NO821714L - PROGRAM FOR CATALYTIC DIVISION OF EARTH GAS. - Google Patents
PROGRAM FOR CATALYTIC DIVISION OF EARTH GAS.Info
- Publication number
- NO821714L NO821714L NO821714A NO821714A NO821714L NO 821714 L NO821714 L NO 821714L NO 821714 A NO821714 A NO 821714A NO 821714 A NO821714 A NO 821714A NO 821714 L NO821714 L NO 821714L
- Authority
- NO
- Norway
- Prior art keywords
- gas
- catalytic
- division
- program
- synthesis
- Prior art date
Links
- 230000003197 catalytic effect Effects 0.000 title claims description 6
- PWPJGUXAGUPAHP-UHFFFAOYSA-N lufenuron Chemical compound C1=C(Cl)C(OC(F)(F)C(C(F)(F)F)F)=CC(Cl)=C1NC(=O)NC(=O)C1=C(F)C=CC=C1F PWPJGUXAGUPAHP-UHFFFAOYSA-N 0.000 title 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 30
- 230000015572 biosynthetic process Effects 0.000 claims description 16
- 239000007789 gas Substances 0.000 claims description 16
- 238000003786 synthesis reaction Methods 0.000 claims description 16
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 15
- 238000000034 method Methods 0.000 claims description 7
- 239000003345 natural gas Substances 0.000 claims description 7
- 238000003776 cleavage reaction Methods 0.000 claims 2
- 230000007017 scission Effects 0.000 claims 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims 1
- 239000001301 oxygen Substances 0.000 claims 1
- 229910052760 oxygen Inorganic materials 0.000 claims 1
- 239000001257 hydrogen Substances 0.000 description 6
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- 239000000126 substance Substances 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 238000004523 catalytic cracking Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- -1 naphtha Chemical class 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000004868 gas analysis Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- 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
- C01B3/38—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 using catalysts
-
- 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
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
- C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/1516—Multisteps
- C07C29/1518—Multisteps one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis
Description
Oppfinnelsen vedrører en fremgangsmåte til katalytisk spalting av jordgass til syntesegassfremstilling for metanolsyntesen. Jordgass anvendes i dag som vesentlig råstoff for frembringelse av syntesegass. The invention relates to a method for catalytic splitting of natural gas to produce synthesis gas for methanol synthesis. Natural gas is used today as an essential raw material for the production of synthesis gas.
I henhold til den kjemiske formel for metanol CH^OH kreves for dets syntese , CO og C02. Syntesegassen har den riktige støkiometriske sammensetning når følgende betingelser er opp-fylt: According to the chemical formula for methanol CH^OH, CO and CO2 are required for its synthesis. The synthesis gas has the correct stoichiometric composition when the following conditions are met:
Teoretisk kunne C^-innholdet også være 0, dvs. da ville Mens ved hydrokarboner som nafta, foreligger ét H/C-forhold på 2, får man ved den katalytiske spalting av jordgass, overveiende med høyt CH^-innhold, en gassanalyse hvis verdi Theoretically, the C^ content could also be 0, i.e. then there would be While with hydrocarbons such as naphtha, there is an H/C ratio of 2, the catalytic cracking of natural gas, predominantly with a high CH^ content, results in a gas analysis if value
øker inntil 3, dvs. det foreligger increases up to 3, i.e. it exists
for meget F^O for metanolsyntesen. Dette upassende forhold lar seg bl.a. unngå ved at fra metanolsyntesens kretsløp avspennes fra tid til annen en vesentlig del av kretsløps-gassen. Bare således kan den etterhvert t^-anrikning av kretsløpsgassen imøtegås. Avspenningsgassen fra metanolsyntesens kretsløp anvendes som varmgass for den katalytiske spalting i dampomformingsovner slik det omtales i CA-patent nr. 786.393 resp. i Chemical Economy and Engineering Review, september 1971, bind 3, nr. 9 (nr. 41), side 30, fig. 2. Denne type opprettholdelse av driften av metanolsyntesen too much F^O for the methanol synthesis. This inappropriate relationship allows, among other things, avoid that from time to time a significant part of the circuit gas is released from the methanol synthesis circuit. Only in this way can the eventual t^-enrichment of the circuit gas be countered. The stripping gas from the methanol synthesis circuit is used as hot gas for the catalytic cracking in steam conversion furnaces as described in CA patent no. 786,393 resp. in Chemical Economy and Engineering Review, September 1971, Volume 3, No. 9 (No. 41), Page 30, Fig. 2. This type of maintenance of the operation of the methanol synthesis
har riktignok fordel med enkelthet av gassfrembringelses-anlegg, imidlertid den ulempe at det frembringes for meget hydrogen som dertil dessuten må føres gjennom det samlede has the advantage of the simplicity of the gas production plant, however, the disadvantage is that too much hydrogen is produced, which also has to be passed through the overall
anlegg for etterpå å avspennes omtren.totil atmosfæretrykk for at den deretter kan forbrennes som varmgass i omformerovnen. plant to be subsequently de-stressed to approximately two atmospheric pressures so that it can then be burned as hot gas in the converter furnace.
Etter en ytterligere kjent fremgangsmåte ifølge Chemical Economy and Engineering Review, september 1971, bind 3, nr. 9, (nr. 41), side 21, oppnås den optimale innstilling av H/C-forholdet for metanolsyntesen ved en parallellkoblet CO-konvertering. Derved konverteres en del av den ved entrinnede katalytiske spalting fremstilte H2~rike og CO-holdige rågass i et CO-generatortrinn med CO-konvertering til C02og H2. Following a further known method according to Chemical Economy and Engineering Review, September 1971, Volume 3, No. 9, (No. 41), page 21, the optimum setting of the H/C ratio for the methanol synthesis is achieved by a parallel connected CO conversion. Thereby, part of the H2-rich and CO-containing raw gas produced by one-stage catalytic cracking is converted in a CO generator stage with CO conversion to C02 and H2.
I et etterfølgende C02~absorpsjonstrinn adskilles H2fraIn a subsequent C02~absorption step, H2 is separated from
C02, H2kan anvendes på annen måte, hvorimot C02føres til innstilling av det optimale H/C-forholdet i hovedgass-strømmen. C02, H2 can be used in another way, whereas C02 is used to set the optimum H/C ratio in the main gas stream.
Ved de kjente fremgangsmåter frembringes ved den katalytiske spalting for meget hydrogen, dvs. ballasthydrogen. Den med denne ballasthydrogen økede anleggsdimensjonering fører dessuten ved store anlegg til grenser av den tekniske reali-serbarhet av anleggsdeler. JordgassTog energianvendelse pr. enhet metanol er unødvendig overtrukket. In the known methods, too much hydrogen, i.e. ballast hydrogen, is produced by the catalytic splitting. The increased plant dimensioning with this ballast hydrogen also leads to limits of the technical feasibility of plant parts in the case of large plants. Natural gas Train energy use per unit methanol is unnecessarily overlaid.
En ytterligere mulighet til å forbedre det ugunstige H2/CO-forhold ved den katalytiske spalting av CH4, består i direkte tilsetning av C02i syntesegass-strømmen. Således er det fra Petroleum&Petrochemical, august 1973, bind 13, nr. 8, side 74, fig, 2, kjent til røkgassen fra spaltanlegget ved hjelp av en kjemisk vasking å fjerne C02og komprimere denne og å tilsette til syntesegassen. C02~utvinningen fra den trykkløse røkgass er energimessig og investeringsmessig omstendelig . A further possibility to improve the unfavorable H2/CO ratio in the catalytic splitting of CH4 consists in the direct addition of the CO2i synthesis gas stream. Thus, from Petroleum&Petrochemical, August 1973, volume 13, no. 8, page 74, fig, 2, it is known to the flue gas from the cracking plant by means of a chemical washing to remove C02 and compress this and to add to the synthesis gas. C02 recovery from the depressurized flue gas is expensive in terms of energy and investment.
Til grunn for oppfinnelsen ligger den oppgave å fjerne ulemper ved de kjente fremgangsmåter. The invention is based on the task of removing disadvantages of the known methods.
Denne oppgave løses ifølge oppfinnelsen ved en fremgangsmåte av den innledningsvis omtalte type ved kombinasjonen av de According to the invention, this task is solved by a method of the type mentioned at the outset by the combination of the
karakteriserende trekk.characterizing features.
Den ved fremgangsmåten ifølge oppfinnelsen oppnådde tekniske fordel består i at allerede i det katalytiske spaltingsanlegg innstilles det optimale H/C-forhold for metanolsyntesen. Såkalt ballasthydrogen fremkommer ikke. Derved nødvendig-gjøres heller ingen overproporsjonal energi for kompresjon av dette ballasthydrogen, og forbruk av jordgass reduseres vesentlig. The technical advantage achieved by the method according to the invention consists in the fact that the optimum H/C ratio for the methanol synthesis is already set in the catalytic splitting plant. So-called ballast hydrogen does not appear. Thereby, no over-proportional energy is required for compression of this ballast hydrogen, and consumption of natural gas is significantly reduced.
Videre dimensjoneres alle anleggsdeler med hensyn til volum bare for den faktisk nødvendige gassproduksjon. Furthermore, all plant parts are dimensioned with respect to volume only for the actually required gas production.
Et talleksempel ifølge oppfinnelsen gjengir dataene som følger: A numerical example according to the invention reproduces the data as follows:
For den tørre syntesegass beregnes en analyse: An analysis is calculated for the dry synthesis gas:
Dermed fremkommer et forhold: This results in a relationship:
Den således oppnådde verdi er en beregnet verdi som ved nærvær av mindre avvikende driftsverdier for råstoff, trykk og tempe-ratur lar seg redusere til 2,0. The value thus obtained is a calculated value which, in the presence of less deviant operating values for raw material, pressure and temperature, can be reduced to 2.0.
Det kan bortsees ifølge oppfinnelsen fra de omstendelig kjente forholdsregler til innstilling av den nødvendige r^/CO-forhold. According to the invention, the generally known precautions for setting the required r^/CO ratio can be dispensed with.
Claims (1)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19813122273 DE3122273A1 (en) | 1981-06-04 | 1981-06-04 | "METHOD FOR CATALYTIC FUELING OF NATURAL GAS" |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| NO821714L true NO821714L (en) | 1982-12-06 |
Family
ID=6133946
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO821714A NO821714L (en) | 1981-06-04 | 1982-05-24 | PROGRAM FOR CATALYTIC DIVISION OF EARTH GAS. |
Country Status (7)
| Country | Link |
|---|---|
| JP (1) | JPS582203A (en) |
| DE (1) | DE3122273A1 (en) |
| DK (1) | DK251182A (en) |
| FR (1) | FR2507169B1 (en) |
| GB (1) | GB2099846B (en) |
| IT (1) | IT1198371B (en) |
| NO (1) | NO821714L (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2557555B1 (en) * | 1983-12-30 | 1987-05-15 | Inst Francais Du Petrole | NOVEL PROCESS FOR THE MANUFACTURE OF SYNTHETIC GAS FOR USE IN PARTICULAR FOR THE PRODUCTION OF METHANOL |
| FR2790750B1 (en) | 1999-03-10 | 2001-04-20 | Air Liquide | PROCESS AND DEVICE FOR PRODUCING HYDROGEN BY THERMOCATALYTIC DECOMPOSITION OF HYDROCARBONS |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB616710A (en) * | 1946-04-18 | 1949-01-26 | Standard Oil Dev Co | Improvements in or relating to the froduction of hydrogen containing gases |
| DE1667631C3 (en) * | 1968-01-15 | 1978-09-07 | Metallgesellschaft Ag, 6000 Frankfurt | Process for the production of methanol synthesis gas |
| US4271068A (en) * | 1968-05-10 | 1981-06-02 | Ciba-Geigy Corporation | Process for the manufacture of cystine-containing peptides |
| DE2148430C2 (en) * | 1970-10-01 | 1984-03-29 | The Lummus Co., 07003 Bloomfield, N.J. | Process for reforming hydrocarbon feedstocks for the production of carbon monoxide and hydrogen |
| GB1484366A (en) * | 1974-07-02 | 1977-09-01 | Ici Ltd | Methanol |
| FR2372116A1 (en) * | 1977-03-22 | 1978-06-23 | Banquy David | SYNTHESIS GAS PRODUCTION PROCESS |
| BE865319A (en) * | 1978-03-24 | 1978-09-25 | Texaco Development Corp | PROCESS FOR PRODUCING A CLEANED AND PURIFIED SYNTHESIS GAS AND A CO-RICH GAS |
| FR2420568A1 (en) * | 1978-03-24 | 1979-10-19 | Texaco Development Corp | Synthesis gas and carbon mon:oxide prodn. - and methanol synthesis process |
-
1981
- 1981-06-04 DE DE19813122273 patent/DE3122273A1/en not_active Withdrawn
-
1982
- 1982-05-14 IT IT21293/82A patent/IT1198371B/en active
- 1982-05-24 NO NO821714A patent/NO821714L/en unknown
- 1982-06-03 JP JP57094156A patent/JPS582203A/en active Pending
- 1982-06-03 GB GB8216177A patent/GB2099846B/en not_active Expired
- 1982-06-03 DK DK251182A patent/DK251182A/en not_active Application Discontinuation
- 1982-06-04 FR FR8209739A patent/FR2507169B1/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| FR2507169A1 (en) | 1982-12-10 |
| IT1198371B (en) | 1988-12-21 |
| GB2099846B (en) | 1984-08-15 |
| IT8221293A0 (en) | 1982-05-14 |
| JPS582203A (en) | 1983-01-07 |
| DK251182A (en) | 1982-12-05 |
| GB2099846A (en) | 1982-12-15 |
| DE3122273A1 (en) | 1982-12-23 |
| FR2507169B1 (en) | 1987-03-06 |
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