DE1255642B - Process for producing reducing gas rich in carbon monoxide and hydrogen - Google Patents

Description

FEDERAL REPUBLIC OF GERMANY GERMAN MjWVm PATENTAMT Int. Cl .:

COIb

EDITORIAL

German class: 12 i- 1/24

Number:
. File number:
Registration date:
Display day:

E 22831IV a / 12i

May 4th 1962

7th December 1967

The invention relates to an improved method for producing carbon monoxide and hydrogen rich Reducing gas using temperatures in the range of 927 ° C and higher Gasification of hydrocarbons in a fluidized bed of finely divided solids in a Cleavage zone with the formation of hydrogen and coke are cracked, with the coke on the Solid particles separated from the fluidized bed and then in a separate combustion zone at least is partially burned with an oxygen-containing gas.

The coking of hydrocarbons and the gasification of the product with an oxygen-containing gas, such as air, oxygen or water vapor, is known per se. In a known method, heating and gasification are carried out in layers; the coke mass is first heated with air, the air being passed through the mass from bottom to top after lighting, so that a fluidized bed is formed, but only until the temperature required to decompose the tars is reached. The substances to be gasified are then injected, the temperature gradually falling with the formation of oil gas. In a further known method, a mixture of hydrocarbons and water vapor is introduced into a fluidized bed reactor while the coke particles circulate between the reaction vessel and the combustion line; Since the coke particles have to be heated up again, the combustion in the combustion tube is carried out as completely as possible to the point of carbon dioxide, so that there is no coke-consuming conditions there. The gas produced in the reaction zone contains a little more carbon dioxide than carbon monoxide. It is also known to produce town gas from petroleum hydrocarbons in a single reaction zone and to add the hydrocarbons and either oxygen or superheated steam for the conversion to town gas in this single reaction zone. In these known processes, the hydrocarbon starting material is always split and the split products are oxidized. The mechanism of these reactions has not yet been fully elucidated; however, the initial reaction products are likely to be CO ₂ and H ₂ O. These react at least partially with the carbon present in the fluidized bed and the carbon formed during the cleavage to form H ₂ and CO. The reaction temperatures are around 927 to 1205 ^° C., and the heat required is supplied by the combustion process. The implementation*'

Process for the production of reducing gas rich in carbon monoxide and hydrogen

Applicant:

Esso Research and Engineering Company,

Elizabeth, N. J. (V. St. A.)

Representative:

Dr. K. Th. Hegel, patent attorney,

Hamburg 52, Giesestr. 8th

Named as inventor:
John Frederick Moser,
Karsten Herbert Moritz,
Baton Rouge, La. (V. St. A.)

Claimed priority:

V. St. v. America May 10, 1961 (109 137)

the carbon and the oxygen-containing gas are affected by a number of different factors. These factors are primarily the temperature, the residence time, the ratio of carbon to oxygen-containing gas and the surface properties of the carbon.

It has now been found, surprisingly, that the quality of such gasification process resulting gaseous product can be improved if the gasification under coke consuming Conditions is carried out. The inventive method for the production of carbon monoxide and hydrogen rich reducing gas using temperatures in the range of 927 ° C and higher by gasifying hydrocarbons, which are finely divided in a fluidized bed Solids are cracked in a cracking zone with the formation of hydrogen and coke, with each other the coke is deposited on the solids forming the fluidized bed and then in a separate combustion zone is at least partially burned with an oxygen-containing gas, is accordingly thereby characterized in that the temperature, the residence time and the ratio of oxygen-containing gas to added hydrocarbons are varied so that the ratio of carbon to oxygen in the hydrocarbons added to the Spaftf one

vw » i ί ν« «a turn y

709 707/527

German Palenfamf

and the oxygen-containing gas fed to the combustion zone is less than the ratio of Carbon to oxygen in the gasification products and the carbon of the coke in the fluidized bed is consumed faster than it is deposited there as a result of the splitting of the hydrocarbons, whereby there is direct contact between the oxygen-containing gas and the supplied hydrocarbons avoided the coke used is supplemented by adding coke to the fluidized bed and the gaseous products from the two zones are combined with one another. Particularly advantageous Reaction conditions are achieved when a turbulent, dense fluidized bed is used as the fluidized bed begins.

The hydrocarbons are expediently fed into an intermediate part between the upper main part and the bottom part and air into the bottom part of the fluidized bed, and the gaseous oxides of the Carbon and nitrogen from the bottom part are mixed with hydrogen and hydrocarbon gases in the Intermediate part of the bed, and this gas mixture is passed upwards through the main part of the bed. If you use liquid hydrocarbons, then it is advantageous to spray them with the help of introduce a practically oxygen-free gas into the cleavage zone.

You can also work in two stages; Here, the hydrocarbon is introduced into a maintained by adding an appropriate amount of air at a temperature of 482-705 ⁰ C fluidized bed coking zone advantageously, the gaseous product and the coke present in the swirling state are then in one on the temperature in the range 927-1205 ⁰ C maintained gasification zone, and this gasification zone is also supplied with the air required for coke consumption.

In the process according to the invention, a reducing gas is obtained which consists predominantly of carbon monoxide and hydrogen and has high ratios of CO: CO ₂ and H ₂ : H ₂ O.

In its basic feature, the invention is based on the finding that the quality of the gas is significantly improved if the gasification reactor is operated under "coke-consuming conditions". "Coke Consumption" means that some of the coke bed in the reaction vessel is continuously being consumed, and this is accomplished by reducing the ratio of carbon to oxygen in the feed stream. If z. For example, if, in theory, all of the carbon in the hydrocarbon feed stream is to be converted to carbon monoxide, it is theoretically necessary to introduce 2 gram atoms of carbon into the reaction vessel for every mole of oxygen. Theoretically, the ratio C: O ₂ in the outflowing gas then has the value 2. This ratio is referred to here as "carbon extraction" and is a simple measure of the quality of the reducing gas. If the C: O ₂ ratio in the feed stream is greater than the C: O ₂ ratio in the effluent gas, that is, as the carbon recovery, then it accumulates according to the general equation

since the ratio of C: O ₂ in the feed is less than the ratio of C: O ₂ in the product, coke becomes according to the equation

CH * + O ₂ -> CO ₂ 4 - CO + H ₂ O 4 _{- H 2} - C

consumed in the reaction vessel. This is known as "coke consuming" conditions, and the Coke is then exhausted from the reaction vessel; i.e., there is coke consumption in the fluidized bed instead of.

ftt is the practice of carbon extraction Product far from the value 2 and depends on the kinetics of the gasification reaction. at low temperatures and short residence times on a relatively inert solid such as a Coke fluidized bed, this value can even be 1 or even lower. At high temperatures, long residence times and very reactive carbonaceous solids such as activated carbon the value will be 1.9. The following was observed under coke deposition conditions:

Table I.
Coke production

coke Coke bed
Dwell time in
15j 55 1.36
1.55
1J4 Activated carbon bed
Seconds
15th 982 ° C 1.05
1.22
1.39 1.45
1.65
1.85 1038 ⁰ C 1093 ⁰ C

From these values it follows that one has to go over to very long residence times and / or very high temperatures and / or strongly activated charcoal must apply in order to obtain a good carbon recovery to achieve.

The gasification of hydrocarbons can be carried out for the purpose of obtaining various end products, namely luminous gas, synthesis gas, hydro gas, reducing gas, etc. Of course, the intended use of the gaseous end product determines the desired composition. For many purposes, especially for direct iron ore reduction, the gas must have very high CO: CO ₂ and H ₂ : H ₂ O ratios in order to maintain a favorable equilibrium for iron formation above the iron oxide. Ideally, the gas consists of pure hydrogen and carbon monoxide. Carbon recovery is a simple measure of the reducing efficiency of a gas. This can be seen from the following table:

Table II
Iron ore reduction at 982 ° C

Carbon extraction

1.29

1.6

2.0

Gram atoms of reduced Fe
to gram atoms C in the gas

0.3

0.53

O ₂

CO ₂ + CO + H ₂ O + H ₂ + C

² 1212

coke in the reaction vessel. The conditions that favor this reaction are called "coke deposition" conditions designated. If other-related to emGas with a ratio C: H = 1.6. These numbers are only theoretically determined from the thermodynamic equilibrium; despite this favorable thermodynamic equilibrium

Table I shows that high grades of gas, which are suitable for iron reduction, on a Coke fluidized bed can only be achieved with great difficulty. It is an in the speed-limited process, which is influenced by the properties of the solid which the gassing takes place.

The process according to the invention shows the unexpected result that, under coke-consuming conditions in the reaction vessel, the rate of conversion of hydrocarbons to CO and H _{2 is} greatly increased. This has the advantage that you can work with a smaller reaction vessel and lower temperatures in the process according to the invention.

The process according to the invention is more difficult to convert with particularly good results Oils and residues in a gaseous product, which is richer in hydrogen and carbon monoxide is when it was available by the previously known methods apply. Improvements could be made the conversion by more than 45% can be achieved when under the same conditions of temperature and residence time of the gasification reactor not under coke precipitation conditions as in the known ones Process, but was operated under coke-consuming conditions. These results are off surprising for the following reasons: Although the speed of reactions between solids and gases in general and also, as Table I shows, proportional to the exposure time in the gasification system is on the active surface and longer residence times in the fluidized bed of coke are known Process lead to a better quality of the gas, conversely, the gas quality is worse is when the residence time is shortened, it is surprisingly found that the invention Working under coke-consuming conditions the opposite is true. Although the residence time of the Reactant to the coke due to the fact that coke is being consumed from the reaction vessel is shortened, the quality of the gaseous product increases significantly, as from the following Table II shows:

Table III

Attempt supply air Dwell time Coal duration speed swiftly in the material- in age speed Coke bed win- hours g / h Nm ³ / h in hours tion 3 244 1.98 29.8 1.49 5 244 1.98 28.4 1.50 7th 244 1.98 27.1 1.49 9 244 1.98 25.8 1.53 11 244 1.98 24.6 1.55 13th 244 1.98 23.5 1.58 15th 244 1.98 22.3 1.66

The reasons why the gasification zone was operated under coke-consuming conditions Quality of the gaseous product so significantly influenced are not yet known exactly.

Since in the process according to the invention, the fluidized bed of coke at high temperatures under coke consuming Conditions, it must, when it is exhausted of coke, for the continuous Operation to be supplemented. This can be done easily by adding fresh coke from the reaction vessel take place simultaneously with the addition of the hydrocarbon and the oxidizing gas. Here can if necessary, what is necessary to maintain the "coke inventory" in the gasification zone Supply coke from a cryogenic coking process. Those convertible into the vortex state Coke particles for the operation of the gasification zone are expediently used in a size of about 40 to

ίο 300μ, so that a turbulent, dense bed is formed, if the carrier gas at a linear velocity in the range of 0.15 to 1.22 m / sec. through the bed.

In the gasification reaction, in which the liquid or gaseous hydrocarbon feed in the Is distributed fluidized bed, the temperatures in the fluidized bed are in the range of 954 to 1315 ° C, preferably in the range from 954 to 1149 ° C, with a small temperature gradient in the fluidized bed, preferably less than 55 ° C.

The pressures are in the gasification reaction zone

usually a little above atmospheric pressure, e.g. B. from 0 to 2.7 atm .; however, the pressure can be increased.

The hydrocarbon feed should be high enough above the bottom of the same and into the fluidized bed be introduced above the point where the air enters the bed, so that there is immediate oxidation the hydrocarbons are avoided by the oxygen and no hot spots form in the bed, which can lead to deactivation and the formation of fine soot. Such finely divided soot generally has a particle size of less than 1 micron. The entry point of the hydrocarbons in the fluidized bed, however, should not be too high up near the upper end of the bed, but rather at such a point that the gaseous hydrocarbons in the feed still have a sufficient Contact time is given in which this is in the presence of the coke-containing solids in the fluidized bed can decompose at a temperature above 954 ° C. You can z. B. the hydrocarbons in let the bed enter about 30 cm above the grate that supports the fluidized bed and through which air enters the Bed is introduced, while the remaining 0.9 to 3 m of the bed are above the point at which the hydrocarbons to be introduced. In this way, the backmixing takes place sufficiently quickly in turbulent motion, the carbon and coke deposits absorbing solids in Contact with the air entering at the bottom of the bed takes place so that the deposits are oxidized and a practically uniform temperature is maintained throughout the bed.

To further explain the method according to the invention, reference is made to the drawing, in the

F i g. 1 a device suitable for carrying out the method and

F i g. 2 shows an embodiment in which one of two vessels, namely a coker and a Carburetor, existing system is used.

The in F i g. 1 shown reactor is housed in the vessel 1, which contains a fluidized bed and has communicating parts. The vessel 1 can be made of a heat-resistant, refractory material be lined heat-resistant steel jacket.

A refractory material, e.g. B. silicon carbide, ceramic material, metal alloys or one

7 8

Metal with a refractory lining, consisting of solids separated from the gases in the bed 4 middle suction pipe 2 is in the vessel 1 and gas outlet lines 17 to the main gas line 10, arranges that it divides an inner reaction zone 3, which forwards the gases to any plant, in which the oxidation of the coke or coal deposits where they z. B. used to reduce iron oxide gene on the circulating solids 5 can be. If desired, the trial can take place duct gases are otherwise treated, e.g. B. with

Carbonaceous solids are made from the hot carbon to the concentration in the fluidized bed of coal 4 to increase the hydrocarbon decomposition zone monoxide, or by a catalytic through pipe 5 and inlet pipe 6 into zone 3 water gas treatment, which increases the yield of hydrogen directed. 10 by reacting the carbon monoxide with water

A gas containing free oxygen, ζ. Β. Air increased.

or enriched air, to oxidize the coke. The sufficient turbulence of the solids in the

Deposits on the fixed bed 4 surrounding zone 3, in order to reduce the temperature fluctuation in the bed

Stcffteilchen, is fed through line 7. Keeping this low, i.e. below 55 ° C, is a key

Air can be preheated, e.g. B. to 204 to 538 ⁰ C. 15 Control of the feed rate of the coal

The hydrocarbon feed obtained from e.g. hydrogen feed to the bed. Even methane, a liquid hydrocarbon or if a liquid hydrocarbon feed is injected into a mixture of gaseous and liquid coal, sufficient amounts of hydrogen can be formed immediately, is introduced into the fluidized bed 4 through the supply of gaseous decomposition products, vapors and line 8, where the 20 hydrogen to keep the solid particles in the vortex hydrocarbons at temperatures in the range of state. In this way, the dense 954 to 1093 ° C. bed of solid particles 4 can be decomposed to form hydrogen and coke deposits free of undesirable. A supplied in liquid form gases, particularly oxygen or oxidising gases, hydrocarbon feed can be maintained at 93-343 C ^G.

be preheated. Gaseous hydrocarbon solid coke particles from fluidized bed feeds can be heated to higher temperatures, e.g. B. formation of suitable size, z. B. petroleum coke or up to 649 ⁰ C, are preheated. Activated carbon can be supplied through line 19

The solid heat transfer medium will be in the crevice zone if it is necessary to replenish the solids.

and in the oxidation zone by means of a carrier gas. Consumed solids can be through conduction

which has a certain surface speed, 30 20 can be deducted.

held in the vortex. Under "surface speed for the reaction with the carbon deposits" is the air required for the outflow speed on the solids is preferably introduced into a zone corresponding to the speed of the gas from the reactor, which corresponds to the hydrocarbon gas speed in the reactor. Sufficiently separated from the cleavage zone to maintain the vortex condition will avoid partial oxidation of the hydrocarbon feed to solid particles with a particle size in the range. When operating the in F i g. 1 represented from 25 to 1000 μ by the carrier gas, which is a reactor, air is introduced into the lower end of the suction pipe 2 surface velocity in the range from 0.06 to, and this air converts the carbon, 3 m / sec., Preferably from 0, 15 to 0.91 m / sec., Which has deposited on the bed 4 through the line 5 in the form of a dense bed with a fairly large number of circulating solids, has kept a clear upper level, and there are oxides of carbon. The oxidation reaction also solid particles of this particle size in those in zone 3 is strongly exothermic and enables the gas velocities to be kept in a more dilute state, with temperatures above 1093 ⁰ C being maintained in the cracked state, with zone 3 in both cases. Over 75% of the heat requirement of the invention, the solids at least 20 percent by volume of the gasification process according to 45 are supplied by this oxidation of the carbon deposits, which is filled with the mixture of gas and solids.
Occupy space. The high temperatures in zone 3 favor borrowed solids cause a turbulent through-the formation of a high proportion of carbon monoxide in the mixture and an excellent heat transfer ratio to the carbon dioxide. The reaction in the between the zones. As a result of the turbulent oxidation zone 3 between the carbon and the mixing of the solids, the temperature fluctuation is gradual, while the perception (/ 1 T) in the bed 4 is kept small enough that the carbon initially turns into carbon dioxide, the formation of hot spots to prevent. Heat is oxidized. This reaction is very rapid and is conduit to the solids in bed 4 and is highly exothermic. As radiation from the tube 2 forms the walls of the carbon dioxide, a second reaction takes place in the vessel 1 and the solids flowing over from the tube 2 at the upper end between the carbon dioxide and carbon below it. About formation of carbon monoxide takes place. The second reaction, the upper outlet of the tube 2, can be an ablation, is endothermic, runs relatively slower. as the first reaction and is caused by high temperatures

Gaseous product temperatures from the vessel 1 through 60, preferably temperatures in excess of 1093 ⁰ C, the gas exit line 10 withdrawn. The product favors that it runs completely. The change consists mainly of the conversion to carbon monoxide formed in the pipe 2 and the temperature of the carbon monoxide and the free hydrogen rising from the bed 4 in the oxidation zone inside the suction pipe, which are therefore related to each other. The operation of the solids separation space above the zones 65 with each other, oxidation zone 3 and the need for premixing. This gaseous product flows through a heater depending on the carbon monoxide concentration or several cyclone separators 11 with inlet tration, the openings 13, dip tubes 15 for the return of the desired gas in the gas being formed. For the almost complete conversion of the

i 255

10

Atmospheric oxygen in carbon monoxide temperatures of 1205 ° C. and more are usually required if one wants to work with acceptable residence times in the oxidation zone. In order to achieve such high temperatures, the air should be preheated to 260 ⁰ C.

While gas, which mainly contains nitrogen and carbon monoxide, from the upper open End of the tube 2 flows out when air is used as the source of oxygen is used is almost in bed 4 by the cracking of the hydrocarbon feed pure hydrogen is produced. A relatively small amount of water is formed in the oxidation zone 3 by oxidation of hydrogen, which is at the solid coke particles has been absorbed. In the upper part of the reactor can be turned through the reversible Reaction of carbon dioxide with hydrogen also forms a small amount of water.

The oxidation zone is located within the vertical suction pipe 2 of FIG. 1 and is therefore separated from the hydrocarbon cracking zone; However, there is good heat transfer between the two zones. A large part of the heat generated during the oxidation of the coke deposits can be conducted through the pipe wall and then radiated into the surrounding bed 4 on all sides. In this way, a temperature in the range from 954 to 1093 ^° C. can be maintained in the hydrocarbon cracking zone 3 with only a slight temperature fluctuation within the bed.

Height and diameter of the suction tube 2 are for the highest efficiency of the oxidation Coal and coke deposits on the solids turn into carbon monoxide at a linear gas flow rate up through the pipe in the range of 0.91 to 3 m / sec. measured. At this flow rate hold the gaseous products, mainly carbon monoxide with a small amount of carbon dioxide, solids up to the top End of the pipe in suspension, where the solids splash into the surrounding crevice zone, causing them to this zone give off heat, so that the cleavage reaction is favored and fresh coke deposits form from the cracking of the hydrocarbon feed.

According to the invention, the vessel 1 is operated in such a way that carbon consumption takes place. A special Example of suitable operating conditions when the method is carried out in a device according to FIG. 1 is given in Table IV.

Table IV Working Conditions for Coke Consumption

Wide range until 1205 927 until 6.8 0 until 1.5 0.5 i to 1.22 0.15 until 907 45.5

More preferred until area 982 until 1093 1.36 until 3.4 1.0 until 1.5 0.3 until 0.76 136 454

Temperature, ⁰ C

Pressure, atü

Ratio of gram atoms C to moles O ₂ in the

feed

Surface speed, m / sec

kg solids / mole atmospheric oxygen / hour

40

45

Any form of coke or carbonaceous solids can be used as solids.

F i g. Figure 2 shows schematically a simplified system for producing coke to supplement the coke consumed in the gasification stage. The hydrocarbon feed, e.g. B. a heavy fuel oil is fed through line 56 and pre-coked in the vessel 50 at normal coking temperatures in the range of 482 to 705 ⁰ C in a manner known per se, the coker 50 only so much air is fed through line 54 that the heat balance is maintained. Then on the one hand the coke and on the other hand the gaseous products, mostly hydrocarbons with a smaller amount of oxides of carbon, water, nitrogen, etc., are passed through the lines 52 and 53 into the gasification vessel 60. Here the temperature is increased to the desired gasification temperature by adding more air through line 58. In this way, the gasification stage is always operated under coke-consuming conditions. Another advantage of this two-stage system is that the H ₂ : CO ratio in the gaseous product withdrawn through line 63 can be changed at will by withdrawing portions of the gaseous product from vessel 50 through line 55 or adding further hydrocarbon feed to vessel 60 through line 62 feeds. There is no heat loss because the overall balance remains the same.

example 1

Is in a gasification process, wherein a petroleum fraction having a high coking residue to C ο nr ads ο η gasified by injecting into a fluidized bed of coke, is oig achieves a 45 ° / ^e increase in the degree of conversion when under the same conditions of temperature and residence time, the Gasification is not carried out under coke separation conditions, but under coke consuming conditions.

Carbon extraction in a coke fluidized bed
at 1046 ^° C

55 Dwell time in seconds
Carbon extraction.

Coke consumption

10

1.57

Coke shed
manure

10

1.13

At 1093 ° C the following results are obtained:

Feed speed,

Parts by weight / hour / part by weight

Carbon extraction

Coke consumption

0.017
1.85

Coke shed
manure

0.017
1.74

709 707/527

These values are obtained at 35% coke consumption based on the feed. Depending on the C: O ₂ ratio in the feed, the coke in the reaction vessel can be consumed quickly or slowly.

Example 2

The operating capacity of coke in the reaction vessel is 14.016 kg. A heavy fuel oil with a flash point of more than 65.6 ° C, a viscosity of up to 87.6 ° E at 50 ° C and a specific gravity of 0.9820, a ratio of C: H of 8 is used as feed , 36 and a Conradson coking value of 16.0 percent by weight. The oil is introduced into the reaction vessel with an inert nitrogen stream 30 cm above the grate at a rate of 445 g / h. atomized. Air is the reaction vessel below the grate at a rate of 1.98 Nm ³ / hour. fed. This corresponds to a ratio of gram atoms C to moles O ₂ in the feed of 1.5 and a reciprocal throughput rate (kg C / mole O ₂ / hour) of 363. The temperature of the reaction vessel is 1038 ° C. The speed at the top of the reaction vessel, corresponding to the speed of the outflowing gas, is 20.4 cm / sec. The average composition of the dry product gas is as follows:

30th

H ₂ 8.8 volume percent

N ₂ 72.6 volume percent

CH ₄ 1.0 volume percent

CO 12.5 percent by volume

CO ₂ 5.1 volume percent

H ₂ O * 3.2 volume percent

* Based on moist gas.

This corresponds to a carbon recovery of 1.35.

The C: O ₂ ratio is therefore slightly higher in the feed than in the product. As a result of the losses caused by soot formation and entrainment, however, the coke level in the reaction vessel remains constant at around 13.6 to 14 kg.

The feed rate is now increased to 250 g / hour. lowered and the air speed kept constant. In agreement with previous experience, which was that the quality of the gaseous product only _{depends on the reciprocal oxygen throughput rate (kg C / mol O 2} / hour), but not on the hydrocarbon feed rate, occurs in the first 4 up to 5 hours there is no change in the nature of the gaseous product.

After several hours, however, the level of coke in the reaction vessel begins to drop significantly as a result of the excess oxygen, as a result of which the reciprocal throughput rate decreases. The expected deterioration in the quality of the gaseous product does not take place; on the contrary, the quality of the gaseous product is constantly improving. After 15 hours of operation, the operating capacity of the reaction vessel of coke is 10.115 kg and the reciprocal throughput rate is 260 kg C / mol O ₂ / hour. sunk. The dry product gas now has the following composition:

H ₂ 7.6 percent by volume

N ₂ 70.6 volume percent

CH ₄ 0.3 percent by volume

CO 18.8 percent by volume

CO ₂ 2.7 percent by volume

H ₂ O * 1.7 volume percent

* Based on moist gas.

This is a major improvement over the initial gaseous product and corresponds to a carbon recovery of 1.66. It should be noted that the CO concentration increased from 12.5 to 18.8 percent by volume, while the concentrations of CO ₂ and water decreased from 5.1 and 3.2 to 2.7 and 1.7 percent by volume, respectively are. This corresponds to an increase in the CO: CO ₂ ratio from 2.5 to 7.0. This improvement has been adjusted, despite the fact that the total residence time of the vapors in the coke by 30 ° / decreased _0th

Claims (5)

Patent claims: 1. A process for the production of carbon monoxide and hydrogen-rich reducing gas using temperatures in the range of 927 ⁰ C and higher by gasification of hydrocarbons that are split in a fluidized bed of finely divided solids in a cleavage zone with the formation of hydrogen and coke, the Coke is deposited on the fluidized bed solids and is then at least partially burned in a separate combustion zone with an oxygen-containing gas, characterized in that the temperature, the residence time and the ratio of oxygen-containing gas to added hydrocarbons are varied so that the ratio of carbon to oxygen in the hydrocarbons fed to the cracking zone and the oxygen-containing gas fed to the combustion zone is lower than the ratio of carbon to oxygen in the combustion products and the carbon of the coke in the fluidized bed is consumed more quickly d, when it is deposited there as a result of the splitting of the hydrocarbons, avoiding direct contact between the oxygen-containing gas and the supplied hydrocarbons, the used coke is supplemented by adding coke to the fluidized bed and the gaseous products from the two zones are combined with one another. 2. The method according to claim 1, characterized in that there is a dense fluidized bed Fluidized bed is used. 3. The method according to claim 1 or 2, characterized in that the hydrocarbons into an intermediate part between the upper main part and the bottom part and air into the bottom part of the fluidized bed and the gaseous oxides of carbon and nitrogen from the bottom part mixed with hydrogen and hydrocarbon gases in the intermediate part of the bed and this Gas mixture passes up through the main part of the bed. 4. The method according to claim 1 to 3, characterized in that liquid hydrocarbons are used uses and this by atomization with the help of a practically oxygen-free gas in the Introduces crevice zone. 5. The method according to claim 1, characterized in that there is a two-stage operation and the hydrocarbons are introduced into a fluidized bed coking zone maintained ^{at a temperature of 482 to 705 ° C. by adding an appropriate amount of air, the gaseous product} and the coke, which is in the fluidized state, then ^{passes into a gasification zone maintained at a temperature of 927 to 1205 °} C. and the air required for the consumption of coke is also supplied to the gasification zone. Considered publications:
German Patent Nos. 484 743, 642 526, 489,960 307; German interpretation document J 6511 / IV a / 12 i (published on May 3, 1956). 1 sheet of drawings 709 707/527 11.67 © Bundesdruckerei Berlin