DE2536249A1 - PROCESS FOR THE CONTINUOUS PRODUCTION OF HEATING GAS AND SYNTHESIS GAS FROM SOLID CARBON FUELS - Google Patents

Description

Patent assessor Hamburg, clsn June 4, 1975

Dr. Gerhard Schupfner _{φ ns} - _nX o η

Deutsche Texaco AG ^{x n u} ^ ^v

2000 Hamburg 13

Mittelweg 180 "253B2 & 9

ICO DEVELOPMENO? CORPORATION 135 East 42nd Street New York, N.Y. 10017 U.S.A.

Process for the continuous "production of heating gas and synthesis gas from solid, carbonaceous fuels

The invention relates to a continuous process for the production of heating gas and synthesis gas from solid, carbon-containing fuels by partial oxidation of a hydrocarbon-containing fuel with .einem. oxygen-containing gas in the presence of a temperature moderator in the reaction zone of a packing and flow-free, non-catalytic gas generator, the product gas essentially containing H ₂ and CO and optionally at least one of the following substances: CO ₂ , H ₂ O, CH ₄ , N ₂ , A. , COS and H ₃ S.

Due to rising oil prices and decreasing natural gas deposits is Today it has become necessary to use other natural fuel resources the exploitation of which was uneconomical a few years ago. Although there are large stocks of inexpensive Coal and oil shale deposits exist, preparing the general application of these solid, carbonaceous materials for the present Time still difficulties. They often contain very high levels of sulfur compounds, which makes their use severely restrict as fuel. Environmental regulations also require that all waste products get rid of harmful substances.

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The object of the present invention is the production of heating gas and synthesis gas from solid, carbon-containing To simplify fuels technically and to improve the profitability of production. Another task of the The process is to produce heating gas and synthesis gas in a particularly environmentally friendly way.

The inventive method works with two different, separate slurries of solid, carbonaceous Fuels as starting material. The slurries are simultaneously in a gas generator free of flow obstacles brought together and converted into synthesis gas or a clean fuel gas by partial oxidation. The emerging Heating gas can be burned without polluting the environment.

The two pumpable slurries become simultaneously passed through a double ring burner attached to a gas generator. One slurry contains a solid, carbonaceous fuel and water as the liquid carrier, while the other is a solid, carbonaceous slurry Fuel and liquid hydrocarbon fuel as the carrier substance. Which becomes a slurry passed through the central duct and the other through the outer ring of the burner. At the same time it becomes a free oxygen containing gas sent as a reactant through an intermediate ring line of the burner in such a way that it is between flows through both streams of slurry. The three reactant streams are simultaneously in the refractory lined reaction zone of the unobstructed, non-catalytic gas generator introduced where they collide, atomize and mix with each other. The velocity of the slurry streams is about 0.3 to 150 m / sec, the speed of the oxygen-containing gas about 30 m / sec up to the speed of sound.

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The partial oxidation takes place in the reaction zone of the gas generator at a self-adjusting temperature of about 816 ° to 1 ° / 10 ° C and a bridge of about 1 to 250 atm instead. The exhaust gas leaving the gas generator is divided into two streams. The first partial flow is cooled in a waste heat boiler for production °?) Ampf. This cold one The gas stream is then washed with liquid hydrocarbon fuel or water to remove entrained plague particles to remove. Optionally, acidic gases can also be removed using conventional gas cleaning processes, to produce a clean, dry synthesis gas or heating gas. The second partial flow of the exhaust gas from the gas generator is introduced into a quench tank, where it is cooled and washed with water. This will make one more saturated with water Process gas stream produced in a water gas conversion zone entered to increase the .H ^ / CO molar ratio can be.

The advantage of the method according to the invention is that readily available, solid, carbonaceous fuels can be converted very economically into a clean heating gas or into synthesis gas. The heating gas has with an upper calorific value of about 750 to 4000 Kcal / Hm. The advantage of the method according to the invention is made clear by the reduction in the following weight ratios: Water to fuel, oxygen to fuel, and liquid hydrocarbon to all solid fuel.

In the following the invention is based on an embodiment ■ game and two drawings explained in more detail. The figures show: FIG. 1, a purely schematic arrangement for carrying out the method according to the invention . Procedure,

Figure 2 pure vertical cross section through the central axis a burner operating according to the invention for the simultaneous introduction of two slurries and one containing oxygen Gas in the gas generator.

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The following substances, individually or in mixtures, can be used as the starting material for the solid, carbon-containing fuel: coal, coke from coal, black coal: petroleum coke, oil shale, tar sands, pitch, carbon particles. With the exception of carbon particles, which are less than 10 microns in size, all other solid carbonaceous fuels are ground to a certain particle size. This is selected in such a way that 100% of the ground material is passed through standard sieves of size 425 Λϋη (ASTM E 11/70, alternative no.40) and ^ZU : at least 80 % through standard sieves of size 75 (ASTM E 11/70, alternative no. 200) can happen.

As a starting material, coal can be of any type, e.g. B. anthracite coal, bituminous coal and lignite can be used. Coal is the very porous residue of coal and mineral ash and is produced by heating coal, e.g. B. coal, obtained in the absence of air in a coke oven. One can "Schwelkohle by heating coal to a temperature of about 316 ° gain to 871 ⁰ C, and this can be done with or without the presence of air, hydrogen or synthesis gas. For example, charcoal can be produced in a fluidized bed system as described in US- PS 3 715 30I. Petroleum coke consists of dehydrated and condensed hydrocarbons of high molecular weight and has a matrix form of considerable physical expansion. It contains essentially carbon and only a very small amount of dispersed petroleum-based asphalt-like compounds the process of the invention is suitable and can be prepared by delayed char or by a similar process for converting heavy residue fuels to gasoline, gas oil or coke. A typical delayed char process is described in Kirk-Othmer, Encyclopedia of Chemical Technology, 2nd edition, vol. 15, Inter-Science Publisher 1968, pages 20-23.

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Calcined petroleum coke and liquid coke are also suitable as starting material. As a bridging tand from the distillation of tar or tar products one receives as one black, amorphous, solid or semi-solid hate the bad luck. Carbon particles or free carbon soot are in the ν Exhaust gas from the gas generator after partial oxidation in a proportion of up to 20% by weight (basis weight of the carbon found in the fuel. The carbon particles are okay oleophilic as well as hydrophobic. Its oil absorption number is greater than 1 and it usually has one gram of carbon particles Absorb 2-3 cm * of oil.

Some typical solid carbonaceous fuels are in given in Table I at the end of the description. As soon as these solid fuels in the method according to the invention To be used, they must first be ground to a suitable size and coated with a liquid vehicle be mixed. This is done using a pumpable slurry produced as the first reactant which has a solids content of about 30 to 65% by weight, preferably 4-5 to 60% by weight, having. The first slurry is made by mixing a liquid hydrocarbon fuel with a solid carbonaceous fuel Fuel produced. Preferably, the liquid hydrocarbon fuel consists of scrubbing liquid, which is enriched with carbon particles from the exhaust gas of the gas generator.

The second reactant consists of a slurry that is a mixture of a solid, carbonaceous fuel and Is water and has a solids content of about 30 to 65% by weight, in particular 45 to 60% by weight.

The third reactant used is a gas consisting of air, air enriched with oxygen (at least 22 mol% oxygen), almost pure oxygen (at least 95 mol % oxygen) or mixtures thereof.

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The remaining components of the gas contain N ₂ and rare gases. In order to reduce the content of nitrogen and other gaseous impurities in the product gas, pure oxygen is preferably used as the third reactant.

In the present process, either the first or second reactant is introduced into the reaction zone through the central nozzle of a three-nozzle burner. The other of the two reactant streams is passed through the outer coaxial ring nozzle. The third reactant (gas containing free oxygen) is sent simultaneously through a coaxial intermediate ring nozzle, which is arranged concentrically around the central nozzle and axially symmetrically in the outer ring nozzle. When the first and the second reactant to the burner pass, they have a temperature of about 4 ° to ⁰ 37o C and a speed of about 0.3 to 150 m / sec, preferably 1.5 to 75 m / sec, the torch head . In contrast, the third reactant has a temperature of 4 ° to 816 ⁰ C and a speed of about 30 m / sec to sonic velocity, preferably 60 to 135 m / sec, the torch head on. Through this nozzle shape, the gas containing free oxygen emerges at the burner head as a hollow, conically shaped gas stream which tapers towards the longitudinal axis of the burner and which is arranged between the first and second reactant streams. This allows the gas stream containing free oxygen to penetrate deeply into the two slurry streams and cause them to mix completely. With respect to the longitudinal axis of the burner, the outer and the intermediate ring channel are inclined slightly inward, the angle of inclination being approximately 10 to 70 °. Once the first and second slurry streams collide at the burner tip, the particle size of the solid gas components in both streams is further reduced. The intermediate gas stream containing free oxygen meets the two slurry streams at high speed, forming a mist of small, solid particles. As a result, an essentially homogeneous and observable

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borrowed dispersion of fine particles of the solid, carbonaceous Fuel in the atomized liquid hydrocarbon fuel, HpO and oxygen produced. The efficiency the combustion is improved and the weight ratios of steam to fuel, oxygen to fuel and all liquid hydrocarbon fuel is reduced to solid carbon "fuel.

The ratio of solid carbon fuel, liquid hydrocarbon fuel, water and oxygen when fed into the gas generator is carefully regulated. It is thereby an integral part of the carbon oxide (at least 80 wt .-%) to carbon (CO and CO ₂₎ to be converted and a self-adjusting reaction temperature of about 816 ° to 1927 ° C, maintained preferably 982 ° to 1538 ⁰ C. will. The pressure in the reaction zone varies from 1 "to 250 atm. The reaction time is about 0.5 to 50 seconds, preferably 1.0 to 10 seconds The reaction zone amounts to 0.1 to 1.3, preferably 0.2 to 0.50 The atomic ratio of oxygen in free oxygen-containing gas to carbon in the total fuel is about 0.6 to 1.6, preferably 0.8 to 1 , 4. It is common practice to express the ratios in the manner indicated, since the denominator in the ratio is 1 and the numerator is equal to the specified range, here 0.6 to 1.6.

There are 0.1 to 3 parts by weight, preferably 0.5 to 1.5 parts by weight of said slurry of solid carbonaceous' Fuel and liquid hydrocarbonaceous Fuel into the reaction zone per part by weight of solid carbonaceous fuel and slurry Water introduced.

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About 0.8 to 12 parts by weight, and preferably 2 to 12 Parts by weight of total solid carbonaceous fuel are reacted in the gas generator per part by weight of liquid hydrocarbon-containing fuel.

The off-gas stream from the reaction zone is split into two streams for cooling, cleaning and removing entrained plague. One gas stream is cooled in a waste heat boiler and the other is cooled by quenching in water from a quench tank. If desired, acidic gases can e.g. B. H ₂ S, COS, CO _P and mixtures thereof, are removed from the exhaust gas stream. In this way, heating gases can be produced that can be burned without polluting the environment. The calorific value can also be increased with the help of this process. Alternatively, the product gas can be used as synthesis gas feedstock in order to reduce the consumption of sulfur-sensitive catalysts.

The exhaust gas leaving the synthesis gas generator has the following composition in mol%: H ₂ : 8.0 to 60.0, C ^: 8.0 to 70.0, CO ^: 1.0 to 50.0, H ₃ O : 2.0 to 50.0, CH ₄ : 0 to 30.0, H ₂ S: 0 to 1.0, COS: 0 to 0.7, N ₃ : 0 to 85.0, A: 0 to 2 , 0. About 0.5 to 10% by weight of throat particles are entrained in the exhaust gas stream (basis weight νβη carbon in the gas generator feed gas). As mentioned before, the exhaust gas flow is now divided into two gas flows, which are cooled separately from one another.

The first partial exhaust gas flow is about 5 to 95% by volume, preferably 75 to 95%, v »m total volume of the exhaust gas from the Gas generator. It is at a temperature ν · η about 93 to 982 C, preferably 204 to 316 * C, through indirect heat exchange cooled with water in a waste heat boiler. At the same time steam is produced at a temperature of about 204 ° to 343 ° C. The throat particles are after , known method 1 emerged from the first exhaust gas flow

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see being a liquid hydrocarbon fuel is used as a washing liquid. (See US Pat. No. 3,639,261). The process gas is then dispersed separated from carbon particles / liquid hydrocarbon fuel in a common oil evacuation container. The dispersion contains about 1 to 20% by weight of solid particles which are drawn off from the bottom of the expulsion container and with the grated, solid, carbonaceous one Fuel in an ordinary. . "Grinding system are mixed.

All carbon particles and other entrained solid particles, such as B. Ashes that have remained in the process gas stream can be removed in a second washing stage will. In this case, the process gas flow is passed through a nozzle washer, similar to that of the first washing stage washed with water. This produces a clean product gas that contains less than 5 mg of carbon particles per 2831 liters of gas (100 Standard Cubic -Feet) contains, in the water expulsion vessel, a water dispersion that is about 0.001 to 0.2% by weight Contains entrained solid particles, separated. This dispersion is made by a method described later further concentrated and used as part of the injection into the gas generator. The gaseous impurities can be removed from the process gas stream by known means.

The previously mentioned second partial flow of the exhaust gas from the gas generator is cooled by direct quenching in water in a quench tank. (See U.S. Patent 2,896,927). While 'the process gas in Quencliwösser - rises, which is maintained at a temperature in the range of 10 ° to 232 ⁰ C, can be washed out of the process gas stream all carbon and other entrained solid particles, such as ash substantially, the water being evaporated.

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A product gas saturated with water is withdrawn from the top of the quench tank. If desired, this gas stream can be subjected to a water gas conversion reaction in order to increase the Hp / CO ratio. H ₂ O and any gaseous impurities can then be removed by known methods.

A water dispersion of carbon particles and ash, which contains about 0.1 to 2.0% by weight of solid particles from the sediment of the water quench tank is mixed with the dispersion from water and entrained solid particles, such as. B. Kohl ens to ff particles, which .wurden from the previously described water expulsion vessel .wurden ^ by ordinary ! Liquid / solid separation processes, such as B. settling, filtration and centrifuges processes, clarified water is from the dispersion removed. For example, the dispersion can be discharged into a settling tank, from which the following three streams are withdrawn: Lein stream to coarse ash, d «r from Bottom of the tank is peeled off; a water dispersion stream of fine ash and carbon particles with about 1.0 to 20% by weight of solids, with the withdrawn stream and an ordinary Foam float ion system is initiated, a stream of clarified water that is returned to the water quench tank. A two-stage water flow can be used to separate the water flows into a water-ash and a concentrated carbon particle Z water flow Flotation system can be used.

This concentrated carbon particle Z water stream contains about 10 to 40% by weight of solids and is placed in a collecting tank introduced from which a liquid for the preparation of the slurry or for the wet grinding of solid Fuels can be obtained. The processed, grated, solid fuels containing coal can be used in the mixed and collecting tank are introduced. For example, the solid fuel used in the mixing and collecting tank contains too

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about ~ 20 to 70% by weight of those recycled carbonaceous Solid fuel. A pumpable mixture of solid fuel and water that is 30 to 65% by weight solids is preferred contains, introduced as the first reactant stream into the gas generator.

The product gas stream from the water expulsion vessel or the product gas stream from the water quench tank can optionally be fed to an additional cleaning and purification stage in order to remove all remaining solid particles or at least one of the following components: H ₂ O, CO ₂ , CH ^, H ₃ S, COS, A and N ₂ .

The product gas stream can be used as heating gas or synthesis gas. Some typical compositions of the product gas stream in mol% are given in Table I at the end of the description. . ... .

Those included in the following embodiment of the invention Quantities of the various slurries and gas flows only characterize a certain operating state and are not intended to serve as limit values for the process parameters.

Through the line 1 of the burner 4 in Fig. 1, about 1248 kg of a slurry of ground, carbonaceous are per hour Solid fuel / carbon particles / water in the liquid phase at about 15.6 ° C through the outer ring line 2 into the Reaction zone of the synthesis gas generator 20 entered. Included occurs the slurry through the outer ring nozzle 3 (Fig. 2) of the double ring burner 4 at a speed of 24 m / sec into the reaction zone.

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Details of the double ring burner 4 are described in US Pat. No. 3,705,108. In Fig. 2 are some according to the invention Improvements presented, such as B. the concentric intermediate ring line 5 »which in a concentric !, converging Intermediate ring outlet nozzle 6 opens. Analogously, the central line 7 leads to a central nozzle 8. Is on the burner head a hollow, annular cooling chamber 9 attached, into the Cooling water is introduced through line 10. Cooling coils 11 are wound around the outer wall of the burner 4. On the Flange 13, the burner 4 is attached to the burner housing. The burner housing is via a flange inlet 15 with the vertical, flow obstruction-free, non-catalytic Synthesis gas generator 20 connected, which has a refractory reaction chamber 21 of 0.935 m content.

The slurry of carbonaceous solid fuel / carbon particles / water is pumped through line 1 and pump from the mixing and collection tank 24 via line 23. According to test number 1 in Table III, the slurry contains coal coke / Utah, which has been ground to a particle size corresponding to the passage of the standard sieve ASTM E11-70 (425 µm), and at least 80 % through a standard sieve of size ASTM E 11-70 ( 75 / um) can happen:. The proportions in% by weight in test no. 1 are: coal coke 49.0, carbon particles 1.0 (produced during the process) and water 50.0.

The material mixed in the tank 24 consists of ground material

. Lignite from line 25 and a concentrated dispersion of carbon particles and water with 10 weight -% of solid particles from line 26. The lignite from Utah has the following composition in wt .- & (Elemental analysis) C: 78.9, H: 7.5, N: 1.1, S: 1.1, 0: 7.2, ash: 4.2. The upper calorific value of coal is 8760 Kcal / kg.

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-13- 2536243

At the same time by line 30 a slurry of comminuted solid carbonaceous fuel / carbon particles / about 1873 kg flUssigem hydrocarbon fuel in liquid phase at a temperature of about 93 ⁰ C by the central pipe 7 into the burner 4 entered. This slurry enters the reaction zone of the gas generator 21 through the central nozzle 8 at a speed of 15 m / sec. Processed lignite is fed through line 32 in an amount of 937 kg / h to the grinding and grinding plant 31. To this end, 936 kg of a dispersion of 0.4 wt. An elemental analysis of the reduced crude oil gives the following values in% by weight: C: 85.8, H: 11.26, S: 1.98, 0: 0.11, N: 0.80, ash: 0.05. The heat of combustion is 1-0200 Kcal / kg.

At the same time, about 2460 kg / h of pure oxygen-containing gas (99.7 mol% O ₂ ) at about 37.8 ° C. enters the intermediate ring line 5 through line 40. From there it enters the reaction zone 21 through the converging intermediate ring nozzle 6 at about 105 m / sec. This causes a stream of essentially pure oxygen gas to be blown between the streams of oil and water slurry exiting the burner.

In the reaction zone, the three reactant streams collide with one another with such a force that the particles of lignite coke be pulverized. The slurry streams are atomized and completely mixed with the oxygen stream.

The reaction takes place in the reaction zone 21 of the synthesis gas generator 20 at a self-adjusting temperature of approximately 1427 ^° C. and a pressure of approximately 28 atm. The residence time is 2 seconds. 6450 N / m of synthesis gas leave the gas generator per hour

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The exhaust gas exits the outlet 41 via line 42 in the lower part Trial no. 1 into lines 47 and 43.

The first partial stream of exhaust gas from line 42 is introduced through conduit 43 into a waste heat boiler 44 and there cooled to a temperature of 332 ⁰ C by indirect heat exchange with cooling water which enters through line 45 at a temperature of 93 "3 ⁰ C in the heat exchanger and leaves the waste heat boiler at a temperature of 31O ⁰ C through line 46 as steam. The second substream of the exhaust gas is fed through line 47 into a quench tank 48 and cooled by direct quenching with water. (For a description of a quench tank, see US Pat. No. 2,896,927) “The product gas leaving the quench tank 48 is saturated with water. Optionally, this product gas withdrawn through line 49 can be introduced into a conventional gas cleaning and cleaning zone (not shown in the drawing), in which all remaining solid particles and subsequent gaseous impurities can be removed. COp, HpS, COS, A, CH ^, H ₂ O and N ₃ .

From the first substream leaving the waste heat boiler 44 through line 55, carbon particles can be removed by means of a ordinary nozzle scrubber 56 can be removed. As a washing liquid a mixture of the previously described reduced California crude oil is used, which is supplied through line 57 58 with admixture of a dispersion from line 59 in the Nozzle scrubber 56 enters. The dispersion consists of carbon particles and reduced California crude with a portion from about 0.4% by weight solid particles. It is drawn off from the bottom of the oil expulsion vessel 61 by a pump 60 and fed to nozzle washer 56 through lines 65, 66 and 59. A part of this dispersion is through line 33 into a grinding plant 31 for comminuting the solid, carbonaceous

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Fuel introduced. The process gas vash mixture leaves the nozzle washer 56 through line 62 and is introduced into the oil expulsion vessel 61, where the dispersion, which is liquid under normal conditions, is deposited and, as already described, is drawn off at the foot of the expulsion vessel. The clean process gas leaves the expulsion vessel 61 at the end of the plait through line 68 and is then fed to a nozzle washer 69 to remove the remaining carbon particles. Freshly prepared water enters the nozzle washer 69 as detergent through line 70. The process gas is then introduced into the expulsion vessel 75, from which pure product gas is withdrawn through line 76 at the head end. The composition of the product gas roughly corresponds to that in line 4-9 with the exception that the water content is less than 10 mol% and the proportion of carbon particles is less than 6 ppm (basis weight of the total carbon in the gas generator feed). Optionally, H 1 O and at least one of the following gaseous impurities can be removed from the product gas using a common gas cleaning zone: CO ₂ , H ₂ S, COS, A, and N ₂ . A water dispersion containing 0.1% by weight solids particles (essentially carbon particles and optionally some ash) is withdrawn through line 77 at the base of vessel 75.

The dispersion of water and solid particles in line is made by adding a dispersion of water and solid particles with 1.0 wt .-% solids (carbon particles and ash from the water quench tank 48) in the manifold 78 mixed. The mixture is poured into an ordinary wiper

80 entered. From there, purified water is supplied by pipe

81 by means of a pump 82 to the water quench tank 48 Line 83 returned. A water slurry of carbon particles and fine ash is withdrawn from the settler 80 and passed through line β4 to an ordinary foam

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flotation system 85 led. All of the coarse ash can be withdrawn from the settler 80 through line 86. the end the flotation plant 85 can the fine ash by means of a line 87 and the remaining water can be drawn off by means of line 88. Some of this water can after additional treatment can be removed from the system and is then available for other purposes. The other part of the water can in the quench tank 48 and / or the nozzle washer

to be introduced. A concentrated dispersion of carbon particles and water is added to the through line 26 , Mixing and holding tank 24- entered. About 111 kg / h of ash or other solid particles can be withdrawn from the system through lines 86 and 87.

In Table III are under test no. 1 the data of the method according to the invention and under experiment no. 2 and 3 Data from two comparative methods given. The comparison processes work according to the system of individual feed in Contrasted with the dual feed of slurry streams according to the invention. The process conditions and the product amounts of synthesis gas are in the three processes compared about the same. In experiment no. 2, the feed to the burner contains the following components: a Carbon / carbon particle emulsion on liquid hydrocarbon fuel and pumpable water slurry; a separate stream of free oxygen containing gas. In experiment no. J the burner feed contains the following components: a slurry of coal / carbon particles / pumpable water; a separate stream of free oxygen containing gas.

the

From Table III it is clear that / characteristic parameters of experiment no. 1 and thus of the method according to the invention are superior to the values of the comparison methods.

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- A significant economic saving is achieved and a permanent, continuous process guaranteed. This is particularly evident through the increase the production of Hp + CO per kilo of fuel added and the higher ratio of total solid fuel to liquid hydrocarbon fuel. The advantage of the method according to the invention still occurs by lowering the oxygen consumption per Nmr IL, + CO and by the reduced ratio of water to Fuel clearly visible.

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TABLE I.

Typical, solid carbonaceous fuels Raw anaylse in wt .-% (dry)

money Brown coal
coke Smoldering
money petroleum
coke carbon
particles fleeting
Duration
share 38.6 2.0 3.5 5.0 3-0 more solid
Coals
material 50.0 88.0 76.4 94.3 93 ash 11.4 10.0 20.1 0.7 4.0

Element arsenal in% by weight (dry)

C. 67.2 78.9 76.8 88.4 95.2 H 5.2 7.5 1.4 7.0 1.6 N 1.3 1.1 1.2 2.1 0.2 S. 3.8 1.1 3.1 1.5 0.6 0 11.1 7.2 0.1 0.4 ash 11.4 4.2 17 * -4 0.6 2.4

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TABLE II

Typical composition in mol % of a product gas stream

H ₂ 8.0 to 60.0

CO 8.0 to 70.0

CO ₂ 1.0 to 50.0

H ₂ O 2.0 to 50.0

CH ^ 0.0 to 50.0

COS 0.0 to 0.7

H ₂ S 0.0 to 1.0

N ₂ 0.0 to 85.0

Δ 0.0 to 2.0

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TABLE III

FEED

Carbon-carbon-particle-oil-slurry in kg / h Carbon-carbon-particle-water-slurry in kg / h Carbon-carbon-particle-oil and water emulsion in kg / h free oxygen-containing gas (99.7 mol% O ₂ ), NmVh

Generat or at> ga s (from line 42) in% by volume Vers.No. 1 version no. 2 version no. 5

CD O CO

hydrogen

Carbon monoxide

Carbon dioxide

water

methane

Carbon disulfide

Hydrogen sulfide

nitrogen

argon

"• ^ performance data; oxygen consumption in

Nm ^ H «+ CO (net)

Water / fuel ratio in kg / kg total solid fuel / liquid hydrocarbon fuel

in kg / kg

H ₂ + CO in NmVh

^ H ₂ + CO / kg fuel

H ₂ + CO / kg solid fuel unconverted carbon in% by weight

1875 _—— _ — _ 1245 5000 5560 —_ 1720 1720 1760 55-49
55.08
5.40
9.25
0.09
0.02
0.26
0.55
0.08 50.88
47.05
5.86
15.50
0.08
0.01
0.22
0.52
0.08 24.64
52.59
10.55
51.87
0.06
0.01
0.19
0.49
0.06 506 525 575 0.25 0.45 1.00 1.67 5.5 ___ 5600 5510 4670 2.25 2.15 1.87 κ) 5.59 2.99 1.87 J2 4.0 4.0 4.0 CD
K)

CO

Claims (6)

Claims 1) Process for the continuous production of heating gas and synthesis gas from solid, carbonaceous fuels by partial oxidation of fuel with free oxygen-containing gas in the presence of a temperature moderator in the Reaction zone of a non-catalytic gas generator free of packing and flow obstacles, the product gas essentially H «and CO and optionally at least contains one of the following substances: COp, HpO, CH ^, Np, A, COS and H ^ S, marked that a first slurry containing a solid, grinded, carbonaceous fuel and a liquid hydrocarbonaceous fuel at a rate in the range of about 0.3 to 150 m / sec continuously entered into the reaction zone will, a second separate slurry containing a solid, grated hydrocarbon fuel and water, at a speed in the range of about 0.3 to 150 m / sec continuously and simultaneously with the first Slurry is added to the reaction zone, a third separate stream of free oxygen containing gas continuous between the first and second Slurry is fed into the reaction zone simultaneously, the three streams are brought into contact and mixed together to form an atomized dispersion in which the atomic ratio 609815/0827 from oxygen to carbon of all fuel about 0.6 to 1.6, the weight ratio of HpO too Fuel about 0.10 to 1.3 and the weight ratio from solid, carbonaceous fuel to liquid, hydrocarbonaceous fuel about 0.8 to 12 amounts to and the atomized dispersion at a temperature of about 816 ° to 1910 ⁰ C and a:
react in the reaction zone. about 816 ° to 1910 ⁰ C and a pressure of about 1-250 atm 2) The method according to claim 1, characterized in that the first slurry contains QpO bisC (65 parts by weight of a solid, ground, carbonaceous fuel, which consists of one or more of the following substances: Petroleum coke, coal, carbon particles, black coal, coking coal, oil shale, tar sands and pitch, wherein the parts by weight are based on the first slurry are for every part by weight of liquid hydrocarbon fuel made from one or more of the following Substances consists of: Heating oil j residual oil, reduced crude oil, natural Crude oil, oil coal, oil shale, gasoline, kerosene, naphtha, gas oil fractions from petroleum distillates, benzene, toluene, Hexane, heptane, cyclohexane, tetralin, decalin, and the second slurry! ^) up to 65 parts by weight solid, carbonaceous fuel for every weight 809815/0827 - Contains 23 parts of water. 3) Method according to claim 1 or 2, characterized in that the exhaust gas flow from the Reaction zone is divided into a first and second process gas stream, the first process gas flow through indirect heat exchange is cooled with water to produce steam in a waste heat boiler, at the same time the second process gas stream is cooled and washed to remove the entrained solid constituents to be removed by introducing it into water in a quench tank, the waste gas stream from the waste heat boiler is washed with scrubbing oil to remove entrained solids and to provide a product gas stream which essentially contains H ₂ , CO and less than 10 mol% H ₂ O and the waste gas stream is withdrawn from the quench tank for Provision of a water-saturated product gas stream which essentially contains H ₂ and CO. 4-) Method according to claim 3, characterized that the reaction time of the finely divided dispersion in the reaction zone is 1 to 10 seconds, the exhaust gas flow from the waste heat boiler with a liquid hydrocarbon fuel or a dispersion Carbon particles and liquid hydrocarbon fuel is washed to remove the entrained solid particles to remove, a dispersion of carbon particles and liquid Hydrocarbon fuel is separated, $ 09815/0827 - 2A - part of the dispersion of carbon particles and liquid hydrocarbon fuel for manufacture the first slurry for the gas generator is mixed with processed solid carbonaceous fuel will, a first product gas stream is separated, which in contains essential Hp, CO and at least one of the following substances: CO ₂ , H ₂ O, CH ^, F ₂ , A, COS and H ₅ S, at least one of the substances CO ₂ , H ₂ O, CH ₄ , N ₂ , A, COS and H ₃ S is separated from the first product gas stream in a gas cleaning zone, _{a second product gas stream, which is saturated with H 2} O and essentially free of entrained solid particles, is withdrawn from the quench zone in accordance with the first product gas stream, a dispersion of solid particles and water withdrawn from the quench zone and separated from a "concentrated dispersion of carbon particles and water will and the solid, grinded, carbonaceous fuel with the concentrated dispersion of carbon particles and mixing water to make the second gas generator slurry. 5) Method according to claim 4, characterized in that the first before the gas cleaning zone Product gas stream is washed with water to remove the entrained to completely remove solid components, 609815/0827 a first clean product gas stream in line (76) and a dispersion of entrained plague and water are separated in line (77) and the dispersion from line (77) is mixed with the pest particle water dispersion from the quench zone, line (79) to provide a first slurry for the gas generator in line (78). 6) Method according to claim 5 »characterized that the mixed dispersion from line (78) is fed into a settling zone, pure water is withdrawn from the settling zone and returned to the quench zone, as well as coarse ash and in Water-dispersed carbon particles with fine ash are withdrawn from the settling zone in separate streams, and the water dispersion of carbon particles and fine ash enters a froth flotation zone of which three separate streams are withdrawn containing water, ash and concentrated dispersion of carbon particles and Contain water. 609 815/0827 Blank page