EP2875102A1 - Gazéification à contre-courant/co-courant de substances riches en carbone - Google Patents
Gazéification à contre-courant/co-courant de substances riches en carboneInfo
- Publication number
- EP2875102A1 EP2875102A1 EP13752581.2A EP13752581A EP2875102A1 EP 2875102 A1 EP2875102 A1 EP 2875102A1 EP 13752581 A EP13752581 A EP 13752581A EP 2875102 A1 EP2875102 A1 EP 2875102A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- bulk material
- gas
- process chamber
- vertical process
- column
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
- 239000000126 substance Substances 0.000 title claims abstract description 32
- 238000002309 gasification Methods 0.000 title claims abstract description 29
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 18
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 238000000034 method Methods 0.000 claims abstract description 124
- 239000013590 bulk material Substances 0.000 claims abstract description 100
- 239000007789 gas Substances 0.000 claims abstract description 98
- 230000008569 process Effects 0.000 claims abstract description 90
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 35
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 35
- 239000001301 oxygen Substances 0.000 claims abstract description 35
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 33
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 31
- 230000003647 oxidation Effects 0.000 claims abstract description 16
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 16
- 238000006243 chemical reaction Methods 0.000 claims abstract description 15
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 11
- 239000000047 product Substances 0.000 claims abstract description 9
- 238000001816 cooling Methods 0.000 claims description 27
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 25
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 24
- 239000000292 calcium oxide Substances 0.000 claims description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 239000000428 dust Substances 0.000 claims description 11
- 239000003344 environmental pollutant Substances 0.000 claims description 11
- 231100000719 pollutant Toxicity 0.000 claims description 11
- 238000012216 screening Methods 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 8
- 239000000112 cooling gas Substances 0.000 claims description 8
- 230000001590 oxidative effect Effects 0.000 claims description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 5
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 5
- 239000000920 calcium hydroxide Substances 0.000 claims description 5
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 239000000498 cooling water Substances 0.000 claims description 5
- 229910052739 hydrogen Inorganic materials 0.000 claims description 5
- 239000001257 hydrogen Substances 0.000 claims description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 4
- 239000001569 carbon dioxide Substances 0.000 claims description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 239000002245 particle Substances 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 239000000446 fuel Substances 0.000 claims description 3
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 2
- 238000002407 reforming Methods 0.000 claims description 2
- 230000004992 fission Effects 0.000 claims 1
- 239000003921 oil Substances 0.000 description 12
- 239000000571 coke Substances 0.000 description 10
- 239000000463 material Substances 0.000 description 10
- 239000011269 tar Substances 0.000 description 9
- 239000002956 ash Substances 0.000 description 8
- 239000000203 mixture Substances 0.000 description 7
- 238000000197 pyrolysis Methods 0.000 description 6
- 239000012071 phase Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 3
- 239000000460 chlorine Substances 0.000 description 3
- 229910052801 chlorine Inorganic materials 0.000 description 3
- 238000010304 firing Methods 0.000 description 3
- 229910001385 heavy metal Inorganic materials 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 230000002829 reductive effect Effects 0.000 description 3
- 238000005979 thermal decomposition reaction Methods 0.000 description 3
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000003776 cleavage reaction Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 229910052736 halogen Inorganic materials 0.000 description 2
- 150000002367 halogens Chemical class 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000011368 organic material Substances 0.000 description 2
- 230000007017 scission Effects 0.000 description 2
- 238000007873 sieving Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000012790 confirmation Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 230000003292 diminished effect Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 150000003464 sulfur compounds Chemical class 0.000 description 1
- 230000007704 transition Effects 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
- C10J3/22—Arrangements or dispositions of valves or flues
- C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
- C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
-
- 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
- C10J3/72—Other features
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
-
- 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
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
-
- 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
- C10J2300/0983—Additives
- C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
-
- 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
- C10J2300/0983—Additives
- C10J2300/0996—Calcium-containing inorganic materials, e.g. lime
-
- 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
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
Definitions
- the present invention relates to a process for the production of synthesis gas by gasification of carbon-rich substances using bulk material as the reaction surface.
- a method of the aforementioned type is known from AT 387 786 B, which describes the use of a self-oxidized, circulated bulk material.
- CONFIRMATION COPY From DE 40 30 644 Al a method for producing combustible gases is known, in which a gas conversion is provided in a moving coke bed.
- a moving coke bed For the after-treatment of synthesis gases, which are produced in accordance with DE 10 2007 062 414 A1, a moving coke bed has proved unsuitable.
- Countercurrent gasifiers with a bulk reaction moving bed exhibit excellent mass transfer between the individual phases of the reactants, so that in particular also reactions between the solid phase and the gas phase allow energetically highly efficient embodiments of such gasification processes.
- the main disadvantage of countercurrent gasifiers is that the achievable maximum gas temperature at the upper gas outlet is limited by the preheating of the above introduced solids. This usually only temperatures of 400 ° C can be realized. This usually leads to the fact that the quality of the gaseous reaction products is diminished by not fully gasified oil and tar shares and also undesirable condensation of such by-products in the upper gas space and in the gas exhaust pipes occur.
- the countercurrent gasifiers are usually followed by a second gasification stage, which ensures the thermal decomposition of the oil and tar components at significantly higher temperatures, which are in some cases above 1000.degree.
- a second gasification stage which ensures the thermal decomposition of the oil and tar components at significantly higher temperatures, which are in some cases above 1000.degree.
- two-stage gasification processes are extremely expensive and usually have unsatisfactory thermal efficiencies.
- the object of the present invention is therefore to improve processes of the type described above so that the gaseous reaction products can be obtained in an energy-efficient manner as high-quality synthesis gas in high gas yield and free of oil and tar fractions.
- This object is achieved in a method of the type mentioned by the fact that the gasification in a first stage in a first vertical process space in a first from top to bottom moving column of bulk, which are added to the carbon-rich substances before entering the first vertical process space with oxygen-containing gas is carried out by Partialo idation in countercurrent and passed the resulting gaseous products in a second vertical process space, and in a second stage cocurrent with oxygen-containing gas in a second moving from top to bottom bulk column after increasing the temperature, and in the lower Part of the vertical process space, are deducted, being used as bulk material in the second column of bulk wholly or partially inert substances.
- the bulk material acts as a reaction surface on which such oil and tar-like substances form a condensation and evaporation equilibrium, whereby an extension of the average residence time of such substances in the post-gasification zone is achieved.
- the physical properties of the inert material components are retained over the entire bulk material column.
- the bulk material Because of its inert substance content, it also acts as an energy buffer and ensures an almost ideal energy distribution. This ensures a very efficient thermal decomposition of the oils and tars.
- the moving bulk material column acts as the first dust separation stage in the gasification, wherein the dust separated from the gas phase can be very easily discharged from the post-gasification together with the bulk material by the migrating bulk material column.
- the first bulk material column and / or the second bulk material column are formed from bulk material having a particle size of up to 30 cm.
- This coarse-grained bulk material ensures ideal gas permeability, energy distribution and very good mass transfer in both process chambers.
- the bulk material in the first column of bulk material and / or the second bulk material column consists wholly or partly of alkaline substances, for example of lumpy calcium oxide, and / or this alkaline substances, such as lumpy calcium oxide and particularly preferably powdered calcium oxide and / or calcium hydroxide are admixed.
- the use of calcium oxide has proved to be advantageous, since this substance has catalytic properties which promotes the thermal decomposition of oil and tar-like cracking products and at the same time acts as a pollutant binder.
- chlorine and sulfur compounds for example, chemically bound to the calcium, while heavy metals bind physically to the active upper calcium oxide ⁇ surface of the.
- an oxidation zone is formed in which the pyrolysis coke produced in the upper process zone zones is oxidized, thereby supplying the necessary energy to the process.
- this is equipped with a support firing, which is operated by burner lances with fuel and with oxidizing gas.
- the gasification takes place in the first vertical process chamber by adding air and / or technical oxygen as the oxidizing gas, the air or oxygen quantity being adjusted such that a total lambda of less than 1 is preferred over all stages of the gasification in the process space less than 0.7, and more preferably less than 0.5.
- the gasification in the vertical process space takes place in the presence of steam and calcium oxide and / or calcium carbonate and / or calcium hydroxide.
- This is a calcium-catalyzed reforming of substantial proportions of the resulting oil and / or tar-containing cleavage products having a chain length greater than C4, to carbon monoxide, carbon dioxide and hydrogen at temperatures above 400 ° C is performed.
- a temperature increase which is conducive to the post-gasification in the vertical process space is achieved via burner lances in the upper gas space and / or further down in the bulk material column, the burner lances being operated with oxygen or oxygen-containing gas.
- the temperature increase can also take place in such a way that the temperature is already reached in the vertical process chamber via Nerlanzen done in the upper gas space and / or in the transition to the upper gas space of the process space, which burner lances are operated with oxygen or oxygen-containing gas.
- the withdrawn gaseous reaction products can be cooled after filtration at least partially via a heat exchanger, and the resulting condensates are separated at temperatures below 100 ° C.
- the withdrawal of the gaseous reaction products is preferably carried out by means of a gas delivery device, which is preferably connected downstream of the heat exchanger.
- the countercurrent carburetor or the vertical process chamber is equipped at the lower end with a cooling zone, in which cooling gas is introduced from below.
- Oxygen-containing gas for example air
- syngas can also be used after cooling has taken place.
- water can additionally be used as cooling and / or gasifying agent in the cooling zone of the vertical process chamber.
- the bulk material from at least one of the two bulk solids columns is withdrawn batchwise or continuously by means of metering devices from the respective vertical process chamber.
- Preferably turntable discharge systems can be used here, which allow a uniform and continuous withdrawal of the bulk material from the process spaces.
- the withdrawn bulk material from the first and / or the second bulk material column are discharged via vertical Pitot tubes, in which by means of level controls a minimum damming height is maintained, being ensured by the pressure loss, a gas seal against the outside atmosphere.
- the bulk material from the bulk material column, after exiting the pitot tube, can be separated by physical separation methods, preferably by sieving and / or screening, into different particle fractions, and preferably the fine fraction containing bound contaminants, at least partially removed from the process.
- the resulting coarse fraction can be used at least partially as bulk material in at least one of the two vertical process spaces.
- a very efficient cycle process can be formed, whereby the additional demand for supplied fresh bulk material can be reduced to a minimum.
- the bulk material from the secondary gasification or from the second bulk material column can be cooled countercurrently by introducing synthesis gas purified by dust separation and cooling into the lower part of the vertical process chamber.
- this cooling of the second column of bulk material can also take place by indirect cooling before exiting the pitot tube by means of cooling water and / or by means of an indirectly cooled conveying section operated with cooling water after leaving the pitot tube.
- the bulk material from the second bulk material column can be separated by physical separation methods, preferably by screening and / or screening in different grain fractions, and preferably the fine fraction containing bound pollutants from the process, at least partially discharged.
- the resulting coarse fraction can be at least partially reused as bulk material in at least one of the two vertical process spaces
- the bulk material from the second bulk material column can be used at least partially directly and using the sensible heat as additional bulk material via a separate metering in the first vertical process space.
- FIG. 1 shows a preferred embodiment of the method according to the invention for the gasification of carbon-rich substances.
- a mixture of carbon-rich substances (A) is in coarse-shaped form and a grain size of less than 30 cm a first vertical process chamber (1), which is designed as a countercurrent carburetor, fed from above via a vertical Schurre (2).
- These carbon-rich substances before entering the countercurrent carburetor (1) coarse bulk material (3), for example, lumpy calcium oxide, admixed.
- alkaline substances (4) preferably fine-grained calcium oxide are added to the bulk material bed before entering the vertical process space (1).
- the mixture (5) of carbon-rich substances, lumpy calcium oxide and alkaline substances flows through the vertical process space (1) by gravity from top to bottom.
- the flow rate of the bulk material is controlled by means of a metering device (6), which is at the lower end of the first vertical process chamber (1) and can be formed, for example, as a turntable discharge system.
- This metering device conveys the bulk material into a pitot tube (7) at the lower outlet of the process chamber (1), in which the accumulated material ensures its own pressure loss for a gas seal to the atmosphere.
- the countercurrent carburettor has burner lances (8) in the central region, which provide for base load firing in the vertical process space and for the stationary formation of an oxidation zone (9). These burner lances can be operated with fossil fuels (10) and oxygen-containing gas (11). As an alternative to fossil fuels, synthesis gas from the process can also be used.
- oxygen-containing gas for example air
- This gas is used initially for cooling the bulk material before leaving the vertical process space (1) in a cooling zone (14), wherein the oxygen-containing gas is simultaneously heated to above 800 ° C, and used in the oxidation zone (9) as a gasification agent.
- introduced amount of oxygen-containing gas is adjusted so that sets a total lambda of preferably less than 0.5 in the vertical process space.
- the oxygen continues to decrease, so that finally only can take place smoldering to CO, to even all the oxygen is used up earlier and finally a reduction zone (15) is developed with a completely reductive conditions.
- the provisions in the re- production zone first a drying of the possibly moist feed materials up to a temperature of 100 ° C instead. Thereafter, the actual temperature of the materials continues to increase, so that the gasification process of the plastics contained in the carbon-rich substances, for example, also begins and at an autogenous temperature of up to 500 ° C, the formation of methane, hydrogen and CO begins.
- the intrinsic temperature of the materials continues to increase due to the hot gases rising from the oxidation zone (9), so that the carbon-rich materials are finally completely degassed and consist only of residual coke, the so-called pyrolysis coke, and ash components.
- the pyrolysis coke is transported further with the bulk material in the vertical process space (1) down to where it at temperatures above 800 ° C in the lower part of the reduction zone (15) with the C0 2 shares from the oxidation zone (9) by Boudouard conversion at least partially converted to CO. Part of the pyrolysis coke also reacts in this zone according to the water gas reaction with water vapor, which is also contained in the hot gases, to form CO and hydrogen.
- Residues of pyrolysis coke are finally oxidized in the oxidation zone (9) with the oxygen-containing gas at temperatures below 1800 ° C and used thermally.
- the bulk material moving bed together with the remaining ash portions, reaches the cooling zone (14).
- cooling zone (14) and water (16) via water lances (17) can be metered as another cooling and gasifying agent.
- the synthesis gas formed in the vertical process space is aspirated (18) at the upper end, so that a slight negative pressure is preferably established in the upper gas space (19) of the vertical process space (1).
- the extracted synthesis gas contains dust, which consists essentially of the solid salts of halogens, fine-grained alkaline substances, other pollutants and inert particles. Furthermore, the synthesis gas still contains incompletely gasified oil and tar-like organic cracking products. To completely gas these, the dust, oil and tar-containing synthesis gas in the gas space (19) of the vertical process chamber (1) or after leaving the vertical process space at
- the treatment of the synthesis gas in the presence of steam and fine-grained calcium oxide at temperatures of above 400 ° C in a downstream second vertical process chamber (20) is provided, in which the synthesis gas in DC through a moving from top to bottom
- the bulk material column (21) is guided.
- the bulk material column (21) can also be formed by coarse bulk material (22), for example lumpy calcium oxide.
- coarse bulk material (22) for example lumpy calcium oxide.
- alkaline substances (23) preferably fine-grained niges calcium oxide or calcium hydroxide of the bulk material column (21) are admixed.
- the bulk material column (21) flows through the vertical process chamber (20) by its own gravity from top to bottom.
- the flow rate of the bulk material is controlled by means of a metering device (24), which is installed at the lower end of the vertical process space (20) and can be designed, for example, as a turntable delivery system.
- This metering device conveys the bulk material into a pitot tube (25) at the lower outlet of the process chamber (20), in which the accumulated material ensures its own pressure loss for a gas seal to the atmosphere.
- the treatment of the synthesis gas may preferably be carried out by using direct firing into the synthesis gas via burner lances (26) operated with oxygen-containing gas (27).
- burner lances can be installed, for example, in the gas space (19) of the process space (1) or else in the feed line (18) to the process space (20).
- the use of such burner lances is particularly advantageous when they are installed in the gas space (28) or also further down in the area of the bulk material column (21) of the process space (20).
- the dust-containing synthesis gas (29) is then at Tem ⁇ temperatures above 300 ° C via a hot gas filtration (30) freed from dust.
- the halogen-containing filter dust (31) is discharged from the process.
- the resulting synthesis gas (32) is virtually halogen-free and is cooled by means of a gas cooler (33) and freed from condensates.
- the resulting condensate (34) can be at least partially used again as a cooling and gasifying agent over the water lances (17) in the vertical reaction space.
- the synthesis gas cooled in the gas cooler (33) is drawn off from the second process chamber (20) at (29) via gas filter (30) and gas cooler (33) by means of gas compressor (35) and then conveyed to further thermal or material utilization (12) ,
- the bulk material mixture emerging at the lower end of the first vertical reaction space (1) via the pitot tube (7) contains essentially coarse-grained bulk material, residues of ash and fine-grained calcium oxide.
- the fine sieve fraction (40) contains residues of ash, bound pollutants and fine-grained calcium oxide.
- the remaining fine fraction is discharged from the process.
- An embodiment of the method is that industrial oxygen as oxygen-containing gas at (11) inserted ⁇ is set. As a result, a particularly high-calorie synthesis gas can be generated.
- the burner lances (8) are operated so that the amount of oxygen-containing gas (11) is used more than stoichiometrically based on the fuel (10). At the same time, in this case, cold synthesis gas (41) is used as the cooling gas in the cooling zone (14).
- the synthesis gas flowing into the oxidation zone (9) from the cooling zone (14) is at least partially incinerated, forming further carbon dioxide and water vapor.
- the heat of reaction liberates the energy required for the gasification process.
- the amount of synthesis gas is adjusted in such a way that on the one hand the bulk material moving bed in the cooling zone (14) is completely cooled down and residual embers are extinguished, and on the one hand a high proportion of the necessary process energy is covered by the synthesis gas.
- the bulk material mixture emerging at the lower end of the vertical reaction space (20) via the pitot tube (25) contains essentially coarse-grained bulk material, residues of ash and fine-grained calcium oxide.
- This bulk material can be used without cooling by using its sensible heat directly at (42) as additional bulk material in the vertical process chamber (1).
- the bulk material can also be cooled by means of indirect cooling with cooling water or air.
- the fine sieve fraction (46) contains residues of ash, bound pollutants and fine-grained calcium oxide.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Industrial Gases (AREA)
Abstract
L'invention concerne un procédé permettant de produire du gaz de synthèse par gazéification de substances riches en carbone en utilisant des matières en vrac comme surface de réaction. Ladite gazéification est réalisée, selon une premier étape, dans une première chambre verticale de réaction (1) au sein d'une première colonne de matières en vrac (5) pouvant se déplacer d'en haut vers le bas, les substances riches en carbone (A) y étant ajoutées avant qu'elles n'atteignent la première chambre verticale de réaction (1), par oxydation partielle à contre-courant en mettant en œuvre un gaz contenant de l'oxygène. Afin de pouvoir récupérer les produits gazeux de la réaction d'une manière économe en énergie, avec un rendement élevé en gaz, et sous forme d'un gaz de synthèse de haute qualité lequel est exempt de constituants huileux et bitumineux, les produits gazeux obtenus selon l'invention sont introduits, au sein de la zone supérieure, dans une deuxième chambre verticale de réaction (20) pour réaliser, selon une deuxième étape, dans une colonne de matières en vrac (21) pouvant se déplacer d'en haut vers le bas, une gazéification ultérieure à co-courant en mettant en œuvre un gaz contenant de l'oxygène et en augmentant la température, puis pour soutirer lesdits produits d'une zone (29) située plus en bas de la chambre verticale de réaction (20).
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102012014161.0A DE102012014161A1 (de) | 2012-07-18 | 2012-07-18 | Gegenstrom-/Gleichstrom-Vergasung von kohlenstoffreichen Substanzen |
PCT/EP2013/002094 WO2014012651A1 (fr) | 2012-07-18 | 2013-07-15 | Gazéification à contre-courant/co-courant de substances riches en carbone |
Publications (1)
Publication Number | Publication Date |
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EP2875102A1 true EP2875102A1 (fr) | 2015-05-27 |
Family
ID=49029054
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP13752581.2A Withdrawn EP2875102A1 (fr) | 2012-07-18 | 2013-07-15 | Gazéification à contre-courant/co-courant de substances riches en carbone |
Country Status (3)
Country | Link |
---|---|
EP (1) | EP2875102A1 (fr) |
DE (1) | DE102012014161A1 (fr) |
WO (1) | WO2014012651A1 (fr) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102014012432A1 (de) * | 2014-08-26 | 2016-03-03 | Ecoloop Gmbh | Verfahren zur Spaltung von kohlen- und wasserstoffhaltigen Substanzen |
DE102017102789A1 (de) | 2017-02-13 | 2018-08-16 | Ecoloop Gmbh | Herstellung von Synthesegas aus kohlenstoffreichen Substanzen mittels eines Gleichstrom-Gegenstrom-Verfahrens |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
AT387786B (de) | 1984-03-22 | 1989-03-10 | Waagner Biro Ag | Verfahren zur vergasung von kohlenstoffhaeltigen materialien |
DE4030644A1 (de) * | 1990-09-25 | 1992-03-26 | Sanhog Technik Dr Ing Horst Ga | Verfahren zur erzeugung brennbarer gase mit anschliessender gasumwandlung in einem bewegten koksbett |
EP1373440A2 (fr) * | 2000-12-08 | 2004-01-02 | Foretop Corporation | Procede et generateur de gaz destines a la production de gaz de combustion |
JP3973840B2 (ja) * | 2001-01-18 | 2007-09-12 | 独立行政法人科学技術振興機構 | 固形燃料ガス化装置 |
GR1005536B (el) * | 2006-03-07 | 2007-06-07 | Λαμπρος Ελευσινιωτης | Διβαθμιος συνδυασμενος αεριοποιητης ομορροης -αντιρροης |
WO2008107727A2 (fr) * | 2007-03-06 | 2008-09-12 | Lampros Elefsiniotis | Gazogène à trois phases et lit fixe, qui comprend une zone tampon du courant gazeux entre la zone de pyrolyse et la zone de combustion |
DE102007062414B4 (de) | 2007-12-20 | 2009-12-24 | Ecoloop Gmbh | Autothermes Verfahren zur kontinuierlichen Vergasung von kohlenstoffreichen Substanzen |
DE102007062413B3 (de) * | 2007-12-20 | 2009-09-10 | Conera Process Solutions Gmbh | Verfahren und Vorrichtung zur Wiederaufbereitung von CO2-haltigen Abgasen |
-
2012
- 2012-07-18 DE DE102012014161.0A patent/DE102012014161A1/de not_active Ceased
-
2013
- 2013-07-15 EP EP13752581.2A patent/EP2875102A1/fr not_active Withdrawn
- 2013-07-15 WO PCT/EP2013/002094 patent/WO2014012651A1/fr active Application Filing
Non-Patent Citations (1)
Title |
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See references of WO2014012651A1 * |
Also Published As
Publication number | Publication date |
---|---|
DE102012014161A1 (de) | 2014-02-20 |
WO2014012651A1 (fr) | 2014-01-23 |
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