DE1545461A1 - Process for the production of mainly carbon monoxide and / or hydrogen containing gases from solid fuels - Google Patents

Description

METALLGESELLSCHAFT Frankfurt (Main), May 10, 1966

Corporation. DrWer / GM

Patent Department
Prov * No. 4870

Process for the production of predominantly carbon monoxide and resp. or hydrogen-containing gases from solid fuels

The invention relates to a method for producing heating gases, fuel gases, Synthesis gases or reducing gases for metallurgical processes from solid fuels.

The extraction of such gases, ζ. B, of town gas, coal gas and the like. Can is known to take place by coking, also called degassing, or by gasifying coals.

In the coking of coals, the coke forms the largest share. the Distillation products are tar and tar oil, gas water and gas.

When gasifying coals with oxygen and / or air and water vapor The main product is a gas consisting mainly of carbon monoxide and hydrogen. Tar and water are by-products. the Ashes are rubbish. Compared to coking or smoldering, a relatively large volume of a gas of low calorific value is created which contains tar formed by gasification in great dilution. This complicates the purification of the gas. If the gasification is carried out under pressure, the gas also contains increasing amounts of methane with increasing pressure. 909885/1339

Tar-free gases can be produced by gasifying coke. These gases are only to be cleaned of gaseous impurities. The extraction and utilization of the by-products is not eliminated, but only moved back to coke production.

While the liquid and gaseous fuels, mineral oil and versor ₇ supply gases, easily and cheaply transported by pipeline and can be spread in interconnected networks to consumers, the coal must still be transported on ships and trucks for consumers. In order to create a starting position for solid fuels, which is comparable to that of liquid and gaseous fuels, the extraction and utilization of by-products, in particular tar and gas-water, which today are often negative cost factors, must be largely restricted or completely eliminated. In addition, it is desirable to direct the gas generation in such a way that the cleaning of the gas generated is only based on a few simple gas components, for example on HS; CO and NH needs to extend.

The inventive method for generating combustible gases from solid Fuels is based on the task in coking or gasification

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of coal, one consisting predominantly of carbon monoxide and hydrogen Generate gas and the formation of by-products and waste products on water, Hydrogen sulfide and carbon dioxide sulfide, and to be limited to carbon dioxide.

If the gas produced is to be converted into a very hydrogen-rich gas, e.g. for ammonia synthesis, by converting the carbon monoxide it contains with water vapor to hydrogen and carbon dioxide, then it is generally desirable to keep the methane content of the raw gas as low as possible. This also applies to the synthesis gas for methanol synthesis, if in the CO: H _O ratio is not divided by partial CO conversion but by recycle of CO ₂ in the gasification.

In the process according to the invention, the coking or the Gasification of the coal formed and volatilized tar materials, as far as possible left as vapors in the gas and catalytically split into carbon monoxide, hydrogen and carbon dioxide. Dust and high-boiling tar components, which condense out of the raw gas in the course of the process are in the gassing returned. Tar constituents soluble in gas water, these are essentially phenols, tar acids, fatty acids and bases in the enrichment of the raw gas with water vapor for the catalytic Splitting by injection evaporation back into the process.

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The inventive treatment of tar-containing gases is applicable to the Raw gases from coal degassing, i.e. on raw coke oven gas or carbonization gas and on the raw gas from coal gasification at normal or increased pressure Oxygen and water vapor. Depending on the nitrogen content permitted in the product gas, the technical oxygen can be completely or partially replaced by air be replaced.

It is known to increase the calorific value of pressurized gasification gas by that the tar materials contained in the raw gas are thermally split. For this purpose, the raw gas is passed to the pressure carburetor after it has passed through it A partial flow branched off immediately following the washing cooler, through The addition of oxygen and / or air is partially burned and heated as a result.

In this partial flow, condensed hydrocarbons are formed from the main flow injected and split into lower gaseous hydrocarbons. (DBP 969 851}

It is also known that the carbon monoside contained in the pressurized gasification gas by conversion with water vapor into carbon dioxide and To convert hydrogen, with the Waeserdampfüberschuss contained in the raw gas from the gasification is largely implemented *

$ 909 885 / $ 133

The raw gas is directly connected to the pressure carburetor in the »» the washing cooler by sprinkling with the precipitated in the subsequent cooling Self-condensate only cooled to the extent that high-boiling Teeranteii Ie and pitch precipitate and entrain the dust contained in the raw gas. The raw gas containing water vapor and tar oils is then increased to about 350 to 400 C heated and over a sulfur-resistant conversion catalyst, which has a hydrating effect at the same time. In addition to the conversion of the carbon monoxide, a hydrogenation of unsat is carried out on this catalyst saturated hydrocarbons and organic, sulfur, oxygen or Nitrogen-containing compound »with formation of hydrogen sulfide, Water and ammonia. During the cooling process, the converted gas turns into hydrogenating refined liquid hydrocarbons and water deposited. Then carbon dioxide and hydrogen sulfide are washed out of the gas. (DBP 1 094 395)

It has been proposed to increase the calorific value before or in place the conversion of carbon monoxide is a catalytic splitting of those in the gas Contained vaporous hydrocarbons and possibly also of additionally vpn externally supplied hydrocarbons, z. B, from light gasoline with steam at 450 to 650 ° C over sulfur-resistant catalysts make lower gaseous hydrocarbons.

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In all of these pressurized gasification processes, it is Usually, the thick tears separated in the washer cooler for further decomposition into the carburetor. Even with the degassing process the return of high-boiling tar components to the coking itself is known, e.g. in the briquetting of fine coals for the subsequent process Smoldering, whereby the briquette binding agent is obtained from the smoldering tar, or in the case of the return of heavy tar oil into the ceiling channel of Horizontal chamber furnace to improve the benzene output.

After all, it is known that fine coals and / or heavy oils are not essential Gas formation of by-products. However, this must be very high temperatures of 1200 to 1500 C applied and high specific Oxygen quantities are used. In this gasification of coal can mostly the ashes cannot be completely burned out while at the Gasification of heavy oil ali-3in or together with fine coal the often unavoidable formation of less reactive soot is the process management complicates gas cleaning.

The subject of the invention is., A method for the production of gases consisting predominantly of carbon monoxide and / or hydrogen from solid fuels by degassing or gasifying with water vapor and oxygen.

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The method according to the invention is characterized in that the * the tar gas coming from the degassing or gasification indirect or Cooled directly to temperatures above 180 C and freed from dust and condensing substances, then enriched with water vapor 400 brs 550 heated and after addition of oxygen at temperatures above 700 C on a dissociation catalyst on a high-temperature-resistant carrier material is split, and that from the exchange of heat with that to be split Raw gas cooled cracked gas in a known manner carbon dioxide, sulfur compounds and ammonia are washed out.

In addition to oxygen, the raw gas to be split can also contain carbon dioxide be added. The hot raw gas can be used during cooling to separate dust and thicker and / or during the subsequent heating vaporizable hydrocarbons are added before the catalytic cleavage.

In the process according to the invention, the hot, still tar-containing raw gas is used initially cooled and, if necessary, washed with water to separate pitch and coal dust, high-boiling ones. Tar constituents for condensation to bring, and, if necessary, to increase the water vapor content of the gas. The water introduced here is used as the cooling down of the

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^"8 ~ 1545481

Product gas accumulating condensate removed. This water can be supplemented or partially by foreign vaporizable hydrocarbons be replaced.

The gas freed from dust and thickener is then released by indirect Heat exchange with the hot product gas to 400 to 550 C, where the water vapor content is obtained by injection evaporation of im Procedure accruing gas water is further increased. By this measure, the water-soluble tar components and ammonia in the Process returned. At this point, too, can evaporate hydrocarbons of another origin can also be introduced into the gas.

Then it will dampen in hydrocarbons and rich in water vapor Gas after adding oxygen and / or air at 700 - 1100 ° C, preferably at 850 to 10000 C. on a high temperature-resistant cracking catalyst converts, with an almost exclusively carbon monoxide and hydrogen as well as water vapor and carbon dioxide Gas is produced. The methane content of this gas is low and can almost completely disappear by adjusting the reaction temperature on the catalyst to be brought. In the case of mild temperature conditions on the catalyst, this corresponds to a gas outlet temperature below Around 850 C, small amounts of aromatics, e.g. benzene, can appear in the gas.

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Then the ammonia contained in the gas is not completely oxidized and accordingly appears in the aqueous condensate of the final cooling. From this condensate, the ammonia can be driven off with low-pressure steam and to be focused on. If this concentrate is fed back into the raw gas before the cleavage, then this is done during the coking or coking. The ammonia formed in the solution of the coal is converted into nitrogen. Of impurities only hydrogen sulphide, carbon monoxide sulphide and carbon dioxide are to be removed from this gas. The only liquid end product is water, that is pure enough to be discharged directly into a receiving water.

If a gas that is particularly rich in carbon monoxide is to be produced, then t

some of the carbon dioxide leached from the end gas can be removed from the Catalytic Sapltung be returned to the gas stream. If the end gas is to be rich in hydrogen, the catalytic cleavage can be used a known carbon monoxide conversion with water vapor connect to sulfur-resistant catalysts.

For separating dust, pitch and thicker in the first process ens step are one embodiment each for pressureless and under hot raw gas produced under increased pressure.

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If the hot raw gas under increased pressure of, for example, 15-30 atm is available, then it is washed in the first stage with a circulated water excess, and thereby to about 18O - 200 C cooled. At this temperature the waves condense Tar constituents, especially pitch, from and separate from the wash water. They are made with a water content that is approximately between 0.05 and

0.3 kg / Nm raw gas is branched off from the scrubber circuit and separated from the water by delamination. This dust tar fraction is returned to the gasification shaft. The water will taken back into the scrubber circuit or injected into the heated gas in the second stage.

If the hot gas is unpressurized, for example from the high temperature

r ο

Peraturvgkokung, then it is first cooled to about 350 to 400, for example by injecting water. This cooling is expediently carried out in a radiation boiler with smooth heat exchange surfaces. This cooling creates dust, pitch and. heavy tar parts separated from the gas. After that, the pre-cleaned gas brought to the pressure suitable for the subsequent stages by means of a hot blower.

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The reheating of the cooled for the separation of dust and thicker Raw gas is expediently carried out in two exchanges ™ through which hotter cracked gas flows and one connected between them Satiator. Here the raw gas is heated further, further enriched with water vapor and heated again before it is filled with oxygen mixed and passed over the Sja !! catalyst, into the Saturators of this stage are introduced all the amounts of water that Contain water-soluble tar and gas components, so that they are completely fed to the cleavage and disappear as by-products to be brought.

In the catalyst bed of the cleavage reactor, the steam-rich, oxygen-containing raw _{gas is split at temperatures between TOO and 1100 C to form a gas consisting predominantly of CO and H 4} , which also contains CO and steam. The catalysts suitable for splitting the liquid and gaseous hydrocarbons at temperatures above 700 ° C. contain metals of the 6 and / or 8 group of the periodic table or the oxides or sulfides on a high temperature resistant carrier material.

Suitable carrier materials are preferably high-temperature resistant Oxides of aluminum and / or magnesium.

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BATH

In the cleavage reactor, two catalyst layers can have different levels of activity Components to be arranged.

In principle, all catalysts are suitable, which at temperatures above

ο *

700 C a substantial breakdown of the ammonia to nitrogen and water and as complete as possible from hydrocarbons to carbon monoxide and Cause hydrogen.

Special catalysts are, for example, magnesium oxide or aluminum oxide with 3 to 30% nickel or 10% cobalt or 10% Ni and 10% tungsten, on aluminum oxide and magnesium oxide, in each case on the total weight of the catalyst based. The catalysts can be sulphurized in a known manner.

The gas then immediately flows out of the cleavage reactor in one Waste heat boiler for high pressure steam generation and is here on 550 bis 600 chilled. The further cooling of the cracked gas then takes place in the two heat exchangers of the saturation stage, which are connected upstream of the cracked catalytic converter is. Here the cracked gas is cooled to around 260 to 300 ° C.

A system for converting the carbon monoxide contained in the cracked gas with water vapor to carbon dioxide can be used in this cooling process

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and hydrogen, if a particularly hydrogen-rich one Gas is to be generated.

The gas, which is now around 260 to 300 ° C, is e.g. in a waste heat boiler for low-pressure steam generation and other conventional coolers brought to the temperature required for gas cleaning.

The gas cleaning itself only requires a simple system for washing out the acidic gas components CO ₀ and HS.

In this way, the method according to the invention achieves the object solved the "by-product recovery in degassing and gasification of coal, which is associated with a number of waste problems, turn off completely. In the degassing of coals, especially in coke, gas and water remain as end products, while in the gasification of coal only the solid residue remains Ash remains.

Using two flow diagrams and the associated exemplary embodiments the invention is further explained.

Example 1 with Fig. 1 relates to production free of byproducts of a gas by gasifying coal with water vapor and oxygen under increased pressure. '

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from

Example 2 with Fig. 2 concerns the completely pressureless splitting Raw coke oven gas including all organic by-products and ammonia it contains.

The system according to Fig. 1 essentially consists of the pressure gasifier 1, the washing cooler 2 directly adjoining it with associated waste heat recovery 3, the heat exchangers 4 and 5 with the interposed saturator 6, dm cracking furnace 7, the high pressure waste heat boiler 8 and gas cleaning 9.

In the embodiment shown, there is a system for conversion of the carbon monoxide contained in the cracked gas with water vapor to hydrogen and carbon dioxide with the reactors 10 and 11 are provided.

A tar separator for separating the thick tar from the liquid circulated through the washing cooler 2 is designated by 12. 13 and 14 denote an ammonia expeller with the associated condenser.

In the compressed gas generator 1, 730kg / h of coal are gasified, which is 11.2% Moisture, 11.6% Asehe, 13.1% tar (according to Fischer) 4, 8% S, Contains 1.2% N and has an upper calorific value Ho = 5640 kcal / kg. The coal is fed to the gasifier from the lock bunker 15.

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3
140 Nm / h of 90% oxygen and 668 kg / h of high-pressure steam serve as gasification agents. The oxygen is supplied in line 16 from an air separation plant (not shown). The high-pressure steam is taken from the steam samn, ler 1 7 of the high-pressure waste heat boiler 8 and fed into the gasifier 1 through line 18.

3 leads. In the carburetor, 1000 Nm / h of raw gas are produced with a Pressure of 32 ata and a temperature of about 300 C through the connection piece 19 enter the washer cooler 2. This raw gas has the following gas composition and impurities:

Raw gas analysis: 27.3% ^CO 2 19% ^H 2 ^S Q.5% CnIIm ia2% CO 3 ^ 9% ^H 2 ία 9% CH ₄ Q.5% ^C 2 ^H 6 0.2% ^C 3 ^R 8 1.6% ^N 2 3098 Kcal / Nm ³ H
O

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Gas constituents:

Terr oil 49.0 g / Nm petrol 14.5 g / Nm Phenols 4.8 g / Nm Fatty acids 0.65 g / Nm ammonia 8.00 g / Nm HCN 0.15 g / Nm ³

3
Water vapor content ©, 469 kg / Nm

3
Organ. SO, 63 g / Nm of which about 30% COS 10% CS-

25% mercaptan 35% thipphen

This gas is cooled in the washing cooler 2 by direct sprinkling with water and at the same time saturated with steam, the entrained Dust and the heavy tar fractions precipitated and in the swamp 20 of the washer cooler are collected.

200 kg / lh of water are continuously transferred from the washing cycle the dusty tar carried away together. In order to compensate for the water balance, 197 kg / h of water then have to pass through line 27 be returned to the washing cooler 2 by means of pump 28 in the circuit. Most of them are separated from the tar separator 12.

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Water ^ and on the other part from the condensate of the ammonia abortion 13, 14 taken. The remainder of 50 kg / h of water is used for injection used in the saturator 6 of the following stage, the tar dust mixture, consisting of 3 kg / h tar and 1 kg / h dust is from the tar separator 12 is fed back through the line 29 by means of the pump 30 in a known manner to the gasifier and mixed with the coal.

By interposing the waste heat boiler 3 on the head wash cooler 2, in which 85 kg / h Ni. ederdruckdampf are generated, the Outlet temperature of the gas to 183 C and to the corresponding water

3
vapor content of. Precisely adjusted to 0.466 kgfNm.

The washed raw gas Mdrd is introduced into the next treatment stage in line 31, heated to 302 ° C. in heat exchanger 4 and out in line 32 in'den saturator 6. In this the 50 kg / h aqueous condensate, the through line 33 by means of pump 34 the Tar separator 12 are removed, evaporated into the hot raw gas, so that at a temperature of 268 C necessary for the cleavage

3 required amount of water vapor 0.516 kg / Nm is contained in the gas. In the line 35 the gas reaches the heat exchanger 5 and is further heated to 400 ° therein. The heating of the raw gas in the heat exchangers 4 and 5 takes place in the heat exchange with the split and possibly converted gas, theÄ from the high pressure waste heat

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boiler 8 in lines 36, 37, 38, 40 through the conversion reactors 10, 11 and the heat exchangers 4 and δ for the gas purification system 9 flows.

The gas passes through the line 41 into the cleavage stage. Here it becomes

3
Superheated raw gas with 162 Nm / h, 90% oxygen, from line 42, mixed and passed over the cracking catalyst in reactor 7, all higher hydrocarbons and almost all impurities and the larger part of the Mette, ns being converted to CO and H. The pressure

2t

in the cleavage reactor is 30 ata and the temperature 900 C. The sensible Heat of this gas from 900 - 400 down is used in the waste heat boiler 8 flanged to the reactor 7, in which 877 kg / h High pressure steam can be generated. A part of this steam is the gasifier 1 in the line 18 for pressure gasification of the solid fuel fed. The remainder of 209 kg / h is available for other purposes, for example for gas cleaning and dejg.eichen.

3 The cracked gas in an amount of 1 283 Nm / h has behind the Ahitzekessel 8 in line 36 the following composition and impurities:

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₂ 24.27%

H ₂ S. 1.49%

CO 25.97%

H ₂ 42.29%

CH ₄ 3.51%

N ₂ Ar 2.47% H ₀ · 2.5OC lcg / Nm- ³ H ₂ O = 0.453 kg / Nm ³

In addition to HS and CO "as well as HO and impurities still present:

i ί C.

₃ 1.0 g / Nm ³

COS 0.2 g / Nm ³

The cracked gas is passed in line 36 at 400 ° C. into the first conversion stage 10, from which it slides at 480 ° C. in line 37 to heat exchanger 5, where it is cooled down to 38 ° C. will. It then becomes the 2nd conversion reactor in line 38 10 and further converted therein, the gas outlet stemperEtur

will 400 ° C reached ^ and the CO content sinks to 5.4%. This gas is in the Line 39 led to the heat exchanger 4 and cooled in this so far that it is at 290 ° C and 29 ata for further heat recovery

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Available. It is used in line 40 for further cooling, for desulphurisation and washing out of the CO and possibly further Cooling and drying of the cleaned gas is passed into the system called gas cleaning. From the line 43 is a mixture of CO and H removed.

The converted gas in an amount of 1583 Nm / h has the following composition and quality [in line 40):

^CO 2 36.79 ^H 2 ^S 1.24 CO 5.37 H ₂ 51.56 CH.
4th 2.95 N ₂ - ^ Ar 2.09 H
O 2093 kcal / Nm ... 3

Water vapor content 0.277 kcal / Nm " There are still some impurities;

NH- = 0.83g * im

COS »0.15 g / Nm

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For use as a town gas component, it is sufficient to remove the H ₀ S from the gas and partially remove CO ₀ . While the organic sulfur can remain in the gas. The ammonia is absorbed in the condensate when the gas cools down. This a.mmoniakhaltige condensate is from the gas cleaning system 9 in the line 44 to. Abteibkolonne 13 out, in which the ammonia is removed by a distillation process, so that finally 390kg / h of pure, soft water without impurities leaves the system through line 45.

When driving the NBL out of the water with 22 kg / h of low-pressure steam 47 kg / h of NH concentrate are produced, which pass through line 46 to the condenser 14 and be knocked down in it. The condensate is fed through the line 47 to the tar separator 12, in this with others Mixed condensates and the washing cooler 2 through the line 46 by means of the pump 47 and / or the saturator 6 through the line 33 by means the pump .34 supplied.

The example described can be modified in that in the Washer cooler with the condensate to be returned OeI e of foreign origin be introduced or that in the water injection into the Saturator 6 also vaporizable hydrocarbons are added, which are then also split in the reactor 7. This can reduce the yield of gas increase.

909885/1339 " ²² "

If a mixture of hydrogen and carbon monoxide is to be produced, the conversion reactors 10, 11 can be omitted. The heat supply to the heat exchangers 4 and 5 then takes place one after the other the hot cracked gas, the lines 36, 37 on the one hand and 38, 39 on the other hand being directly connected with a corresponding shortening. The outlet temperature from the waste heat boiler is then expediently set to about 500 ° C.

The system shown in Fig. 2 is used for by-product-free extraction a gas consisting predominantly of hydrogen and carbon monoxide from the volatile products of high-temperature coking of hard coal in the so-called smelter coking plant.

The system connects to the manifold 101 of the ceiling ducts Battery of Horizonattkammeröfen 102 on. The plant consists essentially from the radiation boiler 103, the heat exchangers 104 and 105 with the interposed saturator 106, the cleavage reactor 107 with the directly adjoining waste heat boiler 108 and from a plant 109 for cooling and cleaning the cracked gas.

The approx. 700 ° C. hot raw gas flowing out of the ceiling ducts of the coke oven chambers passes through the collecting pipe 101 into the radiation boiler 103 and is cooled here to around 400 ° C. Here the divorces

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Dust off. As should be indicated with the line 111, it is added again to the coking coal to be used.

The dedusted gas is extracted from the radiation boiler by means of a hot gas blower 112 passed in line 113 to heat exchanger 104 and in this in indirect heat exchange with the hot cracked gas heated to over 400 ° C. from the waste heat boiler 108. At this temperature, the gas in line 114 reaches the saturator 106 in which it is achieved by injecting water from line 115 with steam is enriched. This gas then becomes in the line 116. heated to over 609 C for heat exchange with the hot cracked gas from the waste heat boiler. Through the line 117 the gas is then in introduced the cleavage reactor 107 and in this on a catalyst layer 118 reacted with oxygen «supplied through line 119, whereby a gap temperature of over 900 C is established. From the cracking reactor 107 gd-angt the cracked gas for pre-cooling in the immediate subsequent waste heat boiler 108 and is made from the em in the lines 120, 121 through the one behind the other with respect to the heat-absorbing medium switched heat exchangers 104 and 105 and in the line 22 to Cooling and cleaning system 109 passed. The clean gas flows out of this at about ambient temperature for further use through line 123.

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The in the steam collector 124 of the radiation boiler 103 and in the steam collector 125 of the waste heat boiler 108 ess-eugte steam is in the line 126 combined and superheated by a steam superheater 127 in heat exchange with the cracked gas in line 122 and through the line given for recycling.

When cooling and cleaning the gas in the system B9 is involved Water containing ammonia. This is conducted in line 129 to an ammonia stripper 130, and in this with steam blown out. Pure soft water is repelled through line 131 and is then available as boiler feed water.

The distillate from the stripper 130 becomes an ammonia water in the cooler 132 condensed; which in line 115 by means of the pump 133 is passed to saturator 106.

The following numerical example under? judge:

3 The coke chamber battery 102 produces 1000 Nm of raw material per hour Coke oven gas introduced into the plant. The raw gas has the following gas composition and contains the following! Impurities :.

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^CO 2 ^H 2 ^S CH

η m

° 2 CO-

^H 2
CH,

2.5

0.5

2.2

0.4

6.0

58.0

26.0

^N 2
Ho

HO content

4.4%

4745 kcal / Nm '3

0.362 kg / Nm with the following ingredients:

3
Tar + oil including naphthalene 100g / Nm raw gas

Benzene 25 ¹ l "

Phenols approx. 1 ""

NH _Q ..... 7.5 ""

HCN ..! ... 2.0 ""

organic sulfur compounds .. 0.4 ""

The organic sulfur compounds consist of about;

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50% CS_

5 % COS

20% mercaptans

25% Tiophene

After exiting the coke canister 102, this gas is at approx. 700 ° C average Temperature in the radiation boiler 103 cooled to about 400 ° C and freed from dust =, 443 kg of steam with 45 atmospheres are generated (Line 126). The dust, mixed with friscta charcoal, returned to the coking chamber.

The raw gas at 400 C is initially in the heat exchanger 104

ο
warmed up to 537 C. In the saturator 106, 23 kg of water are then evaporated into the hot gas, where it cools down to 507 ° C. In the heat exchanger 105 it then continues to rise to 650.degree

3 heated. Then it becomes 95% strength in the cleavage reactor 107 with 245 Nm Oxygen mixed and passed over the cracking catalyst. In the When the gap temperature of 950 C is reached, all hydrocarbons are removed and impurities largely converted and the sulfur compounds converted into HS and a small proportion of COS. After utilizing the sensible heat of the cracked gas in the waste

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heat boiler 108, in which another 374 kg of steam with 45 atmospheres are generated, it reaches the 2nd heat exchanger 105 at 730 C and at 613 C in the 1st heat exchanger 104. At 500 ° C., it arrives in a line to the steam superheater 127, in which there is a total of 817 kg of high-pressure steam

Overheated to 400 ° e. With 402 ° C and a water vapor content of

3
0.1595 kg / Nm is the cracked gas for heat recovery, cooling and possibly further cleaning in the system 109, as far as it is necessary for the purpose of the gas.

The analysis of the gas is »

^CO 2 4.94 * 0.25 % CO 25.06% ^H 2 66.75 % CH ₄ 0.15% ^N 2 2.85% Ho » 2820 kcal / Nm ³

Impurities:

NH ₃ 0.3 g / Nm ³

COS 0.15 g / Nm ³

3 The amount of cracked gas is 1986 Nm

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" ^2β "

When the gas is cooled, about 300 kg of NH2 -containing water are produced.

In the stripper 130 23 kg of NH are concentrated therefrom by distillation generated, which are used for the injection in the on saturator 106. The remaining amount of water leaves the system in pure form »

The high-pressure steam generated and superheated to 400 C can be used for propulsion of machines serve. About half of it is enough for the energy requirement the oxygen system (air turbo compressor), which supplies the oxygen for the split supplies. The rest can be used elsewhere.

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Claims

909885/1339

Claims (5)

Claims 1.1 Process for the production of predominantly carbon monoxide and / or hydrogen-containing gases from solid fuels by degassing or gasifying with water vapor and oxygen, characterized in that the tar-containing gas coming from the degassing or gasification is cooled indirectly or directly to temperatures above 180 C. and freed from dust and condensing substances, then heated to 400 to 550 C under enrichment with water vapor and after the addition of oxygen at temperatures above 700 C it is split on a ceramic high-temperature-resistant carrier material, and that from the exchange of goods with the raw gas to be split cooled cracked gas in a known manner carbon dioxide, sulfur compounds and ammonia are washed out. 2. The method according to claim 1, characterized in that the to In addition to the oxygen, carbon dioxide is also added to the splitting raw gas. 3. Process according to claims 1 and 2, characterized in that the fortified ammonia water that occurs during the final gas cleaning is used to enrich the raw gas with water vapor. - 30 - 909885/1359 ! ο Α 5 4 6 1 4. The method according to claims 1 to 3 _#, characterized in that the hot raw gas during the cooling for the separation of dust and thicker or during the subsequent heating before the catalytic cleavage, evaporable hydrocarbons are added, 5. Process according to claims 1 to 4, characterized in that that the fission catalysts metals of the 6 and / or the 8 group of the periodic table in elementary oxidic or sulfidic form on a carrier substance made of oxides of aluminum and / or magnesium. 909885/1339 ORlGfMAL INSPECTED 3 / Blank page