AT521321A1 - Bottom cycle and top cycle process for the production of weak gases from residues and residual gases for the production of dimethyl ether - Google Patents

Abstract

The method according to the invention comprises the combination of a gasification system (40) with double flaps (38, 39) and a carbon dioxide purge (75), a supply of oxygen via a PSA (16) with a control valve (17), and the supply of carbon dioxide (18) from one Tank (19) via a pump (20), with a control valve (21), an evaporator (21), a superheater (26) and a control valve (29) for the entry, a steam generator (9), comprising a water tank (2) , a pump (3), a control valve (4), an evaporator (9,5,6,7,8,9) with drum (11), and regulator (30). The raw gas (41) is made available to a gas cleaning device (49) and the compressor (51) via a cyclone (42). The coal is returned via the screw (45) and discharged with the screw (47) and fed to the second gasification stage. The second gasification stage (64) comprises superheated carbon dioxide (33) and water vapor (34) in a nozzle base (60), the entry of the residues (54) via the double flap (55, 56) and entry screw (57), the cleaning of the synthetic gas (65) via a cyclone (67), gas cleaning (68) and recycling via a compressor (72). The ash is discharged via a discharge screw (62). The invention comprises an external combustion chamber (83} for the combustion of residual gases (78) to carbon dioxide and water vapor for the nozzle base (60) and the introduction of external residual gases (112) via a compressor (85), a control valve (86) and a superheater (88 ) in the nozzle bottom (90) of the reactor (64).

Description

Summary

The method according to the invention comprises the combination of a gasification system (40) with double flaps (38, 39) and a carbon dioxide purge (75), a supply of ^}

Oxygen via a PSA (16) with control valve (17), the supply of carbon dioxide (18) from a tank (19) via a pump (20), with control valve (21), an evaporator (21), a superheater (26) and a control valve (29) for the entry, a '

Steam generator (9), comprising a water tank (2), a pump (3), a channel ⁽ 7 ⁾ ; ^e L ^{nem evaporator (9} ' ⁵ · ⁶ ' ⁷ ' ⁸ · ⁹ ) with ^drum (11), and regulator (30). The raw gas (41) is made available to a gas cleaning device (49) and the compressor (51) via a cyclone (42). The coal is returned via the screw (45) and discharged with the screw (47) and fed to the second gasification stage. The second gasification stage (64) comprises superheated carbon dioxide (33) and water vapor (34) in a nozzle floor (60), the entry of residues (54) via the double flap (55, 56) and entry screw (57), the cleaning of the synthetic gas (65) via a cyclone (67) gas cleaning (68) and recycling via a compressor (72). The ash is a 7UR ^S \ / ^a9 h ^auger θ d ^discharged · ^The invention includes an external combustion chamber (83) for combustion of residual gases (78) external to carbon dioxide and water vapor for the Dusenboden (60) and the introduction of residual gases (112) Via a compressor (85), a control valve (86), a superheater (88) into the nozzle bottom (90) of the reactor (64) '/ 32

Bottom cycle and top cycle processes for the production of lean gases

Residues and gases for the production of dimethyl ether

The method according to the invention comprises the combination of a fixed bed gasification plant (VGA) (40) with double flaps (38, 39) and a carbon dioxide purge (75), a supply of oxygen via a pressure swing adsorption (PSA) (16) with control valve (17), the supply of Carbon dioxide (18) from a tank (19) via a pump (20), with a control valve (21), an evaporator (21), a superheater (26) and a control valve (29) for entry into the oxidation zone of the reactor (40), Comprising a steam generator (9), with a water tank (2), a pump (3), a control valve (4), an evaporator (9,5,6,7,8,9) with a drum (11), and a regulator (30). The raw gas (41) is made available to a gas cleaning device (49) and the compressor (51) via a cyclone (42). The coal (44) is returned via the screw (45) and discharged from the reactor (40) with the screw (47) and fed to the second gasification stage (SGA) (64). The second gasification stage (64) comprises superheated carbon dioxide (33) and water vapor (34) introduced via a nozzle base (60), the entry of residues (54) via the double flap (55, 56) and entry screw (57), the cleaning of the synthetic Gases (65) via a cyclone (67), gas cleaning (68) and the suction and compression via a compressor (72). The ash is discharged via a discharge screw (62). The invention comprises an external combustion chamber (83) for the combustion of residual gases (78) and the lean gas (52) generated in the first gasification stage (VGA) (40) to form carbon dioxide and water vapor, which flows through the nozzle base (60) into the second gasification stage ( SGA) (64) and the introduction of external hydrocarbon-containing residual gases (112) via a compressor (85), a control valve (86), a superheater (88) into the nozzle bottom (90) of the reactor (64). _t

The invention includes the conversion of the high-quality lean gas to dimethyl ether and the use of the off-gas (110) from the dimethyl ether process (106) in the combustion chamber (83) to generate carbon dioxide and water vapor and usable waste heat from the exhaust gas for the gasification process (SGA) ( 64).

Residues arise in various production processes, in agriculture, in trade, in the construction industry, forestry and in manufacturing processes. Residues also arise when products from use are transferred to waste. In the course of recycling, groups of substances are created, such as metals, plastics, glass, paper, wood and wood materials, substances, ... around the solid components. The burning of residues is known, leads to heat generation and, with an efficiency of ~ 22%, to electricity. However, electricity and heat from residues are to be rated as subordinate forms of energy, since there is little added value.

Treatment of the substances is always associated with the residues. As a rule, the substances do not appear as pure, immediately usable and usable substances. Treatment means collecting, the separation using mechanical physical processes so that substances can be obtained, although the shape can be different. A treatment has now been used to obtain material flows that can be used in various processes .2 / 32. We are now concentrating on those material flows of the solid phase that are provided with a high oxidizable fraction. An example is given here:

Waste wood, paper, foils and cardboard, wood and plastics, forest residues, digestate fibers from

Biogas plants.

grade C 0 H N H2O ugh % % % % % kJ / kg old wood 45 36.37 5.63 0,376 20 18.9 + Cardboard sheets 27.5 20.6 3.7 0.83 23.2 11.2 Forest residues 43 35.1 6.20 0,251 40.0 15.9 Peel 42.2 33.2 5.12 1.38 10.0 16.8 cores 44.1 43.1 5.84 1.50 13.5 16.8 plastics 74.0 8.7 14.1 0.15 1.0 41.0 RDF 32.2 25.3 4.3 0.37 21.2 - 13.2

Table 1: Exemplary elementary composition of residues

In addition to solid residues (Table 1), gaseous residues also arise in many processes. Gaseous residues are biogenic gases from biogas plants, landfill gases, fermentation gases, coking gas, blast furnace gas, converter gas, residual gases from the extraction of oils and gases, shale gases. The residual gases always have a different composition and thus in the form of a different density and calorific value. Some of these residual gases are listed as examples in the table below:

grade CO H2 CH4 CO2 H2O CxHy N2 H2S ugh % % % % % % % 0 kJ / m ³ Biogas______ 0 0 50 50 1 0 0 0 5.0 biogas 0 0 40 50 1 0 0 10____ 4.0 Flaregas 0 5 30 20 1 14 30 0 6.5 Shalegas 0 10 60 13 2 15 0 0 8.1 coke oven gas 30 35 20 10 2 3 0 0 3.8

Table 2: Exemplary composition of residual gases

Sludge and liquid residues will not be considered and treated in the following, since the gasification and pyrolysis processes are not directly accessible. However, sludges and organic residues with a high proportion of water have the property that they decompose under anaerobic conditions and either form fermentation gases or biogas. These residual gases (Table 2) can be reformed with great efficiency in the second gasification stage to synthetic gas with this invention.

The process of gasification is known. Gasification is the conversion of substances into a lean gas with a low calorific value and the carbon in the form of coal that can be obtained from the substances through gasification. The heat necessary for the gasification is either generated in the gasification process with the help of the substrate itself, by burning a small part of the substrate and the heat generated is used for the gasification process. A special case is pyrolysis, a process in which the heat is supplied allothermally, i.e. from the outside. The substrate is brought to a temperature of 400 ° C to 1000 ° C, where the carbonization and gasification process can then take place. But pyrolysis has not proven itself in everyday practice.

The task according to the invention is now to utilize the different solid and gaseous residues in a gasification plant, so that the effort and / 32 the energy input is low, a separation into inferior and high-quality material flows is possible through the utilization process, through two combined processes the utilization of the inferior ones solid substances at high temperatures to the substances carbon, ash and lean gas is enabled and a conversion of the high-quality heterogeneous substances and residual gases to high-quality low-energy lean gases is made possible, and thus the yield and utilization of residual gases, residual substances to the higher-quality liquid substance dimethyl ether is made possible. ("Waste to liquid"). The principle of "zero emission" should also be used.

The process described in patent EP 2 291 492 B1 combines the process of partial low-temperature pyrolysis in the form of a rotary tubular furnace and a slight generation of hydrogen from the coal-ash mixture. The pyrolysis gas from the sub-stoichiometrically operated rotary kiln leads to a pyrene gas which is burned with air. With the waste heat from the combustion of the pyrolysis gas, water vapor is generated and the coal ash mixture is reduced to carbon dioxide and hydrogen (water gas reaction). The disadvantage of this invention is the pyrolysis, because it takes place only partially, and it is not a Zeo emission plant like the present invention, it is only a question of utilizing the carbon so that it does not completely arise as waste.

The process shown in patent WO 2016/169661 A1 represents a combination of fixed bed gasification of hard coal, the fine fractions of hard coal being used with the waste heat from the gasification process in a pyrolysis process to pyrolysis oil and tar. The disadvantage is the use of pyrolysis oil and tar, which cannot be used instead of petroleum and which are also highly toxic and also do not allow zero emissions.

The method described in the patent US 201810023 003 A1 describes a combination of gasification and hydrothermal liquefaction of biomass, to a synthetic gas and a bio oil. The disadvantage of this process is the production of bio oil, which cannot be regarded as a substitute for biodiesel or petroleum. The combustion of this tar oil enriched with tar leads to highly toxic residues and high technical expenditure.

The method according to the invention shown here takes advantage of the different properties of the residues (37, 54) and the residual gases (112, 78). In order to be able to use residual materials easily and efficiently, they are processed. The preparation includes sorting, shredding, drying to a water content <10%. Either the lumpiness is so large that the residues prepared in this way can be fed directly to the gasification process, or they are comminuted to such an extent that they are now chips that can be pressed. Pressing means pellets with a diameter of d ~ 25mm and a length L ~ 50mm and a density of p ~ 650 kg / m ³ . These pellets are also known as industrial pellets. These coarse pellets can be used in a classic gasification reactor (40) in a cocurrent or countercurrent process. The pellets have the advantage of high density (p ~ 650 kg / m ³ ) and due to the coarse bulk, the porosity of the bed is very large, so that the gas can be sucked out between the pellets with low suction pressures. The porosity, also gas permeability, is of particular importance for the function of the reactor (40) / 32

Importance. Since the residence time of the substrate in the reactor is often very short, the

Water content of the pellets should be of the order of 10%.

The process of gasification is known, however it is pointed out that the advantage of this process is the generation of heat so that the carbonization process and outgassing process can take place in the reactor itself from the substrate. The gasification process differs from the pyrolysis process. In pyrolysis, the heat is generated externally and thus fed to the reactor in different phases. One example is the well-known “Lurgi process” for quick degassing of hard coal. In this process, sand is used as a heat transfer medium. The major disadvantage is the mixture of sand and coal that you get at the end of the process. The separation of the coal-sand mixture is a considerable effort and represents a considerable disadvantage in small systems. Another option is ceramic balls, such as those used in the "BioLique process". The balls make it easier to separate the coal-ball mixture, because you can use the sieving process to separate the balls from the coal. However, this separation can only take place if the coal ball mixture is processed into different pieces using a grinding process.

Another disadvantage is the fact that neither sand nor balls can cause the temperatures in the pyrolysis process to exceed 500 ° C. As soon as you have moving mechanical components such as a rotating screw or a rotary kiln, you are limited to the heat resistance of the metallic, inserted and moving components. Even ceramic and metal composites are not a viable solution that can withstand tough operation and wear.

On the one hand, the gasification process results in an ash mixture in coal, whereby ash consists of inert components such as carbonates, nitrates and oxides of metals. The proportion of coal and ash is between 10% and 40% by mass of ash, the rest is carbon in the form of coal particles.

grade C 0 N H metals K / A H2O ugh % % % % % kJ / kg coal 83.1 7.9 0.4 8.0 0 100% 1 33.0 ash K2CO3 Na2CO3 SiO2 MeO2 100% 1 0 Coal / ash 74.79 7.11 0.36 7.2 90% 10% 1 28.7 Coal / ash 49.86 4.74 0.24 4.8 60% 40% 1 19.8

Table 3: Exemplary composition of residual coal and ash

Another disadvantage of the simple gasification processes, which are often used instead of biomass boilers, is the proportion of coal / ash mixture. There is generally no further usability, the operator of these systems can only dispose of this residual material.

The invention now uses the possibility of utilizing the gasification process in a further gasification stage, in the form of steam gasification, steam reforming and dry reforming. This gasification stage now uses the properties of the water gas reaction (WGS = water vapor shift reaction) and the generator gas reaction ("Bouduard reaction").

C + H ₂ O - CO + H ₂

C + CO ₂ - 2CO.

/ 32

In order to obtain a high degree of implementation, the substrate must be applied

Residues (54) and carbon must now be ground in order to obtain a large surface. Milling means a lump size of d ~ 1mm to 5 mm to a large one

Creating surface.

The invention also uses the energetic potential of the residues such as coal (48) from the gasification process (40), such as high-quality ground residues (54), wood chips, paper and plastic, waste wood, shells, fibers, cores, in a second gasification process (64) known as steam gasification and gas reforming. The invention combines steam gasification and gas reforming as shown in the following chemical reactions:

C + H ₂ O - CO + H,

CO + H ₂ O— * CO ₂ + H ₂

CH ₄ + H ₂ O - CO + 3H ₂

C + CO ₂ - 2CO

CH ₄ + CO ₂ - 2CO + 2H,

The lean gas thus generated has a composition as shown in the following table:

grade CO η ₂ CO ₂ ch ₄ C _x H _v H ₂ O n ₂ - ugh % % % % % % ppm kJ / m ³ Syngas 1 1 60 20 1 3 10 100 10.14 Syngas 2 20 60 1 1 3 10 100 12.67 Syngas 3 40 40 10 1 3 6 100 12.65 Table 4: Step Example adhesive composition of synthe table gases

A distinction is made between the proportion of carbon, methane, water vapor and carbon dioxide that are introduced into the reactors as gas and vapor components and solids, such as carbon (C): 'a CH ₄ + bH ₂ O + cCO ₂ + dC — ►xCO + yH ₂

grade a b c d X y - Syngas 1 0 X 0 X 0 X Syngas 2 0 X 0 X X X Syngas 3 χ X X X X X

Table 5: Shows the exemplary combinations of the gas and steam flows introduced into the reactor (64)

The invention therefore uses steam gasification not only in the form of the water vapor generated, but also in the form of the injected carbon dioxide and the injected residual gas consisting of methane. Residual gases are to be understood as any gases as in Table 2. The decisive factor is the methane content, since the reforming of methane generates from hydrogen, whereby methane can be reformed with the help of water vapor and with the help of carbon dioxide.

The invention also enables the use of different regulated (35, 36) volume flows and proportions of water vapor, carbon dioxide based on the / 32

Gas composition of the residual gases (composition in methane, hydrogen, carbon dioxide, carbon monoxide) (Table 2), as well as the introduced and required carbon (Tables 1, 3), in order to generate a corresponding composition of the weak gas thus generated. The lean gas (65) from the second gasification stage (SGA), often also referred to as synthetic gas, can thus be processed for the following reactions:

Step 1

Methanol synthesis:

CO + 3H ₂ -CH3OH

2CH ₃ OH —► CH3OCH3 + H ₂ O

2nd step

DME synthesis

2CH ₃ OH — ► CH ₃ OCH ₃ + H ₂ O

Or the direct dimethyl ether synthesis (1st step and 2nd step in one step)

3CO + 3H ₂ --- CH ₃ OCH ₃ + CO ₂

The invention also uses a part of the weak gas (52) generated in the first gasification stage (40) in order to generate the necessary heat for the steam generation. This is done in the form of a combustion chamber (83) using artificial air consisting of oxygen (77) and carbon dioxide (76) in order to completely oxidize the lean gas in the combustion chamber to carbon dioxide and water vapor.

According to the invention, artificial air (gas mixture of oxygen and carbon dioxide) means a gas mixture of oxygen and carbon dioxide with a nitrogen content <0.01% by volume. The nitrogen content comes from the oxygen obtained from the air by means of pressure swing adsorption. According to the invention, a volume fraction of 10% of oxygen is required for the gasification in order to generate the necessary heat in the reactor (VGA) (40). By diluting the oxygen with carbon dioxide there is the possibility of reducing the nitrogen content <100 ppm (~ 0.01 vol%). With this method according to the invention, the need to separate nitrogen from the lean gas (73) of the second gasification stage (SGA) can be avoided.

The hot exhaust gas (84) obtained in this way from the combustion chamber (83), consisting of carbon dioxide and water vapor, is introduced into the second gasification reactor (SGA) (64) via the nozzle base (60). The advantage is that the gasification temperature (64) can be increased from 500 ° C to temperatures from 80 ° C to 1200 ° C.

According to the invention, it is not turbulent combustion that is used in the combustion chamber (83), but surface combustion. In order to achieve surface combustion, i.e. a reaction on a surface, ceramic balls are used in the combustion chamber, which store the heat generated. The combustion chamber is operated at a temperature of 1600 ° C. In addition to the lean gas that needs to be oxidized, the oxygen is injected into the combustion chamber. The chemical reaction of the oxidation takes place on the surface due to the hot surface. The chemical / 32

The heat generated during the reaction serves on the one hand to heat the gas and to keep the ceramic balls warm.

In a temperature range from 1000 ° C. to 1200 ° C. in the gasification reactor (64), biogases (112) and residual gases (112) can now also be added according to the invention, because the chemical reaction of the reforming of methane and carbon dioxide can now take place:

CH ₄ + CO ₂ --► 2CO + 2H ₂

Another advantage according to the invention is the very low nitrogen content in the lean gases generated in both gasification stages. The nitrogen content is less than <100 ppm, so that the formation of nitrogen oxides NO, NO ₂ , in the presence of oxygen and compression of the synthetic gas (73) to a pressure of 50 bar to 100 bar, is almost suppressed. This has the advantage that there are hardly any nitrogen oxides (NO, NO ₂ ) that could inhibit the effectiveness of the catalysts used in methanol synthesis and in dimethyl ether synthesis. As catalysts for methanol synthesis and for dimethyl ether synthesis, aluminum oxides are generally used as the base body with copper oxide and zinc oxide: AI2O3 - CuO - ZnO. If nitrogen oxide accumulates in the form of NO and NO ₂ , then the catalyst is blocked in its action and the methanol synthesis cannot take place.

The application of this invention is made possible by the combination of the two gasification processes, the utilization of inferior residues in the first gasification stage and the use of the lean gas to generate water vapor in the second gasification stage. The first gasification stage is operated with a reactor temperature of 1200 ° C to 1600 ° C, and the lean gas is also sucked out of the reactor. This has the advantage that the lean gas is never pushed out of the reactor into the environment during operation, as in the overpressure process.

The recycling of carbon from the first gasification stage gives the possibility of a highly efficient use of the solid and gaseous residues. The utilization of gaseous residues at a reactor temperature in the second reactor stage also requires the availability of carbon, water vapor and methane, as well as the corresponding proportion of carbon dioxide.

With this method according to the invention, the diversity in the utilization of residues is increased. In addition, the lean gas has a very high calorific value in a range from 2.5 kWh / m ³ to 4.0 kWh / m ³ . This calorific value is 2.5 times to 4.0 times higher than in the first gasification stage (VGA) (40).

The process according to the invention is not only limited to organic solid residues, but can also be applied to synthetic solid residues, and the combination with the second gasification stage (SGA) (64) enables not only the organic biogenic residual gases (Table 2) but also synthetic residual gases (Table 2 Recycle.

The power of the gasification stage is in an electrical power range from 250 kWh to 1000 kWh, which is a volume flow of 500 m ³ / h to 2000 m ³ / h with a calorific value of 1.0 kWh / m ³ to 1.5 kWh / m ³ , In the second gasification stage (SGA) (64) an electrical output of 500 kWh to 5000 kWh can be achieved, which corresponds to a volume flow of 500 m ³ / h to 5000 m ³ / h with a calorific value of the gas of 2 5 kWh / m ³ to 4.0 kWh / m ³ .

/ 32

The thermodynamic relationship is discussed in the following section: Steam is required for steam gasification:

C + H ₂ O --- CO + H ₂

This results in the following mass balance: 1 kg / h of carbon requires 1.5 kg / h of water vapor, with an evaporation enthalpy of h _v ~ 2560 kJ / kg of water, 1.35 kWh of heat are required. For heating to a temperature, 1.0 kWh of heat is required in buzzer 2.35 kWh of heat. This gives the relation with the chess gas from the first gasification stage. With a heating value of 1.0 kWh / m ³ , 2.35 m ³ / h are required, with a heating value of 1.5 kWh / m ³ , 1.6 m ³ / h are required.

The following relation results from the mass balance: 1 kg / h carbon results in 2kg / h carbon monoxide and 0.16 kg / h hydrogen.

3CO + 3H ₂ —►CH ₃ OCH ₃ + CO ₂

The following relation results for the production of dimethyl ether (DME): 1kg / h carbon monoxide and 0.16kg / h hydrogen produce 2 L / h DME and 1.22 kg / h carbon dioxide.

The invention also follows the principle of "zero emission" since the exhaust gases (4, 114, 115) from the combustion chamber (83, 113) are converted to carbon dioxide and water vapor.

The invention also has the advantage of upscaling small production units of dimethyl ether (DME) from 200L / h to 5000L / h without considerable equipment and plant outlay. This shows that this invention is suitable for the regional, decentralized generation of "waste to liquid".

/ 32

Signs and symbols

Water (process water)

water tank

Process water pump

Control valve (process water)

Heat exchanger (economizer)

Heat exchanger (evaporator 1)

Heat exchanger (evaporator 2)

Water condensate return

Evaporator water vapor

Steam - water mixture

Steam drum - saturated steam

Saturated steam steam

Superheater steam

air

Nitrogen (N ₂ )

Pressure swing adsorption to obtain enriched oxygen.

Control valve for oxygen (O ₂ ) liquid carbon dioxide, which is supplied externally.

Carbon dioxide tank

Carbon dioxide pump

Control valve for carbon dioxide

Vaporizer - carbon dioxide vaporous carbon dioxide

Hot gas flow

Hot gas return

Superheater for carbon dioxide

Control valve Kohlendixoid

Control valve carbon dioxide

Control valve carbon dioxide

Control valve water vapor

Hot gas flow

Hot gas return

Carbon dioxide for the second stage of gasification

Water vapor for the second gasification stage

Control valve carbon dioxide

Control valve water vapor

First gasification residues (VGA)

Flap 1 / double flap

Flap 2 / double flap

First gasification stage (VGA) reactor

raw gas

cyclone

raw gas

Cyclone coal

Recirculation scroll

rectifier

Coal and ash discharge screw

Gas-tight control valve / 32

gas cleaning

clean gas

compressor

Clean gas - external use

Clean gas for electricity and heat generation

Second gasification residues (SGA)

Flap 1

Flap 2

feed screw

Gas and steam mixer

Water vapor and carbon dioxide

Second gasification stage (SGA)

rectifier

discharge screw

Recirculation scroll

reactor

raw gas

Raw gas from cyclone

cyclone

Gas cleaning, gas-tight fitting

Carbon from cyclone

clean gas

compressor

clean gas

Carbon dioxide flushing filling flaps second gasification stage (SGA)

Carbon dioxide flushing filling flaps first gasification stage (VGA) carbon dioxide control valve

Carbon dioxide control valve

Residual gases for the combustion chamber

compressor

control valve

Low gas compressor from first gasification stage (VGA)

control valve

combustion chamber

Exhaust gas from the combustion chamber

Compressor residual gases

Control valve for residual gases

residual gases

Superheater residual gases are hot residual gases

Nozzle base of residual gases

Clean gas for dimethyl ether plant

Stage 1 compressor

drycoolers

Stage 2 compressor

drycoolers

capacitor

preheater

Carbon dioxide tank

Pump liquid carbon dioxide liquid carbon dioxide / 32 • · ·· · · · · · · · · · ·

101 Syngas in dimethyl ether synthesis

102 Methanol synthesis

103 Offgas

104 water from methanol synthesis

105 methanol recycling

106 DME reactor

107 Water from DME synthesis

108 dimethyl ether (DME)

109 Offgas control valve

110 offgas

111 water

112 residual gases (carbon water rich)

113 water vapor and carbon dioxide

114 compressors

115 control valve

116 combustion chamber

117 Control valve for oxygen from pressure swing adsorption (16)

abbreviations

PSA pressure swing adsorption: separation of air into oxygen and nitrogen VGA gasification first stage (cocurrent / countercurrent)

SGA steam gasification, gas reforming in the second gasification stage

CO2 carbon dioxide

H2O water / water vapor

CH4 methane

CO carbon monoxide

H2 hydrogen

CHP combined heat / 32

Figures Figure 1

Figure 1 shows the combined gasification levels. Water (1) is stored in a tank (2) and fed to the evaporator (9) via a pump (3) with the control valve (4). The evaporator consists of an economizer (5), a saturated steam evaporator (6,7), a steam drum (11), a superheater (8) which is filled with the saturated steam (12) from the steam drum (11), the superheated steam ( 13) is fed to the gasification reactor (40) of the first stage via the control valve (30). The steam evaporator is supplied with hot gas (31) in the flow and the cooled hot gas (32) is removed in the return.

In addition to water (1), liquid carbon dioxide (18) is also supplied to the carbon dioxide tank (19). The liquid carbon dioxide is fed to the evaporator (22) via the pump (20) and the control valve (21), and is subsequently fed to the gasification reactor (40) via the superheater (26) and the control valve (29).

Air (14) is drawn in and separated into oxygen and nitrogen in the pressure swing adsorption (16), the nitrogen (N2) (15) is released to the environment, and the oxygen is supplied to the overheated carbon dioxide via the control valve (17).

In order to keep the proportion of nitrogen input into the gasification reactor (40) low, vaporous carbon dioxide (23) is fed to the double flap (38, 39) via the control valve (28) and the air is flushed out before the reactor (40) is filled.

Residual material (37) is fed to the gasification reactor (40) via the double flap (38, 39), the raw gas (41) is cleaned of coal dust via a cyclone (42), the raw gas (43) is fed to the gas cleaning system (49), the clean gas (50) via the compressor (51) for further utilization (52, 53). The coal dust (44) from the cyclone (42) is fed to the reactor (40) via the return screw (45), the coal and ash mixture via the rectifier (46) and the discharge screw (47) with gas-tight fitting (48) of the second gasification stage (64) fed.

The second gasification stage (64) consists of a reactor (64) with an entry screw (57) for the residues (54) via a double flap (55, 56) which is flushed with carbon dioxide (74) via the control valve (27).

Hot carbon dioxide (33) is fed via the control fitting (35) to the nozzle base (60) via the gas and steam mixer (58) in which water vapor and carbon dioxide are mixed (59). The superheated steam (34) is fed to the gas and steam mixer (58) via the control valve (36).

The raw gas (65) from the reactor (64) is passed over the cyclone (67) and the dust-free raw gas (66) is fed to the gas cleaning (68), the clean gas (71) via the compressor (72) for further use Syngas (73) provided.

The ash in the reactor (64) is discharged from the reactor (64) via the rectifier (61), the discharge screw (62) and the gas-tight fitting (69). The coal (70) obtained from the cyclone (67) is returned to the reactor (64) via the return screw (63).

/ 32

Figure 2

Figure 2 shows the combined gasification levels. Water (1) is stored in a tank (2) and fed to the evaporator (9) via a pump (3) with the control valve (4). The evaporator consists of an economizer (5), a saturated steam evaporator (6,7), a steam drum (11), a superheater (8) which is filled with the saturated steam (12) from the steam drum (11), the superheated steam ( 13) is fed to the gasification reactor (40) of the first stage via the control valve (30). The steam evaporator is supplied with hot gas (31) in the flow and the cooled hot gas (32) is removed in the return.

In addition to water (1), liquid carbon dioxide (18) is also supplied to the carbon dioxide tank (19). The liquid carbon dioxide is fed to the evaporator (22) via the pump (20) and the control valve (21), and is subsequently fed to the gasification reactor (40) via the superheater (26) and the control valve (29).

Air (14) is drawn in and separated into oxygen and nitrogen in the pressure swing adsorption (16), the nitrogen (N2) (15) is released to the environment, and the oxygen is supplied to the superheated carbon dioxide via the control valve (17).

In order to keep the proportion of nitrogen input into the gasification reactor (40) low, vaporous carbon dioxide (23) is fed to the double flap (38, 39) via the control valve (28) and the air is flushed out before the reactor (40) is filled.

Residual material (37) is fed to the gasification reactor (40) via the double flap (38, 39), the raw gas (41) is cleaned of coal dust via a cyclone (42), the raw gas (43) is fed to the gas cleaning system (49), the clean gas (50) via the compressor (51) for further utilization (52, 53). The coal dust (44) from the cyclone (42) is fed to the reactor (40) via the return screw (45), the coal and ash mixture via the rectifier (46) and the discharge screw (47) with gas-tight fitting (48) of the second gasification stage (64) fed.

The second gasification stage (64) consists of a reactor (64) with an entry screw (57) for the residues (54) via a double flap (55, 56) which is flushed with carbon dioxide (74) via the control valve (27).

Hot carbon dioxide (33) is fed via the control fitting (35) to the nozzle base (60) via the gas and steam mixer (58) in which water vapor and carbon dioxide are mixed (59). The superheated steam (34) is fed to the gas and steam mixer (58) via the control valve (36).

The raw gas (65) from the reactor (64) is passed over the cyclone (67) and the dust-free raw gas (66) is fed to the gas cleaning (68), the clean gas (71) via the compressor (72) for further use Syngas (73) provided.

The ash in the reactor (64) is discharged from the reactor (64) via the rectifier (61), the discharge screw (62) and the gas-tight fitting (69). The coal (70) obtained from the cyclone (67) is returned to the reactor (64) via the return screw (63).

The clean gas (52) obtained from the first gasification stage (40) is fed to the combustion chamber (63) via the compressor (61), a control valve (62). In the combustion chamber (83) the lean gas (52) is burned with oxygen via the control valve (77) and carbon dioxide via / 32 the control valve (76) to water vapor and carbon dioxide (84) and the

Mixing chamber (58) fed to the second carburetor stage. External residual gases (78) can also be in the combustion chamber (63) via the compressor (79) and the control valve (80)

Combustion chamber (83) are supplied.

Figure 3

Figure 3 shows the combined gasification levels. Water (1) is stored in a tank (2) and fed to the evaporator (9) via a pump (3) with the control valve (4). The evaporator consists of an economizer (5), a saturated steam evaporator (6,7), a steam drum (11), a superheater (8) which is filled with the saturated steam (12) from the steam drum (11), the superheated steam ( 13) is fed to the gasification reactor (40) of the first stage via the control valve (30). The steam evaporator is supplied with hot gas (31) in the flow and the cooled hot gas (32) is removed in the return.

In addition to water (1), liquid carbon dioxide (18) is also supplied to the carbon dioxide tank (19). The liquid carbon dioxide is fed to the evaporator (22) via the pump (20) and the control valve (21), and is subsequently fed to the gasification reactor (40) via the superheater (26) and the control valve (29).

Air (14) is drawn in and separated into oxygen and nitrogen in the pressure swing adsorption (16), the nitrogen (N2) (15) is released to the environment, and the oxygen is supplied to the superheated carbon dioxide via the control valve (17).

In order to keep the proportion of nitrogen input into the gasification reactor (40) low, vaporous carbon dioxide (23) is fed to the double flap (38, 39) via the control valve (28) and the air is flushed out before the reactor (40) is filled.

Residual material (37) is fed to the gasification reactor (40) via the double flap (38, 39), the raw gas (41) is cleaned of coal dust via a cyclone (42), the raw gas (43) is fed to the gas cleaning system (49), the clean gas (50) via the compressor (51) for further utilization (52, 53). The coal dust (44) from the cyclone (42) is fed to the reactor (40) via the return screw (45), the coal and ash mixture via the rectifier (46) and the discharge screw (47) with gas-tight fitting (48) of the second gasification stage (64) fed.

The second gasification stage (64) consists of a reactor (64) with an entry screw (57) for the residues (54) via a double flap (55, 56) which is flushed with carbon dioxide (74) via the control valve (27).

Hot carbon dioxide (33) is fed via the control fitting (35) to the nozzle base (60) via the gas and steam mixer (58) in which water vapor and carbon dioxide are mixed (59). The superheated steam (34) is fed to the gas and steam mixer (58) via the control valve (36).

The raw gas (65) from the reactor (64) is passed over the cyclone (67) and the dust-free raw gas (66) is fed to the gas cleaning (68), the clean gas (71) via the compressor (72) for further use as syngas (73) provided.

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The ash in the reactor (64) is discharged from the reactor (64) via the rectifier (61), the discharge screw (62) and the gas-tight fitting (69). The coal (70) obtained from the cyclone (67) is returned to the reactor (64) via the return screw (63).

The clean gas (52) obtained from the first gasification stage (40) is fed to the combustion chamber (63) via the compressor (61), a control valve (62). In the combustion chamber (83), the lean gas (52) is burned with oxygen via the control fitting (77) and carbon dioxide via the control fitting (76) to water vapor and carbon dioxide (84) and fed to the mixing chamber (58) of the second gasification stage. In the combustion chamber (63), external residual gases (78) can also be fed to the combustion chamber (83) via the compressor (79) and the control valve (80).

Additional external residual gases (112) are fed to a superheater (88) via the compressor (85) and the control valve (86), and the hot residual gases (89) are introduced into the reactor (64) via the nozzle base (90).

Figure 4

Figure 4 shows the combined gasification levels. Water (1) is stored in a tank (2) and fed to the evaporator (9) via a pump (3) with the control valve (4). The evaporator consists of an economizer (5), a saturated steam evaporator (6,7), a steam drum (11), a superheater (8) which is filled with the saturated steam (12) from the steam drum (11), the superheated steam ( 13) is fed to the gasification reactor (40) of the first stage via the control valve (30). The steam evaporator is supplied with hot gas (31) in the flow and the cooled hot gas (32) is removed in the return.

In addition to water (1), liquid carbon dioxide (18) is also supplied to the carbon dioxide tank (19). The liquid carbon dioxide is fed to the evaporator (22) via the pump (20) and the control valve (21), and is subsequently fed to the gasification reactor (40) via the superheater (26) and the control valve (29).

Air (14) is drawn in and separated into oxygen and nitrogen in the pressure swing adsorption (16), the nitrogen (N2) (15) is released to the environment, and the oxygen is supplied to the superheated carbon dioxide via the control valve (17).

In order to keep the proportion of nitrogen input into the gasification reactor (40) low, vaporous carbon dioxide (23) is fed to the double flap (38 39) via the control valve (28) and the air is flushed out before the reactor (40) is filled.

Residual material (37) is fed to the gasification reactor (40) via the double flap (38, 39), the raw gas (41) is cleaned of coal dust via a cyclone (42), the raw gas (43) is fed to the gas cleaning system (49), the clean gas ( 50) via the compressor (51) for further utilization (52, 53). The coal dust (44) from the cyclone (42) is fed to the reactor (40) via the return screw (45), the coal and ash mixture via the rectifier (46) and the discharge screw (47) with gas-tight fitting (48) of the second gasification stage (64) fed.

The second gasification stage (64) consists of a reactor (64) with an entry screw (57) for the residues (54) via a double flap (55, 56) which is flushed with carbon dioxide (74) via the control valve (27).

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Hot carbon dioxide (33) is via the control valve (35) the nozzle bottom (60)

Gas and steam mixers (58) in which water vapor and carbon dioxide are mixed (59). The superheated steam (34) is the gas and the control valve (36)

Steam mixer (58) fed.

The raw gas (65) from the reactor (64) is passed over the cyclone (67) and the dust-free raw gas (66) is fed to the gas cleaning (68), the clean gas (71) via the compressor (72) for further use as syngas (73) provided.

The ash in the reactor (64) is discharged from the reactor (64) via the rectifier (61), the discharge screw (62) and the gas-tight fitting (69). The coal (70) obtained from the cyclone (67) is returned to the reactor (64) via the return screw (63).

The clean gas (52) obtained from the first gasification stage (40) is fed to the combustion chamber (63) via the compressor (61), a control valve (62). In the combustion chamber (83), the lean gas (52) is burned with oxygen via the control fitting (77) and carbon dioxide via the control fitting (76) to water vapor and carbon dioxide (84) and fed to the mixing chamber (58) of the second gasification stage. In the combustion chamber (63), external residual gases (78) can also be fed to the combustion chamber (83) via the compressor (79) and the control valve (80).

The heat required for the evaporator (9) in the form of a hot gas is sucked in from the combustion of the weak gas (52) via a compressor (114) via a control fitting (115) in the combustion chamber (116) to a hot exhaust gas consisting of carbon dioxide and water vapor and then introduced as a gas and steam mixture (113) into the second gasification stage (64) via the nozzle base (60).

Figure 5

Figure 5 shows the recovery of the purified synthetic gas (73) from the second gasification stage (64). The synthetic gas (91) is fed to the first compressor stage (91), then fed to the second compressor stage (94) via the recooler (93), cooled via the recooler (95), and carbon dioxide is eliminated in the liquid phase via the condenser (96) and stored in the carbon dioxide tank (98) and made available for recycling by the pump (99) as liquid carbon dioxide (100). The compressed synthetic gas is heated (101) via the heat exchanger (97) and fed to the methanol synthesis (102). The offgas (110) obtained from the methanol synthesis (102) is made available via the control valve (109). Water (104) from the methane mole synthesis (102) and water (107) from the dimethyl ether synthesis (106) are made available to the process as process water (111). Dimethyl ether (108) is obtained from dimethyl ether synthesis (106). The unused methanol (105) is recycled in the methanol synthesis (102).

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Claims (6)

Expectations 1. The process according to the invention for combining gasification processes, comprising a reactor (40), a double flap (38, 39), a cyclone (42), a return screw (45), a discharge screw (47), a pressure swing adsorption (16) and one Control valve (17), a reactor (54), with a nozzle plate (60), with a cyclone (67), with a return screw (63), with a discharge screw (62), with a carbon dioxide tank (19) with associated pump (20 ), Control valve (21), with evaporator (22), with a superheater (26), with a water tank (2), with an associated pump (3), with a control valve (4), an evaporator (9), the control valves (29.30), the control valves (35.36) Characterized in that - Residues (37) is introduced into the reactor (40) via a double flap (38, 39) - Under residual materials (37) waste wood, plastic, paper, plastic foils, shells and cores, which have a lump with a diameter of at least 15 mm, maximum 50 mm, preferably 25 mm, with a length of minimum 25 mm, maximum 80 mm, preferably 50 mm have, - The water content of the residues (37) is a minimum of 5%, a maximum of 15%, preferably 15%, - The reactor (40) works according to the cocurrent principle or countercurrent principle as a fixed bed reactor - The reactor (40) is operated in a negative pressure and has a pressure of at least 0.4 bar, at most 0.95 bar, preferably 0.8 bar - The raw gas (43) is sucked out of the reactor (40) from the reactor (40) with a hydraulically driven piston compressor, - The volume flow of the raw gas (41) is a minimum of 500 m ³ / h, a maximum of 2500 m ³ / h, preferably 2000 m ³ / h - The necessary heat in the reactor (40) is achieved by a substoichiometric combustion with oxygen from a pressure swing adsorption (16) and has an air mass to residual mass ratio of minimum 0.1, maximum 0.8, preferably 0.25 - The temperature in the reactor (40) in the oxidation zone has a minimum of 800 ° C, a maximum of 1600 ° C, preferably 1200 ° C - The raw gas from the reactor (40) is passed over a cyclone (42), and so the discharged coal content is reduced by a minimum of 50%, a maximum of 98%, preferably 90% - The coal obtained from the cyclone is returned to the reactor (40) via a return screw (45) with a minimum volume flow of 0.1 m ³ / h, maximum 10 m ³ / h - Carbon dioxide (16) from a carbon dioxide tank (19) with a pump (20) via a control valve (21) in an evaporator (22) and a superheater (26) and a control valve (29) introduced into the oxidation zone of the reactor (40) becomes - The pressure of the introduced carbon dioxide is a minimum of 0.9 bar, a maximum of 1.5 bar, preferably 1.1 bar 18/32 - The temperature of the introduced carbon dioxide is a minimum of 100 ° C, a maximum of 600 ° C, preferably 400 ° C - The volume flow of the introduced carbon dioxide is a minimum of 1 m ³ / h, a maximum of 500 m ³ / h, preferably 100 m ³ / h. - Water (1) from a water tank (2) with a pump (3) via a control valve (4) in an evaporator (9) and a superheater (8) and a control valve (30) introduced into the oxidation zone of the reactor (40) becomes - The pressure of the introduced water vapor is a minimum of 0.9 bar, a maximum of 1.5 bar, preferably 1.1 bar - The temperature of the introduced water vapor is a minimum of 120 ° G, a maximum of 600 ° C, preferably 400 ° C - The volume flow of the introduced water vapor is a minimum of 1 m ³ / h, a maximum of 500 m ³ / h, preferably 100 m ³ / h - Residues (54) is introduced into the reactor (64) via a double flap (55, 56) - Under residual materials (54) waste wood, plastic, paper, plastic foils, shells and cores that have a lump with a diameter of at least 1 mm, maximum 10 mm, preferably 5 mm, with a length of minimum 5 mm, maximum 20 mm, preferably 10 mm have, - The water content of the residues (54) is a minimum of 5%, a maximum of 15%, preferably 15%, - In addition to residues (54), a coal-ash mixture can also be introduced via the double flaps (55, 56), the carbon content being a minimum of 60%, a maximum of 100%, preferably 90% - The reactor (64) works according to the countercurrent principle as a fixed bed reactor - The reactor (64) is operated in negative pressure and has a pressure of at least 0.4 bar, at most 0.95 bar, preferably 0.8 bar - The raw gas (65) is sucked out of the reactor (64) with a hydraulically driven piston compressor (72), - The volume flow of the raw gas (65) is a minimum of 500 m ³ / h, a maximum of 10000 m ³ / h, preferably 2500 m ³ / h - The necessary heat in the reactor (64) is introduced through the hot exhaust gas (84) from the combustion chamber (83) and through the hot carbon dioxide (33) and the hot water vapor (34) via the nozzle base (60) - The exhaust gas (84) from the combustion chamber has a temperature of minimum 600 ° C, maximum 1200 ° C, preferably 1000 ° C - The carbon dioxide (33) has a temperature of a minimum of 200 ° C, a maximum of 600 ° C, preferably 400 ° C, - The water vapor (34) has a temperature of a minimum of 200 ° C, a maximum of 600 ° C, preferably 400 ° C, - The temperature in the reactor (64) in the nozzle zone (60) has a minimum of 800 ° C, a maximum of 1600 ° C, preferably 1000 ° C - The raw gas (65) from the reactor (64) is passed through a cyclone (67), and so the discharged coal content is reduced by a minimum of 50%, a maximum of 98%, preferably 90%, - The coal obtained from the cyclone (67) is returned to the reactor (64) via a gas-tight return screw (63) with a minimum volume flow of 0.1 m ³ / h, maximum of 10 m ³ / h, 19/32 - The heat required for the evaporator (9) is provided externally via a hot gas flow (31) and a hot gas return (32) - The temperature of the hot gas (32) in the flow is a minimum of 600 ° C, a maximum of 1600 ° C and preferably 1200 ° C - The heat required for the evaporator (22) and the superheater (26) of the carbon dioxide (23) is provided externally via a hot gas flow (25) and a hot gas return (24) - The temperature of the hot gas (25) in the flow is a minimum of 600 ° C, a maximum of 1000 ° C and preferably 800 ° C 2. The method according to claim 1, comprising a combustion chamber (83), a compressor (81), with a control valve (82), with a control valve (77), with a control valve (76), characterized in that - Part of the lean gas (52) generated in the reactor (40) is introduced into the combustion chamber (83) - Via the hydraulically driven piston compressor (81), the lean gas (52) is sucked in and compressed to that pressure so that it can be injected into the combustion chamber (83). - The volume flow of the weak gas (52) can be controlled with the control valve (82) at least 1 m ³ / h, maximum 500 m ³ / h, preferably 100 m ³ / h - The weak gas (52) together with oxygen (77) from the pressure swing adsorption system (16) is completely oxidized to carbon dioxide and water vapor - In addition to the lean gas (52), carbon dioxide (23) can also be introduced into the combustion chamber (83) via the control fitting (76). The volume flow of carbon dioxide into the combustion chamber (83) is a minimum of 1 m ³ / h, a maximum of 500 m ³ / h, preferably 100 m ³ / h, - The temperature of the exhaust gas (84) from the combustion chamber (83) is a minimum of 400 ° C, a maximum of 1600 ° C, preferably 1000 ° C - The oxidation in the combustion chamber (83) takes place on the surface of balls which have a minimum diameter of 10 mm, a maximum of 50 mm, preferably 25 mm - The balls in the combustion chamber are made of ceramic zirconium oxide (ZrO2), so that they store the temperatures and can give off heat to the gas flows introduced, 3. The method according to claim 1, comprising a combustion chamber (116), a compressor (114), with a control valve (115), with a control valve (117), characterized in that - Part of the weak gas (52) generated in the reactor (40) is introduced into the combustion chamber (116) - Via the hydraulically driven piston compressor (114), the lean gas (52) is sucked in and compressed to that pressure so that it can be injected into the combustion chamber (116). , - The volume flow of the weak gas (52) can be controlled with the control valve (82) at least 1 m ³ / h, maximum 500 m ³ / h, preferably 100 m ³ / h 20/32 - The weak gas (52) together with oxygen (117) from the pressure swing adsorption system (16) is completely oxidized (113) to carbon dioxide and water vapor - The temperature of the exhaust gas (31) for the water evaporator (9) from the combustion chamber (116) is a minimum of 400 ° C, a maximum of 1600 ° C, preferably 1200 ° C - The temperature of the exhaust gas (25) for the superheater (26) of carbon dioxide from the combustion chamber (116) is a minimum of 400 ° C, a maximum of 1600 ° C, preferably 1200 ° C - The oxidation in the combustion chamber (116) takes place on the surface of balls which have a minimum diameter of 10 mm, a maximum of 50 mm, preferably 25 mm - The balls in the combustion chamber are made of ceramic zirconium oxide (ZrO2) so that they can store the temperatures and give off heat to the gas flows introduced, - The hot exhaust gas (32) from the water evaporator (9) and the hot exhaust gas (24) from the carbon dioxide evaporator (22) are introduced together as exhaust gas (113) into the nozzle base (60) of the reactor (64) 4. The method according to claim 2, comprising a compressor (79), with an associated control valve (80), characterized in that - Residual gases (78) which are understood as offgas (110) from a dimethyl ether process and have a calorific value of at least 0.1 kWh / m ³ and at most 5 kWh / m ³ - Via the hydraulically driven piston compressor (79), the remaining guests (78) are sucked in and compressed to that pressure so that they can be injected into the combustion chamber (83). - The residual gases (78) are compressed via the compressor (79) to a minimum pressure of 1.05 bar, maximum 2.5 bar, preferably 1.5 bar - The volume flow of the residual gases (78) can be regulated with the control fitting (80) at least 1 m ³ / h, at most 500 m ³ / h, preferably 100 m ³ / h 5. The method according to claim 1, comprising the control valve (27), the control valve (28), characterized in that - The control valve (27) serves to flush the filling space of the double flap (38, 39) of the reactor (40) with carbon dioxide - The air is exchanged for carbon dioxide by flushing the filling volume of the double flap (38, 39) - The carbon dioxide in the filling chamber of the double flap (38, 39) minimizes the oxygen input into the reactor (40) - The carbon dioxide in the filling chamber of the double flap (38, 39) minimizes the nitrogen input into the reactor (40) - The control valve (28) serves to flush the filling space of the double flap (55, 56) of the reactor (64) with carbon dioxide - The air is exchanged for carbon dioxide by flushing the filling volume of the double flap (55, 56) - The carbon dioxide in the filling chamber of the double flap (55, 56) minimizes the oxygen input into the reactor (64) 21/32 - The carbon dioxide in the filling chamber of the double flap (55, 56) minimizes the nitrogen input into the reactor (64) 6. The method according to claim 1, comprising a compressor (85), with a control valve (86), with a superheater (86), with a nozzle bottom (90), characterized in that - Residual gases (112) are understood to mean biogases, fermentation gases, landfill gases, digestate gases, which have a methane concentration of at least 0.5% by volume, at most 70%, preferably 50%, ’ - Via the hydraulically driven piston compressor, the residual gases (112) are sucked in and compressed to that pressure so that they can be injected into the reactor (64) via the nozzle base (90). - The residual gases (112) are compressed via the compressor (85) to a minimum pressure of 1.05 bar, maximum 2.5 bar, preferably 1.5 bar - The volume flow of the residual gases (112) can be controlled with the control valve (86) at least 1 m ³ / h, at most 500 m ³ / h, preferably 100 m ³ / h The temperature of the residual gases (112) can be increased to a minimum of 100 ° C., a maximum of 500 ° C., preferably 400 ° C. using the superheater (88), - The residual gases (112) can be introduced into the reactor (64) in a uniformly distributed manner via the nozzle base (90) 22/32 illustration 1 Figure 2 Figure 3 25/32 Figure 4 m 27/32 austrian patent office