# Patent

## Title
Extensible absorbent article including a release agent

## Abstract

A process for the production of propylene and ethylene by non-catalytic oxidative conversion of propane by allowing the endothermic hydrocarbon cracking reaction to occur simultaneously with the exothermic hydrocarbons oxidative conversion reactions in an empty tubular reactor is disclosed. The process comprises mixing of oxygen and propane at ambient temperatures, mixing of sulfur compound with steam, admixing the mixture of steam and sulfur compound and the mixture of oxygen and propane and preheating the resulting admixture, passing said mixture through an empty tubular reactor, cooling and separating the components of effluent product gases by known methods and recycling the unconverted reactants, if required.

## Background
This invention relates to a process for the production of propylene and ethylene by non-catalytic oxidative cracking of propane or propane-rich C.sub.2 -C.sub.4 paraffins. The invention particularly relates to production of propylene and ethylene by non-catalytic oxidative conversion of propane or propane-rich C.sub.2 -C.sub.4 paraffins in a most energy efficient manner by allowing the endothermic hydrocarbon cracking reactions to occur simultaneously with the exothermic hydrocarbons oxidative conversion reactions in an empty tubular reactor.

The process of this invention could be used for the production of propylene from propane or propane-rich C.sub.2 -C.sub.4 paraffins.

Propylene, an important feedstock in the petrochemical industry, is produced commercially along with ethylene by the thermal cracking of ethane, propane, ethane-propane mixture or naphtha in the presence of steam (ref. L. Kniel et al., in Chemical Industries, Vol. 2 "Ethylene: Key-stone to the Petrochemical Industry, Marcel Dekkor, Inc., New York, 1980 and L. F. Albright et al., eds., in Pyrolysis: Theory and Industrial Practice, Academic Press, New York, 1983). In the thermal cracking of these paraffins, ethylene is produced in larger quantities than propylene. The cracking process is highly endothermic and hence highly energy intensive and also involves extensive coke formation. Typical results given in the above references indicate that at 93% conversion of propane, 23.7 wt %, 41.4 wt % and 12.9 wt % yield for methane, ethylene and propylene, respectively, could be obtained by the thermal cracking of propane. The ethylene, propylene and also other olefins produced in the cracking process and the unreacted paraffins are separated from the product stream by the well-known cryogenic separation method involving liquefaction and fractionation of hydrocarbons.

The process for the production of propylene and ethylene, based on thermal cracking of propane or other paraffins have following limitations: (1) They are highly endothermic and hence require a large amount of energy for the cracking of paraffins. (2) They involve extensive coke deposition inside the pyrolysis reactor tubes, thus causing increase in pressure drop and hence there are frequent break-downs for removing the coke from the pyrolysis reactor tubes. (3) The life of the pyrolysis reactor tubes is low because of their high temperature operation; the temperature at external surface of the tubes is about 200.degree. C. higher than the temperature inside the tubes.

Catalytic processes based on oxidative dehydrogenation of propane for the productions of propylene area also known in the prior art. A number of catalysts are known for the oxidative dehydrogenation of propane [ref. JP 58,153,538 (matushi Electric Ind. Co. Ltd.), 1983; U.S. Pat. No. 4,472,314, Conner et al., 1984; U.S. Pat. No. 4,547,618 (Mobil Oil Corp.), Porbus and Nancy, 1985; U.S. Pat. No. 4,607,129 (Phillips Petroleum Col.), Lee and Fu, 1985; U.S. Pat. No. 4,886,928, Imai and Schmidt, 1989; U.S. Pat. No. 5,306,858, Salem et al., 1994; JP 08,231,441, Saito et al., 1996 and DE 19,530,454, Baerns et al., 1997]. In the catalytic oxidative propane dehydrogenation processes, the catalyst is deactivated during the process due to the loss of active components from the catalyst by evaporation at hot spots and/or due to the catalyst sintering. The catalysts are also deactivated due to coke deposition on their surface during the process. Moreover, since these processes are highly exothermic, their operation is hazardous.

The present energy crisis and/or high energy cost, and also the environmental pollution problems have created a great need for developing a process for the production of propylene, the demand of which is increasing day-by-day, by non-catalytic oxidative cracking of propane or propane-rich C.sub.2 -C.sub.4 paraffins to propylene and ethylene with high propylene/ethylene mole ratio, which requires little (i.e. much smaller than that required for the thermal cracking process) or no external energy, operates in a most energy efficient manner and with high conversion, selectivity and productivity but without coke formation and also has absolutely no hazards (i.e. very safe operation). This invention is, therefore, made with the following objects so that most of the drawbacks or limitations of the earlier processes could be overcome.

1. Accordingly the main object of this invention is to provide process for the production of propylene and ethylene, with propylene/ethylene mole ratio of at least 0.15, from propane or propane-rich C.sub.2 -C.sub.4 paraffins by non-catalytic oxidative cracking of propane or propane-rich C.sub.2 -C.sub.4 paraffins in the presence of steam, volatile sulfur compound and limited oxygen so that the endothermic thermal cracking and exothermic oxidative conversion reactions of propane, described later, occur simultaneously.

2. Another important object of this invention is to provide a non-catalytic process for the production of propylene and ethylene, with propylene/ethylene mole ratio of at least 0.15, from propane or propane-rich C.sub.2 -C.sub.4 paraffins, which requires little (i.e. much smaller than that required for the thermal cracking process) or no external energy and also operates in a most energy efficient manner without any hazards (i.e. with a very safe process operation) through coupling of the exothermic oxidative hydrocarbon conversion reactions with the endothermic hydrocarbon cracking or pyrolysis reactions.

3. Yet another object of this invention is to be provide process for the production of propylene and ethylene, with propylene/ethylene mole ratio of at least 0.15, from propane or propane-rich C.sub.2 -C.sub.4 paraffins by their simultaneous oxidative conversion and thermal cracking, which operates with high conversion, selectivity and productivity without deposition of coke on the reactor walls.

This invention provides a non-catalytic process for the production of propylene and ethylene, with propylene/ethylene mole ratio of at least 0.15, by oxidative cracking of propane or propane-rich C.sub.2 -C.sub.4 paraffins with high conversion, selectivity and productivity, operating in most energy efficient and safe manner, in an empty tubular reactor. The process comprises of passing continuously a gaseous feed, comprising of propane or propane-rich C.sub.2 -C.sub.4 paraffins, oxygen, steam, and volatile sulfur compound, preheated at 200.degree.-550.degree. C. through an empty tubular reactor at the temperature of 550.degree.-900.degree. C., pressure 0.5-5 atm, space velocity 500-50,000 h.sup.-1 and mole ratios of O.sub.2 /hydrocarbon, steam/hydrocarbon and sulfur compound/hydrocarbon in the feed 0.01-1.0, 0.1-10 and 10.sup.-2 -10.sup.-6, respectively.

The main finding of this invention is that in the present process, the endothermic thermal cracking and exothermic oxidative hydrocarbon conversion reactions occur simultaneously and because of this there is a coupling of the exothermic and endothermic reactions and thereby the process operates in a most energy efficient manner and also without formation of hot spots in the reactor, making the process operation safe. Another important finding of this invention is that the present process requires a little or no external energy and it can be made thermoneutral or mildly exothermic or mildly endothermic by manipulating the process conditions. Yet another important finding of this invention is that the present process operates with high conversion, selectivity and productivity, producing propylene and ethylene with propylene/ethylene mole ratio of at least 0.15, and moreover there is no coke deposition on the reactor walls. Further one more important finding of this invention is that because of the addition of volatile sulfur compound in the feed, the propane conversion and/or selectivity for olefins is increased.

Accordingly, this invention provides a process for the production of propylene and ethylene by non-catalytic oxidative cracking of propane or propane-rich-C.sub.2 -C.sub.4 paraffins, which comprises: C.sub.2 -C.sub.4 paraffins at ambient temperature, mixture of oxygen or O.sub.2 -enriched air and propane or propane-rich C.sub.2 -C.sub.4 paraffins, and preheating the resulting admixture to a temperature between about 200.degree. C. to about 550.degree. C., tubular reactor, while maintaining the mole ratio of oxygen to hydrocarbon, steam to hydrocarbon and volatile sulfur compound to hydrocarbon in said admixture feed between about 0.01 to about 1.0, between about 0.1 to about 10, and between about 10.sup.-2 to about 10.sup.-6, respectively, with a gas hourly space velocity of said admixture feed between about 500 h.sup.-1 to about 50,000 h.sup.-1 at a reaction temperature between about 620.degree. C. to about 900.degree. C. and a pressure between about 0.5 to about 5.0 atm, such that propylene to ethylene mole ratio in products is at least 0.15 and there is a coupling of exothermic hydrocarbon oxidative conversion and endothermic hydrocarbon cracking reactions due to the simultaneous occurrence of these exothermic and endothermic reactions, and methods and, it required, recycling the unconverted reactants.

In the process of the present invention, the preferred reaction temperature is between about 635.degree. C. and about 800.degree. C.; the preferred pressure ranges from about 1 atm to about 3 atm; the preferred mole ratio of O.sub.2 to hydrocarbon, steam to hydrocarbon and volatile sulfur compound to hydrocarbon in the feed ranges from about 0.05 to about 0.5, about 0.3 to about 3.0 and about 10.sup.-3 to about 10.sup.-5, respectively; and the preferred gas hourly space velocity of the feed ranges from about 1000 h.sup.-1 to about 20,000 h.sup.-1. The preferred volatile sulfur compound in the feed is thiophene.

In the process of the present invention, the products formed are propylene, ethylene, methane, ethane, hydrogen, carbon monoxide, carbon dioxide and water and C.sub.4+ hydrocarbons. The gaseous product stream comprises of ethylene, propylene, C.sub.4+ hydrocarbons, methane, ethane, H.sub.2, CO, CO.sub.2, H.sub.2 O and unconverted propane and oxygen or air components.

The feed used in the process of the present invention comprises of propane or propane-rich C.sub.2 -C.sub.4 paraffins, oxygen or O.sub.2 -enriched air, steam and volatile sulfur compound. The hydrocarbon components of the feed and oxygen are reactants but steam is a feed diluent and acts as an indirect reactant for the gasification of the carbon or coke formed in the process under oxygen deficient conditions or by thermal cracking or pyrolysis of hydrocarbons. The presence of steam in the feed has two beneficial effects: one, the formation of coke and tar-like product in the process are avoided and second, the severity of the exothermic hydrocarbon oxidation reactions is reduced due to the feed dilution. The steam in the product stream can be easily separated simply by its condensation. The oxygen in the feed plays following important roles in the process. Because of the presence of O.sub.2 in the feed, not only the total conversion of propane but also its conversion purely by its thermal cracking is much higher than that observed in the absence of O.sub.2. Further, because of the oxidation of coke precursors (i.e. hydrogen deficient or highly unsaturated hydrocarbon species formed in the conversion of the propane or propane-rich C.sub.2 -C.sub.4 paraffins) by the oxygen, the coke formation in the process of this invention is avoided. The volatile sulfur compound in the feed plays two significant roles: (1) its passivates the inner walls surface of the tubular reactor by deactivating the coke forming sites present on the reactor inner walls through sulfidation and (2) its presence in the feed causes a significant increase in the conversion and/or selectivity for olefins. The preheating of the feed gases can be effected by exchanging heat between the hot reactor effluent product gas stream and the feed gases by known prior art methods.

Following non-catalytic exothermic and endothermic reactions occur in the process of present invention.

Exothermic reactions

a) Oxidative dehydrogenation of propane or propane rich C.sub.2 -C.sub.4 paraffins: kcal.mol.sup.-1 (at 700.degree. C.)                       (1)

(when n=2-4)

b) Combustion of propane or propane rich C.sub.2 -C.sub.4 paraffins, which are highly exothermic reactions: kcal.mol.sup.-1 (at 700.degree. C.)                       (3) (at 700.degree. C.)                                       (4)

C) Oxidation of hydrogen to water, which is also highly exothermic:

Endothermic reactions

Thermal cracking or pyrolysis of propane or propane-rich C.sub.2 -C.sub.4 paraffins: 700.degree. C.)                                           (7) 700.degree. C.)                                           (8) C.sub.4+ hydrocarbons, CH.sub.4 and H.sub.2 -heat         (9)

In the process of the present invention, since the above exothermic and endothermic reactions are occurring simultaneously, the heat produced in the exothermic reactions is used instantly for the endothermic reactions, thus making the process operation most energy efficient and safe. Since the thermal hydrocarbon cracking reactions have high activation energy, their reaction rate increases very fast with the increase in the temperature. The coupling of the exothermic and endothermic reactions, as described above, leads to an establishment of a sort of a buffer action for the reaction temperature in the process thus restricting the temperature rise and, therefore, an occurrence of run-away reaction condition during the operation of the process is totally eliminated. Because of the coupling of the exothermic and endothermic reactions occurring simultaneously, the process of this invention can be made mildly exothermic, thermoneutral or mildly endothermic by manipulating the process conditions.

The process can be operated in an empty non-adiabatic tubular reactor, containing single or multiple parallel coiled tubes, without any serious problems for removing heat from the reactor, when the process is mildly exothermic or providing energy to the reactor, when the process is mildly endothermic, thus requiring no or little (i.e. much smaller than that required for the thermal cracking process) external energy, respectively.

The present invention is described with respect to the following examples illustrating the process of this invention for the simultaneous exothermic oxidative conversion of propane or propane-rich C.sub.2 -C.sub.4 paraffins and endothermic thermal cracking of propane or propane-rich C.sub.2 -C.sub.4 paraffins in a most safe and energy efficient manner. These examples are provided for illustrative purposes only and are not to be construed as limitations on the invention.

Definition of terms used in the examples

Total conversion of reactant (%)=percent of the reactant converted to all the products. Conversion of a reactant to a particular product=percent of the reactant converted to the particular product.

Selectivity for a particular product (%)=100.times.[Conversion of reactant to the product (%)]/[Total conversion of reactant (%)].

Gas: hourly space velocity, GHSV=Volume of gaseous reactant mixture, measured at 0.degree. C. and 1 atm pressure, passed through an unit volume of reactor per hour.

All the ratios of reactants or products are mole ratios.

The net heat of reactions, .DELTA.H.sub.r, in the overall process is defined as follows:

Net heat of reactions, .DELTA.H.sub.4 =[H.sub.f ].sub.products =[H.sub.f ].sub.reactants.

Wherein, [H.sub.f ].sub.products and [H.sub.f ].sub.reactants are the heat of formation of products and reactants, respectively. The negative value of the net heat of reactions indicates that the overall process is exothermic and the positive value of the heat of reactions indicates that overall process is endothermic.

This example illustrates the process of this invention for the production of propylene and ethylene by non-catalytic oxidative cracking of propane in the presence of oxygen, steam and thiophene.

The process is carried out in a continuous flow empty tubular reactor having internal diameter of 7.0 mm and a volume of 5.2 cm.sup.3, by mixing oxygen with propane at room temperature, mixing thiophene vapors with steam, admixing the steam-thiophene mixture and oxygen-propane mixture, preheating the admixture and then passing continuously the preheated admixture through the reactor at the reaction conditions given below. The reactor was kept in an electrically heated tubular furnace. The reaction temperature was measured by a Chromel-Alumel thermocouple located axially in the center of the reactor. The reactor effluent gases were quenched and cooled at about 0.degree. C. to condense the water from them, using a coiled condenser immersed in ice-water slurry, and then analyzed for the products and unconverted reactants by an on-line gas chromatograph.

Reaction conditions Feed               A mixture of propane, oxygen, steam and thiophene Feed preheating temperature 500.degree. C. O.sub.2 /propane mole ratio in feed 0.25 H.sub.2 O/hydrocarbon mole ratio in feed 0.5 Thiophene/propane mole ratio feed 10.sup.-4 Gas hourly space velocity (GHSV) 3000 h.sup.-1 Pressure 1.1 atm. Reaction temperature 800.degree. C. The results obtained at the above reaction conditions are as follows. No coke deposition is observed in the process. Conversion of propane (%) 79.1 Conversion of oxygen (%) 93.5 Selectivity (%) for Propylene          21.8 Ethylene 42.4 Methane 19.6 Ethane 2.3 C.sub.4+ hydrocarbons 5.6 Carbon monoxide 7.5 Carbon dioxide 0.8 C.sub.3 H.sub.6 /C.sub.2 H.sub.4 ratio in products 0.34 Net heat of reaction (.DELTA.H.sub.r) (kcal.mol.sup.-1) -11.6 ______________________________________

The net heat of reaction is small with --ve sign, indicating that the overall process is mildly exothermic. It also indicates that no external energy is required for the process.

These examples illustrate the process of the present invention for the production of propylene and ethylene by non-catalytic oxidative cracking of propane in the presence of oxygen, steam and different volatile sulfur compounds at different process conditions. The process is carried out in the reactor and by the procedure same as that described in Example 1. The process performance was evaluated at following process conditions. Feed                A mixtures of propane, oxygen, steam and volatile sulfur compound Volatile sulfur compound Thiophene, CS.sub.2 or dimethyl sulfide (DMS) Feed preheating temperature 300.degree. or 500.degree. C. O.sub.2 /propane mole ratio in feed varied from 0.06 to 0.5 Steam/propane mole ratio in feed varied from 0.4 to 2.5 Sulfur compound/propane mole varied form 10.sup.-3 to 10.sup.-5 ratio in feed Gas hourly space velocity (GHSV) varied from 1170 to 7150 h.sup.-1 Pressure 0.95-1.1 atm Reaction temperature varied from 600.degree.-800.degree. C. ______________________________________

The results obtained at different process conditions are given in Tables 1-6. There was no coke deposition on the reactor walls.

This example also illustrates that the net heat of reactions in the process of this invention is quite small; it is with positive or negative sign, indicating that the process at the corresponding reaction conditions is mildly endothermic or mildly exothermic, respectively. This example also illustrates that the process of this invention occurs in a most energy efficient and safe manner and also the process can be made mildly exothermic, near thermoneutral or mildly endothermic by manipulating the process conditions, particularly the reaction temperature and the O.sub.2 /hydrocarbon mole ratio in the feed. This example further illustrates that for the process of present invention, either there is no requirement of external energy, particularly when the net heat of reaction, .DELTA.H.sub.r is negative (i.e. when the present process is mildly exothermic) or there is a requirement of much lower energy than that required for the thermal cracking of propane: C.sub.1 H.sub.x .fwdarw.C.sub.3 H.sub.6 +H.sub.2, which is highly endothermic with a heat of radiation, .DELTA.H.sub.4 =+39.93 kcal.mol.sup.-1 (at 727.degree. C.). The external energy required in the process of process invention is much lower than that required for the propane thermal cracking process and hence there is a large energy saving.

This example illustrates that in the presence of limited O.sub.2 in the feed of the process of present invention, not only the total conversion of propane but also the conversion of propane purely by its thermal cracking is much higher than that observed in the absence of O.sub.2. The propane conversion reactions in the presence of O.sub.2 and in the absence of O.sub.2 were carried out in the reactor and by the procedure similar to that described in Example 1. Results showing the influence of the presence of O.sub.2 in feed at different concentrations (O.sub.2 /C.sub.3 H.sub.8 mole ratio=0-0.5) on the total conversion of propane and its conversion purely by thermal cracking at different temperatures (635.degree.-800.degree. C.) are presented in Table 7. Because of the presence of O.sub.2, not only the total conversion of propane but also its conversion purely by thermal cracking is much higher that that observed in the absence of O.sub.2. Both the total conversion of propane and its conversion by thermal cracking alone are increased markedly with increasing the concentration of O.sub.2 relative to propane at all the temperatures. ______________________________________ Results of the oxycracking of propane at different temperatures Example 2 Example 3 Example 4 Example 5 ______________________________________ Process conditions Reaction temp. (.degree.C.) 620 635 715 810 O.sub.2 /C.sub.3 H.sub.8 mole ratio 0.5 0.5 0.5 0.5 Steam/C.sub.3 H.sub.8 mole ratio 0.5 0.5 0.5 0.5 Thiophene/C.sub.3 H.sub.8 mole 10.sup.-4 10.sup.-4 10.sup.-4 10.sup.31 4 ratio GHSV (h.sup.-1) 3000 3000 3000 3000 Pressure (atm) 0.95 0.95 0.95 0.95 Feed preheating 500 500 500 500 temp. (.degree.C.) Conversion (%) of Propane 12.5 72.0 79.4 91.7 Oxygen 14.0 86.8 93.8 97.9 Selectivity (%) for Propylene 58.3 26.2 20.1 13.8 Ethylene 28.9 38.2 40.5 44.0 Methane 4.2 14.3 16.6 19.7 Ethane 2.9 2.8 2.3 2.3 C.sub.4+ hydrocarbons 5.5 5.1 5.5 4.7 Carbon monoxide 2.0 12.6 13.6 14.5 Carbon dioxide 0.9 0.7 0.9 1.1 C.sub.3 H.sub.6 C.sub.2 H.sub.4 mole 1.35 0.46 0.33 0.21 ratio in products Net heat of reaction  -33.5 -33.4 -32.7 -27.5 .DELTA.H.sub.r (kcal.mol.sup.-1) ______________________________________ ______________________________________ Results of the oxycracking of propane at 800.degree. C. for different O.sub.2 /C.sub.3 H.sub.8 ratios Example 6 Example 7 Example 8 Example 9 ______________________________________ Process conditions Reaction temp. (.degree.C.) 800 800 800 800 O.sub.2 /C.sub.3 H.sub.8 0.0 0.5 0.13 0.06 mole ratio Steam/C.sub.3 H.sub.8 0.5 0.5 0.5 0.5 mole ratio Thiophene/C.sub.3 H.sub.8 10.sup.-4 10.sup.-4 10.sup.-4 10.sup.-4 mole ratio GHSV (h.sup.-1) 3000 3000 3000 3000 Pressure (atm) 1.0 1.1 1.0 1.1 Feed preheating 500 500 500 500 temp. (.degree.C.) Conversion (%) of Propane 53.9 91.7 68.6 61.8 Oxygen  97.9 95.4 94.8 Selectivity (%) for Propylene 29.3 13.3 25.4 27.2 Ethylene 41.9 44.0 42.2 42.1 Methane 20.4 19.7 19.7 19.7 Ethane 2.0 2.3 2.4 2.3 C.sub.4+ hydrocarbons 5.7 4.7 6.3 6.4 Carbon monoxide 0.5 14.5 3.4 1.8 Carbon dioxide 0.1 1.1 0.5 0.4 C.sub.3 H.sub.6 /C.sub.2 H.sub.4 0.47 0.21 0.40 0.43 mole ratio in products Net heat of reaction  -- -30.4 +9.4 +12.1 .DELTA.H.sub.r (kcal.mol.sup.-1) ______________________________________ ______________________________________ Results of the oxycracking of propane at 635.degree. C. for different O.sub.2 /C.sub.3 H.sub.8 ratios Example 10 Example 11 Example 12 ______________________________________ Process conditions Reaction temp. (.degree.C.) 635 635 635 O.sub.2 /C.sub.3 H.sub.8 mole ratio 0.0 0.25 0.10 Steam/C.sub.3 H.sub.8 mole ratio 0.5 0.5 0.5 Thiophene/C.sub.3 H.sub.8 mole ratio 10.sup.-4 10.sup.-4 10.sup.-4 QHSV (h.sup.-1) 3000 3000 3000 Pressure (atm) 1.0 1.0 1.0 Feed preheating temp. (.degree.C.) 300 300 300 Conversion (%) of Propane 0.8 47.8 22.8 Oxygen -- 91.9 94.1 Selectivity (%) for Propylene 1.0 31.5 30.7 Ethylene 65.9 36.7 38.7 Methane 33.1 13.3 15.1 Ethane -- 2.3 2:2 C.sub.4+ hydrocarbons -- 7.5 8.1 Carbon monoxide -- 8.3 4.6 Carbon dioxide -- 0.4 0.4 C.sub.3 H.sub.6 /C.sub.2 H.sub.4 mole ratio 0.01 0.58 0.53 in products ______________________________________ ______________________________________ Results of the oxycracking of propane at 635.degree. C. for different steam/C.sub.3 H.sub.8 ratios Example  Example  Example Example 13 14 15 16 ______________________________________ Process conditions Reaction temp. (.degree. C.) 635 635 635 635 O.sub.2 /C.sub.3 H.sub.8 0.5 0.5 0.5 0.5 mole ratio Steam/C.sub.3 H.sub.8 0.4 1.13 1.6 2.5 mole ratio Thiophene/C.sub.3 H.sub.8 10.sup.-4 10.sup.-4 10.sup.-4 10.sup.-4 mole ratio GHSV (h.sup.-1) 3000 3000 3000 3000 Pressure (atm) 1.0 1.0 1.0 0.95 Feed preheating 500 500 500 500 temp. (.degree.C.) Conversion (%) of Propane 70.8 74.8 73.1 62.7 Oxygen 91.1 90.1 86.5 79.6 Selectivity (%) for Propylene 24.9 25.4 28.1 28.9 Ethylene 38.3 38.0 35.5 36.4 Methane 14.0 14.0 12.3 11.7 Ethane 2.5 2.6 2.4 2.3 C.sub.4+ hydrocarbons 7.4 10.2 9.1 5.2 Carbon monoxide 12.3 13.0 12.1 14.7 Carbon dioxide 0.6 0.8 0.5 0.7 C.sub.3 H.sub.6 /C.sub.2 H.sub.4 0.44 0.45 0.53 0.53 mole ratio in products ______________________________________ ______________________________________ Results of thc oxycracking of propane at 635.degree. C. for different space velocities Example             17     18   19   20   21 ______________________________________ Process conditions Reaction temp. (.degree.C.) 635 635 635 635 635 O.sub.2 /C.sub.3 H.sub.8 mole ratio 0.5 0.5 0.5 0.5 0.5 Steam/C.sub.3 H.sub.8 mole ratio 0.5 0.5 0.5 0.5 0.5 Thiophene/C.sub.3 H.sub.8 mole ratio 10.sup.-4 10.sup.-4 10.sup.-4 10.sup.-4 10.sup.-4 GHSV (h.sup.-1) 1170 2355 3530 4730 7150 Pressure (atm) 0.95 1.0 1.05 1.0 1.1 Feed preheating temp. (.degree.C.) 500 500 500 500 500 Conversion (%) of Propane 88.1 88.2 88.5 75.5 23.7 Oxygen 98.7 98.6 96.1 84.5 36.4 Selectivity (%) for Propylene 27.1 22.9 21.3 27.1 35.9 Ethylene 38.0 41.2 41.1 41.2 40.1 Methane 16.1 14.4 15.4 14.2 11.9 Ethane 2.9 3.9 2.6 1.6 1.6 C.sub.4+ hydrocarbons 3.5 3.2 3.1 2.3 4.8 Carbon monoxide 10.8 12.6 13.8 10.1 2.2 Carbon dioxide 1.7 1.8 2.8 1.6 1.4 C.sub.3 H.sub.6 /C.sub.2 H.sub.4 0.48 0.37 0.35 0.44 0.60 mole ratio in products ______________________________________ ______________________________________ Results of the oxycracking of propane at 635.degree. C. for different sulfur compound additives in the feed Example    22      23    24    25    26    27 ______________________________________ Process conditions Reaction temp. 635 635 635 635 635 635 (.degree.C.) O.sub.2 /C.sub.3 H.sub.8 0.5 0.5 0.5 0.5 0.5 0.5 mole ratio Steam/C.sub.3 H.sub.8 0.5 0.5 0.5 0.5 0.5 0.5 mole ratio Sulfur Thio- Thio- Thio- Thio- CS.sub.2 DMS compound phene phene phene phEne additive Sulfur 0.0 1 .times. 1 .times. 1 .times. 1 .times. 1 .times. compound  10.sup.-5 10.sup.-4 10.sup.-4 10.sup.-4 10.sup.-4 C.sub.3 H.sub.8 mole ratio GHSV (h.sup.-1) 3000 3000 3000 3000 3000 3000 Pressure (atm) 1.0 1.0 1.0 1.0 1.0 i.0 Feed preheat- 500 500 500 500 500 500 ing temp. (.degree.C.) Conversion (%) of Propane 70.8 76.2 77.1 75.7 7101 78.6 Oxygen 91.1 91.4 91.9 91.0 92.3 91.1 Selectivity (%) for Propylene 24.9 23.8 26.2 23.6 25.2 21.6 Ethylene 38.3 39.4 38.2 38.2 40.1 44.0 Methane 14.0 14.6 14.0 14.5 14.0 14.5 Ethane 2.5 2.8 2.9 2.7 2.9 2.5 C.sub.4+ hydro- 7.4 6.3 5.6 6.5 6.7 6.8 carbons Carbon 12.3 12.5 12.4 13.3 12.5 13.8 monoxide Carbon 0.6 0.6 0.7 0.6 0.6 0.7 dioxide C.sub.3 H.sub.6 /C.sub.2 H.sub.4 0.44 0.40 0.46 0.41 0.42 0.33 mole ratio in products ______________________________________ ______________________________________ Total conversion of propane and its conversion purely by thermal cracking at different temperatures and concentrations of O.sub.2 (relative to propane) in the feed. Reaction conditions: steam/C.sub.3 H.sub.8 and thiophene/C.sub.3 H.sub.8 ratios in feed = 0.5 and 1 .times. 10.sup.-4, respectively and GHSV = 3000 h.sup.-1 and feed preheating temperature = 500.degree. C. O.sub.2 /C.sub.3 H.sub.8 Propane conversion (%) Temp. (.degree.C.) ratio       Total  Thermal cracking ______________________________________ 635       0.00        0.8    0.8 0.06 15.1 7.0 0.13 23.4 6.3 0.25 47.0 27.4 0.50 72.0 42.4 660 0.00 1.6 1.6 0.50 74.7 49.0 715 0.00 7.5 7.5 0.50 74.7 56.6 800 0.00 53.9 53.9 0.06 61.8 59.0 0.13 68.6 62.2 0.25 79.2 72.6 0.50 91.7 77.4 ______________________________________

The main advantages of this invention or major improvement achieved by this invention over the earlier processes for the production of propylene from propane or C.sub.2 -C.sub.4 paraffins are as follows

1. In the process of this invention, because of the simultaneous occurrence of the endothermic hydrocarbon cracking reactions and the exothermic oxidative hydocarbon conversion reactions, the heat produced in the exothermic reactions is used instantly in the endothermic reactions and there is a coupling of the exothermic reactions with the endothermic ones. This has imparted following outstanding features to the process of the present invention: energy saving, achieving high conversion of paraffins with high selectivity for propylene and ethylene, with propylene/ethylene mole ratio of at least 0.15, and also the process is operated at higher space velocity at lower contact time, thus increasing the productivity or space-time-yield of propylene and other olefins. reaction run-away conditions. endothermic by manipulating the process conditions. without any serious problems for removing heat from the reactor, when the process is mildly exothermic or for providing energy to the reactor, when the process if mildly endothermic, thus requiring no or much smaller external energy than that required for the thermal cracking process. of propane but also the rate of thermal cracking of propane, which is occurring simultaneously with the oxidative conversion of propane is increased, hence the process is operated at low contact time and thereby the productivity of propylene and ethylene in the process of this invention is higher than that in the earlier thermal cracking process operating in the absence of oxygen and also propylene and ethylene are produced with propylene/ethylene mole ratio of at least 0.15.

2. Because of the presence of oxygen in the feed, there is no coke deposition on the reactor walls in the process of this invention. Whereas, in the earlier thermal cracking process, there is an extensive coke deposition in the pyrolysis reactor tubes, causing increase in pressure drop across the reactor and ultimately process breakdown for the coke removal. Also because of coke deposition, the life of the reactor tubes in the thermal cracking process is low. These limitations of the earlier thermal cracking process are also overcome in the process of present invention.

3. The process of this invention has also number of advantages over the earlier process based on the catalytic oxidative dehydrogenation of propane to propylene. therefore there are no problems of catalyst deactivation due to sintering or loss of active components or coke deposition. The process operating cost is also reduced, as no catalyst is required. exothermic or mildly endothermic by controlling the simultaneously occurring exothermic oxidative conversion and endothermic thermal cracking reactions; hence the process occur in a most energy efficient and safe manner and the operation of process is simple. Whereas the catalytic dehydrogenation is highly exothermic and hence it is a hazardous process; it is not safe to operate. oxidative dehydrogenation process are much more complicated because of its hazardous nature and catalyst deactivation and heat and mass transfer problems in the catalytic process, as compared to the non-catalytic process of this invention.

## Claims

1. A process for the production of propylene and ethylene by non-catalytic oxidative cracking of propane or propane-rich C.sub.2 -C.sub.4 paraffins, which comprises: paraffins at ambient temperature, mixture of oxygen or O.sub.2 -enriched air and propane or propane-rich C.sub.2 -C.sub.4 paraffins and preheating the resulting admixture to a temperature between about 200.degree. C. to about 550.degree. C., tubular reactor, while maintaining the mole ratio of oxygen to hydrocarbon between about 0.01 to about 1.0, steam to hydrocarbon mole ratio between about 0.1 to about 10 and volatile sulfur compound to hydrocarbon mole ratio between about 10.sup.-2 to about 10.sup.-6 in said admixture feed, with a gas hourly space velocity of said admixture feed between about 500 h.sup.-1 to about 50,000 h.sup.-1 at a reaction temperature between about 620.degree. C. to about 900.degree. C. and a pressure between about 0.5 to about 5.0 atm, such that propylene/ethylene mole ratio in the products is at least 0.15 and there is a coupling of exothermic hydrocarbon oxidative conversion and endothermic hydrocarbon cracking reactions due to the simultaneous occurrence of these exothermic and endothermic reactions, and required, recycling the unconverted reactants.

2. A process as claimed in claim 1 wherein the reaction temperature is maintained between about 635.degree. C. and about 800.degree. C.

3. A process as claimed in claim 1 wherein the pressure employed ranges from about 1.0 atm to about 3.0 atm.

4. A process as claimed in claim 1 wherein the mole ratio of O.sub.2 to hydrocarbon, steam to hydrocarbon and volatile sulfur compound to hydrocarbon in feed ranges from about 0.05 to about 0.5, from about 0.3 to about 3.0 and from about 10.sup.-3 to about 10.sup.-5, respectively.

5. A process as claimed in claim 1 wherein the gas hourly space velocity of feed ranges from about 1000 h.sup.-1 to about 20,000 h.sup.-1.

6. A process as claimed in claim 1 wherein the volatile sulfur compound in the feed is thiophene.