US1967667A - Process of nitrating paraffin hydro - Google Patents

Process of nitrating paraffin hydro Download PDF

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US1967667A
US1967667A US1967667DA US1967667A US 1967667 A US1967667 A US 1967667A US 1967667D A US1967667D A US 1967667DA US 1967667 A US1967667 A US 1967667A
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isobutane
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carbon atoms
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    • 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
    • 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

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  • Our process may be used for the nitration of those saturated aliphatic hydrocarbons which have other carbon atoms than primary ones, and especially those which have tertiary carbon atoms. It is applicable to the nitration of aliphatic hydrocarbons having from 3 to 8 carbon atoms; but we have not attempted it with hydrocarbons having more than 8 carbon atoms, nor with such simple hydrocarbons as methane or ethane which have only primary carbon atoms.
  • Our process is especially applicable where there are tertiary carbon atoms, as in the iso-hydrocarbons, for the nitration by our process tends to occur principally on tertiary carbon atoms, and to a somewhat smaller extent on secondary carbon atoms, but to a relatively small extent on primary carbon atoms.
  • Our process is especially advantageous for the nitration of parafilns, such as propane,
  • n-butane iso-butane, the pentanes, the hexanes, 'the heptanes, and the octanes; but it-is also applicable with advantage to other saturated aliphatic hydrocarbons such for instance as the naphthenes (cycloparaflins).
  • Fig. 1 shows an apparatus for carrying out our process in batches
  • Fig. 2 is a sectional view of a water-cooled bomb which is especially suitable for the batch -method of Fig. 1
  • Fig. 3 shows an apparatus for carrying out our process continuously.
  • a reaction vessel or bomb 10 constructed of material which is resistant to dilute nitric acid, such for instance as Allegheny metal, and capable of withstanding highpressure, is filled W5 '0.
  • the isobutane may be supplied by a pump 11 from an isobutane storage tank 12, and the nitric acid from a nitric-acid storage reservoir 13 by way of a measuring tank 14, all suitably connected to the bomb by suitable valved piping 15 shown diagrammatically.
  • the bomb is then'closed, and gradually heated by a burner 16 until abundant reaction starts, which is at about 135-145 C. This temperature is above the critical temperature of isobutane, for such critical temperature is 134 C., but with some bydrocarbons abundant reaction starts below the critical temperature although with the reagents in the gas or vapor phase.
  • the reaction develops a pressure within the bomb of the order of 600 to 2400 pounds per square inch--the fuller the bomb the greater the pressure-; but in spite of the increased pressure, the hydrocarbon remains in the gas or vapor phase by the increase in temperature produced by the heat of the reaction, and the nitric acid is at least partly in vapor phase. Thus the reaction is practically wholly between gases or vapors.
  • the gases therefrom are released through the valved piping 15 into a scrubbing tower 19, and there scrubbed with some reagent which removes nitric-acid vapor from them, such as sodium carbonate.
  • the gases leaving the tower 19 are compressed by means of a compressor 20 and cooled by a condenser 21.
  • a sufficient pressure is produced to condense substantially all of the isobutane, which is removed from the gaseous reaction products in a separator 22.
  • the uncondensed gases are vented from a valve 23 on the separator 22, and the condensed isobutane is recycled or sent to storage. If desired the oxides of nitrogenmay be, converted to nitric acid in known manner.
  • Thetertiary nitrobutane may be recovered from the contents of reaction vessel 10 by the following procedure. Such contents are removed by piping 24 from the rzaction vessel or bomb 10 to a separating tank 25. The spent acid, which forms a lower layer, is removed from the separating tank 25 through a drain-valve 26. The crude tertiary nitrobutane which remains is transferred by piping 2'7 to a washing tank 28; where it is agitated with concentrated sodium hydroxide to dissolve any primary nitrobutane, and the alkali is allowed to settle and is drawn off. The tertiary nitrobutane is then further purified by rectification. If desired it may be still further purified by crystallization.
  • the tertiary nitrobutane thus obtained boils at about 126.4 C., corrected. It is of very high purity; for it melts at about 25 to 26 C., usually about 255 C., instead of at the 24 C. which the literature gives for the melting point of tertiary nitrobutane.
  • the tertiary nitrobutane produced by our process is not lachrymatory, as is the tertiary nitrobutane described inthe literature (Berichte 26, 129, 1893); and it has no peppermint odor, as has an uncrys'tallizable substance reported as tertiary nitrobutane by Tscherniak Liebigs Annalen der Chemie, 180, 155), but has an odor somewhat similar to that of nitromethane but rather milder.
  • Isobutane at atmospheric pressure is supplied through a pipe 29 and vaporizer 30 and bubbled through hot concentrated nitric acid in a suitable container 31.
  • the mixture of isobutane and nitric acid vapor passes from the container 31 by a pipe 32 to a reaction tube 33 which is heated by burners 34 to a temperature of about 300 C. which is sufficiently high to keep both reagents in the gas, or vapor phase.
  • the supply of isobutane is desirably such that it takes about 15 "seconds to pass through the tube 33. The nitration occurs within about this time, to produce a mixture of which tertiary nitrobutane is a predominant constituent.
  • the mixed gases from the reaction tube 33 pass through a cooler 35, in which they are desirably cooled to atmospheric temperature or lower, and then to a separator 36 where the condensed nitrobutane and spent acid are removed from the uncondensed gases.
  • the crude tertiary nitrobutane is purified as in the previous example.
  • the remaining gases, mostly unreacted isobutane, oxides of nitrogen, and of carbon, pass out from the separator 36 by a pipe 39, and are mixed with air entering through inlet 40 and converted to nitric acid in known man-' ner in tower 43.
  • the gases leaving the top of tower 43 by way of pipe 44 are compressed by pump 45 and the isobutane condensed in a cooler 46.
  • the condensed isobutane is separated from uncondensed gases (nitrogen, oxides of carbon, etc.) in a separator 48.
  • the isobutane is recycled, while the uncondensed gases are vented through a valve 49.
  • the whole system of operation in the apparatus of Fig. 3 may be carried out under pressure, by supplying the-isobutane under pressure to the pipe 29 and otherwise maintaining the pressure.
  • an increase in yield may be obtained by:
  • air or oxygen may be mixed with the hydrocarbon, (such as isobutane,) in order to reoxidize the oxides of nitrogen to nitric acid; but if this is done, care must be taken to -avoid explosive proportions.
  • hydrocarbon such as isobutane
  • isobutane is used as an example only. Any of the other saturated aliphatic hydrocarbons. indicated above, having from 3 to 8 carbon atoms, may be used instead of isobutane as the starting hydrocarbon in either the batch process or the continuous process.
  • a composition of matter consisting of tertiary nitrobutane which is in crystalline form below 25 C., has a melting point between 25 C. and 26 C., and which is substantially free from lachrymatory eflects.
  • a composition of matter consisting of tertiary nitrobutane which is in crystalline form below 25 C., has a melting point of substantially 25.5 C., and which is substantially free from lachrymatory efiects.
  • composition of matter consisting of tertiary nitrobutane in solid form free from lachrymatory efiects.

Description

July 24, 1934;
H. B. HASS ET AL PROCESS OF NITRATING PARAFFIN HYDROCARBONSAND PRODUCT THEREOF 2 Sheets-Sheet 1 Filed Oct. 4. 1933 y 1934- H. B. HASS r AL PROCESS OF NITRATING PARAFFIN HYDROCARBONS AND PRODUCT THEREOF Filed Oct. 4, 1933 2 Sheets-Sheet 2 Patented July 24, 1934 UNITED STATES PROCESS OF NITRATING PARAFFIN HYDRO- CARBONS AND PRODUCT THEREOF Henry B. Hess and Edward B. Hodge, West and Lafayette, Ind., Chicago Heights,
Byro n M. Vanderbilt, assignors to Purdue Research Foundation, West Lafayette, Ind., a
corporation of Indiana Application October 4, 1933, Serial No. 692,140
16 Claims. (01. 2s0 144) It is the object of our invention to eflect the nitration of saturated aliphatic hydrocarbons which contain other than primary carbon atoms; and more especially to effect the nitration of parafiin hydrocarbons having from 3 to 8 carbon atoms.
On account of the great abundance of saturated aliphatic hydrocarbons, especially of parafiln hydrocarbons such as occur in petroleum and in natural gas, extensive and intensive study has been made of the relatively few chemical reactions which they will undergo. Among such reactions is nitration.
Nitration of these hydrocarbons, howevenhas not hitherto resulted in any successful commercial application, so far as we know. In fact, in his book entitled Petroleum and its Products, (McGraw-Hill, 1928, page 60,) Gruse says that The nitration of petroleum fractions has been studied to some extent but no results of either scientific or technical importance have been obtained because of the mixed nature of the fractions and the complexity of the reactions.
In most if not all of the previous work on nitration of these saturated aliphatic hydrocarbons, the same general technique has been used as that which has been successful with aromatic hydrocarbons-that is, a liquid-phase reaction, and relatively low reaction-temperatures. In the course of that previous work it was learned that in many respects the nitration of aliphatic hydrocarbons was not strictly analogous to the nitration of aromatic hydrocarbons, as, for instance, that more dilute nitric acid should be employed with paraffins than with aromatics; and that it is inadvisable to use sulphuric acid to aid the reaction in attempting to nitrate parafiins, although sulphuric acid helps the reaction in nitrating aromatics. Nevertheless, investigators continued to adhere to the same general method, of attempting to cause a reaction between nitrict acid and the various paraflln hydrocarbons with both reagents in the liquid phase.
We have discovered that the reason for the uniformly negative and indiiferent results previously obtained has been that the reagents were in the liquid phase, and at low temperatures. Nitric acid and the parafiin hydrocarbons are not soluble in each other to any considerable extent. The nitrated product, however, is much more soluble in nitric acid than is the hydrocarbon from which it is derived. Because of this situation, the initial nitration reaction occurs slowly, but the more soluble nitrated product is more readily attacked by the nitric acid, so that the principal ultimate products are oxides of nitrogen, water, and carbon dioxide. Attempts have been made to increase the mutual solubility of the original reagents by using some mutual solvent in addition; and the most advantageous mutual solvent so far discovered is acetic acid. But the choice of a mutual solvent is greatly limited by the nature of nitric acid, which under the reaction conditions attacks almost all organic compounds. Even acetic acid is oxidized by nitric acid within the temperature range employed by us for the nitration of parafi'in hydrocarbons, and we have also found that the presence of acetic acid seems to favor oxidation of the 'hydrocarbon rather than nitration.
We have discovered that these difiiculties may be avoided by departing from the old procedure, of trying to obtain a reaction between two immiscible liquids; and producing the reaction with both the nitric acid in part and the saturated aliphatic hydrocarbon in the vapor or gaseous. phase, by using such temperatures and pressures as are necessary to produce this. Since all vapors and gases are miscible with one another in all proportions, the maintenance of the vapor or gaseous phase produces eifective mixing; and in consequence causes the reaction to be rapid, and makes it possible to secure relatively good yields of the nitro-aliphatic compounds, such as nitroparaflins.
Therefore, according to our invention, we operate under conditions in which both of the reagents are in the vapor or gaseous phase; and desirably operate under considerable pressure, and above the critical temperature of the hydrocarbon reagent.
Our process may be used for the nitration of those saturated aliphatic hydrocarbons which have other carbon atoms than primary ones, and especially those which have tertiary carbon atoms. It is applicable to the nitration of aliphatic hydrocarbons having from 3 to 8 carbon atoms; but we have not attempted it with hydrocarbons having more than 8 carbon atoms, nor with such simple hydrocarbons as methane or ethane which have only primary carbon atoms. Our process is especially applicable where there are tertiary carbon atoms, as in the iso-hydrocarbons, for the nitration by our process tends to occur principally on tertiary carbon atoms, and to a somewhat smaller extent on secondary carbon atoms, but to a relatively small extent on primary carbon atoms. Our process is especially advantageous for the nitration of parafilns, such as propane,
iii
n-butane, iso-butane, the pentanes, the hexanes, 'the heptanes, and the octanes; but it-is also applicable with advantage to other saturated aliphatic hydrocarbons such for instance as the naphthenes (cycloparaflins).
We have gotten our best results with iso-parafilns, by nitration of the tertiary .carbon atoms. An excellent example of this is isobutane, which has one tertiary carbon atom and three primary carbon atoms, with the general formula:
When this is nitrated, one of the principal products is tertiary nitrobutane, with the following formula:
Small amounts of primary intro-isobutane are also produced; and some carbon dioxide and some water; and also a solid which has not been identified but which'is probably 1,2-dinitro isobutane.
In nitrating these saturated aliphatic hydrocarbons which have secondary and/or tertiary carbon atoms, and of which isobutane is taken as an example, we may carry out the process either in batches or in continuous process. In using isobutane as an example, we do so with no intent to limit the invention; for it is applicable without change to other hydrocarbons of the class mentioned, such for instance as n-butane, propane, etc., as already noted.
The apparatus for doing this is illustrated in the accompanying drawings. Fig. 1 shows an apparatus for carrying out our process in batches; Fig. 2 is a sectional view of a water-cooled bomb which is especially suitable for the batch -method of Fig. 1; and Fig. 3 shows an apparatus for carrying out our process continuously.
In the batch process, we may proceed as follows:
A reaction vessel or bomb 10, constructed of material which is resistant to dilute nitric acid, such for instance as Allegheny metal, and capable of withstanding highpressure, is filled W5 '0. mixture of liquid isobutane and dilu e nitric acid one mole of nitric acid to two moles of isobutane. We prefer to make'the mixture within the bomb by putting in 35% nitric acid in sufiicient amount to give the desired molar proportion to the isobutane used and then run in the isobutane in sufilcient 'quantity to fill the bomb to the extent of 5-20%. The isobutane may be supplied by a pump 11 from an isobutane storage tank 12, and the nitric acid from a nitric-acid storage reservoir 13 by way of a measuring tank 14, all suitably connected to the bomb by suitable valved piping 15 shown diagrammatically. The bomb is then'closed, and gradually heated by a burner 16 until abundant reaction starts, which is at about 135-145 C. This temperature is above the critical temperature of isobutane, for such critical temperature is 134 C., but with some bydrocarbons abundant reaction starts below the critical temperature although with the reagents in the gas or vapor phase. The reaction develops a pressure within the bomb of the order of 600 to 2400 pounds per square inch--the fuller the bomb the greater the pressure-; but in spite of the increased pressure, the hydrocarbon remains in the gas or vapor phase by the increase in temperature produced by the heat of the reaction, and the nitric acid is at least partly in vapor phase. Thus the reaction is practically wholly between gases or vapors.
As the reaction is exothermic, it tends to become very violent once it has started, and hence we provide means for cooling the bomb, as by circulating water through an outside jacket 1'7 with which it is provided as shown in Fig. 2.
' When the reaction has substantially ceased, by the using up of the nitric acid, the pressure substantially stops rising and the bomb is cooled to room temperature. We prefer to have a suitable manometer 18 connected with the bomb, for indicating the pressure within it.
When the bomb has been cooled to room temperature, and the pressure sufficiently lowered, the gases therefrom are released through the valved piping 15 into a scrubbing tower 19, and there scrubbed with some reagent which removes nitric-acid vapor from them, such as sodium carbonate. The gases leaving the tower 19 are compressed by means of a compressor 20 and cooled by a condenser 21. A sufficient pressure is produced to condense substantially all of the isobutane, which is removed from the gaseous reaction products in a separator 22. The uncondensed gases are vented from a valve 23 on the separator 22, and the condensed isobutane is recycled or sent to storage. If desired the oxides of nitrogenmay be, converted to nitric acid in known manner.
Thetertiary nitrobutane may be recovered from the contents of reaction vessel 10 by the following procedure. Such contents are removed by piping 24 from the rzaction vessel or bomb 10 to a separating tank 25. The spent acid, which forms a lower layer, is removed from the separating tank 25 through a drain-valve 26. The crude tertiary nitrobutane which remains is transferred by piping 2'7 to a washing tank 28; where it is agitated with concentrated sodium hydroxide to dissolve any primary nitrobutane, and the alkali is allowed to settle and is drawn off. The tertiary nitrobutane is then further purified by rectification. If desired it may be still further purified by crystallization.
(In case the starting hydrocarbon is such that a secondary nitroparaffin is produced, agitation with sodium hydroxide is not a suitable procedure, since both primary and secondary nitroparaflins are alkali-soluble. In this case a sodium carbonate solution is used to remove traces of nitric acid prior to rectification.)
The tertiary nitrobutane thus obtained boils at about 126.4 C., corrected. It is of very high purity; for it melts at about 25 to 26 C., usually about 255 C., instead of at the 24 C. which the literature gives for the melting point of tertiary nitrobutane. The tertiary nitrobutane produced by our process is not lachrymatory, as is the tertiary nitrobutane described inthe literature (Berichte 26, 129, 1893); and it has no peppermint odor, as has an uncrys'tallizable substance reported as tertiary nitrobutane by Tscherniak Liebigs Annalen der Chemie, 180, 155), but has an odor somewhat similar to that of nitromethane but rather milder.
In the continuous process, we may use various kinds of apparatus, of which that shown in Fig. 3 is an example. Here again we describe the process in connection with isobutane.
Isobutane at atmospheric pressure is supplied through a pipe 29 and vaporizer 30 and bubbled through hot concentrated nitric acid in a suitable container 31. The mixture of isobutane and nitric acid vapor passes from the container 31 by a pipe 32 to a reaction tube 33 which is heated by burners 34 to a temperature of about 300 C. which is sufficiently high to keep both reagents in the gas, or vapor phase. The supply of isobutane is desirably such that it takes about 15 "seconds to pass through the tube 33. The nitration occurs within about this time, to produce a mixture of which tertiary nitrobutane is a predominant constituent. The mixed gases from the reaction tube 33 pass through a cooler 35, in which they are desirably cooled to atmospheric temperature or lower, and then to a separator 36 where the condensed nitrobutane and spent acid are removed from the uncondensed gases. The crude tertiary nitrobutane is purified as in the previous example. The remaining gases, mostly unreacted isobutane, oxides of nitrogen, and of carbon, pass out from the separator 36 by a pipe 39, and are mixed with air entering through inlet 40 and converted to nitric acid in known man-' ner in tower 43.
The gases leaving the top of tower 43 by way of pipe 44 are compressed by pump 45 and the isobutane condensed in a cooler 46. The condensed isobutane is separated from uncondensed gases (nitrogen, oxides of carbon, etc.) in a separator 48. The isobutane is recycled, while the uncondensed gases are vented through a valve 49.
If desired, the whole system of operation in the apparatus of Fig. 3 may be carried out under pressure, by supplying the-isobutane under pressure to the pipe 29 and otherwise maintaining the pressure.
In either the batch method or the continuous method, an increase in yield may be obtained by:
1. Increasing the pressure at which the reaction is carried out.
2. Increasing the excess of the hydrocarbon over the nitric acid.
3. The use of more dilute nitric acid.
If desired, air or oxygen may be mixed with the hydrocarbon, (such as isobutane,) in order to reoxidize the oxides of nitrogen to nitric acid; but if this is done, care must be taken to -avoid explosive proportions.
In both examples isobutane is used as an example only. Any of the other saturated aliphatic hydrocarbons. indicated above, having from 3 to 8 carbon atoms, may be used instead of isobutane as the starting hydrocarbon in either the batch process or the continuous process.
We claim as our invention:
l. The process of nitrating a saturated aliphatic hydrocarbon having from 3 to 8 carbon atoms inclusive, which consists in producing contact between such saturated aliphatic hydrocarbon and nitric acid with both reagents in the bon and the vapor formed by heating nitric acid at a temperature higher than the critical temperature of said saturated aliphatic hydrocarbon.
4. The process of nitrating a paraffin hydrocarbon having from 3 to 8 carbon atoms inclusive, which consists in producing contact between such paraffin hydrocarbon and nitric acid with both reagents in the gas or vapor phase.
a 5. The process of nitrating a paraifin hydrocarbon having from 3 to 8 carbon atoms inclusive, which consists in producing contact between such paraffin hydrocarbon and nitric acid at a temperature higher than the critical temperature of said paraflin hydrocarbon.
6. The process of nitrating isobutane, which consists in producing contact between such isobutane and nitric acid with both reagents in the gas or vapor phase.
7. The process of nitrating isobutane, which consists in producing contact between 'such isobutane and nitric acid at a temperature higher than the critical temperature of isobutane.
8. The process of nitrating n-butane, which consists in producing contact between such nbutane and nitric acid with both reagents in the gas or vapor phase.
9. The process of nitrating n-butane, which consists in producing contact between such nbutane and nitric acid at a temperature higher than the critical temperature of n-butane.
10. The process of nitrating propane, which consists in producing contact between such propane and nitric acid with both reagents in the gas or vapor phase.
11. The process of nitrating propane, which consists in producing contact between such propane and nitric acid at a temperature higher than the critical temperature of propane.
12. Ihe process of nitrating a saturated aliphatic hydrocarbon having from 3 to 3 carbon atoms inclusive, which consists in producing contact between such saturated aliphatic hydrocarbon and nitric acid with both reagents in the gas or vapor phase and at a pressure materially elevated above atmospheric pressure.
13. The process of nitrating a saturated aliphatic hydrocarbon having from 3 to 8 carbon atoms inclusive, which consists in producing contact between such saturated aliphatic hydrocarbon and nitric acid in the presence of free oxygen in excess of. that formed by the decomposition of the nitric acid, with the reagents in the gas or vapor phase.
14. A composition of matter, consisting of tertiary nitrobutane which is in crystalline form below 25 C., has a melting point between 25 C. and 26 C., and which is substantially free from lachrymatory eflects.
15. A" composition of matter, consisting of tertiary nitrobutane which is in crystalline form below 25 C., has a melting point of substantially 25.5 C., and which is substantially free from lachrymatory efiects.
16. A composition of matter, consisting of tertiary nitrobutane in solid form free from lachrymatory efiects.
HENRY B. HASS. EDWARD B. HODGE. BYRON M. VANDERBILT.
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Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2420938A (en) * 1944-04-10 1947-05-20 Union Oil Co Nitric acid as selective solvent in oxidation of naphthenes
US2455425A (en) * 1945-07-30 1948-12-07 Ici Ltd Production of nitroparaffins
US2489320A (en) * 1949-11-29 Nitration of paraffins
US2511454A (en) * 1950-06-13 Nitration of paraffins
US2597027A (en) * 1952-05-20 Production of nitropauaffins
US2609401A (en) * 1952-09-02 Nitration of saturated aliphatic
DE902374C (en) * 1944-03-16 1954-01-21 Ruhrchemie Ag Process for the preparation of nitro compounds
US2886602A (en) * 1955-10-14 1959-05-12 Collier Carbon & Chemical Co Preparation of nitro-tert-butyl alcohol and nitro-isobutene
US3090786A (en) * 1954-11-05 1963-05-21 Hercules Powder Co Ltd Preparation of nitrosamines
US3093640A (en) * 1963-06-11 Jnotxjh ao sisaiohiin
US3133123A (en) * 1961-02-16 1964-05-12 Allied Chem Vapor phase nitration of cyclohexane
US4313009A (en) * 1979-04-10 1982-01-26 Societe Chimique De La Grande Paroisse, Azote Et Produits Chimiques Process and installation for making nitroparaffins by nitration of hydrocarbons in the gaseous phase
US20110028731A1 (en) * 2008-04-16 2011-02-03 Trauth Daniel M Process for the manufacture of nitropropanes
US20110028732A1 (en) * 2008-04-16 2011-02-03 Angus Chemical Company Nitrated hydrocarbons, derivatives, and processes for their manufacture
US20110092749A1 (en) * 2009-10-20 2011-04-21 Dow Global Technologies Inc. Process For Downstream Recovery Of Nitroalkane Using Dividing Wall Column
US20110092737A1 (en) * 2009-10-20 2011-04-21 Angus Chemical Company Isothermal reactor for hydrocarbon nitration
US20110092750A1 (en) * 2009-10-20 2011-04-21 Trauth Daniel M Process for the manufacture of nitrated hydrocarbons
US20110092748A1 (en) * 2009-10-20 2011-04-21 Dow Global Technologies Inc. Process For Nitroalkane Recovery By Aqueous Phase Recycle To Nitration Reactor
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Cited By (37)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3093640A (en) * 1963-06-11 Jnotxjh ao sisaiohiin
US2489320A (en) * 1949-11-29 Nitration of paraffins
US2511454A (en) * 1950-06-13 Nitration of paraffins
US2597027A (en) * 1952-05-20 Production of nitropauaffins
US2609401A (en) * 1952-09-02 Nitration of saturated aliphatic
DE902374C (en) * 1944-03-16 1954-01-21 Ruhrchemie Ag Process for the preparation of nitro compounds
US2420938A (en) * 1944-04-10 1947-05-20 Union Oil Co Nitric acid as selective solvent in oxidation of naphthenes
US2455425A (en) * 1945-07-30 1948-12-07 Ici Ltd Production of nitroparaffins
US3090786A (en) * 1954-11-05 1963-05-21 Hercules Powder Co Ltd Preparation of nitrosamines
US2886602A (en) * 1955-10-14 1959-05-12 Collier Carbon & Chemical Co Preparation of nitro-tert-butyl alcohol and nitro-isobutene
US3133123A (en) * 1961-02-16 1964-05-12 Allied Chem Vapor phase nitration of cyclohexane
US4313009A (en) * 1979-04-10 1982-01-26 Societe Chimique De La Grande Paroisse, Azote Et Produits Chimiques Process and installation for making nitroparaffins by nitration of hydrocarbons in the gaseous phase
US11542277B2 (en) 2008-04-16 2023-01-03 Angus Chemical Company Nitrated hydrocarbons, derivatives, and processes for their manufacture
US20110028731A1 (en) * 2008-04-16 2011-02-03 Trauth Daniel M Process for the manufacture of nitropropanes
US20110028732A1 (en) * 2008-04-16 2011-02-03 Angus Chemical Company Nitrated hydrocarbons, derivatives, and processes for their manufacture
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US8519199B2 (en) 2008-04-16 2013-08-27 Angus Chemical Company Process for the manufacture of nitropropanes
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US10377771B2 (en) 2008-04-16 2019-08-13 Angus Chemical Company Nitrated hydrocarbons, derivatives, and processes for their manufacture
US20110092749A1 (en) * 2009-10-20 2011-04-21 Dow Global Technologies Inc. Process For Downstream Recovery Of Nitroalkane Using Dividing Wall Column
US20110092748A1 (en) * 2009-10-20 2011-04-21 Dow Global Technologies Inc. Process For Nitroalkane Recovery By Aqueous Phase Recycle To Nitration Reactor
US8324435B2 (en) 2009-10-20 2012-12-04 Angus Chemical Company Process for the manufacture of nitrated hydrocarbons
JP2013508365A (en) * 2009-10-20 2013-03-07 ダウ グローバル テクノロジーズ エルエルシー Nitroalkane recovery by recycling aqueous phase to nitration reactor
JP2013508363A (en) * 2009-10-20 2013-03-07 ダウ グローバル テクノロジーズ エルエルシー Downstream recovery of nitroalkanes using a dividing wall column
US8410323B2 (en) 2009-10-20 2013-04-02 Dow Global Technologies Llc Process for downstream recovery of nitroalkane using dividing wall column
US8415514B2 (en) 2009-10-20 2013-04-09 Angus Chemical Company Isothermal reactor for hydrocarbon nitration
US8431754B2 (en) 2009-10-20 2013-04-30 Dow Global Technologies Llc Process for nitroalkane recovery by aqueous phase recycle to nitration reactor
US20110092750A1 (en) * 2009-10-20 2011-04-21 Trauth Daniel M Process for the manufacture of nitrated hydrocarbons
US20110092737A1 (en) * 2009-10-20 2011-04-21 Angus Chemical Company Isothermal reactor for hydrocarbon nitration
US9340486B2 (en) 2009-10-20 2016-05-17 Angus Chemical Company Process for nitroalkane recovery by aqueous phase recycle to nitration reactor
WO2011078931A1 (en) * 2009-12-24 2011-06-30 Dow Global Technologies Llc Hydrocarbon feed flexible high pressure nitration plant design
CN102741217B (en) * 2009-12-24 2015-04-15 陶氏环球技术有限责任公司 Hydrocarbon feed flexible high pressure nitration plant design
US8558039B2 (en) 2009-12-24 2013-10-15 Dow Global Technologies Llc Hydrocarbon feed flexible high pressure nitration plant design
US9504933B2 (en) 2009-12-24 2016-11-29 Angus Chemical Company Hydrocarbon feed flexible high pressure nitration plant design
JP2013515722A (en) * 2009-12-24 2013-05-09 ダウ グローバル テクノロジーズ エルエルシー Hydrocarbon feed flexible high pressure nitration plant design.
CN102741217A (en) * 2009-12-24 2012-10-17 陶氏环球技术有限责任公司 Hydrocarbon feed flexible high pressure nitration plant design
US20110160496A1 (en) * 2009-12-24 2011-06-30 Dow Global Technologies Inc. Hydrocarbon feed flexible high pressure nitration plant design

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