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WO2011112069A1 - Procédé de capture et de fixation du dioxyde de carbone et appareil destiné à réaliser ledit procédé - Google Patents

Procédé de capture et de fixation du dioxyde de carbone et appareil destiné à réaliser ledit procédé Download PDF

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Publication number
WO2011112069A1
WO2011112069A1 PCT/MY2010/000214 MY2010000214W WO2011112069A1 WO 2011112069 A1 WO2011112069 A1 WO 2011112069A1 MY 2010000214 W MY2010000214 W MY 2010000214W WO 2011112069 A1 WO2011112069 A1 WO 2011112069A1
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Prior art keywords
carbon dioxide
sodium
water
yielding
column
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Ceased
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PCT/MY2010/000214
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English (en)
Inventor
Mohd Roslee Othman
Martunus
W. James Noel Fernando
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Universiti Sains Malaysia (USM)
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Universiti Sains Malaysia (USM)
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Priority to CH00023/12A priority Critical patent/CH703745B1/de
Publication of WO2011112069A1 publication Critical patent/WO2011112069A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/60—Preparation of carbonates or bicarbonates in general
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C01D7/12—Preparation of carbonates from bicarbonates or bicarbonate-containing product
    • C01D7/123—Preparation of carbonates from bicarbonates or bicarbonate-containing product by thermal decomposition of solids in the absence of a liquid medium
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C01D7/12—Preparation of carbonates from bicarbonates or bicarbonate-containing product
    • C01D7/126—Multi-step processes, e.g. from trona to soda ash
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/304—Alkali metal compounds of sodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/604—Hydroxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/112—Metals or metal compounds not provided for in B01D2253/104 or B01D2253/106
    • B01D2253/1124—Metal oxides
    • 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
    • B01D53/02—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 by adsorption, e.g. preparative gas chromatography
    • B01D53/04—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 by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • 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
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • the present invention relates to a method for capturing and fixing C0 2 from flue gas and to an apparatus for carrying out this method.
  • Carbon dioxide is a greenhouse gas that is claimed to contribute to global warming as a result of the increase of the gas content in the atmosphere. It is usually released into the air together with the other exhaust gases from the combustion of fossil fuels in coal fired power plants and other plants.
  • the emission of C0 2 is reportedly high and the treatment or capture of this gas using traditional methods is considered very costly and complicated. Even if C0 2 is successfully captured, the gas needs to be injected underground for permanent storage. This solution is clearly cost ineffective and not sustainable.
  • U.S. Pat. No. US 6,245, 127 discloses the use of an adsorption process and apparatus for carbon dioxide adsorption.
  • the adsorbent system consists of zeolite NaY supported on alumina.
  • the feed gas is fed to adsorption column at a pressure of 1.05 bar and at a temperature of 27 °C (low temperature).
  • This process incurs: pressurization, adsorption, depressurization from 1.05 bar to 0.06 bar, evacuation and purging.
  • the process produces 80 % product purity at a recovery of 66 %. Recovery is defined herein as fraction of C0 2 in the feed that is recovered as product.
  • WO 2009/139813 dicloses the use of an absorption column system for C0 2 capture that is accomplished by reacting carbon dioxide in flue gas with an alkali metal carbonate, or a metal oxide, particularly containing an alkaline earth metal or iron, to form a carbonate salt.
  • a preferred carbonate for C0 2 capture is a dilute aqueous solution of additive-free Na 2 C0 3 .
  • Other carbonates include 2 C0 3 or other metal ions that can produce both a carbonate and a bicarbonate salt.
  • suitable metal oxides include several alkaline earths including CaO and MgO.
  • the captured C0 2 is preferrably sequestered using any available mineral or industrial waste that contains calcium magnesium or iron in non-carbonate forms, or iron in the Fe +2 oxidation state.
  • the disadvantages of the prior art are: (a) It is not effective/economical and not flexible because the prior art requires complicated and costly equipment for C0 2 permanent storage, (b) It consumes high energy because the process is not adsorption but absorption, (c) It introduces and makes use of corrosive, degradable and volatile chemicals, (d) It requires a new backpressure steam generator, C0 2 scrubber and C0 2 compressor/dryer. In order to operate the C0 2 scrubber and compressor, additional energy of approximately 30% of the power plant output is needed, and (e) The noticeable weakness of the prior art is that, the preparation of initial CaO and/or MgO liberates C0 2 , thus defeating the purpose of C0 2 abatement.
  • U.S. Pat. Appl. No. US 2005/304,356 dicloses the use of an apparatus for reducing the amount of carbon dioxide released into the atmosphere through fixation by dumping carbon dioxide in seawater or fresh water. At certain temperature and pressure conditions carbon dioxide hydrate or its clathrate is formed. Carbon dioxide is pumped into the pipeline and is discharged by the compressor into the reacting housing from the ejector nozzles under pressure to form carbon dioxide hydrate or its clathrate; the thus produced hydrate or its clathrate is dispersed by the propeller out of the reaction housing to the deep bottom of the sea.
  • a preferred embodiment of the present invention relates to a method for capturing and fixing carbon dioxide, particularly from flue gas from power plants, the method comprising capturing carbon dioxide using a pressure swing adsorption (PSA) unit, containing an adsorbent; reacting the captured carbon dioxide with sodium chloride and ammonium hydroxide, yielding ammonium chloride and precipitating sodium hydrogen carbonate; calcinating said sodium hydrogen carbonate, yielding sodium carbonate, water and excess carbon dioxide; reacting said ammonium chloride with sodium hydroxide yielding sodium chloride, water and ammonia; reacting said ammonia with water yielding ammonium hydroxide.
  • PSA pressure swing adsorption
  • the adsorbent in the pressure swing adsorption (PSA) unit contains hydrotalcite potassium-sodium or modified intercalated adsorbents containing or resembling hydrotalcites or their structures or combination of hydrotalcite with other adsorbents by means of doping, impregnation,coating, juxtapositioning or other means.
  • the presenst invention discloses an apparatus for carrying out the above methods , characterized in that it comprises a continuous stirred tank reactor (1 ), a separation means (2) connected with the reactor (1 ), a calciner (3) connected with the separation means (2), a stripper column (4) connected with the separation means (2) and a scrubber column (5) connected with the stripper column (4) and in that the outlets of the stripper column (4) and the scrubber column (5) are preferabl connected with a stirred tank (6) which supplies reagents to the reactor.
  • Fig. l represents a schematic complete view of C0 2 -capture and fixation unit placement within a power plant.
  • Fig. 2 shows schematically the pressure swing adsorption (PSA) unit for capturing C0 2 .
  • PSA pressure swing adsorption
  • Fig. 3 shows schematically the C0 2 fixation unit.
  • Fig. 4 shows desorption percentage as a function of purge gas amount.
  • Fig. 5 shows the effect of purge to feed ratio on C0 2 product purity .
  • Fig. 6 shows C0 2 reacted as a function of agitation speed.
  • Fig. 7 shows the performance of stripper column as a function of its length.
  • Fig. 8. shows the schematic flow of total material balance in the fixation unit.
  • Fig. 9 shows eflluent mole fraction profiles of the adsorber at adsorption step.
  • Fig. 10 shows molar flow rate of gases at the outlet of the column.
  • Fig. 1 1 shows C0 2 concentration profiles at the end of each step.
  • the present invention objectives are to capture C0 2 from flue gas of coal fired power plant and send it to a converter (fixation) unit to convert it into soda ash by reacting the C0 2 with the ammoniated brine in a continuous stirred tank reactor (CSTR).
  • the temperature of flue gas is in the range of 400 to 600 °C (high temperature) and it contains about 15 % (molar %) C0 2 , 10 % (molar %) water vapor and 75 % (molar %) N 2 .
  • the heat from the flue gas is recuperated during fixation. All the by products can be re-used into the system, making the system highly economical and greener. No prior art suggests a technical solution having all these features.
  • the present invention provides a method for capturing and fixing carbon dioxide, particularly from flue gas from power plants, said method comprising the steps of a) capturing carbon dioxide using a pressure swing adsorption (PSA) unit, containing an adsorbent;
  • PSA pressure swing adsorption
  • step b) calcinating said sodium hydrogen carbonate, yielding sodium carbonate, water and excess carbon dioxide, which can be re-used in step b);
  • step b) reacting said ammonium chloride with sodium hydroxide yielding sodium chloride, water and ammonia, wherein sodium chloride and water can be re-used to prepare the reaction mixture of step b);
  • the process can make use of steam for purging and regenerating the adsorbents, so that the process is more economic than prior arts.
  • the process also interconnects to the fixation unit for ease of C0 2 conversion into soda ash.
  • the adsorbent in the pressure swing adsorption (PSA) unit contains (but not limited to) hydrotalcite potassium-sodium or modified intercalated adsorbents containing or resembling hydrotalcites or their structures or combination of hydrotalcite with other adsorbents known to those of skill in the art such zeolites by way of doping, impregnation, coating, juxtapositioning or other means.
  • the present invention further provides an apparatus for carrying out the method of fixing carbon dioxide, which comprises a continuous stirred tank reactor (CSTR) in which the reaction of carbon dioxide, sodium chloride and ammonium hydroxide takes place, preferably at temperature of about 30 °C to produce sodium bicarbonate (sodium hydrogen carbonate), ammonium chloride and water.
  • CSTR continuous stirred tank reactor
  • the solid sodium bicarbonate can be separated from the mother liquor using any separation means known to those of skill in the art, such as rotary filter.
  • the solution is sent to rotary filter for sodium bicarbonate separation.
  • the rotary filter preferably operates at a temperature of about 30 °C and vacuum pressure.
  • the solid sodium bicarbonate is fed to calciner.
  • the remaining solution is sent to stripper column for ammonia recovery.
  • the calciner is preferably operated at a temperature of about 180° C and at a pressure of about 1 atm.
  • the heater for calciner is supplied from the heat of the flue gas.
  • the sodium bicarbonate forms sodium carbonate, carbon dioxide and water vapor.
  • the solution from the separation means preferably rotary filter, is fed to stripper column on the top column, stripping the ammonium hydroxide to form ammonia, hydrogen ion, hydroxide ion and chloride ion and, then, reacting the sodium hydroxide (inlet from the top column) with chloride ion to form sodium chloride.
  • Sodium chloride and water formed are sent back to CSTR.
  • the stripper preferably operates at a temperature of 100°C and at a pressure 1 atm.
  • ammonia from stripper column is fed to scrubber column and reacts with water to form ammonium hydroxide, preferably at a temperature of about 30 °C and at a pressure of about 1 atm.
  • the ammonium hydroxide is re-used as feed in CSTR.
  • PSA for C0 2 is based on the preferential or selective adsorption of the gas on a microporous-mesoporous solid adsorbent (such as, but not limited to, hydrotalcite potassium -sodium or modified intercalated adsorbents having or resembling those of hydrotalcites or their structures) at a relatively high pressure by contacting the gas with the solid in a packed column of the adsorbent in order to produce a gas stream enriched in the less strongly adsorbed components of the feed gas.
  • the adsorbed components are then desorbed from the solid by lowering their superincumbent gas-phase partial pressures inside the column so that the adsorbent can be re-used.
  • the desorbed gases are enriched in the more strongly adsorbed components of the feed gas.
  • No external heat is generally used for desorption.
  • a PSA process carries out the adsorption step at a superambient pressure, and the desorption is achieved at a near-ambient pressure level.
  • a PSA unit is based on the fact that adsorbents can be easily regenerated by a pressure change.
  • the more adsorbable components (C0 2 ) are removed from a gas mixture by adsorption at high pressures, PH.
  • the adsorbed species are desorbed using low pressures, Pi. Two Packed-bed adsorbers are used.
  • Each bed undergoes a cyclic operation involving four stages: (1 ) The first stage is pressurization (with feed) to a pressure of P H , fed in at a constant flow rate, Fpress, and for a time, t press . (2) The second stage is adsorption of the more adsorbable components (C0 2 ), from a mixture (flue gas of power generation as a feed) fed in at a constant pressure of PH, at a constant flow rate, Ff ee( j, and for a time, t a ds- A raffinate stream richer in the less adsorbable components is produced and, then, goes to gas stack .
  • the third stage is depressurization (reducing the pressure from P H to PL) using purge with a steam stream at a lower inlet pressure, flowing in at a constant rate, Fpu rge , for a time, t purg e.
  • the gas coming out of the purge stage goes as waste (gas stack).
  • the fourth stage is blowdown with no inlet stream, but with a constant outlet flow rate, F Wow , of the extract (C0 2 product) for a time, tbiow
  • the present invention proposes a method for capturing and fixing carbon dioxide in its entirety.
  • the only end product will be commercially attractive that can generate economy. There are 2 main steps to this method:
  • PSA pressure swing adsorption
  • Soda ash is required in many industrial processes, such as glass industry, wherein it is used in the manufacturing of flat and container glass. Acting as a network modifier or fluxing agent, it allows lowering the melting temperature of sand and therefore reduces the energy consumption. Further, soda ash may be used in detergent industry, in a large number of prepared domestic products: soaps, scouring powders, soaking and washing powders containing varying proportions of sodium carbonate, where the soda ash acts primarily as a builder or water softener. Soda ash is also used in steel industry, where it is used as a flux, a desulfurizer, dephosphorizer and denitrider.
  • soda ash may be used, e.g., for treatment of uranium ores, oxidizing calcination of chrome ore, lead recycling from discarded batteries, recycling of zinc, aluminium. And finally, soda ash is used in a large number of industrial chemical reactions to produce organic or inorganic compounds used in very different applications. Soda ash also finds use in electrolysis, water softeners, anti-mold agents, wetting and bonding agents, food additives and stabilizers, etc. Sodium chloride finds many uses as food additive and is important in the manufacture of medicaments. Ammonia finds its uses as fertilizer, cleaner and fuels.
  • the process of the present invention is effective and flexible, it can effectively replace the need for C0 2 injection into subsurface/seawater reservoir for permanent storage that requires complicated and costly equipment. Thanks to the fact that the process of the present invention converts carbon dioxide into commercially usable products such as sodium carbonate (soda ash), it is economically advantageous.
  • the process according to the present invention is also sustainable, because the recovery of ammonia does not use calcium chloride in stripper column. So that there are no cost for the environmentally safe disposal of this calcium chloride. Moreover, the regulation of storage and disposal of calcium chloride could be neglected. The process achieves almost a complete loop, making it sustainable.
  • Fig. 1 shows a diagram showing the entire structure, including the location at which all the important units are placed.
  • PSA pressure swing adsorption
  • Example 1 The PSA unit for capturing C0 2 as shown in Fig. 2 contains a steam tank _ ⁇ with a gas pump ⁇ 2, a gas pump 13. for flue gas inlet, two adsorbent beds 14, 15, a cooler 16, cooled by water from a water tank 17 pumped by a water pump J_8.
  • Figure 2 The process described herein ( Figure 2) is from a bench scale unit using adsorption column packed type with 3 mm of hydrotalcite potasium-sodium modified adsorbent pellet (particle) diameter and 814 kg/m 3 of bulk density of the adsorbent bed.
  • the C0 2 adsorption capacity of adsorbent is 0.84 mol/kg at the temperature of 300 °C.
  • the adsorption column diameter is 2.2 cm and its length is 25 cm.
  • the adsorption column is initially pressurized with feed at the flow rate of 0.568 L/min, at the pressure of 4 bar and at the temperature of 300 °C for 25 minutes.
  • a feed gas containing 15% (v/v) C0 2 , 10% (v/v) water vapor and 75% (v/v) N 2 at the pressure of 4 bar and at the temperature of 302 °C is introduced into the column for 40 minutes.
  • the column is then co-currently depressurized from 4 bar to 1.1 bar purged with steam at a purge to feed ratio of 1.6 and at a pressure of 1.1 bar utilizing a gas pump for 40 minutes.
  • the adsorption column is then evacuated (blowdown) co-currently for 25 minutes, thus yielding a C0 2 product in excess of 99.9% (v/v) purity with 0.1 %.
  • (v/v) water vapor as impurity is then evacuated (blowdown) co-currently for 25 minutes, thus yielding a C0 2 product in excess of 99.9% (v/v) purity with 0.1 %.
  • Fig. 4 shows desorption percentage as function of purge gas amount at desorption step; 300 °C, 1.1 bar.
  • Fig. 5 shows the effect of purge to feed ratio on C0 2 product purity.
  • the purge step in PSA is actually the desorption step that a fraction of the product stream is withdrawn to purge the bed and expended to a low pressure (1.1 bar and 300 °C). As the purge volume increases, purging becomes more effective (optimum at the purge to feed ratio of 1.6).
  • Example 2
  • the details of the C0 2 fixation unit are shown schematically in Fig. 3.
  • the present invention provides a carbonation process using a continuous stirred tank reactor (CSTR) 1 as shown in Fig. 3.
  • CSTR continuous stirred tank reactor
  • This reactor JL carbon dioxide reacts with ammonium hydroxide and sodium chloride to form sodium bicarbonate, ammonium chloride and water.
  • the reaction is carried out at the temperature of 30 °C, the pressure of 1 atm and agitation speed of 150 rpm.
  • Carbon dioxide is fed into the reactor at the pressure of 1.2 atm.
  • the reaction is as follows:
  • the reactor gives conversion of 85%, higher than the carbonator of the prior art at 70%.
  • the solid sodium bicarbonate can be separated using any method known to those of skill in the art such as rotary filter 2.
  • the solution is sent to rotary filter 2 for sodium bicarbonate separation.
  • the rotary filter 2 operates at a temperature of 30° C and at a vacuum pressure.
  • the solid sodium bicarbonate is fed to calciner 3.
  • the remaining solution is sent to stripper column 4 for ammonia recovery.
  • the calciner 3 operates at 180 °C and 1 atm.
  • the sodium bicarbonate forms sodium carbonate, carbon dioxide and water vapor as shown in reaction below:
  • ammonium hydroxide/chloride is stripped into ammonia, hydrogen ion, hydroxide ion and chloride ion and, then, reacting the sodium hydroxide (inlet from the top column) with chloride ion to form sodium chloride at 100 °C and 1 atm,
  • ammonia from stripper column 4 is fed to scrubber column 5 and reacted with water to form ammonium hydroxide at 30 °C and 1 atm.
  • the ammonium hydroxide is used as feed to the CSTR 1.
  • the reaction in scrubber column 5 is given by,
  • ammoniated brine for feeding into CSTR 1 is prepared in ammoniated brine stirred tank 6. Further, in the system are coolers 7, compressor 8 , KO drum 9 and heater 10.
  • Fig. 6 shows the conversion of C0 2 as function of agitation speed of 85% to form sodium bicarbonate at 30° C and 1 atm.
  • Fig. 7 shows the performance of stripper column at 100 °C and 1 atm. Reaction of ammonium chloride with sodium chloride and stripping of ammonium hydroxide are obtained at 100% conversion.
  • Fig. 8. shows the schematic flow of total material balance for system as described in Fig. 3.
  • (v/v) water vapor is fed to this system.
  • Fig. 1 1 shows carbon dioxide concentration profiles inside the column at the end of each step in cyclic steady state: si. pressurization; s2. feed; s3. counter-current blowdown; s4. purge for Example 4 .
  • Example 3 shows carbon dioxide concentration profiles inside the column at the end of each step in cyclic steady state: si. pressurization; s2. feed; s3. counter-current blowdown; s4. purge for Example 4 .
  • This example relates to low temperature application of the invention for separation of carbon dioxide from natural gas (methane).
  • the low quality of natural gas is due to some contaminants like nitrogen and corrosive carbon dioxide.
  • the low-quality gas has to be upgraded according to grade specifications: 4% for nitrogen and 2% for carbon dioxide.
  • the composition of natural gas as a feed composed of 70% methane, 20% carbon dioxide and 10% nitrogen.
  • the PSA utilizes adsorption column (diameter of 2.2 cm and length of 25 cm).
  • the adsorption column is packed with hydrotalcite doped on zeolite adsorbent pellet (3 mm diameter particle) having 792 kg/m 3 of bulk density of the adsorbent bed.
  • the C0 2 adsorption capacity of the adsorbent is 3.63 mol/kg at 30° C.
  • the adsorption column is initially pressurized with feed flow rate of 3.34 L/min, at 1.2 bar and 30° C for 10 minutes.
  • a feed gas containing 20% (v/v) C0 2 , 70% (v/v) methane and 10% (v/v) N 2 at 2 bar and 30° C is introduced into the column for 15 minutes during adsorption.
  • the column is then counter currently evacuated (blowdown) from 2 bars to 0.2 bar for 10 minutes utilizing a gas pump connected to yiel C0 2 product in excess of 91.3% (v/v) purity by nitrogen contamination.
  • the adsorption column is then purged co-currently for 15 minutes using pure methane at a purge to feed ratio of 0.75, at 30° C and 0.2 bar. Results of from this operation are shown in Figure 9 and 10.
  • the C0 2 containing N 2 may need to be treated using PSA again until it is free from N 2 before C0 2 can be sent to fixation unit for Na 2 C0 3 conversion.
  • the following example demonstrates the applicability of the system to remove C0 2 from natural gas at low temperature operation using commercial zeolite 13X adsorbent packed in 2.2 cm diameter, 25 cm length column.
  • the bulk density of the adsorbent adsorption is 758 kg/m 3 and the C0 2 adsorption capacity of the adsorbent is 4.5 mol/kg at the temperature of 30° C.
  • the adsorption column is initially pressurized with feed flow rate of 3.47 L/min, at 1.2 bars and 30° C for 5 minutes.
  • a feed gas containing 20% (v/v) C0 2 , 70% (v/v) methane and 10% (v/v) N at 1.2 bar and 30° C is introduced into the column for 8 minutes during adsorption.
  • the column is then counter currently evacuated (blowdown) from 1.2 bars to 0.1 bar for 5 minutes utilizing a gas pump connected to ejector to yiel C0 2 product in excess of 92.5% (v/v) purity by nitrogen contamination.
  • the adsorption column is then purged co-currently using pure methane for 8 minutes at a purge to feed ratio of 0.4, temperature of 30° C and pressure of 0.1 bar.
  • the carbon dioxide concentration profiles inside the column at the end of each step in cyclic steady state; si . pressurization; s2. feed; s3. counter-current blowdown; s4. purge; is shown in Figure 1 1.

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Abstract

La présente invention concerne un procédé de capture et de fixation du dioxyde de carbone, en particulier à partir (mais non limité à) de gaz de combustion provenant de centrales électriques, ledit procédé comprenant les étapes consistant à capturer le dioxyde de carbone provenant des gaz de combustion en utilisant une unité d'adsorption modulée en pression (PSA), contenant un adsorbant ; faire réagir le dioxyde de carbone capturé avec du chlorure de sodium et de l'hydroxyde d'ammonium, afin d'obtenir du chlorure d'ammonium, et faire précipiter l'hydrogénocarbonate de sodium ; calciner ledit hydrogénocarbonate de sodium, afin d'obtenir du carbonate de sodium, de l'eau et du dioxyde de carbone en excès ; faire réagir ledit chlorure d'ammonium avec de l'hydroxyde de sodium afin d'obtenir du chlorure de sodium, de l'eau et de l'ammoniac ; faire réagir ledit ammoniac avec de l'eau afin d'obtenir de l'hydroxyde d'ammonium. L'invention concerne en outre un appareil destiné à réaliser ledit procédé.
PCT/MY2010/000214 2010-03-09 2010-10-21 Procédé de capture et de fixation du dioxyde de carbone et appareil destiné à réaliser ledit procédé Ceased WO2011112069A1 (fr)

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EP2614877A1 (fr) * 2012-01-13 2013-07-17 Alstom Technology Ltd Procédé et système de capture à faible émission de CO2
EP2910295A1 (fr) * 2014-02-25 2015-08-26 Alstom Technology Ltd Arrangement et procédé de traitement de gaz de fumée intégré et production de carbonate de sodium
FR3030477A1 (fr) * 2014-12-22 2016-06-24 Solvay Procede de production de carbonate/ bicarbonate de sodium
WO2017001690A1 (fr) 2015-07-02 2017-01-05 Solvay Sa Procédé permettant la production de carbonate/bicarbonate de sodium
EP3363523A1 (fr) 2017-02-21 2018-08-22 CIECH R&D Sp. z o.o. Procédé permettant de limiter les émissions de co2 dans des procédés de soude
WO2022219134A1 (fr) * 2021-04-15 2022-10-20 Unilever Ip Holdings B.V. Composition pour le lavage de la vaisselle à la main

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WO2003068685A1 (fr) * 2002-02-15 2003-08-21 Kebmar As Procede et dispositif permettant de dessaler de l'eau et de supprimer le dioxyde de carbone present dans des gaz d'echappement
EP1958683A2 (fr) * 2007-01-11 2008-08-20 Silicon Fire AG Procédé destiné au traitement de gaz de fumée pour centrales et autres installations

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US5917136A (en) * 1995-10-04 1999-06-29 Air Products And Chemicals, Inc. Carbon dioxide pressure swing adsorption process using modified alumina adsorbents
WO2003068685A1 (fr) * 2002-02-15 2003-08-21 Kebmar As Procede et dispositif permettant de dessaler de l'eau et de supprimer le dioxyde de carbone present dans des gaz d'echappement
EP1958683A2 (fr) * 2007-01-11 2008-08-20 Silicon Fire AG Procédé destiné au traitement de gaz de fumée pour centrales et autres installations

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2614877A1 (fr) * 2012-01-13 2013-07-17 Alstom Technology Ltd Procédé et système de capture à faible émission de CO2
WO2013105070A1 (fr) * 2012-01-13 2013-07-18 Alstom Technology Ltd Procédé et système pour la capture de co2 à faible taux d'émission
EP2910295A1 (fr) * 2014-02-25 2015-08-26 Alstom Technology Ltd Arrangement et procédé de traitement de gaz de fumée intégré et production de carbonate de sodium
FR3030477A1 (fr) * 2014-12-22 2016-06-24 Solvay Procede de production de carbonate/ bicarbonate de sodium
WO2016102568A1 (fr) * 2014-12-22 2016-06-30 Solvay Sa Procédé permettant la production de carbonate de sodium/bicarbonate de sodium
EP3733263A1 (fr) * 2014-12-22 2020-11-04 Solvay SA Procédé de production de carbonate/bicarbonate de sodium
WO2017001690A1 (fr) 2015-07-02 2017-01-05 Solvay Sa Procédé permettant la production de carbonate/bicarbonate de sodium
EP3363523A1 (fr) 2017-02-21 2018-08-22 CIECH R&D Sp. z o.o. Procédé permettant de limiter les émissions de co2 dans des procédés de soude
WO2022219134A1 (fr) * 2021-04-15 2022-10-20 Unilever Ip Holdings B.V. Composition pour le lavage de la vaisselle à la main

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MY170412A (en) 2019-07-27

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