DE2108434C3 - Process for the production of mixtures of acetylene and ethylene by thermal cracking of hydrocarbons and cracking reactor for carrying out the process - Google Patents

Description

From DT-PS 8 17 304 is a process for the production of mixtures of acetylene and ethylene by thermal splitting of gaseous and / or vaporized, more highly saturated hydrocarbons known with two to ten carbon atoms in a reaction space in which the required Heat of reaction in the reaction space by burning of continuously introduced into the reaction space solid carbonaceous fuel with oxygen or free oxygen containing gases as an oxidizing agent, and the fission products are then quenched. The hydrocarbon feed is not separated from the oxidizing agent and the carbon.

DT-PS 10 41 033 describes a process for converting gaseous hydrocarbons in a fluidized bed described. The solid phase of the fluidized bed consists of oil coke, that of liquid hydrocarbons when they are split in a fluidized bed at temperatures above 630 ° C is obtained. According to a preferred Embodiment of this process is the to be converted hydrocarbon at one point in the Introduced fluidized bed, at the previously added oxygen already completely or to the greatest extent Part with the oil coke reacted. With this

So have to drive to generate the oil coke vortex mixed with countercurrent heat exchange. There-

bed first liquid cooling hydrogen split at must an uneconomically high burn-up of the too

the secondarily produced oil coke then splitting and the split material being accepted.

be used as an energy source for the endothermic Spal- nommcn.

tion is used. So there are two vortex chambers 5 According to US-PS 27 07 148 air, steam are required. The indirect heat transfer used in this process and fissile hydrocarbons in succession enables the working temperature to be optimized continuously upwards through a coal bed flowing downwards. This cyclical hot and cold blowing table is not possible. heat, water gas are generated in the three switching cycles from DT-PS 10 81 448 a process for \ ₀ and fission product is generated. With regard to the coal autothermal cleavage of gaseous and / or hydrogen cleavage, this is therefore a discontinuously vaporized hydrocarbons with the addition of processes with the time characteristic that is typical for such processes - oxygen and possibly water vapor in the inert see - unfavorable.
Fluidized bed at 650 to 900 ° C known. The coal A process known from US Pat. No. 2,767,233, hydrogen and oxygen are introduced separately in a reactor to split hydrocarbons. E'.in part of the hydrocarbon mixture of combustion gases and fission products. The material feed is used to generate the required This process requires a downstream prochen heat for the endothermic cracking separation, which in principle can be avoided.
processing reaction consumed. In view of the increasing shortage of hydrocarbons known from US Pat. No. 2,790,838, this process is technologically unfavorable product processes uneconomical. Also, that shows as mixing. In addition, this process-heat exchanger serving fluidized bed requires unfavorably high ren an expensive energy supply, since the Erzeu temperature gradients. generation of abrupt temperature gradients is required. Another process for fluidized bed splitting of From US-PS 28 05 131 is a process is known from OE-PS 2 00 566 bc-25, in which hydrocarbons are known to soot and acene. The hydrocarbons and the oxidizing ethylene are split. The hydrocarbon stream medium is fed into the reactor at various points across a spiral upwardly rising gate. The combustion gas stream given up in the lower part of the fluidized bed and the oxygen introduced with it burns the fluid on top of the fluidized bed. At the optimal point of the ascending layer, coke deposited with heat generation. In the upper part of the fluidized bed heated in this way, reaction gas is withdrawn from acetylene and carbon black. The remainder is carried out by the cleavage. The fluidized bed part of the flow is worked up to soot and also has extreme temperature gradients. How by this process, the hydrocarbons are also in the process according to DT-PS 10 81 448, substances must be routed for the most part to soot and only to the small inert fluidized bed material in the cycle 35 ren part to acetylene,
the. Processes of this kind are uneconomical. I _n US-PS 28 85 199 for common Aufin US-PS 18 92 559 a method of cleavage would be of carbon, fuel and Oxidationsmittung described by natural gas. A flame generated from carbon tel a screw conveyor with inner and outer drilling and air radiates vertically after stanchions for the supply of fuel and Oxidaoben into a reactor. A turbulent natural gas layer 40 described medium. This charging device moves in countercurrent on the reactor walls and is not only expensive in terms of apparatus, but is also long downwards. In this turbulent layer, also unable to cleanly separate the glowing carbon particles, split the earth's hydrocarbon feed and the oxidizing gas into hydrogen and coal. To be carried out between the flaming agents.

electricity and the natural gas flow can flow upwards Nitrogen jacket are switched. As a result, driving to hydrocarbon splitting are known is a contamination of the resulting water - but that all known so far, including those in the Substance due to the combustion products of the flame in practice is relatively uneconomical prevents. In the cleavage reaction, essentially, both in terms of material and product Methane to hydrogen and carbon splintered current flow and the energy balance as well as des th. There are no unsaturated hydrocarbons outlay. Another source of contaminants educated. The economic efficiency of the known processes, which has to be controlled relatively carefully, lies in Genstronic technology requires a relatively high level of equipment and insufficient attention and optimization relative effort. the mutual influences and dependencies after the 55 th of the residence time spectra and the Temperaturver method described in US Pat. No. 2,413,407 the hydrocarbon to be split is split. On this "time-temperature dependency" introduced tangentially into a heated reactor and is more detailed below because of its great importance directed downwards in a spiral on its walls. The received.

The reactor is led upwards by a spiral For a better understanding of the state of the art

Flame heated. The cracking of hydrocarbons finds 60 principles belonging to the technology and the invention

held in the flame. Reference is first made to the drawings as the reaction product. It

Mixture of combustion products and fission pro- shows

received products. This material flow guidance is important. 1 a well-known cracking reactor with

due to the additionally required separation of technological combustion with assigned temperature-residence time-

It makes little sense. 65 spectrum,

According to the F i g described in US Pat. No. 2,498,444. 2 in section a storage container and a

Process are the combustion gases of gaseous charging device for the fuel

Fuels with the hydrocarbons to be split - a preferred embodiment of the invention,

3 shows, in section, parts of a Biennstotlejector according to a preferred embodiment of the invention, wherein the foot of the in F i g. 2 loading device shown is also shown,

Figure 4 is a flow diagram of fuel charging with the in F i g. 2 and 3 shown devices and a grinding device according to a preferred Embodiment of the invention,

5A shows the head of a burner partly in section and cracking reactor according to a preferred embodiment of the invention, which with the feed system the F i g. 4 connected,

FIG. 5B shows a section that is shown in FIG. 5A corresponding cut at the base of the reactor,

Fig. 6 shows a section along 6-6 in Fig. 5A and

Fig. 7 is a flow diagram of a collection system that is used with the sampling probe of the cleavage chamber F i g. 5 B is in connection.

In the figures, the same parts are shown with the same reference numerals. For the sake of clarity the individual parts are not shown true to scale.

In Fig. 1, a temperature-residence time spectrum is shown under the schematic representation of a reactor with pre-combustion. The ordinate shows the temperature of the reaction mixture in degrees Celsius, and the abscissa shows the residence time in units of see · 10 ^-3 . The length of the abscissa shown thus comprises a duration of _^3/1000 seconds. The zero point of the abscissa is placed in the center of the loading opening. The length and division of the abscissa is scaled to the longitudinal axis of the reactor. The reactor consists of a tubular chamber 1 with an inlet end 2 and an outlet end 3. Downstream and at some distance from the inlet end 2 there are several identical feed openings 4 for the hydrocarbon feed. Shortly before the outlet end 3, a quenching nozzle 5 with an inlet for the coolant 8 is provided. The material flow indicated by the arrow 6 is a gaseous heating medium, for example a combustion exhaust gas, which is fed in at the inlet end 2 at about 2210.degree. This heating medium is generated in a combustion chamber which is not shown and which is completely separate from the chamber 1. The material flow indicated by the arrow 7 symbolizes the hydrocarbon feed, for example propane preheated to 482 ° C. The propane is instantly mixed with the heating medium 6. It is immediately heated up by the heating medium. The hydrocarbon is heated in a preheater, not shown, which is also independent of the gap chamber 1. The reaction mixture stream 11 which forms in the steady state during continuous operation is directed towards the quenching nozzle 5. The hydrocarbons are split into acetylene and ethylene. The reaction mixture is instantly mixed under the quench nozzle with a stream of relatively cool quench liquid or gases. Water or a hydrocarbon is preferably used for quenching. The coolant flow is indicated by arrow 8. As a result of the quenching, the cleavage reaction comes to a standstill practically completely. The material flow 9 exiting at the outlet end 3 of the reactor is a mixture of quenching medium, reaction products and by-products.

The time of quenching the reaction mixture is indicated by the reference line 10, which is a plumb line is on the abscissa of the temperature-residence time spectrum and with the central axis of the quenching nozzle coincides. The exact definition and monitoring of the time-temperature dependency is due the influence of the pyrolysis temperature on the product composition is of great importance. This is how for example more acetylene at higher temperatures, while more at lower temperatures Ethylene is formed. Likewise, the formation of other products, such as diacetylene, carbon black or tar, is one Function of the pyrolysis temperature.

For each hydrocarbon feed and each assigned target composition of the fission products there is accordingly an optimal gap temperature.

The inventive method offers particular advantages in the production of mixtures Acetylene and ethylene. The relative proportions of acetylene and ethylene in the mixture of cleavage products can be affected to some extent by temperature, both the hydrocarbon feed as well as the resulting fission products is subjected. However, to the extent that it is not possible, the optimal one Working temperature, which corresponds to a particularly desired product mixture, during the process To keep the entire cleavage reaction uniform, larger amounts of undesirable Products. From the above it can be seen that it is useful for achieving high conversion rates of the feed material in a single pass, d. H. without material return, It is of great importance that this loading has the appropriate correct time-temperature dependency to subjugate. Accordingly, in order to achieve the desired product blend, the following operating conditions must be met are adhered to as far as possible:

a) The time required to heat the charge to the optimum temperature must be as small as possible;

b) during the course of the actual cleavage reactions the temperature of the reactants must be as constant as possible at the optimum Temperature to be maintained;

c) after the cleavage reaction has taken place, the reaction mixture must be cooled as quickly as possible will.

To the extent that the above conditions can be met, the decreases total time the hydrocarbon feed is exposed to temperatures, which produce undesirable products. In this way, a regular Maintain the time-temperature dependency, which then results in the desired mixture in the product stream from end products, for example a mixture of acetylene and ethylene.

A hypothetical idealized time-temperature dependence for the production of acetylene-ethylene mixtures, which are rich in acetylene can be seen on the basis of the dashed curve 12 in the graphic Illustration of FIG. 1 will be explained. The curve 12 begins at time 0 and at one Temperature of a little below 650 ° C, which is a

509685/180

represents a desirable upper limit for the preheating temperature of some of the hydrocarbon feedstocks suitable for the splitting. The hypothetical reaction mass and a selected hypothetical hydrocarbon feedstock to be heated practically immediately to the required cracking temperature of, for example 1730 ⁰ C. The temperature of the hydrocarbon charge therefore rises practically immediately from below 650 to about 1730 ° C. without the charge being exposed to intermediate temperatures for prolonged periods of time. The temperature of the charge is then held at exactly 1730 ^° C. for ^{practically 2.5 x 10 -4: 1 seconds.}

Following this, the temperature of the reaction mass and the fission products contained therein are reduced almost instantly to about 425 ° C, this value corresponds to a temperature at which practically no further cleavage reactions occur expire.

The time-temperature dependency shown by curve 12 is very desirable in and of itself, but cannot be achieved in practice for a number of reasons. First of all, no process is known by means of which it is possible to heat or cool the reaction mass practically instantaneously. Accordingly, the heating period and the cooling of the reaction mass require a considerable period of time, during which the hydrocarbon charge and at least some of the cleavage products formed are not at the optimal cleavage temperature, whereby undesired side reactions are favored and the yield is reduced. In addition, cleavage processes of the type described above are highly endothermic. That means every molecule of the hydrocarbon feed. which is split in the actual reaction zone, absorbs a certain amount of thermal energy from the surrounding reaction mass. This thermal energy absorbed by all the split molecules causes during the splitting reaction; considerable heat extraction from the reaction mass. If this knowledge is applied to the usual preheating process, in which the hydrocarbon charge is only heated by mixing it with preheated gases at the beginning of the reaction, it is readily apparent that when a selected volume is moved or weight fraction of the reaction mass downstream of the mixing point and as the reaction proceeds, that is, as the molecules of the hydrocarbon feed are broken down, the temperature of the reaction mass steadily falls. If, therefore, the feed temperatures and the flow rates of the gaseous heating medium or the hydrocarbon feed are set in such a way that the reaction mass has the optimum cleavage temperature at the beginning of the cleavage, the temperature of the reactin mass at the end of the cleavage has fallen significantly below this optimal value, whereby the process undesirable side reactions are favored and the yield is reduced during this period. The above information is based on the assumption that the Spahreakior is operated with high proportions of hydrocarbon feed to fuel + oxidizing agent, which represents very desirable operating conditions from an economic point of view. In addition, the temperature of the active compound falls during the course of the spalling action but also for other reasons. Vol any technical Spaltanlagi are borrowed Wärmcvcrluste to the atmosphere unavoidable. As a result of this heat loss, the reaction mass cools down, and while it is flowing through the reactor, its temperature is reduced

ίο reactor of the type described above, the average temperature To be able to keep the reaction mass at the optimal value, it is necessary that the Infeed temperatures and flow rates of the gaseous heating medium and the hydrocarbon feed set in such a way that the reaction mass assumes a temperature at the beginning, which is significantly above the optimal value and then towards the end of the reaction period to one Value drops, which is below the optimal temperature, as it is also due to the drawn out Curve 13 is shown in the graph. However, this leads to both the Hydrocarbon feed as well as the resulting Fission products take on temperatures for a considerable part of the reaction time, which are significantly above or below the optimal gap temperature, as can also be seen from the graphical representation results. However, this favors the course of undesired side reactions and both the yield and the thermal efficiency of the process are reduced.

Some known methods provide partial solutions to some of the technical problems discussed above. For example, it has been recommended that the temperature within the reaction zone of one with pre-combustion or partial combustion working Spal! - reactor by stabilizing the reaction mass diluted with steam. The temperature stabilization takes place at the expense of the thermal efficiency and the yield of high-quality fission products.

It has also been recommended that the temperature within the reaction zone of one with pre-combustion working fission reactor to stabilize that one already determined in the combustion zone temperature-stabilizing compounds evaporate, whereby they become part of the reaction mass and along with the hot combustion gases and hydrocarbon feed flow through the reaction zone. They are very different Metal oxides and metal salts have been proposed as such temperature stabilizers. By encapsulating such stabilizers in the combustion zone, the hot combustion gases Heat withdrawn and stored in latent form.

If then the hydrocarbon feed to the mixture of hot combustion gases and vaporized metal salt or vaporized Metal oxide is added, the ongoing endothermic cleavage reaction removes the mixture of combustion products and stabilizer steam energy and the stabilizer vapors condense, whereby the latent heat is released as sensible heat and thereby the heat generated by the fission reaction removed heat energy replaced. In this way, the temperature within the reaction zone can be stabilized. Although such a measure

11 12

nit contributes to the stable, efficient process for breaking carbon temperature conditions in the reaction zone rule, it requires hydrogen, especially to generate ace yoke the circulation of further material, ethylene, optionally mixed with ethylene In addition to the fuel and the hydrocarbons, they create the disadvantages discussed above Passing through the reaction system, whereby zu- 5 does not have. According to the invention, the charcoal Devices are needed, for example hydrogen feed during the cleavage reaction wise heaters, storage tanks, circulation pumps subject to a favorable time-temperature dependency. and the like, which are thrown around the temperature stabilizers, resulting in losses in yield to be able to have. of unwanted side reactions avoided In US-PS 31 56 733 and 31 56 734 is be ίο. In addition, according to the invention, mixed rubs, for the stabilization of the temperature inlaid from acetylene and ethylene with low Have energy costs per kg of end product produced in a dissociation reactor within the reaction zone, Finally, the inventive method and. electrical heating element from one end of the gap chamber to arrange to the other. By means of one of the cleavage reactor used for its implementation Such an electrical heating element, the reaction can have the advantage that the vertion mass for the endothermic Cleavage reaction running over the entire length of the reaction zone required thermal energy Heat can be supplied, as a result of which the transfer from the endo to the reaction mass is extremely rapid Fission reaction will wear heat consumed replaced. These tasks are carried out by the and thereby solved a stabilizing tendency towards discovery.

Temperature of the reaction mass is applied. At 20 The invention thus relates to the reactors in the sprinkler type, however, the heat is about the subject identified,
the walls of the cracking chamber on the hydrocarbons. In the process of the invention, the material charge is transferred and the heat overheating of the hydrocarbons to be cracked in the number of usable refractory materials is so small that the glowing particles are not present in technical systems of the carbonaceous fuel, which is usually a very bad time-temperature-dependent fuel. As a result, an extremely high level of quality is obtained. So although this proposal achieves thermal efficiency. The cleavage products of large experimental and theoretical inter- are obtained in high concentration. If you want to show that, with practical separation and purification, it is easier to maintain stable conditions of the reaction temperature, high yields of product will also be achieved if such desired precipitates can be suppressed in the reactor.
Measure hardly on the technical scale. From the foregoing considerations it can be seen that a bedif is made up of a fission process, 35 and a gaseous oxidizing agent continuously achieves it, both the hydrocarbons in one of all sides enclosed crevice zone feed as well as the crevice props formed from it. The fission zone is flowed through quickly, ducts of a practically ideal time-temperature-ab- The solid fuel burns in the presence, subject to dependency, without, however, the thermal efficiency, but largely separated from the coal mixture, is worsened, without 40 Hydrogen feed. In this combustion, the disadvantages and additional costs arise, the heat required for the cleavage reaction is released, which occurs in the circulation of auxiliary materials which, according to experience, is made possible by apparatus, can then occur if one summarizes the dilution with the fact that on the one hand the charging of the water vapor, the circulation of the hydrocarbons which break down oil, and the like are carefully used, whereby Another aspect of carbon-containing fuel and the importance of oxidation is that such a process should be separated from the resources, but that, on the other hand, the advantages shown at the same time should still have all three feed streams in the reactor when one is in the industrial scale 50 Direct current be performed without any work on which auxiliaries, such as those used, for example, in the In particular such an improved gap fluidized bed process would be used, processes of importance for the production of need to be used. This concept is not suggested by acetylene and mixtures of acetylene and ethylene, the prior art.
since the industrial consumption of ethylene is currently increasing, the hydrocarbon feed will increase more rapidly than that of acetylene. This or more streams separate from the carbon tendency is largely due to the fact that the material-containing fuel and the oxidizing agent are such that certain chemicals are no longer fed under the cleavage zone. Also the carbon-containing use of acetylene, but using fuel and the main part of the oxidizing agent preparation of ethylene as the starting material, are kept separate from one another until they get into di, with regard to the essentially Spallzone. The carbonaceous fuel stole reduced the cost of manufacturing ethylene. If the fuel stream is fed in in such a way that the stream of fuel, therefore acetylene, wants to retain its position as the starting material for particulate matter between the stream of the Kohler in the chemical industry or even improve the hydrogen charge and the stream of oxides, there are improvements in the fluid which means that there is a risk of a degree of clogging in acetylene production. Combustion of the hydrocarbon charge is essential. is set. The burning rate of the Brent The invention is based on the object of regulating a substance to the required extent

by determining the particle size, the preheating temperature of the air, which is mostly used as an oxidizing agent, the quantity ratio of fuel to oxidizing agent and the mixing intensity of fuel and Regulates oxidizing agent accordingly. In this way it can be achieved that the burn-up of the Fuel particles takes place over practically the entire length of the crevice zone. Preferably the fuel particles are on reaching the downstream end of the crevice zone practically completely burned, or at least until they leave the reactor. Shine like this the red-hot, burning down particles of fuel practically over the entire length of the Fission zone heats the hydrocarbon feed and thereby continuously replaces it Thermal energy of the reaction mass, which is generated as a result of the endothermic spait reaction has been withdrawn. When the particles of fuel to reach the downstream the end of the Spal! .zone practically completely burned down to ash and hot combustion gases recovery and further handling of the unburned fuel particles are also unnecessary. Due to the relatively low hydrogen content of the carbonaceous fuel, the Gases formed as by-products during burning off are only slightly contaminated by water vapor, entirely in the Contrasted with the use of most liquid hydrocarbon fuels. Hence the Water vapor partial pressure in the cleavage zone is relatively low, so that only relatively little of the hydrocarbon feed is lost due to the water gas reaction.

As can be seen from the explanations above, the burning of the fuel takes place practically separated from the hydrocarbon feed, but in the same fission chamber and practically in closest neighborhood to the hydrocarbon feed. Under the phrase "practically separated" It is understood that the hydrocarbon restriction while under the action of the burning off Fuel is exposed, but practically so far out of contact with the fuel and the oxidizer is kept from burning a major portion of the hydrocarbon feed is avoided. It is not necessary to specify the exact flow paths, the concentration gradients or lines of contact between the hydrocarbon feed streams. n Determine burning fuel and oxidizer to determine if the The above conditions are met, since in general hydrocarbons are much faster burn as the carbonaceous fuel. If that is any hydrocarbon fuel is in sufficient contact with a burning fuel and an oxidizing agent, so that ignition can occur, there is a violent competitive reaction with the fuel of the oxygen available for the burning process, and the question of whether the larger proportion of the hydrocarbon waste sufficiently separated from the fuel and the Oxidizing agent is maintained, can easily be answered by doing in a manner known per se the combustion products and the fission products are analyzed.

The invention also relates to a cleavage reactor with separate feed lines for the hydrocarbon feed to be cracked, the solid carbonaceous fuel and an oxidizer, with a fission chamber and quenching devices, the downstream and upstream located ends of the gap chamber are connected to one another by a wall. the Transverse spacing of these walls can vary from point to point over the entire length of the reactor, however, at least in that part of the gap chamber, which is upstream of the Quenching device is located, no sudden changes in cross-section occur, there should be there are no throttle-like constrictions and there should be wall roughness and protrusions be avoided, which an intimate turbulent mixing of the hydrocarbon feed and the fuel particles flowing through the fission chamber. The length of the Gap chamber can match the width, but it can also be smaller, and preferably it is larger than the width. The feed line for the The hydrocarbon charge to be cracked is connected to the interior of the cracking chamber via a nozzle device in connection which is arranged at the upstream end of the chamber. This Nozzle device includes a flow forming part which feeds the hydrocarbon feed into one Material flow transferred and this forward through the chamber along a flow path flings, which extends downstream in the gap chamber and one of the side walls maintains a certain distance.

The splitting aclor of the present invention is of this type characterized in that the flow-forming part of the nozzle device 50 is the greater portion of the Hydrocarbon stream constricts to a cross section which is less than about half the transverse Cross-sectional area corresponds to that part of the gap chamber 42, which extends up to the quenching device 110 extends that around the feed line 50 for the hydrocarbon feed, this at least partially enveloping or current-forming part 59 for the carbon-containing on the outside at a distance from it Brennsloff is arranged, which the carbonaceous fuel when introduced into the reaction space a component of movement in the main flow direction along the reaction space and optionally a second movement component directed perpendicular to this on the stream of oxidizing agent issued that around the feed line 59 for the carbonaceous fuel, this at least A flow-forming part 69 partially enveloping or at a distance from it towards the outside for the main flow of the oxidizing agent is arranged that within the gap chamber 42 a withdrawal condenser 44 of smaller cross-diameter than this chamber is arranged and that the probe is a in the hydrocarbon feed and opposite the mouth of the HinspisungsleiUing 50 inlet opening 105 for this charge has the fission products formed, and that in the fission chamber 42 in the vicinity of the sampling probe 44 passages 45, 104 for the combustion products are provided.

Preferably, the strombildcndc part consists of

15 ^v 16

the hydrocarbon feed practically from a sampling probe is a straight pipe Pipeline with a substantially circular-reduced cross-section, which is so in the reactor like cross-section and a ratio of length to that is arranged one or more inlet diameters of at least ons about 20: 1, with blown openings in the fissure chamber on one or more lines are located in a non-narrowed opening at the downstream selected points where the cone upward located end of the fission chamber opens, the concentration of the fission products is higher than the concentration and this opening on all sides at a distance from the center of the combustion products. Preferably having the side walls of the gap chamber. this is the point where the

For the quenching and the recovery of the fission products during the operation of the reactor within

The fission products below has practically the highest in one half of the fission chamber

the individual sampling probes described are particularly concentrated. In a fission reactor with

lasts, but it can also be another, on the stream - a practically cylindrical gap chamber with circular

downstream end of the gap chamber arranged round cross-section and one arranged axially

nete device can be used. Nozzle device for the hydrocarbon feed

Through the combination of the above-described effect, which is formed by an annular injection device Portions of the nozzle device are used to control the fuel and oxidizer to feed stream correspondingly narrowed, and that is given, the latter being on the upstream flow The far end of the chamber is the duck of the carbonaceous fuel Movement component, soft from the direction of the probe, preferably in the longitudinal axis of the of the feed stream is directed away and therefore disposed 20 gap chamber, namely downstream helps keep the hydrocarbon streams flowing from the hydrocarbon feed nozzle and sending the burned fuel, the inlet opening of the discharge opening the distance over the entire length of the gap probe in the direction of the feed nozzle for the con-chamber, is oriented upstream of the quench hydrogen feed so that the are practically separate from one another. 25 Fission products directly in-also without changing direction in that the feed line can step for the. The inlet port and the pipe The fuel supply line for the coal preferably has a smaller cross section Hydrogen charge at least partially enveloped than that part of the gap chamber in which and they are arranged between the feed lines for the coal. The smallest distance hydrogen charge and oxidizer 30 are located at the hydrocarbon feed nozzle is, it succeeds. the flow of coal feed and the inlet port of the sampling probe Hydrogen charge upstream of the oxidizing agent is determined by the rate at which the while at the same time the greater part of the rather the hydrocarbon feed and the dar-oxygen is consumed before any noticeable fission products formed through the fission chamber Diffusion between the hydrocarbon feed 35 flow, and it is also determined after the clogging and the oxidizing agent can take place. dwell time, which for a complete expiry of the Though the cleavage reaction is required in practical implementation. The maximum distance The flow of the hydrocarbon feed, on the one hand, is determined by the route along which and the combustible fuel and hydrocarbon feed streams and of the oxidizing agent, on the other hand, does not exit via the cleavage products formed and the streams entire length of the fission zone practically completely fuel, oxidizing agent and combustion samples are present separately, namely in the form of ducts, practically separated from one another and in a secondary physical manner separate streams, is readily flow through the fission chamber to one another. Inside it can be seen that the above-explained conditions of the gap chamber and adjacent to the inlet ducts the practical separation also then 45 opening of the sampling probe, which it preferably are already abundantly fulfilled if only a small one is at least partially surrounded by a circle Portion, i.e. less than about 20% of each stream, there are passages which form a flow path, as a result of the measures explained above, which differs from the one by means of which mix together by diffusion. The formed cleavage products are withdrawn, and measured the diffusion between the individual product 50 which the combustion products from the inlet streams can be forwarded by means of an analysis of the exhaust gas opening of the sampling probe. In the pipe and the fission products using the usual sampling probe and preferably close to one another Calculate formulas and approaches, or there are devices to the inlet opening The extent of the diffusion can also use radio- to deter the fission products, which are caused by the experimentally determine active lead isotopes. 55 extraction tube can be withdrawn. Preferably isi

The sampling probe according to the invention is also used to provide a way to within the dei

Product withdrawal or product withdrawal. The ent-walls of the tube of the sampling probe one

acquisition probe can circulate cooling liquid in any fission reactor, whereby it is urr

are used, in the operation of which the quenching liquid can act in the same. The development

Reaction chamber practically separate flows of 60 sampling probe is connected to a device

Fission products and combustion products, which result in a regulated negative pressure difference

beard flow to each other. between the interior of the reaction zone and the

The sampling probe can be erected particularly well when the inside of the pipe of the sampling probe

use a reactor in which a stream of receives, thereby enabling the split pro

Combustion products is produced, which indicts preferentially over the combustion gas ^

at least partially a practically separate stream and the ash formed in this tube of Ent

the fission product envelops. The above-explained pickup probe can be collected.

Fissure reactor belongs to this type. In general, the invention can be used

Carry out cleavage processes with all flowable, aliphatic and alicyclic hydrocarbons. "Flowable" here are hydrocarbons that are either are gaseous or vaporous, liquid or even solid or semi-solid, but which are either in their natural state or after appropriate pre-treatment, e.g. by heating, Atomizing, diluting and the like, can be converted into a form in which they can be easily pumped and transported in a flowable state through corresponding conduits and then into the above explained procedures can be fed in.

Preferably, however, hydrocarbons are used as the starting material, which are in the gas or in a vaporous state fed into the fission chamber. The term "hydrocarbon" or "more saturated hydrocarbon" refers to any aliphatic or alicyclic Hydrocarbon or a mixture of such hydrocarbons, the atomic ratio of which is hydrogen to carbon is higher than that of the fission products. For making mixes the hydrocarbon charge consists of acetylene and ethylene for economic reasons essentially of one or more aliphatic saturated hydrocarbons with at least 2 and up to 10 carbon atoms in the molecule, namely from ethane, propane, butane, isobutane, pentane, hexanes, octanes, nonanes and decanes. Also commercial hydrocarbon mixtures obtained from petroleum, such as naphtha or liquefied gases, as well as in Gaseous hydrocarbons produced as a by-product of the refinery are also used as feedstock applicable. The method according to the invention can also be carried out with methane; however high To achieve yields of acetylene and ethylene it is generally desirable that the hydrocarbon feed contains greater proportions of higher hydrocarbons than methane, especially hydrocarbons with 2 to 10 carbon atoms in the molecule. Of course, heavy starting materials can also be used to produce other end products be used.

Any finely divided, combustible, solid material consisting essentially of coal and having a particle size corresponding to a mesh size of about 250 microns or smaller is suitable as the carbonaceous fuel used in the context of the invention. Such fuel is characterized by a hydrogen content of less than about 15 percent and it must be free flowing or it must be capable of being treated to become free flowing. For example, ground hard coal, degassed coal or low-temperature sulfur coke are suitable as fuels. It is an advantage of the process of the present invention that it can economically utilize fuels with widely varying ash contents, but best performance is obtained using coal which forms ash with a relatively high melting point; It. With a melting point of more than about 1650 ° C. Such types of coal are easily accessible. In addition to the solid fuel, a fuel gas can also be used in relatively small proportions, for example in an amount which does not provide more than 20 ⁰ O of the total heat value of the mixture of solid fuel and fuel gas. This additional fuel gas can either be fed in separately from or together with the solid fuel. In the context of the invention, one could also use liquid fuel oils, but it should be understood that gaseous fuels are easier to handle. The use of such an additional fuel gas can be important if during the start-up phase of the reaction

keep the combustion process steady during operation shall be. However, once steady-state temperature conditions have been reached, one can turn off the additional fuel gas, and the reactor can then practically only with the solid fuel

be operated, with the exception of a very small, gas-fed lure flame, which is the ignition facilitated.

In the process according to the invention can be used as an oxidizing agent Containing air or free oxygen

ao tendes gas can be used. With a particular advantage air is used. However, special advantages can also be achieved, in particular a high concentration on the desired cleavage products in the product stream when oxygen is in the oxidizing agent is in a higher concentration than in the air. Therefore can be used as an oxidizing agent in the framework According to the invention, oxygen-enriched air or pure oxygen can also be used.

Any flowable fluid can be used for quenching Material can be used, which the formed fission products or the inner lining of the Does not damage the reactor or the collection system. Very often water is used for this purpose used. However, flame-retardant, heat-resistant hydrocarbon oils can also be used will. In addition, gaseous substances, in particular gaseous hydrocarbons including recycled from the hydrocarbon feed itself or from the cracking reaction

refrigerated products can be used for this purpose.

The most varied of factors are of influence for the practical mode of operation, for example the type of fission chamber in which the reaction takes place, the type of flow and the flow velocity the different materials, the temperatures and pressures used, as well as the Type of deterrent and the dwell time.

The reaction chamber is usually designed inside in the form of a cylinder, usually in the form of a longitudinal cylinder. The term "cylinder" is understood here in the broadest sense, d. That is, the reaction space in question need neither have a circular cross-section, nor it must have perfectly straight or parallel side walls. The reaction chamber should be equipped with a high-temperature-resistant, fireproof material be lined, which is also erosion-resistant, such erosion from the high gas

fio velocities, from the friction of the solid fuel particles and from high temperatures in the range of 14 (S (I ⁰ C and higher. Such refractory masses are commercially available. A pourable,

fi5 refractory mass with a high content of alumina proven. The fission chamber itself and the feed lines for the fuel and the oxidizing agent are preferably dimensioned and

lerart arranged that the fuel and the oxylating agent closely adjacent to at least one side wall of refractory material through the gap chamber flow through.

The hydrocarbon feedstock that solid fuel and oxidizer flow jolly minded, d. H. in the same direction through the reaction chamber. Use of the expression "Electricity" on solid fuel particles may seem inappropriate at first, as this expression is am Often used to describe the flow of liquids or gases. Nonetheless This expression is used in the present case to indicate that the solid fuel particles in practically uniform concentration or distribution along a given flow path move.

At the feed points, the hydrocarbon feed streams, the fuel and the oxidizing agent are completely separate from one another. It should be noted, however, that a low or limited degree of mixing is possible and in some cases before the cleavage zone is reached Cases is even beneficial. For example, some of the oxidant can be added prior to feeding of the solid fuel particles in the fission chamber are mixed with these particles as long as only the Most of the combustion itself takes place within this chamber, d. i.e., part of the oxidizing agent can serve as a gaseous transport or distribution medium for the fuel particles. If heavy hydrocarbon feeds are used, a small amount of the oxidant can be used serve as the spray medium for this charge. However, it must be pointed out that only a relatively small proportion of the total oxidizer is used in this way for spraying hydrocarbon feed and that every effort is made must allow diffusion between the main oxidant stream and the hydrocarbon feed stream as much as possible. Therefore practically the total amount of the oxidizing agent, with the exception of those proportions which are intended to support the supply of the feed and the fuel to the cleavage zone, in such a way fed into the cleavage zone and passed through it that the flow of the Oxidizing agent moved practically completely separately from the stream of hydrocarbon feed, until both material flows have been diverted into separate recovery zones, or until they are quenched or otherwise cooled or treated so that no reaction between to them more can take place.

The solid fuel particles are fed in such a way that they form a stream that is between the hydrocarbon feed stream and between the oxidizer stream or streams moving forward. The fuel particles have in addition to their velocity component in the longitudinal direction a velocity component perpendicular to the axis of the fission chamber, which is inclined against the direction of flow of the oxidizing agent. By means of this vertical speed component is achieved that the solid fuel particles gradually into the stream or the Diffuse in streams of oxidizing agent.

This results in a gradual burning off of the solid fuel particles, the burning process taking place extends from one end of the cleavage zone to the other. The vertical component of speed is in relation to the speed factor of solid fuel particles in the longitudinal direction relatively small, but on the other hand must be sufficient to contain practically all of the fuel particles in the Divert stream or streams of oxidant before reaching the end of the cracking zone is.

When the hydrocarbon feed streams moving side by side and practically separately and fission products formed therefrom or from the burning solid fuel particles reaching the end of the cleavage zone where quenching takes place, it is no longer necessary required to keep the flows separate, although certain economic and technical Advantages accrue if the streams are also separated during and after quenching remain, as will be explained in more detail below. So although it is possible to use both the Fission products as well as the combustion gases together to quench in a way that an intimate turbulent mixing of the quenching liquid with both the fission products and the combustion gases takes place and so the identity of the individual streams of material is destroyed, it is preferred to withdraw the fission products from the reaction chamber separately from the combustion gases and only to be deterred immediately afterwards. This also enables the fission products to be extracted economically facilitated and at the same time the thermal efficiency increased, because then the combustion gases Can be used as a heating medium in heat exchangers, reheaters and the like.

Those types of flow which allow the maintenance of separate stream flows in the hydrocarbon feedstock and the oxidizing agent can be easily implemented. In the case of the hydrocarbon feed, the flow is linear very functional. The flow of the oxidant should be somewhat turbulent, but not at all so turbulent that it destroys the character as a separate stream or a diffusion along the Axis of the gap chamber is favored into the hydrocarbon feed. It's the professional known how he can produce gas flows by regulating the gas velocity and by means of a smooth flow path, which through a practically perfect linearity or any desired degree of turbulence are characterized.

Depending on the dimensions of the cracking chamber, the feed rates of the hydrocarbon feed and the oxidizing agent vary within a wide range. The dimensions of the gap chamber itself can also be changed without Disadvantage with regard to the implementation of the method can be modified within wide limits. For one ^ Fission chamber of given dimensions and for a given residence time, for selected ones to be maintained Temperatures or pressures, those skilled in the art can easily determine the correct feed rates calculate for oxidizer, hydrocarbon feed, and solid fuel. The residence time for the hydrocarbon charge should be in the range of 0.1 to 0.0001 Sc-

21 over 434/77

21 ° 22

announce lie. The values to be observed in the cleavage zone for a discussion of the importance of temperature

Temperature and pressure conditions are according to - in the individual zones of the reaction chamber it is

still to be discussed in detail. advantageous to define certain zones in more detail:

Although it has already been explained above that the outer preheating zone for the oxidizing agent; it is not practical to have absolute limits for the outer preheating zone for the hydrocarbon feed rate the feed into the reaction zone; the inner preheating zone for the coal to be fed in Specify material flows, hydrogen loading; the actual cleavage zone and but certain general conditions relating to the quench zone. The outer preheating zones are on the relative Volumenzufuhrgeschwindigkit separate chambers outside the actual be made. The fuel and the oxidation chamber, in which the preheating of the medium in question products fed in should take place in such a ratio. It can be about that a stable flame is created. For each heat exchanger, furnace or the like. Act in welvorvorgenden Reactor lets the hydrocarbon feed and the oxynis get the right proportions easily determined empirically. The one here in the control medium before it is fed into the cleavage chamber The reactor described in more detail could be preheated separately with 15.

operate with adequate flame stability, preheating the stream of oxidant Taking the fuel and the oxidizer is very beneficial and can even be of the greatest leg approximately stoichiometric proportions, which should be significant if the oxygen concentration in Air is low at about 80 to 150 per cent of that speed of the oxidizing agent. If required, which is theoretically necessary 20 is therefore an external preheating for this purpose, to provide a stoichiometric mixture of Sauers'.off zone for the oxidizing agent. Preheating and produce fuel. The correct supply temperatures for air are in the range of about rate for the hydrocarbon feed- 90 to 1095 ° C, with temperatures in the range In practice, one can determine the heat dissipation of about 260 to 815 ° C to be very effective used fuel-oxidant mixture 25 have proven appropriate.

calculate and then using known paths of the endothermic character of the intrinsic

Rules of thermochemistry and thermodynamics of the cleavage processes borrowed can have certain advantages

estimate the amount of feed material, also obtained by taking the hydrocarbons

which preheats to a temperature by means of a predetermined amount of material charge

Can pyrolyze fuel and oxidizing agent. 3 ° which just barely any unwanted decomposition

In any case, however, the optimal proportions and thus blockage of the preheater can occur. the

of hydrocarbon feed, oxidizing agent Hydrocarbon feed should therefore be preferred

and fuel can be determined empirically. be heated wisely to a temperature which

Certain advantages arise when the relative velocities of hydrocarbons are somewhat below the actual fission temperature. For this purpose, an outer preheating zone is provided for the stock feed stream and the burn-off stream. For many hydrocarbon charges, solid fuel and oxidizing agents, suitable maximum temperature currents are kept under control. If you have temperatures in the range of about 538 to 816 ° C.
the velocities of the individual material streams The inner preheating zone for the hydrocarbons aligns as closely as possible, the loading is the upstream boundary surface slide and the turbulence between the end part of the gap chamber, in which the hydrocarbon stream preheated outside the individual material streams to a smallest gap chamber reduce possible value, and diffusion even further up; is heated to the cleavage temperature. In the course of the invention, the hydrocarbon feed into the stream can be used to deposit hydrocarbons of the oxidizing agent with a corresponding charge which, as acetylene cleavage products, is produced as a result of loss of combustion, or mixtures of acetylene and ethylene are formed. If the loss of the coal in the range of 816 to about 1927 ° C caused by a mixing at the should, in the inner preheating zone to temperatures interfaces, is very critical, it can be, with temperatures in the range of about be 109] geous, the flow rates of the ex 5 "are particularly preferred to 1760 ⁰ C. After derr burning stream of fuel and coal fed into the cracking chamber, the temperature should lenwasserstoffbeschickung to keep roughly the same, ie, the hydrocarbon feed as soon as The difference in the flow velocities, up to the above-mentioned target temperature, may not be more than about 20 ° / o. This area will be heated up.

pointed out that the relative flow 55 The actual fissure zone is that area de

The speed can be regulated without the rela-gap chamber in which the hydrocarbons are located

tive volume velocities of the incineration charge based on the actual gap temperature

gases and the hydrocarbon feed. The temperature of the hydrocarbons

have to be changed by simply placing the flow in the center or near the center

Measurement cross-sections of the individual material flows from 6 ° of the center of the product flow

changes. In this way you can get the desired one, preferably near the upstream:

Equality in the velocities of the flow of the end of the fission zone. Near the the Kohler

burning fuel particles and the stream of hydrogen stream surrounding stream of the burn off

Achieve hydrocarbon feed without the fuel particles can temperatures gemes

quantitative and thermal equilibrium between 65 _S en, which are higher than in the actual

the amount of hydrocarbon feed to a minor stream of hydrocarbon feed. Ma

on the one hand and the quantities of fuel and oxidation must therefore be careful that really di

medium on the other hand must be disturbed. Hydrocarbon feed temperature, un

/ If

light about the flame temperature of the burning down of hydrocarbon gases and / or vapors

Fuel particles is measured. to create. Reduce such unstable flames

It is of the utmost importance that in the actual thermal efficiency of the cleavage reaction and If the fission zone lends the temperature in the coal flow, the yield of the fission products is also achieved The hydrogen charge is stable, so that the 5 is down, as it has been in the meantime again and again correct time-temperature dependency realized flow of hydrocarbon feed penetrate, which leads to the highest yields and thus, surprisingly, it has been shown that it leads to the best thermal efficiency. In the scope possible using solid, carbonaceous fuels of the invention, care is taken to produce long flames in a crevice zone the rate of heat release from the io gen, which are extraordinarily stable, thus creating so-electricity of the burning solid fuel, the thermal efficiency as well as the austerity equal to the speed of the heat prey to be improved.

as a result of the fission reaction and the usual

Heat loss is kept. In this way, solid, carbonaceous fuels are formed

It shows that both malcrial currents are higher than the emissivity as a result of a burned flame

exchange of energy through radiation and other flames produced by hydrocarbon gases.

Heat transfer mechanisms between the det. Accordingly, the glowing, hot

Fuel flow and the burning, burning particles of such solid fuel

Hydrocarbon feed stream on each substance heat at a greater rate

desired temperature can be maintained. * ° into the hydrocarbon feed stream,

Solid fuels have at least three different types of hydrocarbon gas with demdenc Benefits on making them hydrocarbon the same amount of thermal units. It was already gasses or hydrocarbon vapors discussed above how important it is to have electricity are, which per se for the same purpose cinge the hydrocarbon feed within the inserts can be. First of all, the outer preheating zone allows you to access the as quickly as possible Turn of finely divided, carbonaceous gap temperature is heated. The high emissive fuel the regulation of the combustion capacity of the solid, carbonaceous burning rate within a wider range. Flame generated by substances favors such a thing In contrast to gaseous hydrocarbons, it heats up more quickly than the flame of a carbon dioxide namely carbon-containing solids 30 hydrogen gas or a vaporous fuel, grind easily to different particle sizes if the solid fuel used is a high one and the rate of combustion has the same solid ash content as most coals Substances is made quite significantly by changes in the case, certain advantages result from it, the particle size influenced. Therefore, if the feed rates of the coheine can be determined Combination of the adjustment in the particulate hydrogen feed, the oxidizing agent size of the fuel, the preheating temperature of the and the solid fuel such an oxidizing agent on each other and the mixing intensity can be controlled so that the temperature below the fuel and oxidizer the burnup melt temperature of the solid fuel speed of the fuel is kept within a white-formed ash or below the th range, and thereby the 40 melting temperature of other solid burn-up rate also easier of the fission products, whereby this rule for practically every speed adapt than that applies to gaseous or part of the preheating and gap zones vaporous hydrocarbon fuels which these material streams flow through. If Case is. on the other hand, temperatures above the melting temperature - however, so that the above-described temperature of the ash can be applied, everyone tends Adjustment between burning speed and object within these zones, which one Fission rate practically over the entire temperature lower than the melting temperature of the Realize fissure zone, it is necessary that ash has, in order to have a coating on it a long and steady flame is formed. Which forms from caking ashes, which on Gap chamber can have a length which increases in strength until a still permissible equal weight larger than its diameter. So that the weight thickness is reached, or the flow of material Flame over the entire length of the cracking chamber through the reactor is generated by the low-ash heat on the hydrocarbon feed is so hindered that finally the plant radiates, it is necessary that this flame is voluntarily or involuntarily in order to remove the 55 ashes must also be switched off over the entire length of the gap chamber, or that stretching to measure. If you try to hit such a long flame you have to pick up the ashes Hydrocarbon gases and vapors to generate the operation of the cracking furnace continuously or gen, it turns out that it is extremely difficult to remove at intervals. If from irwenn is not even quite impossible, with one day for whatever reasons above the melting tempionaries To let the flame burn, at least below 60 temperature of the ash must be worked, so is a those conditions which, in a split, grew the ash layer to a level prevalence. Still permissible under a stationary flame as long as the weight with the a flame is understood, which to a very ash layer covered parts are only so big that a high degree of practically a uniform length - there is still enough room for it to continue and shows practically no lateral flickering. 65 whose material flows, except for the ash, through or Flickering, unstable flames will be able to flow past them, even if they are hold when trying to put a longer flame in an ash layer of equilibrium thickness on that of one Has knocked down the hydrocarbon fission chamber by burning parts. Switching off the

/ 15

\ nLocation at certain time periods must be avoided as far as possible, since long-lasting measures are required to cool the reactor chambers * lined with a refractory material and then reheat to the required reaction temperature. If desired Reactors can also be used when working at temperatures above the ash melting temperature will have soft devices for the continuous removal of ash deposits. However, it is always easiest at temperatures below the melting temperature of the Ash to work, and therefore such an operation is preferred within the scope of the invention. If this temperature limit is observed, the ashes show practically no tendency to show up the walls or the quenching devices in the quenching zone or on the sampling probe precipitate, and therefore there is no need to remove appropriate precipitation.

The quenching zone is that part of the cracking chamber or an adjacent chamber in which the cleavage products formed are cooled well below the actual cleavage temperature. This cooling should take place as quickly as possible. In general, the cleavage products are up to Quenched at a temperature of 427 ° C or below. Preferably, the temperature of the The quenching liquid, the flow velocity and the mixing intensity are regulated in such a way that that the temperature of the fission products and / or the combustion gases up to at least about 260 ° C is reduced.

The method of the invention can be carried out at superatmospheric pressure, at atmospheric pressure or at can be carried out under atmospheric pressure. Working at is of course particularly convenient Atmospheric pressure. Under special conditions, however, higher yields are achieved if operates at a pressure of less than one atmosphere.

It is known per se to those skilled in the art what residence times are required in order to convert a wide variety of hydrocarbon feedstocks into desired products. The residence time is understood to mean that period of time in which the hydrocarbon charge and the cleavage products formed therefrom are exposed to the actual cleavage temperatures. In general, residence times have proved of about 10 ~ · to 10 ~ ⁴ seconds as appropriate. Under certain conditions, that is, when very low residence times are used, it can be difficult to get the hydrocarbon feed stream and the burning particulate stream to travel at about the same linear velocity and also to get the solid fuel to travel within the same amount of time Fissure zone burns off completely. In the context of the invention, the burn-off process can therefore also take place outside the actual cracking zone, namely before the solid fuel is brought together with the flow of the hydrocarbon feed and / or after the cracking reaction is complete and the cracking products formed have been separated from the fuel. It is particularly expedient if at least the main part of the solid fuel burns off in the presence of the hydrocarbon charge. If some of the fuel is burned to the end after leaving the cracking zone and after separating the formed cracking products, such a burning process can be facilitated if additional oxidizing agent is injected into the flow of the combustion products. Of course, it is easiest if virtually all of the solid fuel burns in the presence of the hydrocarbon feed. In this way, the greatest advantages with regard to an energy exchange of the radiant heat between the flow of burning solid particles and the flow of the hydrocarbon feed can be realized, and such a mode of operation is therefore preferred within the scope of the invention.

The end products preferably produced according to the invention are acetylene, ethylene and various combustion gases. In general it is among the Under the prevailing conditions the experiment was not particularly economical, only acetylene and no ethylene or vice versa. By changing the ratio of hydrocarbon feed to solid fuel or by changing the temperature in the cracking zone or by varying the Residence time or a combination of all of these factors and / or other operating conditions however, the ratio of acetylene to ethylene in the cleavage products also change accordingly. Which ratio of acetylene to ethylene is actually chosen depends on complex economic factors Variables, and in particular, the purposes for which the product stream formed is finally used and what measures to separate the acetylene and ethylene from the Combustion gases are applied.

Acetylene and / or ethylene can be removed from the drain by any means known per se separated from the gap chamber and, if desired, further cleaned.

However, it is preferred that practically all of the acetylene and ethylene be in one stream from the fission chamber subtracted, which contains less than half of the combustion gases generated, and the The rest of the combustion gases leave the cracking chamber as a separate stream. The acetylene and ethylene The product stream containing is then treated in a manner known per se to remove the unsaturated products separated from the combustion products. For example, absorption is suitable for this, selective chemical reactions, high pressure distillation, solvent extraction and others known measures.

Particularly preferred configurations of individual system parts are explained below with reference to FIGS. The FIGS. 7 to 4 to a supply device for the solid fuel, FIGS. 5A, 5B and 6 to the actual thermal cleavage, and FIG. 7 to a collection and recovery system.

A feed device for the solid fuel particles, which enables them to be in the form of a supplying extremely uniform flow of the burning device is extraordinary This is important so that a stable flame is obtained in the fission chamber. The trouble, what in test systems of small dimensions since, have certainly contributed to that

11th 28

cracking reactors working with solid fuels as well as a feed screw 27 in the outlet pipe 28 are strengthened with regard to their further development for practice, this screw having caused difficulties with the bottom part of the past. of the reservoir is in communication. Also in the present invention, in the setting gears and thrust bearings 24 is preferably the initial stages of development, great difficulties with a variable speed drive are able to reliably supply the solid bonds, thereby observing the rotational speed of the fuels. The problems of such a feed screw regulate and thus the discharge uniform fuel supply can be adjusted at low speed of the fuel particles, were particularly great because the ratio of Abmcs- pulverized coal, which is suitable for boiler firing solutions of solid particles to the dimensions of the io and of the generally 60 weight feeder, the more it decreases, the smaller the percentage of the size of the feeder through a sieve of the clear mesh size. The 75 microns pass through and which can be used as fuel in the context of the irregular and, in some cases, the invention observed, cyclical fluctuations in the feed rate - has a schülwinkel of 90 °. The solid fuels must then lead to experiments, therefore precautionary measures must be taken so that mental end results, which are essentially related to the feed screw 27, do not run empty. The stirrer 26 differentiating those that could be obtained serves to keep the bulk density of the solid constant when very stable feed conditions are realized, regardless of the amount of solid in the could. Precisely the storage container 22 aimed at according to the invention. This in turn enables low dwell times in combination with the 20 es, the discharge rate of the solid fuel to keep. The stirrer is used particularly urgently. The heat transfer from also to prevent the formation of bridges, which an annular combustion zone could cause to a cleavage zone located in the center before fluctuations in the discharge speed, depends on the size of the solid fuel.
Luminosity or the radiation capacity of the flame, the feed screw 27 has two different ones, which in turn depend on the concentration of the solid, sections, the upper section of conical carbon-containing fuels in the carrier air being frustoconical and depending on the flow as a feed section. A rhythmic s: Ji operated forward. The lower section of the feed screw shows the flow of fuel particles, the formation of threads of equal solid agglomerates in the feed and transport diameter over the entire length. The person skilled in the art is familiar with the system and the occurrence of blind spots or how he can change the dimensions, congestion zones in the transport system, which enables the best results to be achieved. The irregularly accumulated solids and then expelled from the dimensions and properties given above lead to an overall increase in such a feed screw, however, they have proven to be very useful for practical purposes. Preferably, such a gap system has. The feed system for the solid fuels, which is wound here as a ratio of the transport section of the screw, is part of the present invention from pitch to screw diameter of 1: 1, since none have been used to date. The section has a suitable diameter of 38.1 mm, also suitable on a test scale, and is 30.48 cm long and has a grain direction that has been known to allow pressure ratio (ratio of the depth of the flow of fuel particles acquisition channel to the depth of the discharge channel) of about 0.79 to generate in systems of small dimensions. The spacing of the threads from and to be maintained, and since such a continuous housing wall is 0.127 mm inflow on the inlet side, an essential precondition for the practical and 0.178 mm on the discharge side. Both the table implementation of the inventive screw itself and the cylinder 28 are out of action. a commercially available hardenable tool-The according to the invention feed device for the stahl is produced and then solid fuel particles are reached, which are shown in FIG. 2 shows a Rockwell hardness C (cf. ASTM E 18-67) of. can be fixed in any way, 5 ° 62 to 64 heat treated. The base, which is preferably attached to an overhead feed screw, has a backing 20 which is mirror-like attached by polishing by means of a number of surfaces formed. The screw is suspended in such a support system, including one designed so that per hour at 25 to 100 revolutions weight measuring device 21 is, for example, 4.53 to 18.14 kg of fuel per minute discharged in the form of a tension and strain gauge. It can be 55. The ever decreasing depth is known that such measuring devices one of the discharge channel of the feed screw has the we-load or a voltage in an electrical signal kung that the coal captured by the screw can convert during the passage hanging on it from the head of the pipe 28 up to which weight is equivalent. This electrical signal can be more and more compressed at the end, so that the ^{fuel can then be passed on to a remotely positioned indicator} or 6o fuel when it reaches the discharge end of the control device, so that the screw is very close to the thread-fermenting discharge speed of the fuel. packs is. In this way an intrusion is shown and regulated. On the air supply container 22 from the outlet end to the intake end dei, an electric motor 23 with a reduction worm is largely avoided, and thus a gearbox and a thrust bearing 24 are arranged. The ⁶ 5 NEN, corresponding variations in the off bearing 24 is of a suitable Kupplungsvorrich- carrying speed of the solid reducing be tung connected to a shaft 25, is at the turn the discharge end 28 having a Düsenvor a stirrer 26 in the lower part of the reservoir device 29 in connection, which from one sub-company

Part 30 with a tapered bore or nozzle 31 of frustoconical longitudinal section [Cone angle 60 °) is increased. This conical nozzle is directly below the discharge opening and in connection arranged with the feed screw 27, and its longitudinal axis coincides with that of the cylinder 28 together. The inner diameter of the upper end of this nozzle corresponds to the inner diameter of the cylinder 28. The lower end of the nozzle opens into an opening 32, the diameter of which is approximately Va des corresponds to the upper diameter, and this opening is a passage in the line 33 free. To the conical surface of the nozzle and this tangential and at an angle of 45 ° with respect to the longitudinal axis Intersecting, a plurality of passages 34 with supply lines 35 are arranged. Through this Passages 34 become air or other gas in a downward swirling motion guide, and this prevents the solid fuel from building up along the walls of the cone the nozzle occurs. The supply lines 35 are of any supply source Compressed gas connected, for example with pressurized air. With such a nozzle for Solids, which has an inlet 38.1 mm in diameter running down to decreases to 12.7 mm at the outlet, and being three tangentially arranged passages 34 with a diameter of 1.587 mm around the periphery of the cone cone are attached at equal intervals, has an air speed of 2.83 nWh. proved to be very suitable.

The longitudinal axis of the transport section 33 directly below the conical nozzle is perpendicular to the Nozzle axis. In the transport section 33 is located exactly matching the mouth 32 of the Koihschen Section of the nozzle has an opening so that the solid material from the nozzle into the transport section can pass. In the transport section 33 there is a coaxial line 36 of smaller size Diameter which ends near the protruding outlet end of the nozzle 31, but the outlet itself not blocked. The line 36 is through the closed end 37 of the transport section 33 held in their position. With a nozzle with the dimensions mentioned above, in which the Transport section 33 has an inside diameter of 19.05 mm and the air supply line 36 Having an outer diameter of 6.35 mm has been compared to the generation of a reduced pressure with the pressure prevailing in the reservoir 22 in the conical section and thus for the promotion the withdrawal of the solid material from the nozzle, a ventilation speed of about 17 nWh. proved to be very suitable. Another line has also been shown to be useful to be provided, which connects the transport section 33 and the storage container 22 to one another, there In this way, the occurrence of a disruptive pressure difference along the feed screw 27 is prevented gladly or even completely prevented.

The construction elements of the supply device for the solid fuel described so far serve to ensure a regulated flow rate of the solid fuel in a line, for example the transport section 33. However, if a feed screw is used in such a control device, agglomeration can occur to a certain extent. The feed device therefore also has a further device in which such agglomerates which may have formed are broken up and as a result of which slight fluctuations in the solids flowing out of the feed screw are compensated for. According to FIG. 4 is the transport section 33 with the inlet opening of a grinding device 38, for. B. a hammer mill in connection. From FIG. 4 it can be seen that most of the length of the transport section 33 is arranged so that it opens vertically into the upper part of the grinding device. This grinding device, optionally cooled by means of a water jacket, breaks up any agglomerate that may have formed in the compression section of the feed screw 27 and conveys the ground fuel suspension through a sieve (not shown) with round openings with a diameter of 1.587 mm into a line 39, which is extends up to the feed opening 60 of the cleavage reactor 40.

The feed system described here works over long periods of time with a sufficiently stable feed rate for the solid fuel so that the operation of the cracking reactor described here is not disturbed. Since the ratio of the dimensions of the solid fuel particles to the dimensions of the storage container increases as the dimensions of the entire supply system are chosen larger, it is evident that the difficulties in transferring them to an apparatus for industrial scale production are not greater either , but rather decrease. For such a technical installation, the dimensions of the feed system can reach such an order of magnitude that the daily throughput of solid fuel is 100 tons or more. The facilities for grinding, measuring and transporting the solids required for such a daily throughput can also be easily constructed. Such a technical system could consist of a pneumatic conveying _{device which feeds a V 8} · 0 dry coal with a moisture content of less than 5 "/ o into a ball mill, rod mill or other grinding device, by means of which a pulverized coal is produced, such as this one Such a grinding device would then, in such a large-scale plant, supply the cracking reactor with a continuous flow of solid fuel and air serving as a transport medium.

A total splitting line would have to be provided with further auxiliary devices, for example one Feed and measuring device for the hydrocarbon feed to be split and a feed and measuring device for the oxidizing agent. Such auxiliary devices are per se in the splitting technique well known and therefore will not be described in detail here. Such other auxiliary devices however, in FIG. 4 is also shown schematically. According to this schematic representation is a storage container 80 for the supply of hydrocarbons via the pneumatic control valve 81 connected to the flow meter 82 which opens the valve 81 via the return line 8: regulates, so that the feed line 50 opening into the reactor 40 has a constant flow of coals

hydrogen feed is supplied. The ammeter 82 can be set to any fixed value so that a preselectable variable control with respect to any operating temperature the flow rate of the hydrocarbon feed. If as If air is used as oxidant, a conduit 84 can serve to draw air directly from the atmosphere to be fed into a centrifugal circulation pump 85, which is fed into a pneumatic flow control valve 86 and feeds into a side line 36 which transport air via the regulating valve 87 of the Solids ejector nozzle 29 and the lines 35 feeds. This transport air flows together with the dispersed fuel particles through the transport section 33, grinder 38, and conduit 39 and then passes through the feed opening 60 for solid fuel into the split actuator 40. This In the following, transport air is also referred to as part 211m called first air flow. On the other hand, the air flowing from the blower 85 through valve 86 becomes hereinafter referred to in part as the second air stream. The valve 86, the flow meter 88 and the Return line 89 put together a preselectable variable control option for that person Stream of the oxidizing agent, which after passing the control device via the feed line 71 enters the cleavage reactor. It has already been pointed out above that for the Oxidizing agents and the hydrocarbon feed are usually also used in preheaters, which, however, are not shown in the flow diagram and in any suitable place can be built into the system.

The in the F i g. 5 A and 5 B illustrated cleavage reactor 40 has the following structural parts on: gap chamber 42 with the side walls 43, burner 41, sampling probe 44 including one Quenching device as well as the collection chamber 47 for the combustion products with the possibility of 4 " Extraction of the exhaust gas and discharge of the ash.

The side walls 43 of the gap chamber 42 consist of a cast pipe made of a refractory High alumina material such as are commercially available. This tube is used in common Way potted and hardened, just as it is for the manufacture of refractory linings in fission reactors is known per se, for example also in the production of carbon black. In the preferred embodiment if the tube has a completely circular cross-section, it has a uniform one Diameter and is perfectly straight. It has the following dimensions: inner diameter 7.62 cm and outer diameter 30.48 cm. The inner one The surface of the walls is free of eddy currents in the section where the cracking reaction takes place causing protrusions and free from roughness. Therefore are in the actual gap section the fission chamber also has no sharp changes in direction, no constrictions and no built-in components provided in the form of latticework.

The upstream end of the gap chamber is connected to the burner part 41. This Burner has a base plate 55 which is perpendicular to the longitudinal axis of the pipe made of refractory Material is arranged. This plate 55 carries the feed lines for hydrocarbon feed, Oxidant and fuel and seals the upstream end of the fission chamber in Form of an end wall. That surface of the plate 55 which is directed towards the gap chamber 42 is also known as the burner surface. This burner surface is expediently designed to be completely flat, and the openings through which the hydrocarbon feed, fuel and oxidizer are fed into the cracking chamber are located in the burner surface so that they all lie in the same plane. About certain parts that are needed for the feed of hydrocarbon feed and fuel to support, is in the longitudinal axis of the gap chamber 42 on the burner plate 55 a another transport section 56 attached. This transport section 56 has an inner end of reduced cross-section, which enters an opening of reduced cross-section in the outer Surface of the base plate 55 fits, in which the transport part is firmly anchored. An opening of the The same diameter as the inner end of section 56 is also in the burner surface cut and is thus in an exact fit to the inner end of this section. Coaxial a line 50 is arranged in the transport section 56, which is on the burner surface opens, but longer than the section 56 is. This line 50 consists of a straight tube with uniform circular cross-section, the ratio of length to diameter being about 20: 1 and, if desired, can also be somewhat below this value, or else much greater Can assume values. In the illustrated embodiment, the conduit 50 has an inner diameter of 22.225 mm and a length of 50.80 cm. In this illustrated preferred embodiment, the storage container 80 forms the valve 81 and the control device 82 together with the return line 83 and the line 50 the feed system for hydrocarbon feed, the line 50 also acting as a nozzle which discharges the hydrocarbon feed directly into the cracking chamber. The inner surface of the walls of the line 50 represents a flow-forming part, which due to the special arrangement, the external shape and the chosen dimensions serve to control the flow of hydrocarbons, i. H. the hydrocarbon feed and / or other products or at least a portion thereof constrict a flow path that is less than about half the transverse cross-section of the fission chamber is equivalent to. Under the transverse cross-section or the transverse cross-sectional area is the sectional area of the fission chamber, measured in a plane perpendicular to the longitudinal axis of the chamber stands, understood, the condition that the hydrocarbons to be split in their passage are narrowed by the gap chamber to such a cross-section, is valid for that Section of the chamber through which the hydrocarbons flow close to the burning solid and are at temperatures at which ignition and combustion take place can. However, as soon as the hydrocarbons have reached a section of the chamber in which they are separated from the oxidizing agent by means of a physical barrier and / or in which they are on

33 "'34

Temperatures have cooled down at which ignition simultaneously no longer poses any real danger of imposing a rotating movement component on the flow of solid fuel particles and combustion, compliance with the above. However, it has been shown that the same result conditions are not more required. Instead of a simplified and less costly one with the line 50, any example construction can be achieved if any other flow-forming part is used, namely the outer part of the cooling element 51 with which it contributes to the flow of the largest wires 61, the diameter of which practically corresponds to the proportion of the hydrocarbon charge as long as the space between the cooling jacket and the lead on the specified narrowed flow cross-section SO. Keeping the individual turns of wire until the hydrocarbons have reached at least the io are applied longitudinally from one another at spaced downstream ends of the spaiLzne, whereby one or more screws have. This also applies if the restricting shaped passages arise. In the case of the illustrated or limiting effect, the line 50 is approximately reached or not completely or only in the preferred embodiment. For example, the following dimensions can be added: outer diameter of the feed nozzles for the hydrocarbon feed 15 25 * 4 mm, wall thickness 0.406 mm. It is viewed from turns, which in its longitudinal axis is a corrosion-resistant steel. The cooling jacket has the following dimensions: external diameter sen, which means that the speed in the center is 31.75 mm, wall thickness 0.406 mm. It consists of the material flow is reduced, or it can be corrosion-resistant steel. The line 56 has NEN feed nozzles are used, which no 2 ° and an outer diameter of 38.1 mm. Have twelve wires of circular cross-section. Preferably 61 each with a diameter of 3.175 mm, however, a feed nozzle of such a type is used with silver on the outer surface of the cooling, which ensures that the straightened jacket 51 is soldered so that it can pass through the annular mixing of the hydrocarbon feed 59 at an angle of about 30 takes place in the deflagrating fuel, there are arranged 25 spaced from each other and and to which has proved to be very advantageous that no periphery of the conduit are provided with a ¹ angle of 180 internals in that the tube in question rotate while it has a distance of 7.62 cm "in a circular cross-section and that i-twa fill the lengthwise direction of the passage. This a length to diameter ratio of 2½: 1 arrangement along with the fan 85. the ven _oc ( --m ~ hr fipaphniten. 3 ° til 87, the Leituniz 36, the supply device according to The line 50 is surrounded by a cooling jacket 51. 3 and 4 for the solid fuel, the conduit, the interior of which is 54 mi ', the inlet 52 and 33, the grinding device 38, the transport section, the outlet 53 for the coolant in connection 39 and the tangentially arranged inlet for the. The outer surface of the cooling jacket forming fuel in the annular passage 59 and the inner surface of the conduit 56 together form a preferred possibility for the solid fuel entering an annular passage 59 for the supply of the solid fuel entering the gap chamber 42 to force components of movement at one end, which allow a flow of the fuel in a downstream direction through a cap 57 provided with an opening and a gas-tight sealing plate 58 to the outside of the chamber and at the same time it is closed off from the chamber. The coolant circulating in the interior 54 of the coolant in the general direction of flow of the coal jacket 51 contributes to deflecting water leaks,
To prevent the fuel plug particles in the In this embodiment, the through the passage 59 are used. The downstream rotational movement of the fuel flow generated end of the passage 59 forms an opening which centrifugal forces to provide an outwardly directed over the combustion surface in the gap chamber 42 45 component of movement that surrounds the conduit 50 opens. The way in which the flow of fuel particles is diverted from the pressure "enveloping" or "surrounding" means in the flow of the hydrocarbon feed in the description and the claims that this is avoided. It is not necessary, however, to feed more than half of the fuel-speaking structural element into the gap chamber of the hydrocarbon feed feed nozzle 50 by means of a rotational movement. For example, the wires can also envelop or surround the passage 59 surrounds preferably 61 omitted and the ring-shaped passage 59 practically shows the supply line 50 in the combustion cap can completely close to the combustion cap to the outside surface, so that the flow of coal can be expanded . The hydrogen charge can also be practically completely enveloped by the most deflecting devices in the burner part in a flow of the solid fuel. Hence 55 to be built.

an annular outlet is also very useful. In the walls of the line part 5 (> are also This does not exclude the fact that in the ring-shaped passages 62 and 63 are provided around a fuel line or orifice stiffeners mixture of oxygen or air and fuel or spokes, so that the conduits are gas directed from an unillustrated external source in 50 and 56 well against each other, as long as ⁶ »inject an annular Vcrteilerkanimcr, denir of only those stiffeners or spokes! dimcn- consisting of this mixture twelve passages 66 for sioned, shaped and arranged are that the constant attracting or pilot flame is supplied, which is not disturbed in the same spaced manner by a moderate flow of fuel particles in the longitudinal axis of the line 50. Thus stiffeners can be arranged in a circle and their outlet in the form of between the two lines ⁶ 5 open out between the feed oil for extending fixed turbine nshovel !! the fuel and the feed openings for that contribute both to the mutual alignment of the oxidizing agents and to ensure that these two lines are ignited and flames 68 are generated.

Enveloping the annular passage 59 and preferably following the passages 66 offset from the outside, there are feed lines 69 for the oxidizing agent, which extend through the plate 55 and the burner surface extend through and the interior of the distributor 70 with the gap chamber 42 connect. The walls of the manifold 70 are gas-tight with the outer surface of the plate 55 and the Scope of the line 56 connected. De. The storage tank for the oxidizing agent is via a line 71 in connection with the distributor and opens tangentially into the latter via inlet 72. The feed line 69 for the oxidizing agent can take various forms. For example it can be an annular opening or a number, for example twelve, passages, which are arranged circularly around the longitudinal axis of the line 50 at equal intervals. on In all cases, the supply for the oxidizing agent must be designed so that the oxidizing agent is distributed as evenly as possible around the periphery of the gap chamber 42. The following in Results described embodiment have been obtained by means of a reactor in which the Oxidizing agent fed into the gap chamber via 12 passages in the manner described above would. However, even better results could possibly be achieved with an annular feed opening achieve. Regardless of the particular form chosen, however, it is advantageous if the Feed lines for the oxidizing agent a considerable distance to the outside of the feed line 50 for the hydrocarbon feed, for example a distance which is at least corresponds to the radius of the line 50. The feed line for the oxidizing agent can either have the same direction as the feed line 50 for the hydrocarbon feed or one of them deviating direction, but it should not have a direction convergent to it. In those cases where the gap chamber 42 has divergent side walls and therefore the hydrocarbon stream can spread more freely, is such a divergent direction in the feed of the oxidizing agent of particular advantage. In the Ausfülmingsforni shown in the drawing, however, run the passages 69 for the oxidizing agent with their longitudinal axes parallel to the longitudinal axis of the Feed line 50 for the hydrocarbon feed and to the longitudinal axis of the gap chamber 42. whereby at least the largest proportion of the oxidizing agent is diverted downstream of the chamber 42 in the closest vicinity of the side walls 43. One such an embodiment is simple and works satisfactorily. The inlets for the oxidizer however, need not be in the form of a single annular mouth or a single circle of to have passages arranged at a distance from one another. There can also be several such circular ones Arrays or multiple annular mouths, or any combination thereof be applied. Such outlets together with the fan 85, the valve 86, the control return line 87, the control device 88, the line 71 and the manifold 70 form together a way to ensure that the fuel is completely enveloped by the oxidant and to move the oxidant downstream while still at the same time is kept separate from most of the hydrocarbon feed.

It has already been pointed out above that although it is very useful to use a burner mi to use a completely flat surface, in de there are openings through which the coals hydrogen feed, fuel and oxidant all in the same transverse plane ii

ίο reach the gap chamber 42, but this is off guide way for the implementation of the method according to the invention is not essential. If so desired may have one or more inlets for fuel, hydrocarbon feed, and oxidizer be provided downstream at a sufficient distance from each other. For example, can a frustoconical burner surface may be provided with the larger radius of the truncated cone on the upstream side the combustion chamber and the smaller radius of the truncated cone is downstream into the chamber extends, but the axis of the burner and gap chamber coincide. In such an embodiment The opening for the hydrocarbon feed can be in the downstream one The end of the smaller diameter are located in the longitudinal axis of the truncated cone, while the openings for the fuel and the oxidant may be annular outlets, which are in the conical surface at a certain longitudinal distance from each other. Such a one The arrangement is particularly useful in a reactor in which the walls of the gap chamber are downstream diverge. In this context it should be noted that the term "envelop" or "surround" just the spatial relationship between the inlet for the fuel and the inlet for the hydrocarbon feed or between the inlet for the oxidant and the inlet to reproduce for the fuel, but it is not necessary that these openings or mouths are in the same plane. Rather, this term is only used to to make it clear that one stream of material envelops the other, and if such an envelope in one Transverse cross-section of the reactor as viewed upstream from a point immediately downstream of the outlets in question can be seen, then within the meaning of the invention is the Requirement for wrapping met. For the same reason, the terms »after outside "or" outside "should not be construed as having to be an arrangement act in the same transverse cross-sectional plane.

To the plate 55 before in the gap chamber 42 by the combustion of solid fuel and To protect oxidants generated high temperatures, it has proven to be useful to protect them Plate to cool too. For this purpose there is an annular recess 73 in the outer surface the plate 55 is provided, and this recess is covered with an annular cover plate 74, creating a leak-tight annulus. Any coolant, such as water, will be over

^ 5 line 75 fed in dun annulus and removed again via line 76 thereof.

Although within the scope of the invention per se any quenching device. Product withdrawal

1 UO ** ■

Vi

Device and collecting or recovery device can be used, but preferably the de-graining probe reproduced in FIGS. 5 A and 5 B and the one in FIG. 7 is used. In this preferred embodiment, the sampling probe 44 is arranged in the longitudinal axis of the gap chamber 42 , and the inlet opening 105 is aligned directly with the feed line for the hydrocarbon feed. With differently designed reactors it may be necessary to arrange the sampling probe at a point other than the longitudinal axis of the cleavage chamber in order to achieve the highest concentration of the splitting products, but the axial arrangement is preferred in the reactor shown here. The sampling probe may be stationary or movable in any desired manner, and it may be attached to any part of the reactor, but in the reactor shown here the sampling probe is conveniently carried by the end wall of the collection chamber 47 for the combustion products.

This collection chamber 47 has an upper wall 95, side walls 96 and a bottom wall 97 in which a stuffing box 98 is located, which is around the extended axis of the gap chamber 42 and exactly to the passages 104 and 103 in the upper and lower wall the chamber 47 is arranged. The passage 103 has a slightly larger diameter than the outer wall of the tube of the sampling probe, while the passage 104 has a slightly larger diameter than the interior of the gap chamber 42 . The tube of the sampling probe extends from the outer side of the chamber 47 through the stuffing box 98 , through the passage 103, through the chamber 47 and through the passage 104 into the actual gap chamber 42. The stuffing box 98 has a packing 99 and a nut 100, which presses the package against the side walls of the sampling probe 44 and against the outer end of the passage 103rd When this nut is loosened, the tube of the sampling probe can be axially withdrawn and retracted so that the orifice 105 can be adjusted to any desired distance from the end of the supply line 50 for the hydrocarbon feed. Then you can tighten the nut 100 again, whereby the sampling probe is held in the desired position.

As a result of the very high temperatures prevailing in the gap chamber and since the sampling probe usually consists of steel and not of refractory material, it generally has to be cooled externally. This can easily be achieved if the tube of the sampling probe consists of two concentrically arranged tubes 101 and 102 which together form an annular passage 106 for the coolant in the body of the sampling probe. The passage 106 should extend at least over that part of the total length of the sampling probe which can be pushed into the gap chamber 42 , and preferably the coolable part covers the tube of the sampling probe as far as it can be retracted into the reactor as a whole, ie not only into the actual gap chamber 42, but also into the collecting chamber 47, as shown in FIGS. 5A and 5B. The passage for the coolant is preferably closed at both the inner end 107 and the outward end 108 and the inner tube 101 extends beyond the outer terminating end of the cooling passage and is connected to a suitable system for the recovery of the fission products, such as it is shown in Fig. 7 represents. Coolant, for example a gas or a liquid such as water, can be fed in from outside the reactor via feed line 109.

ίο The sampling probe can have any desired outlet for the used coolant at any point. Preferably, the coolant outlet should be located in a part of the sampling probe which is located inside the reactor, so that the escaping coolant can be used to quench the fission products. According to a preferred embodiment, a plurality of outlets HC are therefore provided which connect the passage 106 for the coolant to the interior of the line 101 in the immediate vicinity of the inlet opening 10. In this way, the outlets for used cooling water can be used to directly quench the splitting products at the moment when they reach the sampling probe via the opening 105. The following dimensions have proven to be very useful for such a sampling probe in practice: Outer tube 102: outer diameter 38.1 mm, wall thickness 0.406 mm; corrosion-resistant steel; Inner tube 101: outer diameter 31.75 mm, wall thickness 0.406 mm; corrosion-resistant steel; There are twenty outlets 110 for the cooling water with a diameter of 5.1 mm each, which are uniformly arranged in groups of 8 in three circles and are located at a distance of 1.587, 3.175 and 4.762 mm from the inner end 107 of the sampling probe. However, these dimensions can be changed at will.

Since the transverse dimensions, for example the diameter of the extraction probe, are significantly smaller than the transverse dimensions, for example the diameter of the interior of the gap chamber, an annular passage 45 of considerable width is created between the gap chamber and the extraction probe. This passage serves to withdraw the hot products of combustion from the reactor, and an injector may also be provided there to burn any solid fuel that has reached this point. without being burned down. Of course, the sampling probe described here can also be used in split actuators that do not work with solid, carbonaceous fuels. In the embodiment shown here, however, the passage 45 serves to withdraw both gaseous and solid combustion products in the form of ash. The passage 45 communicates via the opening 104 with the collecting chamber 47 , from which the gaseous combustion products can be drawn off via outlet 111 , while the solids that collect therein can be discharged via the porthole 112 at intervals.

In Fig. 7 is wiedcrgep hen that the conduit 101, through which are deducted abgesc 'stretched cleavage products from the sampling probe in, the reactor communicating with a ^c parator 123 in connection with the bschrccklliissiakcit a \ charged

st and an outlet for this liquid 124 and: an outlet line 125 for the spall products. This line 125 is connected to a separation system 126 for gases and solids, for example an agglomerator and a bag filter, as is usually the case when working thinly when solid fission products, for example soot, are formed. This separation system for gas and solids has an outlet 127 which opens into a line 128. If no solid fission products are formed, this gas-solids separation system can also be bypassed with a secondary line, and the fission products freed from the quenching liquid can then be fed directly into line 128 by opening the bypass valve 129. In this line 128 there is a pneumatically controlled, motor-driven valve 130 and a control device 131 which transmits a pressure difference, the latter being connected to the motor in the valve 130 via a return line 132 . A vacuum gauge 133 is arranged between the control device and this valve, on which the vacuum prevailing in line 128 can be read directly. On the downstream side of the control device 131 , the line 128 is connected to the suction side 122 of a steam jet ejector 120 , the steam required for the operation of the ejector being supplied via line 121. This suction device builds a vacuum in the supply line and upstream in the sampling probe via the separation system 123, the separation system 126 or the bypass valve 129, the motor-driven valve 130 and the control system 131 . The mixture of steam and gaseous fission products leaves the ejector via outlet 134 and then reaches the condenser 119, in which the water vapors are liquefied. The mixture of liquefied vapor and fission products then passes into the separating device 118, from which the condensate is drawn off via outlet 117 and the practically liquid-free, gaseous fission products are withdrawn via outlet 116 . This outlet 116 can be connected to any plant for purifying or recovering the fission products. Since such devices are well known, they will not be further described here.

The device for regulating and transmitting a pressure difference is designed in such a way that it can be set to a preselectable fixed value, and in this way the motor-operated valve 130 can be opened and closed as desired and thereby any vacuum in the line 128 and in of line 101 maintained. Since the pressure in the gap chamber 42 can also be regulated by adjusting the flow rates of the hydrocarbon charge, solid fuel and oxidizing agent and the burn rate accordingly, this results together with the ejector 120, the control device 131, the return line 132 and the valve 130 as a whole good way to maintain a controlled negative pressure differential between the interior of the cleavage chamber and the sampling probe.

By using the sampling probe described above and the control and regulation described above Control devices for maintaining a pressure differential yield certain improvements regarding the operation of the reactor and the implementation of the cracking process. For example the fission products are diluted to a much lesser extent by combustion gases than with a conventional one with pre-combustion or partial combustion processes or with other pyrolytic processes Fission processes. This reduces the size and cost of the recovery system, which is required for the treatment of the fission products. Also decrease the cost of cleaning measures that are otherwise required to make an end product salable or directly applicable form.

By using the sampling probe according to the invention, not all of the hot ones are required Combustion gases in the reactor get quenched, only so that the fission products in the required Way to be cooled, and in this way the remaining'heizwert can be removed as exhaust gas Combustion gases still take advantage, which gives the whole process a high thermal Has efficiency. Since the sampling probe can be moved, it is also easier to control the Fission process, because the residence time of the hydrocarbon feed and the fission products can be set and regulated in a simple manner, without affecting the feed rates of fuel, oxidizer and hydrocarbon feed need to be modified. It has also been shown to be possible to use the sampling probe to move over a considerable distance within the gap chamber without thereby the Overall reactor operation is adversely affected.

Embodiment

This example illustrates the implementation of the method of the invention by means of the above described plant of a cleavage reactor. There are the following conditions in the procedure adhered to:

Feed: propane,

Propane temperature: 593 ° C "

Propane feed rate: 28.8 kg / hr.

Solid fuel: # 2 grit gas coal supplied from a Boone County, W. Va. Pit from Obelbay Norton.

Heat content of the fuel

(moisture-free and ash-free) .. 8062 kcal / kg

Ash content 7 ° / o

Hydrogen content 7%

Volatile matter content 33%

Melting temperature of the ash 1538 ⁰ C

Sulfur 0.8 ⁰ / o

Solid carbon 60%

Free swelling index according to ASTM

D 720-67 5

Moiety which through a sieve of mesh aperture 45 microns is 60 ⁰ / o

Moisture content 2 <7o

Fuel supply 14.06 kg / h

Oxidizing agent air

509 685/180

41

Air temperature

Air supply

Air content in the second air flow approximately air content in the first air flow (Suspension medium for the coal)

approx. distance between sampling probe

and baking surface

Deterrents

Water temperature at the inlet end

the sampling probe

Water speed

Reactor pressure

Gap temperature

Residence time of the hydrocarbon feed in the cracking chamber

about temperature of the quenched

Fission products

Flow rate of the quenched fission products

₅ Q ₃ O _C

164.1 NnVVh 90%

Table I.

42

component

Volume percentage

In sampling probe

In the ring-shaped passage

10 ¹ Vo

11.43 cm of water

26.7 ° C

13.25 liters / hour

0.07 kg / cm- '

Overpressure ^IS 1649 ° C

9.8 0.2 71.6 11.0

CO ₂ 5.2

CH ₄ 0.2

C ₂ = (double bond) 0.4 C ₂ s (triple bond) 1.5

13.3

0.1

66.4

10.2

4.2

1.8

1.0

3.0

The material balance for the carbon is calculated and gives the results summarized in Table II.

1 millisecond ₂₀ Table II

65.6 ° C 24.1 nr'h.

Total load kg / hour

As propane 23,587

As coal 10,660

Total 34,247

The flame formed by the burning of the solid fuel showed good stability and had a color between intense orange and white. After starting up the reactor was no additional fuel gas is used, other than those negligibly small amounts, soft for the Operation of the pilot lights are required. That from the sampling probe and from the one surrounding this probe annular passage withdrawn gas was collected under steady state conditions and analyzed. The results obtained are summarized in Table I below:

Discharge

As C ₂ H ₂
As C ₀ H ₄
AIsC ₃ "".
As CH ₄ .
As CO ₂ .
As CO ..
As soot.

Total ...

4.717

1.996

0.045

1.361

3,583

8.528

6.350

26,580

Loss (unburned carbon in the coal) 7,666

For this purpose 4 sheets of drawings

Claims (30)

Patent claims: 1. Process for the production of mixtures of acetylene and ethylene by thermal cleavage of gaseous and / or vaporized, more highly saturated hydrocarbons with 2 to 10 carbon atoms in a reaction chamber, the required heat of reaction in the reaction chamber by burning continuous Hch in the reaction chamber Introduced solid carbonaceous fuel is generated with oxygen or free oxygen-containing gases as oxidizing agent, and subsequent quenching of the fission products, characterized in that the hydrocarbons to be fissioned, the carbonaceous fuel and the oxidizing agent are introduced separately into the reaction chamber and flow through it in the same direction, the The flow of the hydrocarbons to be split is enveloped by the flow of the carbonaceous fuel and the latter is enveloped by the flow of the oxidizing agent, and that the carbonaceous fuel, when introduced into the reaction space, has a moving component component in the main flow direction along the reaction space and optionally a further movement component which is directed away from the flow of the hydrocarbons to be split and is directed towards the flow of the oxidizing agent. 2. The method according to claim 1, characterized in that a small proportion of the oxidizing agent before the carbonaceous fuel is introduced into the reaction space this is mixed as a suspending agent. 3. The method according to claim 1, characterized in that the flow of the carbon-containing A rotational movement is imposed on the fuel, which is caused by the flow of the to spying more highly saturated hydrocarbons contains movement component directed away. 4. The method according to claim 1 to 3, characterized in that the burn rate of the carbonaceous fuel is adjusted by varying its particle size. 5. The method according to claim 1 to 4, characterized in that the burn rate of the carbonaceous fuel is adjusted so that the burnup practically over the entire length of the cleavage zone takes place and that the burning process only occurs on the downstream End of the split zone is terminated. 6. The method according to claim 1 to 5, characterized in that the cleavage products formed separated from the main part of the combustion products within the cleavage zone and as separate stream of material can be withdrawn from the cleavage zone. 7. The method according to claim 1 to 6, characterized in that the hydrocarbon feed is fed as gas into the cleavage zone. 8. The method according to claim 1 to 7, characterized in that a carbon-containing Use fuel with a particle size of 0.25 mm or less: is. 9. The method according to claim 1 to 8, characterized characterized in that a carbonaceous fuel with a hydrogen content of less than 15% is used. 10. The method according to claim 1 to 9, characterized in that from carbonaceous Fuel used is ground hard coal, degassed coal and / or low-temperature smoldering coke will. 11. The method according to claim 1 to 10, characterized characterized in that air is used as the oxidizing agent. 12. The method of claim 1 to 11, characterized in that the hydrocarbon feed at a temperature of 816-1927 ⁰ C, in particular 1093 to 1760 ° C, and a residence time in the nip zone of 1O ^-1 is treated to 10 ~ ⁴ seconds . 13. The method according to claim 1 to 12, characterized in that the speed the heat dissipation from the stream of burning carbonaceous fuel practically equal to the rate of heat consumption by the fission reaction and by usual Heat loss is kept by the material flows during passage through the Cleavage zone kept at practically constant temperatures as a result of constant energy exchange we.den. 14. The method according to claim 1 to 13, characterized in that the temperature of the fission products formed at the downstream end of the spaitz zone as quickly as possible is lowered to at least 427 ° C and in particular to at least 260 ° C. 15. Fission reactor for carrying out the method according to claim 1 to 14 with one another separate feed lines for the hydrocarbon feed to be cracked, the solid one carbonaceous fuel and an oxidizer, with a fission chamber and quenchers, wherein the downstream and upstream ends of the gap chamber are connected to one another by a wall and the feed line for the hydrocarbon feed to be cracked with the interior of the gap chamber is in communication and also a nozzle device for the Formation and advancement of a stream of hydrocarbon feed in the longitudinal direction the gap chamber, but is provided at a distance from its rope wall, characterized in that that the flow-forming part of the nozzle device (50) the greater part of the hydrocarbon flow narrows to a cross-section which is less than about half the transverse Cross-sectional area of that part of the gap chamber (42) corresponds to the quenching device (HO) extends that around the feed line (50) for the hydrocarbon feed, at least partially enveloping it or having a distance from it towards the outside, a current-forming part (59) for the carbonaceous fuel is arranged, which is the carbonaceous fuel when Introducing a movement component in the main flow direction into the reaction space along the reaction space and optionally a second component of movement perpendicular ■ * *. AT ^ TTT- ■ for this purpose directed to the flow of the oxidizing agent issued that a flow-forming part (69) for the main flow of the oxidizing agent is arranged around the feed line (59) for the carbonaceous fuel, at least partially enveloping it or having a distance from it to the outside, that inside the fission chamber (42) an extraction probe (44) of smaller diameter than this chamber is arranged and that the probe has an inlet opening (105) for the fission products formed in the flow path of the hydrocarbon feed and opposite the mouth of the feed line (50) for this feed and that in the gap chamber (42) in the vicinity of the sampling probe (44) passages (45, 104) are provided for the combustion products. 16. Fission reactor according to claim 15, characterized in that the flow-forming part (59) for the carbonaceous fuel as a helical one Annular channel (50, 61, 56) is formed. 17. Fission reactor according to claim 15 or 16, characterized in that the nozzle device (50) is designed as a cone, through the bore of which the hydrocarbon flow into the gap chamber (42) is fed, and that on the outer surface of the cone outlet openings (59, 69) for the carbonaceous fuel and oxidizer with a tangential component are arranged to the conical surface. 18. Fission reactor according to claim 15 to 17, characterized in that the feed line (39) for the carbonaceous fuel has a feed device (22, 23, 24, 25, 26, 27, 28, 31) , the outlet (32) with a device (33, 36, 46) for mixing the fuel particles leading to the reactor is in communication with a gaseous suspension aid. 19. Fission reactor according to claim 18, characterized in that that this mixing device (33, 36, 46) in turn with a grinding device (38), in particular a beater or hammer mill is connected. 20. Fission reactor according to claim 18 or 19, characterized in that the feed device (22, 23, 24, 25, 26, 27, 28, 31) for the carbon-containing fuel is a continuously metering ignition device. 21. Fission reactor according to claim 18 to 20, characterized in that the ignition device (22, 23, 24, 25, 26, 27, 28 .. 31) is designed such that the in its supply channel (28, contained carbonaceous fuel a sealing plug for the gaseous suspension auxiliary forms. 22. Fission reactor according to claim 18 to 21, characterized in that the ignition device (22, 23, 24, 25, 26, 27, 28, 31) is designed as a compression device, in particular as a screw conveyor (27) for the loosely supplied carbonaceous fuel . 23. Spaltrcaktor according to claim 15 to 22, characterized characterized in that the feed line (71) for the oxidizing agent is in the vicinity is arranged to at least one delimiting side wall (43) of the gap chamber (42). 24. Fission reactor according to claim 15 to 23, characterized characterized in that the gap chamber (42) is designed as an elongated cylinder. 25. Fission reactor according to claim 15 to 24, characterized characterized in that at least one device within the sampling probe (44) (110) is provided for quenching the fission products. 26. Fission reactor according to claim 15 and 25, characterized in that the sampling probe (44) with a device (120, 130, 131, 132) for generating a regulated negative pressure difference between the interior of the fission chamber (42) and the interior of the probe ( 47) is connected. 27. Fission reactor according to claim 15 to 26, characterized in that the sampling probe (44) is arranged displaceably within the gap chamber (42), preferably in the longitudinal direction thereof. 28. Fission reactor according to claim 15 to 27, characterized in that a cooling jacket (101, 102) is arranged around the part of the sampling probe (44) extending into the fission chamber (42). 29. Fission reactor according to claim 15 to 28, characterized in that the outlet of the cooling jacket (101, 102) of the sampling probe (44) is in communication with the quenching device (110) for the fission products. 30. Fission reactor according to claim 15 to 29, characterized in that the downstream End of the cracking chamber (42) with a collecting chamber (47) for the combustion products is connected, which has an exhaust gas outlet (111) and a removal device (112) for the ash products.