and a liquefied fluid from carbon dioxide through a photoconversion reaction, a gas injector that provides a passage, through which the carbon dioxide flows, a vapor injector that provides a passage, through which vapor flows, a gas discharger, through which the generated reaction gas is discharged, a liquid discharger, through which the generated liquefied fluid is discharged, and at least one elongate structure disposed to cross the interior space in a predetermined direction. 1. A carbon dioxide photo-reactor comprising:a body having a closed interior space, provided with a photocatalytic material in the interior space, and configured to generate a reaction gas and a liquefied fluid from carbon dioxide through a photoconversion reaction;a gas injector configured to provide a passage, through which the carbon dioxide flows;a vapor injector configured to provide a passage, through which vapor flows;a gas discharger, through which the generated reaction gas is discharged;a liquid discharger, through which the generated liquefied fluid is discharged; andat least one elongate structure disposed to cross the interior space in a predetermined direction.2. The carbon dioxide photo-reactor of claim 1 , wherein the body forms a hexahedral shape by coupling a plurality of transparent flat plates such that the plurality of transparent flat plates are separable from each other claim 1 , andwherein, among the plurality of transparent flat plates, a transparent flat plate, to which light is input from a light source, is formed of quartz.3. The carbon dioxide photo-reactor of claim 1 , wherein the body further includes:a ventilation plate disposed at a location that is spaced apart from a bottom surface by a predetermined distance, and through which the liquefied fluid ...

SELECTIVE, ADSORBATE-INDUCED SPIN STATE CHANGES IN TRANSITION METAL-BASED METAL-ORGANIC FRAMEWORKS

An adsorbate-selective metal organic framework includes a transition metal; and a plurality of organic molecules coordinated to the transition metal so as to preserve open coordination sites for selectively adsorbing molecules that have low-lying π* orbitals. The transition metal has a lowest energy spin state in the presence of the selectively adsorbed molecules that are strongly bonding to the transition metal through π-donating interactions which is different than the lowest energy spin state in the absence of these adsorbed molecules. The transition metal has also a lowest energy spin state in the presence of non-selected molecules that are weakly bonding to the transition metal through σ- and/or π-accepting and/or donating interactions. 2. The adsorbate-selective metal organic framework according to claim 1 , wherein said transition metal is switchable to a higher energy spin state by controlling a temperature or a pressure claim 1 , or both in said adsorbate selective metal organic framework to enable desorption of said selectively adsorbed molecules.3. The adsorbate-selective metal organic framework according to claim 2 , wherein said transition metal is switchable to a higher energy spin state by increasing the temperature or lowering the pressure claim 2 , or both in said adsorbate selective metal organic framework to enable desorption of said selectively adsorbed molecules.4. The adsorbate-selective metal organic framework according to claim 1 , wherein said transition metal is selected from the group of transition metals consisting of vanadium claim 1 , chromium claim 1 , manganese claim 1 , iron claim 1 , cobalt claim 1 , nickel claim 1 , and copper.5. The adsorbate-selective metal organic framework according to claim 1 , wherein said transition metal is iron.7. The adsorbate-selective metal organic framework according to claim 1 , wherein said transition metal is iron claim 1 , and wherein said plurality of organic molecules are one of HBTTri claim 1 , ...

Thermally Stable Monolith Catalysts for Methane Reforming and Preparing Method of the Same

The present invention relates to a monolith catalyst for carbon-dioxide/methane reforming and a method of manufacturing the same, and more particularly to a novel monolith catalyst for a reforming reaction having improved thermal durability, configured such that a sintering inhibiting layer is formed by coating the surface of a monolith support with at least one element selected from the group consisting of Group 2, 3, 6, 13, 15 and 16 elements among elements in Period 3 or higher and an active catalyst layer is formed on the sintering inhibiting layer, thereby preventing carbon deposition and catalyst deactivation due to deterioration even upon reaction at high temperatures.

METHOD AND APPARATUS FOR THE CRYOGENIC SEPARATION OF A SYNTHESIS GAS CONTAINING A NITROGEN SEPARATION STEP

A method for separating a gas mixture comprising carbon monoxide, nitrogen and hydrogen involves sending a hydrogen-depleted fluid to a denitrification column (K) having a top condenser (C) and a bottom reboiler (R) in order to produce a nitrogen-enriched gas at the top of the column and a nitrogen-depleted liquid at the bottom of the column, cooling the condenser of the denitrification column by means of a nitrogen cycle using a nitrogen compressor (V, V, V), vaporising, in the heat exchanger of the condenser, the liquid nitrogen () from the nitrogen cycle, and returning the nitrogen () vaporised in the heat exchanger to the nitrogen compressor. 113.-. (canceled)14. A process for separating a gas mixture comprising carbon monoxide , nitrogen , hydrogen , and methane , the method comprising:i) cooling the gas mixture in a heat exchanger,ii) separating the gas mixture cooled in the heat exchanger by at least one scrubbing and/or distillation and/or partial condensation step, to form a hydrogen-depleted fluid containing carbon monoxide and nitrogen,iii) introducing the hydrogen-depleted fluid into a denitrification column comprising a column top, a top condenser, a column bottom, and a bottom reboiler, thereby producing a nitrogen-enriched gas at the column top and a nitrogen-depleted liquid at the column bottom,iv) cooling the top condenser by means of a nitrogen cycle using a nitrogen compressor comprising at least a first stage and a second stage, the first stage comprising a first entry pressure and the second stage comprising a second entry pressure, the first entry pressure being lower than that of the second entry pressure,v) expanding the nitrogen-depleted liquid and sending the expanded nitrogen-depleted liquid to the top condenser wherein it is at least partially vaporized by heat exchange in the condenser with the nitrogen-enriched gas, thereby condensing the expanded nitrogen-depleted liquid, a) sending the bottom liquid from the denitrification column to ...

PROCESS AND PLANT FOR SEPARATING A GAS MIXTURE

A process and plant are proposed for separating a feed mixture predominantly or exclusively containing carbon monoxide and hydrogen, in which the feed mixture is subjected to a cryogenic separation process in which a carbon monoxide-rich liquid and at least one residual gas mixture which is depleted in carbon monoxide and enriched in hydrogen, in comparison with the feed mixture, are formed. It is intended that the at least one residual gas mixture is subjected to a membrane separation process in which at least one hydrogen-rich permeate and at least one carbon monoxide-rich retentate are formed, wherein the or at least one of the carbon monoxide-rich retentates is recirculated to the cryogenic separation process. 1. A process for separating a feed mixture predominantly or exclusively containing carbon monoxide and hydrogen , in which the feed mixture is subjected to a cryogenic separation process in which a carbon monoxide-rich liquid and at least one residual gas mixture which is depleted in carbon monoxide and enriched in hydrogen , in comparison with the feed mixture , are formed , characterized in that the at least one residual gas mixture is subjected to a membrane separation process in which at least one hydrogen-rich permeate and at least one carbon monoxide-rich retentate are formed , wherein the or at least one of the carbon monoxide-rich retentates is recirculated to the cryogenic separation process.2. The process according to claim 1 , in which the membrane separation process comprises a first membrane separation step and a second membrane separation step claim 1 , wherein claim 1 , in the first membrane separation step claim 1 , a first hydrogen-rich permeate and a first carbon monoxide-rich retentate are formed claim 1 , and in the second membrane separation step claim 1 , a second hydrogen-rich permeate and a second carbon monoxide-rich retentate are formed.3. The process according to claim 2 , in which the first hydrogen-rich permeate is transferred ...

LIGHT DRIVEN METAL PINCER PHOTOCATALYSTS FOR CARBON DIOXIDE REDUCTION TO CARBON MONOXIDE

Disclosed are N-heterocyclic carbene (NHC) and 4-pyridinol-derived pincer ligands and metal complexes containing these ligands. These compounds can be used to photocatalyticaly reduce COto CO. 2. The compound of claim 1 , wherein Ris OH claim 1 , O claim 1 , halogen claim 1 , or optionally substituted amine claim 1 , alkyl claim 1 , aryl claim 1 , alkoxyl claim 1 , or aryloxyl.3. The compound of claim 1 , wherein Ris alkoxyl.4. The compound of claim 1 , wherein Rand Rcombine together with the atoms to which they are attached to form an aryl or heteroaryl.5. The compound of claim 1 , wherein Rand Rare both hydrogen.6. The compound of claim 1 , wherein M is Ni claim 1 , Ru claim 1 , Fe claim 1 , Co claim 1 , or Ir.7. The compound of claim 1 , wherein at least one L is Cl claim 1 , Br claim 1 , CHCN claim 1 , DMF claim 1 , HO claim 1 , bipyridine or phenylpyridine.9. The compound of claim 1 , further comprising one or more counteranions selected from I claim 1 , Br claim 1 , CFCOO claim 1 , BF claim 1 , or PF.11. The catalytic system of claim 10 , further comprising a photosensitizer.12. The catalytic system of claim 10 , wherein the photosensitizer is Ru(bpy) claim 10 , Ir(ppy) claim 10 , Cu(dmbpy) claim 10 , Os(bpy) claim 10 , Ru(phen) claim 10 , or a derivative or a mixture thereof.13. The catalytic system of claim 10 , wherein the system does not include a photosensitizer.14. The catalytic system of claim 13 , wherein Rand Rcombine together with the atoms to which they are attached to form an aryl or heteroaryl.15. The catalytic system of claim 10 , wherein the electron donor is an amine or alcohol.16. The catalytic system of claim 15 , wherein the electron donor is trimethylamine claim 15 , triethanolamine (TEOA) claim 15 , (1 claim 15 ,3-dimethyl-2-phenyl-2 claim 15 ,3-dihydro-1H-benzo[d]imidazole) (BIH) claim 15 , 1-benzyl-1 claim 15 ,4-dihydropyridine-3-carboxamide (BNAH); 1-(4-methoxybenzyl)-1 claim 15 ,4-dihydropyridine-3-carboxamide (BNAH-OMe) claim 15 , 5-( ...

PROCESS AND APPARATUS FOR STEAM REFORMING

A process and an apparatus for generating a hydrogen- and/or carbon monoxide-comprising gas product, wherein a hydrocarbon feed formed from a hydrocarbons-containing starting material is supplied together with superheated steam to a steam reforming proceeding at elevated pressure to obtain a hydrogen- and carbon monoxide-containing crude synthesis gas from which the gas product is derived are disclosed. The boiler feed water is supplied at a pressure higher than its critical pressure with heat to obtain supercritical water of which subsequently at least a portion is employed as propelling medium in a steam jet ejector by means of which the hydrocarbon feed and/or a substance employed for the formation thereof are compressed. 1. A process for generating a hydrogen- and/or carbon monoxide-comprising gas product , wherein a hydrocarbon feed formed from a hydrocarbons-containing starting material is supplied together with superheated steam to a steam reforming proceeding at elevated pressure to obtain a hydrogen- and carbon monoxide-containing crude synthesis gas from which the gas product is derived , characterized in that boiler feed water is supplied at a pressure higher than its critical pressure with heat to obtain supercritical water of which subsequently at least a portion is employed as propelling medium in a steam jet ejector by means of which the hydrocarbon feed and/or a substance employed for the formation thereof are compressed.2. The process according to claim 1 , characterized in that during compression of the hydrocarbon feed in the steam jet ejector a substance mixture is formed which meets the requirements of steam reforming on account of its composition and/or has a pressure allowing supply to the steam reforming without further compression.3. The process according to claim 1 , characterized in that the boiler feed water is heated in indirect heat exchange against flue gas from which heat is removed beforehand for the steam reforming.4. The process ...

ELECTROCHEMICAL REACTION DEVICE

An electrochemical reaction device, comprises: an anode to oxidize a first substance; a first flow path facing on the anode and through which a liquid containing the first substance flows; a cathode to reduce a second substance; a second flow path facing on the cathode and through which a gas containing the second substance flows; a porous separator provided between the anode and the cathode; and a power supply connected to the anode and the cathode. A thickness of the porous separator is 1 μm or more and 500 μm or less. An average fine pore size of the porous separator is larger than 0.008 μm and smaller than 0.45 μm. A porosity of the porous separator is higher than 0.5. 1. An electrochemical reaction device , comprising:an anode to oxidize a first substance;a first flow path facing on the anode and through which a liquid containing the first substance flows;a cathode to reduce a second substance;a second flow path facing on the cathode and through which a gas containing the second substance flows;a porous separator provided between the anode and the cathode; anda power supply connected to the anode and the cathode,wherein a thickness of the porous separator is 1 μm or more and 500 μm or less,an average fine pore size of the porous separator is larger than 0.008 μm and smaller than 0.45 μm, anda porosity of the porous separator is higher than 0.5.2. The device according to claim 1 ,wherein the cathode includes:a porous conductive layer having a first surface and a second surface; anda reduction catalyst layer provided on the first surface and containing a reduction catalyst to reduce the second substance,the second flow path faces on the second surface, andthe porous conductive layer has water repellency.3. The device according to claim 1 ,wherein the porous separator is hydrophilic.4. The device according to claim 1 ,{'sup': −20', '−16, 'wherein a coefficient of permeability of the porous separator is 1.7×10or more and 1.7×10or less.'}5. The device according to ...

SYNTHESIS GAS MANUFACTURING METHOD AND SYNTHESIS GAS MANUFACTURING APPARATUS

A method of manufacturing synthesis gas by catalytic partial oxidation can prevent formation of hot spots from taking place when driving mixture gas to pass through a catalyst-filled layer at high velocity. The method comprises converting mixture gas of source gas containing lower hydrocarbons and oxidative gas containing oxygen into synthesis gas containing hydrogen and carbon monoxide as main components thereof by causing mixture gas to flow through a fixed bed catalyst layer arranged in a reactor. The method of manufacturing synthesis gas by catalytic partial oxidation is conducted such that the mixture gas is made to flow to the catalyst layer under the condition that the Reynolds number does not exceed 20 at the inlet of the catalyst layer. 1. A method of manufacturing synthesis gas by catalytic partial oxidation , comprising causing mixture gas of source gas containing lower hydrocarbons and oxidative gas containing oxygen to flow through a fixed bed catalyst layer in a reactor and thereby converting the mixture gas into synthesis gas containing hydrogen and carbon monoxide as main components thereof , characterized in that the mixture gas is caused to flow through the catalyst layer under a condition where the Reynolds number does not exceed 20 at the inlet of the catalyst layer.2. The method according to claim 1 , wherein the gas flow velocity of the mixture gas in a mixture gas feed flow path reaching to the catalyst layer is not less than the critical burning velocity.3. The method according to claim 1 , wherein the temperature of the mixture gas is lower than the self-ignition temperature of the lower hydrocarbons at the inlet of the catalyst layer.4. The method according to claim 1 , wherein the mixture gas is obtained by separately introducing the source gas and the oxidative gas into a mixing vessel and then mixing the source gas and the oxidative gas in the mixing vessel.5. The method according to claim 1 , wherein the lower hydrocarbons comprise ...

CERIA-SUPPORTED METAL CATALYSTS AND PROCESSES

Provided herein are catalyst materials and processes for processing hydrocarbons. For example, doped ceria-supported metal catalysts are provided exhibiting good activity and stability for commercially relevant DRM process conditions including low temperature and long term operation. 2. (canceled)3. The method of claim 1 , wherein said method is for production of a syngas product and/or for dry reforming of methane.4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. The method of claim 1 , wherein said hydrocarbon feedstock is obtained or derived from an industrial process that generates both carbon dioxide and methane or an industrial process that generates carbon dioxide in proximity to a source of methane.9. (canceled)10. The method of claim 1 , wherein said hydrocarbon feedstock comprises a product from one or more processes selected from the group of:i. a coal pyrolysis process;ii. a petrochemical oxidization process;iii. a sintering process;iv. a furnace process;v. a kiln process;vi. a steam reforming process;vii. an ammonia production process;viii. a fuel production or treatment process;ix. a mining process; andx. any process that produces carbon dioxide.11. (canceled)12. The method of claim 1 , wherein said doped ceria-supported metal catalyst comprises said one or more metals (M) dispersed on a doped catalyst support characterized by the formula CeBO; wherein said doped catalyst support maintains the structure of pure ceria and produces mixed metal oxides.13. (canceled)14. The method of claim 1 , wherein said one or more metals (M) are provided as particles or clusters having an average size dimension up to 1 micron and wherein the weight percent of said one or more metals (M) in the catalyst is selected from the range of 0.1-20 wt %.15. (canceled)16. The method of claim 1 , wherein said one or more metals (M) in formula (FX1) is Ni; and wherein Ni has a weight percent in the catalyst selected from the range of 1.5-7 wt %.17. (canceled)18. The method of ...

Thermochemical gas reduction process using poly-cation oxide

A two-step thermochemical gas reduction process based on poly-cation oxides includes repeatedly cycling a thermal reduction step and a gas reduction step. In the thermal reduction the poly-cation oxide is heated to produce a reduced poly-cation oxide and oxygen. In the gas reduction step, the reduced poly-cation oxide is reacted with a gas to reduce the gas, while reoxidizing the poly-cation oxide. The poly-cation oxide has at least two distinct crystal structures at two distinct temperatures and is capable of undergoing a reversible phase transformation between the two distinct crystal structures. For example, the poly-cation oxide may be an entropy tuned mixed metal oxide, such as an entropy stabilized mixed metal oxide, where the entropy-tuning is achieved via change in crystal structure of one of more of the compounds involved. The gas reduction process may be used for water splitting, COsplitting, NOreduction, and other gas reduction processes. 1. A two-step thermochemical gas reduction process comprising repeatedly cycling a thermal reduction step and a gas reduction step;{'sub': x', 'x-1', '2, 'wherein the thermal reduction step comprises heating a poly-cation oxide (MeO) under a reduced partial oxygen pressure, producing a reduced poly-cation oxide (MeO) and oxygen gas (O);'}{'sub': x-1', 'x, 'wherein the gas reduction step comprises reacting the reduced poly-cation oxide (MeO) with a first gas to produce a second gas and reoxidized poly-cation oxide (MeO), wherein the first gas is reduced into the second gas;'}{'sub': x', 'x-1, 'wherein the poly-cation oxide has at least two distinct crystal structures at two distinct temperatures corresponding to two distinct average oxidation states of at least one transition metal in a transformation between MeOand MeOand is capable of undergoing a reversible phase transformation between the two distinct crystal structures.'}2. The two-step thermochemical gas reduction process ofwherein the poly-cation oxide is an ...

TUNING PRODUCTS SELECTIVITY OF CO2 REDUCTION REACTION WITH SURFACE LIGANDS

Methods for preparing selective catalytic metal microstructures and nanostructures having at least one surface ligand. The methods include providing a preliminary metal microstructure or nanostructure having at least one preliminary surface ligand, and replacing the preliminary surface ligand with at least one surface ligand to provide the catalytic metal microstructure or nanostructure. 1. A method for preparing a catalytic metal structure comprising:providing a preliminary metal structure comprising at least one preliminary surface ligand, andreplacing the preliminary surface ligand with at least one surface ligand to provide the catalytic metal structure.2. The method according to claim 1 , wherein the catalytic metal structure comprises a metal selected from the group consisting of copper claim 1 , iron claim 1 , cobalt claim 1 , alloys thereof claim 1 , and combinations thereof.3. The method according to claim 1 , wherein the catalytic metal structure comprises a metal nanoparticle.4. The method according to claim 1 , wherein the catalytic metal structure comprises a metal microsheet.5. The method according to claim 1 , wherein the preliminary surface ligand is selected from the group consisting of oleylamine claim 1 , trioctylphosphine claim 1 , and combinations thereof.6. The method according to claim 1 , wherein providing the preliminary metal structure comprises preparing a metal complex claim 1 , andreacting the metal complex with the preliminary surface ligand to provide the preliminary metal structure.7. The method according to claim 1 , wherein the at least one surface ligand is selected from the group consisting of hydrazine claim 1 , ethylene diamine claim 1 , propylene diamine claim 1 , butane diamine claim 1 , trimethylamine claim 1 , acetic acid claim 1 , propionic acid claim 1 , butyric acid claim 1 , valeric acid claim 1 , octanethiol claim 1 , ethanethoil claim 1 , propanethoil claim 1 , butanethiol claim 1 , pentanethoil claim 1 , hexanethoil ...

PROCESS AND PLANT FOR THE COMBINATION PRODUCTION OF A MIXTURE OF HYDROGEN AND NITROGEN AND ALSO OF CARBON MONOXIDE BY CRYOGENIC DISTILLATION AND CRYOGENIC SCRUBBING

Process for the combined production of a mixture of hydrogen and nitrogen, and of carbon monoxide by cryogenic distillation and cryogenic scrubbing, wherein a methane-rich liquid is introduced at a first intermediate level of a scrubbing column as first scrubbing liquid and at least one nitrogen-rich liquid is introduced at a level higher than the first level of the scrubbing column as second scrubbing liquid and a mixture of hydrogen and nitrogen is drawn off as overhead gas from the scrubbing column. 110-. (canceled)11. A process for the combined production of a mixture of hydrogen and nitrogen , of carbon monoxide by cryogenic distillation and cryogenic scrubbing , wherein the process comprises the steps of:i) cooling, in a heat exchanger, a gas mixture containing at least hydrogen, carbon monoxide and methane;ii) sending the cooled mixture to a scrubbing column;iii) introducing a methane-rich liquid at a first intermediate level of the scrubbing column as a first scrubbing liquid;iv) introducing at least one nitrogen-rich liquid at a level higher than the first level of the scrubbing column as a second scrubbing liquid;v) withdrawing a mixture of hydrogen and nitrogen as an overhead gas from the scrubbing column;vi) withdrawing a first bottoms liquid from the scrubbing column and then sending said first bottoms liquid to a stripping column;vii) withdrawing a liquid that is level with an intermediate section of the scrubbing column and sending said liquid either to the heat exchanger, or to a stripping column overhead gas line, or to a second stripping column;viii) withdrawing a second bottoms liquid from the stripping column and then sending to a column configured to separate carbon monoxide and methane; andix) withdrawing a fluid rich in carbon monoxide from the separating column;x) withdrawing a third bottoms liquid from the separating column, wherein at least one portion of the third bottoms liquid from the separating column constitutes the methane-rich ...

LIGHT HYDROCARBON PARTIAL OXIDATION CATALYST AND CARBON MONOXIDE PRODUCTION METHOD USING SAME

The present disclosure relates to a partial oxidation catalyst that causes a light hydrocarbon partial oxidation reaction to proceed readily with high activity and high selectivity and a high-yield carbon monoxide production method using the same. The present disclosure further relates to a light hydrocarbon partial oxidation catalyst containing a zeolite supporting cobalt and rhodium. 1. A partial oxidation catalyst for a light hydrocarbon , comprising cobalt and rhodium-supported zeolite.2. The partial oxidation catalyst according to claim 1 , wherein an amount of the rhodium which is supported is 0.001% by weight or more and 0.01% by weight or less with respect to 100% by weight of the zeolite; and', 'a ratio of the amount of the cobalt to the amount of the rhodium is 1 or more and 6000 or less., 'an amount of the cobalt which is supported is 0.01% by weight or more and 6.0% by weight or less with respect to 100% by weight of the zeolite;'}3. The partial oxidation catalyst according to claim 1 , wherein the zeolite is one or a mixture of two or more selected from the group consisting of mordenite zeolite claim 1 , WI zeolite claim 1 , and beta zeolite.4. The partial oxidation catalyst according to claim 1 , wherein the light hydrocarbon is methane or a mixture mainly comprising methane.5. A method for producing carbon monoxide claim 1 , comprising bringing a light hydrocarbon and oxygen into contact with each other in the presence of the partial oxidation catalyst according to to generate carbon monoxide and hydrogen by partial oxidation.6. The method for producing carbon monoxide according to claim 5 , wherein the light hydrocarbon and the oxygen are brought into contact with each other in a temperature range of 300° C. or more and 1000° C. or less. The present invention relates to a partial oxidation catalyst for a light hydrocarbon and, more specifically, relates to a partial oxidation catalyst comprising cobalt and rhodium-supported zeolite, which enables ...

METHOD AND SYSTEM FOR PRODUCING A GAS PRODUCT CONTAINING CARBON MONOXIDE

The invention relates to a method (-) for producing a gas product containing at least carbon monoxide, in which method at least carbon dioxide is subjected to an electrolysis process () in order to obtain a raw gas (A) containing at least carbon monoxide and carbon dioxide and the carbon dioxide contained in the raw gas (A) is partially or completely fed back to the electrolysis process (). According to the invention, the raw gas (A) is partially or completely subjected to a membrane separation process () in order to obtain a retentate mixture (B) and a permeate mixture (C), which is enriched in carbon dioxide in comparison with the raw gas (A), and that the retentate mixture (B) is partially or completely subjected to a pressure swing adsorption process () in order to obtain the gas product (D), which is enriched in carbon monoxide and depleted of carbon dioxide in comparison with the retentate mixture (B), and a residual mixture (E), which is depleted of carbon monoxide and enriched in carbon dioxide in comparison with the retentate mixture (B). The invention further relates to a corresponding system. 110050010102040. Method (-) for producing a gas product (D) containing at least carbon monoxide , in which method at least carbon dioxide is subjected to an electrolysis process () in order to obtain a raw gas (A) containing at least carbon monoxide and carbon dioxide , and the carbon dioxide contained in the raw gas (A) is partially or completely fed back to the electrolysis process () , characterized in that the raw gas (A) is partially or completely subjected to a membrane separation process () to obtain a retentate mixture (B) and a permeate mixture (C) , which is enriched in carbon dioxide in comparison with the raw gas (A) , and that the retentate mixture (B) is partially or completely subjected to an adsorption process () to obtain the gas product (D) , which is enriched in carbon monoxide and depleted of carbon dioxide in comparison with the retentate mixture ...

METHOD FOR GENERATING REFRIGERATION FOR A CARBON MONOXIDE COLD BOX

The present invention is directed to a method of separating carbon monoxide from syngas mixtures by cryogenic means where a partial condensation cycle is generally employed, and more specifically varying refrigeration generation based on income feed composition of the hydrocarbon feedstock being processed. 1. A method for the separation of carbon monoxide from a syngas feedstock in a carbon monoxide cold box where the cold box is provided refrigeration based on the composition of the incoming feedstock , comprising:cooling and partially condensing the syngas cold box feed stream containing carbon monoxide and hydrogen in a primary heat exchanger to produce a cooled and partially condensed syngas feed stream;separating the cooled and partially condensed syngas feed stream into a first hydrogen rich vapor stream and a first carbon monoxide rich liquid stream in a first separator;feeding the first carbon monoxide rich liquid stream to a second hydrogen removal separator operating at a pressure lower than the first separator, wherein a second hydrogen rich vapor stream is separated from a second crude carbon monoxide rich liquid stream;splitting said second crude carbon monoxide rich liquid stream into two portions wherein a first portion of the second crude carbon monoxide liquid rich stream is at least partially vaporized in the primary heat exchanger and providing a second portion of the second crude carbon monoxide rich liquid stream wherein both portions are introduced into a distillation column for separating purified carbon monoxide product stream from a liquid byproduct stream;providing a turbine feed stream to a turbine disposed within said cold box; andproviding a cryogenic fluid feed to said cold box and varying the flow rate based on the composition of the incoming feedstock.2. The method of claim 1 , further comprising: operating the cold box in a first mode when the methane content of the cold box feed is less than or equal to about 3.6 percent methane ...

Cryogenic Separation of Synthesis Gas

A process and apparatus for separating a feed containing hydrogen, carbon monoxide, methane, and optionally nitrogen to form a product gas having a desired H:CO molar ratio and optionally a hydrogen product gas and a carbon monoxide product gas. The feed is partially condensed to form a hydrogen-enriched vapor fraction and a carbon monoxide-enriched liquid fraction. The hydrogen-enriched vapor fraction and carbon monoxide-enriched liquid fraction are combined in a regulated manner to form an admixture, which is cryogenically separated to form the product mixture having the desired H:CO molar ratio. 1. A process for separating a feed comprising hydrogen , carbon monoxide , methane , and optionally nitrogen , comprising:partially condensing the feed to provide a hydrogen-enriched vapor fraction and a carbon monoxide-enriched liquid fraction;combining at least a portion of the carbon monoxide-enriched liquid fraction with a regulated portion of the hydrogen-enriched vapor fraction to form a two-phase admixture having a vapor fraction and a liquid fraction;cryogenically separating at least a portion of the two-phase admixture in a first fractionator to form a methane-depleted vapor fraction and a hydrogen-depleted liquid fraction;{'sub': '2', 'partially condensing the methane-depleted vapor fraction to form a first product gas and a condensate, wherein the first product gas has a H:CO molar ratio between 0.5:1 and 2.5:1; and'}introducing at least a portion of the condensate into the first fractionator as reflux;wherein at least one of the liquid fraction of the two-phase admixture and the at least a portion of the carbon monoxide-enriched liquid fraction are partially vaporized.2. (canceled)3. The process of wherein the first product gas is withdrawn from the first fractionator at a pressure of 15 to 40 bar.4. The process of wherein the first product gas H:CO molar ratio is between 0.9:1 and 1.5:1.5. The process of further comprising:scrubbing a second portion of the ...

METHOD FOR SEPARATING A SYNTHESIS GAS

A method for separating a synthesis gas containing carbon monoxide and hydrogen including compressing a flow of synthesis gas received from a source of synthesis gas in a compressor, purifying the compressed synthesis gas in a purification unit to purify it of water and/or carbon dioxide, cooling the compressed and purified flow of synthesis gas, separating the cooled flow of synthesis gas by washing and/or distillation at a cryogenic temperature and optionally by adsorption in a separating unit, and producing at least the following three gases in the separating unit: a carbon monoxide-enriched gas, a hydrogen-enriched gas, a residual gas containing carbon monoxide and hydrogen that is less pure with respect to carbon monoxide than the carbon monoxide-enriched gas and less pure with respect to hydrogen than the hydrogen-enriched gas. 115.-. (canceled)16. A method for separating a synthesis gas containing carbon monoxide and hydrogen comprising:i) compressing a flow of synthesis gas received from a source of synthesis gas in a compressor,ii) purifying the compressed synthesis gas in a purification unit to purify it of water and/or carbon dioxide,iii) cooling the compressed and purified flow of synthesis gas,iv) separating the cooled flow of synthesis gas by washing and/or distillation at a cryogenic temperature and optionally by adsorption in a separating unit, andv) producing at least the following three gases in the separating unit: a carbon monoxide-enriched gas, a hydrogen-enriched gas, a residual gas containing carbon monoxide and hydrogen that is less pure with respect to carbon monoxide than the carbon monoxide-enriched gas and less pure with respect to hydrogen than the hydrogen-enriched gas and optionally also a methane-enriched gas, and/or a nitrogen-enriched gas, andvi) sending at least one part of each of the following gases downstream of the source, only if the flow of synthesis gas received from the source and sent to the compressor is below a threshold ...

PROCESS FOR ISOLATING 170 ISOTOPE FROM WATER AND PROCESS FOR CONCENTRATING 170 ISOTOPE USING THE SAME

A process for isolating O from water and a process for concentrating O by using the same are provided. The process for isolating O from water includes: mixing O-containing water with formaldehyde to prepare an aqueous formaldehyde solution; heating the aqueous formaldehyde solution to generate a vapor mixture containing water vapor and formaldehyde vapor; and obtaining O-depleted water, residual formaldehyde, and a gas mixture containing hydrogen and O-enriched carbon monoxide, through photodissociating the vapor mixture. An O-enriched water production process includes: an operation of adding hydrogen to the gas mixture to induce a catalytic methanation reaction to synthesize methane (CH) and O-enriched water (HO) through methanation, the operation being carried out following the process for isolating O from water. 1. A process for isolating O from water , comprising:{'sup': '17', 'preparing an aqueous formaldehyde solution by mixing O -containing water with formaldehyde;'}preparing a vapor mixture containing water vapor and formaldehyde vapor by heating the aqueous formaldehyde solution; and{'sup': 17', '17, 'obtaining O-depleted water, residual formaldehyde, and a gas mixture containing hydrogen and O -enriched carbon monoxide, through photodissociating the vapor mixture.'}2. The process for isolating O from water of claim 1 , wherein the formaldehyde is mixed with water in a molar ratio of formaldehyde to water in a range of 0.01-0.3.3. The process for isolating O from water of claim 1 , wherein the heating is carried out at a temperature in a range of 320-400 K.4. The process for isolating O from water of claim 1 , wherein the photodissociating the vapor mixture is carried out under a pressure in a range of 1-15 Torr.5. The process for isolating O from water of claim 1 , wherein a wavenumber of a photodissociating laser for the photodissociating the vapor mixture is in a range of 28 1 ,370-28 1 ,400 cm.6. The process for isolating O from water of claim 5 , the ...

Method for Using a Solid-Tolerant Heat Exchanger in Cryogenic Gas Treatment Processes

Methods and systems for removing contaminants, such as water and/or carbon dioxide, from a gas stream, such as a natural gas stream or a flue gas stream. One or more solid-tolerant heat exchangers are employed to chill the gas stream to a temperature at which the contaminants solidify. The solidified contaminants may then be separated and removed from the gas stream. In one or more aspects, the one or more solid-tolerant heat exchangers may include a scraped heat exchanger. 1. A method for removing water and carbon dioxide from a feed gas stream containing water and carbon dioxide , the method comprising: i) below which at least a portion of the water contained in the feed gas stream freezes out of the feed gas stream, and', 'ii) above which at least a portion of the carbon dioxide contained in the feed gas freezes out of the feed gas as a pure phase; and, 'producing a first treated gas stream by feeding the feed gas stream to a first solid-tolerant heat exchanger, the first solid-tolerant heat exchanger chilling the feed gas stream to a first temperature, wherein the first temperature is'}producing a second treated gas stream by feeding the first treated gas stream to a second solid-tolerant heat exchanger, the second solid-tolerant heat exchanger chilling the first treated gas stream to a second temperature, wherein the second temperature is below which at least a portion of the carbon dioxide contained in the feed gas stream freezes out of the first treated gas stream as a pure phase.2. The method of claim 1 , further comprising:further chilling the second treated gas stream to at least partially liquefy the second treated gas stream.3. The method of claim 1 , wherein the second treated gas stream comprises primarily methane on a molar basis.4. The method of claim 1 , wherein the first and second solid-tolerant heat exchangers are constructed using different metallurgies.5. The method of claim 1 , wherein the first solid-tolerant heat exchanger is chilled using a ...

METHOD FOR SEPARATING CARBON ISOTOPE AND METHOD FOR CONCENTRATING CARBON ISOTOPE USING THE SAME

The present disclosure relates to a method for separating a carbon isotope and a method for concentrating a carbon isotope using the same, the method for separating a carbon isotope including: cooling a formaldehyde gas to a temperature of from 190K to 250K; and obtaining a mixed gas and residual formaldehyde by photodissociating the cooled formaldehyde gas, the mixed gas including carbon dioxide containing a carbon isotope and hydrogen. 1. A method for separating a carbon isotope comprising:cooling a formaldehyde gas to a temperature of from 190K to 250K; andobtaining a mixed gas and residual formaldehyde by photodissociating the cooled formaldehyde gas, the mixed gas including carbon dioxide containing a carbon isotope and hydrogen.2. The method of claim 1 , wherein the carbon isotope is carbon-13 (C).3. The method of claim 1 , wherein the cooling is performed by a cooling bath or a chiller including a mixture of ethanol and dry ice.4. The method of claim 1 , wherein the photodissociating is performed under a pressure of 0.01 to 5 Torr.5. The method of claim 1 , wherein a wavenumber of a photodissociation laser at the time of the photodissociating is 28396.1 cmto 28401.3 cm.6. The method of claim 1 , wherein a wavenumber of a photodissociation laser at the time of the photodissociating is 28396.1 cm claim 1 , 28401.3 cmor a combination thereof.7. The method of claim 1 , wherein a photodissociation laser used at the time of the photodissociating is an optical fiber laser.8. The method of claim 1 , further comprising: after the obtaining of the mixed gas and the residual formaldehyde claim 1 , the mixed gas including carbon dioxide containing a carbon isotope and hydrogen claim 1 , separating the residual formaldehyde by cooling and condensing the mixed gas and the residual formaldehyde.9. The method of claim 8 , wherein the cooling and condensing is performed at a temperature of 181K (−92° C.) or less.10. A method for concentrating a carbon isotope comprising:{' ...

CONVERSION OF FLUE GAS TO VALUABLE PRODUCTS

A process is disclosed that converts flue gas carbon dioxide to liquid fuels with the aid of biomass and methane. This process incorporates biomass pyrolysis, and gasification of the renewable carbon obtained from this pyrolysis with carbon dioxide and methane in two separate gasification reactors. The gasification reactions occur optionally in the presence of microwave energy. Water, liquid fuels and a sequesterable carbon are expected to be the primary products in this carbon negative process. 1. A process to convert flue gas from to combustible fuels , using biomass and natural gas as additional inputs , comprising:a) Pyrolyzing said biomass to produce a first carbon and volatile gasesb) Gasifying said first carbon in the presence carbon dioxide obtained from said flue gas to produce carbon monoxide in a first gasification system;c) Gasifying said first carbon in the presence of natural gas to produce hydrogen and a second carbon in a second gasification system and;d) Combining the generated carbon monoxide and hydrogen from the first and second gasification systems and inputting this mixture in a Fischer Tropsch process to produce combustible fuels.2. A process claim 1 , according to claim 1 , in which the first gasification system uses microwave energy to lower the gasification temperature in said first gasification system.3. A process according to claim 1 , in which the second gasification system uses microwave energy to lower the gasification temperature in said second gasification system.4. A process according to claim 1 , in which some of the first carbon is used to generate excess biochar in addition to carbon that reacts with carbon dioxide.5. A process according to claim 1 , in which the second carbon is used as biochar.6. A process according to claim 1 , in which the volatile gases are burned to produce energy useful for the first and second gasification systems.7. A process according to claim 1 , in which the synthesis gas ratio of carbon monoxide to ...

NICKEL-CONTAINING CATALYST COMPOSITION HAVING ENHANCED ACIDITY FOR STEAM REFORMING PROCESSES

Modified red mud catalyst compositions, methods for production, and methods of use in steam reforming, the composition comprising: red mud material produced from an alumina extraction process from bauxite ore; and nickel oxide, the nickel oxide present at between about 5 wt. % to about 40 wt. % of the modified red mud catalyst composition. 1. A method for steam reforming over a modified red mud catalyst composition , the method comprising the steps of:{'sub': '2', 'providing a methane feed and a steam feed to react over the modified red mud catalyst composition at increased temperature and increased pressure to produce synthesis gas comprising Hand CO, the composition comprisingred mud material produced from an alumina extraction process from bauxite ore; andnickel oxide, the nickel oxide present at between about 5 wt. % to about 40 wt. % of the modified red mud catalyst composition.2. The method according to claim 1 , where the increased temperature is between about 500° C. to about 1000° C.3. The method according to claim 1 , where the increased temperature is between about 600° C. to about 800° C.4. The method according to claim 1 , where the increased temperature is about 750° C.5. The method according to claim 1 , where the increased pressure is between about 5 bar and about 20 bar.6. The method according to claim 1 , where the increased pressure is between about 10 bar and about 15 bar.7. The method according to claim 1 , where the increased pressure is about 14 bar.8. The method according to claim 1 , where gas hourly space velocity of the methane feed and steam feed is between about 1000 hto 10000 h.9. The method according to claim 1 , where the composition includes at least one component selected from the group consisting of: FeO claim 1 , AlO claim 1 , SiO claim 1 , NaO claim 1 , CaO claim 1 , and TiO.10. The method according to claim 1 , where a majority of the particles of the composition have a particle size of less than about 70 μm.11. The method ...

FLUIDIZED COKING WITH CARBON CAPTURE AND CHEMICAL PRODUCTION

Systems and methods are provided for improving the integration of fluidized coking systems that include an associated gasifier with other refinery and/or chemical plant processes. The improved integration can be based on one or more types of integration improvements. In some aspects, the integration can allow for improved carbon capture. In other aspects, the integration can allow for production of higher quality synthesis gas, which can then facilitate production of various chemicals, such as ammonia or urea. In still other aspects, the integration can allow for incorporation of HS generated during the fluidized coking and gasification into a fertilizer product. In yet other aspects, the integration can allow the fluidized coking system to continue to operate even when the associated refinery and/or chemicals production processes are off-line. In still other aspects, the integration can allow two or more of the above integration advantages, or three or more, such as up to all of the above integration advantages. 1. A method for producing synthesis gas or products derived from synthesis gas , comprising:exposing a feedstock comprising a T10 distillation point of 343° C. or more to a fluidized bed comprising solid particles in a reactor under thermal cracking conditions to form at least a 343° C.− liquid product, the thermal cracking conditions comprising 10 wt % or more conversion of the feedstock relative to 343° C., the thermal cracking conditions being effective for depositing coke on the solid particles;introducing an oxygen-containing stream, a hydrocarbon-containing stream, and steam into a gasifier;passing at least a portion of the solid particles comprising deposited coke from the reactor to the gasifier;{'sub': 2', '2', '2', '2, 'exposing the at least a portion of the solid particles comprising deposited coke to gasification conditions in the gasifier to form a gas phase product comprising H, CO, and COand partially gasified coke particles, the gasification ...

CATALYST CARRIER FOR DRY REFORMING PROCESSES

Methods for dry reforming with a red mud catalyst support composition, one method including providing a methane feed and carbon dioxide feed to react over the red mud catalyst support composition at increased temperature and increased pressure to produce synthesis gas comprising Hand CO, the composition comprising red mud material produced from an alumina extraction process from bauxite ore. 1. A method for dry reforming with a red mud catalyst support composition , the method comprising the steps of:{'sub': '2', 'providing a methane feed and carbon dioxide feed to react in a dry reforming reaction over the red mud catalyst support composition at a temperature between about 500° C. to about 1000° C. and a pressure between about 5 bar and about 20 bar to produce synthesis gas comprising Hand CO, the red mud catalyst support composition comprisingcaustic red mud waste material produced from an alumina extraction process from bauxite ore, where the methane conversion rate via dry reforming is at least about 4% for at least about 6 hours.2. The method according to claim 1 , where the red mud catalyst support composition further comprises at least one added catalytic metal claim 1 , the added catalytic metal not being present at greater than about 1 wt. % in the caustic red mud waste material produced from the alumina extraction process from bauxite ore.3. The method according to claim 2 , where the at least one added catalytic metal is a Periodic Table Group 3-12 metal.4. (canceled)5. The method according to claim 1 , where the increased temperature is between about 600° C. to about 800° C.6. The method according to claim 1 , where the increased temperature is between about 700° C. to about 750° C.7. (canceled)8. The method according to claim 1 , where the increased pressure is between about 7 bar and about 15 bar.9. The method according to claim 1 , where the increased pressure is about 14 bar.10. The method according to claim 1 , where the methane conversion rate is ...

CATALYST CARRIER FOR BI-REFORMING PROCESSES

Methods for bi-reforming with a red mud catalyst support composition, one method including providing a methane feed in the presence of carbon dioxide and steam to react over the red mud catalyst support composition at increased temperature and increased pressure to produce synthesis gas comprising Hand CO, the composition comprising red mud material produced from an alumina extraction process from bauxite ore. 1. A method for bi-reforming with a red mud catalyst support composition , the method comprising the steps of:{'sub': '2', 'providing a methane feed in the presence of carbon dioxide and steam to react in a bi-reforming reaction over the red mud catalyst support composition at a temperature between about 500° C. to about 1000° C. and a pressure between about 5 bar and about 20 bar to produce synthesis gas comprising Hand CO, the red mud catalyst support composition comprising{'sub': '2', 'red mud waste material produced from an alumina extraction process from bauxite ore with a weight ratio of aluminum oxide to iron oxide of about 1:0.74 and a weight ratio of aluminum oxide to titanium oxide of about 1:0.27, where produced His at least about 1 mol. % of produced products from the bi-reforming reaction for at least about 5 hours.'}2. The method according to claim 1 , where the red mud catalyst support composition further comprises at least one added catalytic metal claim 1 , the added catalytic metal not being present at greater than about 1 wt. % in an unmodified form of the red mud material produced from the alumina extraction process from bauxite ore.3. The method according to claim 2 , where the at least one added catalytic metal is a Periodic Table Group 3-12 metal.4. (canceled)5. The method according to claim 1 , where the increased temperature is between about 600° C. to about 800° C.6. The method according to claim 1 , where the increased temperature is about 750° C.7. (canceled)8. The method according to claim 1 , where the increased pressure is ...

CATALYST COMPOSITIONS HAVING ENHANCED ACIDITY FOR STEAM REFORMING PROCESSES

Methods for steam reforming over a modified red mud catalyst composition, one method including providing a methane feed and a steam feed to react over the modified red mud catalyst composition at increased temperature and increased pressure to produce synthesis gas comprising Hand CO, the composition comprising red mud material produced from an alumina extraction process from bauxite ore; nickel oxide, the nickel oxide present at between about 5 wt. % to about 40 wt. % of the modified red mud catalyst composition; and a Periodic Table Group VIB metal oxide, the Group VIB metal oxide present at between about 1 wt. % and about 30 wt. % of the modified red mud catalyst composition. 1. A method for steam reforming over an enhanced-acidity modified red mud catalyst composition , the method comprising the steps of:{'sub': '2', 'providing a methane feed and a steam feed to react in a steam reforming reaction over the enhanced-acidity modified red mud catalyst composition at a temperature between about 500° C. to about 1000° C. and a pressure between about 5 bar and 20 bar to produce synthesis gas comprising Hand CO, the enhanced-acidity modified red mud composition prepared by a homogeneous precipitation process comprising the steps ofproviding an unmodified caustic red mud waste material produced from an alumina extraction process from bauxite ore;dissolving in water the unmodified caustic red mud waste material and neutralizing pH of the unmodified red mud waste material with an acid comprising hydrochloric acid;combining nickel oxide, the nickel oxide present at between about 5 wt. % to about 40 wt. % of the enhanced-acidity modified red mud catalyst composition; andcombining a Periodic Table Group VIB metal oxide, the Group VIB metal oxide present at between about 1 wt. % and about 30 wt. % of the enhanced-acidity modified red mud catalyst composition.2. The method according to claim 1 , where the Group VIB metal oxide comprises at least one metal selected from the ...

ENERGY-EFFICIENT SYSTEM AND METHOD FOR CARBON DIOXIDE CONVERSION

A system and method for converting carbon dioxide are proposed. The system for converting carbon dioxide includes a carbon monoxide generator for generating carbon monoxide through a reverse water gas shift reaction and a hydrocarbon generator for producing a hydrocarbon through a Fischer-Tropsch synthesis reaction, whereby the carbon monoxide generator is packed both with a catalyst for the reverse water gas shift reaction and with a catalyst for the Fischer-Tropsch synthesis reaction, thus increasing the CO yield in the carbon monoxide generator even at a low temperature compared to when the catalyst for the reverse water gas shift reaction is used alone, ultimately increasing the hydrocarbon yield in the hydrocarbon generator. Moreover, the energy of the exothermic Fischer-Tropsch synthesis reaction can be used as the energy required for the endothermic reverse water gas shift reaction, thereby increasing energy efficiency and processing yield and thus reducing operation and maintenance costs. 1. A system for converting carbon dioxide , suitable for converting carbon dioxide using hydrogen , comprising: a case having an inlet, into which carbon dioxide and hydrogen are introduced, formed in one side and an outlet, from which a reaction product is discharged, formed in an opposite side, and', 'a catalytic reactor disposed in an internal space of the case and packed with both a catalyst for a reverse water gas shift reaction and a catalyst for a Fischer-Tropsch synthesis reaction so that the reverse water gas shift reaction and the Fischer-Tropsch synthesis reaction are carried out together, thereby increasing a carbon monoxide yield and allowing reaction heat generated in the Fischer-Tropsch synthesis reaction to be used for the reverse water gas shift reaction., 'a carbon monoxide generator comprising2. The system of claim 1 , further comprising:{'sub': '2', 'a remover disposed downstream of the carbon monoxide generator and receiving a reaction product from the ...

METHOD AND APPARATUS FOR PREPARING REDUCTION PRODUCT OF CARBON DIOXIDE BY ELECTROCHEMICALLY REDUCING CARBON DIOXIDE

The present invention relates to a method and an apparatus of preparing a reduction product of carbon dioxide by electrochemically reducing carbon dioxide. 1. A method of preparing a reduction product of carbon dioxide (CO) by electrochemically reducing carbon dioxide within an electrochemical cell , which comprises an anode , a cathode , and an electrolyte membrane which is disposed between the anode and the cathode to separate the anode region and the cathode region:(1) supplying water or an electrolytic solution to the anode region;(2) supplying a carbon dioxide gas which has been humidified in a condition where the relative humidity exceeds 100% to the cathode region within the electrochemical cell; and{'sup': '+', '(3) applying a voltage between the anode region and the cathode region to generate hydrogen ions (H) in the anode region, wherein the hydrogen ions move through the electrolyte membrane to the cathode region and then electrochemically reduce the carbon dioxide gas so as to produce a reduction product of carbon dioxide.'}2. The method of claim 1 , wherein claim 1 , upon applying a voltage in step (3) claim 1 , the moisture in which carbon dioxide is dissolved is condensed as the relative humidity within the cathode region exceeds 100% and forms a water film on the cathode surface claim 1 , and the reduction product is produced from the carbon dioxide dissolved in the water film as a reactant by electrochemical reduction.3. The method of claim 1 , wherein the electrochemical cell comprises a membrane-electrode assembly having an anode catalyst layer and a cathode catalyst layer formed on each surface of the electrolyte membrane claim 1 , respectively claim 1 , and a gas diffusion layer of supplying the humidified carbon dioxide to the catalyst layer claim 1 , which is placed in the cathode side of the membrane-electrode assembly.4. The method of claim 1 , wherein the reduction product of the carbon dioxide is formic acid claim 1 , formaldehyde claim 1 ...

METHODS OF UTILIZING CARBON MONOXIDE TO INCREASE OIL RECOVERY

A method of utilizing carbon monoxide to increase oil recovery includes injecting an effective amount of carbon monoxide, either as pure carbon monoxide or as a component of a gas mixture, into an oil reservoir. The carbon monoxide increases oil flow and rate of oil flow from the oil reservoir through a variety of chemical mechanisms. 1. A method of increasing the rate of oil recovery from a reservoir , the method comprising:injecting an effective amount of carbon monoxide into a reservoir at natural temperature, the rate of oil recovery being increased as compared to a rate of oil recovery achieved by injecting pure carbon dioxide into the reservoir.2. The method of increasing the rate of oil recovery according to claim 1 , wherein the effective amount of carbon monoxide is at least 10% of a gas mixture injected into the reservoir.3. The method of increasing the rate of oil recovery according to claim 1 , wherein the effective amount of carbon monoxide is at least 20% of a gas mixture injected into the reservoir.4. The method of increasing the rate of oil recovery according to claim 1 , wherein the effective amount of carbon monoxide is at least 30% of a gas mixture injected into the reservoir.5. The method of increasing the rate of oil recovery according to claim 1 , wherein the injection takes place during a primary phase claim 1 , a secondary phase or a tertiary phase of oil recovery operations.6. The method of increasing the rate of oil recovery according to claim 1 , wherein carbon dioxide and the carbon monoxide are injected into the reservoir.7. The method of increasing the rate of oil recovery according to claim 6 , wherein a gas mixture comprising nitrogen claim 6 , the carbon dioxide and the carbon monoxide is injected into the reservoir claim 6 , the carbon monoxide being at least 10% of the gas mixture.8. The method of increasing the rate of oil recovery according to claim 1 , wherein injecting the carbon monoxide into a reservoir at natural temperature ...

SERIAL METHANOL REACTORS

The present relates to a process comprising the steps of Providing a syngas stream with module M to a Methanol loop, In the Methanol loop passing the syngas though a first Methanol reactor, obtaining a first effluent from the first Methanol reactor, Cooling the first effluent and condensing at least part of the produced methanol Separating the first cooled effluent into at least a first raw Methanol stream and a first unreacted stream, Heating the first unreacted stream, Passing the first heated unreacted stream through a second methanol reactor, Obtaining a second effluent from the second methanol reactor, Separating the second effluent into at least a second raw Methanol stream and a second unreacted stream, and Recycling the second unreacted stream to the syngas stream. 1. A process comprising the steps ofproviding a syngas stream with module M to a Methanol loop,in the Methanol loop passing the syngas though a first Methanol reactor,obtaining a first effluent from the first Methanol reactor,cooling the first effluent and condensing at least part of the produced methanolseparating the first cooled effluent into at least a first raw Methanol stream and a first unreacted stream,heating the first unreacted stream,passing the first heated unreacted stream through a second methanol reactor,obtaining a second effluent from the second methanol reactor, cooling and condensing said second effluent,separating the cooled second effluent into at least a second raw Methanol stream and a second unreacted stream, andrecycling the second unreacted stream to the syngas stream.2. A Process according to wherein additional steps of conversion in a methanol reactor and methanol separation is applied.3. A Process according to wherein the first reactor and or second reactor is a boiling water reactor (BWR) claim 1 , an adiabatic reactor and/or a quench reactor.4. A Process according to wherein the first reactor and or second reactor is operated at the same inlet temperature.5. A ...

METHOD AND APPARATUS FOR PRODUCING CARBON MONOXIDE

A method and apparatus for producing carbon monoxide, wherein the carbon monoxide is formed from a gaseous feed which includes at least carbon dioxide. The method includes supplying oxygen to a carbon dioxide stream for forming a carbon dioxide based mixture, supplying the carbon dioxide based mixture to a hydrogen based stream to form the gaseous feed, supplying a hydrocarbon containing stream to the hydrogen based stream before the supply of the carbon dioxide based mixture, feeding the gaseous feed into a reactor which includes at least one catalyst, treating the gaseous feed by partial oxidation in the reactor so that carbon dioxide reacts with hydrogen in the reactor in presence of oxygen and heat is formed during the reaction, and recovering a product composition including at least carbon monoxide and hydrogen from the reactor. 1. A method for producing carbon monoxide , wherein the carbon monoxide is formed from a gaseous feed which comprises at least carbon dioxide , wherein the method comprisessupplying oxygen to a carbon dioxide stream for forming a carbon dioxide based mixture,supplying the carbon dioxide based mixture to a hydrogen based stream to form the gaseous feed,supplying a hydrocarbon containing stream to the hydrogen based stream before the supply of the carbon dioxide based mixture,feeding the gaseous feed into a reactor which comprises at least one catalyst,treating the gaseous feed by means of a partial oxidation in the reactor so that carbon dioxide reacts with hydrogen in the re-actor in presence of oxygen and heat is formed during the reaction, andrecovering a product composition comprising at least carbon monoxide and hydrogen from the reactor.2. The method according to claim 1 , wherein the gaseous feed is fed with high velocity to the reactor such that the velocity of the gas stream is ≥0.5 m/s.3. The method according to claim 1 , wherein a treatment temperature is 800-1500° C. in the reactor.4. The method according to claim 1 , wherein ...

PROCESS FOR METHANOL PRODUCTION

Integrated process comprising: synthesis of methanol from a methanol synthesis gas (); synthesis of ammonia from an ammonia make-up gas (), and synthesis of carbon monoxide from a methane-containing stream, wherein: the synthesis of methanol provides a liquid stream of methanol () and a gaseous stream () of unreacted synthesis gas; a portion () of said gaseous stream is separated as purge gas; said purge gas is subjected to a hydrogen recovery step, providing a hydrogen-containing stream () which is used as a hydrogen source for making the ammonia make-up gas, and a tail gas () which is used as a methane source for the synthesis of carbon monoxide by oxidation of a methane-containing stream. 2. The process according to claim 1 , comprising a step of air separation in a dedicated air separation unit claim 1 , providing a nitrogen stream and an oxygen stream claim 1 , wherein at least part of said nitrogen stream is a nitrogen source for said ammonia make-up gas and at least part of said oxygen stream acts as oxidant in the oxidation of said methane-containing stream.3. The process according to claim 1 , wherein said purge gas stream is subjected to a water washing step before undergoing said hydrogen recovery step.4. The process according to claim 1 , wherein said hydrogen recovery step is performed by means of separating membranes.5. The process according to claim 4 , wherein the pressure of said hydrogen-containing stream claim 4 , at the outlet of the separating membranes claim 4 , is 25-30 bar less than the pressure of the purge gas stream at the inlet of the separating membranes.6. The process according to claim 4 , wherein the pressure of the tail gas claim 4 , at the outlet of the separating membranes claim 4 , is 2-4 bar less than the pressure of the purge gas stream at the inlet of the separating membranes.7. The process according to claim 1 , wherein at least 90% of the hydrogen contained in the purge gas stream is recovered in the hydrogen-containing ...

METHOD FOR AN IMPROVED PARTIAL CONDENSATION CARBON MONOXIDE COLD BOX OPERATION

The present invention is directed to a method and system of separating carbon monoxide from syngas mixtures with high methane content by cryogenic means where a partial condensation cycle is generally employed, and more specifically towards combining the methane-rich liquid exiting the distillation column with a lower-boiling mixture so that the boiling point of the combined stream is lower than the boiling point of the methane-rich liquid. 1. A method for the separation of carbon monoxide from a syngas feedstock in a partial condensation carbon monoxide cold box , comprising:cooling and partially condensing the syngas feedstock containing carbon monoxide and hydrogen in a process heat exchanger to produce a cooled and partially condensed syngas feed stream;separating the cooled and partially condensed syngas feed stream into a crude hydrogen vapor stream and a high-pressure carbon-monoxide-rich feed liquid stream in a high-pressure separator;feeding the high-pressure carbon-monoxide-rich feed liquid stream to a low-pressure separation unit operating at a pressure lower than the high-pressure separator, wherein a cold flash gas is separated from a crude CO liquid stream;separating said crude CO liquid stream in a distillation column to form a purified carbon monoxide vapor stream and a methane-rich liquid byproduct stream containing at least 50% methane;separating a portion of the cold flash gas having at least 1 vol % and less than 99 vol % and mixing said portion of cold flash gas with the methane-rich liquid byproduct stream before introducing the mixture into the process heat exchanger.2. The method of wherein 5-40 vol % of the cold flash gas is mixed with the methane-rich liquid before introducing the mixture into the process heat exchanger.3. The method of wherein 10-30 vol % of the cold flash gas is mixed with the methane-rich liquid before introducing the mixture into the process heat exchanger.4. The method of claim 1 , further comprising: warming the crude ...

CATALYTIC SYSTEM FOR THE PRODUCTION CARBON MONOXIDE FROM CARBON DIOXIDE INCLUDING IRIDIUM (IR) PHOTOSENSITIZER AND TIO2/RE(I) COMPLEX CATALYST

Disclosed is a catalytic system for the reduction of carbon dioxide to carbon monoxide. The catalytic system includes an iridium (Ir) photosensitizer and a TiO/Re(I) complex catalyst. No additional process is required to anchor the molecule-based dye compound on TiOin the synthesis of the catalytic system. This enables the synthesis of the catalytic system in a relatively easy manner for groups of photosensitizer candidates. In addition, the catalytic system can be utilized as a platform for more easily evaluating the abilities of photosensitizers. Furthermore, the catalytic system can find application in various fields due to its ability to selectively produce carbon monoxide gas with high efficiency. 1. A catalytic system comprising an iridium (Ir) photosensitizer and a TiO/Re(I) complex catalyst.2. The catalytic system according to claim 1 , wherein the valence of the iridium is trivalent.3. The catalytic system according to claim 1 , wherein the iridium photosensitizer is selected from the group consisting of Ir-OMe claim 1 , Ir-Bu claim 1 , Ir-Me claim 1 , and Ir-H.4. The catalytic system according to claim 1 , further comprising a sacrificial reagent.5. The catalytic system according to claim 4 , wherein the sacrificial reagent is BIH.6. The catalytic system according to claim 1 , wherein the catalytic system is a binary system.7. The catalytic system according to claim 1 , wherein the catalytic system reduces carbon dioxide (CO).8. The catalytic system according to claim 1 , wherein the catalytic system produces carbon monoxide (CO). The present application claims the benefit and priority to Korean Patent Application No. 10-2017-0020289, filed in the Korean Patent Office on Feb. 15, 2017. The entire disclosure of the application is incorporated herein by reference.The present invention relates to a catalytic system including an iridium (Ir) photosensitizer and a TiO/Re(I) complex (hereinafter referred to as “ReC”) catalyst, and more specifically to a ...

Calcium Sulfide Decomposition Process

The present invention relates to a process for decomposing calcium sulfide (CaS) into calcium oxide (CaO) and sulfur dioxide (SO), comprising: —providing a reactor containing calcium sulfide and a source of carbon, —oxidizing the source of carbon so as to generate carbon dioxide (CO), —reacting the calcium sulfide with said carbon dioxide so as to produce carbon oxide (CaO), sulfur dioxide (SO) and carbon monoxide (CO) according to the following reaction: CaS+3CO˜CaO+SO+3CO wherein the oxygen and carbon contents in the oxidation step are chosen such that: (i) the mass ratio C/CaS is comprised between 0.15 and 0.35 and (ii) the mass ratio O/C is comprised between 5 and 25. 1. A process for decomposing calcium sulfide (CaS) into calcium oxide (CaO) and sulfur dioxide (SO) , comprising:providing a reactor containing calcium sulfide and a source of carbon,{'sub': '2', 'oxidizing the source of carbon so as to generate carbon dioxide (CO),'}{'sub': '2', 'claim-text': {'br': None, 'sub': 2', '2, 'CaS+3CO→CaO+SO+3CO'}, 'reacting the calcium sulfide with said carbon dioxide so as to produce carbon oxide (CaO), sulfur dioxide (SO) and carbon monoxide (CO) according to the following reactionwherein the oxygen and carbon contents in the oxidation step are chosen such that:(i) the mass ratio C/CaS is comprised between 0.15 and 0.35 and{'sub': '2', '(ii) the mass ratio O/C is comprised between 5 and 25.'}2. The process of claim 1 , wherein the ratio C/CaS is equal to 0.25.3. The process of claim 1 , wherein the ratio O/C is equal to 8.4. The process of claim 1 , wherein in the oxidation step the reactor is heated to a temperature comprised between 900° C. and 1200° C.5. The process of claim 4 , wherein the reactor is heated by induction.6. The process of claim 1 , wherein the source of carbon comprises at least one of: coal claim 1 , coke claim 1 , charcoal claim 1 , and shale oil.7. The process of claim 1 , wherein the reactor is a continuous reactor claim 1 , such as a ...

SELECTIVE OXIDATION USING ENCAPSULATED CATALYTIC METAL

Systems and methods are provided for selective oxidation of CO and/or C hydrocarbonaceous compounds in a reaction environment including hydrocarbons and/or hydrocarbonaceous components. The selective oxidation can be performed by exposing the CO and/or C hydrocarbonaceous compounds to a catalytic metal that is encapsulated in a small pore zeolite. The small pore zeolite containing the encapsulated metal can have a sufficiently small pore size to reduce or minimize the types of hydrocarbons or hydrocarbonaceous compounds that can interact with the encapsulated metal. 1. A method for selective oxidation of CO and C hydrocarbonaceous compounds , comprising:{'sub': 3−', '3−, 'exposing a feed comprising a) CO, C hydrocarbonaceous compounds, or a combination thereof, and b) at least one additional hydrocarbon, hydrocarbonaceous compound, or combination thereof, to an oxidizing environment in the presence of a small pore zeolite-encapsulated metal catalyst comprising 0.01 wt % to 10 wt % of Ru, Rh, Pd, Os, Ir, Pt, Ni, Au, Ag, or combination thereof as a catalytic metal, to oxidize at least a portion of the CO, C hydrocarbons, or a combination thereof, at least 20 wt % of the catalytic metal being encapsulated in the zeolite.'}2. The method of claim 1 , wherein exposing the feed comprises exposing the feed to a catalyst mixture comprising 0.001 wt % to 10 wt % of the small pore zeolite-encapsulated metal catalyst claim 1 , relative to a weight of the catalyst mixture.3. The method of claim 1 , wherein the C hydrocarbonaceous compounds comprise C hydrocarbons.4. The method of claim 1 , wherein the feed comprises CO claim 1 , C-hydrocarbonaceous compounds claim 1 , or a combination thereof.5. The method of claim 1 , wherein the feed comprises CO claim 1 , C-hydrocarbons claim 1 , or a combination thereof.6. The method of claim 1 , wherein the small pore zeolite-encapsulated metal catalyst comprises a synthetic small pore zeolite.7. The method of claim 6 , wherein at least 80 ...

METHOD AND APPARATUS FOR PRODUCING A MIXTURE OF CARBON MONOXIDE AND HYDROGEN

In a method for producing a gaseous mixture of CO and H, a first gas comprising at least 50% CO is compressed in a first compressor to form a first compressed gas cooled to a first temperature and mixes with a second gas comprising at least 50% hydrogen in order to form the gaseous mixture, at least one of the first and second gases originating from a cryogenic distillation separation unit in which a feed gas containing Hand CO cools in a first heat exchanger and is separated in at least one distillation column and at least one part of the second gas heats in the separation unit to a third temperature lower than the first temperature and is then sent to mix with the first gas. 112-. (canceled)13. A process for the production of a gas mixture of carbon monoxide and hydrogen in which:i) compressing a first gas comprising at least 50% of carbon monoxide in a first compressor in order to form a first compressed gas cooled to a first temperature;ii) mixing a second gas comprising at least 50% of hydrogen with the first compressed gas in order to form the gas mixture;iii) at least one of the first and second gases originates from a unit for separation by cryogenic distillation in which a feed gas containing hydrogen and carbon monoxide is cooled in a first heat exchanger and is separated in at least one distillation column;wherein the process further includes a step selected from the group consisting of:a) a part of the first compressed gas is sent to the separation unit, where the part of the first compressed gas is cooled down to a second temperature which is less than the first temperature and is subsequently mixed with the gas mixture or the second gas;b) at least a part of the second gas is reheated in the separation unit up to a third temperature which is less than the first temperature and is subsequently sent to be mixed with the first gas, andc) combinations thereof.14. The process as claimed in claim 13 , in which the first and second gases originate from the ...

SYSTEM AND METHOD FOR ENHANCED ARGON RECOVERY FROM A FEED STREAM COMPRISING HYDROGEN, METHANE, NITROGEN AND ARGON

A system and method for argon and nitrogen extraction from a feed stream comprising hydrogen, methane, nitrogen and argon, such as tail gas of an ammonia production plant is provided. The disclosed system and method provides for nitrogen-argon rectification and the methane rejection within a column system comprised of at least one distillation column. Nitrogen and argon are further separated and to produce liquid products. An argon stripping column arrangement is disclosed where residual argon is further removed from the methane-rich fuel gas and recycled back to the feed stream.

CATALYSTS UTILIZING CARBON DIOXIDE FOR THE EPOXIDATION OF OLEFINS

The present disclosure provides mixed molybdenum oxide catalysts, methods for preparing epoxides from olefins and CO2 using them, and methods of making the mixed molybdenum oxide catalysts by impregnation or co-precipitation. In a preferred embodiment, the mixed molybdenum oxide catalysts are silver/molybdenum oxide catalysts, ruthenium/molybdenum oxide catalysts, or a combination thereof. 1. A method of catalyzing the abstraction of oxygen from carbon dioxide (CO) to form carbon monoxide (CO) comprising contacting a mixed molybdenum oxide catalyst , which comprises a silver oxide , a ruthenium oxide , or a mixture thereof , with an appropriate COfeed stream under suitable temperature and pressure conditions so as to abstract oxygen from the COto form CO.2. The method of wherein the mixed molybdenum oxide catalyst claim 1 , further comprises a Group IA or Group IIA element promoter.3. The method of wherein the mixed molybdenum oxide catalyst claim 1 , further comprises a support.4. The method of wherein the mixed molybdenum oxide catalyst claim 3 , wherein the support is AlO claim 3 , SiO claim 3 , TiO claim 3 , ZrO claim 3 , AlPO claim 3 , carbon claim 3 , graphite claim 3 , or a mixture thereof.5. The method of wherein the mixed molybdenum oxide catalyst claim 1 , wherein the mixed catalyst is a mixed silver/molybdenum oxide catalyst.6. The method of wherein the mixed silver/molybdenum oxide catalyst claim 5 , wherein the molar ratio of AgO to MoOis in the range of about 1.0 to 0.05 to about 1.0 to 20.0.7. The method of wherein the mixed silver/molybdenum oxide catalyst claim 6 , wherein the molar ratio of AgO to MoOis in the range of about 1.0 to 0.1 to about 1.0 to 10.0.8. The method of wherein the mixed silver/molybdenum oxide catalyst claim 7 , wherein the molar ratio of AgO to MoOis in the range of about 1.0 to 0.5 to about 1.0 to 5.0.9. The method of wherein the mixed silver/molybdenum oxide catalyst claim 8 , wherein the molar ratio of AgO to MoOis in the ...

PROCESS AND PLANT FOR PRODUCING SYNTHESIS GAS WITH VARIABLE COMPOSITION

A process and a plant for the continuous conversion of a hydrocarbonaceous feed gas into a synthesis gas comprising carbon monoxide and hydrogen, wherein the H/CO molar ratio of the product gases can be varied within a wide range. This is achieved in that at least a part of a methane-rich gas obtained during the fractionation of the raw synthesis gas is admixed to the feed gas mixture, and that in the alternative 115-. (canceled)16. A process for the continuous conversion of a hydrocarbonaceous feed gas into a synthesis gas comprising carbon monoxide and hydrogen , comprising the following process steps carried out one after the other:a) providing a feed gas mixture which comprises hydrocarbonaceous gas and steam, as well as a heating gas mixture which comprises a fuel gas and an oxygen-rich gas;{'sub': 2', 'B, 'b) splitting the feed gas mixture under reforming conditions by catalytic steam reformation in a tubular reformer fired by burners into a raw synthesis gas containing hydrogen, carbon monoxide, carbon dioxide and methane, wherein heat necessary for splitting, which is indirectly transmitted to the feed gas mixture, is produced by combustion of the heating gas mixture, wherein in normal operation of the process a base H/CO ratio (V) is obtained,'}c) separating the carbon dioxide from the raw synthesis gas;{'sub': '2', 'd) fractionating the raw synthesis gas into a hydrogen-rich gas, a carbon monoxide-rich gas and a methane-rich gas, wherein the hydrogen-rich gas optionally is supplied to a further cleaning step and otherwise is discharged from the process as Hproduct gas, and the carbon monoxide-rich gas is supplied to the further use outside the process as CO product gas;'}{'sub': '2', 'e) optionally cleaning of the hydrogen-rich gas by separating gaseous impurities and admixing the same to the heating gas mixture and discharging the cleaned hydrogen-rich gas as Hproduct gas for the further use outside the process;'}f) admixing at least a part of the methane ...

PROCESS FOR PRODUCING COMPRESSED HYDROGEN IN A MEMBRANE REACTOR AND REACTOR THEREFOR

A process for direct compression of hydrogen separated from a hydrocarbon source is described herein. The process comprises a first zone wherein a hydrocarbon reaction that produce hydrogen occurs, a ceramic proton conductor which under an applied electric field transport hydrogen from said first zone to said second zone, and a second zone where compressed hydrogen is produced. The heat energy generated by ohmic resistance in the membrane is partially recuperated as chemical energy in the hydrocarbon reforming process to generate hydrogen. 1. A process for compressing hydrogen in a membrane reactor; said membrane reactor comprising a first zone separated by a hydrogen transport membrane from a second zone , said first zone having a gas inlet and a product outlet and said second zone having a product outlet; said process comprising:feeding a gas comprising a hydrocarbon to said first zone, and allowing a reaction to take place in said first zone so that hydrogen is formed;applying an electric field over said hydrogen transport membrane; andallowing the hydrogen to disassociate into electrons and protons in said first zone and allowing protons to selectively pass through the hydrogen transport membrane to said second zone, where protons recombine to form of hydrogen in the second zone;wherein the membrane reactor comprises a pressure regulator at said product outlet from said second zone so that, in operation, the partial pressure of hydrogen in the second zone is higher than the partial pressure of hydrogen in the first zone.2. The process as claimed in claim 1 , wherein the gas added to the first zone comprises the hydrocarbon and water claim 1 , the process produces reaction products at the product outlet of the first zone claim 1 , and said reaction products comprise CO and/or CO.3. The process as claimed in claim 1 , wherein the membrane reactor is operated at a temperature above 400° C.4. The process as claimed in claim 1 , wherein the hydrogen extracted from ...

PROCESS FOR SEPARATION OF HYDROGEN AND OXYGEN

Embodiments of the invention are directed to methods, processes, and systems for safely and reliably purifying hydrogen from a gas mixture containing hydrogen and oxygen using a cryogenic separation method. 1. A process for separating hydrogen and oxygen from a gas mixture produced by photocatalytic splitting of water , the process comprising: [{'sub': 2', '2', '2, '(i) compressing a feed source gas comprising H, O, and COto about 1.0 MPa forming a compressed feed source;'}, {'sub': '2', '(ii) filtering water and COfrom the compressed feed source, forming a filtered feed source;'}, '(iii) cooling the filtered feed source to about −180° C., forming a partially liquefied feed source;', '(iv) separating the partially liquefied feed source into an high pressure (HP) feed source and a low pressure (LP) feed source;', '(iv) compressing the HP feed source to a pressure of at least 0.8 MPa and introducing the HP feed source into the bottom portion of a HP cryogenic separation column forming an oxygen enriched liquid at the bottom of the HP cryogenic separation column and a hydrogen enriched gas at the top of the HP cryogenic separation column;', '(v) expanding the LP feed source to a temperature of less than −150° C. and a pressure of at least 0.1 MPa forming a processed LP feed source and introducing the processed LP feed source, oxygen enriched liquid from the HP column, and the hydrogen enriched gas from the HP column to a LP cryogenic distillation column; and', '(vi) collecting the oxygen enriched product liquid from the bottom portion of the LP column and the hydrogen enriched product gas from the top of the LP column; and, '(a) separating hydrogen and oxygen from a photocatalytically produced feed gas by'}(b) collecting, storing, and/or utilizing a hydrogen product gas and an oxygen product liquid or gas.2. The process of claim 1 , wherein the feed source is compressed to at least 1.0 MPa.3. The process of claim 1 , wherein the HP cryogenic distillation process is ...

Metal oxide materials made using self-assembled coordination polymers

A method for making organo-metal material involves providing a metal ion source in a medium that removes metal ions from the source and forms 1D metal-containing coordination polymers that self-assemble and precipitate as at least one of a 2D and 3D coordination polymer material that can be thermally treated to produce a porous metal oxide material. 1. A method of making organo-metal material , comprising providing a metal ion source in a medium that removes metal ions from the source and forms 1D metal-containing coordination polymers which self-assemble and precipitate as at least one of a 2D and 3D coordination polymer material.2. The method of wherein metal ions are removed from the source by an etching component of the medium.3. The method of wherein the etching component comprises a conjugate acid-base pair that serves as an etchant and as a chelating agent.4. The method of wherein the metal ion source comprises a metal particle or metal body.5. The method of claim lwherein the medium comprises an aqueous acidic solution.6. The method of wherein the metal particles are reacted in an aqueous acidic solution to form 1D metal-containing coordination polymers that grow by coordination polymerization and self-assemble as at least one of a 2D and 3D coordination polymer material.7. The method of wherein the metal ion source comprises at least one of a metal of a metal oxide claim 1 , metal-chalcogen claim 1 , metal-pnictogen claim 1 , and/or metal-boron that are soluble in the medium in acetate form.8. The method of wherein the metal comprises at least one of gallium claim 7 , indium claim 7 , bismuth claim 7 , tin claim 7 , iron claim 7 , titanium and other metals and/or alloys that can complex with bidentate ligands to form coordination polymers.9. The method of wherein the metal particle has an oxide layer that is etched by an etching component of the medium wherein the etchant can be an acid claim 4 , base claim 4 , or a derivative of a conjugate acid-base pair. ...

METHOD AND APPARATUS FOR SEPARATING A SYNTHESIS GAS

In a method for separating a synthesis gas containing carbon monoxide and hydrogen, a synthesis gas flow from a synthesis gas source is compressed in a compressor and separated into at least three gaseous products. If there is insufficient synthesis gas, at least three separation products are recycled in the compressor in order to separate said products. 115-. (canceled)16. A method for separating a synthesis gas containing carbon monoxide and hydrogen wherein:i) compressing a synthesis gas flow originating from a synthesis gas source in a compressor;ii) purifying the compressed synthesis gas in a purification unit to remove water and/or carbon dioxide;iii) cooling the compressed purified synthesis gas flow;iv) separating the cooled synthesis gas flow by a separation process selected from the group consisting of scrubbing, distillation at a cryogenic temperature, adsorption in a separation unit, and combinations thereof; andv) producing at least the following three gases in the separation unit: a carbon monoxide-enriched gas, a hydrogen-enriched gas, a residual gas containing carbon monoxide and hydrogen which contains less carbon monoxide than the carbon monoxide-enriched gas and less hydrogen than the hydrogen-enriched gas,wherein only if the synthesis gas flow passed to the compressor is below a threshold or zero, at least a portion of at least two the gases selected from the group consisting of the carbon monoxide-enriched gas, the hydrogen-enriched gas, the residual gas, and combinations thereof, are introduced at a location downstream of the source and upstream of the purification unit.17. The method as claimed in claim 16 , wherein:a) the compressed synthesis gas is stored while the flow of synthesis gas is above the threshold; andb) at least a portion of the compressed synthesis gas and at least a portion of at least each of the first three gases from stage v) are passed downstream of the source to be purified in the purification unit and separated in the ...

METHOD FOR SYNTHESIS GAS PURIFICATION

The present invention relates to an integrated method and apparatus for providing a synthesis gas to a cryogenic separation unit installed for separating synthesis gas into products selected from carbon monoxide, crude hydrogen, methane-rich fuel and syngas with a particular H:CO ratio. More specifically, the invention relates to the purification of synthesis gas routed to a downstream cryogenic separation unit and minimizing temperature disturbances in the separation unit. 1. A continuous purification method of a synthesis gas stream obtained from a pre-purification unit to remove substantially all HO and COprior to routing the synthesis gas product stream to a downstream cryogenic separation unit comprising:{'sub': 2', '2', '2', '2', '2', '2, 'supplying a synthesis gas feed stream to a synthesis gas purification unit comprised of at least two adsorbent beds undergoing a temperature swing adsorption (TSA) cycle where each bed undergoes at least two phases: (1) a feed phase for producing a synthesis gas product stream substantially free of HO and COby adsorbing these components on the adsorbent bed and (2) a regeneration phase to desorb HO and COfrom the adsorbent bed using a regeneration gas and routing the HO and CO-laden regeneration gas to upstream of the pre-purification unit, where said regeneration gas is formed by routing a regeneration portion of the synthesis gas product stream through a compressor, and the regeneration phase of the TSA cycle comprising multiple steps includinga pressurization step to increase the pressure of the adsorbent bed to be regenerated in a controlled manner using the regeneration gas;{'sub': 2', '2, 'a heating step to heat the regeneration gas in a heater and supplying it to the adsorbent bed to remove HO and COfrom the adsorbent bed;'}a first cooling step in which heat addition to the heater stops while continuing the flow of the regeneration gas through the heater and the adsorbent bed;a second cooling step to cool the ...

METHOD AND SYSTEM FOR PRODUCING HIGH-CARBON DRI USING SYNGAS

Producing direct reduced iron (DRI) having chemically-combined carbon includes providing DRI at a temperature above 400° C., providing a first gas stream including hydrogen and carbon monoxide, passing the first gas stream through a methane forming process to yield a second gas stream containing a higher concentration of methane than the first gas stream; and contacting the second gas stream with the DRI. A system for producing the DRI includes a vessel for containing DRI at a temperature above 400° C., a methane forming reactor containing a catalyst bed for producing methane from a first gas stream containing hydrogen and carbon monoxide, a first conduit to feed a gas stream including hydrogen and carbon monoxide to the methane forming reactor, and a second conduit to feed the second gas stream to the vessel containing the DRI. 1. A process for producing DRI having chemically-combined carbon , comprising:providing DRI at a temperature above 400° C.;providing a first gas stream comprising hydrogen and carbon monoxide;passing said first gas stream through a methane forming process where methane is produced from said hydrogen and carbon monoxide resulting in a second gas stream containing a higher concentration of methane than said first gas stream; andcontacting said second gas stream with said DRI.2. A process for producing DRI having a controlled amount of chemically-combined carbon claim 1 , according to claim 1 , wherein said first gas stream contains hydrogen claim 1 , carbon monoxide and carbon dioxide and wherein the ratio of H/(CO+CO) in the gas fed to the methane forming reactor is in the range between 2.5 and 3.5.3. A process for producing DRI having a controlled amount of chemically-combined carbon claim 1 , according to claim 1 , wherein said second gas stream contains at least 20% by volume of methane.4. A process for producing DRI having a controlled amount of chemically-combined carbon claim 1 , according to claim 1 , wherein said methane forming ...

METHOD AND INSTALLATION FOR CRYOGENIC SEPARATION OF A GASEOUS MIXTURE BY METHANE SCRUBBING

In a process for the combined production of a) a hydrogen-enriched gas and a carbon monoxide-enriched gas and/or b) a mixture of hydrogen and carbon monoxide by cryogenic distillation and scrubbing, a still liquor is extracted from a scrubbing column and sent to a stripping column, a still liquor is extracted from the stripping column and sent to a separating column for carbon monoxide and methane and a cooling fluid is used at a pressure greater than that of the head of the separating column for cooling at least one fluid extracted at an intermediate level from the scrubbing column. 115-. (canceled)16. A process for the combined production a) of a hydrogen-enriched gas and a carbon monoxide-enriched gas and/or b) a mixture of hydrogen and carbon monoxide and optionally methane by cryogenic distillation and scrubbing , in which:a. a gaseous mixture containing at least hydrogen, carbon monoxide and methane and optionally nitrogen is cooled in a heat exchangerb. the cooled mixture is sent to a scrubbing columnc. a methane-rich liquid is introduced into the scrubbing column as scrubbing liquidd. a hydrogen-enriched gas is drawn off as top gas from the scrubbing columne. a vessel liquid is drawn off from the scrubbing column and sent to a stripping columnf. a vessel liquid is drawn off from the stripping column and sent to a column for separating carbon monoxide and methaneg. at least a portion of the vessel liquid from the separation column constitutes the liquid of step iii), andh. a carbon monoxide-rich fluid is used as coolant fluid for cooling at least one fluid drawn off at an intermediate level of the scrubbing columnwherein the fluid serving to cool the at least one fluid drawn off at an intermediate level of the scrubbing column is at a greater pressure than that of the top of the separation column, and in that the fluid having served to cool the at least one fluid drawn off at an intermediate level of the scrubbing column is sent to an intermediate level of a ...

SELECTIVE CARBON DIOXIDE REDUCTION CATALYZED BY SINGLE METAL SITES ON CARBON NITRIDE UNDER VISIBLE LIGHT IRRADIATION

A composition of a photocatalyst, a method of manufacturing the photocatalyst, and a method of chemically reducing carbon dioxide to carbon monoxide using the photocatalyst under visible-light irradiation is provided. The photocatalyst comprises a transition metal ion and graphitic carbon nitride and includes single metal sites on carbon nitride. Under visible light, the metal sites that are coordinated to nitrogen atoms get activated, without the use of additional ligands, to catalyze the reduction of carbon dioxide to selectively produce carbon monoxide. The photocatalytic reduction of carbon dioxide to carbon monoxide is highly efficient, resulting a turnover number of more than 800 for carbon monoxide production in 2 hours. The composition is useful in converting carbon dioxide into useful chemicals and carbon-based fuels. A functional model of molecular catalysts for efficient carbon dioxide reduction is also present. 1. A photocatalyst comprising:a graphitic carbon nitride providing nitrogen atoms for direct coordination with a transition metal ion in absence of additional ligands, the transition metal ion forming coordinate bonds with the nitrogen atoms at the edge sites of the graphitic carbon nitride, the nitrogen atoms forming a plane within the graphitic carbon nitride, and the transition metal ion being positioned outside the plane.2. The photocatalyst of claim 1 , wherein the transition metal ion is Co.3. The photocatalyst of claim 2 , wherein Cois at a concentration between 0.004 and 0.430 μmol/mg of the photocatalyst.4. The photocatalyst of claim 2 , wherein Cois uniformly distributed on the graphitic carbon nitride.5. The photocatalyst of claim 2 , wherein a molar ratio of Coto cobalt oxide in the photocatalyst is greater than 1000.6. The photocatalyst of claim 1 , wherein the graphitic carbon nitride is planar.7. The photocatalyst of claim 1 , wherein the graphitic carbon nitride includes carbon doping.8. The photocatalyst of claim 1 , wherein the ...

CARBON DIOXIDE CONVERSION METHOD USING METAL OXIDES

The present invention relates to a catalyst for converting COto synthetic fuel such as CO using metal oxides and a conversion method using the same. The COconversion catalyst according to the present invention can treat a large amount of COper unit mole and is oxidized. In the reduction cycle, the catalyst has relatively high structural stability and excellent long-term stability as a catalyst, and it has excellent activity as a COdecomposition catalyst that can be used in a continuous flow reactor, such as for COdecomposition at a relatively low temperature. 1. A catalyst for converting COhaving a composition represented by Formula 1:{'br': None, 'sub': 1-x', 'y, 'SrFeCoO(SFCO),\u2003\u2003[Formula 1]'}wherein: 0≤x<1, and 2.0≤y≤4.0.2. The catalyst of claim 1 , wherein in Formula 1 claim 1 , x is 0.2-0.8.3. A catalyst for converting COhaving a composition represented by Formula 2:{'br': None, 'sub': '3−δ', 'SrFeO (SFO),\u2003\u2003[Formula 2]'}wherein δ≤1.4. The catalyst of claim 1 ,wherein the catalyst has a particle size of 0.7 μm or less.5. A COconversion method using a metal oxide:{'sub': '2', 'claim-ref': {'@idref': 'CLM-00001', 'claim 1'}, 'wherein the conversion method comprises the steps of selecting a catalyst for COconversion of any one of the catalysts described in ;'}introducing the selected catalyst into a quartz reactor;injecting a reducing gas into the reactor and performing heat-treatment to activate the catalyst; and{'sub': 2', '2, 'injecting a gas containing COinto the quartz reactor and performing heat-treatment to induce a COconversion reaction,'}{'sub': '2', 'wherein the reducing gas is one among an inert gas, hydrogen, and CO; the heat-treatment temperature of the catalyst activation step is in the range of 100-1000° C.; and the heat-treatment temperature of the step of inducing the COconversion reaction is in the range of 300-800° C.'}6. The method of claim 5 ,{'sub': '2', 'wherein the heat-treatment temperature of the step of inducing the ...

PURIFICATION PROCESS FOR PRODUCTION OF ULTRA HIGH PURITY CARBON MONOXIDE

Methods and apparatus for the production of ultra high purity carbon monoxide having a carbon dioxide content of 0.1 ppm or less is disclosed. Carbon dioxide is removed from a product stream using a reversing heat exchanger to freeze the carbon dioxide out of the product stream, This provides the ultra high purity carbon monoxide product which meets the requirements of the electronic industry applications. 1. A method of producing ultra high purity carbon monoxide characterized in that a carbon monoxide stream is cooled in a reversing heat exchanger for freezing out removing carbon dioxide and whereas the gas stream is afterwards directed to a snow trap for removing solid particles and Whereas the gas stream is after the snow trap direct to a liquefier and hydrogen removal vessel , wherein the carbon monoxide is liquefied and hydrogen remains in a gaseous state and is separated.2. The method of producing ultra high purity carbon monoxide according to claim 1 , characterized in that as cooling agent in the reversing heat exchanger claim 1 , in the snow trap and in the liquefier and hydrogen removal vessel liquid nitrogen is used.3. The method of producing ultra high purity carbon monoxide according to wherein the liquid ultra high purity carbon monoxide is compressed by a diaphragm compressor or a cryogenic liquid pump and stored in gas cylinders.4. The method of producing ultra high purity carbon monoxide according to claim 1 , characterized in that the content of carbon dioxide and hydrogen in the ultra high purity carbon monoxide is 0.1 ppm or less.5. An apparatus for producing ultra high purity carbon monoxide characterized in that the apparatus comprises a heat exchanger claim 1 , which is connected to a snow trap claim 1 , which is also connected to a liquefier and hydrogen removal vessel.6. The apparatus for producing ultra high purity carbon monoxide according to claim 5 , characterized in that the heat exchanger claim 5 , the snow trap claim 5 , the ...

MITIGATING OXYGEN, CARBON DIOXIDE AND/OR ACETYLENE OUTPUT FROM AN ODH PROCESS

A method of converting one or more alkanes to one or more alkenes that includes a) providing a first stream containing one or more alkanes and oxygen to an oxidative dehydrogenation reactor; b) converting at least a portion of the one or more alkanes to one or more alkenes in the oxidative dehydrogenation reactor to provide a second stream exiting the oxidative dehydrogenation reactor containing one or more alkanes, one or more alkenes, oxygen, carbon monoxide and optionally acetylene; and c) providing the second stream to a second reactor containing a catalyst that includes a group 11 metal to convert a least a portion of the carbon monoxide to carbon dioxide and reacting the acetylene. 1. A method of converting one or more alkanes to one or more alkenes comprising:a. providing a first stream comprising one or more alkanes and oxygen to an oxidative dehydrogenation reactor;b. converting at least a portion of the one or more alkanes to one or more alkenes in the oxidative dehydrogenation reactor to provide a second stream exiting the oxidative dehydrogenation reactor comprising one or more alkanes, one or more alkenes, and one or more of oxygen, carbon monoxide and carbon dioxide; and{'sub': 2', '2', '2, 'c. providing the second stream to a second reactor containing a catalyst comprising a group 11 metal and optionally a promoter comprising CeO, ZrOand combinations thereof supported on SiOto convert at least a portion of the carbon monoxide to carbon dioxide.'}2. The method according to claim 1 , wherein the one or more alkanes comprise ethane.3. The method according to claim 1 , wherein the one or more alkenes comprise ethylene.5. The method according to claim 1 , wherein the first stream comprises one or more inert diluents claim 1 , an oxygen containing gas and a gas containing one or more lower alkanes.6. The method according to claim 1 , wherein the second stream comprises one or more unreacted lower alkanes; one or more lower alkenes; oxygen; one or more inert ...

Method for modifying carbon dioxide using technical carbon as a catalyst (versions)

FIELD: gas industry. SUBSTANCE: invention relates to a method for producing synthetic gas by carbon dioxide reforming. Method includes feeding hydrocarbon and carbon dioxide in ratio from 1 to 10 into a reactor with fluidized bed using particles of technical carbon as a catalyst. Hydrocarbon interacts with carbon dioxide in fluidization conditions to produce a gaseous product containing synthetic gas, and simultaneous forming particles of technical carbon in a reactor in higher amount. Gaseous product is discharged from the reactor. At least part of technical carbon particles are separated. Remaining technical carbon particles are directed to recirculation into a reactor with the fluidized bed. EFFECT: technical is increased reaction capacity and catalyst activity; possibility to control the ratio of carbon monoxide and hydrogen monoxide in the obtained synthesis gas; possibility to reuse technical carbon, formed as a result of carbon dioxide reforming. 16 cl, 2 ex, 4 tbl, 10 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 597 084 C2 (51) МПК C01B 3/38 (2006.01) C01B 3/44 (2006.01) B01J 21/18 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2015101053/05, 10.06.2013 (24) Дата начала отсчета срока действия патента: 10.06.2013 (72) Автор(ы): КИМ Чи Мин (KR), ХАН Ги Ён (KR) 25.06.2012 KR 10-2012-0067906 (43) Дата публикации заявки: 10.08.2016 Бюл. № 22 R U (73) Патентообладатель(и): ЭсКей ИННОВЕЙШН КО., ЛТД. (KR), ЭсКей ГЛОБАЛ КЭМИКАЛ КО., ЛТД. (KR) Приоритет(ы): (30) Конвенционный приоритет: (45) Опубликовано: 10.09.2016 Бюл. № 25 C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 26.01.2015 (86) Заявка PCT: KR 2013/005070 (10.06.2013) 2 5 9 7 0 8 4 (87) Публикация заявки PCT: R U 2 5 9 7 0 8 4 (56) Список документов, цитированных в отчете о поиске: FIDALGO, Beatriz et al., "Carbon Materials as Catalysts for Decomposition and CO2 Reforming of Methane: A review", Chinese Journal of ...

PROCESS FOR THE CONVERSION OF CARBON DIOXIDE

A process for the production of syngas, the process comprising (i) reacting at least a portion of carbon dioxide with hydrogen within an initial reactor to produce an initial product stream including carbon monoxide, water, unreacted carbon dioxide, and unreacted hydrogen; and (ii) reacting at least a portion of the unreacted carbon dioxide and unreacted hydrogen within a reactor downstream of the first reactor to thereby produce a product stream including carbon monoxide, water, unreacted carbon dioxide, and unreacted hydrogen. 1. A process for the production of syngas , the process comprising:(i) reacting at least a portion of carbon dioxide with hydrogen within an initial reactor to produce an initial product stream including carbon monoxide, water, unreacted carbon dioxide, and unreacted hydrogen; and(ii) reacting at least a portion of the unreacted carbon dioxide and unreacted hydrogen within a reactor downstream of the first reactor to thereby produce a product stream including carbon monoxide, water, unreacted carbon dioxide, and unreacted hydrogen.2. The process of claim 1 , where the carbon dioxide and the hydrogen include at least 50 mol % of the reactants within the initial reactor.3. The process of claim 2 , where the reactor includes less than 10 mol % methane relative to the total moles of reactants within the initial reactor.4. The process of claim 1 , where the initial product stream has a temperature T1 when exiting the initial reactor claim 1 , where the product stream has a temperature T2 when exiting the downstream reactor claim 1 , and where T2>T1 claim 1 , and where T1 is from about 300 to about 1000° C. claim 1 , and where T2 is from about 500 to about 1200° C.5. (canceled)6. The process of claim 1 , where the reactor downstream of the first reactor is a final reactor in series claim 1 , where the product stream produced by said final reactor is the final product stream claim 1 , and where the process further includes reacting unreacted carbon ...

PROCESS AND APPARATUS FOR THE SEPARATION OF A MIXTURE OF HYDROGEN AND CARBON MONOXIDE AT LOW TEMPERATURE

In a process for the separation of a mixture containing hydrogen and carbon monoxide to produce gaseous hydrogen, the mixture is cooled down to a temperature below −180° C. and then separated at a temperature below −100° C. to produce a gas enriched in hydrogen and a fluid enriched in carbon monoxide, at least a part of the gas enriched in hydrogen is sent to a pressure swing adsorption separation apparatus operating at a temperature above 0° C. to produce a gas rich in hydrogen at a pressure of at least 20 bars, and at least a part of the gas rich in hydrogen is cooled in the heat exchanger down to a temperature below −100° C., reduced in pressure in a turbine down to a pressure of at least 8 bars and reheated in the heat exchanger to constitute a product rich in hydrogen at a pressure of at least 8 bars. 1. A process for the separation of a mixture containing hydrogen and carbon monoxide to produce gaseous hydrogen , comprising:i) cooling the mixture in a heat exchanger down to a temperature below −180° C. and then separating the cooled mixture at a temperature below −100° C. by at least one stage of partial condensation and/or distillation and/or scrubbing in order to produce a gas enriched in hydrogen and a fluid enriched in carbon monoxide,ii) sending at least a part of the gas enriched in hydrogen to a pressure swing adsorption separation apparatus operating at a temperature above 0° C. in order to produce a gas rich in hydrogen at a pressure of at least 20 bars andiii) cooling at least a part of the gas rich in hydrogen in the heat exchanger down to a temperature below −100° C., reducing the pressure of the cooled gas rich in hydrogen in a turbine down to a pressure of at least 8 bars and reheating the reduce pressure gas the heat exchanger in order to constitute a product rich in hydrogen at a pressure of at least 8 bars.2. The process according to claim 1 , wherein at least a part of the gas enriched in hydrogen is reheated in the heat exchanger upstream of ...

ELECTRICALLY HEATED CARBON MONOOXIDE REACTOR

A reactor system and a process for carrying out reverse water gas shift reaction of a feedstock comprising COand Hto a first product gas comprising CO are provided, where a methanation reaction take place in parallel to the reverse water gas shift reaction, and where the heat for the endothermic reverse water gas shift reaction is provided by resistance heating. 1. A reactor system for carrying out a reverse water gas shift reaction for production of a first product gas comprising CO from a feedstock comprising COand H , said reactor system comprising:{'sub': 2', '2, 'a supply of feedstock comprising COand H;'}a structured catalyst comprising a macroscopic structure of an electrically conductive material and a catalytically active material capable of catalysing both the reverse water gas shift reaction and a methanation reaction;the structured catalyst arranged for being operated under such temperature and pressure that both the reverse water gas reaction and the methanation reaction take place;a pressure shell housing said structured catalyst, said pressure shell comprising an in-let for letting in said feedstock and an outlet for letting out product gas, wherein said inlet is positioned so that said feedstock enters said structured catalyst in a first end of said structured catalyst and said product gas exits said structured catalyst from a second end of said structured catalyst;a heat insulation layer between said structured catalyst and said pressure shell;at least two conductors electrically connected to said structured catalyst and to an electrical power supply placed outside said pressure shell, wherein said electrical power supply is dimensioned to heat at least part of said structured catalyst to a temperature of at least 500° C. by passing an electrical current through said macroscopic structure, wherein said at least two conductors are connected to the structured catalyst at a position on the structured catalyst closer to said first end of said structured ...

Procedimiento de preparacion de un gas rico en oxido de carbono.

EL PROCESO PARA LA PREPARACION DE GAS RICO EN MONOXIDO DE CARBONO CONSTA DE LA REACCION DE UN GAS MEZCLADO DE HIDROGENO Y DIOXIDO DE CARBONO EN PRESENCIA DE UN CATALIZADOR CONVERSOR A GAS RICO EN MONOXIDO DE CARBONO, CUYO PROCESO ADEMAS CONSISTE EN HACER REACCIONAR PARTE DEL DIOXIDO DE CARBONO E HIDROGENO EN EL ALIMENTADOR DEL GAS EN UNA REACCION EXOTERMICA PARA DAR METANO EN UNA REACCION SIMULTANEA A LA DE PRODUCCION DE MONOXIDO DE CARBONO PRODUCIENDO REACCION Y LLEVANDO A CABO AMBAS REACCIONES BAJO CONDICIONES ADIABATICAS, DE MODO QUE LA REACCION EXOTERMICA DE PRODUCCION DE METANO EXOTERMICAMENTE SUMINISTRA EL CALOR NECESARIO PARA LA REACCION DE PRODUCCION EXOTERMICA DE MONOXIDO DE CARBONO.

Mitigating oxygen, carbon dioxide and/or acetylene output from an ODH process

A method of converting one or more alkanes to one or more alkenes that includes a) providing a first stream containing one or more alkanes and oxygen to an oxidative dehydrogenation reactor; b) converting at least a portion of the one or more alkanes to one or more alkenes in the oxidative dehydrogenation reactor to provide a second stream exiting the oxidative dehydrogenation reactor containing one or more alkanes, one or more alkenes, oxygen, carbon monoxide and optionally acetylene; and c) providing the second stream to a second reactor containing a catalyst that includes a group 11 metal to convert a least a portion of the carbon monoxide to carbon dioxide and reacting the acetylene.

Patent JPH0480725B2

Gas separation process

Hydrogen and carbon monoxide are each separately recovered in high yield from a multicomponent gas stream containing these compounds to­gether with carbon dioxide and a zero to minor amount of one or more gaseous components from the group consisting of nitrogen, methane, water vapor and C₁-C₆ hydrocarbons, by a process wherein the multicomponent gas stream, such as that obtained by steam methane reforming, is initial­ly treated in a pressure swing adsorption unit to remove water and CO₂, and the obtained effluent freed of CO₂ and water is then further sub­jected to (1) cryogenic fractionation to condense CO and to (2) hydrogen purification by selective adsorption (in either order) to recover high purity carbon monoxide and essentially pure hydrogen. The CO₂-laden adsorbent is regenerated by purging with a H₂O and CO₂-free waste gas stream from the hydrogen purification adsorbent bed or from the cryogenic fractionation or from both of these.

Adsorptive process for producing two gas streams from a gas mixture

PROCESS AND PLANT FOR THE PRODUCTION OF CARBON MONOXIDE AND HYDROGEN

Cryogenic H2 and carbon monoxide production with an impure carbon monoxide expander

A process for obtaining purified carbon monoxide from a gaseous mixture of hydrogen and carbon monoxide and one or more additional impurities to be removed by one or more vapor-liquid separation devices is provided which includes the steps of providing a feed stream of the gaseous mixture, cooling and partially condensing the feed stream to partially separate the feed stream into at least one hydrogen rich vapor substream and at least one carbon monoxide rich liquid substream, withdrawing a first and a second substream from one of the carbon monoxide rich substreams, passing the first substream through a first expansion valve to let down the pressure to a pressure nominally the same as that of a vapor-liquid separation device downstream, vaporizing the second substream using a heat exchange device to produce a third substream at a pressure substantially above that of the vapor-liquid separation device, passing the third substream through a work extraction device to provide a substantial portion of all refrigeration for cooling for the process, feeding the third substream to the vapor-liquid separation device, and withdrawing substantially purified carbon monoxide from the vapor-liquid separation device. A similar apparatus is also disclosed.

Integrated processes for the production of carbon monoxide

The present invention is an integrated process for the adsorptive recovery of a high purity carbon monoxide product from a gas mixture containing hydrogen, carbon monoxide, carbon dioxide, methane, and nitrogen, with the potential additional recovery of a hydrogen-rich stream and the recycle of the resulting gas mixture to a reformation reaction to produce the gas mixture with a more favorable carbon monoxide and hydrogen product slate. Separate carbon dioxide recovery can be performed. Hydrogen recovery can be either by adsorptive or by membrane technology. The process achieves high recoveries at reduced capital cost and at reduced product cost.

利用炭黑催化剂来改造二氧化碳的方法

本发明涉及一种方法，包括以下步骤：利用炭黑催化剂，通过使烃与二氧化碳反应来制备包含一氧化碳和氢气的合成气。

Способ получения синтетического газа

Изобретение относится к получению синтетического газа и может быть использовано в химической промышленности. Способ получения синтетического газа включает введение метана и углекислого газа в реакционную камеру. Через реакционную камеру направляют слой углеродсодержащего твердого материала как движущийся слой. В слое углеродсодержащего твердого материала метан и углекислый газ преобразовывают в водород и окись углерода. Образующийся в реакционной камере синтетический газ противотоком подводят к движущемуся слою и в нем охлаждают. В качестве углеродсодержащего твердого материала применяют углеродсодержащий гранулят, содержащий по меньшей мере 80 мас. % углерода. Изобретение позволяет обеспечить непрерывный режим получения синтетического газа, при котором не требуется регенерация катализатора, создать поток газообразного продукта, который в основном лишен примеси твердых частиц. 12 з.п. ф-лы, 1 ил. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 610 082 C2 (51) МПК C01B 3/34 (2006.01) B01J 8/08 (2006.01) C10J 1/20 (2006.01) C10J 1/26 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ФОРМУЛА (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ 2014103786, 05.07.2012 (24) Дата начала отсчета срока действия патента: 05.07.2012 Дата регистрации: Приоритет(ы): (30) Конвенционный приоритет: 05.07.2011 DE 102011106642.3 (73) Патентообладатель(и): ЛИНДЕ АКЦИЕНГЕЗЕЛЛЬШАФТ (DE), БАСФ СЕ (DE) (45) Опубликовано: 07.02.2017 Бюл. № 4 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 05.02.2014 (56) Список документов, цитированных в отчете о поиске: EP 0191522 A2, 20.08.1986. RU (86) Заявка PCT: EP 2012/002837 (05.07.2012) 2361809 C2, 20.07.2009. US 2003/0208959 A1, 13.11.2003. CH 409890 A, 31.03.1966. US 4726913 A, 23.02.1988. US 2003182861 A1, 02.10.2003. (87) Публикация заявки PCT: 2 6 1 0 0 8 2 R U Адрес для переписки: 129090, Москва, ул. Б. Спасская, 25, строение 3, ООО "Юридическая фирма Городисский и Партнеры" (54) СПОСОБ ПОЛУЧЕНИЯ ...

일산화탄소가 풍부한 가스의 제조방법

변환촉매의 존재하에서 수소와 이산화탄소의 혼합가스를 반응시켜서 일산화탄소가 풍부한 가스를 생성시키는 방법으로서, 그 반응은 또한 일산화탄소 생성반응과 함께 공급가스중 이산화탄소와 수소의 일부를 발열적으로 반응시켜 메탄과 형성시키는 반응을 포함하고 그 두가지 반응을 단열상태하에서 수행하여, 발열반응인 메탄생성 반응이 흡열반응인 일산화탄소 생성반응에 필요한 열을 공급하는 것으로 이루어진 것을 특징으로 하는 일산화탄소가 풍부한 가스의 제조방법.

联合生产氨合成混合物和一氧化碳的方法和设备

本发明涉及一种生产氨合成混合物和一氧化碳的方法。在氮清洗塔(61)中提纯氢。在中压汽提塔(62)中，然后在低压蒸馏塔(63)中，从在所述氮清洗塔(61)底部收集的第一种液体馏分(51)中低温回收一氧化碳。从洗涤塔(61)的顶部和底部之间的中间位置排出第二种液体馏分(52)。

탄화수소로부터 수소의 연속적인 제조방법

본 발명은 활성이 떨어진 금속촉매를 재생시켜 재생된 금속촉매를 생성하여, 고순도의 수소를 높은 수율로 연속적으로 생성할 수 있는 탄화수소로부터 수소의 제조방법에 관한 것이다. 이에 따른 제조방법은 활성을 잃은 고체탄소가 침착된 금속촉매로부터 재생된 금속촉매를 생성할 수 있고, 재생된 금속촉매를 탄화수소로부터 수소를 생성하기 위한 촉매분해 반응에 재사용함으로써 새로운 금속촉매의 투입이나 교체 없이도 고순도의 수소를 높은 수율로 연속적으로 생성할 수 있다.

Method for catalytic production of gas rich in carbon oxide

FIELD: chemical technology. SUBSTANCE: hydrogen-containing gas and gas containing carbon dioxide are mixed and heated. The process is carried out in adiabatic condition under pressure and with the help of catalyst. Thus gas containing carbon oxide and methane is obtained. EFFECT: improved efficiency of the method. 5 cl ДОС ПЧ Го РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) 13) ВИ” 2110 477 Сл 5 МК © 01 В 31/18 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 93056193/25, 10.12.1993 (30) Приоритет: 10.12.1992 ОК 1489/92 (46) Дата публикации: 10.05.1998 (56) Ссылки: ЕК, заявка, 2593164, кл. С 01 В 31/18, 1987. (71) Заявитель: Хальдор Топсеэ А/С (ОК) (72) Изобретатель: Рикард Ваннби[0К], Шарлотте Штуб Нильзен[0К] (73) Патентообладатель: Хальдор Топсеэ А/С (ОК) (54) СПОСОБ КАТАЛИТИЧЕСКОГО ПОЛУЧЕНИЯ (57) Реферат: Использование: в производстве богатого окисью углерода газа. Сущность изобретения: водородсодержащий газ и содержащий двуокись углерода газ смешивают и БОГАТОГО ОКИСЬЮ УГЛЕРОДА ГАЗА нагревают при давлении на катализаторе в адиабатических условиях с получением газа, содержащего окись углерода и метан. 4 З.П. ф-лы. 2110477 С1 КО ДОС ПЧ Го КУЗЗАМ АСЕМСУ ГОК РАТЕМТ$ АМО ТКАОЕМАКК$ (19) ВИ "” 2110 477. 13) СЛ о ° © 01 В 31/18 12) АВЗТКАСТ ОЕ 1МУЕМТОМ (21), (22) АррИсаНоп: 93056193/25, 10.12.1993 (30) Рпошу: 10.12.1992 ОК 1489/92 (46) Рае ог рибИсаНоп: 10.05.1998 (71) АррИсапе: Кпа!’аог Торзеей А/$ (ОК) (72) пуетог. — ЕКага Уапп [ОК], Зпапове ЭМиь МИ'7еп[0К] (73) Ргорпеюг: Кпа!’аог Торзеей А/$ (0К) (54) МЕТНОО РОК САТАЕУТ!С РКОВИСТЮМ ОЕ САЗ ЕСН 1М САВКВОМ ОХШЕ (57) АБзГасЕ: НЕЕО: спеглсеа! 1есйптпоюду. ЗУВЗТАМСЕ: пуадгодеп-сощатта даз апа даз сощатта сагроп Чюхае аге пихеяа апа Пезея. Тпе ргосез$ 15 сатмед оШ шт адарацс -2- сопаШоп ипаег ргеззиге апа м Ше пер ог саамуз. ТПу$ 9даз сотатта сагроп ох4е ап тешпапе 15 оМатея. ЕЕЕЕСТ: ипргоуеа ейаепсу о {пе тапоа. 5 < 2110477 С1 КО ДУтОГЕсС ПЧ ГЭ Изобретение относится к производству ...

Synthesis gas generation process

FIELD: synthesis gas production. SUBSTANCE: synthesis gas is generated by catalytic interaction of an organic compound with water steam and carbon dioxide, amount of steam corresponding to 2 mole water or less per 1 mole organic compound and 0.1 to 10 mole water per 1 mole carbon dioxide. Process is conducted at 600-1000 C, pressure 5-40 kg/cu.cm, and average hourly volumetric gas intake 100 to 10000 h -1 . Catalyst contains 0.001 to 0.08 mol % rhodium and/or ruthenium on magnesium oxide carrier and has specific surface 5.8 sq.m/g. EFFECT: reduced production expenses. 5 cl, 21 ex _ сб гоОсс ПЧ сэ (19) РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ ВИ `” 2 201 392 ' (51) МПК” 13) С2 С Ол В 3/38 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 99123630/12, 13.04.1998 (24) Дата начала действия патента: 13.04.1998 (30) Приоритет: 11.04.1997 УР 9/110436 30.04.1997 УР 9/126304 29.08.1997 УР 9/250062 (46) Дата публикации: 27.03.2003 (56) Ссылки: КУ 2058813 С1, 27.04.1996. КУ 2055014 СЛ, 21.02.1996. $4 1831468 АЗ, 30.07.1993. ЕР 0303438 АЗ, 15.02.1989. ЕР 0629578 АЛ, 21.12.1994. ЕР 0367654 А, 09.05.1990. (85) Дата перевода заявки РСТ на национальную фазу: 11.11.1999 (86) Заявка РСТ: УР 98/01687 (13.04.1998) (87) Публикация РСТ: М/О 98/46524 (22.10.1998) (98) Адрес для переписки: 129010, Москва, ул. Б. Спасская, 25, стр.3, ООО "Юридическая фирма Городисский и Партнеры", пат.пов. Е.В.Томской, рег.№ 106 (71) Заявитель: . ЧИЕДА КОРПОРЕИШН (уР) (72) Изобретатель: ЙАГИ Фуюки (.Р), НАГУМО Ацуро ()Р), ВАДА Юкитака (УР), СИМУРА Мицунори (+Р), АСАОКА Сатио (УР), ВАКАМАЦУ Сухеи (.Р) (73) Патентообладатель: ЧИЕДА КОРПОРЕЙШН (.Р) (74) Патентный поверенный: Томская Елена Владимировна (54) СПОСОБ ПОЛУЧЕНИЯ СИНТЕЗ-ГАЗА (57) Изобретение предназначено для получения синтез-газа. Способ получения синтез-газа включает взаимодействие углеродсодержащего органического соединения с паром и диоксидом углерода в присутствии катализатора. Количество пара составляет 2 моль ...

Continuously preparation method of hydrogen from hydrocarbon

본 발명은 활성이 떨어진 금속촉매를 재생시켜 재생된 금속촉매를 생성하여, 고순도의 수소를 높은 수율로 연속적으로 생성할 수 있는 탄화수소로부터 수소의 제조방법에 관한 것이다. 이에 따른 제조방법은 활성을 잃은 고체탄소가 침착된 금속촉매로부터 재생된 금속촉매를 생성할 수 있고, 재생된 금속촉매를 탄화수소로부터 수소를 생성하기 위한 촉매분해 반응에 재사용함으로써 새로운 금속촉매의 투입이나 교체 없이도 고순도의 수소를 높은 수율로 연속적으로 생성할 수 있다. The present invention relates to a method for producing hydrogen from a hydrocarbon capable of continuously generating high-purity hydrogen with a high yield by regenerating a metal catalyst with low activity to produce a regenerated metal catalyst. The manufacturing method according to this can generate a regenerated metal catalyst from a metal catalyst on which solid carbon that has lost its activity, and reuse the regenerated metal catalyst in a catalytic decomposition reaction to generate hydrogen from a hydrocarbon, thereby introducing a new metal catalyst or High purity hydrogen can be continuously produced in high yield without replacement.

制备合成气的方法

本发明提供了制备合成气(3)的方法，其中将甲烷和二氧化碳(2)引入反应空间(R)并使之在升高的温度下在固体(W)的存在下生成氢和一氧化碳。使所述甲烷和二氧化碳通过含碳的颗粒材料(W)并在高温区(H)反应。

Reforming apparatus, reforming method, apparatus for producing chemical products equipped with reforming apparatus and method of producing chemical products

FIELD: oil and gas industry. SUBSTANCE: invention relates to petrochemical industry. Natural gas 21 is fed into compressor 11. Compressed natural gas 21 is successively heated in fourth 20 and first 12 heat exchangers. In first heat exchanger 12 heat source used is flue gases 22. Heated natural gas 21 is fed into desulphuration device 13. In apparatus 14 there is reforming of natural gas purified from sulphur-containing compounds, and H 2 and CO or H 2 and CO 2 are obtained. Gas subjected to reforming is used for synthesis of ammonia, urea and methanol. In second heat exchanger 16 air 26 used for heating in reforming apparatus 14 is heated. Water 75 is heated by flue gases 22 in third heat exchanger 19. EFFECT: invention improves thermal efficiency during reforming of natural gas, prevents corrosion, improves efficiency of producing ammonia, urea and methanol. 6 cl, 19 dwg, 6 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 606 606 C2 (51) МПК C01B 3/38 (2006.01) C01C 1/04 (2006.01) C07C 273/10 (2006.01) C07C 29/151 (2006.01) C07C 31/04 (2006.01) B01D 53/48 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ФОРМУЛА (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ 2015106410, 03.09.2013 (24) Дата начала отсчета срока действия патента: 03.09.2013 Дата регистрации: Приоритет(ы): (30) Конвенционный приоритет: 12.09.2012 JP PCT/JP2012/073374 (56) Список документов, цитированных в отчете о поиске: JPH 11263740 A, 28.09.1999. SU (45) Опубликовано: 10.01.2017 Бюл. № 1 579220 A1, 05.11.1977. RU 2203214 C1, 27.04.2003. RU 2258691 C1, 20.08.2005. JPH 06234517 A, 23.08.1994. JP 2001122812 A, 08.05.2001. JP 2000169411 A, 20.06.2000. (85) Дата начала рассмотрения заявки PCT на национальной фазе: 25.02.2015 (86) Заявка PCT: JP 2013/073705 (03.09.2013) (87) Публикация заявки PCT: 2 6 0 6 6 0 6 (43) Дата публикации заявки: 10.09.2016 Бюл. № 25 (73) Патентообладатель(и): МИЦУБИСИ ХЕВИ ИНДАСТРИЗ, ЛТД. (JP) R U 15.12.2016 (72) Автор(ы): САКУРАЙ Микия (JP), ...

处理合成气和相关气体的方法和装置

公开了一种改进的甲烷洗涤循环,其中需要少量的甲烷洗涤,由此节省了该循环操作的能量成本和建设该循环的投资成本。另外的实施方式可回收能量,并且提高一氧化碳和/或氢气产品的分离。

Parallel preparation of hydrogen, carbon monoxide and carbon-comprising product

FIELD: chemistry. SUBSTANCE: invention relates to a process for the parallel preparation of hydrogen, carbon monoxide and a carbon-comprising product. Described is a process for parallel preparation of hydrogen, carbon monoxide and a carbon-comprising product, wherein one or more hydrocarbons are thermally decomposed, wherein at least a part of the resulting hydrogen-containing gas mixture is removed from the reaction zone of the decomposition reactor at a temperature of 800 to 1400°C and converted with carbon dioxide to carbon monoxide- and hydrogen-containing gas mixture. EFFECT: technical result: a method for the parallel preparation of hydrogen, carbon monoxide and/or a solid carbon-containing product with a low carbon dioxide footprint at economically acceptable limiting conditions for the chemical industry. 13 cl, 6 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 650 171 C2 (51) МПК C01B 3/24 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C01B 32/40 (2018.02) (21)(22) Заявка: 2015129604, 17.12.2013 (24) Дата начала отсчета срока действия патента: Дата регистрации: 09.04.2018 21.12.2012 EP 12199043.6 (43) Дата публикации заявки: 27.01.2017 Бюл. № 3 (45) Опубликовано: 09.04.2018 Бюл. № 10 (73) Патентообладатель(и): БАСФ СЕ (DE) (85) Дата начала рассмотрения заявки PCT на национальной фазе: 21.07.2015 (56) Список документов, цитированных в отчете о поиске: RU 2441837 C2, 10.02.2012. RU IB 2013/061032 (17.12.2013) 2408529 C1, 10.01.2011. EP 601956 A3, 15.06.1994. CN 101249949 A, 27.08.2008. WO 2010069549 A1, 24.06.2010. (87) Публикация заявки PCT: R U 2 6 5 0 1 7 1 WO 2014/097142 (26.06.2014) Адрес для переписки: 105064, Москва, а/я 88, "Патентные поверенные Квашнин, Сапельников и партнеры" (54) ПАРАЛЛЕЛЬНОЕ ПОЛУЧЕНИЕ ВОДОРОДА, МОНООКСИДА УГЛЕРОДА И УГЛЕРОДСОДЕРЖАЩЕГО ПРОДУКТА (57) Реферат: Изобретение относится к способу деструкции при температуре от 800 до 1400°С и параллельного получения водорода, ...

Target gas separation method and target gas separation device

혼합 가스로부터 목적 가스를 농축 분리하는 방법은, 흡착제가 충전된 적어도 3개의 흡착탑을 이용해서 실시된다. 해당 방법에 있어서는, 흡착탑에 혼합 가스를 도입해서 혼합 가스 중의 목적 가스를 흡착제에 흡착시키고, 해당 흡착탑으로부터 비흡착 가스를 도출시키는 흡착공정과, 흡착탑에 세정 가스를 도입해서 해당 흡착탑으로부터 세정 오프 가스를 도출시키는 세정공정과, 흡착탑 내를 감압시켜서 흡착제로부터 목적 가스를 탈착시켜 해당 흡착탑으로부터 탈착 가스를 도출시키는 탈착공정을 포함하는 사이클을 각 흡착탑에서 반복해서 행한다. 사이클을 통해서 어느 하나의 흡착탑에서 흡착공정을 상시적으로 행한다. 탈착공정을 실행하는 탈착공정시간은 흡착공정을 실행하는 흡착공정시간보다도 길게 된다. The method of concentrating and separating the objective gas from the mixed gas is carried out using at least three adsorption towers filled with the adsorbent. According to the method, adsorption is carried out by introducing a mixed gas into an adsorption column to adsorb a target gas in a gas mixture to an adsorbent and deriving a non-adsorbed gas from the adsorption column; introducing a purge gas into the adsorption tower, And a desorption step of desorbing a target gas from the adsorbent by depressurizing the inside of the adsorption tower to derive a desorbing gas from the adsorption tower is repeatedly performed in each adsorption tower. The adsorption process is continuously performed in any one adsorption tower through the cycle. The desorption process time for performing the desorption process becomes longer than the adsorption process time for performing the adsorption process.

METHOD FOR PRODUCING SYNTHETIC GAS

1. Способ получения синтетического газа, по которому метан и углекислый газ вводят в реакционную камеру и в слое углеродсодержащего твердого материала преобразовывают в водород и окись углерода, отличающийся тем, что слой углеродсодержащего твердого материала направляют через реакционную камеру как движущийся слой, причем синтетический газ, который образуется в реакционной камере, противотоком подводят к движущемуся слою и там охлаждают в прямом теплообмене с углеродсодержащим твердым материалом.2. Способ по п. 1, отличающийся тем, что метан и углекислый газ преобразовывают при температурах между 800 и 1600°С, предпочтительно между 900 и 1400°С.3. Способ по п. 1 или 2, отличающийся тем, что в качестве углеродсодержащего твердого материала применяют углеродсодержащий гранулят, который содержит по меньшей мере 80 мас. % углерода и имеет зернистость от 0,1 до 100 мм.4. Способ по п. 1 или 2, отличающийся тем, что соотношение кислород/углерод в газообразных реагентах целенаправленно устанавливают таким образом, что углерод образуется в реакционной камере или отделяется от углеродсодержащего твердого материала.5. Способ по п. 1 или 2, отличающийся тем, что по меньшей мере часть тепловой энергии, которая требуется для производства синтетического газа, вырабатывается в реакционной камере и/или подается в реакционную камеру через горячий газ.6. Способ по п. 1 или 2, отличающийся тем, что углеродсодержащий твердый материал непрерывно направляют через реакционную камеру как движущийся слой.7. Способ по п. 1 или 2, отличающийся тем, что синтетический газ, который образуется в реакционной камере, охлаждают при циркуляции в углеродсодержащем � РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК C01B 3/34 (13) 2014 103 786 A (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2014103786/05, 05.07.2012 (71) Заявитель(и): ЛИНДЕ АКЦИЕНГЕЗЕЛЛЬШАФТ (DE), БАСФ СЕ (DE) Приоритет(ы): (30) Конвенционный приоритет: 05.07.2011 DE 102011106642.3 ( ...

Carbon monoxide production facility including cryogenic separator

Process for production of synthesis gas

합성 가스(3)의 제조를 위한 프로세스로서, 메탄 및 이산화탄소(2)가 반응 공간(R) 안으로 유입되고 수소 및 일산화탄소를 주기 위해 상승된 온도들에서 고체(W)의 존재 하에 반응된다. 메탄 및 이산화탄소는 탄소 함유 과립 재료(W)를 통과하고 고온 구역(H)에서 반응된다. As a process for the production of syngas 3, methane and carbon dioxide 2 are introduced into reaction space R and reacted in the presence of solid W at elevated temperatures to give hydrogen and carbon monoxide. Methane and carbon dioxide pass through the carbon-containing granular material (W) and are reacted in the hot zone (H).

Cobalt-based catalyst and CO 2 Method for preparing CO by catalytic hydrogenation

本发明属于二氧化碳催化转化技术领域，具体涉及一种钴基催化剂，还涉及一种采用上述钴基催化剂的CO 2 催化加氢制CO的方法。本发明的钴基催化剂由SBA‑15基体和负载在SBA‑15基体上的钴活性中心组成，所述钴活性中心由所述SBA‑15基体上负载的钴氧化物沉积层还原得到，所述钴氧化物沉积层以原子层沉积方式形成。本发明的钴基催化剂具有较好的催化活性以及稳定性。当本发明的钴基催化剂用于催化CO 2 加氢制CO时，具有较好的选择性以及稳定性。

Selective adsorption of carbon monoxide from gas streams

Zeolitic molecular sieves having high SiO 2 /Al 2 O 3 molar ratios and containing Cu + cations are found to exhibit a high degree of selectivity and affinity for CO molecules and are capable of separating CO from gas streams even when water vapor is present.

Sea urchin shape CoZnAl-LDH/RGO/g-C3N4Z-type hetero-junctions and its preparation method and application

本发明公开了一种海胆状CoZnAl‑LDH/RGO/g‑C 3 N 4 Z型异质结及其制备方法，其通过简单的水热反应制备而成，将经过超声分散的还原氧化石墨烯和石墨悬浮液逐滴加入到硝酸钴、硝酸锌、硝酸铝和尿素的去离子水溶液中，搅拌后转移至高压釜中进行高温水热反应，得到尺度介于5‑7μm的海胆状CoZnAl‑LDH/RGO/g‑C 3 N 4 Z型异质结。本发明的海胆状CoZnAl‑LDH/RGO/g‑C 3 N 4 Z型异质结具有较高的比表面积、光子利用率和光生电子、空穴分离效率，可应用于催化和能源转化领域。