PL138697B1 - Method of obtaining methyloacohol and other higher alcohols - Google Patents
Method of obtaining methyloacohol and other higher alcohols Download PDFInfo
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- PL138697B1 PL138697B1 PL1982248949A PL24894982A PL138697B1 PL 138697 B1 PL138697 B1 PL 138697B1 PL 1982248949 A PL1982248949 A PL 1982248949A PL 24894982 A PL24894982 A PL 24894982A PL 138697 B1 PL138697 B1 PL 138697B1
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- Prior art keywords
- catalyst
- higher alcohols
- reaction zone
- kpa
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- 238000000034 method Methods 0.000 title claims description 14
- 150000001298 alcohols Chemical class 0.000 title claims description 12
- 239000003054 catalyst Substances 0.000 claims description 29
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 27
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 10
- 229910052783 alkali metal Inorganic materials 0.000 claims description 7
- 150000001340 alkali metals Chemical class 0.000 claims description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims description 6
- 239000001257 hydrogen Substances 0.000 claims description 6
- 239000002184 metal Substances 0.000 claims description 6
- 150000002739 metals Chemical class 0.000 claims description 6
- 239000001569 carbon dioxide Substances 0.000 claims description 5
- 239000011261 inert gas Substances 0.000 claims description 5
- 229910052751 metal Inorganic materials 0.000 claims description 5
- 229910052684 Cerium Inorganic materials 0.000 claims description 3
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 3
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 3
- 229910052782 aluminium Inorganic materials 0.000 claims description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 3
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 claims description 3
- 229910052746 lanthanum Inorganic materials 0.000 claims description 3
- FZLIPJUXYLNCLC-UHFFFAOYSA-N lanthanum atom Chemical compound [La] FZLIPJUXYLNCLC-UHFFFAOYSA-N 0.000 claims description 3
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 claims description 3
- 229910052750 molybdenum Inorganic materials 0.000 claims description 3
- 239000011733 molybdenum Substances 0.000 claims description 3
- 229910052719 titanium Inorganic materials 0.000 claims description 3
- 239000010936 titanium Substances 0.000 claims description 3
- 229910052720 vanadium Inorganic materials 0.000 claims description 3
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 claims description 3
- 239000010949 copper Substances 0.000 description 5
- 229910052802 copper Inorganic materials 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 3
- 239000011701 zinc Substances 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 239000011651 chromium Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000008246 gaseous mixture Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 229910052725 zinc Inorganic materials 0.000 description 2
- LRHPLDYGYMQRHN-UHFFFAOYSA-N Butanol Natural products CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 1
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- -1 Methanol Ethanol n-propanol i-butanol Chemical compound 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- 229910000272 alkali metal oxide Inorganic materials 0.000 description 1
- 229910000287 alkaline earth metal oxide Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- JJLJMEJHUUYSSY-UHFFFAOYSA-L copper(II) hydroxide Inorganic materials [OH-].[OH-].[Cu+2] JJLJMEJHUUYSSY-UHFFFAOYSA-L 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- LYAOUQAGWKWFOX-UHFFFAOYSA-N ethanol;methanol;propan-1-ol Chemical compound OC.CCO.CCCO LYAOUQAGWKWFOX-UHFFFAOYSA-N 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000011572 manganese Substances 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 238000001465 metallisation Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- CHWRSCGUEQEHOH-UHFFFAOYSA-N potassium oxide Chemical compound [O-2].[K+].[K+] CHWRSCGUEQEHOH-UHFFFAOYSA-N 0.000 description 1
- 229910001950 potassium oxide Inorganic materials 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 229910052709 silver Inorganic materials 0.000 description 1
- 239000010944 silver (metal) Substances 0.000 description 1
- 229910052727 yttrium Inorganic materials 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
- C07C31/02—Monohydroxylic acyclic alcohols
-
- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
- B01J23/88—Molybdenum
- B01J23/885—Molybdenum and copper
-
- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
- B01J23/86—Chromium
- B01J23/868—Chromium copper and chromium
-
- 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
- C07C29/153—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 characterised by the catalyst used
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Description
Przedmiotem wynalazku jest sposób wytwarzania metanolu i wyzszych alkoholi z wodoru i tlenku wegla, ewentualnie w obecnosci dwutlenku wegla i innych obojetnych gazów, droga reakcji prowadzonej na katalizatorze* Mieszaniny metanolu i wyzszych alkoholi sa stosowane jako produkt zastepczy benzyny i moga byc równiez mieszane w róznych stosunkach i stosowane jako paliwo w silnikach spalinowych. Znane sa liczne katalizatory proceau wytwarzania meta¬ nolu i wyzszych alkoholi z mieszanin wodoru z tlenkiem wegla• Na przyklad, z publikacji Br;Linet'a "Catalysis" tom 5, znany jest katalizator zawierajacy Cu, ZnO i Cr205 w stosunku molowym 82%, 16# i 2%p przy czym do tych skladników nalezy dodawac tlenek potasowy, w celu uzyskania katalizatora o koniecznej selektywnej aktywnosci* Inny katalizator opisany w po¬ wyzszej publikacji wytwarza sie z Zn(0H)2, Cu(0H)2 i K,(Cr/C0^/J.3H20 w równomolowej mie¬ szaninie.Z kanadyjskiego opisu patentowego nr 273 984 znany jest katalizator zlozony z jednego lub z wiekszej liczby tlenków metali, takich jak Ag, Cu, Zn, Mn, Mo, U i V oraz z jednego lub wiekszej liczby tlenków metali alkalicznych lub tlenków metali ziem alkalicznych, przy czym liczba atomów metali alkalicznych w tlenkach powinna byc równa polowie liczby atomów wszystkich innych metali.Znane katalizatory nie dzialaja jednak selektywnie i nie umozliwiaja wytwarzania meta¬ nolu i wyzszych alkoholi z wysoka wydajnoscia* Poza tym wiadomo, ze katalizatory zawieraja¬ ce miedz nie moga byc z powodu zjawiska metalizacji stosowane w temperaturach wyzszych od okolo.300°C.Nieoczekiwanie stwierdzono, ze proces wytwarzania metanolu i wyzszych alkoholi z wodo¬ ru i tlenku wegla, ewentualnie w obecnosci dwutlenku wegla i innych obojetnych gazów, moze byc korzystnie prowadzony w temperaturze wyzszej niz 300°C, w obecnosci katalizatora zawiera¬ jacego miedz", jezeli stosuje sie katalizator o odpowiednim skladzie i proces prowadzi sie w odpowiednio dobranych warunkach cisnienia, temperatury i przy odpowiedniej predkosci przeply¬ wu reagujacych gazów. \2 138 697 y procesie prowadzonym sposobem wedlug wynalazku stosuje sie katalizator skladajacy sie z nastepujacych pierwiastków: cynku, chromu, miedzi, jednego lub wiekszej liczby metali alka¬ licznych, korzystnie potasu i ewentualnie jednego lub wiekszej liczby metali wybranych spos¬ ród molibdenu, manganu, lantanu, ceru, glinu, tytanu i wanadu, przy czym wszystkie te pier¬ wiastki lub tylko ich czesc, sa chemicznie zwiazane z tlenem i/albo miedzy soba* Katalizator ten ma empiryczny wzór ogólny 2nCr CaxkyKez0^9 w którym A oznacza metal alkaliczny lub meta¬ le alkaliczne, Me oznacza jeden lub wieksza liczbe wspomnianych wyzej innych metali, ewentual¬ nie obecnych w katalizatorze, w oznacza liczbe 0,1-0,8, korzystnie 0,3-0,6, x oznacza liczbe 0,005-0,05, korzystnie 0,01-0,03, y oznacza liczbe 0,002-0,2, korzystnie 0,01-0,1, z oznacza liczbe 0,0-0,1, korzystnie 0,0-0,04 oraz t oznacza liczbe 3,75-1,3, przy czym ta ostatnia war¬ tosc powinna byc dostosowana do wartosciowosci róznych pierwiastków wystepujacych w kataliza¬ torze • Cecha sposobu wedlug wynalazku jest to, ze do strefy reakcji zawierajacej katalizator o o wyzej podanym wzorze ogólnym wprowadza sie wodór i tlenek wegla, ewentualnie z dwutlenkiem wegla i innymi gazami obojetnymi, w molowym stosunku H2:C0 wynoszacym 0,2-10,. korzystnie 0,5-3 i w strefie reakcji utrzymuje sie temperature 330-460°C, korzystnie 360-440°C, cisnienie 2000-30000 KPa, korzystnie 6000-18000 kPa i mieszanine gazowa prowadzi sie z predkoscia obje¬ tosciowa 5000-30000 g/godzine, korzystnie 5000-15000 g/godzine. Jako gazowa mieszanine mozna • stosowac gaz syntezowy, np. pochodzacy z czesciowego spalania wegla, gazu naturalnego albo weglowodorów* Proces prowadzi sie przez powodowanie stykania sie gazowej mieszaniny z katalizatorem w odpowiednim reaktorze, ze zlozem fluidalnym lub nieruchomym* Z mieszaniny odplywajacej z re¬ aktora ciekly produkt reakcji i oddziela sie znanymi sposobami, stosujac chlodzenie i konden¬ sacje. Przyklady I-VII.Proces wedlug wynalazku prowadzono stosujac gaz syntezowy o nastepujacym skladzie objeto¬ sciowym: Hg 66-6996, CO 30-33^, C02 0-3#, CH^ 0,1#, NT2 0,396. W kolejnych próbach prowadzonych w reaktorze rurowym stosowano katalizatory o nastepujacym skladzie: przyklad I: ZnCro,35Cu0,027K0,O2 przyklad II: ZnCr0,33Cu0,018K0,023 przyklad III: ZnCr0,33Cu0,18 ^,06 przyklad IV: ZnCr0,35Cu0,027K0,23J'In0,04 przyklad V: ZnCr0,35Cu0,027K0,023A10,082 przyklad VI: ZnCrO,4CuO,028K0,023 przyklad VII: ZnCr0,45Cu0,029K0,02 Procesy wytwarzania metanolu i wyzszych alkoholi prowadzono przy uzyciu kazdego z wy^ej podanych katalizatorów, stosujac warunki reakcji i podane w tabeli. Ciekly produkt reakcji oddzielano przez chlodzenie i skraplanie i produkty zbierane w ciagu 24 godzin trwania procesu analizowano metoda chromatografii gazowej. Wyniki podane w tabeli swiadcza o korzystnym prze¬ biegu tych procesów.Tabela I Katalizator, jak w przykladzie I I Cisnienie Temperatura I Predkosc I objetosciowa I Metanol I Etanol I n-propanol i-butanol , wyzsze alkohole |_(C_ 5) | I kPa °C g/godzine % wagowe % wagowe % wagowe % wagowe % wagowe j I 9000 398-404 10650 57,7 1,9 1,5 18,1 ] 21,5 13000 397-404 11400 61,5 1,6 1,7 15,8 19,3 I 16000 I 397-404 10340 I 68,2 V 1,4 13,6 | 15,5 j 13000 398-403 15030 66,2 1,4 1,6 15 \ 15,5 | 13000 398-404 6870 54 1,8 1,8 19,5 22,5 | I 13000 I 416-421 10650 I 53,2 2,3 1,8 21,6 I 21 I138697 3 Tabela Cid# Katalizator Cisnienie Temperatura Predkosc objeto- I sciowa Metanol Etanol n-propanol i-butanol wyzsze alkohole I (C 5) kPa °C g/godzine % wagowe % wagowe % wagowe % Y/agowe % wagowe jak w przykla¬ dzie II 13 000 392-405 ¦9 560 71,4 1,8 1,5 9,7 15,6 ' jak w przy¬ kladzie III 13 000 ,- 398-400 10 200 78,6 1,4 1,9 8,7 7,8 jak w przy- ! kladzie IV 13 O00 I • 397-402 I 11 170 67,6 j 2,1 3,7 14,3 I 11,3 Tabela c#d# Katalizator Cisnienie I Temperatura I Predkosc objeto- I sciowa Metanol Etanol n-propanol i-butanol j wyzsze alkohole i [_(C 5) i kPa °C g/godzine % wagowe % wagowe % wagowe % wagowe % wagowe j i jak w przy¬ kladzie V 13 000 399-403 11 400 79,2 1,3 1,9 8,7 3,8 jak w przy- | kladzie VI 13 000 398-401 11 800 69,6 1»8 2,3 | 14,9 11,4 i jak w przy¬ kladzie Vii 13 000 396-400 I 10 200 57,3 1,9 2,3 16,6 21,4 I Zastrzezenia patentowe 1# Sposób wytwarzania metanolu i wyzszych alkoholi, polegajacy na wprov;adzaniu do strefy reakcji, zawierajacej katalizator, mieszaniny wodoru i tlenku wegla, ewentualnie w obecnosci dwutlenku wegla i innych gazów obojetnych, przy stosunku molowym HptCO wynoszacym 0,2-10, ko¬ rzystnie 0,5-3, w temperaturze 330-460°C, korzystnie 360-440°C, znamienny tym, ze stosuje sie katalizator o empirycznym wzorze ogólnym ZnCrwCUxAvMe 0. , w którym A oznacza metal alkaliczny lub metale alkaliczne, Me oznacza jeden lub wieksza liczbe metali wybranych sposród molibdenu, manganu, lantanu, ceru, glinu, tytanu i wanadu, ewentualnie obecnych w ka¬ talizatorze, w oznacza liczbe 0,1-0,8, x oznacza liczbe 0,005-0,05, y oznacza liczbe 0,002-0,2, z oznacza liczbe 0,0-0,1 i t oznacza liczbe 3,75-1,3, przy czyni ta ostatnia wartosc jest do¬ stosowana do wartosciowosci pierwiastków wystepujacych w katalizatorze i w strefie reakcji utrzymuje sie cisnienie 2000-30000 kPa i predkosc objetosciowa 5000-30000 g/godzine.k 133 697 2. Sposób wedlug zastrz. 1, znamienny tym, ze w strefie reakcji utrzymuje sie cisnienie 6000-18000 kPa i predkosc objetosciowa 5000-15000 g/godzine.Pracownia Poligraficzna UP PRL. Naklad 100 egz.Cena 130 zl PL PL PL PL PL PL PL PL
Claims (1)
1. Zastrzezenia patentowe 1. # Sposób wytwarzania metanolu i wyzszych alkoholi, polegajacy na wprov;adzaniu do strefy reakcji, zawierajacej katalizator, mieszaniny wodoru i tlenku wegla, ewentualnie w obecnosci dwutlenku wegla i innych gazów obojetnych, przy stosunku molowym HptCO wynoszacym 0,2-10, ko¬ rzystnie 0,5-3, w temperaturze 330-460°C, korzystnie 360-440°C, znamienny tym, ze stosuje sie katalizator o empirycznym wzorze ogólnym ZnCrwCUxAvMe 0. , w którym A oznacza metal alkaliczny lub metale alkaliczne, Me oznacza jeden lub wieksza liczbe metali wybranych sposród molibdenu, manganu, lantanu, ceru, glinu, tytanu i wanadu, ewentualnie obecnych w ka¬ talizatorze, w oznacza liczbe 0,1-0,8, x oznacza liczbe 0,005-0,05, y oznacza liczbe 0,002-0,2, z oznacza liczbe 0,0-0,1 i t oznacza liczbe 3,75-1,3, przy czyni ta ostatnia wartosc jest do¬ stosowana do wartosciowosci pierwiastków wystepujacych w katalizatorze i w strefie reakcji utrzymuje sie cisnienie 2000-30000 kPa i predkosc objetosciowa 5000-30000 g/godzine.k 133 6972. Sposób wedlug zastrz. 1, znamienny tym, ze w strefie reakcji utrzymuje sie cisnienie 6000-18000 kPa i predkosc objetosciowa 5000-15000 g/godzine. Pracownia Poligraficzna UP PRL. Naklad 100 egz. Cena 130 zl PL PL PL PL PL PL PL PL
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| IT25390/81A IT1169281B (it) | 1981-12-02 | 1981-12-02 | Sistema catalitico e procedimento per la produzione di miscele di metanolo ed alcoli superiori |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| PL138697B1 true PL138697B1 (en) | 1986-10-31 |
Family
ID=11216562
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PL1982248949A PL138697B1 (en) | 1981-12-02 | 1982-12-01 | Method of obtaining methyloacohol and other higher alcohols |
| PL1982239300A PL137518B1 (en) | 1981-12-02 | 1982-12-01 | Catalyst for use in a process of obtaining methanol and higher alcohols |
Family Applications After (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PL1982239300A PL137518B1 (en) | 1981-12-02 | 1982-12-01 | Catalyst for use in a process of obtaining methanol and higher alcohols |
Country Status (32)
| Country | Link |
|---|---|
| US (2) | US4513100A (pl) |
| JP (1) | JPS58104635A (pl) |
| KR (2) | KR860002159B1 (pl) |
| AU (1) | AU550713B2 (pl) |
| BE (1) | BE895208A (pl) |
| BR (1) | BR8206776A (pl) |
| CA (1) | CA1194013A (pl) |
| CH (1) | CH650946A5 (pl) |
| CS (1) | CS236697B2 (pl) |
| CU (1) | CU21442A3 (pl) |
| DD (1) | DD205680A5 (pl) |
| DE (1) | DE3244313C2 (pl) |
| DK (1) | DK531782A (pl) |
| EG (1) | EG16016A (pl) |
| ES (1) | ES517749A0 (pl) |
| FI (1) | FI71883C (pl) |
| FR (1) | FR2517296A1 (pl) |
| GB (1) | GB2110558B (pl) |
| GR (1) | GR77106B (pl) |
| IE (1) | IE53599B1 (pl) |
| IN (1) | IN157897B (pl) |
| IT (1) | IT1169281B (pl) |
| LU (1) | LU84494A1 (pl) |
| NO (1) | NO158722C (pl) |
| NZ (1) | NZ202305A (pl) |
| PH (1) | PH17792A (pl) |
| PL (2) | PL138697B1 (pl) |
| RO (1) | RO86064B (pl) |
| SE (1) | SE451545B (pl) |
| SU (1) | SU1279516A3 (pl) |
| YU (1) | YU259682A (pl) |
| ZA (1) | ZA827980B (pl) |
Families Citing this family (27)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU565013B2 (en) * | 1982-11-29 | 1987-09-03 | Research Association For Petroleum Alternatives Development | Production of mixed alcohols |
| US4843101A (en) * | 1983-06-01 | 1989-06-27 | Lehigh University | Catalyst and method for producing methanol |
| DE3403491A1 (de) * | 1984-02-02 | 1985-08-14 | Süd-Chemie AG, 8000 München | Katalysator zur synthese von methanol und hoehere alkohole enthaltenden alkoholgemischen |
| US4882360A (en) * | 1984-07-30 | 1989-11-21 | The Dow Chemical Company | Process for producing alcohols from synthesis gas |
| US4752622A (en) * | 1984-07-30 | 1988-06-21 | The Dow Chemical Company | Process for producing alcohols from synthesis gas |
| US4831060A (en) * | 1984-07-30 | 1989-05-16 | The Dow Chemical Company | Mixed alcohols production from syngas |
| US4762858A (en) * | 1985-09-16 | 1988-08-09 | The Dow Chemical Company | Syngas conversion to oxygenates by reduced yttrium/lanthanide/actinide-modified catalyst |
| US4943551A (en) * | 1985-11-08 | 1990-07-24 | Union Carbide Chemicals And Plastics Company, Inc. | Catalyst for synthesis of mixtures of methanol and higher alcohols |
| US4681868A (en) * | 1986-05-29 | 1987-07-21 | The Standard Oil Company | Oxygenate condensation catalyst |
| US4789502A (en) * | 1986-11-24 | 1988-12-06 | Shell Oil Company | Carboxylic acid production |
| US4886651A (en) * | 1988-05-18 | 1989-12-12 | Air Products And Chemicals, Inc. | Process for co-production of higher alcohols, methanol and ammonia |
| US5155086A (en) * | 1989-09-12 | 1992-10-13 | Engelhard Corporation | Hydrogenation catalyst, process for preparing and process of using said catalyst |
| US5345005A (en) * | 1989-09-12 | 1994-09-06 | Engelhard Corporation | Hydrogenation catalyst, process for preparing and process of using said catalyst |
| US5070058A (en) * | 1990-01-22 | 1991-12-03 | Texaco, Inc. | Method for making a catalyst composition used in the production of lower aliphatic alcohols |
| US5134108A (en) * | 1991-05-22 | 1992-07-28 | Engelhard Corporation | Process for preparing catalyst with copper or zinc and with chromium, molybdenum, tungsten, or vanadium, and product thereof |
| US5410015A (en) * | 1991-06-22 | 1995-04-25 | Basf Aktiengesellschaft | Polyamides having a low water absorptivity |
| US5300695A (en) * | 1992-12-07 | 1994-04-05 | Amoco Corporation | Process for preparing alcohols |
| IT1276931B1 (it) * | 1995-10-13 | 1997-11-03 | Snam Progetti | Procedimento per produrre miscele di metanolo ed alcoli superiori |
| KR20030085284A (ko) * | 2002-04-30 | 2003-11-05 | 고양복합영농조합법인 | 열무를 절단 포장하는 제조방법 및 그 포장 열무 |
| TW200519073A (en) * | 2003-08-21 | 2005-06-16 | Pearson Technologies Inc | Process and apparatus for the production of useful products from carbonaceous feedstock |
| US8394863B2 (en) | 2003-08-21 | 2013-03-12 | Pearson Technologies, Inc. | Process and apparatus for the production of useful products from carbonaceous feedstock |
| JP5592250B2 (ja) * | 2007-04-27 | 2014-09-17 | サウディ ベーシック インダストリーズ コーポレイション | 二酸化炭素の合成ガスへの接触水素化 |
| US20090156697A1 (en) * | 2007-12-14 | 2009-06-18 | Range Fuels, Inc. | Catalyst compositions and methods for alcohol production from synthesis gas |
| MX2013004318A (es) | 2010-11-08 | 2013-06-03 | Topsoe Haldor As | Proceso para la preparacion selectiva de 1-propanol, iso-butanol y otros alcoholes c3+ a partir de gas de sintesis y metanol. |
| US10875820B2 (en) | 2013-06-20 | 2020-12-29 | Standard Alcohol Company Of America, Inc. | Catalyst for converting syngas to mixed alcohols |
| US9290425B2 (en) | 2013-06-20 | 2016-03-22 | Standard Alcohol Company Of America, Inc. | Production of mixed alcohols from synthesis gas |
| EP4112169A1 (en) | 2021-07-03 | 2023-01-04 | Studiengesellschaft Kohle mbH | Process for converting synthesis gas to higher alcohols |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE553785C (de) * | 1923-05-23 | 1932-07-01 | I G Farbenindustrie Akt Ges | Verfahren zur Herstellung von oeligen Produkten |
| US2960518A (en) * | 1957-09-27 | 1960-11-15 | Peters Kurt | Ethylene production process |
| US3326956A (en) * | 1962-06-08 | 1967-06-20 | Ici Ltd | Production of oxygenated hydrocarbons |
| FR1390776A (fr) * | 1963-04-23 | 1965-02-26 | British Petroleum Co | Procédé de production d'un gaz contenant de l'hydrogène et gaz obtenu |
| JPS4937708B1 (pl) * | 1970-12-31 | 1974-10-11 | ||
| FR2369234A1 (fr) * | 1976-10-29 | 1978-05-26 | Inst Francais Du Petrole | Procede de fabrication d'alc |
| US4107089A (en) * | 1977-03-14 | 1978-08-15 | Petr Grigorievich Bondar | Catalyst for the synthesis of methanol and method for preparing same |
| DE2738269C3 (de) * | 1977-08-25 | 1980-02-21 | Chemische Werke Huels Ag, 4370 Marl | Verfahren zur Herstellung von Aceton aus Isobutyraldehyd |
| FR2444654A1 (fr) * | 1978-12-19 | 1980-07-18 | Inst Francais Du Petrole | Procede de fabrication d'alcools et plus particulierement d'alcools primaires, satures et lineaires, a partir de gaz de synthese |
| DE3005550A1 (de) * | 1980-02-14 | 1981-08-20 | Süd-Chemie AG, 8000 München | Verfahren zur herstellung von olefinen |
| IT1140947B (it) * | 1980-05-16 | 1986-10-10 | Snam Progetti | Processo per la produzione di una miscela di metanolo ed alcoli superiori "grado carburante" |
| IT1148864B (it) * | 1980-05-16 | 1986-12-03 | Snam Progetti | Processo pe la produzione di una miscela di metanolo ed alcoli superiori grado carburante |
-
1981
- 1981-12-02 IT IT25390/81A patent/IT1169281B/it active
-
1982
- 1982-10-28 US US06/437,439 patent/US4513100A/en not_active Expired - Lifetime
- 1982-10-28 NZ NZ202305A patent/NZ202305A/en unknown
- 1982-10-29 NO NO823601A patent/NO158722C/no unknown
- 1982-11-01 CA CA000414582A patent/CA1194013A/en not_active Expired
- 1982-11-01 ZA ZA827980A patent/ZA827980B/xx unknown
- 1982-11-03 SE SE8206257A patent/SE451545B/sv not_active IP Right Cessation
- 1982-11-04 AU AU90168/82A patent/AU550713B2/en not_active Ceased
- 1982-11-05 PH PH28093A patent/PH17792A/en unknown
- 1982-11-05 GB GB08231640A patent/GB2110558B/en not_active Expired
- 1982-11-09 GR GR69769A patent/GR77106B/el unknown
- 1982-11-09 KR KR8205053A patent/KR860002159B1/ko active
- 1982-11-19 ES ES517749A patent/ES517749A0/es active Granted
- 1982-11-22 YU YU02596/82A patent/YU259682A/xx unknown
- 1982-11-22 BR BR8206776A patent/BR8206776A/pt unknown
- 1982-11-25 CS CS828464A patent/CS236697B2/cs unknown
- 1982-11-26 FR FR8219935A patent/FR2517296A1/fr active Granted
- 1982-11-26 SU SU3516802A patent/SU1279516A3/ru active
- 1982-11-29 DD DD82245316A patent/DD205680A5/de unknown
- 1982-11-29 LU LU84494A patent/LU84494A1/xx unknown
- 1982-11-30 CH CH6960/82A patent/CH650946A5/it not_active IP Right Cessation
- 1982-11-30 DK DK531782A patent/DK531782A/da not_active Application Discontinuation
- 1982-11-30 DE DE3244313A patent/DE3244313C2/de not_active Expired
- 1982-11-30 RO RO109181A patent/RO86064B/ro unknown
- 1982-12-01 BE BE0/209617A patent/BE895208A/fr not_active IP Right Cessation
- 1982-12-01 PL PL1982248949A patent/PL138697B1/pl unknown
- 1982-12-01 PL PL1982239300A patent/PL137518B1/pl unknown
- 1982-12-01 EG EG708/82A patent/EG16016A/xx active
- 1982-12-01 IE IE2861/82A patent/IE53599B1/en unknown
- 1982-12-01 CU CU8125390AA patent/CU21442A3/es unknown
- 1982-12-02 JP JP57210701A patent/JPS58104635A/ja active Granted
- 1982-12-02 IN IN1403/CAL/82A patent/IN157897B/en unknown
- 1982-12-02 FI FI824150A patent/FI71883C/fi not_active IP Right Cessation
-
1986
- 1986-10-16 US US06/918,668 patent/US4778827A/en not_active Expired - Fee Related
- 1986-10-24 KR KR1019860008931A patent/KR890004344B1/ko active IP Right Grant
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