WO2009095581A2 - Procede de combustion de combustibles carbones avec filtration des fumees de combustion avant compression - Google Patents
Procede de combustion de combustibles carbones avec filtration des fumees de combustion avant compression Download PDFInfo
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- WO2009095581A2 WO2009095581A2 PCT/FR2009/050078 FR2009050078W WO2009095581A2 WO 2009095581 A2 WO2009095581 A2 WO 2009095581A2 FR 2009050078 W FR2009050078 W FR 2009050078W WO 2009095581 A2 WO2009095581 A2 WO 2009095581A2
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- filtration
- combustion
- combustion fumes
- fumes
- downstream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/006—Layout of treatment plant
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/38—Removing components of undefined structure
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0266—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/404—Nitrogen oxides other than dinitrogen oxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
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- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/50—Carbon dioxide
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- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2217/00—Intercepting solids
- F23J2217/10—Intercepting solids by filters
- F23J2217/103—Intercepting solids by filters ultrafine [HEPA]
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- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L2900/00—Special arrangements for supplying or treating air or oxidant for combustion; Injecting inert gas, water or steam into the combustion chamber
- F23L2900/07001—Injecting synthetic air, i.e. a combustion supporting mixture made of pure oxygen and an inert gas, e.g. nitrogen or recycled fumes
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
- F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
- F25J2260/80—Integration in an installation using carbon dioxide, e.g. for EOR, sequestration, refrigeration etc.
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/32—Direct CO2 mitigation
Definitions
- the present invention relates to a carbonaceous fuel combustion process characterized in that the combustion fumes are filtered so as to achieve a concentration of solid particles less than 1 mg / m before compression, purification and sequestration or transport.
- the thermal power plants allow by combustion of fuels to release usable heat to produce steam and possibly mechanical or electrical energy. Combustion fumes release significant amounts of CO 2 into the atmosphere.
- a technology aims to capture CO 2 emitted during the combustion of carbonaceous fuels to transport it and / or to sequester it underground.
- a portion of the combustion fumes will have to be compressed to a pressure typically of the order of 4 to 60 bar abs before being purified and then compressed again until at a pressure typically of 100 to 200 bar abs to be sequestered.
- Both the compression wheels and the inter-stage exchangers are subject to fouling by solid particles from combustion.
- the particles can clog the exchangers and reduce their thermal capacities.
- these can be unbalanced by the inhomogeneous accumulation of mass on the wheels. This leads to an imbalance of the mechanical shaft, vibrations and potentially the destruction of the machine.
- dusting any action or process in which a smoke or gas is removed by a gas / solid separation of a substantial fraction of the solids it conveys.
- the devices or equipment performing this task are called dust collectors or dust separators.
- a solution of the invention is a method of combustion of carbonaceous fuels employing a combustion unit producing combustion fumes further comprising carbon dioxide (CO 2 ), solid particles and at least one of the impurities chosen from water, nitrogen, oxygen, argon, nitrogen oxides (NOx) including nitrogen monoxide and nitrogen dioxide and sulfur oxides (SOx) including sulfur dioxide, characterized in that the following steps are carried out: a) the filtration of the combustion fumes so as to reach a solid particles concentration of less than 1 mg / m, b) the compression of the combustion fumes filtered in step a ), c) purifying the flue gases compressed in step b) so as to at least partially remove one of the impurities, and d) recovering a gas stream enriched in CO 2 .
- the flue gases are compressed in step b) at a pressure greater than 4 bar.
- the compression implemented in step b) is carried out by means of centrifugal compressors.
- step a) a concentration of solid particles of less than 500 ⁇ g / m 2 is preferably reached, more preferably less than 300 ⁇ g / m 2.
- the method according to the invention may have one of the following characteristics:
- step a) the combustion fumes are filtered so as to reach a concentration of solid particles of less than 100 ⁇ g / m 3 ,
- step a) the filtration is carried out using a cartridge filter
- step a) is carried out after a first compression of the combustion fumes
- At least one heat exchanger is used downstream of the filtration step a) and upstream of the step c),
- the combustion unit is a unit employing as air oxidant in which the capture of CO 2 is carried out by absorption of CO 2 in the flue gases; we talk about so-called capture
- the combustion unit is an oxy-combustion unit employing, as the oxidant, a nitrogen-depleted gas with respect to the air,
- step a) the filtration of step a) is completed between step a) and step c) by static filtration
- the combustion fumes leaving the static filtration have a solid particle concentration of less than 10 ⁇ g / m
- At least one exchanger chosen from plate heat exchangers, finned tube heat exchangers and brazed aluminum heat exchangers,
- plastic exchangers are used downstream of the filtration step a), for combustion fumes of temperatures below 100 ° C.
- washing towers and / or distillation columns equipped with packing are used to at least partially remove at least one of the impurities chosen from SO 2 , NO 2 and N 2 , O 2 , Ar and N 2 O 4 , a desulphurization step and / or a cooling step are used to remove the water by condensation, upstream of the filtration step a) and / or downstream of the filtration step a),
- the fumes of the oxycombustion are divided into at least two parts, a first part being recycled towards the combustion unit, and a second part undergoing stages b), c) and d), and only the second part undergoes a desulfurization step and / or a cooling step to remove water by condensation,
- the totality of the combustion fumes undergoes at least one desulfurization stage, then a first portion of the desulfurized combustion fumes are recycled to the boiler while a second part of the desulfurized combustion fumes undergoes the steps a), b), c ) and D).
- the carbonaceous fuel is coal and the first part of the combustion fumes undergoes before being sent back to the boiler a second desulphurization stage,
- the totality of the combustion fumes undergoes a first desulfurization step before the filtration step a), then a second desulfurization step after the filtration step a), before being divided into two parts, a first part of combustion fumes being recycled to the boiler, and a second part of the combustion fumes undergoing steps b), c) and d).
- the recycled portion of fumes can represent up to 80% of the combustion fumes.
- afterburner is meant a conventional combustion process in air followed by separation of CO 2 from combustion fumes, for example by absorption with amines or with ammonia.
- the desulphurization steps may for example be carried out by washing with a solution which contains limestone or sodium hydroxide.
- Filtration step a may be carried out using a cartridge filter. It is carried out at a temperature between 0 0 C and 300 0 C, preferably between 100 0 C and 200 0 C.
- Cartridge filter means filter cartridges consisting of pleated fibrous media implemented in cylindrical form. This filter technology makes it possible to offer large filtration surfaces for a small volume of space and lower generated pressure losses for the same gas flow rate to be treated. In fact, the pleating operation makes it possible to increase the filter area used in a duct of given section, and thus makes it possible to reduce the front speed of the gas at the level of the filter, thereby reducing the pressure drops.
- the cartridge filter is decoloured after filtration using a fluid rich in CO 2 or in air.
- This fluid rich in CO 2 may be from step b) and / or d).
- compact exchanger an exchanger whose compactness is greater than 700 m 2 / m 3 ; the compactness being defined by the ratio of the area of the exchange surface to the volume of the exchanger.
- the finned tube exchangers consist of tubes for improving the heat exchange coefficient.
- Plate heat exchanger means a heat exchanger with primary surface or secondary surface.
- Primary surface exchangers consist of corrugated, ribbed or pitted plates. The pattern of the plate profile can be quite varied but it always has a dual role of intensifying heat transfer and pressure resistance by multiplication of the contact points.
- Primary surface exchangers include exchangers with welded or brazed plates which enable to use these primary heat exchange surfaces at temperatures above 150 0 C. In the context of the present invention, these heat exchangers can be used, without fouling concern, due to the prior implementation of step a) filtration.
- Secondary surface exchangers use pleated or corrugated fins.
- plastic media such as, for example, PPS (Polysulfide of phenylene), polyester, PTFE (polytetrafluoroethylene). These plastics make it possible both to reach submicro filtration levels and to withstand, depending on the case, temperatures between 50 0 C and 200 0 C.
- fine filter means a filter that is class F5 to F9 in the sense of the European standard EN 779: 2002; it is for example a static filter pockets or cassettes, typically dimensions of 24 inches by 24 inches (610 mm by 610 mm).
- coarse filter is meant a filter class G1 to G4.
- the static filter according to the invention may be followed by a HEPA or ULPA filter.
- the HEPA filter is a class H10 to H14 filter and the ULPA filter is a class U15 to U17 filter in the sense of the European standards EN 1822-1: 1998, 1822-2: 1998 and 1822-3: 1998.
- the method according to the invention implements a combustion unit powered by a carbonaceous fuel.
- this fuel is coal but it can be any fuel based on carbon atoms: petroleum residues, hydrocarbons, natural gas, biomass, household waste ...
- the combustion is preferably oxycombustion, that is to say a combustion whose oxidant is a nitrogen-depleted gas with respect to air and enriched in CO 2 .
- This depletion of nitrogen is obtained by separating air into a fraction enriched with oxygen and a fraction enriched in nitrogen, for example in a cryogenic air separation unit.
- the fraction enriched with oxygen is mixed with a portion of the combustion fumes rich in recycled CO2 to form the oxidant. It usually presents a oxygen concentration higher than air.
- the oxycombustion can also be carried out with pure oxygen, that is to say undiluted with a part of the combustion fumes rich in CO2. Its content is then typically between 85% and 99.9%.
- FIG. 1 illustrates a general method according to the invention, implementing a pulverized coal boiler and operating with a poorer oxidant. nitrogen as air, characterized in that all of the combustion fumes undergo a desulfurization step.
- Air 1 is introduced into the unit 2 for separating the gases from the air, which then produces oxygen 3.
- Oxygen 3 is sent to a mixer 4 where it can be mixed via a recirculation channel.
- CO 2 to a recycle gas 6 rich in CO 2 .
- the oxidant 5 from the mixer 4 is then introduced into the pulverized coal boiler 7, which then operates on an oxidant that is poorer in nitrogen than air.
- the fuel 8, here the raw coal, is first sent to a pulverizer 10 before being introduced into the pulverized coal boiler 7.
- the combustion fumes 13 may be subjected to various treatment: removal of mercury (not shown) and nitrogen oxides 19, dedusting 14 and desulfurization and / or cooling 15.
- a first portion 6 of these oxy-fuel fumes can be recycled to the boiler so as to reduce the oxygen content at the combustion and therefore the combustion temperature.
- the non-recycled combustion fumes (second part of the combustion fumes) are in turn filtered by means of a cartridge filter 20 before being sent to the compression and purification unit 16 (CPU) CO 2 .
- the fumes Prior to step 16 of compression, the fumes can be washed 9 to remove SOx and / or NOx and / or cool by direct contact to remove some of the water by condensation.
- the purified CO 2 from the CPU 16 can then be conditioned and / or transported and / or stored.
- dedusting 14 is meant dusting by traditional techniques; for example, dedusting by means of electrostatic filters or bag filters.
- FIG. 2 illustrates a method, according to the invention, implementing a pulverized coal boiler operating with an oxidant that is lower in nitrogen than air, characterized in that all the combustion fumes undergo a first step of desulfurization. before the filtration step a) then a second desulfurization step before being divided into two parts, a first part of the combustion fumes being recycled to the boiler, and a second part of the combustion fumes undergoing the steps b), c) and d).
- This method differs from the preceding in that:
- the totality of the combustion fumes is filtered by means of a cartridge filter 20 before being sent into the scrubber 9 intended to eliminate SOx and / or NOx and / or cooled by direct contact in order to eliminate a part of it condensation water,
- a first part 6 of the combustion fumes can be recycled after the washer 9 to the boiler, and
- the non-recycled combustion fumes (second part of the combustion fumes) are in turn sent to the compression and purification unit (CPU) 16 of the CO 2 .
- CPU compression and purification unit
- Figure 3 provides a more detailed description of steps a), b), c) and d) of the method according to the invention.
- fine filtration will be used to filter the combustion fumes so as to reach a concentration of solid particles of less than 1 mg / m 2.
- the fumes of the oxycombustion 101 undergo fine filtration 103 and washing / cooling in a tower with direct contact 105. In this tower, it will be possible to eliminate
- the low pressure washing tower can be packed thanks to fine filtration. Indeed, conventional filtration would lead to fouling of the packings. It would then be necessary to clean the tower more often or to resort to trays, less subject to fouling but generating more losses.
- the cooled fumes 107 enter a first compression stage 109 before being cooled in an exchanger 111 and then in a second compression stage 113 before being cooled again in a heat exchanger 115. These heat exchangers 111 and 115 may be finned or plate or compact thanks to fine filtration.
- the pressure of the fluid 117 is typically between 4 and 60 bar abs, preferably between 15 and 35 bar abs. The number of compression stages is adapted according to the pressure.
- Each compression stage may consist of one or more centrifugal wheels (s).
- the fluid 117 then enters a high pressure washing / cooling tower 119 and is dried in an adsorber 121 and undergoes a step of adsorption demercurization in an adsorber 123.
- the high pressure washing tower can be packed by fine filtration. .
- the fluid 125 obtained then undergoes partial condensation in the exchangers 127 and 128.
- These exchangers can be brazed aluminum through fine filtration. In some cases, this fine filtration sufficient to prevent the clogging of the compressors may be insufficient for the use of such exchangers.
- the steps of drying and adsorptive demercurization can introduce solid particles into the fluid.
- Additional filtration for example by sintered metal cartridge, can be carried out on the fluid 125.
- the partially condensed fluid is separated into a CO 2 enriched liquid fraction and a vapor fraction typically enriched with N 2 , Ar, O 2 .
- the liquid fraction is expanded and enriched in CO 2 in a distillation column 137.
- a gaseous fluid 139 is removed from the column, heated in the exchanger 127 and optionally compressed in a compressor 171 and recycled upstream of the exchanger 127 of to improve CO 2 efficiency.
- a liquid fluid 141 is optionally expanded and vaporized in the exchanger 127 and then introduced into a distillation column 155 to purify it with heavy compounds such as SO 2 and NO 2 / N 2 O 4 which would not have been removed by the purification steps. preceding.
- the distillation columns can be packed thanks to the use of fine filtration.
- a liquid fraction 157 enriched with heavy compounds is extracted from this column and a fraction enriched in CO 2 is produced and compressed in a compressor 151 ready for sequestration at a pressure typically between 100 and 200 bar abs.
- the gaseous fraction 133 is heated in the exchanger 127 and expanded in one or more stages in turbines 163 having been preheated in exchangers 161 so as to recover the energy in the form of pressure. This fluid then enters the heater 165 and serves to regenerate the adsorber 121.
- the combustion method according to the invention can implement an oxy-fuel combustion unit producing oxyfuel combustion fumes comprising approximately 55% of CO 2 , 20% of H 2 O, 20% of N 2 , 5% O 2 and argon and traces of other impurities, and be characterized by the recovery in step d) of a gas stream comprising at least 90% of
- CO 2 preferably at least 95% CO 2 .
- the process according to the invention has the following advantages in particular: the use of heat exchangers more efficient than the smooth tubes, which are the only exchangers that can be used with a dust content greater than 1 mg / m 3 , better compression, a reduction in the number stop for maintenance in a given time, the use of washing towers and / or distillation columns equipped with packings instead of trays, thus generating less pressure losses and thereby improving the energy efficiency of the system , and improving the purity of the final product in solid particles, which reduces the fouling downstream equipment, including the pipeline.
Abstract
Description
Claims
Priority Applications (8)
Application Number | Priority Date | Filing Date | Title |
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JP2010543549A JP5512547B2 (ja) | 2008-01-28 | 2009-01-21 | 圧縮前の煙道ガスの濾過を伴う炭素含有燃料を燃焼させるためのプロセス |
AU2009208873A AU2009208873B2 (en) | 2008-01-28 | 2009-01-21 | Method for burning carbonated fuels with combustion smoke filtration before compression |
EP09706011.5A EP2235443B1 (fr) | 2008-01-28 | 2009-01-21 | Procédé de combustion de combustibles carbonés avec filtration des fumées de combustion avant compression |
CA2712643A CA2712643C (fr) | 2008-01-28 | 2009-01-21 | Procede de combustion de combustibles carbones avec filtration des fumees de combustion avant compression |
PL09706011T PL2235443T3 (pl) | 2008-01-28 | 2009-01-21 | Sposób spalania paliw węglowych z filtracją spalin ze spalania przed sprężaniem |
CN2009801032971A CN101925781B (zh) | 2008-01-28 | 2009-01-21 | 在压缩前进行烟气过滤的含碳燃料燃烧工艺 |
US12/864,891 US8715605B2 (en) | 2008-01-28 | 2009-01-21 | Method for burning carbonated fuels with combustion smoke filtration before compression |
ZA2010/04131A ZA201004131B (en) | 2008-01-28 | 2010-06-09 | Method for burning carbonated fuels with combustion smoke filtration before compression |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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FR0850501 | 2008-01-28 | ||
FR0850501A FR2926876B1 (fr) | 2008-01-28 | 2008-01-28 | Procede de combustion de combustibles carbones avec filtration des fumees de combustion avant compression. |
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WO2009095581A2 true WO2009095581A2 (fr) | 2009-08-06 |
WO2009095581A3 WO2009095581A3 (fr) | 2009-10-01 |
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PCT/FR2009/050078 WO2009095581A2 (fr) | 2008-01-28 | 2009-01-21 | Procede de combustion de combustibles carbones avec filtration des fumees de combustion avant compression |
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US (1) | US8715605B2 (fr) |
EP (1) | EP2235443B1 (fr) |
JP (1) | JP5512547B2 (fr) |
CN (1) | CN101925781B (fr) |
CA (1) | CA2712643C (fr) |
FR (1) | FR2926876B1 (fr) |
PL (1) | PL2235443T3 (fr) |
WO (1) | WO2009095581A2 (fr) |
ZA (1) | ZA201004131B (fr) |
Cited By (7)
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WO2011084508A2 (fr) | 2009-12-15 | 2011-07-14 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé d'obtention de dioxyde de carbone d'un mélange de gaz contenant du dioxyde de carbone |
WO2011084512A1 (fr) | 2009-12-15 | 2011-07-14 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé d'obtention de dioxyde de carbone à partir d'un mélange gazeux contenant du dioxyde de carbone |
WO2011084516A1 (fr) | 2009-12-15 | 2011-07-14 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé d'obtention de dioxyde de carbone à partir d'un mélange gazeux contenant du dioxyde de carbone au moyen d'une membrane et d'une condensation |
US20130319040A1 (en) * | 2011-02-08 | 2013-12-05 | Ihi Corporation | Exhaust gas treatment system for oxyfuel combustion device |
US9452386B1 (en) | 2015-03-04 | 2016-09-27 | L'Air Liquide Socieété Anonyme Pour L'Étude Et L'Exploitation Des Procedes Georges Claude | Hybrid membrane and adsorption-based system and process for recovering CO2 from flue gas and using combustion air for adsorbent regeneration |
US9452385B1 (en) | 2015-03-04 | 2016-09-27 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Hybrid membrane and adsorption-based system and process for recovering CO2 from flue gas and using combustion air for adsorbent regeneration |
US11397049B2 (en) | 2010-07-02 | 2022-07-26 | Union Engineering A/S | High pressure recovery of carbon dioxide from a fermentation process |
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Cited By (12)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2011084508A2 (fr) | 2009-12-15 | 2011-07-14 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé d'obtention de dioxyde de carbone d'un mélange de gaz contenant du dioxyde de carbone |
WO2011084512A1 (fr) | 2009-12-15 | 2011-07-14 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé d'obtention de dioxyde de carbone à partir d'un mélange gazeux contenant du dioxyde de carbone |
WO2011084516A1 (fr) | 2009-12-15 | 2011-07-14 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé d'obtention de dioxyde de carbone à partir d'un mélange gazeux contenant du dioxyde de carbone au moyen d'une membrane et d'une condensation |
US8663364B2 (en) | 2009-12-15 | 2014-03-04 | L'Air Liquide, Société Anonyme pour l'Étude et l'Éxploitation des Procédés Georges Claude | Method of obtaining carbon dioxide from carbon dioxide-containing gas mixture |
US8734569B2 (en) | 2009-12-15 | 2014-05-27 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method of obtaining carbon dioxide from carbon dioxide-containing gas mixture |
US9446347B2 (en) | 2009-12-15 | 2016-09-20 | L'Air Liquide Société Anonyme Pour L'Étude Et L'Exploitation Des Procedes Georges Claude | Method of obtaining carbon dioxide from a carbon dioxide-containing gas mixture |
EP3395428A2 (fr) | 2009-12-15 | 2018-10-31 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé d'obtention de dioxyde de carbone à partir d'un mélange gazeux contenant du dioxyde de carbone |
US11397049B2 (en) | 2010-07-02 | 2022-07-26 | Union Engineering A/S | High pressure recovery of carbon dioxide from a fermentation process |
US20130319040A1 (en) * | 2011-02-08 | 2013-12-05 | Ihi Corporation | Exhaust gas treatment system for oxyfuel combustion device |
US9273900B2 (en) * | 2011-02-08 | 2016-03-01 | Ihi Corporation | Exhaust gas treatment system for oxyfuel combustion device |
US9452386B1 (en) | 2015-03-04 | 2016-09-27 | L'Air Liquide Socieété Anonyme Pour L'Étude Et L'Exploitation Des Procedes Georges Claude | Hybrid membrane and adsorption-based system and process for recovering CO2 from flue gas and using combustion air for adsorbent regeneration |
US9452385B1 (en) | 2015-03-04 | 2016-09-27 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Hybrid membrane and adsorption-based system and process for recovering CO2 from flue gas and using combustion air for adsorbent regeneration |
Also Published As
Publication number | Publication date |
---|---|
PL2235443T3 (pl) | 2019-03-29 |
CN101925781A (zh) | 2010-12-22 |
EP2235443A2 (fr) | 2010-10-06 |
JP5512547B2 (ja) | 2014-06-04 |
FR2926876A1 (fr) | 2009-07-31 |
AU2009208873A1 (en) | 2009-08-06 |
US20100322843A1 (en) | 2010-12-23 |
US8715605B2 (en) | 2014-05-06 |
CA2712643A1 (fr) | 2009-08-06 |
ZA201004131B (en) | 2011-04-28 |
JP2011514959A (ja) | 2011-05-12 |
EP2235443B1 (fr) | 2018-10-24 |
FR2926876B1 (fr) | 2010-03-05 |
CN101925781B (zh) | 2013-12-18 |
WO2009095581A3 (fr) | 2009-10-01 |
CA2712643C (fr) | 2016-03-15 |
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