DD150073A5 - METHOD FOR CONVERTING CARBON-CONTAINING MATERIALS - Google Patents

Abstract

It is a process for converting a carbonaceous feed into more valuable products using a melt as a reactant, comprising the steps of: contacting a carbonaceous feed with a melt as the reaction medium while maintaining at a temperature above the melting point of said medium in the lower part a substantially vertical elongated reaction zone for forming a mixture of the carbonaceous feedstock and the melt as the reaction medium, wherein at least one gaseous material is present under the conditions of the reaction zone and a mixed phase mixture is formed; hydraulic transport of the multiphase mixture substantially in an upward direction through the reaction zone to the upper part thereof in a parallel flow of the components of the mixture and at a rate sufficient to cause a gas lift effect in the reaction zone, wherein a chemical conversion reaction takes place to produce modified multiphase mixture; Forwarding the modified multiphase mixture from the upper part of the reaction zone to a separation device and separating the modified multiphase mixture into a stream of a gaseous product or gaseous products u. a liquid flow corresponding to said melt. It is also an apparatus for carrying out the present method.

Description

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Process for Converting Carbon Halide M aterials Uses for the E.rf ind u η q

The present invention relates to the conversion of carbonaceous materials in a melt as a reaction medium. More particularly, the present invention relates to a process and apparatus for the conversion of carbonaceous materials in a melt wherein at least a portion of the reactants are in the gaseous phase to allow intimate and uniform contact between the reactants and the melt, short reaction times, and independent control of the ratio of the melt flow rates to the feed flow rates through the reaction zone. The present invention can serve to simultaneously carry out more than one continuous chemical reaction in a common melt with continuous transfer of the melt between multiple reaction zones in a series or parallel operation without the aid of a mechanical pump, and the reaction zones can be operated at different pressures ,

Known e tec hni solutions

In recent years, various researchers have reported the conversion of hydrocarbonaceous materials using a melt for such conversions. The predominant category of melt used as a medium for the conversion processes and / or for the equipment is

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For example, some recent U.S. patents include Nos. 3,252,773, 3,252,774, 3,567,412, 3,619,144, 3,708,270, 3,170,737, 3,740,193, 3,758,673, 3,916,617, 3,941 681 and 4,017,271. These enumerated patents suggest the use of an alkali metal salt melt as the reaction medium in the gasification of the hydrocarbon feedstocks. Similarly, U.S. Patent Nos. 3,553,279, 3,081,256, 3,745,109, 3,582,188, 3,862,025, 3,871,992, and 3,876,527 describe the use of an alkali metal salt melt as a reaction medium in cracking Hydrocarbon feedstocks for the production of ethylene »

As another example of the prior art, molten salts have also been suggested for use in the dehydrogenation of hydrocarbon feedstocks. See, for example, U.S. Patent Nos. 3270086, 3309419, 3449458, 3586733, 3637895, and 3697614. As an additional example, U.S. Patent Nos. 3,387,941 and 3,440,164 describe the use of alkali metal salts as the reaction medium in the desulfurization of hydrocarbon materials. , .

Until now, the reported use of a melt as a reaction or conversion medium has been limited to process-specific and mechanical designs that have a relatively low capacity, unlike design systems that are suitable for commercial use. In addition, due to the need to maintain flow rates at low levels, the melt processes become particularly disadvantageous in those types of conversion reactions where the yields are disadvantageously whitened by long contact times between the melt and the hydrocarbon reactants.

The US Patent Nos. 2031987, 3852188, 3862025, 3871992 and 3876527 also bring in a proposal that the hydrocarbon feedstock may be contacted with the melt according to the uniflow principle in B _e emotion. However, in order to achieve sufficient separation between the melt and the gaseous hydrocarbonaceous materials for product recovery, the input quantities in the unit of time must again be limited to undesirably low levels, thereby limiting processing capacities and adversely affecting product yields. It is disclosed in US Pat No. 2055313, it has also been proposed that the hydrocarbon feed can be used to hydraulically transport a melt as the reaction medium. In the context of this mentioned method, however, it comes to the actual conversion of the hydrocarbonaceous feedstock by the

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Contact with the melt in a flow according to the counter-current principle between the substances. Again, the capacity of the largest practical facility to be built according to these proposals would be limited to the flow rate at which the gaseous reactants could escape from the melt at the interface level.

The present invention aims to describe a process and apparatus for converting carbonaceous materials in a melt as a reaction medium, overcoming the shortcomings of the prior art. In the context of the present invention, it is a high capacity, to improve product yields and to allow short contact times between the carbonaceous reactants and the. Melt as reaction medium «

Another object of the present invention is to describe a method and an apparatus in which several different reactions can be carried out in separate reaction zones at different pressures using a common melt as the reaction medium which is circulated without the aid of a pump.

The object of the present invention also comprises a method and an apparatus, wherein an intimate and uniform contact between the reactants and the

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Melt is recorded and the ratio of the reactants to the melt in each reaction zone can be controlled independently.

Were the E r f in du ng;

In accomplishing the foregoing and other objects, it is an object of the present invention to provide a process for the conversion of carbonaceous feedstocks to more valuable products, which results in substantial savings in capital expenditure and improves product yields as compared to the hydrocarbon feedstock. conversion

Prior art melt process. This process can be characterized as follows: by contacting a carbonaceous feed with a melt while maintaining at a temperature above the melting point of the melt in a substantially vertical, extended hydrocarbon conversion zone (in the substantially vertical, extended hydrocarbon conversion zones) with a substantially upwardly parallel flow of the feedstock and the melt and at a rate sufficient to preferably produce at least one foam flow transport state through the reaction zone as defined below; and then the separation of the parallel flow of the feedstock and the melt into a stream of more valuable products and a stream of a melt in the upper part of the reaction zone. A flow of lower turbulence (or flow rate) may be provided and carried out, but the economic benefits would be greatly reduced. By using a parallel flow of the reactants and the melt, the Applicant has found that flow velocities can be realized which are 10 times greater than the velocities of the melt processes possible according to the prior art. As a consequence The much higher feed rates in the unit of time possible with the process of the present invention can effectively process commercially significant amounts of carbon sink feedstock with much smaller technical equipment than the methods and equipment of US Pat the earlier state of the art the Pail is «. In addition, the use of parallel melt flow contacting the melt and carbonaceous reactants of the present invention provides the ability to set the contact time between the melt and the carbonaceous feedstock (or reactants) to very low levels. These are orders of magnitude from 1 second or less * Since "

This results in a significant improvement in the product yield. In other words, by using larger feed rates per unit time, the present invention offers the use of a time / temperature profile that is more optimal for carrying out hydrocarbon conversion reactions.

In general, the process of the present invention can be used in any hydrocarbon conversion reaction using a melt. The melt and hydrocarbon feedstock must be contacted within a parallel flow in a vertically extended reaction zone with the gaseous feed and / or the gaseous reactants and / or the diluent gas forming a hydraulic flow pattern of sufficient turbulence, preferably the foam flow or to represent a more turbulent type of hydraulic transport flow, as further defined below. Any suitable transfer rate above this typical value can be successful and find use in certain situations in the practice of the present invention. It is advantageous to have a hydraulic flow pattern and melt ratio to the gaseous feed and / or gaseous reactants and For example, the hydraulic transport of the melt and hydrocarbon feedstock and / or the reactants through the reaction zone may be accomplished in such a way that in the reaction zone a gas phase can be added to the gaseous diluent materials for an economic balance between operating costs and intimate contact is observed annular puncture of the hydraulic transport state, as defined below, or a hydraulic transport state in the manner of a mist or any hydraulic transport state between them hervo is called ·

According to the use made here, the trans-

Port state of the "Schauraströmung" to that hydraulic state or degree of turbulence within the mixed phase reaction zone or zones, which is necessary or to ensure and maintain the circulation of the melt as a reaction medium according to the phenomenon known in the art as Airlift or Gaslift The optimal design is achieved by a turbulence greater than the minimum turbulence. The optimum degree of turbulence for each reaction zone with the melt must be determined separately for itself, but the Applicant has found that the most logical design in many melt systems is the Flow pattern of "foam flow" as Anderson, RJ and Russe-li, TW ·! ¹ , in which "Chemical Engineering" of December 6, 1965 described and described in more detail. Certain flow conditions characterized by the above authors as "creeping pipe flow" may satisfy the definition of "foam flow" according to the present invention because of the required gas lift effect. It is intended that such conditions also fall within the scope of the term "foam flow" as used in this application, and thus within the scope of the present invention.

The process of the present invention is particularly suitable for cracking a hydrocarbon feed with a high sulfur content into more valuable products. At the same time, it is suitable for the partial oxidation of the carbonaceous product from the cracking reaction. The melt as the reaction medium may be selected will readily retain substantially all the sulfur compounds which are released during cracking and during the reactions of the partially iron oxidation. Such a melt is readily regenerated to remove the retained sulfur therefrom without the need for prior costly desulfurization treatment of the feed. "In addition, there is a further advantage of the present invention.

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It is believed that a single feed of the melt as a reaction medium can be performed to maintain a variety of chemical reactions by recycling the melt therebetween. The hydrocarbon conversion reaction may occur in conjunction with an exothermic reaction, such as with a partial oxidation reaction, wherein the heat released in the exothermic (oxidation) reaction zone serves to provide the necessary heat of reaction for other reactions or transformations The transfer of heat from the exothermic reaction zones is facilitated by the circulation of the melt between the zones concerned, whereby there is the possibility that the melt will conduct heat in the form of the sensible heat of the melt * The circulation rate required to transmit the necessary heat depends on the temperature differences between the respective reaction zones and the heat capacities of the melt used. Regardless of the heat transfer requirements that are met by the circulation of the melt between the respective exothermic and endothermic reactions, the recovery of the melt from a separator and back to the respective lower section of a vertically extended hydraulic transport zone of the foam flow (transport reaction zones) Engineer to control the ratio of melt to feedstock and / or reactants' and / or to the diluent gas within each transport reaction zone. "

Brief description of the figures in the drawings

Figure 1 corresponds to a schematic flow diagram of a closed-cycle gasification process based on the creative principles of the present invention;

Figure 2 gives a schematic flow diagram of a continuous gasification process for a sulfurous coal «

rich input material according to the present invention again;

Figure 3 is a schematic flow diagram of a two reaction zone system according to the present invention using a common melt as the reaction medium;

Figure 4 corresponds to a schematic flow diagram of a system similar to that in Figure 3 and

Figure 5 gives a schematic flow diagram of a three reaction zone system according to the present invention using a common melt as the reaction medium.

Detailed description of the preferred embodiments

The Applicant has found that by using the concept of the parallel hydraulic transport with the aid of the foam flow according to the present invention, input quantities in the unit time can be obtained by means of one-line installations corresponding to the.10 times the entry quantities used in connection with the melting processes according to US Pat It is a range of throughputs which contributes to the commercial use of melt technology for the first time in the conversion of carbonaceous feedstocks into tonnages.

In general, the process according to the present invention is highly suitable for any type of conversion reaction of hydrocarbons familiar to those versed in the art. "This also applies to any other type of chemical reaction that is capable By way of illustration, but without limitation, suitable reactions that may be carried out in accordance with the present invention include cracking, oxidation, partial oxidation, gasification, methanation, polymerization, evolution, and the like.

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alkylation, desulfurization, reforming, isomerization, dehydrogenation, oxidative dehydrogenation, the catalyzed versions thereof, combinations thereof, or any of the processes described in the following U "S" patents with the respective Krn. No. 3252773, 3252774, 3449458, 3081256, 3708270, 3710737, 3745109, 3916617, 4017271, 3871992, 3862035, 3852188, 2031987, 2055313, 3387941, 3440164, 3270086, 3309419, 3586733, 3637895, 3697614, 3553279, 3567412, 3619H4 , 3740193, 3758673, 3941681, 3948759, 2053211, 2334583, 2354355, 2100823, 20/4529, 3449458 and 2682459 · The only limitation with regard to the particular nature of the reaction process and the equipment to which the principle of the present invention is applied is that the particular reaction must be capable of being carried out in a melt as a reaction medium. There must be a gas reactant or gas diluent present in sufficient quantity to produce a foam flow as defined herein in a vertically extended reaction zone. A detailed list of other types of organic reactions that can be carried out in a melt as a reaction medium can be found in Advanc e_s__ in Molten Salt Chemistry, Volume 3, Plenum Press (New York 1975), Library of Congress Catalog Kr. 78-131884 Each of the above-mentioned types of reactions is well known to those skilled in the art, and the melt-applied technical processes according to the present invention are highly suitable for use in this regard.

The melt as the reaction medium may include any melted material suitable as the reaction medium in reactions of the type discussed above. A requirement for successful practice in the practice of the present invention is that the melt must be sufficiently fluid to permit hydraulic mixing with subsequent separation, and at the reaction temperatures and

Of which use is made, so that the reaction can proceed _e Typically, the melt as the reaction medium at which the hydrocarbon feedstock is brought into contact, from a molten metal selected from Groups I-VIII of the table press must be stable, the Periodic system of the elements, or of a molten metal salt, which is melted within the temperature range between about 50 ⁰ C and about 2500 ⁰ G. It must here be sufficiently low volatility, thus losses of the melt as a reaction medium with the product gas to a minimum Preferred materials for the melt as the reaction medium include alkali metal melts, mixtures of alkali metal melts, alkali metal salt melts, mixtures of alkali metal salt melts and mixtures of molten alkali metals and alkali metal salts. Suitable alkali metal salts are: alkali metal carbonates, hydroxides, -Nitrates, sulphides, chlorides and oxides, of which the carbonates, sulphides, chlorides and hydroxides are preferred * The use of the carbonate is particularly advantageous when the removal of sulfur from the product is required because the carbonate is capable of is to react with sulfur compounds released from the feed at elevated temperatures during the overall reaction *

While it is possible to use a single alkali metal salt as the reaction medium, it is often preferred to use a eutectic or near eutectic mixture, for example, a binary, ternary, quaternary, etc. Especially preferred for use as a melt as a reaction medium in the present invention The invention will include mixtures of alkali metal salts such as alkali metal carbonates. Examples include sodium carbonate-potassium carbonate-lithium carbonate; Katriumkarbonat-lithium carbonate; Likewise, all other salts thereof can be used. Mixtures of the alkali metal salts form ideal constituents for the melt as the reaction medium

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in the context of the present invention, because these materials bind the sulfur very quickly and can be easily regenerated. When the process according to the present invention is used for the gasification of carbonaceous feedstocks, a single alkali metal salt can be used to advantage because the higher temperatures encountered allow the use of a higher melting point melt. The sodium carbonate is particularly preferred in this respect This material is readily available in the typical refining or petrochemical complex and can be supplied from any existing waste alkali. ,

The present invention also contemplates that the melt may also contain, as a reactant medium, an additional catalytic material as an admixture to enhance and promote the conversion reaction of the carbonaceous materials. When an activator or catalyst is used, the Melt typically containing about 0-50% by mass and preferably about 25% by mass or less of these substances

The carbonaceous material used as feed in the present process may be any carbonaceous material well known to those versed in the art. Suitable carbonaceous feedstocks include: vegetable and mineral oils, other naturally occurring carbonaceous materials, asphalts, hydrocarbon residues produced by distillation or by distillation and solvent extraction of crude oil, heating oil, cycle oil, gas oil, rubbers, heavy crudes, pitch, coal tar, coal, natural tars, hydrocarbonaceous polymers, tar sand oil, naphtha, shale oil, natural gas, refinery gas, light hydrocarbons such as ethane, propane and butane, kerosene, defatted motor vehicle tires, automotive crankcase oil, etc.

mixtures or products thereof «

The carbonaceous feed may have a high sulfur content. Examples include: heavy hydrocarbon feeds such as crude oils, heavy residues, asphalts, hydrocarbon residues produced by distillation or solvent extraction, crude oil distillation residues, pitch, other heavy pitch hydrocarbon residues, coal, Coal tar or distillates, natural tars, cycle oil, sludge oil, tar sands, and oil shale «. Of particular interest are high sulfur, low ash content materials such as asphalts, cycle oil, tar sands oil, shale oil, mud oil, as well as hydrocarbon residues and aromatic tars *. ".

The carbonaceous feedstock and the melt are brought into contact with each other in parallel flow through the reaction zone and at speeds sufficient to preferably maintain at least one "foam flow" transport condition in the reaction zone as defined above Flow rate, which is necessary to realize this type of transport phenomenon, for example, with the particular melt used as the reaction medium, the special carbonaceous feedstock and the need to maintain contact times within certain limits vary ₀ This flow rate (input amount in the unit time) can without Further, as is well known to those who are versed in this field of technology, "The particular transport speed we have used under the conditions of use d, can vary over a wide range, it being necessary, however, be assumed that the transport ₉ states must be sufficient to main- at least the transport state according to the gas-lift effect in said reaction zone in accordance with the definition given above

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In practice, the speed will often be greater than the minimum required to produce this gas lift effect. For example, in such types of hydrocarbon conversion reactions, such as cracking and partial oxidation or gasification,. wherein the hydrocarbon conversion reaction is favored by minimal contact times, generally using very high transport speeds to minimize contact time. In addition, the use of multi-phase foam flow transport eliminates the need to use pumps to pass the melt through the processing equipment to circulate · *

When cracking asphalt to produce ethylene, for example, using a melt as the reaction medium of a mixture of potassium and lithium carbonates having an alkali metal sulfide content of about 1 mass% under steady state operating conditions, typical flow rates involve a carry-on amount of the carbonaceous feedstock in the unit time corresponding to a surface speed of about 10 to 100 ft / s, and preferably about 20-35 ft / s; and a mass ratio of the melt to the carbonaceous feedstock of about 2-20, and preferably about 4-8, depending on the heat of reaction, the heat capacity of the melt, and the temperature differences between the reaction zones. With the conditions of the reaction zone in this range, contact times of about 0.5 to 10 or more seconds are to be achieved without difficulty.

Similarly, in the gasification of carbonaceous materials to obtain low or middle Btu gas using a molten sodium carbonate reaction medium containing about 0-25 mass% of alkali metal sulfide under steady-state operating conditions, air and steam are more typical Vtfeise supplied in a ratio to the control of Gesamtwärmeerezeugurig such that said

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Total heat 1 * is removed in the form of sensible heat of the escaping product gas and 2. is lost through the walls of the container «The temperature is thus adjustable by adjusting the ratio between air and steam» The typical air flow rate is equivalent to 3-7 pounds of air per pound of carbonaceous feed and the typical rate of use of steam is equal to about 0.2-0.5 pounds of water vapor per pound of carbonaceous feed. The transport reactor is sized so that the gaseous and liquid mixture typically rises at a rate of upwards which corresponds to the surface velocity of about 25-100, preferably about 10-80, and typically 10-40 ft / s

While not critical to the reaction, an inert diluent may be used to control or control the partial pressure of the reactants in the melt as reactants in the reaction zone and / or to aid the gas lift effect of the multiphase hydrocarbon melt mixture "Diluents that may be used include, but are not limited to, helium, carbon dioxide, nitrogen, steam, methane, and the like, in such types of conversion reactions of the carbonaceous materials where the presence of hydrogen is necessary or desirable. The inert diluent would typically be present in a molar ratio of about 0.1-50 moles of diluent per mole of water. *** For example, in reforming, hydrogen desulfurization, or hydrocracking, suitable amounts of hydrogen gas may also be injected into the reaction zone of the carbonaceous feedstock or reactant, and preferably about 0.1-1. "

The present invention is particularly useful for the cracking and partial oxidation or gasification of heavy carbonaceous feeds with a high sulfur content. The conversion of these materials is yet to come

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been economically disadvantageous to the known methods. Such a situation is' undesirable. The reasons are the product conditions that can be achieved and / or the excessive coking in the reaction zones and the need for costly desulfurization treatments to reduce the high sulfur content of the feeds. The present process and technical equipment are suitable for those high sulfur hydrocarbon conversion reactions favored by minimal contact times, such as, for example, cracking heavy carbonaceous feedstocks into ethylene and other products preferred embodiments incorporating cracking and partial oxidation or gasification of heavy hydrocarbon feedstocks to produce ethylene and other products and a gas having low or moderate Btu values, although it is to be understood that the present invention describes a broad reaction technique. which is suitable for any type of chemical conversion reaction capable of being carried out in a melt as a reaction medium.

Generally, in the cracking of asphalts and other heavy hydrocarbon feedstocks for the production of ethylene, the hydrocarbon feedstock with a mixture of carbonates of alkali metals or with a mixture of alkali metal carbonates and alkali metal sulfides at a temperature of about 600-850 ⁰ C and a pressure of about 0 , 5-10 atmospheres, preferably at about 1 atmosphere absolute, contacted. The entry quantities in'der unit of time of the hydrocarbon feedstock and the melt as the reaction medium are adjusted in such a way that in the reaction zone, a transport state of the foam flow is maintained, with a maximum contact time of about 25 seconds is observed. Preferably, the input quantities in the unit of time are adjusted to give a contact time of less than about 5 seconds

and, most preferably, a contact time of about 1 second or less, since ethylene production is favored by a reaction profile with a minimum contact time and temperature. "Optionally, a suitable diluent gas, such as steam or hydrogen, can be the multi-phase mixture of the melt and the hydrocarbon In this case, a molar ratio between the steam and / or the hydrogen and the reactants in the range of about 0.1-1 and preferably of about O ₅ 3 is observed ·

In the partial oxidation or gasification of heavy hydrocarbonaceous feedstocks or in the carbonaceous product of, for example, cracking to produce a gas of low or moderate Btu, composed predominantly of carbon monoxide and hydrogen, the hydrocarbon feedstock will typically be melted an alkali metal carbonate or a mixture of alkali metal carbonates and sulfides at a temperature of about 800-1200 ⁰ O and preferably at a temperature of about 1000 ⁰ G and at a pressure of about 1-20 atmospheres absolutely brought into contact "A 'suitable melt the reaction medium may be sodium carbonate or an admixture of sodium carbonate and sulphide, because at the temperatures used, the sodium metal salt is molten and very fluid. The use of the sodium metal salt as a melt is also desirable because this material is The gasification reaction proceeds almost instantaneously and the stirring time will generally be less than about 10 seconds, preferably less than about 5 seconds, and most preferably less than about 2.0 seconds, "The specific rates of oxygen use will vary depending on whether air, pure oxygen or certain other oxygen-containing gases are used." The ratio of the oxygen-containing gas to the carbonaceous feed becomes

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regulated in the agreement that the production of carbon monoxide and hydrogen from the feedstock is preferred. In order to control the temperature by the extent of the water gas reaction, steam is usually injected into the reaction zone, the specific amount necessarily increasing with increasing temperature. Where use is made of partial oxidation in conjunction with an endothermic reaction, it may be necessary for the purpose of heat supply to regulate heat generation by injecting steam to promote a water gas reaction. Where desired, a complete one To obtain oxidation of the feedstock, the same reaction conditions are usually used, with the exception that the amount of oxygen or the oxygen-containing gas addition is increased in sufficient quantities to cope with complete oxidation. When the oxidation is used in conjunction with cracking to supply heat and the carbonaceous material formed during cracking is insufficient to meet the heat demand, additional feedstock (the same as that supplied to the cracking reaction zone or different therefrom) can be used. be fed directly to the oxidation zone.

In a further embodiment of the present invention, a hydrocarbon conversion reaction according to the present invention is combined with a second reaction or reactions to advantageously utilize the heat transfer capacity of the melt as a reaction medium to sustain a variety of different reactions * For example in cracking heavy carbonaceous feeds, it is desirable to carry out the cracking in conjunction with exothermic coke oxidation and partial oxidation reaction, wherein the coke in the melt can be used as the reaction medium as a result of the energy source cracking to raise the temperature in the endothermic cracking reaction zone -at. to maintain a closed loop operation. In addition, one can

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Reaction to remove the sulfur in conjunction with the krakene and / or the carbon oxidation reaction to convert the sulfide contained in the melt as the reaction medium to valuable hydrogen sulfide gas as a result of the cracking and / or oxidation reaction. "One significant advantage of using the technology Thus, with the melt as the reaction medium in the conversion of carbonaceous feedstock, this technology is readily available for multi-reaction processing.

We now turn to the drawings. Figure 1 illustrates a continuous gasification process according to the present invention in its simplest form. In this Figure, a single reaction zone is used wherein the melt is circulated in a closed loop system The carbonaceous feedstock is passed through the feed line 2 introduced into the lower part of a gasification reaction zone 1 with mixed phases An oxygen-containing gas and steam, if desired, and optionally a diluent gas enter the lower part of said reaction zone through the .Zuleitung 3 a »The melt as a reaction medium occurs the lower part of the said gasification zone 1 with the mixed phases through the feed line (or through the channel) 4 a. The feed can be mixed with the oxygen-containing gas and / or with the vapor, if present, and / or with the diluent gas, if present, prior to actually entering the lower part of said reaction zone. When mixing feedstock, steam, oxygen-containing gas and diluent gas with the melt as the reaction medium in said lower part of said reaction zone, the mixture with the mixed phases flows in a parallel turbulent flow pattern into the upper part of said vertically elongated gasification zone 1 '. During this transport, the chemical reactions take place. "From the upper part of said gasification zone flows the mixed phase, consisting of the

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gaseous products and a melt containing the liquids as well as from i-soaking unused liquid or solid reactants, through the pipe 5 in a separator, which is shown here as a cyclone 6. In the cyclone 6, the gaseous products exit from the upper part of said cyclone through the conduit 7 for further use or separation elsewhere. The liquid portion of the mixed phase working fluid, after entering the cyclone 6, is directed to the lower portion of said cyclone by the operation of the cyclone and exits the lower portion of the cyclone through the conduit 9. The accumulation of fluid in the system is called an interface level 8 which can be maintained in the lower part of the cyclone 6 or in the pipeline 9. As can be seen from Figure 1, the line 9 becomes the inlet 4, through which the melt as the reaction medium to the lower part of the The circulating rate of the melt and the unconsumed liquid or solid reactants can be adjusted during operation by increasing or decreasing the supply of molten iron in the melt is going to the border level 8 within the pipeline 9 and / or at the lower part of the cyclone 6 to increase or decrease (a higher level leads to a higher flow rate for the melt). Some types of feedstock accumulate heavy metals in the form of the elemental metal or in the form of oxides or compounds thereof and / or ashes, resulting in continuous or intermittent removal of the molten medium from the system and replacement of these feeds with one Compensation can be regulated.

We now turn to Figure 2. It is a schematic flow diagram of a continuous gasification process for a sulfur-rich carbon-rich feedstock.

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material "In this figure, the melt flows in a continuous cycle through the gasification zone and the associated cyclone and back to the gasification zone, although separated from each other; but at the same time the fungible or common melt also flows in a continuous cycle between the mixed phase enrichment zone, the associated cyclone and the heat exchanger. Also simultaneously, but independently, the melt flows between the two closed cycles in a separately controlled cycle High sulfur feedstock enters the mixed phase gasification reaction zone 200 through feed line 201 in the lower part of said zone. * Oxygen-containing gas, steam, if present, and / or diluent gas, if any, occur at the bottom of said gasification zone 200 through inlet 202. At this lower zone of the gasification reaction apparatus, the melt enters through inlet 203 and mixes with said feedstock from the feed line and with said oxygen-containing gas and with the steam, if present, and / or with the diluent gas, if present, to form a multiphase mixture in the lower part of said gasification zone. The mixed phase mixture passes from there through the vertically elongated gasification zone to the upper part of said zone, said mixture passing through the pipeline 207 into the cyclone 208 is transferred. The product may be introduced into the mixed phase gasification zone either separately or in the form of a mixture with steam and / or the diluent gas, if present. Although a cyclone is represented in this preferred example, other separators may also be used In the cyclone 208, the gaseous reactants are separated from the liquid consisting of the melt as the reaction medium and the non-gaseous part of the reaction participants. The gaseous reactants leave the cyclone 208 via line 209 and become the subsequent (not shown) separation plant forwarded

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or used as such. The liquid separated in the cyclone 208 passes into the lower part of the cyclone and settles there and is removed via the line 211. In this case, an interface level 210 is formed, which can be maintained in the pipeline 211 or in the lower part of the cyclone 208. The liquid in the line 211 is separated into two parts: a part of which returns via the line 204 in the supply line 203 to complete one of the continuous circuits, which were discussed above. The circulation of the melt within this closed loop system is dependent upon the location of the interface level of the liquid 210 and other physical factors of the reactants and the engineering equipment. The second part of the liquid in the line 211 flows through the conduit 206 for merging with the melt in line 223 to form a mixture in the Rohrlei device 212, wherein the Strö-. In the heat exchanger 213, the melt is cooled by a working medium, such as steam, which enters the heat exchanger 213 through the supply line 225 and leaves through the outlet 224. The cooled melt flows from the heat exchanger 213 through the conduit 214 into the lower part of a mixed-phase enrichment zone 217 for carbonation. A rich CO2 gas enters the lower part of the enrichment zone 217 through the feed line 215. Steam and / or diluent gas, if present, enters the lower portion of zone 217 through conduit 216. The COg-rich gas, vapor and diluent gas, if present, combine with the cooled melt of conduit 214 in the lower part of said carbonization enrichment zone 217 to form a mixed phase mixture flowing upwardly and in parallel through the catalyst The enrichment zone 217 serving for carburizing is dimensioned such that the multiphase mixture of the gases and the liquid will cause a flow which is sufficiently turbulent to allow the enrichment zone 217 to enter the upper part thereof

average density is sufficiently low to achieve a gas lift effect within the vertically elongated enrichment zone 217. The multiphase mixture from the upper part of the enrichment zone 217 exits through line 218 and from there into the associated cyclone 219. Said multiphase mixture is separated in the cyclone 219 into a hydrogen sulfide-rich product gas and a liquid consisting of the desulfurized melt and The hydrogen-rich product gas exits the cyclone 219 through line 220 and from there to an external recovery system, such as a Claus sulfur plant. This is not reproduced? The separated melt in the cyclone 219 passes into the lower part of said cyclone and settles there and leaves the cyclone through the line 222. It is divided into two parts. "The first part of the desulfurized medium in line 222 passes through the line 223 and merges with the melt in line 206 to form a common melt in line 212, as previously mentioned. The melt passes in the continuous cycle through the heat exchanger 213, the enrichment zone and the cyclone 219 back to the heat exchanger 213 to complete that cycle.

In addition to the two continuous circulating systems of the melt, as shown in Figure 2 above, the melt flows from line 222 through line 205 for fusion with line 204, from where the melt enters line 203, as indicated above At the same time, the melt flows back and forth between the two reaction systems, with part of the melt from the gasification system passing via the line 206 to the enrichment reaction system, while an equal amount of the melt flowing in the opposite direction through the line Complete cycle *

Figure 2 shows the pressure in the reaction zone 217 for

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with CO ₂ and in the associated cyclone 21.9 smaller than the pressure prevailing in the gasification zone 200 and the associated cyclone 208. This is accomplished by placing the carbonation zone 217 and associated cyclone in such a manner that the interface level 221 between the hydrogen sulfide gas product and the melt is higher than the corresponding interface level 210 between the gaseous product of the gasification zone and the melt Both reaction zones represent a puncture of the difference in the respective height of the interface levels and other physical factors. During actual operation, the absolute pressure differential can be varied somewhat by adjusting the relative height between the interface level 221 and the other interface level 210 For example, the circulation rate of the melt within the gasification zone 200 and associated cyclone 208 may be varied within allowable limits by raising or lowering the interface level 210 (a higher level Similarly, the circulation rate of the melt in the circuit between the carbonation zone 217 _{5 and} the cyclone 219 and the heat exchanger 213 is set within the allowable limits by the interface level 221 is raised or lowered *

In order to control the flow of the melt back and forth between the two respective closed systems of the reaction zone via the lines 206 and 205, the line 205 is dimensioned in such a way to restrict the flow due to the static differential pressure, or alternatively may be a throttle line or a throttle plate or a valve can be inserted in this line. Throttlings or control valves may also be considered desirable to control the flow of the melt, such as orifice 226 in FIG

- £ 4 -

Line 205 or the throttling 227 in line 2O6 _e Other control or throttling means for regulating the flow are useful, in particular, when a plurality of carbonaceous feedstocks in recurring time intervals is to be processed.

Turning now to Figure 3 · This is a system of two reaction zones where the fungible or common melt is used as the reaction medium for various reactions in each of the two reaction zones. A carbonaceous feedstock enters the bottom of the mixed phase cracking reaction zone 10 via the feed line (or tubing) 11 into this zone. Steam, if present, and / or diluent gas, if any, enters this zone at line 12 at the lower portion of cracking zone 10. The feed may be mixed with the vapor, if present, and / or with the diluent gas, if present, prior to the actual entry into the lower portion of said cracking zone 10. The melt passes at the lower part of said cracking zone 10 via the feed line 13 into the zone. In the lower part of the cracking zone 10 there is a mixing between the melt, the carbonaceous feedstock and the vapor, if present, and the diluent gas, if present, in order to arrive at a turbulent mixed-phase mixture, this flows upwards in a parallel flow principle through the vertically extended cracking reaction zone 10 into the upper part of said zone. In the upper part of said cracking zone 10, the mixed phase consists of gaseous reactants and a liquid from the melt and / or liquid or solid reactants. Said mixed phase mixture is supplied from the upper part of said vertically elongated cracking reaction zone 10 via line 14 to a separator which here corresponds to a cyclone 15. The gaseous products of the cracking reaction emerge from the top of the cyclo ns 15 via line 16 and from there to a separation plant and / or are processed in a further technical system

ν- »- 2 201 72

(not shown). The liquid portion of the material entering the cyclone 15 settles in the lower part of said cyclone and exits through the conduit 18. This forms at the point 17, an interface level, which can be maintained in the conduit 18 or in the lower part of the cyclone 15. "The liquid of the conduit 18 consists of the melt and liquid or solid reactants from the cracking reaction zone» This liquid flows into the line · 19 »enters the lower part of the mixed-phase oxidation zone 22. An oxygen-containing gas enters the lower part of said mixed-phase oxidation zone 22 via the supply line 20. Steam, if present, and / or diluent gas, if present, enters the lower portion of said mixed phase oxidation zone 22 via feed line 21. The oxygen-containing gas may be mixed with steam, if present, and / or diluent gas, if present, prior to introduction into the lower part of said oxidation zone 22. Additional carbonaceous feed may also be introduced into the lower part of said oxidation zone 22 to compensate for any build-up of liquid or solid reaction products to maintain the desired overall system operation and to compensate for the heat balance. Feedstock, steam, if any, and diluent gas, if present, mix with the liquid, consisting of the melt, and liquid or solid carbonaceous reactants to form a multiphase mixture. This flows in a turbulent upward direction through the vertically extended oxidation reaction zone 22 in the upper part of said zone. From the upper part of said oxidation zone ^ 22, the mixed-phase mixture passes via the pipeline 23 into a separation device which here corresponds to a cyclone 24. In this cyclone 24 there is a separation between the vapor phase and the liquid phase. The vapor phase with the gaseous products of the oxidation reaction leaves the cyclone 24 via line 25 for further processing or separation

Liquid from the melt and any liquid or solid reactants accumulates in the lower part of said cyclone 24 and exits through line 27. At this point, an interface level is formed. The interface level 26 may be maintained in the conduit 27 or in the lower portion of the cyclone 24. The conduit 27 is connected to the conduit 13, through which 'the melt completes the circulation by returning to the lower part of the cracking zone 10. The pressure in the oxidation zone 22 and in the associated cyclone 24 can be maintained at a value which varies differs from the pressure in the cracking zone 10 and the associated cyclone 15. For this purpose, the plant must be constructed so that the height of the interface level 26 differs from the height of the interface level 17. By increasing or decreasing the mass of the melt, Thus, by simultaneously raising or lowering the two interface levels, one can increase or decrease the circulation rate of the melt through the plant (raising the two interface levels causes an increase in circulation rate, lowering the two interface levels means a reduced melt circulation rate).

Turning now to Figure 4, this differs from Figure 3 only in that the conduit 28 and a valve or restriction 29 have been added. The insertion of these two constructional elements results in some independent control of the melt circulation rate a reaction zone or through multiple reaction zones is made possible regardless of the total circulation velocity between the respective reaction zones. In Figure 4, the liquid from the cyclone 24, consisting of the melt and any unconsumed liquid or solid reactants, is separated into two parts as follows: A part flows through line 28 and restriction 29 to join the melt and flues -

39 ·

The mixture then flows into the lower part of the oxidation zone 22 from the said pipeline 19. The second part flows into the pipeline 13 (see also FIG the description in connection with Figure 3) · The two independent melts meeting and mixing in the conduit 19 could alternately be introduced into the lower part of said oxidation zone 22 independently of each other · the restriction 29 may consist of a conduit, which is sized so as to allow no current greater than the desired one, or it may be a fixed throttle part, such as a throttle plate or a control valve. The addition of the line 28 and the restriction 29 offers the possibility of regulating the circulation rate the melt through the oxidation zone 22 and the associated cyclone, un Although in some way independent of the circulation rate in the cracking zone 10 and the associated cyclone 15

Turning now to Figure 5, this is a system with three separate reaction zones for independently conducting three separate chemical reactions simultaneously using a fungible or common melt as the reaction medium. This specific example differs from that shown in FIG. 3 in that a portion of the melt is removed after the oxidation reaction has taken place and is used as the reaction medium for carrying out the third chemical reaction. The melt is recycled after use as the reaction medium in the third chemical reaction of the oxidation zone, from where the melt has come. "Alternatively, the melt could be recycled from the third chemical reaction, for example carbonation, instead to the cracking reaction zone. Referring to Figure 5, a carbonaceous feed, such as asphalt, but not limited to this material, enters the bottom of mixed phase cracking zone 100

über.die lead 101 a. Steam, if present, and / or diluent gas, if present, enters the lower portion of said cracking reaction zone 100 via feed line 102. The melt passes into the lower part of the cracking reaction zone 100 via the feed line 103. In the lower part of said cracking reaction zone 100, the melt, the vapor, if present, and / or the diluent gas, if present, then mix these substances. The mixed phase mixture moves through the vertically extended cracking reaction zone 100 into the upper part of this zone. From the upper part of cracking reaction zone 100, the multiphase mixture of gas and liquid flows via line 104 into a separator. This corresponds to the cyclone 105β In the cyclone 105, the gaseous products of the cracking reaction exit via the line 106 and from there to a recovery plant and / or for further use (not shown). The liquid of the cyclone 105, consisting of the melt and the liquid or solid reactants, is separated and settles in the lower part of the cyclone 105, from where the discharge via the line 108 takes place. This results in the formation of an interface level at point 107. This interface level can be maintained in line 108 or in the lower part of cyclone 105. The melt in line 108 merges with the melt from line 131 (described later) becomes). In the pipeline 109, a mixture of these melts, which enters the lower part of the mixed-phase oxidation zone 112 is formed. An oxygen-containing stream is introduced into the lower portion of the oxidation reaction zone 112 via the feed line 110. Steam, precipitate, and / or diluent gas, if present, enters the lower portion of the oxidation reaction zone 112 via the feed line 111. The melt from the pipeline 109 joins and mixes with the oxygen-containing gas of the supply line 110 and with the steam, if present, and / or with the diluent gas, if present, the supply line 111. It forms a multi-phase mixture in the lower Part of said oxidation

3Ί

- * »- 220172

zone 112. This. Multiphase mixture rises in a turbulent parallel flow into the upper part of said oxidation zone 112. From the upper part of said oxidation zone 112, the multiphase mixture flows via line 113 to an associated separation device. It is a cyclone 114, in which the gaseous reaction products of the oxidation reaction are separated from the liquid, consisting of the melt and the liquid or .festen reactants. The gaseous reaction products of the oxidation reaction leave the cyclone 114 via the line 115 for forwarding to a separation device and / or for further processing. The liquid, consisting of the melt and the liquid or solid reactants, settles in the lower part of the cyclone 114, from where the said cyclone is exited via the line 117. In this case, an interface level is formed at the point 116, which can be maintained in the line 117 or in the lower part of the cyclone 114. The liquid in line 117 is divided into two parts. The one part flows through the line 103 back into the lower part of the cracking zone 100. The second part of the liquid in the line 117 passes via the line 118 into a heat exchanger 119, in which the temperature of the melt is reduced by heating a working medium. In this working medium is a circulating oil, which passes into the heat exchanger 119 via the supply line 120 and exits from said heat exchanger 119 via the line 121. The thus cooled melt of the line 118 enters the lower part of the Karbonisierungsreaktionszone 125 via the feed line 124 after the passage through the heat exchanger 119 in the lower part. A CO ₂ rich gas enters this carbonation reaction zone 125 via line 123. Steam and diluent gas, if present, enter the bottom of the mixed phase CO ₂ enrichment zone 125 via line 122. Alternatively, the CO ₂ rich gas and / or vapor and / or diluent gas may be introduced into the melt Lead 118 before the said melt in the heat

Exchanger 119 enters »The melt mixes with the carbon dioxide-rich gas and the steam and with the diluent gas, if present, in the lower part of the carbonation zone 125. This results in the formation of a multiphase mixture. This rises through the vertically extended carbonation reaction zone 125 into the upper part of said zone. From the upper part of said carbonation zone, the multiphase mixture of gaseous reactants and liquid flows via line 126 to a separator, dealing with the cyclone 127 "From the cyclone 127, the gaseous products in the form of a hydrogen sulfide rich gas via the line 128 for further processing, for example, in a Claus system (not shown) from« elemental sulfur is obtained or there is a further processing · The in the Zyklon 127 entering liquid consists of the melt and unused liquid or solid reactants, it settles in the lower part of the said cyclone 127 and exits via the line 130. From the cyclone 127 from. At point 129, an interface level is formed. This can be maintained in line 130 or in the lower part of cyclone 127. The liquid in line 130, which in Figure 5 becomes line 131, returns to mixing with the liquid in line 108 to return via conduit 108 to the lower part of the oxidation zone 112, as mentioned above.

While we still remain at Figure 5, but as shown in Figure 4, the liquid in line 130 could alternatively be divided into two parts: one part, according to the display, returns to the oxidation zone via line 131 and the other part over returning a line (not as shown) to line 118, returning it through carbonation zone 125 with a corresponding restriction or valve, if desired. See the description in conjunction with Figure 4

2 2 01 72

In each of the embodiments illustrated in Figures 1-5, the mixed phase reaction zones are designed and dimensioned such that the multiphase mixtures cause a parallel flow at such a rate that the average density within said reaction zones causes a gas lift effect and a circulation of the melt conditioned as reaction medium. It will be understood, however, that the reaction zones of the second and / or third stages need not be designed and / or operated in this manner so that each of the illustrated embodiments as a whole is within the scope of the present invention.

Optionally, in each of the illustrated embodiments, the stream of melt as the reaction medium exiting the separator (cyclone) for recycle purposes may be subjected to a second or subsequent separation treatment to further remove any gases dissolved therein second separation stage may take the form of a second separation device, such as in a cyclone, or alternatively the melt may be contacted as reaction medium with a stripping agent such as a stripping gas. Such stripping gas may also be used in parallel flow with a second cyclone become.

example 1

An asphalt with a high sulfur content is cracked to produce ethylene by the process with reference to Figure 3. "The melt consists of a eutectic mixture of lithium, potassium and sodium carbonates. In this mixture, an alkali metal sulfide concentration of about 5% by mass is maintained. The. Asphalt feedstock is first preheated to a temperature of about 250 ° C. Subsequently, the contact with the melt takes place as a reaction medium in the lower part of the reaction zone such that the upward velocity of the. Range of 10-100 ft / s, preferably in the range of 20-40 ft / s. Steam and / or dilution

Gas can also enter the lower part of the cracking reaction zone. The circulation rate of the melt is maintained between 1 and 15 pounds of the melt per pound of the total feed including the vapor and the diluent gas in addition to the asphalt Thus, a steady state operating condition of a foam flow in the Crack reaction zone justified. There is a total contact time between the reactants and the molten salt of about 1-10 seconds, preferably about 2 seconds. The processing capacity and ethylene yields of the present process are then measured by the known cracking process using a melt as the prior art reaction medium compared to the technique as described in the U S. Patent Ur 3745109. All other reaction conditions are maintained in each process to similar values, wherein the temperature is about 850 ⁰ C and the pressure is about 1.3 atmospheres absolute corresponds in each cracking zone "In contrast to the present method, the cracking process according to the counter-Etromprinzip according to the prior In the prior art, input quantities in the unit of time corresponding to about 1/10 of those used in the present invention are used. "The contact times in the old method are approximately 3-5 times as long as those in the present invention Invention·

Example 2

Similar to Example 1, a heavy hydrocarbon residue recovered by distillation is gasified according to the procedure in Figure 1. The results are compared with those obtained by a known countercurrent gasification reaction. Each reaction zone is maintained at a temperature of about 1000 ⁰ C and at a pressure of about 1.5-15 atmospheres. oxygen-containing

-% - 2 20172

Gas (air) and steam are fed to the reaction zone, with a mass ratio between the steam and the oxygen of about 0.3-5.0 pounds of water vapor per pound of oxygen depending on the heat losses and the purity of the oxygen. The feed rate in the unit time of the hydrocarbon residue and the oxygen-containing gas and steam in the process of the present invention is regulated to give a steady state operating condition of the foam flow within the reaction zone. The feed rate in the unit time is about 10-100 ft / s, and preferably about 20-40 ft / s. Conversely, to maintain a countercurrent flow between the melt and the hydrocarbon residue by the prior art method, the feed rate in The time units per unit time of the hydrocarbon residue and the oxygen-containing gas and vapor are maintained at about 2.0 ft / sec. The above-mentioned unit time inputs are sufficient to provide approximately 0.5 second contact times in the method of the present invention and about 3-5 seconds in the gasification process of the earlier type. A comparison of the two methods shows that far greater amounts of hydrocarbon residue, on the order of about 10 times, can be processed by the process of the present invention, comparing the processing capabilities of the prior art countercurrent process. Added to this is the greater extent of the technical equipment according to the prior art · The percentage total heat losses through the container walls are about 4 times larger.

It can thus be seen from the above examples that a significant increase in the processing capacity results from the contact of a hydrocarbon-containing feedstock with the melt as Reaktionsraedium when transported in the context of a multiphase DC foam flow. This exists

2 2 0172

the ability to realize, for the first time, the competitive, commercial use of melt technology as a reaction medium in the conversion of hydrocarbonaceous feedstocks. "In addition, many reactions have improved product yields due to the much shorter contact times that can be achieved. Accordingly, the present invention is an improved and highly effective process for the conversion of carbonaceous feeds.

While the present invention has been described by way of preferred embodiments and illustrated by way of example, various modifications, subtleties, omissions and changes may be made without departing from the spirit of the invention. Accordingly, it is intended that the scope of the present invention is defined solely by the scope of the points of the invention claim below.

Claims (17)

17, 9. 80 AP C 10 G / 220 172 GZ 57 266 12 - 220172 Inventive claim A process for the conversion of a carbonaceous material into more valuable products by means of a melt as a reaction medium, characterized in that it comprises the following steps: a) contact of a carbon-containing Starting material with a melt as reaction medium while maintaining at a temperature above the melting point of the medium in the lower part of a substantially vertical extended reaction zone to form a mixture of the carbonaceous feedstock and the melt as the reaction medium, wherein at least one gaseous material under the conditions of the reaction zone is present and a multiphase mixture is formed; b) hydraulically transporting the multiphase mixture substantially in an upward direction through the reaction zone into the upper part thereof in a parallel flow of the components of the mixture and at a rate sufficient to cause a gas lift effect in the reaction zone, wherein a chemical conversion reaction for production a multi-component mixture takes place; c) passing the multicomponent mixture from the upper part of the reaction zone to a separation device; d) separating the multicomponent mixture into a gaseous product stream and a liquid stream consisting of the melt containing at least one non-gaseous product; Passing at least a portion of the liquid stream of the melt as the reaction medium containing a non-gaseous product to a recovery plant; f) removing at least a portion of the non-gaseous product from the liquid stream of the melt as the reaction medium and g) recycling the melt as the reaction medium after removal of at least a portion of the non-gaseous. from this product to the vertical extended reaction zone -1-220172 2. The method according to item 1, characterized in that the remainder of the separated liquid stream of the melt is returned as a reaction medium in the lower part of the reaction zone * 3. The method according to item 2, characterized in that a gaseous reactant is introduced into the lower part of the vertical, extended reaction zone. 4 _e method according to item 3, characterized in that the gaseous reactant is selected from the group consisting of an oxygen-containing gas, steam, halogen, Leichtkohlenwassorstoff, hydrogen or mixtures thereof « 17. 9. SO AP C IO G / 220 172 57 266 12 4-S Liquid stream is contacted with carbon dioxide and steam to adjust the concentration of sulfur compounds in the liquid stream and remove a portion of the sulfur content of the melt as hydrogen sulfide rich gas. 34. A method according to item 30, characterized in that at least a portion of the first liquid stream is supplied to a third reaction zone and the first liquid stream is contacted with carbon dioxide and steam to adjust the concentration of sulfur compounds in the liquid stream and remove a portion of the sulfur content the melt as hydrogen sulfide rich gas. 35. A method according to item 30, characterized in that the first liquid stream is contacted with an oxygen-containing gas in the second reaction zone to at least partially oxidize the carbonaceous reactants present in the first liquid stream. » 36, method according to item 33 or 34, characterized in that the step of sulfur adjustment takes place following the cooling of the first liquid stream, 37. The method according to item 1 or 30, characterized in that the carbonaceous feedstock is selected from the group consisting of crude oil, shale oil, natural tars, coal, pitch, tar sand oil, from the fractions, residues, products, polymers, resins, 17. 9. 80 AP C 10 G / 220 172 GZ 57 266 12 synthetic tars and waste thereof and mixtures thereof, 38, process according to item 37, characterized in that the feedstock is an asphalt or a hydrocarbon residue, prepared by distillation or distillation and solvent extraction of crude oil, 39, process according to item 1 or 30, characterized in that the melt contains as reaction medium a catalytic material as an admixture, 40, process according to item 39, characterized in that the melt contains as reaction medium about O to 50% by mass of the catalytic material, 41, method according to item 39, characterized in that the melt contains as reaction medium about 10 to 25 mass% of the catalytic material, 42, Process according to item 30, characterized in that the melt as the reaction medium is a mixture of an alkali metal or of alkali metals selected from the group consisting of sodium, potassium and lithium, the carbonates, sulfides, chlorides, sulfates and sulfites thereof Alkali metals or mixtures thereof, 43, method according to item 30, characterized in that the transport speed of the first multiphase mixture in the first reaction zone is so great that the 17. 9. 30 AP C 10 G / 220 172 GZ 57 266 12 velvet contact time between the feed and the melt as the reaction medium is less than about 5 seconds. Process according to item 30, characterized in that the conversion reaction comprises at least one gasification reaction in which a carbonaceous feedstock is converted to a gas with low or medium ßu-LVerten. 45. Method according to item 30, characterized in that. the conversion reaction consists of a dehydrogenation reaction, 46. A method according to item 30, characterized in that the conversion reaction consists of the dehydrogenation of ethylbenzene, 47. The method according to item 30, characterized in that the conversion reaction consists of the reforming of naphtha * Method according to item 13 or 30, characterized in that the conversion reaction for the conversion of the carbonaceous feedstock consists of the gasification of coal, asphalt, circulating oil, tar sand oil, shale oil or hydrocarbon residues. 49. The method according to item 30, characterized in that the second reaction treatment of the melt as the reaction medium comprises a sulfur content adjustment stage, wherein the melt as the reaction medium with CO ₉ and steam • 17. 9 * 80 AP C 10 G / 220 172 GZ 57 266 12 is brought into contact to convert a portion of the sulfur compounds contained in the melt into a hydrogen sulfide-rich gas, 50 _e method according to item 49, characterized in that the melt as the reaction medium also has a content of carbon or a carbon-rich material and the carbon content or on the carbonaceous material during the entire sulfur content adjustment step remains. 51. The method according to item 49, characterized in that the sulfur content of the melt is adjusted as the reaction medium such that the melt has less than about 25% by mass of sulfur compounds, 52. The method according to item 30, characterized in that the melt is brought as a reaction medium between the reaction zones without the aid of a pump for circulation. Method according to item 30, characterized in that each separation stage consists of separating the gaseous product and the melt by means of a cyclone. 54, method according to item 30, characterized in that the ratio of the melt as the reaction medium to the feed which must be reacted in each of the first and second reaction zones is independently controlled. 55, method according to item 30, characterized in that the first reaction is kept at a pressure which 17. 9. 80 AP C 10 G / 220 172 GZ 57 266 12 54
- 49 - differs from the pressure of the second reaction zone. 56, device for converting a carbonaceous material into more valuable products using a melt as a reaction medium in a closed circuit by the method according to item 1 - 55, characterized in that it comprises the following components: a) means for contacting a carbonaceous feedstock with a first melt as the reaction medium while maintaining at a temperature above the melting point of the melt in the first lower portion of a substantially vertical extended first reaction zone to form a mixture of the carbonaceous feedstock and the melt as the reaction medium; wherein at least one gaseous material is present under the conditions of the first reaction zone and a first multiphase mixture is formed; b) means for hydraulically transporting said first multi-phase mixture substantially upwardly through said first reaction zone in the first upper portion thereof in a parallel flow of the components of the first mixture and at a speed sufficient to provide a gas lift effect in said first reaction zone to effect; c) means for passing the first multiphase mixture from the first upper part of the first reaction zone to a first separation device, 17. 9 * 80 AP C IO G / 220 172 GZ 57 266 12 Sl . d) means for separating the first multiphase mixture into a first gaseous product stream and a first liquid stream consisting of the melt as the reaction medium; e) means for supplying at least a portion of the first liquid stream to a second reaction zone; · ' F) means for carrying out a second chemical reaction in the melt as a reaction medium of the first liquid stream in the second reaction zone and g) means for returning at least part of the melt as reaction medium from the second reaction zone back to the first lower part of the first reaction zone. 57. Apparatus according to item 56, characterized in that it comprises a) means for contacting at least a portion of the first liquid stream corresponding to the melt as the reaction medium with an oxygen-containing gas in the second lower portion of the second substantially vertical extended reaction zone to form a second multiphase mixture within the lower portion, wherein 'at least' a gaseous material is present under the conditions of the second reaction zone; 17. 9. 80 AP C 10 G / 220 172 GZ 57 266 12 53
-SL- c) means for passing the second multiphase mixture from the second upper part of the second reaction zone to a second separation device; d) means for separating the second multiphase mixture into a second gaseous product stream and a second liquid stream consisting of the melt as the reaction medium and e) means for supplying at least a portion of the second liquid stream, which corresponds to the melt as the reaction medium, to the first lower part of the first reaction zone. Apparatus according to item 57, characterized by comprising means for feeding at least part of the second liquid stream to a third reaction zone and means for contacting the liquid stream with carbon dioxide and steam to adjust the concentration of sulfur compounds contained therein and removing part of the sulfur content the melt as hydrogen sulfide rich gas. Apparatus according to item 57, characterized by comprising means for supplying at least a portion of the first liquid stream to a third reaction zone and means for contacting the first liquid stream with carbon dioxide and steam to adjust the concentration of sulfur compounds contained therein and removing part of the product 17, 9. 80 AP C 10 G / 220 172 GZ 57 266 12 Sulfur content of the melt as a hydrogen sulfide-rich gas. 60, device according to item 58 or 59, characterized in that the means for contacting for the purpose of setting sulfur adjoin a device for cooling for the third reaction zone. 61o method, according to point 1 for the conversion of a carbon. containing feedstock into other products by means of a melt as a reaction medium, characterized in that it comprises the following steps: a) contacting a carbonaceous feedstock with a melt as reaction medium while maintaining at a temperature above the melting point of the medium in the lower part of a substantially vertical extended reaction zone to form a mixture of the carbonaceous feedstock and the melt as the reaction medium, at least one gaseous Material is present under the conditions of the reaction zone and a multiphase mixture is formed, * b) hydraulic transport of the multiphase mixture substantially in an upward direction through the reaction zone into the upper part thereof in the course of a parallel flow of the components of the mixture and at a rate sufficient to produce a gas lift effect in the reaction zone, wherein the supplied hydrocarbons are chemical to a 5, process according to item 2, characterized in that a diluent gas is introduced into the lower part of the vertical extended reaction zone, 6 «method according to item 5, characterized in that the diluent gas consists of nitrogen or steam. 7. The method according to item 2, characterized in that the gaseous product stream is subjected to an additional gas / liquid separation stage for the purpose of recovering additional melt as the reaction medium, which was entrained in the stream. 8. The method according to item 2, characterized in that the separate liquid flow of the melt is brought as a reaction medium with a stripping gas for the purpose of removing the dissolved gas from it in contact * The process according to item 2, characterized in that the conversion reaction of the carbonaceous feedstock in the cracking of a less valuable carbonaceous feedstock at least partially consists of a more valuable gaseous hydrocarbon product. 10. The method according to item 2, characterized in that the carbonaceous feed is selected from a group consisting of vegetable and mineral oils, crude oils, Schieferöf, natural tars, coal, pitch, tar sand oils; from the fractions, residues, products, polymers, resins, synthetic tars and waste therefrom; and mixtures thereof. 17. 9. 80 AP C 10 G / 220 172 GZ 57 266 12 - 58 - Process according to item 9, characterized in that the inferior hydrocarbon feedstock is an asphalt or hydrocarbon residue produced by the distillation or distillation and solvent extraction of crude oil, shale oil, tar sand oils or coal in the liquid phase, 12 * Process according to item 2, characterized in that the carbonaceous feedstock consists of rubber, carbon black and lubricating oils and waste or fractions thereof or a combination thereof, A method according to item 2, characterized in that the conversion reaction for converting the carbonaceous feedstock from the partial oxidation of a less valuable carbonaceous feedstock into a more valuable gas 14. The method according to item 13, characterized in that the conversion reaction for the conversion of the carbonaceous feedstock consists of the partial oxidation of coke. 15. The method according to item 1, characterized in that at least part of the separated liquid stream of the melt is treated as the reaction medium in a manner to remove some of the existing sulfur content before the melt is recycled to the reaction zone. 16. The method according to item 15, characterized in that the 17. 9. 80 AP C 10 G / 220 .172 GZ 57 266 12 - 59 - Reducing the sulfur content of the melt as the reaction medium by contacting the melt with carbon dioxide and steam to chemically convert the alkali metal-sulfur compounds present in the melt into alkali metal carbonates and hydrogen sulfide gas, and then separating the hydrogen sulfide gas from the melt, 17, method according to item 15 or 16, characterized in that the melt as the reaction medium also has a content of carbon or on a carbonaceous material and the content of carbon or on the carbonaceous material remains in the melt during the entire treatment. A process according to item 15, characterized in that the amount of melt subjected to the treatment to remove the sulfur compounds is sufficient to maintain, under steady-state operating conditions, the amount of sulfur compounds in the melt below about 25% by weight thereof becomes, 19. The method according to item 1, characterized in that takes place relative to the part of the separated liquid stream of the melt as the reaction medium heat transfer, 20, process according to item 19, characterized in that the non-gaseous product content of the part of the separated liquid stream of the melt is treated as reaction medium by the following steps: 17. 9. 80 AP C 10 G / 220 172 GZ 57 266 12 Hl a) feeding the part of the separated liquid stream of the melt as a reaction medium in the lower part of a second, substantially vertical extended reaction zone; b) contacting the separated liquid stream of the melt as a reaction medium with a CO ₂ - and steam-containing gas to form a second multi-phase mixture; c) hydraulically transporting the second multiphase mixture of the CO ₂ and vapor containing gas and the melt upwardly through the second reaction zone into the upper part thereof in a parallel flow of gas and liquid to thereby carbonize the non-gaseous product, wherein the second multiphase mixture is transported at a rate sufficient to effect a gas lift effect in the second reaction zone; d) forwarding the second multiphase mixture from the upper part of the second reaction zone to a second separation device and e) separation of the second multiphase mixture into a second gaseous product stream and second liquid stream of the melt reduced in respect of the non-gaseous product content. 21. The method according to item 19, characterized in that the amount of the part of the separated liquid stream - 41 - 17. 9. 80 AP C 10 G / 220 172 GZ. 57 266 12 22Qi ₇₂ the melt as the reaction medium, which is subjected to the treatment steps, such a proportion, the. sufficient to maintain a steady state equilibrium sulfur content of the process during a continuous operation, 22, Method according to item 2 or 9, characterized in that the melt as the reaction medium consists of ein.em alkali metal selected from the group consisting of , Sodium, potassium and lithium, the carbonates, sulphides, sulphates, sulphites and chlorides of these alkali metals and mixtures thereof « 23, process according to item 22, characterized in that the melt as the reaction medium consists of an alkali metal carbonate, an alkali metal sulfide or a mixture thereof, 24, method according to the items 1, 9 or 13, characterized in that the transport speed of the multiphase mixture is so large that the Gesarntzuührungszeit between the carbonaceous feedstock and the melt as the reaction medium is less than about 3 seconds. 25, method according to item 24, characterized in that the contact time is less than about 1 second, 26, method according to item 1, characterized in that the melt of an elemental metal, a mixture of elemental metals, a metal salt, 17. 9 _β 80 AP C 10 G / 220 172 GZ 57 266 12 a mixture of metal salts and a mixture of the metal salt and the elemental metal. 27, process according to item 26, characterized in that the melt is composed as the reaction medium of an alkali metal, a mixture of alkali metals, an alkali metal salt, a mixture of alkali metal salts or a mixture of an alkali metal and an alkali metal salt, 28 .. Method according to item 1, characterized in that the method is operated continuously, Method according to item 1, characterized in that the method is operated without the use of a mechanical pump, Method according to item 1 for the conversion of a carbonaceous material into more valuable products in the context of a closed circuit using a melt as a reaction medium, characterized in that it comprises the following steps; a) contacting a carbonaceous feedstock with a first melt as the reaction medium while maintaining at a temperature above the melting point of the melt in the first lower portion of a substantially vertical extended first reaction zone to form a mixture of the carbonaceous feedstock and the melt as the reaction medium , wherein at least one gaseous material under the conditions of the first reaction 17. 9. 80 AP C 10 G / 220 172 GZ 57 266 12 HS
- 43 - zone is present and a first multiphase mixture is formed; b) hydraulically transporting the first slurry mixture substantially upwardly through the first reaction zone into the first upper portion thereof in parallel flow of the components of the first mixture and at a rate sufficient to effect a gas lift effect in the first reaction zone; c) passing the first multiphase mixture from the first upper part of the first reaction zone to a first separation device; d) separating the first multiphase mixture into a first gaseous product stream and a first liquid stream consisting of the melt as the reaction medium; e) feeding at least a portion of the first liquid stream into the lower portion of a second, substantially vertical extended reaction zone to form a second multiphase mixture within the lower portion, wherein at least one gaseous material is present under the conditions of the second reaction zone; f) hydraulic transport of the second multiphase mixture substantially in an upward direction through the , second reaction zone to the second upper part thereof in the course of a parallel flow of the components of 17. 9 »80 AP C 10 G / 220 172 GZ 57 266 12 hb. - 45 * - second multiphase mixture and at a rate sufficient to effect a gas lift effect in the second reaction zone; g) passing the second multiphase mixture from the second upper part of the second reaction zone to a second separation device; h) separation of the second multiphase mixture into a second gaseous product stream and a second liquid stream consisting of the melt as the reaction medium and i) feeding at least part of the second liquid stream of the melt as reaction medium to the lower part of the first reaction zone. « 31 »Process according to item 30, characterized in that a cracking reaction also takes place in the first reaction zone« 32. The method according to item 30 or 31, characterized in that the second chemical reaction comprises at least one partial oxidation reaction, wherein the oxygen of an oxygen-containing gas is reacted with the reactants, which are in the first liquid keitsstrom «. 33, method according to item 30, characterized da-by that at least a portion of the second liquid stream is supplied to a third reaction zone and the second 17. 9. 80 AP C 10 G / 220 172 GZ 57 266 12 S-2201 17. 9. 80 AP C 10 G / 220 172 GZ 57 266 12 SS React multicomponent mixture; c) passing the Mehrkcmponentengemisches from the upper part of the reaction zone to a separator; d) separation of the multicomponent mixture into a gaseous product stream and a liquid stream _t comprising the melt, all reactants introduced into the melt flowing parallel to the medium, and the gaseous reaction products flowing separately from the multicomponent mixture without passing through a liquid phase interface. See. .3 .Sides Drawings