WO2024033830A1 - Procédé et installation de fabrication d'un matériau cimentaire - Google Patents

Procédé et installation de fabrication d'un matériau cimentaire Download PDF

Info

Publication number
WO2024033830A1
WO2024033830A1 PCT/IB2023/058045 IB2023058045W WO2024033830A1 WO 2024033830 A1 WO2024033830 A1 WO 2024033830A1 IB 2023058045 W IB2023058045 W IB 2023058045W WO 2024033830 A1 WO2024033830 A1 WO 2024033830A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
carbonizing
furnace
calcining
decarbonized
Prior art date
Application number
PCT/IB2023/058045
Other languages
English (en)
Inventor
Iver Blankenberg SCHMIDT
Leif GUNDTOFT
Original Assignee
Flsmidth A/S
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
Application filed by Flsmidth A/S filed Critical Flsmidth A/S
Publication of WO2024033830A1 publication Critical patent/WO2024033830A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/364—Avoiding environmental pollution during cement-manufacturing
    • C04B7/367—Avoiding or minimising carbon dioxide emissions
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B2/00—Lime, magnesia or dolomite
    • C04B2/10—Preheating, burning calcining or cooling

Definitions

  • Carbon capture from industrial process plants that produce CO2 is a societal need to reduce global warming.
  • thermal processing leads to conversion of the carbonates into CO2 gas.
  • Carbon capture in the form of separation of CO2 from the flue gas can be practiced in several ways that all exhibits pro's and con's when applied as part of a clinker production process.
  • One of the promising routes is the so-called oxyfuel method, where the di-oxygen required for combustion is separated from the nitrogen and argon in ambient air prior to introducing it to the cement process.
  • Thermal processing with a gas substantially free from nitrogen and argon provides a much higher concentration of CO2 in the flue gas and thus makes the flue gas much more suitable for efficient carbon capture.
  • an in-line calciner system have been used in the manufacturing of cement clinker.
  • This means that the cement is manufacturing in a single string comprising a preheater, calciner, rotary kiln and a clinker cooler.
  • air is used for combustion and for conveying of solid powder in the process.
  • Using air for combustion require approximately 1.4 kg of air per 1000 kcal fired (depending on fuel type). For a typical heat consumption of 750 kcal/kg clinker this is roughly 1.05 kg of air (minimum) per kg of cement clinker.
  • Oxyfuel also requires that the system is substantially gas tight such that as little air is introduced into the system. This is called false air. False air will bring Nitrogen to the system at the same time as it brings oxygen and thus the concentration of CO2 in the flue gas will be diluted.
  • cooling of the calcined clinker in a clinker cooling provides a challenge.
  • 300 kcal/kg of clinker is recuperated in the clinker cooler using air.
  • using air for cooling and combustion will not be possible in an oxyfuel system.
  • Special cooling is thus required using recirculated Low N2, High CO2 gas which will require further complication of the system or by introducing high concentrated O2 to the cooler which would lead to elevated temperatures in the burning zone and thus require further remediations.
  • a process for calcining a carbonaceous material comprising the steps of: a) heating a carbonaceous material, in a calcining device in the presence of an oxygen-containing gas, to a calcination temperature such that the carbonaceous material releases a carbon containing species to provide a decarbonized material; b) contacting a portion of the decarbonized material with a CCh-containing gas in a carbonizing device at a temperature around a carbonization temperature to provide a carbonaceous material and a CCh-depleated gas; c) heating a portion of the carbonaceous material in a furnace device to a sintering temperature to provide a final product; d) cooling the final product; wherein i) the oxygen-containing gas having a nitrogen content of less than 78 V/V% and/or an oxygen content greater than 21 V/V % measured on dry basis; ii) gas from the furnace device is provided to the carbonizing device and substantially
  • the carbonaceous material may be a cement clinker raw meal, a clayey material, lime, dolomite and any other material that will release CO2.
  • the carbonaceous material may be a solid material.
  • the carbonaceous material may be a particulate or powder material.
  • the carbonaceous material may be a Geldart-C type powder material.
  • the carbonaceous material may be a material which has been decarbonized and subsequently carbonized or it may be a carbonaceous raw material.
  • the carbonaceous material may consist of a part of a carbonaceous raw material and a part which has been decarbonized and subsequently carbonized.
  • substantially no gases is to be understood as the furnace device and the calcining device are coupled to exchange solid material but fluidly isolated. This should be understood as being within technical tolerances.
  • the exchange of solid material is carried out in a manner intended to prevent or reduce the volume of gases from being exchanged.
  • the carbonaceous material may be a material that after decarbonization achieves cementitious properties.
  • the final product may be cement clinker, heat treated clay, quick lime, burnt dolomite, a cementitious material or other decarbonized material.
  • the carbon containing species that is released from the carbonaceous material may be CO2.
  • the CCh-containing gas provided to the carbonizing device may be exhaust gas from the furnace device and typically has a concentration of CO2 of 15-45 V/V%.
  • the CO2- depleated gas may have a concentration of CO2 of below 30 V/V% such as between 5-30 V/V%.
  • the carbonizing temperature is typically at temperatures below 800°C such as 450°C -800°C.
  • the calcination temperature may be above 750°C such as around 750°C -1100°C.
  • the oxygen-containing gas may have a nitrogen content of less than 78 V/V%, such as less than 70 V/V%, such as less than 60 V/V%, such as less than 50 V/V%, such as less than 40 V/V%, such as less than 30 V/V%, such as less than 20 V/V%, such as less than 10 V/V%, such as less than 5 V/V%, preferably less than 2 V/V%.
  • the oxygen-containing gas may additionally or alternatively have an oxygen content greater than 22 V/V%, such as 30 V/V%, such as 40 V/V%, such as 50 V/V%, such as 60 V/V%, such as 70 V/V%, such as 80 V/V%, such as 90 V/V%, such as 95 V/V%, preferably greater than 98 V/V%.
  • the oxygen-containing gas may be preheated before being provided to the calcining device.
  • the oxygen-containing gas may be preheated by heat exchanging with exhaust gas from the cooler or heat exchanging with meal leaving the calcining device.
  • the present invention provides a process having two process strings which are configured to exchange solid material substantially without exchanging gases.
  • the first string may be referred to as the furnace string and comprises the furnace device and carbonizing device.
  • the second string may be referred to as a calciner string and comprises the calcining device.
  • This allows the furnace string to be operated with air whereas the calciner string is operated with a gas which has a low concentration of nitrogen and a high concentration of oxygen.
  • This allows carbonated material to be transferred from the furnace string to the calciner string and in the presence of oxygen to decarbonize and produce CO2.
  • the gas produced in the calcining device has a low concentration of nitrogen and is therefore better suited for Carbon Capture compared to a regular calcining device operated with air as a combustion gas.
  • a first portion of the decarbonized material is returned to the carbonizer where it is carbonized again and provided to either to furnace device or to the calciner string. If the carbonized material is provided to the furnace device, it is again decarbonized, and any released CO2 gas will flow to the carbonizing device where at least some of it reacts with decarbonized material. In this way CO2 is bound in the carbonized material and is shifted from the furnace string to the calciner string.
  • the second portion of the decarbonized material is provided directly to furnace device.
  • the second portion of decarbonized material has a temperature around the calcination temperature and is hotter than the carbonized material provided to the furnace device from the carbonizing device, which has a temperature around the carbonization temperature.
  • the inventors have found that it is sufficient to use only a portion of the decarbonized material for shifting CO2 from the furnace string of the process to the calciner string of the process.
  • the remaining decarbonized material is provided directly from the calcining device to the furnace device and thus require less energy to be heated to the sintering temperature in the furnace device. The heat efficiency of the process is thereby increased.
  • a first fraction of 10 to 95 w/w% of decarbonized material is provided to the furnace device directly from the calcining device.
  • the first fraction comprises 15 w/w%, 20 w/w%, 30 w/w%, 40 w/w%, 50 w/w%, 60 w/w%, or 70 w/w% of the decarbonized material.
  • a second fraction of 5 to 90 w/w% of the decarbonized material is provided to the carbonizing device from the calcining device.
  • the second fraction comprises 10 w/w%, 15 w/w%, 20 w/w% 30 w/w% 40 w/w%, 50 w/w%, 60 w/w%, or 70 w/w% of the decarbonized material.
  • the first fraction and second fraction should substantially add up to 100 w/w%.
  • At least one performance parameter is measured, said performance parameter being indicative of how efficient CO2 is shifted from the furnace string to the calcination string.
  • the at least one performance parameter may be the CO2 content, fraction of CO2 shifted, the O2 content, the temperature, overall heat and power consumption.
  • the temperature may indicate if the temperature in the carbonizing device is within a temperature range suitable for carbonizing.
  • solids to gas ratios are dependent on the content of oxygen.
  • the solids to gas ratio in the calcining device is larger than the solid to gas ratio in the carbonizing device.
  • the solids to gas ratio in the calcining device is in the range of 0.5 to 7 w/w measured on dry basis.
  • the solids to gas ratio may be 1, 2, 3, 4, 5, 6.
  • the solids to gas ratio in the carbonizing device is in the range of 0.25 to 7 w/w measured on dry bases.
  • the solids to gas ratio may be 1, 2, 3, 4, 5, 6.
  • the furnace device is configured to operate with a gas having a nitrogen content of at least 30V/V%, such as in the range of 78 V/V%.
  • the furnace device is operated with atmospheric air as the combustion gas.
  • the carbonizing device may be configured to receive the exhaust gas from the furnace device.
  • the majority of the carbonaceous material is initially provided to the furnace string. In one or more embodiments substantially all carbonaceous material is initially provided to the furnace string. In particular, the carbonaceous material may be provided to the carbonation device or upstream of said carbonation device.
  • the raw material the carbonaceous material
  • the calcining string instead of the calcining string, has the advantage that unwanted emission species released during heating of the feed material will stay in the furnace string. The amount of unwanted emission species in the calcining string (i.e. the concentrated CO2 gas) is reduced. It should be understood that solid material in the process is transferred between the furnace string and the calcining string, but that "initially provided” means that the raw material feed (carbonaceous material) is provided to process by introducing it into the furnace string.
  • the method further comprising the step of preheating at least a portion of the material suitable for binding carbon towards a carbonization temperature and/or preheating at least a portion of the material suitable for binding carbon to a calcination temperature.
  • a preheating device may be a preheating tower comprising a number of cyclone preheaters. Such a preheating tower may be connected to the furnace string or to the calciner string.
  • a portion of the gas from the furnace device is subjected to gas treatment before being provided to the carbonizing device.
  • gas treatment may be achieved by a by-pass system in which some of the gases from the furnace device are extracted and provided to a by-pass system.
  • the gas treatment may be up to 100% of furnace gasses to avoid build-up of volatiles in the process.
  • the feed of carbonaceous material may be provided to the calcining string, optionally to the preheating device and/or directly to the calcining device.
  • the feed of carbonized material may additionally or alternatively be provided to the furnace string, optionally to the preheating device and/or directly to the carbonizing device. Feeding a portion of the carbonized material to both preheaters allows for better heat utilization.
  • the invention relates to a plant for producing cementitious material comprising:
  • the calcining device is substantially fluidly isolated from the carbonizing device, furnace device, and cooling device.
  • the calcining device is configured to receive and provide a solid material to/from the carbonizing device.
  • the carbonizing device is configured to provide solid material to the furnace device.
  • the calcining device may additionally be configured to operate under oxygen-enriched conditions and to additionally provide a solid material directly to the furnace device.
  • solid material is provided to the furnace device from both the carbonizing device and the calcining device.
  • oxygen-enriched conditions is meant that the oxygen-containing gas provided to the calciner may have a nitrogen content of less than 78 V/V%, such as 5 V/V%, preferably less than 2 V/V%, and additionally and/or alternatively the oxygen-containing gas may have an oxygen content greater than 21 V/V%, such as 95 V/V%, preferably greater than 98 V/V%.
  • the carbonizing device may be a vessel suitable for contacting a solid material with a CO2 containing gas. Preferably the contacting occurs in counter current.
  • the solid material may be a cementitious raw material suitable for binding carbon.
  • the carbonizing vessel may have any suitable shape and should be configured to operate under carbonizing conditions.
  • the temperature suitable for carbonization is typically below 750°C such as around 400-750°C.
  • the carbonizing vessel may be configured as a flash calciner.
  • the carbonizing vessel is a flash calciner operated without a burner.
  • the calcining device may be any suitable vessel configured to accommodate a solid material and a gas under calcination temperatures.
  • the calcining vessel may have at least one burner.
  • the calcining vessel is a flash calciner.
  • the calcining device is an oxyfuel calciner.
  • the furnace device is preferably a rotary kiln.
  • the cooling device is preferably a clinker cooler or a similar cooler configured to cool a hot cementitious material from around 1450°C to 85°C.
  • a solid material splitting device is connected to the calciner.
  • the solid material splitting device being configured to provide a first portion of solid material form the calcining device to the carbonizing device and a second portion of solid material from the calcining device to the furnace device.
  • the solid material splitter comprises two cyclones and a valve. The valve configured to adjust the amount of gas to or from at least one of the cyclones.
  • the material splitter is configured to provide between 5-90 w/w% of solid from the calcining device to the carbonizing device, and between 10-95 w/w% of solid material from the calcining device to the furnace device.
  • the solid material may be the decarbonized material.
  • the solid material is calcined cement raw meal.
  • the plant further comprising at least one preheating device connected to the calciner string.
  • the calciner string preheating device being configured to receive a gas from the calciner and to contact a solid material with said gas.
  • the preheating device is a cyclone preheater comprising a number of connected cyclones.
  • the plant further comprising at least one preheating device connected to the kiln string and configured to exchange gas and solids with the carbonizer.
  • the kiln string preheating device being configured to receive a gas from the carbonizing device and to contact a solid material with said gas.
  • the kiln string preheating device is a cyclone preheater comprising a number of connected cyclones
  • the calcining device is configured with a source of oxygen.
  • the source of oxygen may be a gas tank or an oxygen manufacturing plant fluidly connected to the calcining device.
  • the oxygen provided by the source of oxygen may have a nitrogen content of less than 78% and/or an oxygen content greater than 21 V/V %.
  • the nitrogen content is below 5 V/V %.
  • the oxygen content is above 95 V/V %
  • the plant further comprising a by-pass system fluidly connected to the kiln string.
  • the by-pass system may be configured to receive a gas from the furnace device.
  • the gas may undergo gas treatment to remove volatiles.
  • the gas is returned to the kiln string.
  • the gas is returned to the furnace device or provided to the carbonizing device.
  • the by-pass system may comprise gas treatment means in the form of heat exchanger and dust removing device.
  • the plant is fluidly connected to a carbon capture system.
  • the calcining device may be fluidly connected to the carbon capture system such that the CO2 rich gas provided in the calcining device may be further processed in the carbon capture system.
  • the invention in yet another aspect relates to a retrofit system.
  • the retrofit system is adapted for being connected to a cement clinker manufacturing plant which operates with ambient air and to provide the cement clinker manufacturing plant with means to provide a gas stream with concentrated CO2.
  • the cement clinker manufacturing plant comprising a furnace device, a cooling device and optionally one or more of a calciner, a kiln riser, and a preheating device.
  • the retrofit system comprising: an oxy-calcining device configured with a source of an oxygen-containing gas, said oxygen containing gas having a nitrogen content of less than 78% and/or an oxygen content greater than 21 V/V % , a carbonizing device or means for converting an existing part of the cement clinker manufacturing plant into a carbonizing device, a first solids provision means configured to provide solids from the carbonizing device to the oxy-calcining device at least a second solids provision means configured to provide solids from the oxy-calcining device to the carbonizing device and the furnace device.
  • Oxy-calcining device means a calcining device configured to operate with a gas comprising having an oxygen concentration higher than ambient air.
  • the optional preheating device may be a cyclone preheater connected to the optional calcining device and configured to receive a hot gas from the calcining device.
  • the preheating device provides for efficient utilization of the heat from the calcining device.
  • a carbonizing device may be a vessel suitable for contacting a solid material and a CCh-containing gas, preferably in counter-flow, at a carbonization temperature. This may for instance be the case if the cement clinker manufacturing plant comprises a calcining device or a kiln riser. If these are in good condition, they may be converted into a carbonizing device. As an example, if the calcining device is a flash calciner , it may be converted into a carbonizing device by at least shutting off the fuel supply and burner during normal operation.
  • the complete system comprises a kiln string and a calciner string.
  • the two strings are connected such that substantially no gases may flow between them, whereas solids are allowed to flow from the carbonizing device to the oxy-calcining device, and from the oxy-calcining device to the carbonizing device and the furnace device.
  • false air In a typical air operated clinker manufacturing plant there will be some air that flows into the process due to leaky equipment, so-called false air. This is not problematic when the equipment is operated below atmospheric pressure and with ambient air.
  • the retrofit system allows existing equipment to be operated in air mode and does not require expensive tightening.
  • the additional equipment is on the other hand configured to be operated with an elevated oxygen concentration and a lower nitrogen content, i.e., it is more gas tight. Utilizing existing equipment in this manner allows the provision of a so-called oxyfuel cement plant in a more cost effective way.
  • the carbonizing device is either : a carbonizing device provide with the retrofit system, a calcining device, which is part of the cement clinker manufacturing plant, configured as a carbonizing unit, or a kiln riser, which is part of the cement clinker manufacturing plant, configured as a carbonizing unit.
  • the retrofit system further comprising a preheating device connected to the oxy-calcining device.
  • Preheating device connected to the oxy-calcining devices is configured to receive a gas from the oxy-calcining device and to contact a solid material with said gas.
  • the preheating device is a cyclone preheater comprising a number of connected cyclones.
  • the source of an oxygen-containing gas is a tank or vessel. In yet another embodiment the source of an oxygen-containing gas is an oxygen manufacturing plant.
  • the oxygen containing gas has a nitrogen content of less than 78% and/or an oxygen content greater than 21 V/V %. More preferably the nitrogen content is below 5 V/V %. Preferably the oxygen content is above 95 V/V %
  • the retrofit system further comprising a solid material splitter.
  • the solid material splitter may be connected to the oxy-calciner such that solid material from the oxy-calciner can be divided into two or more streams of solids.
  • the solid material splitter being configured to provide a first portion of calcined material from the oxy-calciner to the carbonizing means and a second portion of calcined material from the oxy-calciner to the kiln.
  • a cementitious raw material suitable for binding carbon may be utilized to transfer CO2 from the kiln string to the oxy-calciner string.
  • the solid material splitter may thus be used to provide a sufficient amount of decarbonized cementitious raw material from the oxy-calcining device to the carbonizing device. The remaining decarbonized cementitious raw material may be provided from the oxy-calcining device directly to the furnace device to improve the heat utilization of the plant.
  • the solid material splitter may be configured to adjust the first portion and second portion of calcined material.
  • the solid material splitter is connected to a control system.
  • One or more CO2 sensors may be located in the plant such that they may measure the CO2 in the gas.
  • a CO2 sensor may be a sensor that measures a parameter indicative of the CO2 content. Preferably it measures the CO2 content before and after the carbonizing device.
  • a CO2 sensor may also be located in the carbonizing unit. The sensor being coupled to and being in communication with the control system, and based on the measurements from the one or more sensors, the control system may adjust the first portion and second portion. In a preferred embodiment the control system is configured to minimize the amount of CO2 flowing out of the carbonizing device to the preheating device.
  • the plant may comprise one or more sensors for measuring 02, temperature, moisture and control system may optionally adjust the first portion and second portion based on a combination of measured parameters.
  • sensors are located near the solid transfer points, i.e. in the calcining device, carbonizing device, furnace device, preheating device and/or in the cooling device.
  • the sensors may be connected to and being in communication with the control system.
  • first solid provision means and/or second solid provision means may be connected to the control system to adjust the transfer of solids between the furnace string and the calcining string.
  • the feed of carbonized material may also be adjusted by the control system.
  • an increased amount of calcined material may be provided from the calcining device to the carbonizing device.
  • the amount of solid material to the carbonizing device from the calcining device may be decreased and consequently the amount of solid material from the calcining device to the furnace device is increased and the heat utilization is improved.
  • the measurement may not only be a direct measurement of oxygen, but also an indirect measurement, i.e., a measurement of another parameter which is indicative of the oxygen concentration. This applies for all the possible parameters which may be measured.
  • the retrofit system comprising a by-pass system configured to be fluidly connected to furnace device such that a portion of the gases from the furnace device is provided into the bypass system.
  • gases may undergo gas treatment to remove volatiles. After gas treatment the gas is returned to either the furnace device and/or the carbonizing device.
  • the by-pass system may comprise gas treatment means in the form heat exchanger and dust removing device.
  • the retrofit system further comprising carbon capture system suitable for being fluidly connected to the oxy-calciner.
  • the invention relates to a method of retrofitting a cement clinker manufacturing plant with means to provide a gas stream with concentrated CO2.
  • Said cement clinker manufacturing plant may be a regular air operated plant.
  • the cement clinker manufacturing plant comprising: a) optionally a preheating device b) optionally a calcining device c) a furnace device kiln d) a cooling device.
  • the method comprising: providing an oxy-calcining device configured with a with a source of an oxygencontaining gas, said oxygen containing gas having a nitrogen content of less than 78% and/or an oxygen content greater than 21 V/V %; providing a carbonizing device or means for converting an existing part of the cement clinker manufacturing plant into a carbonizing device; providing a first solids provision means configured to provide solids from the carbonizing means to the oxy-calciner substantially without exchanging any gas between the carbonizing means and the oxy-calciner and connecting said first solids provision means to the oxy- calcining device and carbonizing device; providing a second solids provision means configured to provide solids from the oxy-calciner to the carbonizer and kiln substantially without exchanging any gas between the carbonizing means and the oxy-calciner and kiln and connecting said second solids provision means to the oxy-calcining device and carbonizing device.
  • the carbonizing device is preferably coupled to the furnace device such that gases may flow from the furnace device to the carbonizing device and optionally further to the preheating device.
  • the solid provision means may be a rotating screw feeder or a loop seal where the solid material is fluidized.
  • the solid material is fluidized with an oxygen-rich gas.
  • the solid material is a Geldart-C type powder it may be beneficial to fluidize the solid material using pulsated gas to avoid channeling.
  • the carbonizing device is either: a carbonizing device provided with the retrofit system and adapted for meal and gas exchange with the kiln; a calcining device, which is part of the cement clinker manufacturing plant, which is converted into a carbonizing unit by at least lowering the operating temperature of the calcining device from a calcining temperature to a carbonizing temperature, optionally by also shutting of the fuel provision means to the calcining device; a kiln riser, which is part of the cement clinker manufacturing plant, which is converted into a carbonizing device by at least lowering the operating temperature in the kiln riser from a temperature near a calcining temperature to a carbonizing temperature.
  • the method further comprising the step of providing a preheating device and connecting said preheating device to the oxy-calciner such that the preheating device is suitable for meal and gas exchange with the oxy-calciner.
  • the method comprising the step of providing a solid material splitter and connected said solid material splitter to the oxy-calciner, the furnace device, and either the carbonizing device or the second solids provision means.
  • the solid material splitter may be configured to provide a first portion of calcined material from the oxy-calciner to the carbonizing device and a second portion to the furnace device.
  • the method further comprising the step of providing a by-pass system and fluidly connecting said by-pass system to the furnace device and the carbonizing device.
  • the by-pass system comprising gas-treating means.
  • the method further comprising the step of providing a carbon capture system and fluidly connected said carbon capture system to the to the oxy-calcining device or optionally the preheater located in the calcining string.
  • Fig. 1 shows a flow chart of a process for manufacturing a cementitious material according to one embodiment of the invention
  • Fig. 2 shows a flow chart of a process for manufacturing a cementitious material according to a further embodiment of the invention
  • Fig. 3 shows a flow chart of a process for manufacturing a cementitious material according to a further embodiment of the invention
  • Fig. 4 shows a flow chart of a process for manufacturing a cementitious material according to yet a further embodiment of the invention.
  • Fig. 1 shows a process chart for a plant 100 for producing a cementitious material from at least a carbonaceous material.
  • the plant 100 comprising a carbonizing device 4, a calcining device 3 a furnace device
  • the cooling device 1, the furnace device 2, and the carbonizing device 4 are located in a furnace string 20 and are fluidly connected.
  • the calcining device 3 is located in a separate calcining string 21 and is substantially fluidly isolated from components in the furnace string 20.
  • the calcining device 3 is connected to the carbonizing device 4 such that solid material transfer is possible.
  • the calcining device 3 is further configured to provide a solid material to the furnace device 2.
  • a cementitious raw material 10 is provided to the carbonizing device 4.
  • the cementitious raw material may be a carbonaceous material, such as cement raw meal.
  • a portion of the carbonized material is provided from the carbonizing unit to the calcining device 3.
  • Cementitious raw material 11 may additionally be added to the calcining device
  • the calcining device is provided with an oxygen containing gas 12.
  • the carbonized material is heated to a calcination temperature in the presence of oxygen to form a decarbonized material and CO2.
  • the calciner string 21 may be operated with a gas 12 with a low concentration of nitrogen, the CO2 may be removed from the calcining devices as an CCh-rich exhaust gas 15.
  • a portion of the decarbonized material is returned to the carbonizer 4 where it achieves a carbonization temperature in the presence of a CCh-containing gas.
  • As material is re-carbonated the gas becomes at least partially depleted from CO2.
  • the at least partially CCh-depleated gas 16 is removed from the carbonizer.
  • a portion of the carbonized material may again be provided to calcining device 3 whereas another portion is provided to the furnace device 2.
  • the carbonized material is heated to a sintering temperature to provide a cementitious material.
  • CO2 is released and provided to the carbonizer where it may react with decarbonated material.
  • the cementitious material is then provided to a cooling device 1 where it is cooled and extracted 14.
  • the cooler receives a cooling gas 13, which is heated by contacting the hot cementitious material. It is then provided to the furnace device 2 as a combustion gas. If an excess amount of cooling gas 13 is provided to the cooling device a portion of the cooling gas may be removed as hot gas 18.
  • the hot gas 18 may be used for heat exchange.
  • Another portion of the decarbonized material is provided from the calcining device 3 to the furnace device 2.
  • an excess amount of decarbonized material which is not required for sufficient transfer of CO2 from the furnace string 20 to the calciner string 21 is directly provided to the furnace device 2.
  • the decarbonized material provided directly from the calcining device 3 to the furnace device 2 is hotter than carbonized material from the carbonizer.
  • the direct provision of decarbonized material from the calcining device to the kiln provides a more energy efficient process.
  • Fig. 2 shows a process chart for a plant 101 for producing cementitious material.
  • the plant 101 is similar to that shown in 100, but additionally comprises a preheating device 5 located in the furnace string 20 and a preheating device 6 located in the calcining string 21.
  • the preheating device 5 is configured to receive a gas from the carbonizing device 4.
  • a cementitious raw material 10 is provided to the preheating device 5 and is in counter flow contacted with and heated by the gas from the carbonizer 4.
  • An example of a preheating device 5 may be a cyclone preheating tower comprising a plurality of cyclones.
  • the preheating device 6 is configured to receive a gas from the calcining device 3.
  • a cementitious raw material 10 is provided to the preheating device 6 and is in counter flow contacted with and heated by the gas from the calcining device 3.
  • An example of a preheating device 6 may be a cyclone preheating tower comprising a plurality of cyclones.
  • the plant 101 thus provides a process having better heat utilization.
  • Fig. 3 shows a process chart for a plant 102 for producing cementitious material.
  • the plant 102 is similar to that shown in 101, but additionally comprises a by-pass system 7.
  • a portion of the gases from the furnace device 2 may be provided to the by-pass system 7 where it is subjected to gas treatment.
  • By-pass dust and volatiles 17 may be removed from the gas before it may be reintroduced to the furnace device 2 or to the carbonizing device 4.
  • Fig. 4 shows a process chart for a plant 103 for producing cementitious material.
  • the plant 103 is similar to that shown in 101, but additionally comprises a system (8,9,10) for splitting solid material from the calcining device 3 into to separate streams.
  • the solid material splitter comprises a first cyclone 8, a second cyclone 9, a valve 10, and optionally a valve 11.
  • Exhaust gas 15 and decarbonized material is together provided into the first cyclone 8 or the second cyclone 9.
  • the amount of exhaust gas 15 and decarbonized material to each of the cyclones is determined by the valve 10 and valve 11. If the valve 11 is shut and valve 10 is open, all decarbonized material is provided to the cyclone 8 and further to the carbonizer 4.
  • valve 10 is shut and valve 10 is open, all decarbonized material is provided to the cyclone 9 and further directly to the furnace device 2.
  • valve 10 and valve 11 is coupled to a control system. Based on measurements of CO2 content in the exhaust gas 16 the valve 10 and valve 11 may be adjusted to provide a desired transfer of CO2 from the furnace string 20 to the calcining string 21.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Ceramic Engineering (AREA)
  • Structural Engineering (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental Sciences (AREA)
  • Public Health (AREA)
  • Health & Medical Sciences (AREA)
  • Ecology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Furnace Details (AREA)

Abstract

L'invention concenre un procédé et une installation de fabrication d'un matériau cimentaire et d'un flux de gaz d'échappement riche en CO2. L'installation comprend un dispositif de carbonisation, un dispositif de calcination, un dispositif de four et un dispositif de refroidissement. Le dispositif de carbonisation, le dispositif de four et le dispositif de refroidissement sont en communication fluidique. Le dispositif de calcination est sensiblement isolé de manière fluidique du dispositif de carbonisation et du dispositif de four. Le procédé comprend les étapes consistant à mettre en contact une matière première cimentaire appropriée pour lier du carbone avec un gaz contenant du CO2 dans un dispositif de carbonisation pour fournir un matériau carbonisé. Le matériau carbonisé est calciné dans le dispositif de calcination pour fournir un gaz CO2 et un matériau décarbonisé. Une partie du matériau décarbonisé est fournie au dispositif de carbonisation et une autre partie est fournie à l'autre dispositif. Le matériau est en outre fritté et refroidi pour fournir un matériau cimentaire.
PCT/IB2023/058045 2022-08-10 2023-08-09 Procédé et installation de fabrication d'un matériau cimentaire WO2024033830A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DKPA202200747 2022-08-10
DKPA202200747A DK202200747A1 (en) 2022-08-10 2022-08-10 Method and plant for manufacturing a cementitous material

Publications (1)

Publication Number Publication Date
WO2024033830A1 true WO2024033830A1 (fr) 2024-02-15

Family

ID=87760586

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/IB2023/058045 WO2024033830A1 (fr) 2022-08-10 2023-08-09 Procédé et installation de fabrication d'un matériau cimentaire

Country Status (2)

Country Link
DK (1) DK202200747A1 (fr)
WO (1) WO2024033830A1 (fr)

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
ARIAS BORJA ET AL: "CO 2 Capture by Calcium Looping at Relevant Conditions for Cement Plants: Experimental Testing in a 30 kW th Pilot Plant", INDUSTRIAL & ENGINEERING CHEMISTRY RESEARCH, vol. 56, no. 10, 15 March 2017 (2017-03-15), pages 2634 - 2640, XP093102122, ISSN: 0888-5885, Retrieved from the Internet <URL:http://pubs.acs.org/doi/pdf/10.1021/acs.iecr.6b04617> [retrieved on 20231116], DOI: 10.1021/acs.iecr.6b04617 *
SPINELLI M ET AL: "Integration of Ca-Looping Systems for CO2Capture in Cement Plants", ENERGY PROCEDIA, ELSEVIER, NL, vol. 114, 18 August 2017 (2017-08-18), pages 6206 - 6214, XP085178229, ISSN: 1876-6102, [retrieved on 20231116], DOI: 10.1016/J.EGYPRO.2017.03.1758 *

Also Published As

Publication number Publication date
DK202200747A1 (en) 2024-02-19

Similar Documents

Publication Publication Date Title
CA3098519C (fr) Fabrication de clinker par oxycombustion avec apport d&#39;oxygene special
US10434469B2 (en) Method for capturing carbon dioxide
RU2466950C2 (ru) Способ производства цемента
TWI436962B (zh) Carbon dioxide gas recovery method and recovery equipment in cement manufacturing equipment
US20240018039A1 (en) Method of calcining a raw material to obtain a cementitious material
JP5575126B2 (ja) 設備におけるセメントクリンカの製造方法及びそのようなセメントクリンカ製造設備
RU2535855C2 (ru) Способ и установка для изготовления цементного клинкера
JP5686798B2 (ja) 設備内でのセメントクリンカ製造方法、およびこのようなセメントクリンカ製造設備
JP4730394B2 (ja) セメント製造設備におけるｃｏ２ガスの回収方法および回収設備
US20190047911A1 (en) Plant for production of cement with reduced emission of pollutant gasses
US20240002288A1 (en) Method of producing clinker from cement raw meal
CN105152141B (zh) 一种石膏制酸热工工艺及装置
WO2024033830A1 (fr) Procédé et installation de fabrication d&#39;un matériau cimentaire
WO2024033831A1 (fr) Procédé et installation de fabrication d&#39;un matériau cimentaire
US8377198B2 (en) Gasification with separate calcination
CN114735956A (zh) 一种水泥熟料的低碳生产方法及其系统
CN109970370B (zh) 一种预热器窑技术制备纯铝酸钙水泥的装置以及生产工艺
CA2877418C (fr) Procede et dispositif pour accroitre le pouvoir calorifique d&#39;un flux de matiere contenant du carbone
JP4730455B2 (ja) セメント製造設備におけるｃｏ２ガスの回収方法および回収設備
OA20344A (en) Oxyfuel Clinker Production Without Recirculation of The Preheater Exhaust Gases
OA20590A (en) Oxyfuel clinker production with special oxygen addition

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 23758040

Country of ref document: EP

Kind code of ref document: A1