Systems and methods for continuous carbonization processes

Abstract

The present invention relates to a system (1000) and method for a carbonization process, and a loop furnace apparatus (100, 200) for such a process. The loop furnace apparatus (100, 200) according to the present invention comprises a slurry inlet (120, 220), at least one elongated furnace (110, 210), at least one pump (170, 270), at least one continuous separator (150, 250), and a COD inlet (130, 230). The elongated furnace (110, 210) and the continuous separator (150, 250) form a loop (100', 200'). The continuous separator (150, 250) is configured to continuously separate at least a portion of particles having a particle size smaller than a first predetermined particle size from the loop furnace apparatus (100, 200).

Description

[Technical Field]

[0001] The present invention relates to a system and method for carbonization processes and to a furnace apparatus for such processes. [Background technology]

[0002] Global warming and climate change due to human greenhouse gas emissions are an increasing problem. One way to combat global warming is to accelerate the naturally occurring carbonization of magnesium silicates, such as olivine or other (ultra)mafic minerals. Carbonization of olivine leads to the formation of magnesium carbonate and silicon dioxide, both of which are stable and can be stored indefinitely without CO2 release. The conversion of olivine to magnesium carbonate and silicon dioxide, even in nature, is a very slow process. Therefore, there is a need to increase the reaction rate and carry out this process industrially. Increasing the reaction rate can be achieved using various techniques, such as milling, heating, and increasing pressure.

[0003] SJGerdemann et al., "Carbon dioxide sequestration by aqueous mineral carbonation of magnesium silicate minerals," Journal Volume: I:, Conference: 2 nd Annual Conference on Carbon Sequestration, Alexandria, VA, May 5-8, 2003, discloses a method for accelerating the carbonation of the magnesium silicate minerals, olivine and serpentine.

[0004] There is a need in the art for a furnace for energy efficient carbonization of minerals such as olivine. Summary of the Invention [Problem to be solved by the invention]

[0005] It is an object of the present invention to provide a system, furnace apparatus and method for the carbonization of (ultra)mafic minerals. [Means for solving the problem]

[0006] This and other objects are met by the furnace apparatus, system, and method of the present invention.

[0007] The invention is defined in the independent claims. Further embodiments of the invention are defined by the dependent claims.

[0008] A first aspect of the present invention relates to a loop furnace apparatus for continuous carbonization. The loop furnace apparatus comprises an elongated furnace including a furnace outlet opening, a furnace inlet opening, and at least one CO inlet for gaseous and / or supercritical carbon dioxide (CO). The loop furnace apparatus also comprises a slurry inlet for continuous flow of slurry into the elongated furnace, at least one pump, and at least one continuous separator. The continuous separator includes a continuous separator inlet opening in fluid communication with the furnace outlet opening and a continuous separator outlet opening in fluid communication with the furnace inlet opening. The loop furnace apparatus also includes a slurry outlet. The elongated furnace and the continuous particle separator form a loop, and the at least one pump is configured to pump at least a portion of the slurry through the loop at least once. The continuous separator is configured to continuously separate at least a portion of particles having a particle size smaller than a first predetermined particle size from the loop furnace apparatus.

[0009] In one embodiment of the invention, the elongated furnace additionally includes at least one CO sensor and at least one CO controller configured to control the CO level within the elongated furnace.

[0010] In one embodiment of the present invention, the CO2 control unit is configured to control the amount of gaseous and / or supercritical CO2 injection through the at least one CO2 inlet based on an output signal representative of the CO2 level within the elongated furnace, generated by the at least one CO2 sensor.

[0011] In one embodiment of the invention, the continuous separator comprises a hydrocyclone.

[0012] In one embodiment of the invention, the loop furnace apparatus includes a cooler in fluid communication with the slurry outlet.

[0013] In one embodiment of the invention, the loop furnace apparatus comprises at least one temperature regulation device configured to heat or cool the elongated furnace.

[0014] In one embodiment of the present invention, the CO2 gas pressure within the elongated furnace fluctuates by no more than 10% during use of the loop furnace apparatus.

[0015] In one embodiment of the present invention, the loop furnace apparatus further comprises a large particle separator configured to separate large particles having a particle size greater than a third predetermined particle size, the third predetermined particle size being greater than the first predetermined particle size.

[0016] A second aspect of the present invention relates to a carbonization system comprising two or more loop furnace apparatuses according to the above, the two or more loop furnace apparatuses being arranged in sequence such that a first loop furnace apparatus of the two or more loop furnace apparatuses is arranged upstream of a second loop furnace apparatus of the two or more loop furnace apparatuses, the two or more loop furnace apparatuses being in fluid communication with each other.

[0017] In one embodiment of the invention, the slurry outlet of the first loop furnace apparatus is in fluid communication with the slurry inlet of the second loop furnace apparatus.

[0018] A third aspect of the present invention relates to a method for carbonizing minerals using the loop furnace apparatus or carbonization system described above. The method includes forming a first slurry comprising mineral particles and water, continuously feeding the first slurry into an elongated loop furnace to allow the mineral particles to react with dissolved CO2, and flowing the first slurry through the elongated furnace, CO2 being dissolved in the liquid of the slurry. The method also includes separating particles having a particle size below a first predetermined particle size of the first slurry from the elongated loop furnace using a continuous separator. Optionally, the method includes flowing the separated particles in the form of a second slurry into a second loop furnace apparatus of the carbonization system, and separating particles having a particle size below a second predetermined particle size of the second slurry from the elongated furnace of the second loop furnace apparatus using a continuous separator of the second loop furnace apparatus. The method further includes cooling the slurry exiting the elongated furnace.

[0019] One advantage of the present invention is that due to its loop configuration, the loop furnace system does not require multiple injection points for CO2 through the elongated furnace. Instead, CO2 resides in the elongated furnace over multiple loops and can be added to the reaction continuously.

[0020] One advantage of the present invention is that it allows for cost-effective and scalable processing.

[0021] One advantage of the present invention is that it allows for high flow rates, which allows particles to stay in suspension and not sink to the bottom. If particles stay in suspension, they are more likely to have some mechanical interactions, which is beneficial.

[0022] One advantage of the loop furnace system of the present invention is that a wide particle size distribution can be used in the carbonization process, as the reacted smaller particles are continuously removed from the elongated furnace.

[0023] One advantage of having two or more loop furnace systems in fluid communication with each other is that the particles are allowed to react with CO in at least two elongated furnaces, potentially leading to a more complete carbonization process, or more complete conversion and more uniform quality of the output material.

[0024] The present invention has the advantage that the CO2 can be more evenly distributed when the slurry flows through the elongated furnace two or more times.

[0025] In the following, the invention will be described in more detail, by way of example only, with reference to the accompanying drawings, in which: FIG.

[0026] The embodiments, together with further objects and advantages thereof, may best be understood by reference to the following description taken in conjunction with the accompanying drawings. [Brief explanation of the drawings]

[0027] [Figure 1] 1 is a schematic diagram of a loop furnace apparatus according to one embodiment of the present invention. [Figure 2] 1 is a schematic diagram of a carbonization system according to one embodiment of the present invention. [Figure 3] FIG. 2 is a schematic diagram of a carbonization system according to another embodiment of the present invention. [Figure 4] 1 is a schematic diagram of a loop furnace apparatus according to one embodiment of the present invention. [Figure 5] 1 is a flowchart according to one embodiment of the present invention. DETAILED DESCRIPTION OF THE INVENTION

[0028] Terms such as "top," "bottom," "upper," "lower," etc. are used solely to refer to the geometry of the embodiments of the invention as shown in the drawings and are not intended to limit the invention in any way.

[0029] As explained in the Background section, there is a need for a system and furnace apparatus for the energy-efficient carbonization of minerals such as olivine (Mg2SiO4), serpentine ((Mg,Fe)3SiO2O5(OH)4), wollastonite (CaSiO3), and / or nickel laterite (Fe,Ni)O(OH)·xH2O). Additionally, other minerals or materials may be used, such as alkaline residues, asbestos materials, etc. The general chemical reaction for the carbonization of olivine is: Mg2SiO4+2CO2→SiO2+2MgCO3(1) is.

[0030] Magnesium carbonate (MgCO3) is thermodynamically more stable than olivine (MgSiO4). However, the nature of both magnesium carbonate and olivine often dictates that the reaction (1) above is very slow and not on the timescale relevant to carbon dioxide sequestration. Therefore, there is a need to increase the reaction rate to industrially implement processes using reaction (1) for CO2 storage. However, for CO2 storage to be environmentally friendly, this increase in reaction rate must be accomplished in an energy-efficient manner.

[0031] A first aspect of the present invention relates to a loop furnace apparatus 100, 200 for continuous carbonization processing. The loop furnace apparatus 100, 200 comprises an elongated furnace 110, 210 including a furnace outlet opening 110', 210', a furnace inlet opening 110", 210", and at least one CO inlet 130, 230 for gaseous and / or supercritical CO. The loop furnace apparatus 100, 200 also comprises a slurry inlet 120, 220 for continuous flow of slurry into the elongated furnace 110, 210, at least one pump 170, 270, and at least one continuous separator 150, 250. The continuous separator 150, 250 includes a continuous separator inlet opening 150', 250' in fluid communication with the furnace outlet opening 110', 210' and a continuous separator outlet opening 150", 250' in fluid communication with the furnace inlet opening 110", 210". The loop furnace system 100, 200 further includes a slurry outlet 160, 260.

[0032] Thus, the furnace outlet openings 110', 210' are in fluid communication with the continuous separator inlet openings 150', 250', and the continuous separator outlet openings 150", 250" are in fluid communication with the furnace inlet openings 110", 210". In this manner, the elongated furnaces 110, 210 and the particle continuous separators 150, 250 form loops 100', 200'. The loops 100', 200' can be continuous such that the slurry can flow continuously through the elongated furnaces 110, 210 and the continuous separators 150, 250 for at least one revolution.

[0033] The pumps 170, 270 are configured to pump at least a portion of the slurry at least once through the loops 100', 200'. The continuous separators 150, 250 are configured to continuously separate at least a portion of particles having a particle size smaller than a first predetermined particle size from the loop furnace systems 100, 200. Such furnaces are shown schematically in Figures 1 and 2.

[0034] In one embodiment, the elongated furnace 110, 210 additionally includes at least one CO sensor 140, 240, such as at least one CO gas sensor 140, 240, and at least one CO controller 180, 280. In this embodiment, the CO controller 180, 280 is configured to control the CO level within the elongated furnace 110, 210.

[0035] In certain embodiments, the CO2 control unit 180, 280 is configured to control the amount of gaseous CO2 injected through the at least one CO2 inlet 130, 230 based on an output signal representative of the CO2 level within the elongated furnace 110, 210 generated by at least one CO2 gas sensor 140, 240, such as at least one CO2 gas sensor 140, 240.

[0036] In one embodiment, the slurry outlets 160, 260 are in fluid communication with pumps 170, 270. Such an embodiment is shown schematically in Figure 4, which is further described in more detail below.

[0037] The slurry inlets 120, 220 are configured to receive a slurry typically comprising olivine or another (ultra)mafic mineral and water. As used herein, (ultra)mafic minerals include mafic minerals (typically having a silica content of 45-55 weight percent (wt%)) and ultramafic minerals (typically having a silica content of less than 45 wt%). Mafic minerals are silicate minerals or igneous rocks rich in magnesium and iron. Common mafic minerals include olivine, pyroxene, amphibole, and biotite. The slurry may additionally comprise additives, such as oxygen or other reducing agents, or acids such as oxalic acid, ascorbic acid, or the like. The slurry inlets 120, 220 are in communication with or connected to the elongated furnaces 110, 210. The slurry typically comprises an excess of water relative to the solids, e.g., 10-50 wt% of the solids, preferably 30-40 wt%. The solids may be pretreated, for example, by grinding to reduce particle size, before entering the loop furnace system 100, 200. The particles entering the slurry inlet 120, 220 generally have a particle size of 5-200 μm, or a particle size of 10-100 μm. The loop furnace system 100, 200 is configured for continuous processing, and thus the slurry inlet 120, 220 is configured to continuously receive the slurry. The loop furnace system 100, 200 is configured to flow the slurry through the loop 100', 200', i.e., through the elongated furnace 110, 210 and the continuous separator 150, 250, at least once or once around the loop.

[0038] In one embodiment of the present invention, the water and / or additives used in the loop furnace system 100, 200 are at least partially recycled.

[0039] The elongated furnace 110, 210 is configured to provide a furnace for reaction (1) above or any other reaction in which a mineral or mixture of minerals is carbonized. As the slurry flows through the elongated furnace 110, 210, it reacts with CO2 dissolved in the liquid, such as water, of the slurry. If the slurry contains olivine, the olivine will form magnesium carbonate and silicon dioxide during the reaction according to reaction (1) above. During the reaction, the particle size generally decreases. To remove reacted particles from the elongated furnace 110, 210, the loop furnace system 100, 200 includes a continuous separator 150, 250. The continuous separator 150, 250 is configured to separate particles from the loop furnace system 100, 200 that have an average particle size smaller than a first predetermined particle size. The first predetermined particle size can be the average particle size of the slurry entering the elongated furnace 110, 210 or a smaller average particle size. In one embodiment, the particle size of the particles entering the elongated furnace 110, 210 is 5-200 μm, or 10-100 μm, or 50-100 μm. In one embodiment, the first predetermined particle size is smaller than the average particle size of the particles in the slurry entering the elongated furnace 110, 210. For example, the first predetermined particle size may be selected within the range of 5-20 μm, such as 5-15 μm or about 10 μm. In general, the size of the particles exiting the loop furnace system 100, 200 is typically smaller than the average of the particle size distribution of the particles entering the loop furnace system 100, 200.

[0040] In one embodiment, the continuous separator 150, 250 is a hydrocyclone. Other examples of the continuous separator 150, 250 include a centrifuge, a decanter, a shear-induced diffusion, and a ratchet design. The continuous separator 150, 250 is disposed in fluid communication with the elongated furnace 110, 210, as shown in Figures 1 and 2. The continuous separator 150, 250 can be configured to separate particles below a first predetermined particle size.

[0041] The slurry may contain large particles that are essentially inert. These large particles may continue to circulate through the loop furnace 100, 200 and eventually risk clogging the loop furnace 100, 200. Therefore, in one embodiment of the present invention, the loop furnace 100, 200 further includes a large particle separator (not shown). Such a large particle separator may be located upstream of the slurry inlet 120, 220. The large particle separator may also be located inside the loop furnace 100, 200 or at any other suitable location. Thus, the purpose of the large particle separator is to separate large, inert particles from the slurry, thereby reducing the risk of clogging the loop furnace 100, 200. In one embodiment, the large particle separator is configured to separate large particles having a particle size larger than a third predetermined particle size. The third predetermined particle size is larger than the first predetermined particle size.

[0042] The loop furnace systems 100, 200 are configured for continuous processing, where the slurry continuously enters the elongated furnace 110, 210 at the slurry inlet 120, 220, flows through the elongated furnace 110, 210 for at least one revolution, and when particles in the slurry reach a particle size smaller than a first predetermined particle size, the particles are separated by a continuous separator 150, 250 and exit the loop furnace system 100, 200 at the slurry outlet 160, 260. It is not necessary for all particles below the predetermined particle size to be separated at the same time; some particles below the first predetermined particle size may continue an extra revolution or revolutions in the loop furnace system 100, 200 before being separated.

[0043] The CO2 controller 180, 280 is configured to control the CO2 level within the elongated furnace 110, 210. Preferably, the CO2 controller 180, 280 is configured to control the CO2 level so that excess CO2 is present within the elongated furnace 110, 210. During use of the elongated furnace 110, 210, CO2 dissolves in the slurry. The dissolved CO2 lowers the pH of the slurry, which can be beneficial for reaction (1). When there is excess CO2, CO2 will also be present in gaseous or supercritical form within the elongated furnace 110, 210. The presence of gaseous CO2 within the loop furnace system 100, 200 can be used as an indicator that the liquid within the loop furnace system 100, 200 is saturated with CO2.

[0044] The elongated furnace 110, 210 may include two or more CO2 sensors 140, 240, such as two, three, or four CO2 sensors. In such cases, multiple CO2 sensors 140, 240 may be positioned at different locations along the elongated furnace 100, 210. The CO2 sensors 140, 240 may be CO2 gas sensors 140, 240, i.e., configured to detect CO2 in gaseous form. For example, the CO2 gas sensors 140, 240 may be gas bubble detectors or any other type of detector configured to detect the presence of CO2 in gaseous form. Alternatively, the CO2 sensors 140, 240 may be CO2 supercritical sensors 140, 240 configured to detect CO2 in supercritical form. It is also possible to use a combination of at least one CO2 gas sensor and at least one CO2 supercritical sensor. The CO2 sensors 140, 240 are configured to communicate with the CO2 controller 180, 280 to regulate the gas pressure, particularly the partial pressure of CO2, within the elongated furnace 110, 210. In that manner, the gas pressure can be maintained at a level such that excess CO2 is present within at least the elongated furnace 110, 210 during use of the loop furnace apparatus 100, 200. To this end, the one or more CO2 sensors 140, 240 are preferably configured to generate an output signal representative of a CO2 level, such as the partial pressure of CO2, within the elongated furnace 110, 210. The output signal from the CO2 sensor 140, 240 can then be input to the CO2 controller 180, 280 and used by the CO2 controller 180, 280 to control the amount of gaseous and / or supercritical CO2 injection or flow through the at least one CO2 inlet 130, 230.

[0045] CO2 is arranged to enter the elongated furnaces 110, 210 in gaseous form via CO2 gas inlets 130, 230. Before entering the elongated furnaces 110, 210, CO2 may be stored in liquid form, e.g., in a tank. In such cases, CO2 may be heated before entering the elongated furnaces 110, 210. In one embodiment, CO2 enters the elongated furnaces 110, 210 in supercritical form. The supercritical state of CO2 is dependent on both temperature and pressure. The temperature and pressure within the elongated furnaces 110, 210 depend on various parameters, such as length, diameter, material, etc., as well as reaction parameters, such as additives in the slurry, their concentration, etc. Typical temperature values are 150-200°C, e.g., 180°C, and typical pressure values are 50-150 bar (5-15 MPa), e.g., 100 bar (10 MPa).

[0046] Typical dimensions of the elongated furnaces 110, 210 are 5-50 cm in diameter and 5-50 m in length. Typical time for the particles in the elongated furnaces 110, 210 is 6-60 minutes, during which time the particles will flow through the loops 100', 200' several times.

[0047] In one embodiment, the loop furnace system 100, 200 includes two or more elongated furnaces, such as a first elongated furnace 110, 210, a second elongated furnace 110a, and a third elongated furnace 110b. In such an embodiment, the elongated furnaces 110, 210, 110a, 110b are sequentially arranged in fluid communication with one another. The first elongated furnace 110, 210 is arranged upstream of the second elongated furnace 110a, which is arranged upstream of the third elongated furnace 110b. Finally, the third elongated furnace 110b is arranged upstream of the continuous separator 150b. Such an embodiment is shown schematically in FIG. 4. As used herein, upstream and downstream refer to the flow of slurry through the loop furnace system 100, 200 from the slurry inlet 120, 220 to the slurry outlet 160, 260.

[0048] To increase the reaction rate, the loop furnace 100, 200, and particularly the elongated furnace 110, 210, may be heated. As shown in FIG. 3 , heating may be achieved by a temperature regulation device 320 positioned in contact with, connected to, or in close proximity to the elongated furnace 110, 210. Additionally, due to the exothermic nature of the reaction, it may be beneficial to cool the loop furnace 100, 200. This may be additionally achieved by the temperature regulation device 320. In one example, the loop furnace 100, 200 may be heated by the temperature regulation device 320 during start-up to reach a predetermined temperature for initiating the reaction. Once the reaction begins, the loop furnace 100, 200 may instead be cooled because the reaction is exothermic and thereby generates heat. Cooling may be additionally performed by the temperature regulation device 320.

[0049] Instead of the temperature regulation device 320, the loop furnace apparatus 100, 200 according to the present invention may also include a separate heating device and a separate cooling device, both of which are located in connection with or in close proximity to the loop furnace apparatus 100, 200.

[0050] After the particles react with CO in the loop furnace system 100, 200, the particles may have a high temperature, especially if the elongated furnace 110, 210 is heated. Therefore, the loop furnace system 100, 200 may additionally include a cooler 310 disposed downstream of the loop furnace system 100, 200, as shown in FIG. 3. In one embodiment, the loop furnace system 100, 200 further includes a cooler 310 in fluid communication with the particle outlet 160, 260. In such an embodiment, the loop furnace system 100, 200 is configured to cool the particles (slurry) by the cooler 310 after it exits via the particle outlet 160, 260.

[0051] Another aspect of the present invention relates to a carbonization system 1000 comprising two or more loop furnace apparatuses 100, 200 in fluid communication with each other. As shown schematically in Figure 3, a first loop furnace apparatus 100 of the two or more loop furnace apparatuses 100, 200 is positioned upstream of a second loop furnace apparatus 200 of the two or more loop furnace apparatuses 100, 200.

[0052] In one embodiment, the slurry outlet 160 of the first loop furnace system 100 is in fluid communication with the slurry inlet 220 of the second loop furnace system 200 .

[0053] During use, the carbonization system 1000 is configured to flow particles in the form of a slurry from the particle inlet 120 of the first loop furnace apparatus 100, through the first and second loop furnace apparatuses 100, 200, and to the particle outlet 260 of the second loop furnace apparatus 200. The first and second elongated furnaces 110, 210 are preferably configured to contain an excess of CO relative to the amount of particles present in each elongated furnace 110, 210. The carbonization system 1000 is configured to perform carbonization in the first and second elongated furnaces 110, 210 such that the average particle size of the particles in the first elongated furnace 110 is typically larger than the average particle size of the particles in the second elongated furnace 210. Such a carbonization system 1000 is shown schematically in FIG. 2.

[0054] In the carbonization system 1000 according to the present invention, all of the elongated furnaces 110, 210 preferably have excess gaseous CO. Excess gaseous CO is beneficial because it is an indicator that the liquid in the slurry, e.g., water, is saturated with CO. It is the dissolved CO that can react with the particles in the slurry. For this reason, it is advantageous for the liquid to be saturated with CO at all times, or nearly so. Without being bound by any theory, the dissolved CO serves a dual purpose by also lowering the pH, which increases the reaction rate and enhances reaction with the particles. The excess CO can be as much as 10% or 5% in excess relative to the amount of particles in the slurry.

[0055] A further aspect of the present invention relates to a method for carbonizing minerals, see Figure 5. The method comprises: Slurry formation step S1: Mixing water and mineral particles to form a first slurry (the mineral particles may be, for example, olivine, and the amount of particles in the slurry may be 10-40 wt%, for example, 35 wt%); Supply step S2: continuously supplying the first slurry to the elongated furnaces 110, 210; First reaction step S3: flowing at least a portion of the first slurry at least once through the elongated furnace 110, 210, wherein CO2 is dissolved in the liquid of the slurry; A first separation step S4: separating at least a portion of particles having a particle size below a first predetermined particle size; Second reaction step S5: Optionally, flowing the separated particles in the form of a slurry into a second loop furnace apparatus 200; A second separation step S6: separating at least a portion of particles having a particle size below a second predetermined particle size; Cooling step S7: A step of cooling the slurry leaving the elongated furnace 110, 210; Includes.

[0056] Such a method is shown in the flow chart of FIG.

[0057] In one embodiment, the method includes steps S1 to S4 and S7. In such an embodiment, these steps S1 to S4 and S7 are performed in a loop furnace system 100, 200 according to the present invention.

[0058] In another embodiment, the method includes steps S1 to S7. In such an embodiment, the method steps are performed by a carbonization system 1000 according to the present invention. More specifically, steps S1 to S4 are performed by a first loop furnace apparatus 100 of the carbonization system 1000, while steps S5 to S7 are then performed by a second loop furnace apparatus 200 of the carbonization system 1000.

[0059] In step S3, as the slurry flows through the elongated furnace 110, 210, it reacts with the dissolved CO2 in the slurry as described above. In step S4, the particles are separated according to particle size by the continuous separator 150, 250. Larger particles continue to flow through the elongated furnace 110, 210 and may therefore continue to react with the dissolved CO2. After separation, the smaller particles exit the loop furnace 100, 200 at the slurry outlet 160, 260. Optionally, the slurry outlet 160 is in fluid communication with a second loop furnace 200; in such case, the separated particles flow into the elongated furnace 210 of the second loop furnace 200 in step S5. If the two loop furnaces 100, 200 are in fluid communication with each other, the particles are again separated according to particle size by the continuous separator 250 in the second loop furnace 200 in step S6. The separation performed in step S6 can be substantially the same as that performed in step S4. Thus, in such an embodiment, the second predetermined particle size referred to above in connection with step S6 is the same as the first predetermined particle size referred to above in connection with step S4. In another embodiment, the second predetermined particle size used in step S6 is smaller than the first predetermined particle size used in step S4. In such an embodiment, the particles separated in step S6 typically have a smaller average particle size compared to the particles separated in step S4. For example, the second predetermined particle size can be selected based at least in part on the desired characteristics, such as size characteristics, of the final product output from the second loop furnace apparatus 200.

[0060] After the particles are separated from the most downstream loop furnace apparatus 100, 200, they are cooled in step S7. Cooling can be performed using a cooler 310, for example.

[0061] Typically, the feed rate is constant in the feed step S2. However, at the beginning of the process or method, the feed rate may be lower. It is also possible to feed only water at the beginning and then start feeding the slurry.

[0062] In one embodiment, the method additionally includes a pressurization step and a depressurization step. For example, the slurry may be pressurized in a pressurization step between the slurry formation step S1 and the feeding step S2, i.e., before entering the elongated furnace 110, 210. Depressurization typically occurs in conjunction with, before, during, or after the cooling step S7. Typically, the slurry is depressurized before exiting the loop furnace apparatus 100, 200. Depressurization can be performed in one step, two steps, or multiple steps. Two or more steps can reduce the risk of water freezing. Optionally, CO2 vented during the depressurization step can be reused in the process.

[0063] The present invention is not limited to the above-described embodiments. Various alternatives, modifications, and equivalents may be used. In particular, all embodiments and aspects may be combined with each other.

Claims

1. A loop-type furnace apparatus (100, 200) for continuous carbonization processing, Furnace outlet opening (110', 210'), Furnace inlet openings (110'', 210'', and Gaseous and / or supercritical carbon dioxide (CO2) ２ ) at least one CO ２ Entrance (130, 230) A long, narrow furnace (110, 210) including, A slurry inlet (120, 220) for a continuous flow of slurry into the aforementioned elongated furnace (110, 210), At least one pump (170, 270) and The furnace outlet openings (110', 210') and the continuous separator inlet openings (150', 250') are in fluid communication. The furnace inlet openings (110'', 210'', and the continuous separator outlet openings (150'', 250'', which are in fluid communication with the furnace inlet openings (110'', 210'', and Slurry outlet (160, 260) A continuous separator (150, 250) including at least one such separator Equipped with, The elongated furnace (110, 210) and the continuous particle separator (150) form a loop (100', 200'), The pumps (170, 270) are configured to pump at least a portion of the slurry through the loops (100', 200') for at least one rotation. The continuous separators (150, 250) are configured to continuously separate at least a portion of particles having a particle size smaller than a first predetermined particle size from the loop-type furnace apparatus (100, 200). Loop-type reactor system (100, 200).

2. The aforementioned elongated furnaces (110, 210) are further, at least one CO ２ Sensors (140, 240) and at least one CO ２ Control unit (180, 280) and Includes, The aforementioned CO ２ The control unit (180, 280) controls the CO2 in the elongated furnace (110, 210). ２ It is configured to control the level. The loop-type furnace apparatus (100, 200) according to claim 1.

3. the CO ２ The control units (180, 280) control the at least one CO ２ in the elongated furnace (110, 210) generated by the at least one CO ２ sensor (140, 240). Based on the output signal representing the level, the at least one CO ２ inlet (130, 230) gaseous and / or supercritical CO ２ The loop-type furnace device (100, 200) according to claim 2, which is configured to control the injection amount of

4. The loop-type furnace apparatus (100, 200) according to any one of claims 1 to 3, wherein the continuous separator (150, 250) includes a hydrocyclone.

5. The loop-type furnace apparatus (100, 200) according to any one of claims 1 to 3, further comprising a cooler (310) in fluid communication with the slurry outlets (160, 260).

6. The loop-type furnace apparatus (100, 200) according to any one of claims 1 to 3, further comprising at least one temperature control device (320) configured to heat or cool the elongated furnaces (110, 210).

7. The loop-type furnace apparatus (100, 200) according to any one of claims 1 to 3, further comprising a large particle separator configured to separate large particles having a particle diameter larger than a third predetermined particle diameter, wherein the third predetermined particle diameter is larger than the first predetermined particle diameter.

8. A carbonization system (1000) comprising two or more loop-type furnace devices (100, 200) according to any one of claims 1 to 3, wherein the two or more loop-type furnace devices (100, 200) are arranged in order such that the first loop-type furnace device (100) of the two or more loop-type furnace devices (100, 200) is located upstream of the second loop-type furnace device (200) of the two or more loop-type furnace devices (100, 200), and the two or more loop-type furnace devices (100, 200) are in fluid communication with one another.

9. The carbonization system (1000) according to claim 8, wherein the slurry outlet (160) of the first loop-type furnace apparatus (100) is in fluid communication with the slurry inlet (220) of the second loop-type furnace apparatus (200).

10. A method for carbonizing minerals using a loop-type furnace apparatus (100, 200) according to any one of claims 1 to 3, Step (S1) of forming a first slurry comprising mineral particles and water, Dissolved CO ２ Step (S2) is to continuously supply the first slurry to the elongated loop furnace (110, 210) in order to enable the mineral particles to react with the first slurry, The step of flowing the first slurry through the elongated furnace (110, 210), CO ２ However, step (S3) is in which the slurry liquid is dissolved, Step (S4) of separating particles having a particle size lower than a first predetermined particle size of the first slurry from the elongated loop furnace (110, 210) using the continuous separator (150, 250), Optionally, step (S5) of flowing the separated particles in the form of a second slurry into the second loop-type furnace apparatus (200) of the carbonization system (1000), Optionally, step (S6) of separating particles having a particle size lower than a second predetermined particle size of the second slurry from the elongated furnace (210) of the second loop-type furnace apparatus (200) using the continuous separator (250) of the second loop-type furnace apparatus (20), Step (S7) of cooling the slurry that exits the elongated furnace (110, 210) and A method that includes this.

Images