NO860746L - THERMAL REFORM OF GAS HYDROCARBON. - Google Patents
THERMAL REFORM OF GAS HYDROCARBON.Info
- Publication number
- NO860746L NO860746L NO860746A NO860746A NO860746L NO 860746 L NO860746 L NO 860746L NO 860746 A NO860746 A NO 860746A NO 860746 A NO860746 A NO 860746A NO 860746 L NO860746 L NO 860746L
- Authority
- NO
- Norway
- Prior art keywords
- gas
- plasma generator
- reforming
- water vapor
- outlet
- Prior art date
Links
- 229930195733 hydrocarbon Natural products 0.000 title claims description 11
- 150000002430 hydrocarbons Chemical class 0.000 title claims description 11
- 239000004215 Carbon black (E152) Substances 0.000 title claims description 4
- 238000000034 method Methods 0.000 claims description 28
- 238000002407 reforming Methods 0.000 claims description 16
- 239000000203 mixture Substances 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 14
- 229910052799 carbon Inorganic materials 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 11
- 239000002893 slag Substances 0.000 claims description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 10
- 229910052717 sulfur Inorganic materials 0.000 claims description 9
- 239000011593 sulfur Substances 0.000 claims description 9
- 238000005255 carburizing Methods 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 239000007787 solid Substances 0.000 claims description 7
- 239000000370 acceptor Substances 0.000 claims description 6
- 239000000969 carrier Substances 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 2
- 235000019738 Limestone Nutrition 0.000 claims description 2
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 2
- 239000000571 coke Substances 0.000 claims description 2
- 238000006477 desulfuration reaction Methods 0.000 claims description 2
- 230000023556 desulfurization Effects 0.000 claims description 2
- 239000010459 dolomite Substances 0.000 claims description 2
- 229910000514 dolomite Inorganic materials 0.000 claims description 2
- 239000004571 lime Substances 0.000 claims description 2
- 239000006028 limestone Substances 0.000 claims description 2
- 241001669679 Eleotris Species 0.000 claims 1
- 239000007789 gas Substances 0.000 description 36
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 5
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 238000002303 thermal reforming Methods 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 239000002245 particle Substances 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010891 electric arc Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
- B01J12/002—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor carried out in the plasma state
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/342—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents with the aid of electrical means, electromagnetic or mechanical vibrations, or particle radiations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
- B01J2219/0894—Processes carried out in the presence of a plasma
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0211—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step
- C01B2203/0222—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step containing a non-catalytic carbon dioxide reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/049—Composition of the impurity the impurity being carbon
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0861—Methods of heating the process for making hydrogen or synthesis gas by plasma
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1276—Mixing of different feed components
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Health & Medical Sciences (AREA)
- Physics & Mathematics (AREA)
- Health & Medical Sciences (AREA)
- Combustion & Propulsion (AREA)
- Electromagnetism (AREA)
- Mechanical Engineering (AREA)
- Toxicology (AREA)
- Plasma & Fusion (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
- Carbon And Carbon Compounds (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Description
Foreliggende oppfinnelse vedrører en fremgangsmåte ved fremstilling av en i det vesentlige CO + r^-inneholdende gass ved termisk reformering av gassformige hydrogenkarbon-er, foreksempel CH^, med vanndamp i tilnærmet støkiometr-isk forhold samt en anordning for gjennomførsel av fremgangsmåten i henhold til oppfinnelsen. The present invention relates to a method for the production of an essentially CO + r^-containing gas by thermal reforming of gaseous hydrocarbons, for example CH^, with water vapor in an approximately stoichiometric ratio as well as a device for carrying out the method according to the invention.
Reformering av gassformige hydrokarboner så som CH^ved fremstillingen av en CO + r^-inneholdende gass skjer i henhold til kjent teknikk ved katalytisk reformering ved temperaturer under ca. 1000°C. Ved fremstillingen av reduksjonsgass ved hjelp av en såkalt ett-trinnsreformering skjer reformeringen ved et tilnærmet støkiometrisk forhold mellom H^ O og C. Denne fremgangsmåte begunstiges av høy temperatur, men temperaturen begrenses av styrken til materialet i reformerrørene. Reforming of gaseous hydrocarbons such as CH^ in the production of a CO + r^-containing gas takes place according to known technology by catalytic reforming at temperatures below approx. 1000°C. In the production of reducing gas using a so-called one-stage reforming, the reforming takes place at an approximately stoichiometric ratio between H^O and C. This method is favored by high temperature, but the temperature is limited by the strength of the material in the reformer tubes.
En ulempe ved denne kjente fremgangsmåte er at katalysator-en er meget følsom for svovel, av hvilken hydrogenkarbon-ene må renses for svovel før reformeringen. A disadvantage of this known method is that the catalyst is very sensitive to sulphur, from which the hydrogen carbons must be purified of sulfur before the reforming.
Det er i og for seg allerede kjent at reformering av hydro-genkarboner kan skje uten katalysatorer ved temperaturer over 1200- 1300°C, men verken en egnet fremgangsmåte eller anordning for gjennomførsel av denne prosess er kjent. It is already known in and of itself that reforming of hydrocarbons can take place without catalysts at temperatures above 1200-1300°C, but neither a suitable method nor device for carrying out this process is known.
Hensikten med foreliggende oppfinnelse er således å frem-bringe en fremgangsmåte og en anordning for termisk reformering av hydrogenkarbon uten anvendelse av reformerrør og katalysatorer. The purpose of the present invention is thus to produce a method and a device for the thermal reforming of hydrogen carbon without the use of reformer tubes and catalysts.
Fremgangsmåten i henhold til oppfinnelsen kjennetegnes ved at gassformig hydrogenkarbon og vanndamp, separat eller i blanding og i tilnærmet støkiometriske forhold tilføres en reformeringsreaktor, og at gassen helt eller delvis oppvarmes med plasmagenerator, slik at gassblandingens temperatur overstiger 1200°C. The method according to the invention is characterized by the fact that gaseous hydrogen carbon and water vapour, separately or in a mixture and in approximately stoichiometric conditions, are supplied to a reforming reactor, and that the gas is fully or partially heated with a plasma generator, so that the temperature of the gas mixture exceeds 1200°C.
Foruten at tilførselen av ekstern energi ved hjelp av plasmageneratoren muliggjør den termiske reformering i henhold til oppfinnelsen, oppnås herved allerede fra be-gynnelsen et lavt innhold av CC^+ H20, ^vs-under 10% In addition to the fact that the supply of external energy by means of the plasma generator enables the thermal reforming according to the invention, a low content of CC^+ H20, ^vs-less than 10% is achieved from the start
i gassen.in the gas.
I henhold til en passende utføringsform av fremgangsmåten i henhold til oppfinnelsen bringes hydrokarbonene og/eller vanndampen til helt eller delvis å passere gjennom plasmageneratoren, mens resterende gass injiseres direkte i reaktoren. According to a suitable embodiment of the method according to the invention, the hydrocarbons and/or water vapor are made to pass completely or partially through the plasma generator, while the remaining gas is injected directly into the reactor.
Plasmageneratoren kan være utformet med to ringformige elektroder eller alternativt være av typen "transferred are " . The plasma generator can be designed with two annular electrodes or alternatively be of the "transferred are" type.
I henhold til en annen egnet utføringsform av fremgangsmåten i henhold til oppfinnelsen utnyttes varmetapet i fremgangsmåten og/eller den fysiske varmen i den genererte gassblanding i det minste delvis for fremstilling av den i prosessen anvendte vanndamp. According to another suitable embodiment of the method according to the invention, the heat loss in the method and/or the physical heat in the generated gas mixture is utilized at least partially for the production of the water vapor used in the process.
I henhold til en annen egnet utføringsform av fremgangsmåten i henhold til oppfinnelsen utnyttes den fysiske varmen i den genererte gassblanding i det minste delvis for avsvovling av den fremstilte gass. Herved kan avsvovlingen gjennomføres ved injisering av en svovelakseptor, som pulverforming kalksten eller dolomit, i reaktoren, hvoretter hoveddelen av svovelet avskilles med den forbrukte kalken i fast og/eller flytende form. According to another suitable embodiment of the method according to the invention, the physical heat in the generated gas mixture is utilized at least partially for desulfurization of the produced gas. Hereby, the desulphurization can be carried out by injecting a sulfur acceptor, such as pulverized limestone or dolomite, into the reactor, after which the main part of the sulfur is separated with the spent lime in solid and/or liquid form.
I henhold til en annen egnet utføringsform av fremgangsmåten i henhold til oppfinnelsen utnyttes den fysiske varmen i den genererte gassblanding i det minste delvis for karburering av den fremstilte gassen. Dette gjennomføres fortrinnsvis ved injisering av pulverformige reaktive karbonbærere, vanligvis koks, i reaktoren hvoretter til-bakeblivende aske avskilles i fast og/eller flytende form. Restinnholdet av CO^+ f^O kan herigjennom senkes ytterligere, teoretisk helt ned til 0%. According to another suitable embodiment of the method according to the invention, the physical heat in the generated gas mixture is utilized at least partially for carburizing the produced gas. This is preferably carried out by injecting powdered reactive carbon carriers, usually coke, into the reactor, after which remaining ash is separated in solid and/or liquid form. The residual content of CO^+ f^O can thereby be further lowered, theoretically down to 0%.
Det er i og for seg også tenkbart å gjennomføre svovelrens-ing og/eller karburering i separate reaktorer gjennom hvilke den varme, fremstilte gassen etter reformeringen. It is in and of itself also conceivable to carry out sulfur cleaning and/or carburisation in separate reactors through which the hot, produced gas after the reforming.
Oppfinnelsen gjennomføres således i en tom, varmeisolert reaktor i hvilken temperaturen overstiger 1200°C og fortrinnvis når opp til ca. 1300°C. Gassblandingens trykk i reaktoren tilpasses til gassens påtenkte anvendings -formål, for anvending som reduksjonsgass hensiktsmessig oppad til ca. 2-3 bar (a) og ved anvending som syntesegass vanligvis overstigende ca. 20 bar (a). Temperaturreguler-ingen av den fremstilte gassen skjer på for formålet hensiktsmessig måte, foreksempel ved varmeveksling og/eller avkjøling. The invention is thus carried out in an empty, heat-insulated reactor in which the temperature exceeds 1200°C and preferably reaches up to approx. 1300°C. The pressure of the gas mixture in the reactor is adapted to the intended use of the gas, for use as a reducing gas, suitably up to approx. 2-3 bar (a) and when used as synthesis gas usually exceeding approx. 20 bar (a). The temperature regulation of the produced gas takes place in a manner appropriate for the purpose, for example by heat exchange and/or cooling.
Anordningen for gjennomførsel av fremgangsmåten i henhold til oppfinnelsen omfatter minst et reaksjonskammer, minst en plasmagenerator for tilførsel av ekstern energi i reaksjonskammeret, tilførselsanordninger for hydrogenkarbon og vanndamp som skal oppvarmes med plasmageneratoren, gass-uttak samt uttak for slagg og aske. The device for carrying out the method according to the invention comprises at least one reaction chamber, at least one plasma generator for supplying external energy in the reaction chamber, supply devices for hydrogen carbon and water vapor to be heated with the plasma generator, gas outlet and outlet for slag and ash.
I henhold til en foretrukket utføringsform av anordningen omfatter denne foruten dette tilførselsanordninger for reaktive karbonbærere og svovelakseptorer. According to a preferred embodiment of the device, this also includes supply devices for reactive carbon carriers and sulfur acceptors.
Plasmageneratoren kan inneholde sylindriske elektroder mellom hvilke det dannes en elektrisk lysbue. Alternativt kan plasmageneratoren være av typen "transferred are". The plasma generator can contain cylindrical electrodes between which an electric arc is formed. Alternatively, the plasma generator can be of the "transferred are" type.
I henhold til en annen hensiktsmessig utførsel av anordningen i henhold til oppfinnelsen omfatter denne en vertikal stående, sylindrisk sjakt inndelt i soner for reformering respektivt karburering, eventuelt utformet med en forsmalning mellom sonene, og utstyrt med et utløp i sjakt ens bunn for flytende slagg, et i sjaktens nedre anordnet gassutløp, forbundet med en etterfølgende avskilningsanordning med et i dens nedre del anordnet utløp for fast slagg og ufordampet materiale og et i dens øvre del anordnet gassutløp. Tilførselsanordninger for reaktive karbonbærere og svovelakseptorer er anordnet på et eller flere steder i sjakten og i tilslutning til gassutløpet av sjakten. According to another suitable embodiment of the device according to the invention, this comprises a vertical standing, cylindrical shaft divided into zones for reforming or carburizing, possibly designed with a narrowing between the zones, and equipped with an outlet in the bottom of the shaft for liquid slag, a gas outlet arranged in the lower part of the shaft, connected to a subsequent separation device with an outlet arranged in its lower part for solid slag and unvaporized material and a gas outlet arranged in its upper part. Supply devices for reactive carbon carriers and sulfur acceptors are arranged in one or more places in the shaft and in connection with the gas outlet of the shaft.
I henhold til en annen egnet utføringsform av anordningen i henhold til oppfinnelsen er plasmageneratoren eller plasma-generatorene anordnet i toppen av den vertikale sjakten. According to another suitable embodiment of the device according to the invention, the plasma generator or plasma generators are arranged at the top of the vertical shaft.
I henhold til en annen passende utføringsform av anordningen i henhold til oppfinnelsen er avskilleranordningen utformet som en syklon for å lette avskilning av faste partikler. According to another suitable embodiment of the device according to the invention, the separator device is designed as a cyclone to facilitate the separation of solid particles.
I henhold til en annen egnet utføringsform av anordningen i henhold til oppfinnelsen inneholder denne en varmeutveksler i gassutløpet fra det vertikale sjaktet og/eller fra av-skil ler anordningen . According to another suitable embodiment of the device according to the invention, this contains a heat exchanger in the gas outlet from the vertical shaft and/or from the separator device.
Ytterligere trekk, fordeler og utføringsformer av oppfinnelsen vil fremgå av den følgende detaljerte beskrivelse i tilslutning til de vedlagte tegninger på hvilken figuren viser en prinsippskisse av en anordning for gjennomføring av den termiske reformering i henhold til oppfinnelsen. Further features, advantages and embodiments of the invention will be apparent from the following detailed description in connection with the attached drawings, in which the figure shows a schematic diagram of a device for carrying out the thermal reforming according to the invention.
Anordningen omfatter en vertikal sylindrisk sjakt 1 som rommer en reformeringssone 2 og en karbureringssone 3. De to sonene vises delvis adskilt av en forsmalning 4 men står i direkte forbindelse med hverandre. I sjaktens topp er det anordnet minst en plasmagenerator 5. Hydrokarbon kan injiseres helt eller delvis direkte i sjakten gjennom ledningen 6 alternativt innføres gjennom ledningen 7 i en blandeanordning 8. I den på tegningen viste utføringsform varmeveksles vannet med den genererte gass og vanndamp kan innføres i blandeanordningen gjennom ledningen 9 alternativt helt eller delvis injiseres i reformeringssonen gjennom ledningen 10. En gassblanding kan genereres i blandeanordningen 8, hvilken helt eller delvis gjennom ledningen 11 kan bringes til å passere plasmageneratoren 5 alternativt kan en del av gassblåndingen injiseres direkte i reformeringssonen gjennom ledningen 12. The device comprises a vertical cylindrical shaft 1 which accommodates a reforming zone 2 and a carburizing zone 3. The two zones are shown partially separated by a narrowing 4 but are in direct connection with each other. At the top of the shaft, at least one plasma generator 5 is arranged. Hydrocarbon can be injected directly into the shaft in whole or in part through line 6, alternatively introduced through line 7 into a mixing device 8. In the embodiment shown in the drawing, heat is exchanged between the water and the generated gas and water vapor can be introduced into the mixing device through the line 9 is alternatively fully or partially injected into the reforming zone through the line 10. A gas mixture can be generated in the mixing device 8, which can be made to pass the plasma generator 5 in whole or in part through the line 11 alternatively part of the gas mixture can be injected directly into the reforming zone through the line 12 .
Utførelsesformen muliggjør selv at kun hydrogenkarbon respektivt vanndamp tilføres gjennom plasmageneratoren via blandeanordningen 8. The embodiment itself makes it possible for only hydrogen carbon or water vapor to be supplied through the plasma generator via the mixing device 8.
Den under fordampningssone 2 liggende karbureringssone 3 står via en gassledning 13 i forbindelse med en avskille-anordning 14, hvorved det oppnås en tilstrekkelig lang opp-holdstid for karburering av gassen til ønsket restinnhold av r^O og CO^-Avskilleanordningen utgjøres fortrinnsvis av en syklon for å lette avskilning av partikkelformede forurensninger i gassen, så som slaggdråper og ufordampet materiale. The carburizing zone 3 below the evaporation zone 2 is connected via a gas line 13 to a separation device 14, whereby a sufficiently long residence time is achieved for carburizing the gas to the desired residual content of r^O and CO^ The separation device preferably consists of a cyclone to facilitate separation of particulate contaminants in the gas, such as slag droplets and unvaporized material.
Hoveddelen av slaggen fra fordampningssonen 2 avskilles ved et slaggutløp 15 i den sylindriske, fordampningssonen rom-mende sjakt 1. I det de i gassen medførte partikler avskilles ved slaggutløpet 16 av avskilleanordningens bunn. The main part of the slag from the evaporation zone 2 is separated by a slag outlet 15 in the cylindrical chamber containing the evaporation zone 1. In it the particles entrained in the gas are separated at the slag outlet 16 by the bottom of the separation device.
Gassledningen 13 utgjør funksjonsmessig en del av karbureringssonen 3. Lanser 17, 18, 19 for tilførsel av reaktive karbonbaerere og/eller svovelakseptorer er anordnet i fordampningssonen, karbureringssone og nevnte gassledning. Eventuelt kan også slaggdannere injiseres gjennom de nevnte lanser. The gas line 13 functionally forms part of the carburization zone 3. Lances 17, 18, 19 for supplying reactive carbon carriers and/or sulfur acceptors are arranged in the evaporation zone, carburization zone and said gas line. Optionally, slag formers can also be injected through the aforementioned lances.
I gassutløpet 20 fra avskilleanordningen 14 vises på tegningen en varmeutveksler 21, hvilken utnyttes for varmeut-veksling eller avkjøling av den genererte gass. Som nevnt ovenfor kan denne varmeutveksler fortrinnsvis utnyttes for generering av vanndamp for reformeringen. Nevnte varmeut- veksling eller avkjøling av den genererte gassblanding kan alternativt eller foruten dette skje i gassledningen 13 som forbinder karbureringssonen med avskilleanordningen. In the gas outlet 20 from the separation device 14, a heat exchanger 21 is shown in the drawing, which is used for heat exchange or cooling of the generated gas. As mentioned above, this heat exchanger can preferably be used for the generation of steam for the reforming. Said heat exchange or cooling of the generated gas mixture can alternatively or in addition take place in the gas line 13 which connects the carburizing zone with the separation device.
Claims (16)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SE8501005A SE8501005L (en) | 1985-03-01 | 1985-03-01 | THERMAL REFORM OF THE GAS SHOULDER |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| NO860746L true NO860746L (en) | 1986-09-02 |
Family
ID=20359323
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO860746A NO860746L (en) | 1985-03-01 | 1986-02-28 | THERMAL REFORM OF GAS HYDROCARBON. |
Country Status (8)
| Country | Link |
|---|---|
| CN (1) | CN86101235A (en) |
| AU (1) | AU5400886A (en) |
| DE (1) | DE3606108A1 (en) |
| FR (1) | FR2578237B1 (en) |
| GB (1) | GB2172011B (en) |
| NL (1) | NL8600429A (en) |
| NO (1) | NO860746L (en) |
| SE (1) | SE8501005L (en) |
Families Citing this family (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2655330A1 (en) * | 1989-12-01 | 1991-06-07 | Shell Int Research | PREPARATION OF HYDROCARBONS CONTAINING ONE OR MORE HETERO-ATOM (S). |
| FR2724806A1 (en) * | 1994-09-16 | 1996-03-22 | Pompes Maupu Entreprise | Novel method for the non-catalytic vapour cracking of hydrocarbon(s) and halogen-organic cpds. |
| WO2001009031A1 (en) * | 1999-07-29 | 2001-02-08 | David Systems Technology, S.L. | Plasma transformer for the transformation of fossil fuels into hydrogen-rich gas |
| ES2168040B1 (en) * | 1999-07-29 | 2003-06-01 | David Systems Technology Sl | PLASMA CONVERTER OF FOSSIL FUELS IN A GAS RICH IN HYDROGEN. |
| FR2802522A1 (en) * | 1999-12-20 | 2001-06-22 | Air Liquide | Hydrogen production process from hydrocarbons comprises using a reactive element and a pressure of 1-10 bar |
| RU2191743C2 (en) * | 2000-09-26 | 2002-10-27 | Плаченов Борис Тихонович | Method of production of synthesis gas and device for realization of this method |
| FR2817444B1 (en) | 2000-11-27 | 2003-04-25 | Physiques Ecp Et Chimiques | GENERATORS AND ELECTRICAL CIRCUITS FOR SUPPLYING UNSTABLE HIGH VOLTAGE DISCHARGES |
| FR2831532B1 (en) * | 2001-10-26 | 2007-09-07 | Armines Ass Pour La Rech Et Le | METHOD AND DEVICE FOR GENERATING HYDROGEN BY CONVERTING AT HIGH TEMPERATURE WITH WATER VAPOR |
| JP3884326B2 (en) * | 2002-05-22 | 2007-02-21 | 大陽日酸株式会社 | Carburizing atmosphere gas generator and method |
| FR2899597A1 (en) * | 2006-04-05 | 2007-10-12 | Commissariat Energie Atomique | Production of fuel gas from organic/organo-halogen product in a form of liquid, gas/powder useful as energy source, comprises mixing the product with water to provide stoichiometric ratios between carbon atoms and oxygen mixtures |
| RU2320531C2 (en) * | 2006-05-04 | 2008-03-27 | Институт нефтехимического синтеза им. А.В. Топчиева РАН (ИНХС РАН) | Method of production of synthesis-gas at combustion and device for realization of this method |
| US8826834B2 (en) | 2006-07-14 | 2014-09-09 | Ceramatec, Inc. | Apparatus and method of electric arc incineration |
| US8618436B2 (en) | 2006-07-14 | 2013-12-31 | Ceramatec, Inc. | Apparatus and method of oxidation utilizing a gliding electric arc |
| EP2116105A4 (en) | 2007-02-23 | 2014-04-16 | Ceramatec Inc | Ceramic electrode for gliding electric arc |
| DE102013020375A1 (en) * | 2013-12-06 | 2015-06-11 | CCP Technology GmbH | PLASMA REACTOR FOR COLLIDING A HYDROCARBON FLUID |
| DE102015218098A1 (en) * | 2015-09-21 | 2017-03-23 | Deutsche Lufthansa Ag | Process for the thermal decomposition of hydrocarbons and corresponding device |
| DE102015014007A1 (en) * | 2015-10-30 | 2017-05-04 | CCP Technology GmbH | Apparatus and method for generating synthesis gas |
| CN111186816B (en) * | 2020-01-17 | 2022-04-01 | 西安交通大学 | Plasma carbon sequestration system and method |
Family Cites Families (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE427542C (en) * | 1925-04-05 | 1926-04-10 | Emil Edwin | Production of gas mixtures consisting of nitrogen and hydrogen |
| FR2143803B1 (en) * | 1971-06-29 | 1978-03-03 | Centre Rech Metallurgique | |
| SE371453C (en) * | 1973-03-26 | 1978-01-23 | Skf Ind Trading & Dev | KIT FOR PRODUCTION OF REDUCTION GAS |
| GB1475731A (en) * | 1973-03-26 | 1977-06-01 | Skf Ind Trading & Dev | Method of producing reduction gas |
| BE814899A (en) * | 1974-05-10 | 1974-11-12 | PROCESS FOR MANUFACTURING HOT REDUCING GAS. | |
| GB2010901B (en) * | 1977-08-19 | 1982-07-14 | Boc Ltd | Gaseous atmospheres |
| CA1147964A (en) * | 1979-05-25 | 1983-06-14 | Francis J. Ii Harvey | Process for reducing spent gas generated in the production of sponge iron |
| DE3120699A1 (en) * | 1980-05-29 | 1982-02-11 | USS Engineers and Consultants, Inc., 15230 Pittsburgh, Pa. | METHOD FOR PRODUCING A HOT, REDUCING GAS WITH LOW SULFUR CONTENT |
| SE448007B (en) * | 1983-04-21 | 1987-01-12 | Skf Steel Eng Ab | PROCEDURE AND DEVICE FOR RECOVERY OF CHEMICALS |
| IT1177075B (en) * | 1983-12-02 | 1987-08-26 | Skf Steel Eng Ab | PROCEDURE AND PLANT TO REDUCE OXIDE MATERIAL |
| AT384007B (en) * | 1984-04-02 | 1987-09-25 | Voest Alpine Ag | METHOD FOR PRODUCING SYNTHESIS GAS AND DEVICE FOR IMPLEMENTING THE METHOD |
-
1985
- 1985-03-01 SE SE8501005A patent/SE8501005L/en unknown
-
1986
- 1986-02-20 NL NL8600429A patent/NL8600429A/en not_active Application Discontinuation
- 1986-02-24 AU AU54008/86A patent/AU5400886A/en not_active Abandoned
- 1986-02-26 DE DE19863606108 patent/DE3606108A1/en not_active Withdrawn
- 1986-02-27 GB GB8604844A patent/GB2172011B/en not_active Expired
- 1986-02-28 NO NO860746A patent/NO860746L/en unknown
- 1986-02-28 FR FR868602842A patent/FR2578237B1/en not_active Expired - Fee Related
- 1986-03-01 CN CN198686101235A patent/CN86101235A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| CN86101235A (en) | 1986-10-01 |
| SE8501005D0 (en) | 1985-03-01 |
| FR2578237B1 (en) | 1990-07-13 |
| DE3606108A1 (en) | 1986-09-04 |
| GB2172011B (en) | 1989-06-14 |
| NL8600429A (en) | 1986-10-01 |
| SE8501005L (en) | 1986-09-02 |
| GB8604844D0 (en) | 1986-04-03 |
| FR2578237A1 (en) | 1986-09-05 |
| AU5400886A (en) | 1986-09-04 |
| GB2172011A (en) | 1986-09-10 |
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