Photolytic bioreactor systems and methods

Abstract

CO2 and other gases are utilized along with mineral feedstocks to synthesize products. As a result of the photochemical reactions of liquids, solids, and gases within the advanced bioreactor of the disclosed embodiments, the synthesized products are precipitated feedstocks for multiple end-consumer and industrial products. Waste heat, pressure, and torque generated from the bioreactor are utilized to generate electricity and / or heat via a combination of energy recovery devices. The energy recovery devices offset and reduce the cost of operating the reactor, as the disclosed reactor incorporates ultraviolet-mediated photolysis as an essential component of a reactor system that also consists of an active mixer-agitator assembly, a pressure and vacuum vessel chamber, a heat source, and a port for media intake. The disclosed reactor is designed to aid in the conversion of gaseous, solid, and liquid feedstocks, such as carbon dioxide (CO2), and other inorganic and / or organic feedstocks in aqueous media, into inorganic and organic products.

Description

[Technical Field]

[0001] Related Patents and Applications This application claims the benefit of Provisional Application No. 63 / 030,916, entitled "Photolytic One Step Reactor with Energy Recovery," filed May 27, 2020, the entire contents of which are incorporated herein in their entirety.

[0002] The present disclosure relates to the utilization of CO2 and other gases using mineral feedstocks to synthesize products. [Background technology]

[0003] Excessive CO2 production from human activities has led to numerous problems for both human and animal life. The continued increase in CO2 emissions from industrial activities poses a series of risks and harmful impacts. These include the impact on the atmospheric radiative balance and the so-called "greenhouse" effect or climate change, which are exemplary consequences of increased CO2 emissions. If this carbon excess continues to accumulate unabated in the atmosphere, it poses the greatest risk of irreversible change. Much technological development has focused on reducing CO2 emissions. However, there is also a technological movement to capture and use CO2 for beneficial purposes. One such technology area is the use of CO2 in bioreactions with mineral feedstocks to synthesize products. Product synthesis can be enhanced by introducing the addition of photolysis into the bioreaction process, combined with the common mixing of CO2 with selected feedstocks. [Brief explanation of the drawings]

[0004] [Figure 1A] 1 illustrates the major components of the disclosed reactor, including the venturi nozzle, flange, electric motor housing, UV-B / C exhaust fairing and shield, and exhaust nozzle. Additionally, the general layout of the pressure tap and support stand is presented in a 2D right-hand elevation view. [Figure 1B]2 is a right-side isometric view of the reactor assembly of FIG. 1 with 3D details of the electric motor, shaft coupling, main drive shaft, and flanged cap, support assembly, and a rear remote view of the UV exhaust fairing, shield, and exhaust nozzle. [Figure 1C] FIG. 1 is an enlarged isometric view of an electric motor without the motor fairing-housing, depicting in 3D detail the shaft coupling, main drive shaft, seal-bearing assembly, and cap end flange section. [Figure 2A] This is a left side elevation view of a cross section of the reactor venturi cavity of Figure 1. The 2D cross section shows a propeller for mixing and stirring the slurry mixture and a main drive shaft extending through the entire venturi nozzle. A side elevation view is displayed showing a crucible formed from walls of quartz, sapphire, or other type of hardened transparent or translucent material with high UV transmission, surrounded by an ultraviolet lighting array mount, and a cap end flange retainer. The side elevation view also depicts the electric motor, electric motor-reactor mount and cap end flange assembly, and ports. [Figure 2B] FIG. 1B is a left side perspective view of the complete bioreactor assembly without the electric motor fairing-cover of FIG. 1A. [Figure 2C] This is an oblique view of the left side of the bioreactor, starting from the main drive shaft and ending with the UV exhaust nacelle and shield. A cross-section of the venturi nozzle cavity is also depicted, illustrating the perforated vessel attached to the inner wall and oriented around the main drive shaft. The cross-section also features the mixer-agitator attached to the main drive shaft and housed within the reactor cavity. [Figure 2D]This is an oblique view of the left side of the bioreactor, starting from the main drive shaft and ending at the divider wall retaining cap end flange. A cross-sectional view of the venturi nozzle cavity depicts a perforated vessel attached to the interior wall of the bioreactor and oriented along the main drive shaft. The cross-sectional view also shows the mixer-agitator, ports, heating band elements, flanged cap end, straight section tubing, and seal-bearing assembly configuration attached to the main drive shaft and housed within the reactor cavity. [Figure 3A] 1 is a left perspective view of a UV and visible LED (light emitting diode) and lamp array mounted around a split retaining wall cap end supported by a block mount and flange. The UV exhaust fairing and shield have been removed and are not shown. Also depicted is a quartz or sapphire cylinder or other type of transparent material cylinder housed within the split wall cap end. [Figure 3B] A dimetric left side view of the split retaining wall cap end flange, a cross section of the venturi nozzle bioreactor and ports, and a cross section of the UV exhaust-shield nacelle revealing the placement and orientation of the UV emitter housing, UV emitter, and quartz, sapphire, or transparent material crucible housed within the split retaining wall cap end flange. [Figure 3C] 2D right-side elevation and cross-sectional views of the reactor body and components. The cross-sectional views start (left to right) at the flanged cap end and end at the UV emitter source for the fiber optic cable. The cross-sectional view of the reactor cavity without the electric motor and UV fairing cover shows the fiber optic cable passing through the reactor cavity, starting from the UV emitter mounted on the outside of the dividing wall retaining flanged cap end. [Figure 3D]Left side perspective view of the bioreactor depicting a cross section of the UV and visible light nacelle-exhaust shield and a cross section of the Venturi nozzle reactor body core or cavity. Inside the reactor core or cavity is a fiber optic cable that originates from the UV or visible light emitter source and is attached to the interior wall of the bioreactor. Inside the UV nacelle is shown an LED or lamp-based UV and visible light source. The optical fiber originates from the UV or visible light source emitter and passes through the cap end flange and crucible into the reactor cavity. [Figure 4] A detailed perspective view of the rotor and stator housing of the propeller blade tip ring with windings forming a permanent magnet generator. In this configuration, the rotation of the propeller blades generates electrical energy that can be stored for future power consumption or converted into usable electricity to operate an electric motor. This configuration facilitates energy recovery during reaction or post-reaction times. [Figure 5] 2D right side elevation view of the primary reactor assembly with multiple pressure tap ports for recovering pressure energy. Depicted is a liquid gas boost pump assembly that increases the pressure of the waste CO2 and water vapor or steam that is reinjected into the reactor, induces rotation of the propeller mixer, purges the reactor of reaction products or carbonates, and recycles CO2 that may not have been carbonated in the aqueous slurry feed. [Figure 6] This is a 2D right-side elevation view of the reactor. A cross-sectional view of the Venturi nozzle reactor depicts a perforated cylinder for storing organic and inorganic media contained within the reactor cavity, oriented around the main drive shaft. Additionally, a multi-port injection system for non-contact feedstock loading is depicted. The perforated container contains either mineral feedstock or cell tissue culture, and the perforations allow for multi-port diffusion of the organic nutrient media and inorganic feedstock injected into the reactor cavity via the circulation of the mixer turbine. [Figure 7]1 is a biaxial close-up view of a perforated cylinder for containing organic and inorganic media, the cylinder being oriented along the main drive shaft and receiving liquid, solid, and gaseous media streams circulated from the reactor cavity by a mixer turbine. [Figure 8] 1 is a two-axis perspective view and spatial location reference of an optional configuration of inlet and outlet ports mounted along the exterior wall of the venturi nozzle section of a bioreactor. The ports are used for the injection and evacuation of liquids, solids, and gases into and out of the bioreactor.

[0005] In the above figures, the depiction of the cross section is illustrated by the cross section filled lines. DETAILED DESCRIPTION OF THE INVENTION

[0006] This disclosure presents a method for utilizing CO2 and other gases with mineral feedstocks to synthesize products. As a result of photochemical reactions of liquids, solids, and gases within the advanced bioreactor of the disclosed embodiments, the synthesized products are precipitated feedstocks for multiple end-use consumer and industrial products. Waste heat, pressure, and torque generated from the bioreactor are utilized for heat exchange for power generation and / or environmental conditioning via a combination of energy recovery devices for energy efficiency. The energy recovery devices offset and reduce the cost of operating the reactor, as the disclosed reactor incorporates ultraviolet-mediated photolysis as an essential component of the reactor system, which also consists of an active mixer-agitator assembly, pressure and vacuum vessel chamber, heat source, and a port for media intake. The disclosed reactor is designed to simulate a wide range of environmental conditions conducive to the conversion of gaseous, solid, and liquid feedstocks, such as carbon dioxide (CO2), and other inorganic and / or organic feedstocks in aqueous media, into inorganic and organic products.

[0007] Carbonate CO3 is the result of photochemical and chemical dissociation of compounds and subsequent binding to the carbonate form through ion exchange. As a result of these photochemical, electrochemical, and natural kinetic reactions, carbon dioxide CO2 binds to inorganic metal silicates, resulting in a stable long-term carbonate form. The source of CO2 may be derived from, but is not limited to, direct air capture of CO2 from free-flowing atmosphere and / or capture from exhaust and flue gases of industrial plants, factories, and buildings. More specifically, this disclosure describes the incorporation of energy recovery devices as part of the disclosed reactor. Potential products resulting from the photochemical reaction within the advanced bioreactor of this embodiment include, but are not limited to, inorganic carbonates, fluid and gel media, gases, cell and plant culture foods, reagents, solid inorganic oxides, mineral feedstocks, and enzymes and organisms such as microorganisms for human and non-human utilization and consumption.

[0008] In general, the products resulting from the photochemical reactions in the advanced bioreactors of the disclosed embodiments can be broadly categorized as liquid, solid, and gaseous products for human and non-human consumption and use.

[0009] The disclosed bioreactor with photolysis and energy recovery capabilities operates at high temperatures and high CO2 partial pressures (P (CO2) Carbonation of CO2 with minerals and additives under atmospheric conditions (also referred to as CO2 carbonation) is used, but is not limited to this. CO2 is a greenhouse gas and is the primary gas released into the atmosphere contributing to the climate crisis. International Panel on Climate Change The International Panel on Climate Change (IPCC) has set goals calling for the active removal of CO2 through direct air capture from a myriad of technological and natural solutions, many of which do not yet exist. The disclosed reactor utilizes direct air capture CO2, CO2 from industrial emitters, or CO2 separated from industrial flue gas waste streams, converting the CO2 to carbonate via light and chemical reactions, in the process providing a stable, long-term storage solution and use for the sequestered CO2. This type of carbonation is known as accelerated weathering or enhanced weathering. A similar process occurs naturally when either gaseous CO2 or carbonated water, which is water enriched with CO2, reacts with silicates and other minerals to produce partial carbonates by volume and weight. However, the timescale of natural carbonation is hundreds or thousands of years, if not hundreds of thousands of years or longer.

[0010] The disclosed photolysis reactor with energy recovery can complete a full carbonation batch of CO2 within minutes and hours and offset its energy consumption using an energy recovery device. Other types of inert, noble, allotropic, and chalcogen-based gases that can be utilized as feedstocks in the reactor include nitrogen (N2), argon (Ar), krypton (Kr), ozone (O3), and oxygen (O2).

[0011] Generally, bioreactor types fall into two broad flow categories: horizontal and vertical. There are advantages and disadvantages to either vertical or horizontal process flow. A vertical reactor is a structural design of a cylindrical housing, usually a steel alloy material, containing a mixer / propeller (single stage) with enough space to accommodate minerals, additives, and media such as CO2, including headspace. The disclosed photolysis reactor with energy recovery device is referred to throughout the description of the disclosed embodiments as a gas booster pump that injects CO2 at 2200 pounds per square inch (abbreviated psi, P (CO2)The advantages of vertical reactors include a simple construction that facilitates scaling to volumes of 150 cubic meters or larger.

[0012] Vertical reactors can contain mixers or impellers to agitate the slurry and / or media under reaction. Vertical reactors have several drawbacks. First, gravity constantly pulls the slurry downward, causing unswirled or unagitated media to sink to the bottom, where carbonation may occur slowly or not at all. Second, a single mixer struggles to economically actively mix the media that sinks to the bottom. Without constant agitation, a passivating silicone layer forms, inhibiting silicate carbonation and slowing the reaction rate, i.e., CO2 absorption and subsequent carbonation. Third, as the volume and mass of media and / or slurry per batch increase, the slurry and / or media weight can make vertical mixing at volume scales of 150 cubic meters and above a slower-than-expected process, potentially resulting in efficiency losses per batch throughput.

[0013] Horizontal shaft single-stage reactors have important advantages over vertical agitated reactors. The first advantage is efficient use of capacity relative to volume. The entire reactor volume is available for carbonation with increased slurry particle surface area from distribution of slurry weight displacement, horizontal diffusion, and mixing, unlike vertical reactors. The second advantage is improved flow dynamics (pressure) from horizontal venturi nozzle, venturi-type designs, compared to vertical, cylindrical, and / or spherical geometric designs.

[0014] The present reactor in the central pressure body section uses a venturimeter design having a throat or converging section located between the converging and diverging sections of the venturi. The throat section defines the narrowest section where the fluid stream converges and flows at increased velocity and reduced pressure. The diverging section extends away from the throat, increasing in cross section and widening the fluid flowing therethrough.

[0015] Horizontal flow reactors operate at higher throughput per batch because the nozzle geometry provides efficient flow per volume of slurry and / or media through the constricted section of the converging-diverging Venturi nozzle design. The underlying physics are defined by the Bernoulli and Venturi effects. As the mixer moves the aqueous slurry to the right and left sides of the Venturi reactor, and from right to left due to the reversal of rotation of the electric motor, the slurry or media must pass through the constricted section of the reactor, resulting in an increase in the velocity and a decrease in pressure of the slurry as it passes through. A heat band or thermal element is placed around the exterior of the constricted section, which in turn heats the reactor core, which in turn heats the slurry as it passes through the constricted section of the Venturi nozzle reactor.

[0016] Active mixing forces the aqueous slurry through the heated, constricted section of the venturi. Heat is then distributed evenly and quickly throughout the reactor compared to cylindrical, spherical, or non-venturi reactor body designs. Increased heat distribution results in a faster time to optimal reaction temperature.

[0017] Additionally, this embodiment incorporates multiple ultraviolet (UV)-A, UV-B, and UV-C light-emitting diodes (LEDs), excimer lamps, and lamps to accelerate the dissociation of minerals, gases, and additives in the slurry within the reactor vessel cavity. Light energy becomes more energetic as the wavelength approaches shorter. This light energy and intensity in the far-UV, short-UV, and vacuum-UV (VUV) ranges can dissociate compounds in the presence of other gases, independently based on local reactor thermal and pressure conditions. UV-C and UV-B light energy provides ancillary benefits as a germicide during the reaction process. UV-C light is particularly noteworthy for its ability to neutralize pathogens, bacteria, viruses, and other pathogens. The full ultraviolet wavelength range of the UV and visible light emitters, diodes, and lamps incorporated into the bioreactor spans the following ranges: vacuum ultraviolet (VUV) 100 nm to 200 nm, UV-C 200 nm to 280 nm, UV-B 280 nm to 315 nm, and UV-A 291 nm to 400 nm, as well as visible light 400 nm to 700 nm. All of the disclosed UV and visible light emitters are non-ionizing.

[0018] UV-C is a high-energy spectrum of ultraviolet light, a non-ionizing electromagnetic radiation with wavelengths between 125 and 200 nanometers (nm). UV light is used in three primary capacities in the advanced bioreactor of the disclosed embodiments: (a) water purification for enhanced carbonation from UV-C-generated OH (hydroxyl) and O (ozone), (b) fast-reacting OH (hydroxyl) that combines with leached minerals, calcium or magnesium, or other inorganic and organic feedstocks to produce hydroxides, and (c) UV-C-generated OH can be reacted with UV-C by-products CO (carbon monoxide) and O (oxygen) at a wavelength of 160 nm and then recombined to produce CO product for use in mineral carbonation within the reactor or for storage and use elsewhere.

[0019] The general equations governing the photochemical reaction rates under specific heat, pressure, residence time, UV radiation, solid mineral feedstock, gas input, and general products of the bioreactor of the disclosed embodiments are given in the following paragraphs: All inputs in the described reactions are inorganic and do not consider organic inputs for biomineralization or biocarbonation to enhance the weatherability of inorganic silicates.

[0020] The mineral wollastonite is used in Example 1. Wollastonite, which has the general chemical compound of calcium silicate, CaSiO, is a mineral input that reacts with CO to give calcium carbonate (CaCo) and silicon dioxide (SiO) in the reactor of the disclosed embodiments. CaSiO3+CO2→CaCO3+SiO2 formula (1) This reaction is much more efficient in the aqueous phase. When water H2O absorbs CO2, the aqueous phase becomes acidic and the following species are simultaneously present: CO2+H2O→H2CO3 formula (2) moreover, H2CO3→←H + +HCO - 3 formula(3) HCO - 3→←H + +CO3 2- Formula (4) H2O →←H + +OH - Formula (5) The calcium contained in the wollastonite dissolves in the aqueous phase as follows. CaSiO3+2H + →Ca2 + +SiO2↓+H2O Equation (6) Ca 2+ +CO3 2- →←CaCO3↓ Equation (7)

[0021] In this example, the residence time for the reaction to occur is 30 minutes to 6 hours, and the particle size of the reference wollastonite is 38 microns. Active mixing is at 1500 revolutions per minute (rpm). The maximum temperature is 400°F. A pressure of approximately 400 pounds per square inch (psi) or 30 bar is used. CO2 Internal bioreactor pressure in partial pressure.

[0022] In the following Example 2, UV-C irradiation is used. Natural photoexcitation (hv), i.e., the production of hydroxyl (OH) under atmospheric operating conditions in the upper atmosphere, is artificially reproduced in the bioreactor of the disclosed embodiment with UV-C ≈ (λ 160 nm - 172 nm). M is a collision gas, typically nitrogen.

[0023] The following general equation describes the photochemical reaction: O3+hv→←O2+O( 3 P) Equation (8) O( 3 P)+O2(+M)→O3(+M) Equation (9) O( 3 P)+H2O→2OH Formula (10)

[0024] Compressed air and O3, a by-product of UV-C photolysis, can be injected into the bioreactor of the disclosed embodiments to supplement hydroxyl (OH) formation, resulting in: CaSiO3+2H + +OH+hv→Ca(OH)2+SiO 2(s) +H + Formula (11) CO2 is then injected into the reactor, which results in: CO2+Ca(OH)2+SiO 2(s) →CaCO3+H2O+SiO 2(aq) Formula (12) The hydrated slurry is removed from the bioreactor and dried at a temperature T≈212°F. (aq.-蒸気) is collected, purified and recycled for further use, thereby obtaining: CaCO3+H2O+SiO2(aq) +ΔH → CaCO3 + SiO2 Equation (13)

[0025] The residence time for Example 2 is estimated to be 5 minutes to 1 hour, and the particle size of the wollastonite is referenced at 38 μ (microns). The temperature is 250°F / 400°F. The pressure conditions are 200 to 400 pounds per square inch (psi). CO2 The partial pressure may vary. Active mixing is 500 rpm to 1500 rpm.

[0026] The disclosed reactor incorporates energy recovery devices, including, but not limited to, propellers of various configurations and / or ring stator magnets coupled to the blade tips of the motor shaft, capable of generating DC electricity when the turbine blades are rotating. A shaft-mounted turbine and a compressed CO2 gas jet directed toward such a shaft are also coupled to a generator, converting high-pressure fluid energy from the CO2 gas jet into mechanical torque for a multi-element turbine. Additionally, high-pressure steam and compressed air can also be injected and re-injected into the reactor to induce turbine rotation, and if the rotating turbine shaft is also coupled to an electric motor, DC electricity is generated. Thermoelectric generators (TEGs) are solid-state devices that use the Seebeck effect to generate electrical charge from heat flux. TEGs are incorporated into the reactor design. Generating electricity in the form of DC and / or AC power offsets the energy consumption required to operate the disclosed reactor at the optimal thermal and pressure conditions required for carbonation and other types of reactions.

[0027] The bioreactor of this embodiment has a wide range of capabilities for temperature, pressure and vacuum, mixing, artificial UV, and visible light, making it further applicable to the production of food, specifically cell-cultured foods such as fish, meat, and certain vegetables, as well as certain plants for human and animal consumption. The reactor volume, materials, and design for both inorganic and organic products can be scaled from 0.014 cubic meters to 150 cubic meters in volume for processing and culturing tissues and organisms for cell-cultured foods in large batches.

[0028] Preferred reactor materials are stainless steel and / or aluminum. To scale reactor volumes, other light metal alloys, glass, and sapphire attachments may be preferred over some types of plastic. The choice of plastic must be made carefully due to the risk of migration of PFAS / PFOA / PFOS, an acronym for "forever chemicals," and potentially toxic chemicals present in plastic products that could potentially migrate to culture batches incubating in the reactor. However, certain PFAS / PFOA / PFOS-free plastics, molded carbonates, and polycarbonates can be used as reactor lining materials. State-of-the-art bioreactors incorporating Teflon® materials made from PFAS / PFOA / PFOS pose a risk of migration of a group of permanent chemicals into cultured organic products, such as meat, fish, and plant products, posing a risk of human and non-human ingestion of these chemicals.

[0029] The production of muscle cells for cell-cultured meat can be separated into two phases: a proliferation phase, in which cells divide and grow, and a differentiation phase, in which cells differentiate into skeletal muscle cells and then fuse into multinucleated myotubes. Both phases require different culture environments. During the differentiation phase, a 3D support structure may be required to enable the skeletal muscle cells to form muscle tissue.

[0030] Compared to current state-of-the-art bioreactors, the bioreactor of the disclosed embodiments can distribute nutrient flow evenly throughout the volume and length of the reactor, maintain zonal or localized heating and cooling, and distribute heating evenly throughout the culture within the reactor through heat exchange from variable speed mixing, countercurrent mixing, and gas injection.

[0031] Using ultraviolet (UV) and / or visible light sources, each tissue culture enclosed within the bioreactor can be irradiated (dose) using fiber optic cables or directly from UV or visible light sources housed within the cavity of the bioreactor or mounted circumferentially along the exterior wall of the bioreactor. UV and visible light irradiation can enhance the development rate of certain cell cultures and is practical for biophotonic sequencing of various cell tissue-cultured meat, poultry, fish, and certain plants and vegetables.

[0032] The primary method for increasing the yield of cell culture tissues from biophotonics is through its bactericidal benefit to the nutrient flow and cell tissue cultures incubated within the bioreactor. Viruses, microbial bacteria (yeast, fungi), and mycoplasma can cause cell contamination, resulting in tissue loss and potentially contaminating the entire batch housed in the reactor. UV-C / B / A light is a powerful bactericide and RNA disruptor against bacteria, viruses, and pathogens, preventing the spread of bacterial and viral colonies in the tissue culture.

[0033] The bioreactor of this embodiment has multiple ports for injecting reagents, nutrients, and gases, and an exhaust port for removing slurry waste and cell waste by-products. UV lighting can be used to purify and reuse the water used for the nutrient broth.

[0034] The disclosed next-generation photolysis reactor with energy recovery capabilities operates differently from traditional vertically mounted reactors found in laboratories, institutions, and research facilities. The bioreactor design utilizes ultraviolet / UV-A / B LEDs (liquid light-emitting diodes) and excimer lamps in the 200-400 nanometer (nm) wavelength range, as well as a multi-element axial propeller agitator combined with UV-C directed light energy in the 140-200 nm range, to accelerate the carbonation of CO2 using magnesium and calcium silicate minerals and other mineral wastes, oxide feedstocks, and desulfurized calcium sulfate. The resulting effect of photolysis, elevated temperature, and pressure is enhanced carbonation of calcium and magnesium silicates in the presence of CO2, as described in Example 2 in the Background of the Preferred Embodiments section.

[0035] The carbonate precipitates produced can be, but are not limited to, magnesium carbonate (MgCO), calcium carbonate (CaCO), dolomitic carbonate ([Mg / Ca]CO), iron carbonate (FeCO), potassium carbonate (KCO), and sodium carbonate (NaCO). The carbonates then become feedstock materials for numerous industrial processes and end-use products. This embodiment consists of a reactor pressure vessel housing, cap end, and quartz viewport that can be pressurized to 2200 psi (pounds per square inch), or 150 atm (atmospheres), to emulate conditions in the Earth's upper mantle. The reactor environment can also be reduced pressure to emulate sub-atmospheric and vacuum conditions.

[0036] The disclosed reactor also withstands heating up to 2000°F under ambient conditions, heating up to 625°F under high-pressure conditions, and freezing to temperatures as low as negative 20°F. Internally and externally mounted heating elements provide thermal energy for simulating high-heat environments. In industrial or plant exhaust settings, heat from the flue gas exhaust can complement the integrated bioreactor heating element, allowing for lower thermal energy consumption. Multi-element mixers agitate exponentially more slurry surface area versus commonly used single-stage agitators, which helps increase the time to precipitation at high temperatures.

[0037] During precipitation from mineral carbonation, past research and experiments have found that a passivating silicone layer, or PL, forms and reforms during the carbonation process, inhibiting the time to precipitate carbonates. Natural weathering of mineral and rock formations results in a laterite layer, a weathered surface area. The laterite layer prevents or inhibits weathering of the underlying unweathered mineral surface area unless the layer is destroyed, exposed, or removed. The disclosed multi-element mixer operates at up to 1500 rpm to continuously chip away at the Passivating Layer (PL), which forms and reforms at high temperatures and pressures during the carbonation process. and destroy.

[0038] UV-C photolysis induces hydroxyl radicals (OH), which can then combine with leached calcium and magnesium silicates to produce hydroxides, which react with injected CO2, producing carbonates in an aqueous slurry that may contain additives or admixtures. The artificial UV-C light emitter disclosed as part of the reactor emulates the photodissociation of oxygen when exposed to UV-C light from sunlight, as occurs in ozone production in the upper atmosphere. Photolysis, also known as photodissociation and photodecomposition, is a chemical reaction in which inorganic or organic chemicals are broken down by energetic photons, the interaction of one or more photons with a target molecule. The use of UV-C-directed light photolysis significantly improves the reaction time per reactor batch of mineral feedstock and CO2. Photolysis can potentially reduce carbonation times to one hour or less. Throughout the embodiments, references to UV or visible light radiation or irradiation are limited to non-ionizing wavelengths of UV and visible light waves.

[0039] Additionally, the disclosed reactor recovers energy consumed during the reaction process through the implementation of a blade tip ring permanent magnet generator. The mixer turbine acts as the generator's rotor and is surrounded by a stator ring housing with windings to complete the generator configuration. Additionally, a pressure energy recovery system that transfers and reinjects waste pressure during and after the reaction is used as part of the disclosed reactor design to offset the energy input required to operate the reactor system.

[0040] FIG. 1A depicts the photolysis reactor, components, and subassemblies. The bioreactor system is divided into three major functional segments: A, B, and C. FIG. 1A depicts boundary separators that delineate the three major functional sections of the bioreactor system: A, B, and C. The boundary of section A begins at the electric motor housing 1 and ends at the straight pipe cap end 19 and flange 2. Section B begins at the end of section A and ends at the split retaining wall cap end flange 6. Section C begins at the end of section B and ends at the discharge tube 15. Section A is the power drive section, section B is the venturi nozzle section, and section C is the UV and visible light section. Each section is modular. Within section A, the electric motor is enclosed by the electric motor housing 1.

[0041] The electric motor within housing cover 1 is mounted to frame stand 9, which supports the electric motor. Alternating flange pairs 2 and 6, typically referred to as male-female slip-on flanges, are shown. Straight section pipe cap ends 19 are secured to flange 2 by welding. The flanges 2 are then joined together with high-strength, high-temperature fasteners 2.1. In section B, venturi nozzles 11, 12, 12.1, and 13 form the central pressure body of the bioreactor system of FIG. 1A. The geometry of the venturi nozzles in section B promotes improved fluid flow compared to a continuous, straight cylinder or tube. Venturi nozzle section 12 diverges toward straight section 11. Venturi nozzle section 12.1 diverges toward short, straight section tube 13. Straight section tubes 11 and 13 in section B are attached to alternating flanges 2 and 6 by welding. Welded to the back of flange 6 at section C is a cap end tube with a split retaining wall comprising the components of section C, and the cap end tube with split retaining wall is surrounded by a UV nacelle-shield fairing 8. Attached to UV nacelle-shield fairing 8 is an exhaust nozzle 15 connected to a sleeved support tube 14 that facilitates 360° rotation of exhaust tube 15. UV nacelle-shield fairing 8 is a modular section that can be removed from or secured to the split retaining wall cap end tube by clamps 7.

[0042] The sleeved support tube 14 allows the discharge nozzle 15 to rotate 360° (degrees) to direct the ozone waste to water tanks or storage bins at different stack heights. Ozone (chemical formula O3) is generated during the batch reaction by dissociating ambient oxygen (chemical formula O2) with a high-intensity UV-C LED (light-emitting diode) and lamp. The UV nacelle-shield fairing 8 also provides a barrier shield against UV-C light, eliminating the possibility of human exposure to UV-C light energy during installation. Two ports 3 and 4 allow the injection of media feedstock and CO2 gas into section B, where the gas can then diffuse through sections A and B and exit section B of the bioreactor system. A heating element or heating band 5 controls the thermal environment of the reactor assembly in Figure 1A. The heating band 5 is installed around the outer diameter of the converging section 12.3 (see Figures 2C, 3B, 3D, and 6) or the constricting section of the venturi nozzle in section B. The reactor body and assembly of Figure 1A consists of two sections, 10 in Section A and 10.1 in Section B. Supported by block stands.

[0043] FIG. 1B is a right-hand isometric (ISO) view of the bioreactor assembly of FIG. 1A without the fairing cover 1 (FIG. 1A), and includes 3D detailed views of the electric motor 22, electric motor shaft 22.1, drive shaft coupling 22.2, main drive shaft 21, flanged cap end 2 (FIG. 1A, 2), and straight section pipe cap end 19 (FIG. 1A, 19), split retaining wall flanged cap end 6 (FIG. 1A, 6), heating band element 5 (FIG. 1A, 5), as well as a distant view of the configuration of the UV nacelle-shield fairing 8 (FIG. 1A, 8), and discharge nozzle 15 (FIG. 1A, 15). During operation, the electric motor 22 rotates the electric motor shaft 22.1, which is fixedly connected to the shaft coupling 22.2, which is fixedly connected to the main drive shaft 21, which may or may not be the same diameter as the electric motor shaft 22.1. Rotation can be performed at variable speeds of 1 to 1800 revolutions per minute under ambient pressure and in gas mixtures or CO2 partial pressures up to 2200 pounds per square inch (psi), or in vacuum environments approaching -5 psi or -517 torr.

[0044] Rotation of the main drive shaft 21 imparts rotation to the mixer-agitator turbine, which agitates, mixes, and disperses the slurry and / or media, and any other liquid, solid, or gaseous feedstocks, organic or inorganic, within the reactor. The term slurry is defined as a mixture of inorganic mineral feedstocks of various particle sizes combined with water and additives. The slurry may be premixed and injected into the reactor, or it may be generated within the reactor from separate injections of water, additives, and inorganic mineral feedstocks.

[0045] The Venturi effect and the placement of electric band heaters or electric heating elements 5 (FIG. 1A, 5) on the outer surface of the constricted section of the Venturi nozzle 12, 12.1 (FIG. 1A, section B) distribute heat evenly throughout sections A, B, and C of FIG. 1A and the bioreactor assembly of FIG. 1B via mixer rotation. The discharge nozzle 15 (FIG. 1A), sleeved support tube 14 (FIG. 1A), and additional slurry injection port 4.1 are shown relative to the UV nacelle-shield fairing 8 (FIG. 1A). Additional injection ports 34 for gases, inorganic slurry port 35, organic culture port 36, and nutrients and general additive port 37 for organic culture are shown mounted along the surface of the Venturi nozzle section 12 (FIG. 1A).

[0046] FIG. 1C is an isometric close-up view of the electric motor 22 (FIG. 1B) without the motor fairing-housing 1 (FIG. 1A), depicting the shaft coupling 22.2 (FIG. 1B), the main drive shaft 21 (FIG. 1B), at least one seal-bearing shaft support assembly 20, at least one retaining shaft support plate 20.1, fasteners 41, and the cap end flange 2 (FIGS. 1A, 1B) with the straight pipe section 19 (FIGS. 1A, 1B).

[0047] Figure 2A shows in cross section the mixer-agitator axial turbines 25, 25.1, 25.2 and 26, 26.1, and 26.2, which are multi-element configurations for permanent and intermittent mixing of the reacting medium within the venturi reactor body sections 12, 12.1, 11, and 13 (Figures 1A and 1C). The main drive shaft 21 (Figures 1B and 1C) is shown extending horizontally from the shaft coupling 22.2 (Figures 1B and 1C) and passing through the seal-bearing shaft support assembly 20 (Figure 1C). The main drive shaft 21 (Figures 1B and 1C) passes through the venturi nozzle sections 12, 12.1, 11, and 13 (Figures 1A and 1B) and terminates in the venturi nozzle diverging section 13 (Figure 1A). Mixer-agitator axial turbines 25, 25.1, 25.2 and 26, 26.1, 26.2 agitate the medium under reaction. The crucible 17 is enclosed within the divided retaining wall cap end 24, flange 6 (Fig. 1B, Fig. 1A). Transparent or The translucent material forms the crucible 17, and the transparent or The translucent material allows transmission of UV and visible light emitted from an array of UV LEDs (light emitting diodes) and visible light emitters 23, which are mounted circumferentially on a plate structure 16 surrounding a split retaining wall cap end 24. Support for the electric motor 2 (FIGS. 1B, 1C) is provided by a platform support structure 9 (FIG. 1A). Sections A, B, and C of FIG. 1A are depicted for reference.

[0048] A UV or visible light emitter 23 can irradiate the medium at high or low temperatures, high or low pressure, or under vacuum to enhance the reaction rate. An additional pressure tap port 4.1 allows high-pressure CO and steam to be injected into the turbine blades inside the venturi nozzle section 12, 12.1 (FIGS. 1A, 1B) to induce rotation of the mixer-agitator axial turbines 25, 25.1, 25.2 and 26, 26.1, 26.2, which in turn rotates the electric motor 22 (FIGS. 1B, 1C, 22). Reinjecting CO and steam partially offsets the energy input from operating the bioreactor system of FIGS. 1A, 1B, 1C, 2A.

[0049] Band heaters or heating elements 5 (FIGS. 1A, 1B) are the primary heat source for controlling the thermal environment within the reactor body, sections A, B, and C (FIGS. 1B and 2A) of FIG. 1A. Once heat is distributed through the core, sections A, B, and C of the bioreactor assembly of FIG. 1A and optimal reaction temperatures are reached, CO2 and other inert gases can be injected through ports 4, 4.1 of FIGS. 1A and 1B and then enter the Venturi nozzle reactor cavity shown in FIGS. 1A, 1B, and 2A in supercritical and / or critical states, depending on the thermal gradient established by heating elements 5 shown in FIGS. 1A and 1B and the partial pressure of CO2 at the time of injection.

[0050] Figure 2B is a left-side perspective view of the complete bioreactor assembly of Figures 1A, 1B, and 2A, without the electric motor housing cover 1 of Figure 1A. The UV nacelle-shield fairing 8 (Figures 1B, 1A) is shown in Figures 1A and 1B, along with the discharge nozzle 15. Flanges 6 and 2 of Figures 1A, 1B, and 2A are depicted in the left-side perspective view. Port 4.1, shown in Figures 1A and 2A, and additional port 30 are shown. The electric motor 22, shown in Figures 1B, 1C, and 2A, and the shaft coupling 22.2, shown in Figures 1B, 1C, and 2A, are shown in their relative positions to the UV nacelle-shield fairing 8.

[0051] FIG. 2C is a perspective view of the left side of the bioreactor, beginning with the main drive shaft 21 shown in FIGS. 1B, 1C, and 2A and ending with the UV nacelle-shield fairing 8 shown in FIGS. 1A, 1B, and 2B. A cross-sectional perspective view of the venturi nozzle sections 12, 12.1, and 11 shown in FIGS. 1A, 1B, and 2A reveals that the mixer-agitator axial turbines 26.2, 26, 25, and 25.2 (FIG. 2A) are oriented along the main drive shaft 21 shown in FIGS. 1B, 1C, and 2A. Two perforated conical cylinders 33, 33.1 are shown attached to the inner walls of the venturi nozzle segments 12, 12.1 shown in FIGS. 1A, 1B, and 2A. The primary purpose of the perforated cylinders 33, 33.1 is to contain the inorganic and organic feedstocks separately from the remaining components of the reactor cavity.

[0052] For organic feedstocks, such as tissue culture, pre-filling the perforated cylinders 33, 33.1 with the tissue organic culture may be preferable to injecting the tissue culture. The perforations in each cylinder 33, 33.1 allow organic and inorganic nutrients to be injected into the reactor body cavity of Figures 1A, 1B, 2A, and 2B and flow into and out of the cylinders 33, 33.1. An additional port 31 is also shown.

[0053] FIG. 2D is an oblique view of the left side of the bioreactor system of FIGS. 1A, 1B, 2A, 2B, and 2C. The cross-sectional view shows the straight pipe cap end 19 (FIGS. 1A, 1C, and 2A). 2C)。 Main drive shaft 21 (FIGS. 1B, 1C, 2A, 2C) is depicted surrounded by at least three sealing glands 20.2 for pressurization. At least one bearing-seal support housing 20 (FIGS. 1C, 2C) for supporting main drive shaft 21 (FIGS. 1B, 1C, 2A, 2C) and at least one retaining support plate 20.1 (FIGS. 1C, 2C) are shown in cross section. A cross section of one of flange pairs 2 (FIGS. 1A, 1B, 1C, 2A, 2B, 2C) is also shown.

[0054] FIG. 3A is a close-up perspective view of a UV and visible light LED (light-emitting diode) emitter 23 and plate mount structure 16 (FIG. 2A) mounted around a split retaining wall cap end 24 (FIG. 2A) and flange 6 (FIGS. 1A, 1B, 2A, 2B, and 2C). The UV and visible light LED (light-emitting diode) emitter 23 directs UV and visible light, with wavelengths between 120 nm and 700 nm, through the transparent material forming crucible 17 (FIG. 2A) for photodissociating the medium and gas contents of the reactor assembly of FIGS. 1, 1B, 2A, 2B, 2C, and 2D. Crucible 17 (FIG. 2A) is hollow and of substantial thickness and material to handle pressurized pressures of up to 2200 psi.

[0055] A plurality of UV and visible light LEDs (light emitting diodes) and lamps 23 are housed and supported by a plate mount structure 16 (FIG. 2A). A crucible 17 (FIG. 2A) is sealed within a divided retaining wall 24 (FIG. 2A), a cap end flange 6 (FIGS. 1A, 1B, 2A, 2B, 2C). The divided retaining wall 24 (FIG. 2A) is attached to the cap end flange 6 (FIGS. 1A, 1B, 2A, 2B, 2C) by welding, threads, or other fastening methods, and is attached to or supported by a block mount 10.1 (FIGS. 1A, 2A).

[0056] Figure 3B is a biaxial view of the split retaining wall cap end 24 (Figures 2A, 3A). A cross-sectional view of the UV nacelle-shield fairing 8 (Figures 1A, 1B, 2B, 2C) reveals the placement and orientation of the UV and visible light source emitter 23 (Figure 3A) and plate mounting structure 16 (Figure 3A). Depicted is the split retaining wall cap end 24 (Figures 2A, 3A), the crucible 17 (Figures 2A, 3A) housed within the flange 6 (Figures 1A, 1B, 2A, 2B, 2C, 3A).

[0057] Figure 3C shows a 2D right-side elevation and cross-sectional view of the reactor interior cavity of Figures 1A, 1B, 2A, 2B, 2C, 2D, and 3B. Optical fibers and fiber optic cables 39, 39.1 are depicted attached to the interior wall. Fiber optic cables 39, 39.1 transmit UV and visible light directly into the cavity to impinge on more surface area of ​​the slurry for photon interaction. A UV or visible light source emitter 40 with attached fiber optic cable 39, 39.1 is mounted on the outside of the split retaining wall cap end 24 (Figures 2A, 3A, and 3B).

[0058] FIG. 3D is a perspective view with cross-sections of the UV nacelle-shield fairing 8 (FIGS. 1A, 1B, 2B, 2C, 3B), the crucible 17 (FIGS. 2, 3A, 3B, 3B), and the venturi nozzle segments 12, 12.3, 12.1, 11 (FIGS. 1, 1B, 2A, 2B, 2C, 2D, 3B, 3C). A UV and visible light emitter 40 is shown with an attached fiber optic cable 39, 39.1 (FIG. 3C). The fiber optic cable 39, 39.1 (FIG. 3C) is shown originating from the emitter 40 located within the dividing wall retaining cap end 24 (FIGS. 2A, 3A, 3B, 3C). Fiber optic cables 39, 39.1 (Figure 3C) extend through the crucible 17 (Figures 2A, 3A, 3B, 3C) and terminate within the bioreactor cavity of the Venturi nozzle diverging segment 11 (Figures 1A, 2A, 2D). 1B, 2A.1, 2C, 3B) also show the duct passages 43.

[0059] FIG. 4 is a cross-sectional close-up perspective view of at least one mixer-agitator axial turbine 25.2 (FIGS. 2A, 2C) having a blade tip stator ring with windings 27. This configuration of the rotating mixer-agitator axial turbine rotor 25.2 (FIGS. 2A, 2C) and wound stator ring 27 is the configuration of a permanent magnet generator capable of generating DC power when the main drive shaft 21 (FIGS. 1B, 1C, 2A, 2C, 2D, 3D) is rotating. The tip of the mixer-agitator axial turbine rotor 25.2 (FIGS. 2A, 2C) is sealed inside the stator ring by the windings 27, generating DC current when rotating. The exposed mixer-agitator axial turbine surface area 25.2 (FIGS. 2A, 2C) is used to agitate and mix the media and / or slurry.

[0060] Figure 5 highlights the CO2 gas and other waste gas streams flowing through and out of the bioreactor cavity, as well as the return paths, depicted in the cross-sectional views of Figures 2A, 2C, 2D, and 3D. The directional thick arrows represent gas and slurry outlet port 31 (Figures 3D, 3C, 2D, 2C, and 2B) and additional port 30. The gas-slurry stream first enters filter 44, which strains and filters the slurry, circulating bypass gas through filter-strainer 44. During operation, the venturi nozzle section of Figure 1A, sections A, B, and C, and venturi nozzle sections 11, 12, and 12.1 (Figures 1B, 2A, 2C, 2D, 3C, and 3D), and the core of venturi nozzle section 13 (Figures 1A and 2A), are thermally conditioned and maintained at specific temperature levels for various time intervals to promote reaction of the media within the reactor. To offset the energy input required for the electric motor, heating, and compression, the pressure within the reactor is exhausted through pressure port 31 (FIGS. 2B, 2C, 2D, 3C, 3D) and port 30. The arrows with black circles at the ends represent the flow of CO2 and exhaust steam outside the bioreactor assembly. The CO2 and exhaust steam pass through liquid-gas booster pump 28, which increases the pressure of the CO2 and steam. The CO2 and steam are reinjected through additional pressure port 29, and the flow is focused into mixer-agitator axial turbine 42 (FIG. 3D) or any other mixer-agitator axial turbine 26.2, 26.1, 26, 25, 25.1, 25 (FIGS. 2A, 2C, 2D, 3D) to induce rotation of main drive shaft 21 (FIGS. 1B, 1C, 2A, 2C, 2D, 3D). The torque then rotates the electric motor-generator 22 (FIGS. 1B, 1C, 2A, 2B), generating DC current. The power generated from the steam and CO2 reinjection is available for consumption or storage, thereby potentially offsetting the power input required to operate the reactor system.

[0061] FIG. 6 depicts the Venturi nozzle cavity section B of FIG. 1A in cross section. Housed within cavity segment B of FIG. 1A are at least two perforated containers 33, 33.1 (FIGS. 2C, 2D, 3D) that can store inorganic and organic media, such as mineral feedstocks, if inorganic materials are used, or if the application is cell culture food. The perforated containers 33, 33.1 (FIGS. 2C, 2D, 3D) can house cell tissue cultures. The perforated containers 33, 33.1 (FIGS. 2C, 2D, 3D) can be attached to the inner wall of the Venturi reactor cavity of segment B of FIG. 1A, allowing the main drive shaft 21 (FIGS. 1B, 1C, 2A, 2C, 2D, 3D, 4) to pass through the bore sections of the perforated containers 33, 33.1 (FIGS. 2C, 2D, 3D). The above-described mounting method can also facilitate the distribution of heat, cooling, gas, liquid, mineral and nutrient flow through the organic or inorganic medium contained within the perforated container 33, 33.1 (Figures 2C, 2D, 3D).

[0062] Mixer-agitator axial turbines 26.2, 26.1, 25.1, 25.2 (FIGS. 2A, 2C, 2D) are mounted on the main drive shaft 21 (FIGS. 1B, 1C, 2A, 2C, 2D, 3D, 4) and can be solid, liquid, and gas or a combination thereof. The venturi nozzle provides mixed flow and dispersion of inorganic or organic media, such as nutrient broth. Rotation of the mixer-agitator axial turbines 26.2, 26.1, 25.1, 25.2 (FIGS. 2A, 2C, 2D) uniformly distributes the heat and cooling fluid flow at various revolutions per minute (rpm) to the inorganic or organic media throughout the reactor cavity, as well as to inorganic and organic media, such as cell tissue cultures, contained in perforated vessels 33, 33.1 (FIGS. 2C, 2D, 3D). Figure 6 shows ports 34, 35, 36, 37 (FIG. 1B) and an additional port 38 mounted on the exterior wall of the venturi nozzle reactor segment 12 (FIGS. 1A, 1B, 2A, 2C, 2D, 3B, 3C, 3D, 5).

[0063] Each port 34, 35, 36, 37 (FIG. 1B), and 38 can be arbitrarily designated. For example, gas can be injected through port 34 (FIG. 1B), port 35 (FIG. 1B) for mineral feedstock, or liquid can be injected through port 36 (FIG. 1B), or solids can be injected through port 37 (FIG. 1B), and inorganic or organic slurry can be injected through additional port 38. The injection of liquids, solids, and gases facilitates a non-contact feedstock loading method to minimize and prevent contaminant disruption of carbonation or nucleation of inorganic mineral feedstock by CO gas and multi-nucleation of organic feedstock, primarily tissue cell cultures housed in perforated vessels 33, 33.1 (FIGS. 2C, 2D, 3D).

[0064] The heating unit or heating element 5 (FIGS. 1A, 1B, 2A, 2B, 2C, 2D, 3D), depicted as a trapezoid, generates a waste heat flow, indicated by the directional thick arrows, which is then conducted via a heat exchanger, thermocouple, or other type of thermally conductive material to the thermal generator 32 of FIG. 6. The thermoelectric generator or TEG 32 is an energy recovery device that utilizes the heat flux from the reactor exterior of segments A, B, and C of FIG. 1A and the heating band elements 5 (FIGS. 1A, 1B, 2A, 2B, 2C, 2D, 3D) to generate electricity via the Seebeck effect.

[0065] Figure 7 shows a detailed perspective view of only the perforated cylinders 33, 31 (Figures 2C, 2D, 3D) oriented along the main drive shaft 21 (Figures 1B, 1C, 2A, 2C, 2D, 3D, 4, 6). The mixer-agitator axial turbines 26.2, 26.1, 25.1, 25.2 (Figures 2A, 2C, 2D, 6) rotate in any direction at variable rpm for purposes of mixing reacting liquids, solids, and gases, mechanical activation pretreatment, media surface agitation, heating, cooling, and fluid and media dispersion.

[0066] FIG. 8 is a biaxial view of a multi-port configuration referenced throughout the description of this embodiment. It illustrates the ports of the venturi nozzle module of section B (FIGS. 1A and 2A). The configuration, location, and number of ports may vary based on the application and the type of media injected into the venturi nozzle module of section B of FIGS. 1A and 2A. Two heating bands or heating elements 5 (FIGS. 1A, 2A, 2B, 2C, 2D, 3D, and 6) are depicted circumferentially mounted in the converging section of the venturi nozzle module 12.3 (FIGS. 2C, 3B, 3C, 6), section B of FIGS. 1A and 2A. Ports 34, 35, 36, 37, 38 (Figure 6) are shown with spatial reference to port 31 (Figures 5, 3C, 2D, 2C, 2B), port 30 (Figure 5), port 4.1 (Figures 1B, 2A, 2B, 2C, 2D, 3B, 3C, 3D, 6), port 4 (Figures 1A, 2A), port 3 (Figure 1A), and port 29 (Figure 5).

[0067] The foregoing detailed description of exemplary and preferred embodiments is presented for purposes of illustration and disclosure in accordance with statutory requirements. It is not intended to be exhaustive or to limit the invention to the precise form described, but is intended only to enable one skilled in the art to understand how the invention may be adapted for a particular use of implementation. Possibilities for modification and variation will be apparent to those skilled in the art. Specific examples, including tolerances, feature dimensions, specific operating conditions, technical specifications, etc., are within the scope of the present invention. No limitation is intended by the description of exemplary embodiments, which may vary from implementation to implementation or as the state of the art changes, and no limitation should be inferred therefrom. This disclosure is made with respect to the current state of the art, but contemplates advances, and future adaptations may take these advances into account, i.e., conform to the then-current state of the art.

Claims

1. 1. A photolysis bioreactor system for converting CO by reaction with a CO reaction feedstock to produce a carbonate reaction material, comprising: a central pressure body portion comprising a converging-diverging venturi nozzle extending along a horizontal axis; a heating band disposed about an outer diameter of the converging section of said converging-diverging venturi nozzle; a mixer-agitator assembly comprising a plurality of axial turbines mounted on a drive shaft along the horizontal axis to selectively rotate an axial aqueous slurry having an initial composite comprising the CO2 reaction feedstock and input slurry within the converging-diverging venturi nozzle, the mixer-agitator assembly being rotatable in clockwise and counterclockwise directions as selected by a power module portion comprising a direction-selectable electric motor connected to drive the drive shaft; at least one port inlet into the converging-diverging venturi nozzle for providing an inlet flow of CO2 into the converging-diverging venturi nozzle; and at least one port inlet into the converging-diverging venturi nozzle for providing an entry flow of the input slurry into the converging-diverging venturi nozzle; a venturi nozzle section comprising: An optical section, a crucible formed with walls translucent to light, the optical section having at least one optical emitter source connected to an open end of the converging-diverging venturi nozzle, whereby the axial flow aqueous slurry flows into the crucible, and the at least one optical emitter source is directed into the crucible to irradiate and react the CO2 reaction feedstock in the axial flow aqueous slurry to produce a carbonate product; The light section and A power module section, the drive shaft extending from the venturi nozzle section to the power module section; and a reversible motor connected to said drive shaft, said reversible motor being selectively operable for selected directions of rotation; a power module section comprising: whereby, during operation of the system, incoming CO2 reacts with the initial slurry.

1. A photolytic bioreactor system in which the feedstock is continuously intermixed to cause a reaction to occur and provide a carbonate reaction material as a product of said feedstock.

2. 10. The photolytic bioreactor of claim 1, wherein the at least one light emitter source comprises an ultraviolet light emitter source.

3. 10. The photolytic bioreactor of claim 1, wherein the at least one light emitter source comprises a visible light emitter source.

4. 10. The photolytic bioreactor of claim 1, further comprising an organic feedstock in the axial flow aqueous slurry enclosed within at least one perforated cylinder contained within the reactor for multinucleation of cell tissue culture.

5. 10. The photolytic bioreactor of claim 1, wherein at least one optical fiber strand and at least one optical fiber cable are installed along the interior walls of the bioreactor for the purpose of irradiating the organic feedstock, organic and inorganic media, and inorganic and organic components of the axial flow aqueous slurry under reaction within the bioreactor.

6. 10. The photolytic bioreactor of claim 1, further comprising at least one thermoelectric generator for converting waste heat into electricity.

7. 10. The photolytic bioreactor of claim 1, further comprising at least one permanent magnet generator enclosed around said axial turbine for the purpose of generating electricity to offset the energy consumed from the operation of said reactor.

8. 10. The photolytic bioreactor of claim 1, wherein the light section further comprises a visible light emitting source for irradiating and reacting selected feedstocks in the axial flow aqueous slurry.

9. 10. The photolytic bioreactor of claim 1, wherein the source of CO2 is from at least an industrial exhaust.

10. 10. The photolytic bioreactor of claim 1, wherein the source of CO2 is from at least industrial emissions and direct air capture CO2.

11. 1. A method for producing a carbonate reaction material, comprising: collecting an initial slurry and a CO2-containing input slurry; processing the collected input slurry in a converging-diverging venturi nozzle section of a bioreactor, the bioreactor comprising: a central pressure body portion comprising a converging-diverging venturi nozzle extending along a horizontal axis; a heating band disposed about an outer diameter of the converging section of said converging-diverging venturi nozzle; a mixer-agitator assembly comprising a plurality of axial turbines mounted on a drive shaft along the horizontal axis to selectively rotate an axial aqueous slurry having an initial composite comprising a CO2 reaction feedstock and an input slurry within the converging-diverging venturi nozzle, the mixer-agitator assembly being rotatable in clockwise and counterclockwise directions as selected by a power module portion comprising a direction-selectable electric motor connected to drive the drive shaft; at least one port inlet into the converging-diverging venturi nozzle for providing an inlet flow of CO2 into the converging-diverging venturi nozzle; and to provide an entrance flow of the input slurry into the converging-diverging venturi nozzle, At least one port inlet into the converging-diverging venturi nozzle and looping the axial aqueous slurry back into the converging-diverging venturi nozzle section by selectively rotating the mixer-agitator assembly clockwise and counterclockwise; a crucible of translucent, optically transparent material connected to the open end of the converging-diverging venturi nozzle, wherein the axial flow aqueous slurry flows into the crucible, and at least one optical emitter source is directed into the crucible to irradiate and react the CO2 reaction feedstock in the axial flow aqueous slurry to produce a carbonate product; moving the axial flow aqueous slurry through an optical section comprising: irradiating the crucible with light from at least one light emitter source to react the CO2 reaction feedstock in the axial flow aqueous slurry to produce the carbonate product; and outputting the axial flow aqueous slurry from the converging-diverging venturi nozzle. whereby during operation of the bioreactor system, incoming CO2 reactively intermixes with the axial flow aqueous slurry to continuously cause a reaction and provide a carbonate reaction material as a product of the CO2 reaction feedstock.

12. The method of claim 11 , wherein the optical section further comprises at least one visible light emitter source.

13. The method of claim 11 , wherein the optical section further comprises at least one ultraviolet light emitter source.

14. 12. The method of claim 11, wherein the organic feedstock in the axial flow aqueous slurry is confined within at least one perforated cylinder contained within the bioreactor for multinucleation of cell tissue culture.

15. 12. The method of claim 11, wherein at least one optical fiber strand and at least one optical fiber cable are installed along the interior wall of the bioreactor for the purpose of irradiating the organic feedstock, organic and inorganic media, inorganic and organic components of the axial flow aqueous slurry under reaction within the bioreactor.

16. 12. The method of claim 11, wherein the bioreactor also comprises at least one thermoelectric generator for converting waste heat into electricity.

17. 12. The method of claim 11, wherein the bioreactor also comprises at least one permanent magnet generator enclosed around the axial turbine for the purpose of generating electricity to offset energy consumed from the operation of the reactor.

18. 12. The method of claim 11, wherein the source of CO2 is from at least industrial emissions.

19. 12. The method of claim 11, wherein the source of CO2 is from at least industrial emissions and direct air capture CO2.

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