US2597027A - Production of nitropauaffins - Google Patents
Production of nitropauaffins Download PDFInfo
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- US2597027A US2597027A US2597027DA US2597027A US 2597027 A US2597027 A US 2597027A US 2597027D A US2597027D A US 2597027DA US 2597027 A US2597027 A US 2597027A
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- 238000004519 manufacturing process Methods 0.000 title claims description 13
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 40
- 239000007789 gas Substances 0.000 claims description 26
- 238000000034 method Methods 0.000 claims description 26
- 230000008569 process Effects 0.000 claims description 24
- 229930195733 hydrocarbon Natural products 0.000 claims description 23
- 150000002430 hydrocarbons Chemical class 0.000 claims description 23
- 230000001590 oxidative effect Effects 0.000 claims description 23
- 229910021529 ammonia Inorganic materials 0.000 claims description 20
- 238000007254 oxidation reaction Methods 0.000 claims description 14
- 239000004215 Carbon black (E152) Substances 0.000 claims description 13
- 239000012188 paraffin wax Substances 0.000 claims description 13
- 230000003647 oxidation Effects 0.000 claims description 12
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 9
- 229910017604 nitric acid Inorganic materials 0.000 claims description 9
- 230000003197 catalytic effect Effects 0.000 claims description 7
- 238000005336 cracking Methods 0.000 claims description 7
- 230000000694 effects Effects 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 7
- 230000015572 biosynthetic process Effects 0.000 claims description 6
- 230000035484 reaction time Effects 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 5
- 239000002253 acid Substances 0.000 claims description 4
- MCSAJNNLRCFZED-UHFFFAOYSA-N nitroethane Chemical compound CC[N+]([O-])=O MCSAJNNLRCFZED-UHFFFAOYSA-N 0.000 claims description 4
- JCXJVPUVTGWSNB-UHFFFAOYSA-N Nitrogen dioxide Chemical class O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 claims 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen(.) Chemical class [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 description 31
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 19
- 239000003054 catalyst Substances 0.000 description 11
- 239000007795 chemical reaction product Substances 0.000 description 11
- 150000002829 nitrogen Chemical class 0.000 description 9
- 239000000047 product Substances 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 238000005194 fractionation Methods 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 238000006396 nitration reaction Methods 0.000 description 4
- 125000000449 nitro group Chemical group [O-][N+](*)=O 0.000 description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- RGSFGYAAUTVSQA-UHFFFAOYSA-N Cyclopentane Chemical compound C1CCCC1 RGSFGYAAUTVSQA-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- GNTDGMZSJNCJKK-UHFFFAOYSA-N divanadium pentaoxide Chemical compound O=[V](=O)O[V](=O)=O GNTDGMZSJNCJKK-UHFFFAOYSA-N 0.000 description 2
- 229910052748 manganese Inorganic materials 0.000 description 2
- 239000011572 manganese Substances 0.000 description 2
- NUJOXMJBOLGQSY-UHFFFAOYSA-N manganese dioxide Chemical compound O=[Mn]=O NUJOXMJBOLGQSY-UHFFFAOYSA-N 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- FRWYFWZENXDZMU-UHFFFAOYSA-N 2-iodoquinoline Chemical compound C1=CC=CC2=NC(I)=CC=C21 FRWYFWZENXDZMU-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 229910001260 Pt alloy Inorganic materials 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- WGLPBDUCMAPZCE-UHFFFAOYSA-N Trioxochromium Chemical compound O=[Cr](=O)=O WGLPBDUCMAPZCE-UHFFFAOYSA-N 0.000 description 1
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 150000001555 benzenes Chemical class 0.000 description 1
- LTPBRCUWZOMYOC-UHFFFAOYSA-N beryllium oxide Inorganic materials O=[Be] LTPBRCUWZOMYOC-UHFFFAOYSA-N 0.000 description 1
- 229910052797 bismuth Inorganic materials 0.000 description 1
- JCXGWMGPZLAOME-UHFFFAOYSA-N bismuth atom Chemical compound [Bi] JCXGWMGPZLAOME-UHFFFAOYSA-N 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 229940087373 calcium oxide Drugs 0.000 description 1
- 235000012255 calcium oxide Nutrition 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- DMEGYFMYUHOHGS-UHFFFAOYSA-N heptamethylene Natural products C1CCCCCC1 DMEGYFMYUHOHGS-UHFFFAOYSA-N 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 230000000802 nitrating effect Effects 0.000 description 1
- 150000005181 nitrobenzenes Chemical class 0.000 description 1
- NJNQUTDUIPVROZ-UHFFFAOYSA-N nitrocyclohexane Chemical compound [O-][N+](=O)C1CCCCC1 NJNQUTDUIPVROZ-UHFFFAOYSA-N 0.000 description 1
- CJSZWOGCKKDSJG-UHFFFAOYSA-N nitrocyclopentane Chemical compound [O-][N+](=O)C1CCCC1 CJSZWOGCKKDSJG-UHFFFAOYSA-N 0.000 description 1
- VLZLOWPYUQHHCG-UHFFFAOYSA-N nitromethylbenzene Chemical compound [O-][N+](=O)CC1=CC=CC=C1 VLZLOWPYUQHHCG-UHFFFAOYSA-N 0.000 description 1
- 125000000018 nitroso group Chemical group N(=O)* 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 229910001404 rare earth metal oxide Inorganic materials 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- ZCUFMDLYAMJYST-UHFFFAOYSA-N thorium dioxide Chemical compound O=[Th]=O ZCUFMDLYAMJYST-UHFFFAOYSA-N 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 229910052726 zirconium Inorganic materials 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C201/00—Preparation of esters of nitric or nitrous acid or of compounds containing nitro or nitroso groups bound to a carbon skeleton
- C07C201/06—Preparation of nitro compounds
- C07C201/08—Preparation of nitro compounds by substitution of hydrogen atoms by nitro groups
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C205/00—Compounds containing nitro groups bound to a carbon skeleton
- C07C205/01—Compounds containing nitro groups bound to a carbon skeleton having nitro groups bound to acyclic carbon atoms
- C07C205/02—Compounds containing nitro groups bound to a carbon skeleton having nitro groups bound to acyclic carbon atoms of a saturated carbon skeleton
Definitions
- a further object of this invention is to provide an improved process for the direct manu facture of nitrogen derivatives of parafiin hydrocarbons, by nitrating these hydrocarbons with the reaction product obtained from the catalytic oxidation of ammonia.
- a method of nitration which comprises the steps of charging ammonia and an oxidizing gas into a reaction system over a suitable catalyst under controlled conditions of temperature, pressure, and reaction time to generate nitric acid and/ or some quantities of oxides of nitrogen in the presence of introduced paraffins or paraffin derivatives, immediately reacting these paraffins with the synthesized nitric acid and/or nitrogen oxides at a temperature slightly below the cracking temperature of the paraffins to form corresponding nitroso-paraflins, subjecting these nitroso-paraflins to further oxidation with an oxidizing gas to form the corresponding nitroparafiins, and separating nitro-paraffins thus obtained from resulting gaseous products.
- ammonia and an oxidizing gas such as air, oxygen, or oxygen-enriched air are introduced, respectively, through valved charging-lines l0 and H .to a reaction system.
- This reaction system is illustrated diagrammatically in the drawing by reaction tower [2; which comprises a suitable reaction vessel having a mixing and preheating zone and a series of reaction zones, the functions of which will be hereinafter described in accordance with the process of the invention.
- the ammonia and oxidizing gas, thus introduced into tower l2, are first passed into a mixing and preheating zone A.
- zone A the charging stock thus introduced through lines [0 and l l is mixed, and preferably heated rapidly to a temperature sufficiently high to maintain the proper operating conditions of temperature and pressure in reaction zone B as hereinafter described and into which the mixed and preheated charging stock is next transferred.
- the mixed charging stock of ammonia and an oxidizing gas thus introduced intoreaction zone B, is passed overa suitable catalytic material under conditions of temperature, pressure, and reaction time eifective to convert by oxidation a substantial proportion of the ammonia to nitric acid in the vapor state.
- oxidation is most efficiently carried out by operating reaction zone B at a temperature within approximately the range of 800 C. to 1000 C. and at a super-atmospheric pressure from as indicated above, the charging stock in zone A should preferably be preheated suiiiciently high to maintain the catalyst mass within the aforementioned temperature range, to effect necessary oxidation without the application of external energy.
- the catalytic; material employed in the. oxidation reaction in zone B may be a solid material in a fluid-bed or fixed-bed state. While we have found that alloys of platinum may be overall suitable when used as catalysts in the aforementioned oxidation reaction, other catalysts may be efiectively employed; for example, we may use such catalysts as iron, cobalt, nickel or their oxides. It is also possible to use such catalysts as oxides of manganese and magnesium; dioxides of manganese and zirconium; and vanadium pentoxide.
- catalysts comprise thoria and rare earth oxides; .cobalti'c oxide and either bismuth'trioxide, aluminum oxide or berylliumoxide; ;manganese dioxide and calcium-oxide: and silica gel and chromic oxide.
- the mixed charging stock ofpreheated ammonia, and oxidizing gas is passed over the catalyst under conditions of temperature. and pressure within the aforementioned ranges, .for a time-sufficient to oxidize substantial proportions of ammonia to nitric acid inthe vapor state.
- The, product of the reaction thus produced .in zone B and comprising substantial quantities or. nitric acid, and/or some quantities of oxides of nitrogen is passed. to a reaction zone C where it. is immediately contacted with a. preheated gaseous stream of the parafiin hydrocarbon or a mixture of paraffin hydrocarbons to be nitrated.
- Parafiins which: are thus to be nitrated, are introduced into zone 6' through valved. line I3.
- the gaseous reaction. pro uc s. pro uced in zone, .C' and comprising, substantially corresponding nitroso-paraflins of the, introduced paraflins, as described above, are passed to a reaction zone D.
- the temperature of the products thus introduced' into zone D is; next reduced to a temperature suitable for further oxidation to form corresponding;nitro-parafiins.
- the' products introduced into zone D are first passed through a heat exchange medium, illustrated diagrammatically in the drawing by heat exchanger l4.
- an oxidizing gas such as air,-o-xygen, or oxygenenriched-ai r to form a reaction product, com-
- other catalysts may be.
- the reaction product withdrawn from'zone D through line It comprises substantially nitro-paraflins.
- unreacted parafiins and other gaseous products wherein the latter may comprise one or more unabsorbed gases.
- unabsorbed gases thus obtained may comprise a mixture consisting largely of nitrogen, carbon dioxide, and other gases normal- 1y present in the air.
- oxidation of corresponding n-i-trosoparafiins in zone D may of necessity be conducted at such low temperatures as to prevent direct fractionation of" the nitro-paraflin thus produced.
- reaction temperatures in zone D are at or near the boiling point of unreacted paraiiins, it will be necessary .toadd additional heat in order to obtain the desired fraction and reflux conditions in tower IT.
- the necessity for this preheating or reheating is dependent upon the quantities of the parafli-ns fedinto tower l2 through line I3.
- this may be accomplishedby transferring the aforementioned reaction product withdrawn from zone Dthrough line I6, via valved line 22, through any conventional heating device; illustrated diagrammatically thedrawing by heat exchanger 23.
- the reaction product thus. heated to a temperature'sufliciently high to permit subsequent fractionation of nitro-paraffins from other component contained therein, is transferred from heat exchanger 23 through line 24 into line. "5, with which line 24' connects, and is subjected to subsequent fractionation in tower I! in the process described above.-
- the aforementioned reaction system illustrated diagrammatically in the drawing by tower l2
- the aforementioned reaction system comprises a series of mixing, preheating, and reaction zone in a single vessel for carrying out the process of the invention, as described.
- the process of manufacturing nitrogen derivatives from paraffin hydrocarbons which comprises the steps of passing ammonia and an oxidizing gas through a heating zone at a temperature between about 800 C. and about 1000 C. and at a pressure between about and about atmospheres in the presence of a catalytic material for a reaction time effective to convert a substantial proportion of the ammonia to nitric acid in the vapor state, contacting the vapors thus produced immediately upon formation with at least one gaseous parafiin hydrocarbon at a temperature slightly below the cracking temperature of said paraffin hydrocarbon to form the corresponding nitroso-paraffin and in an amount in excess of that required to efiect substantially complete consumption of nitric acid thus formed, subjecting said nitroso-paramn to further oxidation at a reduced temperature with an additional quantity of said oxidizing gas to form the corresponding nitro-paraflin, and recovering said nitro-paramn.
- the process of manufacturing nitrogen derivatives from parafiin hydrocarbons which comprises the steps of passing ammonia and an oxidizing gas through a heating zone at a temperature between about 800 C. and about 1000 C. and at a pressure between about 10 and about 15 atmospheres in the presence of a catalytic material for a reaction time effective to convert a substantial proportion of the ammonia to nitrogen oxides in the vapor state, contacting the vapors thus produced immediately upon formation with at least one gaseous paraffin hydrocarbon at a temperature slightly below the cracking temperature of said paraflin hydrocarbon to form the corresponding nitroso-paraffin and in an amount in excess of that required to effect oxides thus formed, subjecting said nitroso parafiin to further oxidation at a reduced temperature with an additional quantity, of said oxidizing gas to form'the correspondingnitroparafiin, and recovering said nitro-parafiin.
- the process. of manufacturing nitrogen derivatives from .parafiin hydrocarbons which comprisesthe steps of passing ammonia andan oxidizing gas through a heating zone at a temperature between about 800 C. and about 1000 C. and at a pressure between about 10 and about 15 atmospheres in the presence of a catalytic material for a reaction time efiective to convert a substantial proportion of the ammonia to nitric oxide in the vapor state, and contacting the vapors thus produced immediately upon formation with at least one gaseous paraflin hydrocarbon at a temperature slightly below the cracking temperature of said paraflin hydrocarbon to form the corresponding nitroso-paraifin and in an amount in excess of that required to effect substantially complete consumption of nitric oxide thus formed, subjecting said nitrosoparafiin to further oxidation at a reduced temperature with an additional quantity of said oxidizing gas to form the corresponding nitroparaiiin, and recovering said nitro-paraffin.
- the process of manufacturing nitrogen derivatives from parafiin hydrocarbons which comprises the steps of preheating a charging stock comprising ammonia and an oxidizing gas to a temperature between about 800 C. and about 1000 C. and at a pressure between about 10 and about 15 atmospheres, passing said preheated charging stock into a first reaction zone in contact with a catalyst comprising platinum for a time effective to convert a substantial proportion of the ammonia to nitric oxide in the vapor state, passing the vapors thus produced into a second reaction zone, contacting said vapors in said second reaction zone with a gaseous parafiin hydrocarbon at a temperature slightly below the cracking temperature of said paraifin hydrocarbon to form the corresponding nitroso-paraffin and in an amount in excess of that required to effect substantially complete consumption of nitric oxide thus formed, passing the nitroso-parafiin thus formed and unreacted parafiin hydrocarbon into a third reaction zone, subjecting said nitroso-paraflin in said third reaction zone to further
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
y 20, 1952 H. J. PAssINO ETAL 7 7 PRODUCTION OF NITROPARAFFINS Filed March 27,1947
PARAFFIN RECYCLE GASEOUS PRODUCTS FRACTIONATIION PARAFFINY T WER 2| HYDROCARBONS MR l3- x 1 UNREACTED PARAFFINS REACTION CATAL-YST 20 -lo I2 g ,1 l4 l6 mxmc AND REACTION 1 REACTION REACTION k PREHEATING ZONE B ZONE C 20m: D
ZONEA NITRO- PARAFFINS INVENTORS HERBERT J.PASSINO LOUIS 'C. RUBIN B a. M
' ATTOR N EYS Patented May 20, 1952 "UNITED STATES PATENT ()FFICE PRODUCTION OF NITRQBARAFFINS Herbert J. Passino, Englewood, and Louis C. Rubin, West Caldwell, N. J., assignors to'The M. W. Kellogg Company, Jersey corporation of Delaware City, N. J., a
Application March 27, 1947, Serial No. 737,666
8 Claims. 1
vaporization zone has presented important economic obstacles because of severe corrosion problems arising from the reaction of the nitric acid upon costly equipment. In order to overcome the corrosive eifect of the acid, utilization of highly expensive corrosion-resistant material has heretofore been necessary when theaforementioned nitration technique is practiced.
It is therefore an object of the present invention to provide for an improved process for the manufacture of nitrogen derivatives of parafiin hydrocarbons.
A further object of this invention is to provide an improved process for the direct manu facture of nitrogen derivatives of parafiin hydrocarbons, by nitrating these hydrocarbons with the reaction product obtained from the catalytic oxidation of ammonia.
Other objects and advantages inherent 'in the invention will be apparent from the following more detailed disclosure.
In accordance with the process of this invention, these objects are accomplished, in general, by a method of nitration which comprises the steps of charging ammonia and an oxidizing gas into a reaction system over a suitable catalyst under controlled conditions of temperature, pressure, and reaction time to generate nitric acid and/ or some quantities of oxides of nitrogen in the presence of introduced paraffins or paraffin derivatives, immediately reacting these paraffins with the synthesized nitric acid and/or nitrogen oxides at a temperature slightly below the cracking temperature of the paraffins to form corresponding nitroso-paraflins, subjecting these nitroso-paraflins to further oxidation with an oxidizing gas to form the corresponding nitroparafiins, and separating nitro-paraffins thus obtained from resulting gaseous products.
The details, including additional features and advantages of the process of the invention, will 2 be understood by those skilledin the art from the accompanying drawing which illustrates diagrammatically one form 'of the apparatus employed and capable of carrying out one embodimentof the process of our invention. While the invention will bedescribed in detail by reference to one embodiment of the process employing the apparatus illustrated in the drawing, it should be noted that it is not intended that the.
invention be limited to the embodiment as illustrated, but is capable of other embodiments which may extend beyond the scope of the apparatus illustrated in the drawing. Some of the mechanical elements, which form no part of the invention but are necessary to eifect the transfer or liquids and vapors and to maintain the conditions of temperature and pressure necessary to carry out the function of the apparatus, are omitted in order to simplify the description.
It willbe understood, however, that much equip ment of this nature is necessary and will be supplied byfthose skilled in the art.
Referring to the drawing, ammonia and an oxidizing gas, such as air, oxygen, or oxygen-enriched air are introduced, respectively, through valved charging-lines l0 and H .to a reaction system. This reaction system is illustrated diagrammatically in the drawing by reaction tower [2; which comprises a suitable reaction vessel having a mixing and preheating zone and a series of reaction zones, the functions of which will be hereinafter described in accordance with the process of the invention. The ammonia and oxidizing gas, thus introduced into tower l2, are first passed into a mixing and preheating zone A. In zone A the charging stock thus introduced through lines [0 and l l is mixed, and preferably heated rapidly to a temperature sufficiently high to maintain the proper operating conditions of temperature and pressure in reaction zone B as hereinafter described and into which the mixed and preheated charging stock is next transferred. i
The mixed charging stock of ammonia and an oxidizing gas, thus introduced intoreaction zone B, is passed overa suitable catalytic material under conditions of temperature, pressure, and reaction time eifective to convert by oxidation a substantial proportion of the ammonia to nitric acid in the vapor state. We have found that such oxidation is most efficiently carried out by operating reaction zone B at a temperature within approximately the range of 800 C. to 1000 C. and at a super-atmospheric pressure from as indicated above, the charging stock in zone A should preferably be preheated suiiiciently high to maintain the catalyst mass within the aforementioned temperature range, to effect necessary oxidation without the application of external energy.
The catalytic; material employed in the. oxidation reaction in zone B may be a solid material in a fluid-bed or fixed-bed state. While we have found that alloys of platinum may be overall suitable when used as catalysts in the aforementioned oxidation reaction, other catalysts may be efiectively employed; for example, we may use such catalysts as iron, cobalt, nickel or their oxides. It is also possible to use such catalysts as oxides of manganese and magnesium; dioxides of manganese and zirconium; and vanadium pentoxide. used where such catalysts comprise thoria and rare earth oxides; .cobalti'c oxide and either bismuth'trioxide, aluminum oxide or berylliumoxide; ;manganese dioxide and calcium-oxide: and silica gel and chromic oxide.
As. described above, the mixed charging stock ofpreheated ammonia, and oxidizing gas is passed over the catalyst under conditions of temperature. and pressure within the aforementioned ranges, .for a time-sufficient to oxidize substantial proportions of ammonia to nitric acid inthe vapor state. The, product of the reaction thus produced .in zone B and comprising substantial quantities or. nitric acid, and/or some quantities of oxides of nitrogen is passed. to a reaction zone C where it. is immediately contacted with a. preheated gaseous stream of the parafiin hydrocarbon or a mixture of paraffin hydrocarbons to be nitrated. Parafiins which: are thus to be nitrated, are introduced into zone 6' through valved. line I3. These preheated gaseous paraffinsor parafiin mixtures are introduced into zone through line l3; in such proportions" that the temperature in this zone is maintained slightlybelow thecracking temperature of the introduced paraflins The immediate contact of the synthesizednitric. acid; and/or nitrogen oxides obtained; as. the reactionproduct'from zone B in the. nrocessdescribedabove, with h i r e pa laml silhzonefi results in the formation of thecorresponding nitroso-parafilns, in thi 'zone' as a.- gaseous reaction-product. by reason of; the intermediate reaction of nitric. aci a d/ or nitr enoxidesin .thevapor form produced from their reaction with the introduced uaramns. It willt'h noted; that the immediate reaction oi the t i cid with-narafiins in zone Cifollowi g the ab vementioned; acid synthesis; results in the prevention or theioorrosiv e fe t f the cid upon equ ment...
The gaseous reaction. pro uc s. pro uced in zone, .C' and comprising, substantially corresponding nitroso-paraflins of the, introduced paraflins, as described above, are passed to a reaction zone D. The temperature of the products thus introduced' into zone D is; next reduced to a temperature suitable for further oxidation to form corresponding;nitro-parafiins. To effect such reduction 'in temperature, the' products introduced into zone D are first passed through a heat exchange medium, illustrated diagrammatically in the drawing by heat exchanger l4. Nitrosoparafiinspresent inthereaction product thus reduced mtemperature, are next subjected to further oxidationin zone D- by admixture with an oxidizing gas, such as air,-o-xygen, or oxygenenriched-ai r to form a reaction product, com- In addition other catalysts may be.
prisin substantially the corresponding nitroparaffins of the parafl-lns introduced into zone C through line H3. The oxidizing gas thus employed is introduced into zone D through valved line IS. The reaction product thus produced is withdrawn from zone D through valved line l6.
As described above, the reaction product withdrawn from'zone D through line It, comprises substantially nitro-paraflins. In addition there may also be present unreacted parafiins and other gaseous products wherein the latter may comprise one or more unabsorbed gases. For example, where air or oxygen-enriched air is used as the oxidizing gas introduced into the reaction system through line H and/or line [5, in the process described above, unabsorbed gases thus obtained may comprise a mixture consisting largely of nitrogen, carbon dioxide, and other gases normal- 1y present in the air. The reaction product thus withdrawn from zone D is next transferred through line l5 to an intermediate point ina fractionation tower I1. Tower I! is operated underconditions of temperature and pressure ef fective to separate the higher boiling nitro-paraffins from unreacted paraffins and gaseous prodmentioned reaction product obtained from zone D, 'arewithd-rawn from tower I! at an intermediate point through valved line 20 which is at a point above the inlet of line It into the tower. These paraflins' may be next recycled through valved line-2l into line 13-, with which line 2| connects, for further use in tower I-Z- in the process described above.
In certaininstances, depending upon properties of the paraiiins introduced into zone'C- through line [3, oxidation of corresponding n-i-trosoparafiins in zone D may of necessity be conducted at such low temperatures as to prevent direct fractionation of" the nitro-paraflin thus produced. For -example, when the reaction temperatures in zone D are at or near the boiling point of unreacted paraiiins, it will be necessary .toadd additional heat in order to obtain the desired fraction and reflux conditions in tower IT. The necessity for this preheating or reheating is dependent upon the quantities of the parafli-ns fedinto tower l2 through line I3. In'such cases, the temperatureof the reaction product obtained from zone D-maybe raisedsufiicientlyhighto permit subsequent direct fractionationof nitroparafiins from unreacted paraffins and gaseous products in tower H the process described above Conveniently, this may be accomplishedby transferring the aforementioned reaction product withdrawn from zone Dthrough line I6, via valved line 22, through any conventional heating device; illustrated diagrammatically thedrawing by heat exchanger 23. The reaction product thus. heated to a temperature'sufliciently high to permit subsequent fractionation of nitro-paraffins from other component contained therein, is transferred from heat exchanger 23 through line 24 into line. "5, with which line 24' connects, and is subjected to subsequent fractionation in tower I! in the process described above.-
It will be noted that the aforementioned reaction system, illustrated diagrammatically in the drawing by tower l2, comprises a series of mixing, preheating, and reaction zone in a single vessel for carrying out the process of the invention, as described. However, where so desired, it is possible to carry out the process of the invention in a series of suitable vessels, rather than a single vessel, each of such vessels being adapted to maintain the same function as the corresponding mixing, preheating, or reaction zones illustrated in the drawing by the zones in tower 12.
Although our invention has been described with particular reference to a process for the manufacture of nitrogen derivatives of parafiin hydrocarbons, as shown above, it should be noted that it is not restricted to the nitration of openchain parafiins. The process of the invention may be also similarly applied in the manufacture of nitrogen derivatives of cyclo-parafiins to produce corresponding cyclo-nitro-parafiins; similarly nitro-benzenes may be produced from benzene or benzene derivatives; nitro-toluene from toluene or its derivatives; and nitro-cyclopentane and nitro-cyclohexane from cyclopentane and cyclohexane respectively. In each instance the degree of nitration (mono-, di-, or tri-) substition will depend upon the severity of operating conditions. In addition, while we have described a particular embodiment of our invention for purposes of illustration, it should be understood that various modifications and adaptations thereof which will be obvious to one skilled in the art may be made within the spirit of the inven-' tion as set forth in the appended claims.
Having thus described our invention, what we claim and desire to secure by Letters Patent is:
1. The process of manufacturing nitrogen derivatives from paraffin hydrocarbons which comprises the steps of passing ammonia and an oxidizing gas through a heating zone at a temperature between about 800 C. and about 1000 C. and at a pressure between about and about atmospheres in the presence of a catalytic material for a reaction time effective to convert a substantial proportion of the ammonia to nitric acid in the vapor state, contacting the vapors thus produced immediately upon formation with at least one gaseous parafiin hydrocarbon at a temperature slightly below the cracking temperature of said paraffin hydrocarbon to form the corresponding nitroso-paraffin and in an amount in excess of that required to efiect substantially complete consumption of nitric acid thus formed, subjecting said nitroso-paramn to further oxidation at a reduced temperature with an additional quantity of said oxidizing gas to form the corresponding nitro-paraflin, and recovering said nitro-paramn.
2. The process of manufacturing nitrogen derivatives from parafiin hydrocarbons which comprises the steps of passing ammonia and an oxidizing gas through a heating zone at a temperature between about 800 C. and about 1000 C. and at a pressure between about 10 and about 15 atmospheres in the presence of a catalytic material for a reaction time effective to convert a substantial proportion of the ammonia to nitrogen oxides in the vapor state, contacting the vapors thus produced immediately upon formation with at least one gaseous paraffin hydrocarbon at a temperature slightly below the cracking temperature of said paraflin hydrocarbon to form the corresponding nitroso-paraffin and in an amount in excess of that required to effect oxides thus formed, subjecting said nitroso parafiin to further oxidation at a reduced temperature with an additional quantity, of said oxidizing gas to form'the correspondingnitroparafiin, and recovering said nitro-parafiin.
3.. The process as defined by claim 2 inwhich said oxidizing gas comprises essentially free oxygen. a a
4. The process as defined by claim 2 in which said oxidizing gas comprises air. p
5. The process as defined by claim,2 in-which said oxidizing gas comprises oxygen-enriched air.
6. The process. of manufacturing nitrogen derivatives from .parafiin hydrocarbons which comprisesthe steps of passing ammonia andan oxidizing gas through a heating zone at a temperature between about 800 C. and about 1000 C. and at a pressure between about 10 and about 15 atmospheres in the presence of a catalytic material for a reaction time efiective to convert a substantial proportion of the ammonia to nitric oxide in the vapor state, and contacting the vapors thus produced immediately upon formation with at least one gaseous paraflin hydrocarbon at a temperature slightly below the cracking temperature of said paraflin hydrocarbon to form the corresponding nitroso-paraifin and in an amount in excess of that required to effect substantially complete consumption of nitric oxide thus formed, subjecting said nitrosoparafiin to further oxidation at a reduced temperature with an additional quantity of said oxidizing gas to form the corresponding nitroparaiiin, and recovering said nitro-paraffin.
7. The process of manufacturing nitrogen derivatives from parafiin hydrocarbons which comprises the steps of preheating a charging stock comprising ammonia and an oxidizing gas to a temperature between about 800 C. and about 1000 C. and at a pressure between about 10 and about 15 atmospheres, passing said preheated charging stock into a first reaction zone in contact with a catalyst comprising platinum for a time effective to convert a substantial proportion of the ammonia to nitric oxide in the vapor state, passing the vapors thus produced into a second reaction zone, contacting said vapors in said second reaction zone with a gaseous parafiin hydrocarbon at a temperature slightly below the cracking temperature of said paraifin hydrocarbon to form the corresponding nitroso-paraffin and in an amount in excess of that required to effect substantially complete consumption of nitric oxide thus formed, passing the nitroso-parafiin thus formed and unreacted parafiin hydrocarbon into a third reaction zone, subjecting said nitroso-paraflin in said third reaction zone to further oxidation at a reduced temperature with an additional quantity of said oxidizing gas to form the corresponding nitroparaflin, and removing said nitro-paraffin from said third reaction zone.
8. The process of manufacturing nitrogen derivatives from paraifin hydrocarbons which comprises the steps of preheating a charging stock comprising ammonia and an oxidizing gas to a temperature between about 800 C. and about 1000 C. and at a pressure between about 10 and about 15 atmospheres, passing said preheated charging stock into a first reaction zone in contact with a catalyst comprising platinum for a time efiective to convert a substantial proportion of the ammonia to nitric oxide in the vapor state, passing the vapors thus produced into a second reaction zone, contacting said vapors in saidSehcl reeifitieifiiohe witli a gaseousparamn hydi c'firbon'at a; temperature slightly belw the cracking temperature ot saidparamn hydrm carbon to form the corresponding: nitrcsm'pab amn anamafi amount in excess of that requird to effect subsfiafitiallycomplete consum tm'n of nitric? oxide thus formed, passing the nitros'oparaflm thus' forme'ct anci' unreactedparafiin hy-'- drocarbon into a third reaction zone, subjecting said nitros'u-paramn in said third reaction zone to further oxidatidn' Eta reduced 'temperature' with an additibnal'quantityof saidoxmiz'ing gas t6 form the 'cdr'ffipondmg "nitro parafiih; sepa= rating said nitro iiaramn from-unreacted paramnhydrcscarbam and returning un'reactedvpar 15 amn-hydrocarbon to 2 said second reacuon: zone;
HERBERT J PASSING. LDUIs c; RUBIN,
REFERENCES CITED The following references are of record in the file (2f this patent:
UNITED STATES PATENTS Number Name Date 1;967,-66'7 Hass et 21,1. a July 24', 1934 2,109,873 Wilhelm Mar. 1', 1938 2,153,065 Martin Apr. 4, 1939 2,161,475 Landon June 6; 1939- 2,288,091 Hbover June 30, 1942 2,291,345 Rideout July 28, 1942 2;4-18-,-241' Stengel et a1 Apr. 1, 1947 2,455,425 Levyet a1. u h-Dec. 7, 1948: 2,465,984 Nygaard et a1. Mar. 29, 1949' OTHER REFERENCES- Taylor, Ind. Eng. Chem, v01. 19, 1250-2 (1927
Claims (1)
1. THE PROCESS OF MANUFACTURING NITROGEN DERIVATIVES FROM PARAFFIN HYDROCARBONS WHICH COMPRISES THE STEPS OF PASSING AMMONIA AND AN OXIDIZING GAS THROUGH A HEATING ZONE AT A TEMPERATURE BETWEEN ABOUT 800* C. AND ABOUT 1000* C. AND AT A PRESSURE BETWEEN ABOUT 10 AND ABOUT 15 ATMOSPHERES IN THE PRESENCE OF A CATALYTIC MATERIAL FOR A REACTION TIME EFFECTIVE TO CONVERT A SUBSTANTIAL PROPORTION OF THE AMMONIA TO NITRIC ACID IN THE VAPOR STATE, CONTACTING THE VAPORS THUS PRODUCED IMMEDIATELY UPON FORMATION WITH AT LEAST ONE GASEOUS PARAFFIN HYDROCARBON AT A TEMPERATURE SLIGHTLY BELOW THE CRACKING TEMPERATURE OF SAID PARAFFIN HYDROCARBON TO FORM THE CORRESPONDING NITROSO-PARAFFIN AND IN AN AMOUNT IN EXCESS OF THAT REQUIRED TO EFFECT SUBSTANTIALLY COMPLETE CONSUMPTION OF NITRO ACID THUS FORMED, SUBJECTING SAID NITROSO-PARAFFIN TO FURTHER OXIDATION AT A REDUCED TEMPERATURE WITH AN ADDITIONAL QUANTITY OF SAID OXIDIZING GAS TO FORM THE CORRESPONDING NITRO-PARAFFIN, AND RECOVERING SAID NITRO-PARAFFIN.
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US2597027A true US2597027A (en) | 1952-05-20 |
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US2597027D Expired - Lifetime US2597027A (en) | Production of nitropauaffins |
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US3065270A (en) * | 1954-10-27 | 1962-11-20 | Olin Mathieson | Preparation of dimethylnitrosoamine |
US3480517A (en) * | 1968-08-26 | 1969-11-25 | Commercial Solvents Corp | Purification of nitroethane by azeotropic distillation with n-heptane or isooctane |
US3480518A (en) * | 1968-08-26 | 1969-11-25 | Commercial Solvents Corp | Separation of nitromethane and nitroethane by co-distilling with pentane |
US3480516A (en) * | 1968-08-26 | 1969-11-25 | Commercial Solvents Corp | Separation of nitroalkanes and alkanes by codistilling with methanol |
US4233249A (en) * | 1979-04-26 | 1980-11-11 | The United States Of America As Represented By The Secretary Of The Air Force | Method for the preparation of alkali metal salts of dinitromethane |
US4233250A (en) * | 1979-04-26 | 1980-11-11 | The United States Of America As Represented By The Secretary Of The Air Force | Process for synthesizing the alkali metal salts of dinetromethane |
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US1967667A (en) * | 1934-07-24 | Process of nitrating paraffin hydro | ||
US2109873A (en) * | 1938-03-01 | Process of nitrating hydrocarbons | ||
US2153065A (en) * | 1939-04-04 | Vapor phase nitration of the lower | ||
US2161475A (en) * | 1938-08-02 | 1939-06-06 | Hercules Powder Co Ltd | Process of nitrating methane |
US2288091A (en) * | 1940-08-02 | 1942-06-30 | Commerical Solvents Corp | Process for the recovery of nitric oxide from gaseous mixtures |
US2291345A (en) * | 1942-07-28 | Hydrocarbon nitration | ||
US2418241A (en) * | 1944-07-22 | 1947-04-01 | Commercial Solvents Corp | Process for vapor phase nitration of alkanes |
US2455425A (en) * | 1945-07-30 | 1948-12-07 | Ici Ltd | Production of nitroparaffins |
US2465984A (en) * | 1946-05-21 | 1949-03-29 | Union Oil Co | Production of cycloalkyl nitrites |
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US1967667A (en) * | 1934-07-24 | Process of nitrating paraffin hydro | ||
US2109873A (en) * | 1938-03-01 | Process of nitrating hydrocarbons | ||
US2153065A (en) * | 1939-04-04 | Vapor phase nitration of the lower | ||
US2291345A (en) * | 1942-07-28 | Hydrocarbon nitration | ||
US2161475A (en) * | 1938-08-02 | 1939-06-06 | Hercules Powder Co Ltd | Process of nitrating methane |
US2288091A (en) * | 1940-08-02 | 1942-06-30 | Commerical Solvents Corp | Process for the recovery of nitric oxide from gaseous mixtures |
US2418241A (en) * | 1944-07-22 | 1947-04-01 | Commercial Solvents Corp | Process for vapor phase nitration of alkanes |
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US3065270A (en) * | 1954-10-27 | 1962-11-20 | Olin Mathieson | Preparation of dimethylnitrosoamine |
US3480517A (en) * | 1968-08-26 | 1969-11-25 | Commercial Solvents Corp | Purification of nitroethane by azeotropic distillation with n-heptane or isooctane |
US3480518A (en) * | 1968-08-26 | 1969-11-25 | Commercial Solvents Corp | Separation of nitromethane and nitroethane by co-distilling with pentane |
US3480516A (en) * | 1968-08-26 | 1969-11-25 | Commercial Solvents Corp | Separation of nitroalkanes and alkanes by codistilling with methanol |
US4233249A (en) * | 1979-04-26 | 1980-11-11 | The United States Of America As Represented By The Secretary Of The Air Force | Method for the preparation of alkali metal salts of dinitromethane |
US4233250A (en) * | 1979-04-26 | 1980-11-11 | The United States Of America As Represented By The Secretary Of The Air Force | Process for synthesizing the alkali metal salts of dinetromethane |
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