DD202733A5 - METHOD AND DEVICE FOR PREPARING SYNTHESEGAS - Google Patents

Abstract

In the process for the production of synthesis gas (CO + H tiief 2) by autothermal gasification of finely divided carbon-rich materials with O deep 2 thest coal dust with a particle size v.0 to 0.01 mm together with d.Sauerstoff and possibly an additional gas in a 2000 Gasification zone held to 2600 degrees C, leading the formed fly ash crude synthesis gas with its inherent thermal energy by a reduction zone filled with the starting materials for an endothermic carbothermic reduction and, increased by the synthesis gas resulting from the carbothermic reduction, by an adjoining thereto The preheating zone filled with the same substances is drawn off at a temperature of from 300 to 1500 ° C. for purification and conversion and removes below the reduction zone the reaction product of the carbothermic reduction and molten slag formed from a collection and post-reaction zone. The invention also relates to a device for carrying out the method.

Description

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Process for the production of synthesis gas Field of application of the invention

The invention relates to a process for the production of synthesis gas and to an apparatus for carrying out the process.

Characteristic of the known technical solutions

The autothermal gasification of carbon-rich materials, especially of coke and coal, with technically pure oxygen or mixtures of oxygen and additional gases, preferably water vapor, nitrogen or carbon dioxide, is known gasification is carried out in a suitable reactor space, which may have different embodiments, so that the gasification can proceed in the manner of Z, B, entrained flow gasification or fixed bed gasification at normal pressure or elevated pressure. Previously used aggregates for carbon-rich material should predominantly favorably influence the physical properties of the slag »

Thus, DE-PS 1 068 415 describes a method for producing synthesis or fuel gas by gasification of solid fuels with oxygen at temperatures of 1200 to 1375 ⁰ C, wherein in order to reduce the slag melting temperature, a flux, for. As lime, can be added. In the process of DE-AS 1 508 083 for the production of reducing gases for the production of iron by gasification of

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solid carbonaceous fuels with air in a fluidized bed at 1000 to 1500 ⁰ G is added to the fuels limestone, lime or silicic acid and alumina-containing materials in such an amount that they increase the ash melting point above the working temperature · DE-AS 2 520 584 describes the gasification sulfur-containing coal in an iron bath reactor, with lime, limestone or dolomite being added to the iron bath to produce a desulphurising slag. The DE-PS 930 539 and 1012420 describe a method for generating gas is introduced in which water vapor at 775 to 980 ⁰ G in a mixture of carbonaceous solid fuel and calcium oxide or lime, the present in the reaction zone quantity of calcium oxide or lime is enough to convert almost all the carbon dioxide into carbonate.

According to the process of US Pat. No. 3,017,259 coke and lime are dispersed in water vapor and reacted with oxygen in a fluidized bed reactor at 1,650 to 2,750 ⁰ G to form calcium carbide and synthesis gas (GO + H ₂ ). The reaction products are reacted with a hydrocarbon oil cooled below 425 ⁰ G, wherein a suspension of calcium carbide is separated from the synthesis gas.

As is generally known, the fossil solid carbon carriers, such as hard coal, lignite or coke, are often provided with very different levels of dietary fiber. The dietary fiber consists mainly of a large number of minerals, which, for T in intimate mixing

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With the carbon present and form as ash residue in ashes · In the ash more than 35 elements can be detected, which is why interest in obtaining raw materials from the ashes has always existed · To date, however, no corresponding method has prevailed. This is mainly due to the usually very low content of ashes in valuable, steel-refining metals, which were previously in the foreground of interest. · Although fly ash and granulated ashes are exploitable in the building materials industry, the amounts of slag and ash already produced in power plants only make up about 75 % of hard coal and about 8% of brown coal can be fed, big problems. These become even more oppressive when large-scale coal gasification plants are put into operation in the future, because on the one hand the high level of enrichment of heavy metals and radionuclides excludes certain applications of ash or slags, which were previously proposed, on the other hand, the capacity is exhausted in the recovery and the Ash and impact output by the coal gasification is still increased.

In the known coal gasification plants prevail at the site of ash and slag formation in general very high temperatures, At the same time, the ash or slag is melted in the rule before. The minerals in coal, mainly ilite and kaolinite as l'onminerale, sericite as mica mineral, pyrite, marcasite, limonite, kaitite and iron phosphate as ure minerals, brown feldspar, anchoringite, calcite

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and dolomite as Garbonspäte, apatite as phosphorus mineral and quartz, in addition to a number of other, but more rarely found oxides, hydroxides and sulfides and certain salts, show different behavior depending on the rate of heating and atmosphere. Generally adsorbed water on heating, then water of crystallization, water is expelled from OH groups and carbon dioxide from carbonates · At temperatures above 1500 ⁰ G takes place a significant transport of many oxides over the gas phase to form gas complexes, monoxides or sulfides instead, after the reverse reaction lead to aerosol formation »This is especially true of silica, alumina and iron oxide. In addition, the minerals decompose at high heating rates largely in amorphous oxides, which are entrained by the syngas stream, a large part of the silica melts and later forms a glassy phase. Under strongly reducing conditions, above all in the presence of carbon, reduction of metal oxides on metals can also be observed. Preference is given to the occurrence of iron, but also the formation of calcium carbide, which is also formed intermediately via a metallic step, or the occurrence of ferrosilicon.

Object of the invention

The aim of the invention is to provide an improved process for the production of synthesis gas in which technically utilizable products are simultaneously obtained from the additives and slag constituents.

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Presentation of the essence of the invention

The invention has for its object to change the production technology and to use selected additives.

According to the invention, selected additives are used which bind at least some constituents of the ash or slag resulting from the minerals in the coal by chemical reaction, whereby chemically technically utilizable products, so-called recyclables, are obtained in a secondary reaction. The aggregates are preheated to the required temperature by the hot synthesis gas, and the energy demand of endothermic secondary reactions is completely covered by part of the energy released during autothermal gasification. The secondary product is melted off the reactor space.

In the method according to the invention, the known properties of the mineral constituents of the carbon-rich materials, in particular of the coal, are advantageously combined and utilized.

This will be or become

1. large amounts of slag and ash are chemically converted and converted into chemical-technical products,

2. individual components, eg. B. AIpOo, enriched in a dust fraction, this good hydraulic binder-

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lend properties,

3 · the gasification heat generated at a particularly high temperature level is directly utilized for high-temperature reactions,

4. the carbon dioxide content of the syngas minimized and

5. large 'portion of the otherwise exiting the reactor flue dust retained in the reactor and also converted by chemical reaction.

This is achieved in that the hot synthesis gas is passed directly after its formation directly into a bed of a mixture of aggregates · The aggregate mixture contains a reducing agent, in particular carbon in the form of coke-coke, anthracite, charcoal or peat coke, for slag reduction For the most part, the z, T, liquid slag particles are deposited on the surface of the packed bed and form a surface film thereon. Here occurs now due to the high temperatures reaction, and it forms a reduction zone. Consumption of the additive mixture forms the desired secondary product. This can be, for example, ferro silicon or calcium carbide. The design of the specific quantities of additive, based on the amount of carbon-rich material used, can be varied within wide limits. Reasonably, the amount of key component to be reacted in the ash is above the stoichiometry of the conversion.

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the lower limit of the quantities of aggregates (see Example 1), while the amount of heat released during the autothermal gasification reaction represents the upper limit of the quantities of aggregates over the energy consumption of the conversion reaction (cf., Example 2),

In particular, the invention now relates to a process for the production of synthesis gas (GO + H ₂ ) by autothermal gasification of finely divided carbon-rich materials with oxygen, optionally in the presence of additional gases, which is characterized in that coal dust with a particle size of 0 to 0 , 1 mm together with the oxygen and possibly an additional gas in a held at 2000 to 2600 ⁰ C gasification zone einsetzt that the formed fly ash containing crude synthesis gas with the inherent thermal energy through a filled with the starting materials for an endothermic carbothermic reduction H-reduction zone and, increased by the resulting in the carbothermal reduction synthesis gas passed through an adjoining, filled with the same substances preheating zone and at a temperature of 300 to 1500 ⁰ C for purification and conversion, and that below the reduction zone, the reaction product of carbothermis reduction as well as molten slag arising from a collection and post-reaction zone.

The process of the invention may further be preferred and optionally characterized in that

a) the ash content of the pulverized coal injected and that used for the carbothermic reduction

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Coal is at least partially used as a reactant in the carbothermic reduction;

b) removing the raw synthesis gas leaving the preheating zone from dust and ash and re-injecting these solids into the reduction zone at least partially in the circulation along with fresh coal dust via the gasification zone;

c) the starting materials for the carbothermic reduction in a particle size of 10 to 20 mm or from 20 to

40 mm inserts;

d) the reduction zone is laterally in open communication with at least 2 gasification zones and upwardly with the preheating zone;

e) the preheating zone and reduction zone with coke, iron scrap and optionally quartz charged, whereby is obtained as a reaction product of carbotherinischen reduction at 1300-1800 ⁰ C Perrosilicium;

f) charging the preheating zone and the reduction zone with coke or calcined anthracite and lime to obtain calcium carbide as the reaction product of the carbothermic reduction at 1800 ^° C. to 2300 ^° C.

g) charging the preheating zone and the reduction zone with coke, calcium phosphate and quartz to obtain elemental phosphorus as the reaction product of the carbothermic reduction at 1300 to 1700 ⁰ G;

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h) charging the preheating zone and the reduction zone with coke and oxidic iron ore, obtaining as the reaction product of the carbothermic reduction at 1300 to 1800 ⁰ G metallic iron;

i) one uses as additional gas GO, GOp, i «» steam or recycled synthesis gas;

(j) working in the gasification zone with a stoichiometric excess of oxygen in relation to the oxidation to GO;

k) one metered in a component of the starting materials for the carbothermic ^ reduction targeted along the inner wall of the preheating zone and the reduction zone.

The invention further relates to a device for carrying out the method according to the invention »

In the attached drawing show:

S ¹ Ig. 1: a schematic representation of a plant for carrying out the method according to the invention;

3, 2: a schematic representation of a further embodiment of a system for carrying out the method according to the invention,

The device according to the invention comprises a shaft furnace 6,

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consisting of an elongated preheat 6c from top to bottom, a reduction chamber 6fa and a post-reaction chamber 6d, which openly merge; at least two opposite, laterally adjacent to the reduction chamber 6b and openly connected to it, cylindrical gasification chambers 6a, in each of which a nozzle of a Staubvergasungsbrenners 3 for the joint supply of coal dust, oxygen and any additional gases is admitted; a feed 8 for the starting materials of the carbothermic reduction and a discharge line 9; 12 for raw synthesis gas at the head of the shaft furnace 6; at least one discharge line 7a, 7b at the downstream reaction chamber 6d for withdrawing molten slag and molten reaction product from the carbothermal reduction

The device of the invention may further be preferred and optionally characterized by

a) one each nozzle 3 upstream intermediate bunker 2 for coal dust; a dedusting device 11 in the discharge line 9; 12 for raw Syntesegas and return lines 13 for the deposited mineral dust from the Sntstaubseinrichtung 11 to the individual intermediate bunker 2;

b) in the upper part of the shaft furnace 6 vertically and circularly arranged separating plates 16 for delimiting an annular space 6e between the separating plates 16 and the inner wall of the shaft furnace 6 and by at least 2 transports 15 for the supply of a component

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the starting materials for the carbothermic ^ reduction through the annular space 6e with the formation of an annular bulkhead jacket protecting the inner wall of the shaft furnace 6 (cf. FIG. 2).

The method according to the invention can be realized in various ways. With reference to FIGS. 1 and 2 of the drawings, the method and apparatus of the invention are explained in more detail, wherein the carbon-rich material intended for gasification (coal dust) is referred to below as gasification coal becomes.

FIG. 1

Finely ground and pre-dried gasification coal (particle diameter 90 % </ Um) is given via the leads "1 and the intermediate bunker 2 to a respective dust gasification burner 3, where it is oxygenated from line 4 and possibly additional gas, in particular carbon dioxide, water vapor, carbon monoxide or Rohsynthesegas , is injected from "line 5 into the gasification chamber 6a of the reactor space according to the invention (shaft furnace) 6 and gasified autothermally. In the sense of the invention, oxygen and / or additional gas can be used as carrier gas for the gasification coal. The reactor chamber in the shaft furnace 6 is designed according to the invention so that directly adjacent to the gasification chamber 6a to the axis of an S-eduction chamber 6b adjacent, consisting of a debris layer of the respective aggregate mixture. .Dabei the grain size of the aggregates of this mixture is preferably 10 to 20 mm or 20 to 40 mm. Above the bulk layer

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a preheating chamber 6c is arranged, which likewise contains a saturated layer of aggregate mixture, so that the aggregate mixture migrates downward as a result of gravitational influence in accordance with the consumption in the reduction chamber 6b. Below the reduction chamber 6b, a collection and post-reaction chamber 6d is arranged, into which drips molten slag dripping from the reduction chamber 6b and reduction product. The saccarous and post-reaction chamber 6d is provided with at least one closable kink opening so that molten slag and molten reduction product can be withdrawn via lines 7a and / or 7b. Then it is granulated or cooled in vessels.

While in the gasification chamber 6a, the temperature is adjusted by means of the additional gas to about 2000 to 2600 ⁰ G, resulting in the reduction chamber 6b, a temperature of 1300 to 2300 ⁰ C. The aggregate mixture contains a reducing agent, preferably coke, carbon, anthracite, charcoal or Torfkoks, and specific for the desired reaction further materials. Volatile constituents are permitted in the reducing agents only to the extent that their oxygenating reaction products (eg hydrocarbons, tar) do not interfere with the further processing of the synthesis gas obtained. Optionally, such reducing agents may be previously calcined. The gasification products formed in the gasification chamber 6q are forcibly passed through the reduction chamber 6b and the preheating chamber 6c, where they release the inherent heat to the aggregate mixture and even at the top.

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Part of the reaction chamber with temperatures between about 350 and 1500 ⁰ G emerge. Depending on. Requirement for the amount of reduction product produced and / or the desired outlet temperature of the raw gas can be metered according to quantity and composition. Minimum raw synthesis gas temperatures are obtained if the preheating chamber is designed such that the surface of the debris available for heat exchange becomes very large and the energy consumption by reduction reactions corresponds to the release of energy by the autothermal gasification reaction. At the top of the reaction chamber, a suitable device for introducing the supplied over 8 aggregate mixture is provided, preferably in the form of chutes, which are sealed against gas, or Gichtverschlüssen. In line 9, a waste heat boiler 10 may be provided at high outlet temperatures of Rohsynthesegases so that the raw synthesis gas in the hot dedusting 11 dedusted and can be derived via line 12. The dust withdrawn from the hot dedusting 11 can either be returned via the lines 13 and intermediate bunker 2 back into the gasification chamber 6a and the reduction chamber 6b ^ or removed via the line 14 or in certain proportions simultaneously via line 13nd line 14. In this way, you can either remove all residual ash and fiber from the use of materials as slag via the lines 7a and 7b or parts thereof as dust from the Entstaübungseinrichtung 11 via line.

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FIG. 2

In a further embodiment of the method according to the invention may be provided in contrast to 3 · ig · 1, separately introduce a component of the aggregate mixture via line 15 of the remaining aggregate mixture in the reactor space and with auxiliary installations, such as dividing plates 16, a column or cylinder jacket-like distribution of To achieve components in the bed

The gasification zone can be charged with excess oxygen, resulting in higher gas temperatures. In addition, the outer Schüttungsmantel takes in the annular space 6e a protective function for the inner wall of the reactor space.

embodiment

The invention is explained in more detail below by some examples. · In the following examples, the volume data relate to the ITormal state at 273 ⁰ K and 1,013 bar ·

example 1

Synthesis gas is needed to produce around 52.5 t / h of methanol. For this purpose, about 121,000 m-fyh of CO + H ₂ must be produced, which corresponds to the inventive transformation of the silicon dioxide of the asus to perrosilicon 45 % Si by autothermal gasification of pre-dried, very finely ground (0 = 90 % 90 90 '/ um), unwashed raw Peinkohle

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with the addition of pre-dried blast furnace coke crushing 4 (0 10 to 20 mm) and iron scrap (95 % Fe) should happen ·

For this purpose, according to Fig. 1 via line 1 about 60 t / h Feinkohlenataub (0 90% ^ 90 / um) promoted in the bunker 2 and from there in dust gasification burners 3 together with about 39.290 m Vh 99.9 $ iger oxygen from line 4, via the line 8, the shaft furnace 6 has been provided with a bed of a mixture (0 = 10 to 20 mm) of coke (for the reduction of SiO 2) and crushed iron scrap, of which about 4.17 t (2.08 t / h coke and 2.09 t / h scrap iron) are consumed. While synthesis gas is formed in the gasification chamber 6a with the addition of about 5000 nrvh of carbon dioxide on line 5 as additional gas at temperatures of about 2000 to 2300 ⁰ G, slag reduction occurs in the reduction chamber 6b. Both SiO ₂ and Fe ₂ O., reduced and formed at about I6OO ⁰ G ferrosilicon. This falls molten and drips through the bed in the collection and Hachreaktionskammer 6d, from where every hour about 4.2 t of ferrosilicon 45 % Si via line 7a or line 7b are withdrawn · The synthesis gas is then passed through the bed of aggregate mixture and this heats up in the preheating 6c to about 1500 ⁰ G · Here, a portion of the generated fly ash is retained by .The bed and fed back to the reduction chamber 6b. The synthesis gas escapes via line 9, the waste heat boiler 10 and the hot dedusting 11. Via line

-3

12, around 122,100 nrVh of pre-dedusted raw synthesis gas (around 121,000 nrh CO + H ₂ ) with the composition:

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about 76 to 7u Vol.-SS GO, about 22 vol .-% H ₂ and about 1 to 2 V0I .- / 6 Ip, deducted GO ₂ . The dust separated off in the dedusting device 11 is partially returned via line 13. The dust component removed via line 14 contains about 57% by weight of Al ₂ O, in addition to mainly GaO and MgO. About the Rückstaubmenge also the amount of mitzuggezogenen from the post-reaction chamber 6d via line 7a and 7b slag can be influenced. This causes a total of around 4.2 t / h of dust and slag.

In a conventional entrained flow gasification, the accumulation of dust and slag would be around 7.9 t / h. The slag and ash output can thus be reduced by the method according to the invention by about 42% compared to the prior art. At the same time, by increasing the Al ₂ O content in the plug dust fraction (line 14), a hydraulic product which can be used as a binder is produced, as well as perosilicon 45 % Si as the desired, valuable reduction product.

Example 2

Ferrosilicon generation is a high-temperature process that has hitherto been carried out in electrothermal furnaces. The process according to the invention can also be extended by adding quartzite to the aggregate mixture and thus increasing the amount of ferrosilicon. In this way, the vast majority of gasification heat can be recovered in the form of chemically bound energy.

A gas generator, the process according to the invention Rohaynthesegas for the operation of a 1000 tpd methanol plant

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produces about 95 800 m ^ CO + EL · · · According to Fig. 1 via the line 1 and the bunker 2 46.73 t / h unwashed, pre-dried and finely ground (0 = 90 % ^ 90 / Um) raw Fine coal passed to the dust gasification burners 3 and gasified with about 32 560 no oxygen, 99.9%, but without additional gas, at 2200 ⁰ G to 2600 ⁰ O autothermal. Via line 8 is the shaft furnace 6 with the aggregate mixture (0 = 10 to 20 mm), consisting of about 5.15 t / h blast furnace coke crushed 4 (pre-dried), about 7.41 t / h of crushed quartzite (95%) and about 0.67 t / h - egg scrap (lumpy, about 95 % Fe) beschick.worden.

In the reduction chamber 6b conditions prevail as in Example 1. There are about 5 »98 t / h ferrosilicon 75 % Si formed, the melt flows into the collection and post-reaction chamber 6d and is withdrawn from there via line 7a and 7b. The synthesis gas and the liberated by reduction of CO flow in the preheating 6c through the bed of aggregate mixture and cool there to about 350 to 450 ⁰ C. Thereafter, via line 9 »dedusting 11 and line 12, about 97,050 m 3 / h of pre-dedusted raw synthesis gas (about 95,800 nr / h C / + H ₉ ) with the composition: about 77% VOC-5 & CO, about 21% by volume H ₂ and around 2 vol. Hp, CO2 deducted. The flue dust, in which AIpO 2 is again enriched as in Example 1, can be returned to the dust gasification burners 3 via line 13 and intermediate bunker 2 in variable proportions or taken off via line. "Together, 3.49 t / h dust and slag.

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These are only about 52 % of the normal dust and slag output compared to conventional entrainment gasification. In addition, according to the invention, about 5.89 t / h of ferrosilicon 75 % of Si are still produced as the desired valuable reduction product.

Example 3

Apart from ferrosilicon, the calcium carbide otherwise produced in electrothermal furnaces can also be obtained in a coal gasification process according to the invention as a reduction product.

The gasification coal used is American fiber coal, which in its raw state contains about 11.5% by weight of ash and 2.8% by weight of water. The combustible portion of this fiber carbon contains 85.55 wt .-% G, 5-23 wt% H, 6.24 wt % 0, 1.52 wt% N, 1.46 wt% S The ash content of the ash is quite high at about 50% by weight. The reducing agent used is calcined anthracite.

If, analogous to the above examples 106.91 t / h pre-dried, fo at 90 of less than 90 / f order once ground coal dust and gassed him at 2200-2600 ⁰ C with about 70 720 W? / H oxygen 99.9 $ ig, Thus, in the reduction chamber (6b of the process according to the invention from the aggregate mixture consisting of about 48.55 t / h quick lime 96% and about 36.06 t / h calcined anthracite at about 2000 ⁰ G around 60 t / h 80th % calcium

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melting carbide, wherein about 10.82 t / h of dust are withdrawn via line 14. At the same time about 231 * 000 m ^J / h arise vorentstaubtes raw synthesis gas leaving the shaft furnace with approximately 400 ⁰ G and about 73-74 VoI · -% CO, 24-25 VoI · -% H ₂ and about 1 to 3 percent by volume % N ₂ , GO ₂ contains "The high content of basic additives in the mixture is particularly advantageous, so that the raw synthesis gas is virtually free of sulfur.

Claims (12)

2 5 5 O 7 - ²⁰ - ² · ² · ¹⁹⁸³ AP C 10 J / 242 550/7 61 170/18 Erfindungsansprach 1. A process for the production of synthesis gas (C0 + H ₂ ) by autothermal gasification of finely divided carbon-rich materials with oxygen, optionally in the presence of additional gases, characterized in that coal dust with a particle size of 0 to 0.1 mm together with the oxygen and ggf an additional gas injected into a maintained at 2000 to 2Ö00 ⁰ G gasification zone, that one formed the fly ash-containing crude synthesis gas with the inherent thermal energy by a with the starting materials for an endothermic carbothermic reduction ^ reduction reduction zone and, increased by that in the carbothermal reduction resulting synthesis gas, passing through an adjoining, filled with the same substances preheating zone and at a temperature of 300 to 1500 ⁰ G for cleaning and converting, and that is below the reduction zone, the reaction product of the carbothermic reduction and slag formed molten a collection and Lachreaktionszone takes. 2 · Process according to item 1, characterized in that the ash fraction of the pulverized coal and the coal used for the carbothermic reduction are used at least partly as a reaction partner in the carbothermal reduction, 3. The method according to item 1 or 2, characterized in that the leaving the preheating raw synthesis gas 247550 7 ~ ²¹ ~ 2.2.1983 £. £. .J »W # - APG 10 J / 242 550/7 61 170/18 free of dust and ash and these pests at least partially in circulation together with fresh
Coal dust again over the gasification zone in the
Reduction zone " 4. The method according to any one of items 1 to 3 », characterized in that one uses the starting materials for the carbothermic ^ reduction in a particle size of 10 to 20 mm or from 20 to 40 mm. 5. The method according to any one of items 1 to 4j, characterized in that the reduction zone laterally with at least 2 gasification zones and up to with the Vorheizaone
is in an open connection. 6. The method according to any one of items 1 to 5 », characterized in that the preheating zone and the reduction zone with coke, scrap iron and possibly quartz fed, wherein
one wins as the reaction product of carbothermic reduction at 1300 to 1800 ⁰ C ferrosilicon. 7. The method according to any one of the items 1 to 5 »characterized by charging the preheating zone and the reduction zone with coke or calcined anthracite and lime, wherein the reaction product of the carbothermic
Reduction at 1800 to 2300 ⁰ G Calcium carbide gains. 8. The method according to any one of items 1 to 5 », characterized in that the preheating zone and the reduction zone 255 0 7 - ²² - 2.2.1983 AP G 10 J / 242 55O / ¹ } 61 170/18 Charged with coke, calcium phosphate and quartz, which is obtained as a reaction product of carbothermic reduction at 1300 to 1700 ⁰ C elemental phosphorus. 9. The method according to any one of items 1 to 5 », characterized in that the preheating zone and the reduction zone is charged with coke and oxidic iron ore, wherein one obtains as the reaction product of the carbothermic reduction at 1300 to 1800 ⁰ C metallic iron. 1Oo process according to one of the items 1 to 9, characterized in that one uses as additional gas GO, GO ₂ , N ₂ , steam or recycled synthesis gas. 11. A process according to any one of items 1 to 10, characterized in that a stoichiometric acid excess in the gasification zone is used in relation to the oxidation to CO. 12. The method according to any one of items 1 to 11, characterized in that one metered a component of the starting materials for the carbothermic reduction targeted along the inner wall of the preheating zone and the reduction zone. 13. Apparatus for carrying out the method according to any one of items 1 to 12, characterized by a shaft furnace (6) from top to bottom of an elongated preheat chamber (6c), a reduction chamber (6b) and a Nachreaktioriskammer (6d), the open 2425.50 7 - ²³ ~ ² · ² · ¹⁹⁸³ AP G 10 J / 242 550/7 61 170/18 merge into one another; at least two opposite cylindrical gasification chambers (6a) adjoining the reduction chamber (6b) and openly connected to the reduction chamber (6b), into each of which a nozzle (3) for the common supply of pulverized coal, acid and possibly additional gases is introduced; (8) for the carbothermal reduction feedstock and a raw synthesis gas discharge line (9; 12) at the top of the shaft furnace (6); at least one discharge line (7a; 7b) at the itch reaction chamber (6d) for withdrawing molten slag and molten reaction product from the oecarbothermal reduction » 14. Device according to point 13> characterized by a respective each nozzle (3) upstream intermediate bunker (2) for pulverized coal; a dedusting device (11) in the discharge line (9; 12) for raw synthesis gas and return lines (13) for the separated mineral dust from the dust extraction device (11) to the individual intermediate bins (2), 15. The device according to item 13 or 14, characterized by in the upper part of the shaft furnace (6) vertically and circularly arranged separating plates (16) for delimiting an annular space (6 e) between the separating plates (16) and the inner wall of the shaft furnace (6) and by at least 2 transport lines (15) for the supply of a component of the starting materials for the carbothermic reduction through the annular space (6e) to form a the inner wall of the shaft furnace (6) protective annular bulkhead. To this 1 page Zelchnunaen