NO138476B - SCISSORS FOR CUTTING METAL AND THE LIKE - Google Patents
SCISSORS FOR CUTTING METAL AND THE LIKE Download PDFInfo
- Publication number
- NO138476B NO138476B NO71617A NO61771A NO138476B NO 138476 B NO138476 B NO 138476B NO 71617 A NO71617 A NO 71617A NO 61771 A NO61771 A NO 61771A NO 138476 B NO138476 B NO 138476B
- Authority
- NO
- Norway
- Prior art keywords
- ammonia
- catalyst
- air
- equal
- propylene
- Prior art date
Links
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 42
- 238000000034 method Methods 0.000 claims description 29
- 239000003054 catalyst Substances 0.000 claims description 25
- 229910021529 ammonia Inorganic materials 0.000 claims description 24
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 229910052751 metal Inorganic materials 0.000 claims description 6
- 239000002184 metal Substances 0.000 claims description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 5
- 150000002825 nitriles Chemical class 0.000 claims description 5
- 230000008569 process Effects 0.000 claims description 5
- 239000004215 Carbon black (E152) Substances 0.000 claims description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 4
- 229930195733 hydrocarbon Natural products 0.000 claims description 4
- 150000002430 hydrocarbons Chemical class 0.000 claims description 4
- 150000002739 metals Chemical class 0.000 claims description 3
- 229910052742 iron Inorganic materials 0.000 claims description 2
- 229910052759 nickel Inorganic materials 0.000 claims description 2
- 229910052720 vanadium Inorganic materials 0.000 claims description 2
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 claims 1
- HGINCPLSRVDWNT-UHFFFAOYSA-N Acrolein Chemical compound C=CC=O HGINCPLSRVDWNT-UHFFFAOYSA-N 0.000 description 21
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 11
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 11
- WEVYAHXRMPXWCK-UHFFFAOYSA-N Acetonitrile Chemical compound CC#N WEVYAHXRMPXWCK-UHFFFAOYSA-N 0.000 description 9
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 description 9
- 239000000203 mixture Substances 0.000 description 9
- 239000012876 carrier material Substances 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 6
- 239000007789 gas Substances 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 4
- 235000012239 silicon dioxide Nutrition 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000011261 inert gas Substances 0.000 description 3
- 238000006116 polymerization reaction Methods 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 239000000741 silica gel Substances 0.000 description 3
- 229910002027 silica gel Inorganic materials 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical group CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 229910052797 bismuth Inorganic materials 0.000 description 2
- JCXGWMGPZLAOME-UHFFFAOYSA-N bismuth atom Chemical compound [Bi] JCXGWMGPZLAOME-UHFFFAOYSA-N 0.000 description 2
- 229910000416 bismuth oxide Inorganic materials 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- TYIXMATWDRGMPF-UHFFFAOYSA-N dibismuth;oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[Bi+3].[Bi+3] TYIXMATWDRGMPF-UHFFFAOYSA-N 0.000 description 2
- 239000013067 intermediate product Substances 0.000 description 2
- -1 pyridine compound Chemical class 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- FKNQCJSGGFJEIZ-UHFFFAOYSA-N 4-methylpyridine Chemical compound CC1=CC=NC=C1 FKNQCJSGGFJEIZ-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910005578 NiBi Inorganic materials 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000006735 deficit Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 239000003701 inert diluent Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 150000002823 nitrates Chemical class 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- NWJZFGOFYNPABH-UHFFFAOYSA-N prop-1-ene;prop-2-enenitrile Chemical group CC=C.C=CC#N NWJZFGOFYNPABH-UHFFFAOYSA-N 0.000 description 1
- 239000008262 pumice Substances 0.000 description 1
- JUJWROOIHBZHMG-UHFFFAOYSA-N pyridine Substances C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 description 1
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 description 1
- 229910010271 silicon carbide Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- GPPXJZIENCGNKB-UHFFFAOYSA-N vanadium Chemical compound [V]#[V] GPPXJZIENCGNKB-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B23—MACHINE TOOLS; METAL-WORKING NOT OTHERWISE PROVIDED FOR
- B23D—PLANING; SLOTTING; SHEARING; BROACHING; SAWING; FILING; SCRAPING; LIKE OPERATIONS FOR WORKING METAL BY REMOVING MATERIAL, NOT OTHERWISE PROVIDED FOR
- B23D15/00—Shearing machines or shearing devices cutting by blades which move parallel to themselves
- B23D15/04—Shearing machines or shearing devices cutting by blades which move parallel to themselves having only one moving blade
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B23—MACHINE TOOLS; METAL-WORKING NOT OTHERWISE PROVIDED FOR
- B23D—PLANING; SLOTTING; SHEARING; BROACHING; SAWING; FILING; SCRAPING; LIKE OPERATIONS FOR WORKING METAL BY REMOVING MATERIAL, NOT OTHERWISE PROVIDED FOR
- B23D17/00—Shearing machines or shearing devices cutting by blades pivoted on a single axis
- B23D17/02—Shearing machines or shearing devices cutting by blades pivoted on a single axis characterised by drives or gearings therefor
- B23D17/08—Shearing machines or shearing devices cutting by blades pivoted on a single axis characterised by drives or gearings therefor actuated by hand or foot operated lever mechanism
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B23—MACHINE TOOLS; METAL-WORKING NOT OTHERWISE PROVIDED FOR
- B23D—PLANING; SLOTTING; SHEARING; BROACHING; SAWING; FILING; SCRAPING; LIKE OPERATIONS FOR WORKING METAL BY REMOVING MATERIAL, NOT OTHERWISE PROVIDED FOR
- B23D33/00—Accessories for shearing machines or shearing devices
- B23D33/02—Arrangements for holding, guiding, and/or feeding work during the operation
- B23D33/025—Guillotines with holding means behind the knives
-
- 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
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
- Y10T83/00—Cutting
- Y10T83/202—With product handling means
- Y10T83/2092—Means to move, guide, or permit free fall or flight of product
- Y10T83/2198—Tiltable or withdrawable support
-
- 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
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
- Y10T83/00—Cutting
- Y10T83/929—Tool or tool with support
- Y10T83/9411—Cutting couple type
- Y10T83/9447—Shear type
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Shearing Machines (AREA)
- Nonmetal Cutting Devices (AREA)
- Food-Manufacturing Devices (AREA)
- Knives (AREA)
- Scissors And Nippers (AREA)
- Details Of Cutting Devices (AREA)
Description
Fremgangsmåte til fremstilling av umettede nitriler. Process for the production of unsaturated nitriles.
Oppfinnelsen vedrører en fremgangsmåte til fremstilling av umettede nitriler av olefiner ved omsetning med luft og ammoniakk på katalysatorer. The invention relates to a method for producing unsaturated nitriles from olefins by reaction with air and ammonia on catalysts.
Det er allerede kjent fremgangsmåter, There are already known methods,
eksempelvis til å omdanne propylen ved katalytisk omsetning med oksygen resp. luft og ammoniakk i gassfase til akrylnitril. I en gruppe av slike fremgangsmåter omsettes propylenet først på en kontakt med surstoff resp. luft til akrolein. Akroleinet omsettes i et annet fremgangsmåte-trinn med ytterligere oksygen resp. luft og med ammoniakk til akrylnitril. For det annet trinn kommer det fortrinnsvis til anvendelse MoO.,-holdige katalysatorer. for example to convert propylene by catalytic reaction with oxygen or air and ammonia in gas phase to acrylonitrile. In a group of such methods, the propylene is first reacted in contact with oxygen or air to acrolein. The acrolein is reacted in another process step with additional oxygen or air and with ammonia to acrylonitrile. For the second step, catalysts containing MoO., are preferably used.
Ulempene ved denne kjente fremgangsmåte ligger i at akroleinet danner bipro-dukter med ammoniakk, nemlig fortrinnsvis pyridinforbindelsen som p-picolin. Dessuten fører her akroleinet på grunn av polymerisasjon til driftsforstyrrelser. The disadvantages of this known method lie in the fact that the acrolein forms by-products with ammonia, namely preferably the pyridine compound such as p-picoline. In addition, the acrolein here leads to operational disturbances due to polymerization.
Ved en annen likeledes tidligere kjent fremgangsmåte omsettes propylen under samtidig tilsetning av oksygen resp. luft og ammoniakk til akrylnitril, idet igjen MoO.,-holdig kontakt anvendes som på den annen side gir akrolein med et ammoniakk - overskudd eller helt uten ammoniakk. Også ved denne fremgangsmåte er altså akroleinet å anse som først dannet mellom-produkt. En ulempe ved denne fremgangsmåte ligger således deri at alt etter den tilsatte ammoniakkmengde akrolein som opptrer i forskjellig konsentrasjon, idet polymerisasjon kan føre til tilstoppinger. En videre ulempe ved denne kjente fremgangsmåte er at ved siden av akrylnitril oppstår dessuten acetonitril i betraktelige mengder og som deretter må adskilles fra akrylnitrilet. Endelig blir som ytterligere ulempe ved fremgangsmåten i tidsforløpet verdifullt MoO., på grunn av sin flyktighet, ført bort fra katalysatoren som dermed taper i aktivitet. In another similarly previously known method, propylene is reacted with the simultaneous addition of oxygen or air and ammonia to acrylonitrile, again using a MoO.,-containing contact which, on the other hand, gives acrolein with an excess of ammonia or no ammonia at all. Also in this method, the acrolein is therefore to be considered as the intermediate product formed first. A disadvantage of this method thus lies in the fact that, depending on the added amount of ammonia, acrolein appears in different concentrations, as polymerization can lead to blockages. A further disadvantage of this known method is that, alongside acrylonitrile, acetonitrile also occurs in considerable quantities and which must then be separated from the acrylonitrile. Finally, as a further disadvantage of the method, in the course of time, valuable MoO., due to its volatility, is carried away from the catalyst, which thus loses activity.
Det er nu overraskende funnet at en med godt utbytte forløpende omdannelse av propylen med oksygen resp. luft og ammoniakk er mulig i et trinn også på MoOt-frie katalysatorer. En fordel ved fremgangsmåten ifølge oppfinnelsen ligger deri at uavhengig av forholdet ammoniakk: propylen dannes praktisk talt intet akrolein, hvorved polymerisasjonsfaren er ned-satt. På katalysatorene som anvendes ved fremgangsmåten ifølge oppfinnelsen dannes imidlertid også helt uten tilsetning av ammoniakk av en propylen-oksygen resp. propylenluftblanding intet akrolein. Akrolein er følgelig ikke å anse som mellompro-dukt ved fremgangsmåten ifølge oppfinnelsen. Det er desto mer tenkbart at det pri-mære oksydative angrep ikke foregår på propylen men på ammoniakk. Det sannsyn-ligvis intermediært dannede oksydasjons-produkt av ammoniakk kan deretter direkte reagere med propylenet. For den tekniske og økonomiske anvendelse av fremgangsmåten er imidlertid reaksjonsmekanismen bare av underordnet betydning. It has now surprisingly been found that a continuous conversion of propylene with oxygen or air and ammonia is possible in one step also on MoOt-free catalysts. An advantage of the method according to the invention lies in the fact that, regardless of the ammonia:propylene ratio, practically no acrolein is formed, whereby the risk of polymerization is reduced. On the catalysts used in the method according to the invention, however, a propylene-oxygen resp. propylene air mixture no acrolein. Acrolein is therefore not to be considered an intermediate product in the process according to the invention. It is all the more conceivable that the primary oxidative attack does not take place on propylene but on ammonia. The probably intermediately formed oxidation product of ammonia can then directly react with the propylene. For the technical and economic application of the method, however, the reaction mechanism is only of secondary importance.
En ytterligere fordel ved fremgangsmåten ifølge oppfinnelsen ligger deri at ved siden av det ønskede akrylnitril oppstår bare en ubetydelig mengde acetonitril, hvis adskillelse fra akrylnitril ikke byr på noen vanskeligheter. Den dannede mengde acetonitril utgjør mindre enn 3 pst. referert til den dannede mengde akrylnitril. Videre er det å anse som en ytterligere fordel ved fremgangsmåten at anvendelsen av dyrt MoOs unngås, hvilket under de anvendte reaksjonsbetingelser ellers lett vil kunne føres bort fra katalysatoren. A further advantage of the method according to the invention lies in the fact that next to the desired acrylonitrile only an insignificant amount of acetonitrile occurs, the separation of which from acrylonitrile does not present any difficulties. The amount of acetonitrile formed amounts to less than 3 percent in reference to the amount of acrylonitrile formed. Furthermore, it is to be considered a further advantage of the method that the use of expensive MoOs is avoided, which under the reaction conditions used would otherwise easily be carried away from the catalyst.
Oppfinnelsen vedrører altså en fremgangsmåte til fremstilling av umettede nitriler ved at man behandler et olefinisk hydrokarbon, eventuelt etter tilsetning av vanndamp med luft og/eller oksygen samt ammoniakk ved forhøyet temperatur i nærvær av en katalysator og fremgangsmåten er karakteristisk ved at det anvendes en katalysator som har den generelle sam-mensetning MeaBibP(., 0(1, idet a, b, c, og d betyr de respektive atomantall og idet a er lik 1, b kan være lik 0 til 10,5, e kan være lik 0—3,5 og d kan være lik 1 til 26, under forutsetning av at b og c samtidig ikke er lik 0, mens Me er minst et av metallene jern, vanadin eller nikkel. The invention therefore relates to a process for the production of unsaturated nitriles by treating an olefinic hydrocarbon, optionally after adding steam with air and/or oxygen and ammonia at elevated temperature in the presence of a catalyst, and the process is characterized by the use of a catalyst which has the general composition MeaBibP(., 0(1, where a, b, c, and d mean the respective atomic number and where a is equal to 1, b may be equal to 0 to 10.5, e may be equal to 0— 3.5 and d can be equal to 1 to 26, provided that b and c are not equal to 0 at the same time, while Me is at least one of the metals iron, vanadium or nickel.
Katalysatoren som anvendes ved fremgangsmåten ifølge oppfinnelsen er fordel-aktig påført på et bærestoff. Som spesielt gunstig har anvendelsen av kiselsyre vist seg som bærestoff. Denne kiselsyre kan anvendes i ønskelig form, eksempelvis som kolloidal oppløsning sammen med metall-saltene som oppløsninger eller i stykke-formet fortørket og også sintret form. The catalyst used in the method according to the invention is advantageously applied to a carrier. The use of silicic acid as a carrier material has proven to be particularly beneficial. This silicic acid can be used in the desired form, for example as a colloidal solution together with the metal salts as solutions or in piece-shaped pre-dried and also sintered form.
Det ble fastslått at disse katalysatorers selektivitet forbedres ved tilsetningen av vismutoksyd således at anvendelsen av blandinger av oksyder av metallene fra første overgangsperiode på den ene side og av vismutoksyd på den annen side er spesielt gunstig. Imidlertid kan molfor-holdet av tilsvarende overgangselementer: vismut variere innen vide grenser. Således kan katalysatoren inneholde mellom 0 og ca. 80 mol-pst. Bi.,0.,, idet disse mol-pst. er referert til bærefri kontaktmasse. Slike katalysatorer ble anvendt med resultat. Som denne angivelse viser, er fremgangsmåten ifølge oppfinnelsen imidlertid ikke begren-set til vismutholdige kontakter. It was determined that the selectivity of these catalysts is improved by the addition of bismuth oxide so that the use of mixtures of oxides of the metals from the first transition period on the one hand and of bismuth oxide on the other hand is particularly beneficial. However, the molar ratio of corresponding transition elements: bismuth can vary within wide limits. Thus, the catalyst can contain between 0 and approx. 80 mole percent Bi.,0.,, as these mol-pst. is referred to non-bearing contact mass. Such catalysts were used with results. As this statement shows, however, the method according to the invention is not limited to bismuth-containing contacts.
Til fremstillingen av katalysatoren som anvendes ved fremgangsmåten ifølge oppfinnelsen setter man til en vandig oppløs-ning av de tilsvarende metallsalter og eventuelt forforsyre eksempelvis kiselgel som bærematerial inndampet til tørrhet og rø-ster tilslutt residuet ved øket temperatur. Som metallsalter anvendes spesielt de tilsvarende nitrater, eventuelt i salpetersur oppløsning eller ammoniumsaltene. Kisel-syren innføres i kolloidal form resp. kisel-gelen som bærematerial i stykkeform med en diameter på fortrinnsvis ca. 2 til 4 mm. Katalysatormassen røstes ved temperaturer fra ca. 300 til 1100° C, fortrinnsvis ved ca. 400 til 600° C. Deretter aktiveres katalysatoren ved oppvarmning i en luftammoni-akkstrøm idet luft-ammoniakkblandingen inneholder ca. 10 til 20 volumpst. ammoniakk og idet aktiviseringstemperaturen igjen omtrent tilsvarer røstetemperaturen. For the production of the catalyst used in the method according to the invention, an aqueous solution of the corresponding metal salts and possibly pre-acid, e.g. silica gel as a carrier material, is evaporated to dryness and the residue is finally roasted at an elevated temperature. As metal salts, the corresponding nitrates are used in particular, possibly in nitric acid solution or the ammonium salts. The silicic acid is introduced in colloidal form or the silica gel as carrier material in piece form with a diameter of preferably approx. 2 to 4 mm. The catalyst mass is roasted at temperatures from approx. 300 to 1100° C, preferably at approx. 400 to 600° C. The catalyst is then activated by heating in an air-ammonia battery stream, as the air-ammonia mixture contains approx. 10 to 20 vol. ammonia and since the activation temperature again approximately corresponds to the roasting temperature.
Katalysatoren ifølge oppfinnelsen som anvendes ved fremgangsmåten kan komme til anvendelse i konsentrert form. Den kan imidlertid som nevnt fortrinnsvis også være påført på et bærestoff, idet det som bærematerial for katalysatoren kan anvendes i The catalyst according to the invention used in the method can be used in concentrated form. However, as mentioned, it can preferably also be applied to a carrier material, since it can be used as a carrier material for the catalyst in
stedet for kiselgel (kiselsyre) andre inerte instead of silica gel (silicic acid) other inert
stoffer som f. eks. silisiumkarbid, alumini-umoksyd, pimpsten eller liknende eller substances such as silicon carbide, aluminum oxide, pumice or similar or
blandinger av slike stoffer. I stedet for den mixtures of such substances. Instead of it
beskrevne type av påføring av tilsvarende katalytisk virksomme forbindelser på bære-stoffet ved f. eks. impregnering av dette described type of application of corresponding catalytically active compounds to the carrier by, e.g. impregnation of this
med en vandig oppløsning av disse forbindelser, kan også hvilke som helst andre kjente og ønskelige metoder til påføring på bærematerial benyttes. Under det ole-finiske hydrokarbons omsetning i blanding med luft og/eller oksygen så vel som ammoniakk på katalysatoren opprettholdes temperaturer mellom ca. 250° og 600° C og trykk mellom ca. 0,1 ato og 10 ato idet valget av strømningshastighet og oppholds-tid av gassblandingen på kontakten er under innflytelse av stillingen av temperatur optimum. Trykket i reaktoren er ikke spesielt utslagsgivende for fremgangsmåten. with an aqueous solution of these compounds, any other known and desirable methods for application to carrier material can also be used. During the reaction of the olefinic hydrocarbon in a mixture with air and/or oxygen as well as ammonia on the catalyst, temperatures are maintained between approx. 250° and 600° C and pressure between approx. 0.1 ato and 10 ato, as the choice of flow rate and residence time of the gas mixture on the contact is influenced by the position of temperature optimum. The pressure in the reactor is not particularly decisive for the method.
Generelt arbeides det med normalt trykk eller svakt overtrykk til ca. 3 ato og som spesielt gunstig ved temperaturer mellom ca. 375 og 550° C. Oppholdstiden av olefin-luft-ammoniakkblandingen over katalysatoren ligger endelig mellom ca. 0,05 og 50 sekunder, fortrinnsvis mellom ca. 0,2 til 20 sekunder. In general, work is done with normal pressure or slight overpressure to approx. 3 ato and as particularly favorable at temperatures between approx. 375 and 550° C. The residence time of the olefin-air-ammonia mixture over the catalyst is finally between approx. 0.05 and 50 seconds, preferably between approx. 0.2 to 20 seconds.
Gassenes gjensidige mengdeforhold er ikke spesielt utslagsgivende da det heller ikke ved en arbeidsmåte med ammoniakk-underskudd opptrer noe akrolein. Et vo-lumforhold på olefinisk hydrokarbon: ammoniakk: luft på ca. 1 : 1 : 7,5 har vist seg som gunstig. The mutual quantity ratio of the gases is not particularly decisive, as no acrolein appears in a working method with an ammonia deficit either. A volume ratio of olefinic hydrocarbon: ammonia: air of approx. 1 : 1 : 7.5 has proven beneficial.
Til reaksjonsgassene kan det settes vekslende mengder av inerte gasser. Således kan det ifølge oppfinnelsen arbeides i nærvær av inerte gasser resp. fortynnings-midler som eksempelvis vanndamp, kar-bondioksyd eller nitrogen. Herved oppnås en mest mulig jevn temperaturfordeling i reaktoren og det unngås en uønsket dan-nelse av overopphetede soner. Den hertil nødvendige inertgassmengde influerer sterkt på typen og formen av reaktoren og kontaktens lagtykkelse og er avhengig av dette. Alternating amounts of inert gases can be added to the reaction gases. Thus, according to the invention, work can be done in the presence of inert gases or diluents such as water vapour, carbon dioxide or nitrogen. This achieves the most even possible temperature distribution in the reactor and avoids the unwanted formation of overheated zones. The amount of inert gas required for this strongly influences the type and shape of the reactor and the layer thickness of the contact and is dependent on this.
Katalysatoren som anvendes ved fremgangsmåten ifølge oppfinnelsen kan være anordnet som fast sjikt eller som hvirvel-eller fluidisert sjikt. The catalyst used in the method according to the invention can be arranged as a solid layer or as a vortex or fluidized layer.
Ved fremgangsmåten ifølge oppfinnelsen anvendes det til fremstilling av akrylnitril propylen. Det kan imidlertid eksempelvis også fremstilles metakrylsyrenitril eller liknende av isobutylen osv. Vanligvis fåes det karbonkjeder, det kan imidlertid også under spesielt energiske arbeidsbetin-gelser dannes et nitril med en forkortet kjede f. eks. akrylnitril av isobutylen. De følgende eksempler anskueliggjør fremgangsmåten ifølge oppfinnelsen: In the method according to the invention, it is used for the production of acrylonitrile propylene. However, it is also possible, for example, to produce methacrylic acid nitrile or the like from isobutylene, etc. Usually carbon chains are obtained, however, it is also possible under particularly energetic working conditions to form a nitrile with a shortened chain, e.g. acrylonitrile of isobutylene. The following examples illustrate the method according to the invention:
Eksempel 1. Example 1.
Ca. 200 cm<3> av en katalysator som besto av 24,4 vektspst. Fe20.,, 70,7 vektspst. Bi20.t, 4,9 vektspst. P2Ofi med formel FeBiP,, 256.u;2 fylles i en oksydasjonsreaktor. Det innføres en blanding av 116 liter luft, 15,5 liter propylen, 15,5 liter ammoniakk og 55 liter About. 200 cm<3> of a catalyst which consisted of 24.4 wt. Fe2O.,, 70.7 wt. Bi20.t, 4.9 wt. P2Ofi with formula FeBiP,, 256.u;2 is filled in an oxidation reactor. A mixture of 116 liters of air, 15.5 liters of propylene, 15.5 liters of ammonia and 55 liters of
vanndamp pr. time. Temperaturen varierer slik det fremgår av følgende tabell: water vapor per hour. The temperature varies as shown in the following table:
Eksempel 2. Example 2.
Ca. 200 cm<3> av den ovennevnte katalysator ifylles en oksydasjonsreaktor. Ved en About. An oxidation reactor is filled with 200 cm<3> of the above-mentioned catalyst. By one
temperatur på 450° C i reaktoren innføres 116 liter luft, 15,5 liter propylen og 55 liter vanndamp pr. time. Ammoniakkmengden varierer slik det fremgår av følgende tabell: temperature of 450° C, 116 liters of air, 15.5 liters of propylene and 55 liters of steam are introduced into the reactor per hour. The amount of ammonia varies as shown in the following table:
Eksempel 3. Example 3.
Ca. 200 cm3 av hver av følgende katalysatorer: 1. 24,4 vektspst Fe20;i, 70,7 vektspst. Bi20,,, 4,9 vektspst. P20- med formel FeBi., 2. 95,1 vektspst. Fe20.(, 4,9 vektspst. P20-med formel FeP(l 0.-kSO, -v 3. 23 vektspst. NiO, 71,9 vektspst. Bi20;!> 5,1 vektspst. P;iO- med formel NiBi<P>,)04<0.>(1,. 4. 22,8 vektsp~st. Fe20.,, 66,2, vektspst. Bi20:), 6,3 vektspst" V20-, 4,8 vektspst. P2Or, med formel Fe0 8V(I2Bi() 8P0 20., 5. 25,5 vektspst. Fe.,0;1, 74,5 vektspst. About. 200 cm3 of each of the following catalysts: 1. 24.4 wt.ppt Fe20;i, 70.7 wt.ppt. Bi20,,, 4.9 wt. P20- with formula FeBi., 2. 95.1 wt. Fe2O.(, 4.9 wt% P20-with formula FeP(l 0.-kSO, -v 3. 23 wt% NiO, 71.9 wt% Bi2O;!> 5.1 wt% P;iO- with formula NiBi<P>,)04<0.>(1,. 4. 22.8 wt. sp~st. Fe20.,, 66.2, wt. spst. Bi20:), 6.3 wt. spst" V20-, 4.8 wt. spst. . P2Or, with formula Fe0 8V(I2Bi() 8P0 20., 5. 25.5 wt.ppt. Fe.,0;1, 74.5 wt.ppt.
Bi20:1 med formel FeBiOs, Bi20:1 with formula FeBiOs,
innfylles i en oksydasjonsreaktor. Ved en temperatur på 400° C innføres 116 liter luft, 15,5 liter propylen, 15,5 liter ammoniakk og 55 liter vanndamp pr. time. is filled into an oxidation reactor. At a temperature of 400° C, 116 liters of air, 15.5 liters of propylene, 15.5 liters of ammonia and 55 liters of water vapor are introduced per hour.
Claims (1)
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| ZA701132A ZA701132B (en) | 1970-02-20 | 1970-02-20 | Cutting or shearing machines |
| ZA706300 | 1970-09-15 | ||
| ZA706732 | 1970-10-05 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| NO138476B true NO138476B (en) | 1978-06-05 |
| NO138476C NO138476C (en) | 1978-09-13 |
Family
ID=27420846
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO61771A NO138476C (en) | 1970-02-20 | 1971-02-19 | SCISSORS FOR CUTTING METAL AND THE LIKE |
Country Status (13)
| Country | Link |
|---|---|
| US (2) | US3757621A (en) |
| JP (1) | JPS5548923B1 (en) |
| BE (1) | BE763219A (en) |
| CA (1) | CA981180A (en) |
| DE (1) | DE2108064C3 (en) |
| DK (1) | DK144674C (en) |
| FR (1) | FR2078868A5 (en) |
| GB (1) | GB1346641A (en) |
| IL (1) | IL36242A (en) |
| NL (1) | NL168735C (en) |
| NO (1) | NO138476C (en) |
| SE (1) | SE403263B (en) |
| SU (1) | SU465770A3 (en) |
Families Citing this family (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2238841C2 (en) * | 1972-08-07 | 1984-08-23 | Intermenua (Proprietary) Ltd., Johannesburg | Machine scissors |
| US3924504A (en) * | 1973-08-17 | 1975-12-09 | Hill Acme Company | Shearing apparatus |
| US3913433A (en) * | 1974-06-19 | 1975-10-21 | Magnasync Moviola Corp | Film cutter |
| US4246816A (en) * | 1978-12-21 | 1981-01-27 | Ivanoff Osmo O | Sheet cutting apparatus |
| EP0111598B1 (en) * | 1982-12-10 | 1986-10-01 | International Business Machines Corporation | Mechanism for cutting single thickness paper or like sheet material and apparatus including such mechanism |
| DE3431111A1 (en) * | 1984-08-24 | 1986-03-06 | Steiner, Richard, 5901 Wilnsdorf | Sheet shears |
| FR2588205B1 (en) * | 1985-10-07 | 1989-08-18 | Gerard Michel | THREADED ROD CUTTING APPARATUS |
| US5363729A (en) * | 1987-08-03 | 1994-11-15 | Amada Company, Ltd. | Shearing machine |
| GB2208363B (en) * | 1987-08-03 | 1991-05-29 | Amada Co Ltd | Shearing machine |
| WO1992016328A1 (en) * | 1991-03-13 | 1992-10-01 | Hannu Juhani Alitalo | Shearing machine having a moving curved support surface |
| US5569146A (en) * | 1994-01-28 | 1996-10-29 | Ranpak Corp. | Cushioning conversion machine including a cutting/aligning assembly |
| EP1534083B1 (en) * | 2002-08-05 | 2011-11-09 | Tetra Laval Holdings & Finance SA | Device and method for through-cutting of an extruded ice mass |
| ES2339264T3 (en) * | 2004-08-24 | 2010-05-18 | Soudronic Ag | IMPACT SHEAR FOR SHEETS. |
| CN100525972C (en) * | 2007-10-23 | 2009-08-12 | 重庆齿轮箱有限责任公司 | Bronze tablet shearing mechanism for adjustable flat spring coupling |
| ES2399117B1 (en) * | 2010-10-18 | 2014-01-29 | Maquinaria Geka, S.A. | IMPROVED SYSTEM TO CUT TIRES IN CUTTING MACHINES. |
| CN104117726A (en) * | 2014-06-16 | 2014-10-29 | 张龙 | Aluminum substrate raw material board cutting machine |
| NL2021522B1 (en) * | 2018-08-30 | 2020-04-24 | Sdd Holding B V | Cutting device and method for cutting paper |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US294966A (en) * | 1884-03-11 | Haevey b | ||
| DE7939C (en) * | 1879-05-15 | 1879-11-04 | R. B. jentzsch und H. zwanziger in Wien | Combined tool for cutting, punching, riveting and the like. |
| US1000789A (en) * | 1910-09-29 | 1911-08-15 | Fred L Elliott | Printer's lead and rule cutter. |
| US2814343A (en) * | 1950-12-22 | 1957-11-26 | Bliss E W Co | Strip splicer |
| US2742087A (en) * | 1954-05-25 | 1956-04-17 | Rudolph O Smith | Sheet severing equipment |
| US2973678A (en) * | 1957-04-25 | 1961-03-07 | Proctor Silex Corp | Cutting and transfer mechanism for gelatinous treating apparatus |
| US3408888A (en) * | 1965-09-17 | 1968-11-05 | Buffalo Forge Co | Shearing apparatus |
| GB1158187A (en) * | 1966-04-19 | 1969-07-16 | Emile Breetvelt | Improved shearing machine for plates. |
| AT282303B (en) * | 1968-11-15 | 1970-06-25 | Haemmerle Ag Maschf | Tin snips |
-
1971
- 1971-02-17 US US00116041A patent/US3757621A/en not_active Expired - Lifetime
- 1971-02-17 CA CA105,659A patent/CA981180A/en not_active Expired
- 1971-02-18 NL NL7102184A patent/NL168735C/en not_active IP Right Cessation
- 1971-02-18 SE SE209071A patent/SE403263B/en unknown
- 1971-02-19 SU SU1623817A patent/SU465770A3/en active
- 1971-02-19 DE DE2108064A patent/DE2108064C3/en not_active Expired
- 1971-02-19 NO NO61771A patent/NO138476C/en unknown
- 1971-02-19 FR FR7105834A patent/FR2078868A5/fr not_active Expired
- 1971-02-19 BE BE763219A patent/BE763219A/en not_active IP Right Cessation
- 1971-02-19 IL IL3624271A patent/IL36242A/en unknown
- 1971-02-20 JP JP794271A patent/JPS5548923B1/ja active Pending
- 1971-02-22 DK DK78971A patent/DK144674C/en not_active Application Discontinuation
- 1971-04-19 GB GB2215871A patent/GB1346641A/en not_active Expired
-
1974
- 1974-03-19 US US45257074 patent/USRE28345E/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| NL168735B (en) | 1981-12-16 |
| SU465770A3 (en) | 1975-03-30 |
| DK144674B (en) | 1982-05-10 |
| SE403263B (en) | 1978-08-07 |
| DE2108064A1 (en) | 1971-08-26 |
| FR2078868A5 (en) | 1971-11-05 |
| NL168735C (en) | 1982-05-17 |
| NO138476C (en) | 1978-09-13 |
| DK144674C (en) | 1982-10-11 |
| DE2108064B2 (en) | 1977-03-31 |
| NL7102184A (en) | 1971-08-24 |
| JPS5548923B1 (en) | 1980-12-09 |
| BE763219A (en) | 1971-07-16 |
| US3757621A (en) | 1973-09-11 |
| DE2108064C3 (en) | 1983-12-08 |
| CA981180A (en) | 1976-01-06 |
| USRE28345E (en) | 1975-02-25 |
| IL36242A0 (en) | 1971-04-28 |
| IL36242A (en) | 1974-03-14 |
| GB1346641A (en) | 1974-02-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| NO138476B (en) | SCISSORS FOR CUTTING METAL AND THE LIKE | |
| US3642930A (en) | Process for the manufacture of isoprene from isoamylenes and methyl butanols and catalyst therefor | |
| US4816603A (en) | Process for the production of methacrolein and methacrylic acid | |
| US6916763B2 (en) | Process for preparing a catalyst for the oxidation and ammoxidation of olefins | |
| CA1113498A (en) | Preparation of methacrylic derivatives from tertiary butyl-containing compound | |
| EP0437056A2 (en) | Catalyst and process for the manufacture of acrylonitrile and methacrylonitrile | |
| US4156660A (en) | Catalyst useful for the manufacture of acrylonitrile and methacrylonitrile | |
| US4503001A (en) | Process for the manufacture of acrylonitrile and methacrylonitrile | |
| US4767878A (en) | Process for the manufacture of acrylonitrile and methacrylonitrile | |
| US3522299A (en) | Process for the oxidation of olefins to aldehydes and acids and catalyst therefor | |
| US3135783A (en) | Process for the manufacture of unsaturated nitriles | |
| EP1309402A2 (en) | Improved catalyst for the manufacture of acrylonitrile | |
| US4138430A (en) | Process for ammoxidation of 1-propanol | |
| US3542842A (en) | Ammoxidation of propylene or isobutylene to acrylonitrile or methacrylonitrile | |
| US3544616A (en) | Ammoxidation of propylene or isobutylene to acrylonitrile or methacrylonitrile | |
| US3541129A (en) | Process for the preparation of acrylonitrile | |
| US3998867A (en) | Process for the simultaneous preparation of methacrylonitrile and 1,3-butadiene | |
| US4495109A (en) | Production of unsaturated nitriles using catalysts promoted with various metals | |
| US3576764A (en) | Catalyst for the oxidation of olefins to unsaturated aldehydes and acids | |
| US4035262A (en) | Acrolein oxidation catalyst | |
| US3959384A (en) | Oxidation catalyst and process for oxidation of olefins to unsaturated aldehydes | |
| NO148936B (en) | Vapor trap with free-flowing floats | |
| US2398612A (en) | Oxidation of organic compounds | |
| US3956376A (en) | Process for the production of acrolein and acrylic acid | |
| US3313856A (en) | Preparation of acrolein or methacrolein |