AU2014334025B2 - Process for the production of a synthesis gas from carbonaceous fuel with low fixed-carbon content - Google Patents
Process for the production of a synthesis gas from carbonaceous fuel with low fixed-carbon content Download PDFInfo
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- AU2014334025B2 AU2014334025B2 AU2014334025A AU2014334025A AU2014334025B2 AU 2014334025 B2 AU2014334025 B2 AU 2014334025B2 AU 2014334025 A AU2014334025 A AU 2014334025A AU 2014334025 A AU2014334025 A AU 2014334025A AU 2014334025 B2 AU2014334025 B2 AU 2014334025B2
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- gasification
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- 239000000446 fuel Substances 0.000 title claims abstract description 97
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 36
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 31
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 8
- 239000007789 gas Substances 0.000 claims abstract description 49
- 238000000197 pyrolysis Methods 0.000 claims abstract description 30
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000001257 hydrogen Substances 0.000 claims abstract description 12
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 12
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 9
- 238000002309 gasification Methods 0.000 claims description 40
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 27
- 238000007599 discharging Methods 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 238000011144 upstream manufacturing Methods 0.000 abstract description 2
- 239000000571 coke Substances 0.000 description 8
- 239000003245 coal Substances 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 4
- 239000000470 constituent Substances 0.000 description 4
- 239000002023 wood Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000010791 domestic waste Substances 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000003077 lignite Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 235000003625 Acrocomia mexicana Nutrition 0.000 description 1
- 244000202285 Acrocomia mexicana Species 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000001963 growth medium Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000005022 packaging material Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000002123 temporal effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
- C10J3/34—Grates; Mechanical ash-removing devices
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/06—Continuous processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/64—Processes with decomposition of the distillation products
- C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0903—Feed preparation
- C10J2300/0909—Drying
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
- C10J2300/092—Wood, cellulose
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/094—Char
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0943—Coke
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
Abstract
Process and plant for the production of a synthesis gas containing carbon monoxide and hydrogen from carbonaceous fuel with low fixed-carbon content, wherein upstream of the synthesis gas production a pyrolysis treatment of the fuel is provided in a separate reactor.
Description
Field of the Invention
This invention relates to a process for the production of a synthesis gas containing carbon monoxide and hydrogen from carbonaceous fuel with low fixed-carbon content. This invention also relates to a plant in which the process according to the invention is operated.
Prior art
Processes and plants for the gasification of carbonaceous fuels, such as lignite, hard coal or coke, are known from the prior art. What has proven particularly suitable is the use of fixed-bed gasification reactors, cf. Ullmann's Encyclopedia of Industrial Chemistry, Sixth Edition, Vol. 15, pp. 367 to 371.
With the gasification media oxygen and steam the fuel is gasified to a synthesis gas chiefly consisting of carbon monoxide and hydrogen, by forming an ash. In the following, the term synthesis gas is to be understood such that this gas is a
WO 2015/052050
PCT/EP2014/071014 synthetically, i.e. artificially, produced gas. Nothing should be stated here as to the further use of the gas.
For some time, fixed-bed gasification reactors also have been used for the gasification of fuels with low fixed carbon content, such as wood, biowaste and domestic waste.
Fixed-carbon content Cfix, indicated in wt-%, is understood to be that amount of fuel which is left after subtraction of the water content (determined according to DIN 51718), the ash content (determined according to DIN 51719) and the content of volatile constituents, i.e. constituents to be expelled by pyrolysis (determined according to DIN 51720).
In the following, the indicated values for the fixed-carbon content Cfix relate to the water- and ash-free reference state, i.e.
Cfix [wt-%] = (Mtotai [g] — Mw [g] — Mash [g] MVoiatiies [g])/(Mtotai [g] — Mw [g] — Mash [g]) wherein
M = mass
Mtotai = total mass of the sample
Mw = mass of the moisture in the sample
Mash = mass of the ash in the sample
Mvoiatiies = mass of the volatile constituents in the sample to be expelled by pyrolysis
In the fixed bed of the gasification reactor, the fuel passes through the phases of drying, pyrolysis, gasification, combustion and discharge of the ash or slag from top to bottom i.e. in direction of rising temperature.
In the pyrolysis, the non-fixed carbon in the fuel is expelled from the fuel in the form of highly volatile gases, chiefly carbon dioxide and methane, and
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-3condensable hydrocarbons, such as tar and oils. These gases leave the reactor unburnt and mixed with the synthesis gas, so that subsequently further process steps are required for separating these gases.
Of the usual fuels coke, hard coal and lignite the latter has the lowest Cfix content of about 45 wt-%. The synthesis gas produced from fuels with even lower CfjX content, such as wood or garbage, therefore contains an unusually high content of volatile pyrolysis gases and therefore requires further technical measures, in order to be processed together with the synthesis gas of usual composition.
When the fixed-carbon content of the fuel merely lies in the range of 15 wt-% or below, the problem furthermore arises that the amount of fixed carbon is not sufficient to produce the required heat for the formation of carbon monoxide and hydrogen for the pyrolysis and for drying the fuel in the upper region of the fixed bed by its combustion and at the same time be available as reactant for the formation of hydrogen and carbon monoxide.
When the content of fixed carbon is very low, this can lead to the fact that these fuels merely are pyrolyzed and burnt, and the formation of synthesis gas, i.e. carbon monoxide and hydrogen, hardly occurs. In these cases, the endothermal, heat-consuming reactions for the formation of synthesis gas then take place only to such a small extent that the temperature of the produced gas leaving the reactor rises so much, in some cases to more than 650 °C, that the reactor can be damaged.
Because fixed-bed gasification reactors mostly are operated at elevated pressure, the addition of fuel via a pressure lock mostly is effected in a discontinuous way. Since the pyrolysis of these fuels is effected very quickly, this discontinuous fuel supply leads to temporal fluctuations of the gas quantity produced. These fluctuations can have a disturbing effect on the methods with which the gas produced is treated further.
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-4An additional difficulty in the use of these fuels consists in that during the pyrolysis taking place in the upper region of the fixed bed they are converted into a very fine-grained coke. This can impair the uniformity of the traversal of the fixed bed with the gasification media, oxygen and steam. In addition, the pressure loss of the gas flowing through the fixed bed is increased with progressive deposition of coke.
One method to improve the processability of these fuels in the fixed-bed gasification reactor consists in increasing the content of fixed carbon in the fuel by admixing coal or coke to the fuel.
However, it is difficult to uniformly distribute the coal or the coke in the fuel, which e.g. consists of domestic waste. The consequence is a nonuniform operation of the reactor, with large fluctuations of the quality and quantity of the gas produced. In addition, the fuel costs are increased by admixing high-grade fuels with high CfjX content, partly due to the transport costs for the high-grade additional fuels.
The above-mentioned problem of the increased amount of pyrolysis gases in the gas produced, when using fuels with small CfjX content, only is reduced, but not eliminated by this measure of admixing coal.
In view of these numerous problems, it therefore has been the object to provide a process which avoids these disadvantages.
Description of the Invention
The object substantially is solved by a process for the production of a synthesis gas chiefly consisting of carbon monoxide and hydrogen from carbonaceous fuel with low fixed-carbon content, comprising the following process steps:
a) providing dried fuel and the gasification media oxygen and steam,
b) introducing at least a part of the fuel into a first reactor,
c) pyrolyzing the introduced part of the fuel in the first reactor and discharging the gases produced for the further treatment,
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-5d) discharging the fuel from the first reactor,
e) mixing the fuel treated in step c) with the untreated part of the fuel from step a),
f) introducing the fuel from step e) into a second reactor,
g) gasifying the fuel in the second reactor by using the gasification media under gasification conditions to obtain a synthesis gas containing hydrogen and carbon monoxide, wherein the synthesis gas and the ash are discharged from the second reactor for the further treatment.
Further advantageous aspects of the process according to the invention can be found in the sub-claims.
Gasification conditions are understood to be those conditions which by using the described gasification media lead to a conversion of the fuel to the synthesis gas constituents, which is acceptable from an economic point of view. They are well known to the skilled person from the relevant prior art, for example from the reference mentioned above.
Due to the at least partial displacement of the pyrolysis of the fuel from the fixedbed gasification reactor into a separate, upstream reactor, in particular the following advantages are achieved:
- The hydrocarbons released during the pyrolysis in gaseous form are not mixed with the gas produced during the gasification of the bound carbon, which chiefly consists of carbon monoxide and hydrogen. Therefore, they can be supplied to a specific further treatment or conditioning which is optimized with regard to their composition.
- The pyrolysis increases the content of fixed carbon in the fuel and thus provides for carrying out the gasification in the fixed-bed pressure gasifier without having to admix coal or coke to the fuel. Increasing the content of fixed carbon on the one hand is effected relatively, i.e. by expelling the non-fixed carbon with the pyrolysis
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-6gases from the fuel, but on the other hand also absolutely by converting non-fixed carbon into fixed carbon in the pyrolysis.
- The pyrolysis of the fuel, as it is carried out separate from the gasification, can be carried out such that a coke is produced which is more coarse-grained than would be possible in the fixed bed.
- Due to the inventive separation of pyrolysis and gasification it is possible to carry out these two process steps at separate plant locations. For example, garbage provided as fuel can be pyrolyzed at decentralized locations and then be further processed in a central gasification plant. Since the volume of the fuel is reduced by the pyrolysis, transport costs can be saved and the central gasification can be designed with a larger, more economic capacity.
The invention advantageously is applicable in particular for the gasification of wood, in particular waste wood, as well as biowaste and domestic waste which chiefly consists of biowaste and plastic residues, such as packaging material.
In a further aspect, the invention also relates to a plant for operating the process according to the invention, wherein the plant comprises at least one first reactor for the pyrolysis of the fuel, at least one second reactor for the gasification of the previously pyrolyzed fuel, feeding devices each for feeding a part of the untreated fuel to the first reactor and to the second reactor, a draining device for draining the fuel pyrolyzed in the first reactor, a mixing device for untreated and pyrolyzed fuel, and discharge devices for discharging pyrolysis gas from the first reactor as well as for discharging ash and synthesis gas from the second reactor.
Further preferred aspects of the invention
An advantageous aspect of the invention consists in that depending on its quality not the entire fuel must pass through the separate pyrolysis reactor, but that a part of the fuel is supplied untreated to the second reactor designed as fixed-bed pressure gasification reactor. In this way, the investment and operating costs of the gasification plant can be optimized. It is possible that a single fuel grade is submitted to the process according to the invention, wherein a part thereof is
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PCT/EP2014/071014 branched off, pyrolyzed and admixed again, or that two fuel grades are submitted, only one of which, wholly or in part, is pyrolyzed and then admixed for the gasification of the other grade.
In principle, carrying out the invention is independent of the kind of gasification process, i.e. independent of whether the fuel is converted to ash or slag and to synthesis gas in a fluidized bed, in an entrained flow or in a fixed bed. The process according to the invention, however, is particularly expedient for use in conjunction with fixed-bed gasifiers in which the fuel is present in a fixed bed held by a discharge grate. Fixed-bed gasifiers require a higher CfjX content in the fuel than for example entrained-flow gasifiers, as in the fixed bed the fixed carbon is the only supplier of thermal energy, whereas in the entrained flow the pyrolysis gases additionally contribute to the supply of thermal energy by combustion.
Another advantageous aspect of the invention consists in adjusting the content of fixed carbon in the fuel, which is introduced into the fixed-bed gasification reactor, by separate pyrolysis to at least 15 wt-%, preferably to at least 25 wt-%, and particularly preferably to at least 45 wt-%. Due to this measure, enough fixed carbon is present in the fixed bed of the fuel, in order to carry out the exothermal combustion reactions and the endothermal reactions for forming carbon monoxide and hydrogen, wherein the temperature of the gas produced in the gasification reactor remains below 600 °C and the wear of the reactor wall is limited.
In a further aspect of the process according to the invention, the amount of the untreated fuel, which must be treated in the first reactor, in order to adjust a desired content of fixed carbon in the fuel supplied to the second reactor, is calculated as follows:
M-| / Mtotal = (1 Cfix4(M4) / Cfixtotal (M total)) / (1 C^/IVU) X Οίίχβ/Μβ) / Cfixtotal(Mtotal) Cfix4(M4) / Cfix total (Mfotal));
wherein
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-8Mi/Mtotai = amount of the untreated fuel to the first reactor
CfiX4(M4) = content of fixed carbon in the fuel to the second reactor
Cfix,total (Mtotai) = content of fixed carbon in the untreated fuel
CfiX3(M3) = content of fixed carbon in the product stream of the first reactor
Exemplary embodiments and numerical examples
Further developments, advantages and possible applications of the invention can also be taken from the following description of non-limiting exemplary embodiments and numerical examples. All features described form the invention per se or in any combination, independent of their inclusion in the claims or their back-reference.
In the only Figure
Fig. 1 shows a schematic diagram of the mass flows of the process according to the invention.
This schematic diagram will be explained below. The mass flow Mtotai of the fuel, which is to be converted into synthesis gas G6, contains the mass flow CfjX,totai of fixed carbon. In dependence on its quality, the fuel is introduced into the first reactor R-ι completely or only in part for pyrolysis. In the latter case, the part M2 not treated in the reactor Ri and the pyrolyzed part M3 are mixed with each other by means of a non-illustrated mixing device before introduction into the reactor R4 to obtain the mass flow M4. The material stream G3 represents the pyrolysis gas withdrawn from the reactor R1 for the further treatment. The mass flow M4 is introduced into the second reactor R4 and by means of gasification medium G4 converted into synthesis gas G6 and ash M5. The synthesis gas stream G6 and the ash stream M5 are discharged from the reactor R4 for the further treatment.
With reference to the following example it will be explained how the necessary size of the fuel content ΜΊ/Μ is determined, which is to be adjusted, in order to
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-9adjust in the fuel stream M4, which is introduced into the gasification reactor R4, a desired content of fixed carbon suitable for the gasification in R4.
Numerical example:
Desired: Cfix4(M4): 45 wt-%
Measured: Cfix,totai (Mtotai) = Cfixi(ΜΊ): 17 wt-%
Measured: CfiX3(M3): 28 wt-%
The amount of the fuel, Mt/Mtotai, which must be treated in the reactor R1; in order to obtain the desired content of CfiX4 = 45 wt-% of fixed carbon in the fuel stream M4, which is introduced into the second reactor R4, is calculated as follows:
M-| / Mtotai = (1 Cfix4(M4) / Cfixtotal (Mtotai)) / (1 Cf|x4(M4) X Cfix3(M3) / Cfixtotal(Mtotal) Cf|x4(M4) / Cfix total (Mtotai))
i.e.
Mt / M,otai = (1 - 0.45 / 0.17) / (1 - 0.45 x 0.28 / 0.17 - 0.45 / 0.17 ) = 0.69 = 69 wt-%, consequently, 69 wt-% of the submitted fuel mass Mtotai accordingly must be subjected to the pyrolysis in reactor R1; in order to adjust a specific content of fixed carbon Cfix4 of 45 wt-% in the fuel M4 supplied to the gasification reactor R4.
Industrial Applicability
The invention provides an alternative process which provides for the production of synthesis gas also from fuels with very low fixed-carbon content, in particular also by means of fixed-bed gasification reactors.
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- 10List of Reference Numerals:
Mtotai, M-ι, M2, M3j M4 mass flow [kg/h] of the fuel
CfjX;total, Cfjxi, Cfix3, Cfix4 mass flow [kg/h] of the fixed carbon contained in the 5 fuel
M5 mass flow of ash
G3 mass flow of pyrolysis gas
G6 mass flow of synthesis gas
Ri pyrolysis reactor
R4 reactor for synthesis gas production
-112014334025 26 Mar 2018
Claims (5)
- Claims:1. A process for the production of a synthesis gas chiefly consisting of carbon monoxide and hydrogen from carbonaceous fuel with low fixed-carbon content, comprising the following process steps:a) providing dried fuel and the gasification media oxygen and steam,b) introducing at least a part of the fuel into a first reactor,c) pyrolyzing the introduced part of the fuel in the first reactor and discharging the gases produced for the further treatment,d) discharging the fuel from the first reactor,e) mixing the fuel treated in step c) with the untreated part of the fuel from step a),f) introducing the fuel from step e) into a second reactor,g) gasifying the fuel in the second reactor by using the gasification media under gasification conditions to obtain a synthesis gas containing hydrogen and carbon monoxide, wherein the synthesis gas and the ash are discharged from the second reactor for the further treatment, wherein the amount of the untreated fuel, that is introduced into the first reactor, in order to adjust a desired content of fixed carbon in the fuel supplied to the second reactor, is calculated as follows:Ml I Mtotal -(1- Cfix4(M4) I Cfix,total (Mtotal)) /(1- Cfix4(M4) X Cfix3(M3) ICfix,total (Mtotal) - Cfix4(M4) I Cfix,total (Mtotal)), whereinMi /Mtotai = amount of the untreated fuel to the first reactorCfix4(M4) = content of fixed carbon in the fuel to the second reactorCfix,total (Mtotai) = content of fixed carbon in the untreated fuelCfix3(M3) = content of fixed carbon in the product stream of the first reactor.
- 2. The process according to claim 1, wherein a part of the fuel is supplied untreated to the second reactor designed as a fixed-bed pressure gasification reactor.
- 3. The process according to claim 1 or 2, wherein the fuel in the second reactor is present in a fixed bed held by a discharge grate.
- 4. The process according to any one of the preceding claims, wherein the fixedcarbon content Cfix of the fuel introduced into the second reactor in step 1 .e) is at least 15 wt-%, preferably at least 25 wt-%, particularly preferably at least 45 wt-%.-122014334025 26 Mar 2018
- 5. A plant for operating the process according to any one of the preceding claims, wherein the plant comprises at least one first reactor for the pyrolysis of the fuel, at least one second reactor for the gasification of the previously pyrolyzed fuel, feeding devices each for feeding a part of the untreated fuel to the first reactor and to the second reactor, a draining device for draining the fuel pyrolyzed in the first reactor, a mixing device for untreated and pyrolyzed fuel, and discharge devices for discharging pyrolysis gas from the first reactor as well as for discharging ash and synthesis gas from the second reactor.WO 2015/052050PCT/EP2014/0710141/1Fig. 1
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102013111145.9 | 2013-10-09 | ||
DE201310111145 DE102013111145A1 (en) | 2013-10-09 | 2013-10-09 | A method for producing a synthesis gas from low carbon content carbonaceous fuel |
PCT/EP2014/071014 WO2015052050A1 (en) | 2013-10-09 | 2014-10-01 | Process for the production of a synthesis gas from carbonaceous fuel with low fixed-carbon content |
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AU (1) | AU2014334025B2 (en) |
DE (1) | DE102013111145A1 (en) |
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Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4541345A (en) * | 1983-03-23 | 1985-09-17 | C. Deilmann Ag | Apparatus for recovering energy from pyrolyzable, carbonaceous waste materials of varying composition |
US20090260286A1 (en) * | 2005-12-28 | 2009-10-22 | Chugai Ro Co., Ltd., A Corporation Of Japan | Biomass gasification apparatus |
DE102011011807A1 (en) * | 2011-02-19 | 2012-08-23 | Hans Walter Kirchner | Method for performing integrated biomass overpressure fixed bed gasification of steam turbine in power plant, involves carrying out regenerative heating of low temperature deaerator, and filtering dust from hot generator gases |
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DK200000417A (en) * | 2000-03-15 | 2001-09-16 | Cowi Radgivende Ingeniorer As | Process and plant for decomposition, gasification and / or combustion of moist fuel. |
JP5432554B2 (en) * | 2009-03-25 | 2014-03-05 | 一般財団法人電力中央研究所 | Gasification system |
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2013
- 2013-10-09 DE DE201310111145 patent/DE102013111145A1/en not_active Withdrawn
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2014
- 2014-10-01 WO PCT/EP2014/071014 patent/WO2015052050A1/en active Application Filing
- 2014-10-01 AU AU2014334025A patent/AU2014334025B2/en active Active
- 2014-10-09 CN CN201410528338.4A patent/CN104560214B/en active Active
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Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4541345A (en) * | 1983-03-23 | 1985-09-17 | C. Deilmann Ag | Apparatus for recovering energy from pyrolyzable, carbonaceous waste materials of varying composition |
US20090260286A1 (en) * | 2005-12-28 | 2009-10-22 | Chugai Ro Co., Ltd., A Corporation Of Japan | Biomass gasification apparatus |
DE102011011807A1 (en) * | 2011-02-19 | 2012-08-23 | Hans Walter Kirchner | Method for performing integrated biomass overpressure fixed bed gasification of steam turbine in power plant, involves carrying out regenerative heating of low temperature deaerator, and filtering dust from hot generator gases |
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ZA201508103B (en) | 2017-05-31 |
DE102013111145A1 (en) | 2015-04-09 |
AU2014334025A1 (en) | 2016-05-05 |
WO2015052050A1 (en) | 2015-04-16 |
CN104560214A (en) | 2015-04-29 |
CN104560214B (en) | 2019-08-16 |
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