WO2008110609A2 - Procédé de traitement de gaz de fumées dans des centrales et autres installations - Google Patents

Procédé de traitement de gaz de fumées dans des centrales et autres installations Download PDF

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Publication number
WO2008110609A2
WO2008110609A2 PCT/EP2008/053025 EP2008053025W WO2008110609A2 WO 2008110609 A2 WO2008110609 A2 WO 2008110609A2 EP 2008053025 W EP2008053025 W EP 2008053025W WO 2008110609 A2 WO2008110609 A2 WO 2008110609A2
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WO
WIPO (PCT)
Prior art keywords
alkali
plant
flue gas
reactor
gas
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Application number
PCT/EP2008/053025
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German (de)
English (en)
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WO2008110609A3 (fr
Inventor
Florian Krass
Ingo Krossing
Günther STEINFELD
Original Assignee
Silicon Fire Ag
Albert-Ludwigs-Universität Freiburg
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Priority claimed from EP07104246A external-priority patent/EP1961479A3/fr
Priority claimed from EP07113903A external-priority patent/EP1958683A3/fr
Priority claimed from PCT/EP2008/051097 external-priority patent/WO2008110405A2/fr
Application filed by Silicon Fire Ag, Albert-Ludwigs-Universität Freiburg filed Critical Silicon Fire Ag
Priority to EP08717769A priority Critical patent/EP2132280A2/fr
Publication of WO2008110609A2 publication Critical patent/WO2008110609A2/fr
Publication of WO2008110609A3 publication Critical patent/WO2008110609A3/fr

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    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/34—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis
    • 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
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • 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
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • 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
    • 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

  • Patent Application EP 07 113 903.4 filed with the EPO on 7 August 2007 and Patent Application PCT / EP2008 / 051097, filed on 1 February 2008 with the EPO.
  • the present application relates to the flue gas cleaning of power plants and other facilities.
  • one sub-process involves the binding of gaseous CO 2 .
  • Carbon dioxide (usually called carbon dioxide) is a chemical compound of carbon and oxygen. Carbon dioxide is a colorless and odorless gas. It is a natural constituent of the air at a low concentration and is produced in living beings during cellular respiration, but also in the combustion of carbonaceous substances under sufficient oxygen. Since the beginning of industrialization, the CO 2 share in the atmosphere has increased significantly. The main reason for this is man-made - the so-called anthropogenic - C0 2 emissions. The carbon dioxide in the atmosphere absorbs part of the heat radiation. This property makes carbon dioxide a so-called greenhouse gas and is one of the contributors to the greenhouse effect.
  • the aim of this project is the development of a simple and cost-effective process for the separation of CO 2 as almost pure electricity from the exhaust gas of a power plant using a sodium-based, solid sorbent.
  • Another disadvantage is that energy is the biggest cost factor in extracting drinking water from salty seawater. If the plant is connected to a conventional power plant for energy production, the required energy can be supplied by the power plant. Unfortunately, the power plant produces environmentally harmful substances, such as CO 2 , which enter the air with the flue gas.
  • the flue gases from power plants and other (industrial) plants, as well as heaters or incinerators often also contain considerable amounts of sulfur or sulfur compounds, nitrogen or nitrogen compounds (eg NOx), and possibly also hydrocarbons, for example can be harmful to your health. There may also be other (harmful) substances in the flue gases.
  • Soda Na 2 CO 3
  • Soda is used in many other areas besides glass production (with silicon dioxide) and is an important raw material. It is used for the production of detergents, soaps and food as well as for dyeing and bleaching. However, soda is also found in paints, catalysts, pesticides and fertilizers, in cellulose or other substances, and in the reduction of alumina and silica.
  • FIG. 4 A corresponding first method of the applicant is described in the priority applications mentioned above.
  • a corresponding schematic illustration of the basic principle is shown in FIG. 4.
  • An ammonia brine is introduced into which CO 2 is introduced.
  • ammonium chloride (NH 4 Cl) is released.
  • this first method may possibly have certain disadvantages.
  • An important point is ammonia recycling.
  • Ammonia recycling is best done using a base.
  • the cheapest available base is lime (CaO), which makes the process more complex and expensive.
  • lime is extracted by the burning of calcium carbonate (CaCO 3 ) and can fix only as much CO 2 as previously released from this rock. All procedures for base preparation are with a CO 2 - Output connected and / or show high energy consumption. Naturally occurring, degradable bases do not exist.
  • the methods and corresponding devices are to be designed to find wide acceptance by using materials that can be recycled as much as possible, or that can be used in various stages of the process sub-processes and that have a commercial value. This should enable a technical implementation on a broad basis.
  • the CO 2 released by the use of fossil fuels is retained (preferably in a solid), respectively bound, and stored long-term in a medium other than the atmosphere.
  • a method according to the invention has been developed which is particularly economical due to the consciously planned use of raw materials and the provision of reusable products.
  • the other (harmful) substances that are contained in the flue gas are bound.
  • Fig. 1 a diagram of a flue gas cleaning system according to the invention
  • Fig. 2 is a schematic of a conventional seawater desalination plant which can be used in the context of the present invention
  • FIG. 3 shows schematically the known Solvay method
  • FIG. 4 shows schematically a first method in a first embodiment (this method is also described here as a modified version)
  • FIG. 5 shows schematically the method according to the invention
  • Fig. 6A shows schematically a sub-device, in the inventive
  • FIG. 6B shows schematically a further part device which can be used in the method according to the invention
  • Fig. 6C shows schematically a further part device which can be used in the method according to the invention
  • Fig. 7 shows schematically two further sub-devices which can be used in the method according to the invention
  • Fig. 8 shows schematically a countercurrent reactor according to the invention, which can be used to react CO 2 with a liquor;
  • Fig. 9 shows schematically a batch reactor according to the invention which can be used to react CO 2 with a caustic solution
  • 10 shows schematically a double-batch reactor according to the invention which can be used to react CO 2 with a caustic solution
  • Fig. 11 shows schematically a multiple-batch reactor according to the invention which can be used to react CO 2 with a caustic solution;
  • FIG. 12 shows in a schematic flow chart aspects of a particularly preferred method according to the invention.
  • the process according to the invention is based on a novel concept which binds the CO 2 in an alkali metal hydrogencarbonate using existing starting materials. Especially for binding, storing or storing CO 2 , sodium bicarbonate (NaHCO 3 , also known as
  • Sodium bicarbonate) or soda (Na 2 COs, sodium carbonate) proven. It is quasi the gaseous CO 2 reacted in a solid, respectively in a powder according to the invention. On the one hand, this results in a drastic reduction in volume, since the solid per unit volume contains significantly more CO 2 than the CO 2 gas or the CO 2 -containing flue gas. In this case, free, gaseous CO 2 takes up about 1000 times as much space as the same amount in the solid state (eg bound as Na 2 CO 3 ).
  • the alkali metal bicarbonate, or the alkali carbonate obtained therefrom can be easily reused in other processes, or it can be stored permanently.
  • the flue gas is preferably provided via pipes, chimneys or other line (also referred to herein as a flue gas supply 200) and transmitted / transferred to the corresponding flue gas cleaning system 51, as indicated in Fig. 1.
  • alkali metal salts and / or alkaline earth metal salts, which in the following are referred to simply by the generic term alkali metal salts.
  • alkali metal salts is to be understood in particular as meaning the following substances: NaCl; LiCl; KCl; BeCI 2 ; MgCl 2 ; CaCl 2 . That is, it is alkali / alkaline earth salts of hydrochloric acid. According to the invention, it is possible to use alkali metal salts of only one alkali metal or alkaline earth metal, or else mixtures of different alkali metal salts.
  • alkali lye and / or alkaline earth liquor which in the following will be referred to simply by the generic term alkali lye.
  • alkali metal hydroxides also called alkali hydroxides
  • alkaline earth metal hydroxides also called alkaline earth hydroxides
  • alkali metal hydroxide is to be understood in particular as meaning the following substances: NaOH; LiOH; KOH; Be (OH) 2 ; Mg (OH) 2 ; Ca (OH) 2 .
  • alkali solutions of only one alkali metal or alkaline earth metal, or else solutions of different alkali metal hydroxides and / or alkaline earth metal hydroxides can be used.
  • alkali hydrogencarbonate is produced.
  • This generic term is used to describe the following hydrogencarbonates: sodium bicarbonate (NaHCOs); Lithium hydrogencarbonate (UHCO 3 ); Potassium bicarbonate (KHCO 3 ); Beryllium hydrogencarbonate (Be (HCO 3 ) 2 ); Magnesium hydrogencarbonate (Mg (HCO 3 ) 2 ); Calcium bicarbonate (Ca (HCOs) 2 ).
  • Alkali carbonate According to the invention - depending on the specific embodiment - alkali carbonate is produced. This generic term is used to describe the following carbonates: sodium carbonate (Na 2 CO 3 ); Lithium carbonate (Li 2 CO 3 ); Potassium carbonate (K 2 CO 3 ); Beryllium carbonate (BeCO 3 ); Magnesium carbonate (MgCO 3 ); Calcium carbonate (CaCO 3 ).
  • seawater is preferably used (see box 201 in Fig. 12) to produce therefrom a concentrated aqueous alkali salt solution (e.g., a sodium chloride solution).
  • a concentrated aqueous alkali salt solution e.g., a sodium chloride solution.
  • the concentrated aqueous alkali chloride solution produced from the seawater is referred to here for simplicity as concentrated alkali salt brine 24 (see box 202 in FIG. 12).
  • this concentrated alkali salt brine 24 is produced by an evaporation process (thermal distillation process).
  • the multi-stage flash evaporation has proven particularly useful.
  • a corresponding system 10 is shown in FIG.
  • alkali lye 31 e.g., NaOH
  • alkali salt brine 24 can be prepared from the alkali salt brine 24 by one of the following three electrolytic processes:
  • the amalgam method A is ideally started with 310-280 g NaCl in 11 solution.
  • the salt concentration should be at least 260 g / l.
  • the electrolysis is stopped when only about 170 g / 11 solution are available. It can be started with all concentrations that are higher. That is, the salt concentration should be at least 170 g / l. Typically, the solution will eventually contain 12% NaOH and still 15% NaCl.
  • the membrane method C can be used NaCI contents of 20-35%, the solution may contain little impurities (calcium ⁇ 20 ppb), otherwise the membranes are damaged.
  • the salt brine of magnesium and calcium should be purified (for example by means of special ion exchangers). Magnesium and calcium form otherwise poorly soluble hydroxides, which can clog the diaphragm or the amalgam decomposer. In addition, sulfate should be carefully removed beforehand.
  • suitable precipitants eg NaOH and / or Na 2 CO 3 .
  • the concentrated alkali salt brine 24 thus preferably has a salinity which is greater than 170 g / l, and is preferably greater than 280 g / l (depending on the electrolysis process, A., B. or C., slightly different values of salinity may be used here) , It is particularly advantageous to monitor the total salt content (salinity) of the concentrated alkali salt brines 24 by a conductivity measurement.
  • the total salt content can also be monitored by measuring the density and thereby controlling the entire process. Particularly preferred is the combination, for example, of a conductivity measurement with the density measurement, e.g. to control the electrolysis process. Additionally or alternatively, a pH measurement can be carried out to give an indication of the NaOH concentration.
  • the multistage flash evaporation is based on the evaporation and subsequent condensation of the resulting vapor.
  • the seawater which was supplied through a supply line 11, heated in a heating area 12.
  • the seawater passes through several cooling loops 16.
  • the sea water is used to cool the water vapor in low-pressure tanks 13, so that Steam condenses out there.
  • the heated seawater is then passed into the low-pressure tanks 13. Due to the low pressure, the water relaxes and evaporates there. This steam then condenses on the corresponding cooling loop 16 and pure water is obtained (here as
  • Fresh water in a region 17. This water can be removed through a line 14.
  • the concentrated alkali metal brine 24 NaCl-SoIe is removed through a (fresh water) line 15.
  • So-called multi-effect distillation (MED - multiple effect distillation) systems operate at temperatures of 63 - 80 0 C.
  • the seawater is repeatedly (8 - 16 times) sprayed through heat exchanger tubes and evaporated with the return of condensation heat until all volatile substances escaped are.
  • a filtering method can be used, which is based for example on a reverse osmosis.
  • a membrane is used which separates a concentrated and a dilute solution from each other.
  • Preferred is a solution that combines a multi-stage relaxation process with a filtering process.
  • the amount of energy needed to operate the multi-stage expansion process may be at least partially provided by a power plant process.
  • alkali salt sols 24 e.g., a NaCl sol
  • sea water was provided.
  • FIG. 3 The basic scheme of a first subprocess according to the invention is shown in FIG.
  • Fig. 3 the reactants (starting materials) and the products are shown with a border.
  • FIGS. 4 and 5 the valuable products with borders are shown. Valuable intermediates are shown with dashed border.
  • seawater can be used, which is converted into fresh water (H 2 O) and NaCl soil 24 (box 201 in FIG. 8).
  • the concentrated alkali salt brine 24 used in the process according to the invention can also be produced from "solid" salt (see box 203 in Fig. 12) and water, for which purpose salt deposits can be decomposed and supplied 24 be prepared.
  • the salt can be e.g. from salt mines that do not deliver clean and edible salt, or from seawater near the sea. In Germany, there are still large salt deposits that could be used.
  • alkali metal salt which originates from another partial process (see box 216 in FIG. 12).
  • an alkali lye 31 is used, which is particularly inexpensive and easy to manufacture.
  • the alkali lye 31 is provided by converting the alkali salt brines 24 while supplying energy (see box 205 in Fig. 12).
  • a preferred apparatus 25 for providing the caustic 31 is shown. Shown is a highly schematic electrolysis device 25. It is the alkali salt brine 24 is introduced into the device 25 and there under the influence of current, respectively by the application of a voltage to alkali leach 31st electrolyzed. Since the salts are chlorine salts in aqueous solution, H 2 and Cl 2 are liberated during the electrolysis, while the alkali metal hydroxide or alkaline earth metal hydroxide (alkali metal hydroxide 31) forms.
  • the alkali salt brine 24 is preferably purified (see box 202.1 in FIG. 12). This step is optional and the corresponding box in Fig. 12 is therefore shown in phantom. It is also possible to purify the alkali lye 31 (not shown in FIG. 12). This step is also optional.
  • CO 2 is provided, respectively supplied and introduced into the alkali lye 31.
  • This process is identified in FIG. 12 by reference numeral 206. This can be done by passing the alkali lye 31 from above into a device 30 (eg in the form of a filling tower) while at the same time pumping in CO 2 from below or laterally (see FIG. 6B).
  • the alkali lye 31 is preferably introduced into the device 30 through an inlet 35 and via a distributor head 33 or through injection nozzles.
  • a device 30 (eg in the form of a filling tower) is filled with alkali lye 31.
  • the filling can take place continuously or discontinuously through an inlet 35.
  • a distribution head 34.1 is mounted inside the device 30.
  • injection nozzles or similarly acting agents can also be used in order to be able to inject or pump in the CO 2 into the alkali lye 31.
  • a large number of bubbles are formed, which increases the effective surface area and hence the efficiency of the reaction.
  • the process which preferably proceeds in the device 30, is exothermic and, with evolution of heat, the alkali bicarbonate 26 (eg, sodium bicarbonate; NaHCOs) precipitates.
  • the alkali metal bicarbonate 26 is highly schematic in the lower part of the Device 30 is shown.
  • the process can also be conducted in such a way that alkali metal carbonate (eg sodium carbonate, Na 2 CO 3 ) is formed.
  • alkali hydrogen carbonate 26 can be converted by the supply of energy (energy expenditure 2, E2) into alkali carbonate.
  • the alkali hydrogen carbonate 26 (eg, sodium bicarbonate; NaHCO 3 ) may preferably be used in a further sub-process to neutralize constituents of the flue gas, as described further below (see, eg, box 207 in FIG. 12).
  • cooling means 32 should be used to dissipate the heat generated during the exothermic reaction.
  • Such cooling devices can also be used analogously in the reactors shown in FIGS. 8, 9, 10 and 11.
  • This cooling device 32 can be cooled with water (eg sea water), as indicated in FIGS. 6B and 6C.
  • water eg sea water
  • the seawater is thus (further) preheated before it is finally brought to a temperature above 100 ° C. in the heating 12 (see FIG. 2).
  • the cooling device 32 may be traversed by a heat transfer medium that transports heat through tubes to the heater 12 to assist in heating the seawater. In this case, the cooling device 32 is not flowed through by the seawater.
  • the cooling loops 16 and the cooling device and 32 are connected in series and successively flowed through by seawater, before then the heated seawater passes through the input-side feed line 11 into the device 10.
  • the cooling capacity of the cooling loops 16 decreases. These cooling loops 16 work best at seawater temperatures below 50 0 C and preferably below 30 0 C. Therefore, in an alternative embodiment, the preheated by the waste heat water directly over a Bypass line 18 are directed into the heating area 12, while cooler seawater is passed through the cooling loops 16.
  • the bypass line 18 is indicated in Fig. 2 approach. The cooler seawater is mixed in this embodiment with the preheated seawater and then brought to about 100 0 C before it then enters the low-pressure tanks 13.
  • sodium bicarbonate (NaHCO 3 ) can be formed as alkali metal bicarbonate 26 (see box 208 in FIG. 12).
  • the sodium bicarbonate (NaHCO 3 ) can be stored to permanently bind the CO 2 .
  • sodium bicarbonate can also be used in downstream chemical (industrial) processes in which as far as possible no CO 2 is produced (see box 209 in FIG. 12).
  • the sodium bicarbonate (NaHCO 3 ), or other alkali bicarbonate 26, may also be used in a further sub-process to neutralize the flue gases, as described further below (see box 207 in FIG. 12).
  • the flue gases (see flue gas supply 200 in FIG. 1 and FIG. 12) of the power plant are introduced into a highly concentrated alkali lye 31 (see reference numeral 206 in FIG. 12).
  • sodium bicarbonate 31 NaHCO 3
  • the alkali metal bicarbonate 26 eg sodium bicarbonate, NaHCO 3
  • Decisive for a rapid absorption is the greatest possible common interface between the liquid and the gaseous phase, ie, for example, the NaOH solution and the purified (of SO 2 and NO x -frereitem) flue gas, or CO 2 -containing gas mixtures or pure CO 2 -GaS.
  • the gaseous phase ie, for example, the NaOH solution and the purified (of SO 2 and NO x -frereitem) flue gas, or CO 2 -containing gas mixtures or pure CO 2 -GaS.
  • As large as possible common interfaces are preferably obtained by blowing the gas in the form of small gas bubbles as possible from below into the solution, which then move vertically upwards due to their lower density through the solution.
  • various systems offer (for example, serving as an atomizer distribution head 34.1), such as fine nozzles, filters or porous materials, but also systems that cause strong horizontal movements in the solution Like stirring systems of all kinds. Also suitable are combined systems of atomizer and stirring system.
  • aqueous NaOH solution of 1.0 g / l (higher concentrations are even better), one can expect pure CO 2 (> 90%) over a path length of several Centimeters (in about 10 cm) almost completely (> 90%, preferably> 99%) as long as the pH of the resulting solution is strongly basic (eg pH> 12). If the pH drops by absorption of CO 2 , this slows down and longer path lengths are necessary. At a pH of about 8 no absorption takes place. At a pH of about 8, all the NaOH in the system was chemically converted to NaHCO 3 .
  • the path lengths also lengthen when using gas mixtures, the longer they extend the lower the original fraction of CO 2 was in this gas mixture. In principle, it is possible with such a system to absorb arbitrarily large amounts of CO 2 almost completely from mixtures, provided that sufficient NaOH or another alkali lye 31 is available.
  • the systems and systems according to the invention for avoiding or reducing CO 2 emissions should be optimized to use the existing base equivalents as completely as possible, ie For example, completely convert existing NaOH into NaHCO 3 . In addition, it is easier to obtain pure products (NaHCO 3 , Na 2 CO 3 ) that can be used further.
  • Na 2 CO 3 is desired as a product, some process parameters can be chosen almost arbitrarily.
  • solubility of NaOH (and also that of Na 2 CO 3 ) is much better than that of NaHCO 3 , so that rather low NaOH concentrations, preferably less than 5 g / l, are suitable for the starting solution 31 in order to prevent the precipitation of NaHCO 3 in the wrong places of the plant 30 to avoid.
  • Fig. 8 is a schematic diagram in Fig. 8.
  • Countercurrent tube 38 has an upper end inlet 35 for caustic 31 (preferably NaOH).
  • CO 2 inlet 34 At the lower end of the countercurrent tube 38 is the CO 2 inlet 34, through which CO 2 -GaS (eg flue gas or purified flue gas) enters the device 30.
  • CO 2 -GaS eg flue gas or purified flue gas
  • the inlet side (ie at the inlet 35 for the alkali lye 31) results in a flow direction of the liquid, which leads from the inlet 35 to an underlying outlet 37 (the direction of flow of the liquid is indicated in Fig. 8 by the arrow FF).
  • a gas outlet 36 NaHCO 3 solution can be removed.
  • the clean gas released from the CO 2 exits the upper end of the counterflow tube 38 through a gas outlet 36.
  • the filling level FH is located in the counterflow pipe 38 above the inlet 35 for the alkali lye 31st
  • an atomizer or a similar means is arranged to produce the smallest possible gas bubbles.
  • the counterflow tube 38, or the potential reaction region 39 of the countercurrent tube 38 must be as long as possible. That is, the limits as to when NaOH (denoted by Y1 in FIG. 8) and CO 2 (denoted by Y2 in FIG. 8) are completely fixed are not fixed.
  • the boundary Y1 and Y2 only have to be above the CO 2 inlet 34 or below the inlet 35 for the alkali lye 31 (preferably NaOH). Another problem arises that at too high flow rate of the solution (the direction of flow of the liquid is indicated in Fig.
  • the gas (the direction of flow of the gas is indicated in Fig. 8 by the arrow FG) entrained downwards is and can not exit at the top of the gas outlet 36.
  • the working pressure on the input side ie, at the inlet 35 for the caustic 31
  • the working pressure on the input side is controlled to be in a predetermined relation to the gas pressure at the CO 2 inlet 34. Fluctuations in the gas pressure can therefore be best compensated by the working pressure on the inlet side of the alkali lye 31 is adjusted accordingly control technology.
  • Fig. 9 is a schematic diagram in Fig. 9.
  • a device 30 is used whose essential component is a batch reactor 44.
  • the batch reactor 44 has an upper end inlet 35 for the caustic 31 (preferably NaOH).
  • the CO 2 inlet 34 At the lower end of the batch reactor 44 is the CO 2 inlet 34, through which CO 2 -GaS (eg flue gas or purified flue gas) enters the device 30.
  • the filling level is designated FH. It is here preferably below the inlet 35 for the alkali lye 31.
  • the batch reactor 44 further comprises an underlying outlet 37. At this outlet 37 NaHC ⁇ 3 solution can be removed. The clean gas released from the CO 2 exits the upper end of the batch reactor 44 through a gas outlet 36.
  • a nebulizer 46 or similar means is preferably arranged so that the incoming CO 2 -GaS is divided or disassembled by the nebulizer 46 into small bubbles and then these bubbles through the liquid in the Batch reactor 44 rise through it.
  • porous material can also be used to achieve bubble formation.
  • the batch reactor 44 is filled with NaOH solution 31, then the inlet 35 is closed again.
  • the gas outlet 36 is typically always open and provides for pressure equalization in the batch reactor 44 during the feed.
  • the CO 2 inlet 34 is opened and CO 2 -containing gas is blown / pumped.
  • the CO 2 -free gas flows out of the reactor 44 through the gas outlet 36.
  • a pH meter 45 or detector is used to continuously or discontinuously adjust the pH of the liquid in the batch reactor
  • Measuring devices for the volume flow at the CO 2 inlet 34 and at the gas outlet 36 can additionally control the course of the process. These measuring devices may alternatively or in addition to the pH meter
  • FIG. 10 is a schematic diagram in FIG. Because this double-batch process in the
  • the double-batch process works analogously to the batch process according to FIG. 9.
  • the advantage of this device 30 with a double-layout system lies in the continuous decrease of CO 2 -containing gas. While a batch, for example, in the first batch reactor 44.1 with CO 2 -containing gas is added, the other batch is pumped out in the second batch reactor 44.2 and refilled.
  • This double-batch process therefore runs intermittently. It can be processed a continuously accumulating flue gas stream.
  • the valve 47 is a valve which releases either the inlet to the first batch reactor 44.1 or the inlet to the second batch reactor 44.2. That is, the CO 2 -containing gas flows either into one or the other batch reactor 44.1 or 44.2.
  • Fig. 11 is a schematic diagram in Fig. 11. Since this multiple-batch process is based essentially on the batch process already described, reference is made to the description of FIGS. 9 and 10 for the basic aspects.
  • the multiple-batch process works analogously to the batch process according to FIG. 9.
  • the advantage of this device 30, for example with a five-fold design, lies in the fact that not only the CO 2 removal works continuously, but also the inflow of NaOH solution , as well as the effluent of NaHCO 3 solution.
  • reactor II While the finished NaHCO 3 solution is pumped out of the reactor I (batch reactor 44.1) through the underlying outlet 37 (sinking filling level FH, as indicated by the arrow pointing downwards in the interior of the reactor I), reactor II (batch reactor 44.2) is in Waiting state and is pumped off as soon as reactor I (batch reactor 44.1) is empty. At the same time, CO 2 -containing gas is blown into the reactor III (batch reactor 44.3) through the CO 2 inlet 34, as indicated by the arrow pointing to the left in the CO 2 inlet 34. It results in the reactor III (Batch Reactor 44.3) temporarily a slightly increased fill level FH, since the gas reduces the effective density of the solution in the reactor. Of the
  • Reactor IV (Batch Reactor 44.4) is in the standby state and is charged with CO 2 -containing gas as soon as the completion of the reaction in Reactor III (Batch Reactor 44.3) is diagnosed.
  • the reactor V (batch reactor 44.5) is simultaneously filled with NaOH solution (increasing filling level FH, as indicated by the arrow pointing upwards inside the reactor V). Filling with NaOH Solution is indicated in the region of the inlet 35 by the arrow pointing to the left.
  • alkali lye 31 preferably NaOH
  • the filling with alkali lye 31 occurs through the inlet 35.
  • the CO 2 -containing gas is blown through the CO 2 inlets 34 and the final NaHCO 3 solution is pumped or removed through the underlying outlets 37.
  • the multiple-batch process can also be reduced to 3 reactors 44.1 to 44.3.
  • Inlet 35 and 34 and the outlets 37 would be more susceptible to disturbances or changing CO 2 content in the (smoke) gas. In any case, more would be needed
  • Sensors are needed to control the progress of the reaction, for example, to adjust the strength of the CO 2 flow.
  • This process is indicated schematically in FIG. This requires an energy expenditure, which is designated in FIG. 5 with energy expenditure 2.
  • the fresh water produced during heating is collected.
  • the heating is preferably carried out at a temperature between 80 0 C and 300 0 C, preferably at 170 0 C to 180 0 C and the liberated CO 2 is recycled via a return 204 in the circuit, as in Fig. 5 by the perpendicular to above arrow and indicated in Fig. 12 by the dashed line 204.
  • the same procedure can be followed with the other alkali bicarbonates 26.
  • the alkali carbonate (eg sodium carbonate) can be stored to permanently bind the CO 2 .
  • the alkali carbonate (eg sodium carbonate) can also be used in chemical processes in which no possible CO 2 is formed (see box 209 in Fig. 12).
  • the flue gases (see flue gas supply 200 in FIG. 1 and FIG. 12) of the power plant 41 are introduced into a highly concentrated caustic 31, as mentioned (see 206 in FIG. 12).
  • alkali bicarbonate 26 and / or alkali carbonate which is more or less polluted, because in the flue gas other gases and substances may be (depending on which other sub-processes 214, 207, 217 this cleaning process is performed).
  • an alkali lye 31 is used, as mentioned.
  • three different approaches for providing or producing alkali lye 31 are designated by the reference symbols 210, 211 and 212.
  • chloralkali electrolysis processes have different advantages and disadvantages in terms of energy consumption (A.>B.> C), purity of the starting materials (C>A.> B.) And purity of the products (A.>C> B.) As well as the maintenance effort of plants (big at C). If particularly pure alkali bicarbonate products or alkali carbonate products are needed for further processing, then currently the process A. is preferred, although this process requires somewhat more energy A. When it comes to generating permanently storable or interposable alkaline bicarbonate or alkali carbonate, then process B is best suited.
  • alkaline-state chlor-alkali electrolysis processes have been deliberately chosen because these processes do not cause direct CO 2 emissions and energy consumption can be met by coupling to a power plant.
  • the chloralkali electrolysis process produces alkali lye 31 (eg sodium hydroxide, NaOH) without direct CO 2 emission.
  • reaction equations (7) and (8) are examples of alkali solutions.
  • CO 2 can be converted directly to the desired products of soda or sodium carbonate when working with caustic soda (NaOH).
  • NaOH caustic soda
  • the other alkali solutions can be used analogously.
  • the corresponding process control is shown schematically in FIG.
  • the inventive method for binding of CO 2 has not only been optimized from an environmental point of view, but it is also meaningful from a business point of view.
  • the meaningfulness results from the energy and cost balance, which then turns out to be particularly favorable if the method according to the invention is carried out in the environment of a power plant or another industrial process, since here with a heat coupling and with the direct reuse of electric current (eg for electrolysis).
  • electric current eg for electrolysis
  • part of the energy can be used, which otherwise either remains unused, or otherwise with great effort, eg by means of a district heating system, must be made usable.
  • the price for sodium carbonate (Na 2 CO 3 ) is currently approx. 4 times the price for caustic soda (NaOH) at the price of the educts and products.
  • the chloralkali electrolysis for example, of a specially produced NaCl solution, or of pre-purified, concentrated seawater, yields the following valuable products: sodium hydroxide (NaOH), chlorine (Cl 2 ) and hydrogen (H 2 ).
  • the hydrogen (H 2 ) can either be returned to the power plant to be used there as an energy supplier, or the hydrogen can be stored or transported away. In this way, power plants could produce additional hydrogen in the future.
  • the hydrogen is particularly suitable as a temporary energy storage and the energy of the stored hydrogen, for example, can be released (by combustion or in a fuel cell) when peak loads occur.
  • the process according to the invention has further inherent advantages, since the substances that are needed (educts) or produced (products or recyclables), form a group of materials in other contexts in the vicinity of a power plant 41 or other industrial process, as well as of heaters or Incineration plants, can be used advantageously (see sub-processes 214, 207 and 217 in Fig. 12).
  • Ammonia may optionally be added e.g. for denitrification (box 217 in Fig. 12) of the power plant exhaust gases (flue gas) can be used, as indicated in the following equation (9):
  • a catalyst is needed in this process.
  • Ammonia can be prepared by directly combining nitrogen and hydrogen according to equation (10): JM 2 + 3 H 2 ⁇ 2 NH 3 + 92 fcJ (10)
  • the ammonia synthesis according to equation (10) is exothermic (reaction enthalpy - 92.28 kJ / mol). It is an equilibrium reaction that proceeds with volume reduction.
  • the nitrogen can be provided, for example, according to the Linde method, in which, on the one hand, the oxygen and, on the other hand, the nitrogen are separated from the ambient air, as represented schematically by the method block 41 in FIG. The corresponding
  • Process block 41 may be part of the overall system 40 for NH 3 synthesis.
  • the overall system 40 for NH 3 synthesis can again be part of the flue gas cleaning 51 of the overall system 50 (see FIG. 1).
  • the NH 3 synthesis is carried out in a NH 3 synthesis reactor, for example in the form of a cooled pressure vessel 43.
  • a cooling device 42 which in turn is part of a series circuit of seawater cooled cooling devices 16, 32 and 42.
  • the NH 3 synthesis according to (10) may, in a preferred embodiment, provide a portion of the energy needed, for example, to operate the thermal distillation process to provide the alkali salt brines 24, assuming seawater as the salt source.
  • the energy can also be used for the electrolysis (energy expenditure 1, El) and production of the alkali lye 31.
  • cooling with a heat transfer medium can also be carried out here, as described above, in order to convey the energy to the heating area 12.
  • urea can also be prepared from the ammonia (NH 3 ) according to the following equation (11) if required.
  • this sub-process is indicated by reference numeral 219. In this process, a portion of the CO 2 is bound again.
  • This optional sub-process (11) can be used if, for example, in the parallel power plant or industrial process, urea is needed to remove soot particles or other pollutants from the exhaust gases (flue gas).
  • the urea discharge is indicated by reference numeral 214 in FIG.
  • the urea can also be used as an energy storage, since urea can be easily and easily stored and / or transported.
  • sodium bicarbonate can be used analogously to the Neutrec® process or sodium bicarbonate ("bicarbonate”) process to neutralize the acidic constituents of the flue gas (hydrochloric acid, sulfur dioxide, hydrofluoric acid, etc.) (see box 207 in FIG. 12)
  • the acidic constituents of the flue gas hydroochloric acid, sulfur dioxide, hydrofluoric acid, etc.
  • heavy metals as well as dioxins and furans can be separated by addition of activated charcoal or hearth furnace coke.
  • the sodium compounds (sodium chloride, sodium sulphate, sodium fluoride, sodium carbonate, etc.) resulting from the neutralization of the acid flue gas components are separated from the flue gases by filtering techniques
  • Sodium chloride may optionally be reused (see box 216 in Figure 12).
  • the neutralization of the acidic components by the sodium hydrogencarbonate can be described by the following reaction equations:
  • the sodium bicarbonate is brought into contact with the hot flue gases. Thereby, it is thermally activated and converted into sodium carbonate (soda; Na 2 CO 3 ) having a high specific surface area and porosity, as indicated by the following equation (15):
  • the neutralization process 207 can be made even better and more ecological by replacing sodium bicarbonate (NaHCO 3 ) with sodium carbonate (soda, Na 2 CO 3 ).
  • This soda falls according to the invention as a product of the process and can be used in part in the same plant for the neutralization of the acidic components of the flue gas.
  • Another essential aspect of the invention is seen in the fact that when binding CO 2 , which comes from a combustion, pyrolysis or other industrial process, in addition to the valuable alkali carbonate (eg soda) also drinking water / fresh water is produced.
  • This water is virtually a waste product and can be used eg for drinking water supply or irrigation.
  • the inventive method for flue gas cleaning comprises in summary the following steps:
  • alkali hydrogen carbonate eg NaHCO 3
  • alkali carbonate eg Na 2 CO 3
  • alkaline hydrogen carbonate eg NaHCO 3
  • Alkali carbonate eg Na 2 CO 3 .
  • the alkali hydrogen carbonate (eg NaHCO 3 ) and / or alkali metal carbonate (eg Na 2 CO 3 ) is used to form a sub-process for neutralizing the flue gas (Box 207). to dine with it.
  • this sub-process is performed before the sub-process after step 4.
  • sodium salt e.g., NaCl
  • flue gas cleaning residue e.g., from the sodium products resulting from neutralization, Box 207.
  • This sodium salt may be reused in the process according to the invention (see box 216 in FIG. 12).
  • the sodium salt thus obtained can therefore be used to supplement the salt feed 26 from seawater (box 201) or the production of brine from solid salts (box 203).
  • the inventive method can be operated efficiently and safely, in which case preferably should be used with the amalgam method A.
  • the use of contaminated brine would have the consequence that the resulting NaOH and also the resulting NaHCO 3 would be contaminated accordingly.
  • the nitrogen oxides in the flue gas can be eliminated (box 217).
  • the NOx in the flue gases may be purified by a catalyst system (eg, SCR; selective catalytic reduction), as previously mentioned.
  • a catalyst system eg, SCR; selective catalytic reduction
  • urea is used as the reducing agent in such a system for eliminating or reducing the nitrogen oxides.
  • SCR technology can be used particularly advantageously as one of the last sub-processes for flue gas treatment, since it is also able to eliminate ammonia residues in the flue gas. That can be important if the flue gas contains ammonia per se, as may be the case with the flue gases of a cement plant, or that may be important if in other sub-processes ammonia is used.
  • the removal of nitrogen oxides may also be effected by the injection of ammonia into the firing space (e.g., in the boiler of a power plant 41) by the non-catalytic denitrification (SNCR) process.
  • SNCR non-catalytic denitrification
  • the nitrogen produced in the SCR process in addition to water vapor can e.g. used in the Haber-Bosch process.
  • the apparatus technical effort is particularly low according to the invention, since similar or related substances are used in all sub-procedures. With a suitable, cascade-like coupling of the sub-processes, even products of one sub-process can be used in other sub-processes, as described.
  • salt and coal are the most important raw materials that Germany owns.
  • the salt can be used to provide the alkali salt sols.
  • all important raw materials are available on site.
  • the method described here and the corresponding system 50 can be used not only in stationary but also in mobile systems.
  • the method can also be used for cleaning the exhaust gases of vehicles, the apparatus design must be adjusted accordingly.
  • the pathway shown in the present application is significantly better and less risky than pumping gaseous CO 2 gas into calcareous rock strata.
  • the present process also has significant advantages over the processes in which rock is spread and ground to capture CO 2 gas by carbonate formation.

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Abstract

L'invention concerne un procédé et un dispositif (30) de liaison de CO2 gazeux. Le procédé fait intervenir une saumure concentrée transformée en lessive de soude caustique (31) par électrolyse. Le CO2 à lier est ensuite introduit dans la lessive de soude caustique (31). Il se forme alors de l'hydrogénocarbonate de sodium et/ou du carbonate de sodium. D'autres constituants des gaz de fumées peuvent être éliminés ou considérablement réduits dans d'autres processus partiels antérieurs ou ultérieurs.
PCT/EP2008/053025 2007-03-15 2008-03-13 Procédé de traitement de gaz de fumées dans des centrales et autres installations WO2008110609A2 (fr)

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EP07104246.9 2007-03-15
EP07104246A EP1961479A3 (fr) 2007-01-11 2007-03-15 Procédé et dispositif de liaison de CO2 gazeux en relation avec la désalinisation de l'eau de mer
EP07113903.4 2007-08-07
EP07113903A EP1958683A3 (fr) 2007-01-11 2007-08-07 Procédé destiné au traitement de gaz de fumée pour centrales et autres installations
PCT/EP2008/051097 WO2008110405A2 (fr) 2007-03-15 2008-01-30 Procédé et dispositif de liaison de co2 gazeux et de traitement de gaz de combustion à l'aide de composés carbonate de sodium
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ITMI20100920A1 (it) * 2010-05-21 2011-11-22 Eni Spa Procedimento per la fissazione dell'anidride carbonica proveniente da una centrale termica alimentata tramite combustibile fossile
WO2022101287A1 (fr) * 2020-11-10 2022-05-19 Shell Internationale Research Maatschappij B.V. Systèmes et procédés de génération d'un acide carboxylique à partir d'un flux de gaz co2
DE102022119806A1 (de) 2022-08-05 2024-02-08 Metaliq GmbH Verfahren und System zur Natriumcarbonatherstellung

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2792283A (en) * 1953-01-28 1957-05-14 Diamond Alkali Co Process of making sodium bicarbonate from sodium hydroxide cell liquor
US3368866A (en) * 1962-08-13 1968-02-13 Solvay Process for the manufacture of sodium carbonate
US3707453A (en) * 1971-05-06 1972-12-26 Olin Corp Mercury cell having rotating anodes
US4417970A (en) * 1981-11-24 1983-11-29 Chlorine Engineers Corp. Ltd. Electrolytic cell for ion exchange membrane method
US5980848A (en) * 1995-06-23 1999-11-09 Airborne Industrial Minerals Inc. Method for production of sodium bicarbonate, sodium carbonate and ammonium sulfate from sodium sulfate
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
EP1733782A1 (fr) * 2005-06-15 2006-12-20 Kvaerner Power Oy Procédé et appareil pour éliminer le dioxyde de carbone de gaz de combustion contenant du dioxyde de soufre

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2792283A (en) * 1953-01-28 1957-05-14 Diamond Alkali Co Process of making sodium bicarbonate from sodium hydroxide cell liquor
US3368866A (en) * 1962-08-13 1968-02-13 Solvay Process for the manufacture of sodium carbonate
US3707453A (en) * 1971-05-06 1972-12-26 Olin Corp Mercury cell having rotating anodes
US4417970A (en) * 1981-11-24 1983-11-29 Chlorine Engineers Corp. Ltd. Electrolytic cell for ion exchange membrane method
US5980848A (en) * 1995-06-23 1999-11-09 Airborne Industrial Minerals Inc. Method for production of sodium bicarbonate, sodium carbonate and ammonium sulfate from sodium sulfate
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
EP1733782A1 (fr) * 2005-06-15 2006-12-20 Kvaerner Power Oy Procédé et appareil pour éliminer le dioxyde de carbone de gaz de combustion contenant du dioxyde de soufre

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
ABDEL-AAL H K ET AL: "Chemical Separation Process for Highly Saline Water. 1. Parametric Experimental Investigation" INDUSTRIAL & ENGINEERING CHEMISTRY RESEARCH, AMERICAN CHEMICAL SOCIETY, US LNKD- DOI:10.1021/IE9405706, Bd. 35, 1. Januar 1996 (1996-01-01), Seiten 799-804, XP002241220 ISSN: 0888-5885 *
JIBRIL B E-Y ET AL: "Chemical conversions of salt concentrates from desalination plants" DESALINATION, ELSEVIER, AMSTERDAM, NL LNKD- DOI:10.1016/S0011-9164(01)00321-6, Bd. 139, Nr. 1-3, 20. September 2001 (2001-09-20), Seiten 287-295, XP004320397 ISSN: 0011-9164 *

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ITMI20100920A1 (it) * 2010-05-21 2011-11-22 Eni Spa Procedimento per la fissazione dell'anidride carbonica proveniente da una centrale termica alimentata tramite combustibile fossile
WO2022101287A1 (fr) * 2020-11-10 2022-05-19 Shell Internationale Research Maatschappij B.V. Systèmes et procédés de génération d'un acide carboxylique à partir d'un flux de gaz co2
DE102022119806A1 (de) 2022-08-05 2024-02-08 Metaliq GmbH Verfahren und System zur Natriumcarbonatherstellung

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