WO2020149744A1 - Carbon capture and storage - Google Patents

Carbon capture and storage Download PDF

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Publication number
WO2020149744A1
WO2020149744A1 PCT/NO2019/050006 NO2019050006W WO2020149744A1 WO 2020149744 A1 WO2020149744 A1 WO 2020149744A1 NO 2019050006 W NO2019050006 W NO 2019050006W WO 2020149744 A1 WO2020149744 A1 WO 2020149744A1
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WIPO (PCT)
Prior art keywords
carbonation
plant
gas
caustic soda
calcination
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Application number
PCT/NO2019/050006
Other languages
French (fr)
Inventor
Olfi Mohammed
Original Assignee
Engsl Minerals Dmcc
GUSTAD, Trond
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Application filed by Engsl Minerals Dmcc, GUSTAD, Trond filed Critical Engsl Minerals Dmcc
Priority to PCT/NO2019/050006 priority Critical patent/WO2020149744A1/en
Publication of WO2020149744A1 publication Critical patent/WO2020149744A1/en

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Classifications

    • 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
    • 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
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • 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
    • C01D7/07—Preparation from the hydroxides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F11/00—Compounds of calcium, strontium, or barium
    • C01F11/02—Oxides or hydroxides
    • C01F11/04—Oxides or hydroxides by thermal decomposition
    • C01F11/06—Oxides or hydroxides by thermal decomposition of carbonates
    • 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
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • 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
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/606—Carbonates
    • 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
    • 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
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • 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 invention pertains to a process for carbon capture and making available carbon dioxide (“C0 ”) gas for storage/enhanced oil recovery through an industrial plant assembly consisting mainly of limestone calcination, hydrated lime production, causticization of sodium carbonate and carbonation of caustic soda using flue gas from a power plant/other industrial plant.
  • C0 carbon dioxide
  • Limestone is calcinated through heating resulting in quick lime (CaO) and C0 2 gas.
  • CaC0 3 > CaO + C0 2
  • the quick lime is converted into calcium hydroxide by the addition of water.
  • Sodium carbonate (Soda ash, Na 2 C0 3 ) solution produced by carbon mineralization in a carbonation reactor, is causticized with hydrated lime to produce a slurry of caustic soda and calcium carbonate.
  • Another goal for present developments is using energy by less than 5 % of power plant production by using low temperature decomposable bicarbonates to produce high purity streams of C0 2 .
  • Some processes in early stages also target the relatively rare pressurized energy conversion technologies. This needs retrofits to be carried out to the boilers.
  • the present invention is aimed at meeting the requirement of producing essentially pure C0 2 gas for storage or enhanced oil recovery.
  • the enhanced oil recovery process works by injecting C0 2 into already developed oil fields, where the C0 2 mixes and releases or drives out additional oil from the reservoir thereby freeing the oil to move to production wells.
  • the process according to the present invention may be performed and realized by generating C0 2 in an amount greater than the quantity of C0 2 gas captured from the flue gas of a power/other industrial plant using waste heat, thus resulting in an efficient method of carbon capture and making C0 2 gas available for storage/ enhanced oil recovery.
  • the industrial plant assembly and process according to the present invention is particular by the fact that it does not use any amine solution to capture the C0 2 gas from power plants or other industrial installations. Rather, it combines time tested and globally proven processes of
  • the process according to the present invention uses no energy from the power/industrial plant (except waste heat) and makes available more C0 2 gas for storage or enhanced oil recovery than the quantity of C0 2 captured from the flue gas of the power/industrial plant.
  • the invention relates to a process for carbon capture for storage/enhanced oil recovery comprising the following three major steps:
  • Step 1 Calcination and hydration of lime (main step)
  • Step 2 Causticization and recovery of limestone (recycling step)
  • Step 3 Carbonation reaction and recovery of soda ash (recycling step)
  • the process and the structure/assembly of a plant for carbon capture and recovery of carbon dioxide for storage or enhanced oil recovery according to the present invention may be better understood with reference to the block flow diagram provided as Fig. 1 infra.
  • limestone from mining is crushed, screened and washed with water (beneficiation) according to the specifications requirement of kiln design for the calcination of the limestone.
  • limestone of high calcium content > 95% CaC0 3 may be used.
  • the limestone is crushed and screened according to the particle size requirements of kiln design.
  • the limestone is calcined in a calcination reactor (V) at 900 °C using heat recovered from the power plant or, alternatively, fuel energy.
  • the limestone is dissociated into the quick lime and carbon dioxide, the carbon dioxide exiting the reaction as gas.
  • the quick lime produced from the calcination process is fine grounded and reacted with water (VI) to produce hydrated lime (calcium
  • Soda ash solution preferably with a concentration in the interval 10 to 20 wt% calculated from the weight of the solution is added to a dissolving tank which is mixed with recycle stream of weak liquor obtained from a rotary filter.
  • the solution is mixed with hydrated lime in the required proportion such as 1 :6 and for series of causticizers which act like a CSTR (Cyclic Steel Tank Reactor).
  • Causticization reaction in a caustication reactor (II) is preferably carried out at 80-90 °C. Injection of steam and air is used for additional agitation. The operation is carried out until the equilibrium is attained.
  • the caustic soda in liquid form and calcium carbonate precipitate is produced.
  • the slurry of the CSTR (Cyclic Steel Tank Reactor) is fed to a thickener (III) which normally is a tank equipped with a low rpm thickener blade.
  • the stream is fed in the centre of the thickener and slurry outlet from bottom is fed to washing and overflow of the thickener is fed back for recycle; it contains 10-11 wt % NaOH which is sent to a carbonation reactor (I).
  • the sludge which settles at the bottom of the thickener (III) is washed and again sent to second thickener and finally the sludge from the second thickener is sent to rotary drum vacuum filter (IV) to remove the CaC0 3 in solid form and weak liquor is sent to starting dissolving tank. NaOH obtained from the overflow of the thickener is sent to the carbonation reactor (I). The CaC0 3 solid is sent to calcinations (V) to produce the hydrated lime.
  • the caustic soda solution normally with a concentration in the interval 10-11 wt% calculated on the weight of the solution, is fed to the carbonation reactor (I) where treated flue gas is reacted with caustic soda to produce the soda ash liquid preferably having a concentration in the interval 12.5 to 13 wt% calculated on the end weight of the soda ash liquid.
  • the soda ash solution is recycled to the causticizing reactor (II).
  • Carbon capture and storage is conventionally carried out through various processes. It has been known for a long time that the causticizing of an aqueous sodium carbonate solution by means of the milk of lime generates calcium carbonate and sodium hydroxide. This process, conventionally known as causticizing, results in the formation of 2 molecules of sodium hydroxide per molecule of calcium carbonate produced, a ratio fixed by the stoichiometry of the chemical reaction involved.
  • the caustic soda produced by causticization normally having 10-11 wt%
  • a pressurized carbonation reactor which, in a preferred embodiment, may have a design like a patented design of the Applicant and Inventor of the present invention (European Patent (EPO), Publication Number EP 2558185 Bl; PCT/N02011/000126).
  • the calcium carbonate generated during causticization is filtered and calcinated to recover the lime.
  • the C0 2 gas generated during calcination of calcium carbonate preferably having a concentration in the interval 72-74 wt%, may be used for storage/enhanced oil recovery.
  • Item 1 A process for carbon capture through the production of carbon dioxide based on reaction of limestone, wherein the process comprises of the following stages:
  • Item 2 The process according to item 1, wherein the carbon dioxide gas from the flue gas is converted into soda ash by carbonation of caustic soda (10-11 wt%) concentration and the soda ash solution produced is having 12-13 wt%
  • Item 3 The process according to item 2, wherein carbonation of caustic soda is carried out in a pressurized carbonation reactor.
  • Item 4 The process according to any of the items 1 - 3, wherein the causticization is carried out at temperature between 85 to 95°C.
  • Item 5 The process according to any of the items 1 - 4, wherein the C0 2 gas generated during calcination of calcium carbonate is greater than the quantity of C0 2 gas captured during carbonation of caustic soda.
  • Item 6 The process according to item 5, wherein the C0 2 gas concentration in the exhaust of the calcination process is 72-74 wt% with the other gas component being nitrogen.
  • Item 7 The process according to item 6, wherein the calcination process is carried out at 900 to 1000°C using waste heat of power/industrial plant.
  • Item 8 The use of carbon dioxide produced from the process of any of the items 1 - 7 for storage/enhanced oil recovery.
  • the present invention comprises a plant or assembly of stages for producing soda lime (NaOH) and carbon dioxide, said plant comprising optionally an initial section or stage for limestone mining, crushing and screening (beneficiation), and successive sections or stages for
  • the process stated supra may in one embodiment be a process wherein the carbon dioxide gas from the flue gas is converted into soda ash by carbonation of caustic soda (10-11 wt%) concentration and the soda ash solution produced is having 12-13 wt% concentration. Additionally this process may alternatively be a process wherein the carbonation of caustic soda is carried out in a pressurized carbonation reactor. Preferably the causticization is carried out at temperature between 85 to 95°C.
  • Such a process may in one embodiment be a process wherein the C0 2 gas generated during calcination of calcium carbonate is greater than the quantity of C0 2 gas captured during carbonation of caustic soda, and preferably and optionally the C0 2 gas concentration in the exhaust of the calcination process is 72-74 wt% with the other gas component being nitrogen.
  • the calcination process may be carried out at 900 to 1000°C using waste heat of power/industrial plant.
  • the invention also includes the use of carbon dioxide produced from the process for storage/enhanced oil recovery.
  • the plant or assembly of stages provided by the present invention is a plant or assembly of stages as stated supra, adjusted to carry out the stages and reactions of the process.

Abstract

It is disclosed a process and a plant or assembly of stages for producing soda lime (NaOH) and carbon dioxide, said plant comprising optionally an initial section or stage for limestone mining, crushing and screening (beneficiation) and successive sections or stages for • limestone calcination (V) and hydrated lime production • causticization (II) process • caustic soda separation • CaCO3 sludge separation • carbonation of caustic soda and soda ash solution (I) recycling to the causticization section (II).

Description

CARBON CAPTURE AND STORAGE
AMBIT OF THE INVENTION The invention pertains to a process for carbon capture and making available carbon dioxide ("C0 ") gas for storage/enhanced oil recovery through an industrial plant assembly consisting mainly of limestone calcination, hydrated lime production, causticization of sodium carbonate and carbonation of caustic soda using flue gas from a power plant/other industrial plant.
Limestone is calcinated through heating resulting in quick lime (CaO) and C02 gas. CaC03 = > CaO + C02 The quick lime is converted into calcium hydroxide by the addition of water.
CaO + H20 = > Ca(OH)2
Sodium carbonate (Soda ash, Na2C03) solution, produced by carbon mineralization in a carbonation reactor, is causticized with hydrated lime to produce a slurry of caustic soda and calcium carbonate.
Na2C03 + Ca(OH)2 = > 2NaOH + CaC03 The caustic soda and calcium carbonate is separated and the caustic soda is sent to a carbonation reactor to produce soda ash thus effectively resulting in a recycling of the soda ash. The C02 gas generated in the calcination process is sent to storage or used for enhanced oil recovery. BACKGROUND OF THE INVENTION
Energy usage for regenerating the C02 adsorbent is critical to all current C02 sequestration processes. Lowering the energy use for sequestering C02 is critical for achieving goals of reduction of C02 emissions from the exhaust of power plants or other industrial plants. Process economics is also a vital part of the solution. Conventional amine processes are claimed to use about 4 MJ/kg C02 sequestered and some other processes use about 3.2 MJ/kg C02 sequestered. Currently, C02 is removed from power plant flue gas by several different methods mainly absorbing it in some form of amine solution and producing pure compressed C02 to be deposited. Energy use is estimated at between 10 % to 18 % of power plant production.
Another goal for present developments is using energy by less than 5 % of power plant production by using low temperature decomposable bicarbonates to produce high purity streams of C02. Some processes in early stages also target the relatively rare pressurized energy conversion technologies. This needs retrofits to be carried out to the boilers.
There is thus clearly a need for better solutions to the problem of sequestering carbon dioxide from the point of energy use and the present process invention aims at filling this need.
The present invention is aimed at meeting the requirement of producing essentially pure C02 gas for storage or enhanced oil recovery.
The enhanced oil recovery process works by injecting C02 into already developed oil fields, where the C02 mixes and releases or drives out additional oil from the reservoir thereby freeing the oil to move to production wells.
The process according to the present invention may be performed and realized by generating C02 in an amount greater than the quantity of C02 gas captured from the flue gas of a power/other industrial plant using waste heat, thus resulting in an efficient method of carbon capture and making C02 gas available for storage/ enhanced oil recovery.
GENERAL DISCLOSURE OF THE INVENTION
The industrial plant assembly and process according to the present invention is particular by the fact that it does not use any amine solution to capture the C02 gas from power plants or other industrial installations. Rather, it combines time tested and globally proven processes of
(i) calcination to release C02 gas and
(ii) causticization of soda ash together with a novel process of soda ash production using an already patented process of producing soda ash (reference: European Patent (EPO), Publication Number EP 2558185 Bl; PCT/NO2011/000126) developed by the Applicant and Inventor of the present invention.
As a result, the process according to the present invention uses no energy from the power/industrial plant (except waste heat) and makes available more C02 gas for storage or enhanced oil recovery than the quantity of C02 captured from the flue gas of the power/industrial plant.
DETAILED DESCRIPTION OF THE INVENTION
The invention relates to a process for carbon capture for storage/enhanced oil recovery comprising the following three major steps:
Step 1 : Calcination and hydration of lime (main step)
Step 2: Causticization and recovery of limestone (recycling step)
Step 3: Carbonation reaction and recovery of soda ash (recycling step) The process and the structure/assembly of a plant for carbon capture and recovery of carbon dioxide for storage or enhanced oil recovery according to the present invention may be better understood with reference to the block flow diagram provided as Fig. 1 infra. Initially, limestone from mining is crushed, screened and washed with water (beneficiation) according to the specifications requirement of kiln design for the calcination of the limestone. Preferably, but not exclusively, limestone of high calcium content > 95% CaC03 may be used. STEP 1
(A) Limestone calcination and quick lime production
The limestone is crushed and screened according to the particle size requirements of kiln design. The limestone is calcined in a calcination reactor (V) at 900 °C using heat recovered from the power plant or, alternatively, fuel energy. The limestone is dissociated into the quick lime and carbon dioxide, the carbon dioxide exiting the reaction as gas. The quick lime produced from the calcination process is fine grounded and reacted with water (VI) to produce hydrated lime (calcium
hydroxide). The carbon dioxide gas is transported to storage or used for enhanced oil recovery. CaC03 (s) = > CaO (s) + C02 (g)
CaO (s) + H20 (I) = > Ca(OH)2 (s)
STEP 2
(B) Causticization process and recovery of limestone
Soda ash solution preferably with a concentration in the interval 10 to 20 wt% calculated from the weight of the solution is added to a dissolving tank which is mixed with recycle stream of weak liquor obtained from a rotary filter. The solution is mixed with hydrated lime in the required proportion such as 1 :6 and for series of causticizers which act like a CSTR (Cyclic Steel Tank Reactor). Causticization reaction in a caustication reactor (II) is preferably carried out at 80-90 °C. Injection of steam and air is used for additional agitation. The operation is carried out until the equilibrium is attained. The caustic soda in liquid form and calcium carbonate precipitate is produced.
Figure imgf000005_0001
(C) Caustic soda separation
The slurry of the CSTR (Cyclic Steel Tank Reactor) is fed to a thickener (III) which normally is a tank equipped with a low rpm thickener blade. The stream is fed in the centre of the thickener and slurry outlet from bottom is fed to washing and overflow of the thickener is fed back for recycle; it contains 10-11 wt % NaOH which is sent to a carbonation reactor (I).
(D) CaCC sludge separation
The sludge which settles at the bottom of the thickener (III) is washed and again sent to second thickener and finally the sludge from the second thickener is sent to rotary drum vacuum filter (IV) to remove the CaC03 in solid form and weak liquor is sent to starting dissolving tank. NaOH obtained from the overflow of the thickener is sent to the carbonation reactor (I). The CaC03 solid is sent to calcinations (V) to produce the hydrated lime.
STEP 3
(E) Carbonation of caustic soda solution and soda ash solution recycling
The caustic soda solution normally with a concentration in the interval 10-11 wt% calculated on the weight of the solution, is fed to the carbonation reactor (I) where treated flue gas is reacted with caustic soda to produce the soda ash liquid preferably having a concentration in the interval 12.5 to 13 wt% calculated on the end weight of the soda ash liquid. The soda ash solution is recycled to the causticizing reactor (II).
2NaOH (I) + C02 (g) = > Na2C03 (I) + H20 (I)
TECHNOLOGY REVIEW
Carbon capture and storage is conventionally carried out through various processes. It has been known for a long time that the causticizing of an aqueous sodium carbonate solution by means of the milk of lime generates calcium carbonate and sodium hydroxide. This process, conventionally known as causticizing, results in the formation of 2 molecules of sodium hydroxide per molecule of calcium carbonate produced, a ratio fixed by the stoichiometry of the chemical reaction involved.
The caustic soda produced by causticization, normally having 10-11 wt%
concentration, is carbonated with flue gas in a pressurized carbonation reactor which, in a preferred embodiment, may have a design like a patented design of the Applicant and Inventor of the present invention (European Patent (EPO), Publication Number EP 2558185 Bl; PCT/N02011/000126).
The calcium carbonate generated during causticization is filtered and calcinated to recover the lime. The C02 gas generated during calcination of calcium carbonate preferably having a concentration in the interval 72-74 wt%, may be used for storage/enhanced oil recovery. The process and use of the process according to the present invention may be summarized by the following items:
Item 1 : A process for carbon capture through the production of carbon dioxide based on reaction of limestone, wherein the process comprises of the following stages:
(a) Optionally and initially Limestone mining, crushing and screening
(beneficiation)
(b) Limestone calcination (V) and hydrated lime production
(c) Causticization (II) process
(d) Caustic soda separation
(e) CaC03 sludge separation
(f) Carbonation of caustic soda and soda ash solution (I) recycling to the
causticization in step (c).
Item 2: The process according to item 1, wherein the carbon dioxide gas from the flue gas is converted into soda ash by carbonation of caustic soda (10-11 wt%) concentration and the soda ash solution produced is having 12-13 wt%
concentration.
Item 3: The process according to item 2, wherein carbonation of caustic soda is carried out in a pressurized carbonation reactor.
Item 4: The process according to any of the items 1 - 3, wherein the causticization is carried out at temperature between 85 to 95°C.
Item 5: The process according to any of the items 1 - 4, wherein the C02 gas generated during calcination of calcium carbonate is greater than the quantity of C02 gas captured during carbonation of caustic soda.
Item 6: The process according to item 5, wherein the C02 gas concentration in the exhaust of the calcination process is 72-74 wt% with the other gas component being nitrogen.
Item 7: The process according to item 6, wherein the calcination process is carried out at 900 to 1000°C using waste heat of power/industrial plant. Item 8: The use of carbon dioxide produced from the process of any of the items 1 - 7 for storage/enhanced oil recovery.
Additionally the present invention comprises a plant or assembly of stages for producing soda lime (NaOH) and carbon dioxide, said plant comprising optionally an initial section or stage for limestone mining, crushing and screening (beneficiation), and successive sections or stages for
• Limestone calcination (V) and hydrated lime production
• Causticization (II) process
• Caustic soda separation
• CaC03 sludge separation
• Carbonation of caustic soda and soda ash solution (I) recycling to the causticization section (II).
Furthermore, the process stated supra may in one embodiment be a process wherein the carbon dioxide gas from the flue gas is converted into soda ash by carbonation of caustic soda (10-11 wt%) concentration and the soda ash solution produced is having 12-13 wt% concentration. Additionally this process may alternatively be a process wherein the carbonation of caustic soda is carried out in a pressurized carbonation reactor. Preferably the causticization is carried out at temperature between 85 to 95°C. Such a process may in one embodiment be a process wherein the C02 gas generated during calcination of calcium carbonate is greater than the quantity of C02 gas captured during carbonation of caustic soda, and preferably and optionally the C02 gas concentration in the exhaust of the calcination process is 72-74 wt% with the other gas component being nitrogen.
The calcination process may be carried out at 900 to 1000°C using waste heat of power/industrial plant. The invention also includes the use of carbon dioxide produced from the process for storage/enhanced oil recovery. The plant or assembly of stages provided by the present invention is a plant or assembly of stages as stated supra, adjusted to carry out the stages and reactions of the process.

Claims

1. A process for carbon capture through the production of carbon dioxide based on reaction of limestone, wherein the process comprises of the following stages: (a) Optionally and initially limestone mining, crushing and screening
(beneficiation)
(b) Limestone calcination (V) and hydrated lime production
(c) Causticization (II) process
(d) Caustic soda separation
(e) CaC03 sludge separation
(f) Carbonation of caustic soda and soda ash solution (I) recycling to the causticization in step (c).
2. The process according to claim 1, wherein the carbon dioxide gas from the flue gas is converted into soda ash by carbonation of caustic soda (10-11 wt%) concentration and the soda ash solution produced is having 12-13 wt%
concentration.
3. The process according to claim 2, wherein carbonation of caustic soda is carried out in a pressurized carbonation reactor.
4. The process according to any of the claims 1 - 3, wherein the causticization is carried out at temperature between 85 to 95°C.
5. The process according to any of the claims 1- 4, wherein the C02 gas generated during calcination of calcium carbonate is greater than the quantity of C02 gas captured during carbonation of caustic soda.
6. The process according to claim 5, wherein the C02 gas concentration in the exhaust of the calcination process is 72-74 wt% with the other gas component being nitrogen.
7. The process according to claim 6, wherein the calcination process is carried out at 900 to 1000°C using waste heat of power/industrial plant.
8. Use of carbon dioxide produced from the process of any of the claims 1 - 7 for storage/enhanced oil recovery.
9. Plant or assembly of stages for producing soda lime (NaOH) and carbon dioxide, said plant comprising optionally an initial section or stage for limestone mining, crushing and screening (beneficiation), and successive sections or stages for
• Limestone calcination (V) and hydrated lime production
• Causticization (II) process
• Caustic soda separation
• CaC03 sludge separation
• Carbonation of caustic soda and soda ash solution (I) recycling to the causticization section (II).
10. Plant or assembly of stages according to claim 9, wherein the carbon dioxide gas from the flue gas is converted into soda ash by carbonation of caustic soda (10- 11 wt%) concentration and the soda ash solution produced is having 12-13 wt% concentration.
11. Plant or assembly of stages according to claim 10, wherein carbonation of caustic soda is carried out in a pressurized carbonation reactor.
12. Plant or assembly of stages according to any of the claims 9 - 11, wherein the causticization is carried out at temperature between 85 to 95°C.
13. Plant or assembly of stages according to any of the claims 9 - 12, wherein the C02 gas generated during calcination of calcium carbonate is greater than the quantity of C02 gas captured during carbonation of caustic soda.
14. Plant or assembly of stages according to claim 13, wherein the C02 gas concentration in the exhaust of the calcination process is 72-74 wt% with the other gas component being nitrogen.
15. Plant or assembly of stages according to claim 14, wherein the calcination process is carried out at 900 to 1000°C using waste heat of power/industrial plant.
PCT/NO2019/050006 2019-01-14 2019-01-14 Carbon capture and storage WO2020149744A1 (en)

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CN116628576A (en) * 2023-07-26 2023-08-22 中南大学 Intelligent production yield monitoring method for heat carrier lime kiln

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