DE977548C - Continuous process for the production of synthesis gas - Google Patents

Description

Continuous process for the production of synthesis gas The invention relates to a process for the production of a carbon monoxide and hydrogen containing Gas, which is used as synthesis gas for the production of hydrocarbons, oxygen-containing Connections or the like. Suitable.

This process is carried out with partial combustion of a carbonaceous fuel with oxygen, both of which may be preheated, in a reaction chamber of generally cylindrical shape which is free of internals and has dimensions which have a K value as defined below of greater than 0.7 correspond, at elevated pressure and elevated temperature, which is automatically maintained by the exothermic reaction. According to the invention, the procedure is such that a gas stream consisting of oxygen and up to 20 percent by volume of inert gas and a stream of a gaseous hydrocarbon or a mixture of gaseous hydrocarbons are introduced separately from one another into the reaction chamber near its one axial end in such a way that the two separate streams have a high Speed, preferably at about 30 m / sec or faster: "collide against each other, and that the resulting mixture flow in the axial direction through the reaction chamber and allow it to react with one another in the absence of a catalyst, these gases being combined in proportions such that the atomic ratio of total oxygen to total carbon of the feed is kept between 1.0 and 1.2, and that the product is withdrawn from the chamber at the end opposite the point of introduction at the said elevated temperatures and pressures.

If any of the claimed features of the invention are not complied with, this creates additional amounts of unwanted carbon, and it increases Unchanged hydrocarbon content of the end product, e.g. B. methane. The non-compliance the process conditions thus degrade the degree of conversion of the feed and causes the quality of the synthesis gas to be produced to deteriorate.

The hydrocarbon to be processed, such as. B. methane, and the oxygen or a gas consisting essentially of free oxygen are expediently preheated independently of one another to a temperature which is substantially above that at which the hydrocarbon would react vigorously in the presence of the oxygen under the heating conditions. Good results can also be obtained if only the hydrocarbon or neither of the two reaction components is preheated. The reaction components, either after preheating or without such, are passed separately from one another into the reaction chamber of a generator which essentially contains no internals and no catalyst, is at an operating temperature of about 1100 ° C. and higher and under a pressure of about 14 up to 21 kg per square centimeter. The ratio of the amount of oxygen flowing into the reaction space to the amount of hydrocarbon is selected so that the reaction for converting the hydrocarbon into carbon monoxide and hydrogen takes place without additional heat being supplied to the reaction space from the outside (apart from the heat inherent in the reaction components), and that the gas product leaving the reaction space is essentially free of elemental carbon.

In the schematic drawing, FIG. 1 shows a section along the horizontal axis of a gas generator; Fig. 2 is a longitudinal section of a particularly advantageous form of gas supply device; Figure 3 is a graph of the surface area relationships between generators of various shapes and spheres of corresponding volumes.

A hydrocarbon consisting essentially of methane can be reacted with oxygen in the absence of additional water vapor and in the absence of a catalyst in a reaction space whose ratio between the inner surface and the inner volume is quite small (cf. the explanation below) at a temperature of about 1100 to 1400 ° C. and a pressure corresponding to the values given above. The hydrocarbon gas, if it is to be preheated, is heated by itself to at least 425 ° C., expediently about 650 ° C. and expediently without a cracking effect occurring, and then in an amount of about 1000 to 3000 m3 per hour and per cubic meter of the l- 'reaction room initiated in this. If the oxygen is to be preheated, it is heated by itself to at least 315 ° C., expediently to about 425 ° C. or higher, and then introduced into the reaction space in such an amount that combustion, or in other words, a primary reaction in the reaction space (with the exception of the relatively small point near the point of contact of the gas and oxygen flows) with an essentially non-luminous flame. This primary reaction is essentially exothermic. Some of the primary reaction products then enter into secondary reactions with the excess hydrocarbon, which are essentially endothermic. The end products of the reaction are discharged from the reaction space in a continuous stream consisting essentially of carbon monoxide and hydrogen and containing approximately 5 volts per cent or less of water vapor and significantly less than 2 percent by volume of carbon dioxide (calculated on the anhydrous product). The effluent gas stream is essentially free of suspended carbon since, measured under normal conditions, it contains less than 0.036 g of it per cubic meter of gas produced. The residual methane content in the end gas is not greater than 4 or 5 percent by volume. Carbon monoxide and hydrogen are in the gas in a ratio of about 1 mole of carbon monoxide to 2 moles of hydrogen. However, the molecular mixing ratio also depends on other factors, such as e.g. B. on the composition of the processed hydrocarbon, and these factors are taken into account in the production of the gas, if you want to obtain certain mixing ratios between carbon monoxide and hydrogen.

The temperature of the gas stream leaving the reaction space is quickly suppressed by cooling. It is recommended to use the TemperatLir z. B. from about 1425 ° C to about 540 to 815 ° C within no more than a second to avoid undesirable side reactions, which lead in part to carbon formation at this stage.

The oxygen is as pure as possible, at least as 80%, or better than 95% or even purer gas. This will make great Amounts of nitrogen switched off, which would otherwise with the reaction components in the gas generator would arrive. This measure results in a reduction in the heat requirement. At the same time, a synthesis gas is obtained that is more suitable for synthesis processes is.

The amount of the introduced oxygen in the gas generator in relation to that of the supplied hydrocarbon appears to be important from the viewpoint that the formation of free carbon, excessive amounts of carbon dioxide and b Wasserdampfbildulig must be avoided. Creeignete working conditions are in the preferred minimum temperature of 1 100'C, if initially the amount of oxygen for the Beschikkung of the generator or to another term, to be used when inan the O / C-number (ratio of the total Sauerstoffatonie to total Kohlenstoffatorrien in the batch) regulates and defines within the relatively wide limits of about 1.0 to 1.2, so that the gas coming from the generator contains about 0.5 to 5 percent by volume, expediently 2 to 3 percent by volume, of residual methane. This rule must always be applied, regardless of whether the oxygen comes from an essentially pure source of satire or from an oxygen-enriched gas and the carbon z. B. from one or more gaseous hydrocarbons, such as. B. from natural gas.

If the gas coming from the generator contains more than about 5 percent by volume of residual methane under the conditions mentioned, a noticeable amount of free carbon is produced, which is expressed in the clear discoloration of the water used to cool the gas flow. The cooling water will not be discolored if the residual methanine content is 5 percent by volume or less. It is therefore expedient to keep the residual methane amount of the end gas in the order of magnitude of about 0.5 to 5 percent by volume, which is achieved by setting and maintaining the O / C number at a value between 1.0 and 1..2 will. If so much oxygen is supplied that methane is not present in the finished gas, then a relatively large part of the oxygen is lost in the form of carbon dioxide and water vapor. Furthermore, the reaction temperatures then tend to rise excessively.

If it is important to convert the carbon of the supplied gas as completely as possible into synthesis gas (carbon monoxide and hydrogen) and to suppress the formation of free carbon completely or to the smallest amount, then it is advisable to reduce the methane content of the finished generator gas in an amount of around 0 To hold 5 to 2 percent by volume. Below the lower value, too large amounts of carbon dioxide and water are evidently formed. If, on the other hand, it is important to convert the oxygen into synthesis gas as completely as possible, then it is advisable to keep the 1 \, lethane content at about 2 to 311 / o, otherwise the yield will decrease.

Under the specified temperature and pressure conditions and when using a starting hydrocarbon which consists essentially of methane, the oxygen consumption is usually about 5 to 15 percent by volume above the stoichiometric amount that is required for the total carbon of the hydrocarbon gas in carbon monoxide without the formation of other oxygen compounds convict. The concentration of the oxygen is chosen so that the reaction takes place under the stated temperature and pressure conditions in the generator and when the reacting substances are preheated without external heat being supplied to the reaction space. By preheating the reacting gases separately from one another and then clit them exclusively within the reaction space mi2 #. backfire in the supply pipes and preheaters can be prevented.

A nil mixing of the reacting gases, which takes place completely within the reaction space, is achieved in that separate hydrocarbon and oxygen streams are introduced in such a way that they flow within the reaction space at a high flow rate, e.g. B. from 30 m / sec or in the order of about 9 to 60 m / sec, aufmandersto # en.

It is also important to use a reaction space that does not contain any internals and allows unhindered radiation of elimination between the adjacent walls. The surfaces of all ##, 'ands are expediently arranged in such a way that they can be easily reached by the energy emitted by the reaction components in the exothermic, i.e. H. primary response is developed. If methane is used as the hydrocarbon, 2511 / o of it can burn with the formation of carbon dioxide and water. These products in turn react further with the methane iiii reaction space with the endothermic formation of carbon dioxide and hydrogen. The primary exothermic combustion, which supplies the energy required for the secondary endothermic reactions, apparently takes place mainly in the small area where the first contact between the supplied gas and the oxygen takes place.

In the interests of the most effective possible use of the energy from the primary (exothermic) reaction for the secondary (endothermic) reaction, it has been found necessary not only to keep the generator free of internals, but to design it so that its inner surface is in proportion to its internal volume is small, as is the case with a sphere. However, since a sphere is not always a practical shape for other reasons, shapes such as a ball are usually used. 13. Cylinders with concave or convex end part or parts preferred.

The ratio of the surface to the volume of such a generator can best be defined by reference to a sphere of the same volume, whereby the surface-volume ratio of the generator obviously comes close to the corresponding value of a sphere of the same volume, but can never quite reach it . The degree of approximation to the surface-to-volume ratio of a sphere can be expressed by a constant K. The constant K defines the ratio between the surface area of a sphere and the surface area of a gelling agent to be used according to the invention with the same content. The value of the constant K in its relationship to the ratio between the total length and radius of a purely cylindrical generator, taking into account that inlet and outlet channels are permanent components of its surface, can be determined as follows: Surface of the generator (0g) = 2 Ur R2 ur RL content of the generator (Vg) = irR2L, where R is the radius of the generator and L is its total length.

The surface and the volume of a sphere with the same content can be determined as follows: where Ri means the radius of the sphere. But since Vg = Vk, we get: Since the volumes of the sphere and the generator are assumed to be the same, the following results for K : If the value determined for R, is used here, the result is: In the following table some K-values are compiled for cylindrical generators in which the total length to their radius is in different specific ratios. K L of the formula Total L K 1 0.01 0.011 0.0759 1 0.1 0.1 0.3234 1 0-.2 0.2 0.4706 1 0.5 0.5 0.6934 1 1 1 0.8254 1 2 2 0.8736 1 5 5 0.8046 1 10 10 0.6966 1 20 20 0.5793 1 50 50 0.4394 1 100 10 () 0.3522 The above values for K and L: R are shown graphically in FIG. 3 on a logarithmic scale in the form of the drawn out curve. It can be seen from this that if the value L: R changes, the value K - for a cylinder with flat ends approaches the value 1 and then moves away from it again, and that the 0: V ratio of the sphere never reaches will.

The remaining curves in FIG. 3 explain the K values in relation to the L: R values for cylinders, the end shape of which is designated, and for a generator with a square cross-section, in which case the radius of an inscribed circle is assumed to be R. is. For cylinders with other than flat end parts, R is the radius of the cylinder cross-section. For cylinders with conical end parts, the included angle of 60 'has been assumed. These curves can be determined for each cylinder using the following formulas: The following applies to a cylindrical generator with a hemispherical end part where L is the length of the purely cylindrical part.

For a cylindrical generator with two hemispherical end parts 2-ilt where L is the length of the pure cylinder part.

The following applies to a cylindrical generator with a conical end part of 60 ' where L is the length of the pure cylinder part. The following applies to a cylindrical generator with two conical end parts of 60 'each where L is the length of the pure cylinder part.

For a right-angled parallelepiped with a square cross-section and side length w applies If it is a cylindrical generator with a hemispherical end part, the total L of the L: R value means the total length of the generator, i.e. H. L + R. The following values were used for the corresponding curve in FIG. 3: RL of the formula Total L K R. 1 0 1 0.8399 1 0.01 1.01 0.8427 1 0.1 1.1 0.8643 1 0.2 1.2 0.8828 1 0.5 1.5 0.9148 1 1 2 0.9283 1 2 3 0.9071 1 5 6 0.8073 1 10 11 0.6957 1 20 21 0.5783 1 50 51 0.4389 1 100 101 0.3520 If it is a cylindrical generator with two hemispherical end parts, the total L of the L: R value means the total length of the generator, i.e. H. L 4- 2 R. The following values were used for the corresponding curve in Fig. 3: R L of the formula Total L K 1 row 1 0 (sphere) 2 1.0o0 1 0.01 2.01 0.999 1 0.1 2.1 0.9994 1 0.2 2.2 0.9979 1 0.5 2.5 0.9892 1 1 3 0.9681 1 2 4 0.9210 1 5 7 0.8073 1 10 12 0.6942 1 20 22 0.5722 1 50 52 0.4385 1 100 102 0.3518 In the case of a cylindrical generator with a conical end portion of 60 ', the total L of the L - R value means L + 1.73205 R. For the corresponding curve in FIG. 3 , the following values were used: K L of the formula Total L K R. 1 0 1.73205 0.7631 1 0.01 1.74205 0.7668 1 0.1 1.83205 0.7958 1 0.2 1.93205 0.8210 1 0.5 2.23205 0.8675 1 1 2.73205 0.8948 1 2 3.73205 0.8867 1 5 6.73205 0.7988 1 10 11.73205 0.6918 1 20 21.73205 0.5766 1 501 51.73205 0.4384 1 WO 101.73205 0.3516 If it is a cylindrical generator with two conical end parts of 60 ', the total L of the L: R value means L + 3.46410R. The following values were used for the corresponding curve in FIG. 3: RL of the formula Total L K 1 R. 1 0 3.4641 0.9085 1 0.01 3.4741 0.9092 1 0.1 3.5641 0.9145 1 0.2 3.6641 0.9188 1 0.5 3.9641 0.9239 1 1 4.4641 0.9181 1 2 5.4641 0.8878 1 5 8.4641 0.7921 1 10 13.4641 0.6868 1 20 23.4641 0.5740 1 50 53.4641 0.4375 1 100 103.4641 0.3514 If it is a right-angled parallelepiped with a square cross-section, w means the diameter of an inscribed circle as well as the length of one of the sides. When calculating the following values for the curve in FIG. 3 , 0.5 w was used as the radius. W L of the formula Total L K 2 0.01 0.01 0.07000 2 0.1 0.1 032983 2 0.2 0.2 0.4341 2 0.5 0.5 0.6397 2 1 1 0.7616 2 2 2 0.8060 2 5 5 0.7423 2 10 10 0.6427 2 20 20 0.5344 2 50 50 0.4054 2 100 100 0.3249 It is obvious that from the curves of FIG. 3 thus obtained, the value K can be determined for any generator of various types, provided that the ratio L: R is known. The actual dimensions of the generator are immaterial.

If it is z. For example, if it seems desirable to use a cylindrical generator with a flat and a hemispherical end portion, which is one of the most common shapes, the curve for this shape shows that the best approximation is all the surface-to-volume ratio of a sphere same volume at K = about 0.93 . The corresponding L: R value is about 2.0. If the generator to be used is to have a total length of 3 m, a radius of 1.5 m would have to be selected.

For the process according to the present invention, L: R values between approximately 0.67 and 10 have proven to be expedient; values from 1 to 4 are particularly advantageous.

In any case, it is desirable to have the reaction space free of internals to make it sufficiently crowded so that the temperature in the entire reaction space can be kept uniform.

By avoiding the external heating of the reaction space - and any Refractory fixtures inside the reaction space will be the existing ones Overcome significant apparatus design and process difficulties. By the absence of internals will not only result in a significant pressure drop within of the reaction chamber avoided, but also the tendency to form carbon and -deposition is significantly reduced, since large spaces seem to cause carbon formation support financially. Carbon deposition also increases the pressure differential within the reaction space.

Another advantage of the absence of internals and compliance there is a certain ratio of surface to volume or length to radius in that the full unobstructed space with its in relation to its inner Large volume surface an essentially complete transfer of energy from the primary exothermic reaction to the secondary endothermic reaction by radiation enables. each from the exothermic reaction on the adjacent walls of the reaction space radiated energy is immediately reflected back into the reaction space. Appropriate the wall surfaces are designed in such a way that they ensure maximum reflection. In this way it is achieved that very little energy is lost. Farther can activate all products of the primary reaction, be it in the form of radicals Molecules or otherwise in the high-energy mixed state unhindered into the area the secondary reaction migrate without physical objects, such as built-in components, disturb. The absence of internals makes it possible for both the radiant energy from the primary reaction as well as the energy reflected back from the walls unhindered enters the zone of the secondary reaction, with the result that the secondary Reaction or reactions faster and at higher and more even temperature and energy level to achieve a better composition of the reaction products expire.

This effect is in marked contrast to the effect achieved in a generator with built-in components, which manifests itself in the following way: 1. The products of the exothermic reaction come into physical contact with the internals almost immediately after their formation, which results in the formation of more stable molecules, the deposition of carbon on the internals and the deactivation of the active molecules, whereby energy is lost that would otherwise be required for the secondary Response would have been available; 2. the products entering the zone of the secondary reaction are shielded to a considerable extent against the radiant heat from the exothermic reaction and against the heat reflected back from the walls, and 3. the products of the exothermic reaction tend to get into the gaps in the internals Establish carbon deposition, which results in loss of booty from ZD. In Fig. 1, numeral 1 denotes a cylindrical, lined with refractory material 2 vessel. Within the vessel, a shielding device formed from the walls 3 a and 3 b is provided, which divides the vessel into two spaces, one space representing the reaction space 5 , the z. B. has a length of about 2.5 m in the horizontal axis, while the other space 6 is used for cooling the gas products formed. With a radius of 0.75 m, the L: R value is approximately 3.2 and is therefore within the preferred range. The walls 3 a and 3 b are designed so that they allow the passage of the reaction gases without any significant pressure drop and at the same time protect the interior of the cooling chamber against direct radiation from the reaction chamber as well as against reflection of the reaction chamber radiation into the reaction chamber. This is achieved ABy d in that the openings 3c are staggered.

A cooling pipe system 7 is provided in the refractory lining of the reaction space, through which water or any other flowing heat transfer medium can be passed in order to avoid overheating of the metal shell. The heat absorbed in this way can be used for preheating or to generate steam or energy.

The reaction gases are introduced into the reaction space through a plurality of gas feeders 8 , which will be described in detail in connection with FIG. 2. The reaction products are passed from the generator through the channels 3c in the Kühlraum6, where they are cooled to a suitable temperature by means of a fogging device 9 to be gebpeichert to temporarily or passed into a synthesis generator. The cooling water emerges from the opening 6a together with the synthesis gas. When using a synthesis catalyst of the iron series, the gases are cooled by the cooling water, whereupon they come into contact with the fleece catalyst at this temperature and as long as they are still under a pressure of about 1 -1 to 17.5 kg / cm2, which leads to the conversion of carbon monoxide and hydrogen in hydrocarbons, oxygen-containing compounds or the like.

As shown in FIG. 2, the gas feeders 8 essentially consist of two concentric tubes 11 and 12 which end in a water-cooled tip 13 . Accordingly, the tip 13 is hollow and contains the water space 14 with the water inflow pipe 15 and the water outflow pipe 16.

One of the reaction gases flows through the annular space between the tubes 11 and 12, while the other gas flows through the inner tube 12. So z. B. the methane flow through the annular space and the oxygen through the inner tube or vice versa. In this way it is achieved that the methane and oxygen streams at the point of their exit from the tip 13, i. H. So just within the reaction space, collide. As drawn in Fig. 1 , the tips of the gas feeders can be arranged so that they are substantially flush with the inner surface of the refractory lining.

During operation there is only one small spot in the immediate vicinity Near the tip to observe a blue flame or radiation while im No flame is visible in the rest of the reaction space. In this little place where blue flames appear, 251 / o of the incoming methane becomes proportionate completely burned, producing carbon dioxide and water vapor, which subsequently in the reaction space with excess methane with the formation of carbon monoxide and Hydrogen react.

The heaktionsratim can be equipped with a larger number of such gas feeders 8 . For example, several such gas feeders can be arranged uniformly at the end of the space 1.

The method can be carried out, for example, as follows. A substantially consisting of methane source gas 'is preheated C, during which a substantially pure oxygen to about 425 isolated' to about 500 C is preheated. The preheated gas streams are then introduced into a reaction space free of internals, which has an L: R value of about 2.7, i.e. approx. H. that is, within the above-mentioned advantageous range between 1 and 4 and is under a pressure of about 17.5 kg / CM2. In this room the gases are burned at a temperature of around 1100 ° C. The hydrocarbon or the raw material gas is in the absence of a catalyst being in the reaction chamber in an amount of about 2,000 m3 per hour and per cubic meter of the total reaction space started. The amount of oxygen introduced into the reaction chamber is kept at about 39.3 percent by volume of the total gas supplied (methane plus oxygen) (O: C atomic ratio = 1.1). The reaction produces about 3.2 mol of cold gas per mole of hydrocarbon starting gas. The source and end gas have the following composition: Volume percent starting gas end gas CH4 '- ......... 83.6 2.8 C2H6 ............. 10.2 - C3H8 ............. 4.5 C4H10 0.1 - C02 .............. 1.0 1.4 Air .............. 0.6 - Co .............. - 32.9 H2 - 56.9 N2 ............... - 0.9 H20 ............. - 5.1 100.0 100.0 Under these conditions, more than 801 / o of the oxygen introduced is converted into carbon monoxide, the water used to cool the hot end gas remaining essentially free of solid carbon.

If, however, the reaction chamber under substantially the same temperature and pressure conditions maintained, the amount of oxygen j edoch controlled so that this about 35 volume percent of the supplied ührten total gas makes (0: C atomic ratio = 0.92), then the amount of methane amounts In the end gas to at least 10 percent by volume, while at the same time an excessive amount of carbon is deposited, which results from the distinctly black color of the cooling water due to its high content of free carbon.

On the other hand, if the process is conducted so that the amount of oxygen is 42.2 percent by volume of the total gas supplied (0: C atomic ratio = 1.25), the end gas contains only traces of methane and the oxygen becomes essentially less than 8011 / o converted to carbon monoxide, while the amounts of carbon dioxide and water increase.

The following example shows the relationship between the methane content of the gas flowing out of the generator and the yield of carbon monoxide and hydrogen when a hydrocarbon gas of the above-described composition is under a pressure of about 17.5 kg / CM2 and a temperature of about 1100 ° C in the Reaction space is treated. The hydrocarbon gas was preheated to about 440 ° C and the oxygen to about 315 ° C, both gases on their own. The amount of oxygen supplied was about 53 to 62 parts by volume per 85 parts by volume of the hydrocarbon gas (O: C atomic ratio = 1.06 to 1.24): Yield of CO + H2 in Volume Percent CI-4 Volume Percent of Theoretical in the end, -as maximum yield 6.0 71.9 3.2 75.6 0.4 70.9 0.1 69.0 From the above values it can be seen that a yield of 75.6% of the theoretical yield is obtained when the reaction is conducted so that the end gas contains 3.2% methane. If the methane content of the end gas is significantly below 3 percent by volume or significantly above, the yield of synthesis gas is reduced. The yield of 75.6% corresponds to a conversion of about 80.5 % of the oxygen into carbon monoxide.

In addition to the process of cooling the end gas with water, can also other cooling methods, e.g. B. those with steam generation can be used.

It has been stated that methane or an essentially methane existing gas can be introduced into the generator. However, it is also possible Hydrocarbons of higher molecular weight which are normally gaseous are to be introduced into the generator.

It has already been pointed out that the process can be carried out without preheating or in such a way that only the hydrocarbon or the hydrocarbon and the oxygen are preheated separately from one another. The gas streams can be preheated to as high a level as is practical, given the constraints imposed by the material of construction. The preheating of a stream of oxygen to relatively high temperatures requires the use of a preheater made of a material that can withstand the action of oxygen at such temperatures. The oxygen on its own is expediently preheated to 315 to 425 ° C. and, if possible, also higher, and the hydrocarbon is preheated to 425 to 650 ° C. If higher preheating temperatures are used, higher reaction temperatures are also achieved, which should be aimed at because of the greater overall yield, since the formation of undesired carbon dioxide and methane is reduced. and there is also less tendency to form carbon at lower 0: C values.

If necessary, the hydrocarbons to be processed can be used before they be introduced into the generator to remove sulfur compounds be pretreated. This seems appropriate to generate a synthesis gas, which is free or essentially free of sulfur compounds.

Claims (2)

PATENT CLAIMS: 1. A process for the continuous production of a carbon monoxide and hydrogen-containing synthesis gas by partially burning a carbon-containing fuel with oxygen, both of which may be preheated, in a reaction chamber of generally cylindrical shape which is free of internals and has dimensions corresponding to a K- Value (ratio of the surface of a ball with the same content to the inner reaction surface) of greater than 0.7 , at elevated pressure and elevated temperature, which is automatically maintained by the exothermic reaction, characterized in that one of oxygen and up to 20 percent by volume of inert gas existing gas stream and a stream of a gaseous hydrocarbon or a mixture of gaseous hydrocarbons are introduced separately from one another into the reaction chamber near one axial end thereof that the two separate streams at a high speed, preferably at about 30 m / sec or faster, collide with one another, and that the resulting mixture flows axially through the reaction chamber and is allowed to react with one another in the absence of a catalyst, these gases being combined in such proportions that the atomic ratio of the total oxygen to the total carbon of the charge is between 1.0 and 1.2 is maintained, and that the product is withdrawn from the chamber at the end opposite the inlet point at the reaction temperature and reaction pressure. 2. The method according to claim 1, characterized in that gaseous hydrocarbon is introduced into the chamber at a space velocity of at least 1000 m3 per hour per cubic meter of the chamber volume. Considered publications: German Patent Nos. 458 074, 616 466, 900 986; USA. Patents # 517 681, 1,924,856, 2,002,863, 2,302,156. Austrian Patent Nos. 134 617, 149 358; British Patent Nos. 231218, 252 045, 252 222, 254 713, 288 662, 416 957, 533 877, 867 823;