Systems and Methods for Simultaneous Control of Carbon Dioxide and Nitric Oxide and Generation of Nitrous Oxide

Abstract

Systems and methods for simultaneous control of carbon dioxide and nitric oxide and generation of nitrous oxide are provided. In particular, the present invention provides systems and methods utilizing a titania-based photocatalyst to simultaneously control carbon dioxide and nitric oxide levels generated by combustion systems. Additionally, photoreduction of nitric oxide provided by the photocatalyst is used to generate nitrous oxide.

Description

BACKGROUND OF THE INVENTION

1. Field of the Invention

This invention relates generally to photoreduction and, more specifically, to systems and methods for simultaneous photoreduction control of carbon dioxide and nitric oxide and generation of nitrous oxide.

2. Description of the Related Art

Nitric oxide (NO) and carbon dioxide (CO₂) are typically generated in combustion systems. Numerous techniques have been developed to control NO, most of which employ either a modification of the combustion process or the addition of chemicals (e.g., an ammonia containing liquid such as urea). CO₂ is an important greenhouse gas that is currently a subject of concern due to the US Environmental Protection Agency's new Carbon Rule that limits carbon emissions from stationary combustion sources such as power plants. Thus, a need exists to replace current energy intensive NO_x control techniques for combustion sources (e.g., vehicles, electricity generating utilities, etc.) and simultaneously control carbon dioxide levels.

SUMMARY OF THE INVENTION

The present invention provides systems and methods for simultaneous control of carbon dioxide and nitric oxide and generation of nitrous oxide. In particular, the present invention provides systems and methods utilizing a titania-based photocatalyst to simultaneously control carbon dioxide and nitric oxide levels generated by combustion systems. Additionally, photoreduction of nitric oxide provided by the photocatalyst is used to generate nitrous oxide.

In one aspect, the present disclosure provides a photoreduction system for a fluid stream. The fluid stream includes at least carbon dioxide and nitric oxide therein. The photoreduction system includes a catalyst arranged such that the fluid stream flows over a surface region of the catalyst, and a light source configured to illuminate the surface region of the catalyst. When the light source illuminates the surface region of the catalyst, a concentration of the carbon dioxide and a concentration of the nitric oxide in the fluid stream are reduced as the fluid stream flows over the surface region. The fluid stream may be a post-combustion stream.

In another aspect, the photoreduction system generates nitrous oxide when the concentration of nitric oxide is reduced as the fluid stream flows over the surface region.

In one aspect, the catalyst of the photoreduction system comprises a metal oxide. The metal oxide may have a band gap energy between 2 and 5 eV, or between 2.5 and 4.5 eV, or between 3 and 3.5 eV. In another aspect, the metal oxide comprises a dopant. In one aspect, the metal oxide comprises titanium dioxide. In one aspect, the titanium dioxide comprises a phase of anatase, brookite, rutile, and mixtures thereof. In some aspects, the phase of the titanium dioxide comprises a mixture of anatase and rutile. In other aspects, the dopant is a metal. In one aspect, the metal is selected from copper, platinum, silver, and mixtures thereof. In another aspect, the dopant is a non-metal. The non-metal may be iodine.

In another aspect, the catalyst can be copper modified titanium dioxide. The copper modified titanium dioxide is formed from reaction of a copper-containing compound and titanium dioxide particles having a mean diameter in a range of 10 to 50 nanometers. The copper modified titanium dioxide can have a copper content in a range of 0.01 to 5 wt. %, or in the range of 0.1 to 1 wt. %, or in the range of 0.2 to 0.8 wt. %.

In one aspect, the light source is configured to emit ultraviolet radiation. In some aspects, the catalyst consists essentially of copper modified titanium dioxide. In some aspects, the conversion of nitric oxide in the fluid stream is greater than 50%. In other aspects, the yield of nitrous oxide in the fluid stream is greater than 4%. In another aspect, the fluid stream includes flue gas.

In another aspect, the present disclosure provides a method for simultaneously controlling a carbon dioxide concentration and a nitric oxide concentration and generating nitrous oxide in a fluid stream. The method includes arranging a catalyst in the fluid stream such that the fluid stream flows over a surface region of the catalyst, and illuminating the surface region of the catalyst as the fluid stream flows over the surface region. The fluid stream may be a post-combustion stream.

In one aspect, the method includes a catalyst that comprises titanium dioxide. In another aspect, the catalyst comprises a material selected from the group consisting of anatase titanium dioxide, brookite titanium dioxide, rutile titanium dioxide, and mixtures thereof. In one aspect, the catalyst comprises a mixture of anatase titanium dioxide and rutile titanium dioxide. In another aspect, the catalyst comprises a material selected from the group consisting of copper modified titanium dioxide, iodine modified titanium dioxide, platinum modified titanium dioxide, silver modified titanium dioxide, and mixtures thereof. In one aspect, the catalyst comprises copper modified titanium dioxide.

In another aspect, the copper modified titanium dioxide is formed from reaction of a copper-containing compound and titanium dioxide particles having a mean diameter in a range of 10 to 50 nanometers, or in the range of 10 to 30 nanometers.

In one aspect, the method also includes copper modified titanium dioxide that has a copper content in a range of 0.01 to 5 wt. %, or in the range of 0.1 to 1 wt. %, or in the range of 0.2 to 0.8 wt. %. In another aspect, the method also includes illuminating the surface region of the catalyst which comprises emitting ultraviolet radiation from a light source towards the surface region of the catalyst.

In another aspect, the present disclosure provides a photocatalytic reaction system. The photocatalytic reaction system comprises a photocatalytic reactor having an interior space in fluid communication with an inlet and an outlet. The photocatalytic reactor also includes a light source to irradiate at least a portion of a catalyst in the interior space. The photocatalytic reaction system further includes a fluid separation unit in fluid communication with the outlet of the photocatalytic reactor. The fluid separation unit is configured to separate at least one product of a plurality of products received from the photocatalytic reactor. The photocatalytic reaction system further includes an analyzer in fluid communication with the fluid separation unit for receiving the plurality of products, the analyzer comprising a detector, a second light source, and a controller in electrical communication with the detector and a second light source. The controller executes a program stored in the controller to irradiate at least two products of the plurality of products using the second light source, generate an absorbance spectrum (A_meas) of the at least two products from electrical signals received from the detector, wherein the absorbance spectrum includes a co-eluting peak, and de-convolute the co-eluting peak to compute a concentration of one or more of the at least two products.

In one aspect, the analyzer includes a vacuum ultraviolet detector. In another aspect, the de-convolution of the co-eluting peak includes computing a calculated absorbance spectrum (A_calc) at one or more wavelengths according to:

A _calc =k(σ₁N₁+σ₂N₂+ . . . +σ_nN_n);

wherein σ_n are cross section spectra (cm²/molecule), and N_n is total number of molecules for the one or more of the at least two products.

In one aspect, the de-convolution of the co-eluting peak includes computing a reference spectral absorbance (A) at one or more wavelengths according to:

A=(f₁A_1,ref+f₂A_2,ref+ . . . f_nA_n,ref);

wherein f_n is a fitting parameter to be optimized, and A_n,ref is the absorbance from an individual reference spectrum for the one or more of the at least two products.

In another aspect, the de-convolution of the co-eluting peak includes linear optimization by using a scaling parameter to match the absorbance spectrum (A_meas) to the reference spectral dictionary (A) or the calculated absorbance spectrum (A_calc). In one aspect, the scaling parameter is selected from the group consisting of f_n and N_n. In another aspect, the de-convolution of the co-eluting peak includes generating individual absorbance spectrum for each of the at least two products.

In one aspect, the individual absorbance peaks are integrated to calculate the concentration of each of the at least two products. In another aspect, the one or more wavelengths are between 120 and 250 nm. In one aspect, the fluid separation unit includes a gas chromatography column. In another aspect, a transfer line that is heated to a first temperature is configured to place the fluid separation unit in fluid communication with the analyzer. In one aspect, the first temperature is between 250° C. to 350° C. In another aspect, the transfer line is configured with an inert gas inlet at a first pressure. In one aspect, the first pressure is between 0.2 to 5 psi.

In another aspect, the present disclosure provides a method for determining the concentration of at least two products of a plurality of products from a photocatalytic reaction system. The method includes acquiring an absorbance spectrum (A_meas) of at least two products of a plurality of products using an analyzer where the absorbance spectrum including a co-eluting peak, de-convoluting the co-eluting peak by generating an individual absorbance spectrum for the at least two products, and computing a concentration for one or more of the at least two products based on the individual absorbance spectrums.

In one aspect, the analyzer in the method includes a vacuum ultraviolet detector. In another aspect, step (b) further includes computing a calculated absorbance spectrum (A_calc) at one or more wavelengths according to:

A _calc =k(σ₁N₁+σ₂N₂+ . . . +σ_nN_n);

wherein σ_n are cross section spectra (cm²/molecule), and N_n is total number of molecules for the one or more of the at least two products. In one aspect, step (b) further includes computing a reference spectral absorbance (A) at one or more wavelengths according to:

A=(f₁A_1,ref+f₂A_2,ref+ . . . +f_nA_n,ref);

wherein f_n is a fitting parameter to be optimized, and A_n,ref is the absorbance from an individual reference spectrum for the one or more of the at least two products.

In one aspect, step (b) further includes linear optimization by using a scaling parameter to match the absorbance spectrum (A_meas) to the reference spectral dictionary (A) or the calculated absorbance spectrum (A_calc). In another aspect, the scaling parameter is selected from the group consisting of f_n and N_n.

In another aspect, step (c) further includes integrating the individual absorbance spectrums to calculate the concentration for the one or more of the at least two products.

In another aspect, the present disclosure provides a method for analyzing a sample derived from a photocatalytic reaction. The method steps include using gas chromatography coupled with vacuum ultraviolet detection for analyzing gaseous species in the sample.

In another aspect, the present disclosure provides a method for analyzing a sample derived from a photocatalytic reaction. The method steps include using gas chromatography coupled with thermal conductivity detection for analyzing gaseous species in the sample.

These and other features, aspects, and advantages of the present invention will become better understood upon consideration of the following detailed description, drawings and appended claims.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 shows a photoreduction system according to one aspect of the present disclosure.

FIG. 2 shows a photocatalytic reaction system according to one aspect of the present disclosure.

FIG. 3 shows a method of de-convoluting a co-eluted absorbance spectrum according to one aspect of the present disclosure.

FIG. 4 shows an experimental setup to test the photoreduction system of FIG. 1.

FIG. 5 is a graph illustrating a full GC-VUV chromatogram of species according to one aspect of the present disclosure.

FIG. 6 shows graphs of absorbance spectra of various analytes.

FIG. 7 is a graph illustrating CO formation over P25 TiO₂ and Cu—TiO₂ catalysts in the presence of CO₂/H₂O and CO₂/H₂O/NO as a function of reaction time.

FIG. 8 is a graph illustrating NO degradation over P25 TiO₂ and Cu—TiO₂ catalysts in the presence of CO₂/H₂O and CO₂/H₂O/NO as a function of time.

FIG. 9 is a graph illustrating N₂O formation over P25 TiO₂ and Cu—TiO₂ catalysts in the presence of CO₂/H₂O and CO₂/H₂O/NO as a function of time.

FIG. 10 is a graph illustrating O₂ formation over P25 TiO₂ and Cu—TiO₂ catalysts in the presence of CO₂/H₂O and CO₂/H₂O/NO as a function of time.

DETAILED DESCRIPTION OF THE INVENTION

The conversion of CO₂ to value-added products (i.e., fuels, chemical feedstocks) can be implemented to enhance current post-combustion carbon capture and sequestration (CCS) technologies. Typically composed of approximately 10-12% CO₂, by volume, flue gas from large-point stationary sources, such as coal fired power plants, is considered a highly practical source for CO₂ conversion technologies. Various approaches have been developed to convert CO₂ to value-added products including: electrochemical, photochemical, photo-electrochemical, and photocatalytic conversion. Among these approaches, photocatalytic reduction of CO₂ is particularly attractive due to sunlight being the only energy input.

One such approach for photocatalytic reduction of CO₂ utilize titania (TiO₂)-based materials as a catalyst for UV-driven CO₂ conversion in the presence of water. The band gap energies of its most widely studies polymorphs—anatase (3.24 eV) and rutile (3.03 eV)—makes TiO₂ an ideal choice among other semiconductor materials.

In regard to determining the applicability of a CO₂ photoreduction technology to current post-combustion CCS technologies, it is important to consider various factors that may influence its performance. For example, post-combustion streams generally contain impurities (e.g., oxides of nitrogen NO_x, and oxides of sulfur SO_x) that may impact the CO₂ photoreduction process. Typically, nitric oxide (NO) accounts for 90-95% of the NO_x contained in flue gas. In a typical post-combustion stream, NO concentrations can range between 500 and 1000 parts per million (ppm) by volume.

As will be described, the present disclosure provides an approach that can control a CO₂ concentration, by photoreduction, in the presence of impurities in a post-combustion stream. Additionally, the approach described herein simultaneously enables the control of an NO concentration, by photoreduction, in post-combustion streams. The photoreduction of NO further enables the approach described herein to produce nitrous oxide, which is a commodity utilized by the semiconductor and medical industries.

FIG. 1 shows one non-limiting example of a photoreduction system 100 configured to control CO₂ and NO levels in an effluent stream 106. The photoreduction system 100 includes a catalyst 102 and a light source 104. In one embodiment, the catalyst 102 is arranged within the photoreduction system 100 such that the effluent stream 106 flows over at least one surface region of the catalyst 102. The catalyst 102 and the light source 104 are configured within the photoreduction system 100 such that the light source 104 can illuminate the surface region of the catalyst 102 to promote the conversion of carbon dioxide and nitric oxide in the effluent stream 106 to at least produce nitrous oxide and carbon monoxide.

It should be appreciated that the illustrated arrangement of the catalyst 102 is not meant to be limiting and, in other non-limiting examples, the catalyst 102 may be suspended within the photoreduction system 100 such that the effluent stream 106 flows over any number of surfaces of the catalyst 102. In some non-limiting examples, the catalyst 102 can be arranged within the photoreduction system 100 to form a fixed bed reactor, a fluidized bed reactor, or the like.

The light source 104 is arranged to irradiate the catalyst 102 with electromagnetic radiation. In one embodiment, the light source 104 is configured to irradiate the catalyst 102 to promote photoexcitation. Photoexcitation occurs when energy that is equal or greater than a band gap energy is delivered to the catalyst 102. In one non-limiting example, the light source 104 can be configured to emit ultraviolet radiation, in a wavelength range between approximately 300 nanometers (nm) and 400 nm, onto the catalyst 102. The light source 104 may be in the form of a lamp, a laser, one or more light emitting diodes, or any other device configured to emit electromagnetic radiation. The irradiation of the catalyst 102 provided by the light source 104 can facilitate the photoreduction of certain chemical species present in the effluent stream 106. In some embodiments, the light source 104 can be configured within the photoreduction system 100. In other embodiments, the light source 104 can be configured outside of the photoreduction system 100 and optical fibers, for example, may be used to facilitate the irradiation of the catalyst 102 with the light source 104.

In some embodiments, the catalyst 102 can comprise a metal oxide. In some non-limiting examples, the catalyst 102 comprises the metal oxide modified with a dopant. In some non-limiting examples, the dopant can include a metal. Suitable metals may include copper, platinum, silver, and mixtures thereof. In some embodiments, the dopant can include a non-metal. Suitable nonmetals may include iodine and the like. In another non-limiting example, the catalyst 102 may include a metal oxide that has a band gap energy that is between 2 and 5 eV, or between 2.5 and 4.5 eV, or between 3 and 3.5 eV.

In some embodiments, the effluent stream 106 can be any fluid stream that includes at least carbon dioxide and nitric oxide therein. In other embodiments, the effluent stream 106 could include any flue gas or post-combustion stream. In some non-limiting examples, the effluent stream 106 could include a post-combustion or flue gas stream from any of the following industries: gas, oil refining, pulp and paper industry, gas separation industries, waste management companies, or the like.

In some embodiments, a suitable catalyst 102 can include a metal oxide that comprises titanium dioxide. In other embodiments, the metal oxide can consist essentially of titanium dioxide. In other embodiments, the titanium dioxide includes a phase that comprises anatase titanium dioxide, brookite titanium dioxide, rutile titanium dioxide, and mixtures thereof. A brookite TiO₂, particularly one that has many oxygen vacancies, may result in more conversion of CO₂ to CO. In another non-limiting example, the catalyst 102 can be fabricated from a mixture of anatase titanium dioxide and rutile titanium dioxide. In another non-limiting example, the catalyst 102 can be fabricated from a material that comprises copper modified titanium dioxide, iodine modified titanium dioxide, platinum modified titanium dioxide, silver modified titanium dioxide, and mixtures thereof. In another non-limiting example, the catalyst 102 can be fabricated from P25 titanium dioxide (TiO₂). In another non-limiting example, the catalyst can be fabricated from copper modified TiO₂ (Cu—TiO₂).

In some embodiments, the copper modified titanium dioxide is formed from a reaction of a copper-containing compound and titanium dioxide particles. In some aspects, the titanium dioxide particles have a mean diameter in a range between 10 to 50 nanometer, or between 10 to 30 nanometers. In one non-limiting example, the reaction of the copper-containing compound includes incipient wetness following by a heating step such as drying or calcination. In some embodiments, the copper modified titanium dioxide has a copper content in a range of 0.01 to 5 wt. %, or between 0.1 to 1 wt. %, or between 0.2 to 0.8 wt. %.

In operation, the light source 104 is configured to illuminate the catalyst 102 as the effluent stream 106 flows over the catalyst 102. As the effluent stream 106 flows over the illuminated catalyst 102, carbon dioxide and/or nitric oxide present in the effluent stream 106 can be photocatalytically reduced, as will be described in detail below. Thus, the photoreduction system 100 enables the control of a carbon dioxide concentration and a nitric oxide concentration downstream of the catalyst 102. The photoreduction of the carbon dioxide and the nitric oxide in the effluent stream 106 can lead to the generation of carbon monoxide and nitrous oxide, respectively, as will be described in detail below. In some embodiments, the catalyst 102 enables a conversion of nitric oxide in the effluent stream 106 that is greater than 50%, and a yield of nitrous oxide in the fluid stream that is greater than 4%. One or more of these generated commodities may be harvested and supplied to other industries (e.g., semiconductor industry, medical industry).

FIG. 2 shows one non-limiting example of a photocatalytic reaction system 200 configured to control CO₂ and NO levels from a post-combustion fluid stream. The photocatalytic reaction system 200 includes a photocatalytic reactor 204 in fluid communication with a fluid separation unit 206 and an analyzer 208. The photocatalytic reaction system 200 further includes a controller 210 in electrical communication with the analyzer 208.

In one embodiment, the photocatalytic reactor 204 includes an interior space 212 in fluid communication with an inlet 214 and an outlet 216 fluid stream. The photocatalytic reactor 204 also includes a light source 218 configured to irradiate at least a portion of a catalyst 220 in the interior space 212. In some embodiments, the fluid separation unit 206 is in fluid communication with the outlet 216 of the photocatalytic reactor 204 where it is configured to receive at least one product of a plurality of products from the photocatalytic reactor 204. In some embodiments, the separation unit includes a gas chromatography column.

In some embodiments, the analyzer 208 is in fluid communication with the fluid separation unit 206 and is configured to receive the plurality of products from the separation unit 206. In some embodiments, a transfer line is configured to place the separation unit 206 in fluid communication with the analyzer 208. In some aspects, the transfer line is heated to a first temperature. The first temperature can range between 250 and 350° C. In some embodiments, the transfer line also includes an inert gas inlet 224 that is in fluid communication with a pressurized tank 226. In some aspects, the pressurized tank 226 includes nitrogen or any suitable inert gas. In some embodiments, the pressurized tank 226 is configured to regulate the transfer line to a first pressure. In some aspects, the first pressure is between 0.2 to 5 psi. In other aspects, the first pressure is between 0.4 to 0.8 psi.

In some embodiments, the analyzer 208 includes a second light source, a sample tube configured to transport the plurality of products, and a detector. In one non-limiting example, the second light source is configured to irradiate the sample tube at one or more wavelengths, and a detector is configured to receive the transmitted light that passes through the sample tube. In some embodiments, the controller 210 is in electrical communication with the detector and the second light source. In one non-limiting example, the controller 210 includes a display 222, one or more input devices 224 (i.e., a keyboard, a mouse, etc.), and a processor 226. The processor 226 may include a commercially available programmable machine running on a commercially available operating system. The controller 210 provides an operator interface that facilitates entering in operating wavelengths for the second light source, and allows data received from the detector to be processed.

As mentioned above, one aspect of the present disclosure is to provide a system and method for producing nitrous oxide and carbon monoxide from a post-combustion stream using a photoreduction catalyst. As will be described below, another aspect of the present disclosure is to provide a system and method for accurately analyzing gas phase products derived from photoreduction reactions. One of the challenges associated with such a system is that many of the products from photoreduction reactions include chemically similar products (i.e. polarity, molecular weight, etc.), which has made it difficult to accurately quantitate the amount of all the products exiting the photoreactor due to co-elution of the products after the separation unit. As will be used herein, a co-eluting peak or co-elution may refer to an absorbance spectrum that contains one or more product in a single absorbance peak.

Referring to FIG. 3, another aspect of the present disclosure is to provide a method 300 for de-convoluting absorbance spectrum that include one or more co-eluting peaks to determine the individual concentrations of photocatalytic reaction products using the photocatalytic reaction system 200.

In operation, the controller 210 in the photocatalytic reaction system 200 executes a program stored to acquire an absorbance spectrum at step 302. In some embodiments, acquiring an absorbance spectrum includes irradiating at least two products of the plurality of products using the second light source in the analyzer 208. In some aspects, irradiating the at least two products occurs at one or more wavelengths between 120 and 250 nm. In some embodiments, acquiring an absorbance spectrum also includes generating an absorbance spectrum (A_meas) of the at least two products from electrical signals received from the detector, the absorbance spectrum including the co-eluting peak.

Next, the controller 210 de-convolutes the one or more co-eluting peaks at step 304. In some embodiments, step 304 includes de-convoluting the co-eluting peak and subsequently computing a concentration of the one or more of the at least two products. In some embodiments, the de-convolution step can include computing a calculated absorbance spectrum (A_calc) at one or more wavelengths according to:

A _calc =k(σ₁N₁+σ₂N₂+ . . . +σ_nN_n);   (1)

wherein σ_n are cross section spectra (cm²/molecule), and N_n is total number of molecules for the one or more of the at least two products. Alternatively, the deconvolution step can also include computing a reference spectral absorbance (A) at one or more wavelengths according to:

A=(f₁A_1,ref+f₂A_2,ref+ . . . +f_nA_n,ref);   (2)

wherein f_n is a fitting parameter to be optimized, and A_n,ref is the absorbance from an individual reference spectrum for the one or more of the at least two products. In some embodiments, the individual reference spectrum for the one or more of the at least two products are stored in a library in the controller 210. In some embodiments, the individual reference spectrum include oxygen, carbon monoxide, nitric oxide, methane, carbon dioxide, nitrous oxide, and water. Next, the reference spectral dictionary (A) or the calculated absorbance spectrum (A_calc) can be matched to the absorbance spectrum (A_meas) by using linear optimization and adjusting a scaling parameter. In some embodiments, the scaling parameter can include f_n or N_n. Once the scaling parameter has been optimally adjusted, equations (1) and (2) can be used to generate individual absorbance spectrum for the at least two products in the co-eluting peak at step 306. Next, the individual absorbance spectrum for the at least two products can be integrated to calculate the concentration of each of the at least two products 308.

EXAMPLES

The following examples set forth, in detail, ways in which the photoreduction system 100 may be used or implemented, and will enable one of skill in the art to more readily understand the principles thereof. The following examples are presented by way of illustration and are not meant to be limiting in any way.

The photocatalytic reduction of carbon dioxide (CO₂) in the presence of water (H₂O) vapor and nitric oxide (NO) over a titanium dioxide and a copper-modified Cu—TiO₂ photocatalyst was studied in a custom-designed cylindrical photoreactor system operating at room temperature. A gas chromatograph (GC) with a vacuum ultraviolet (VUV) detector was utilized to analyze the formation of gas phase products derived from CO₂ photoreduction over these TiO₂ materials in the presence and absence of NO. Experimental results indicate that a CO₂/H₂O system assists in the favorable formation of carbon monoxide (CO) over both TiO₂ and Cu—TiO₂. After 2 hours of UV illumination, the Cu—TiO₂ catalyst delivered a CO production amount of 3.51 μmol/g-catalyst. The photoreduction of CO₂ in the presence of H₂O and NO over the Cu—TiO₂ catalyst resulted in a decrease in CO formation (1.80 μmol/g-catalyst at two hours) using the same mass of catalyst, but also resulted in the formation of nitrous oxide (N₂O). In systems with NO, conversions of 53.3% and 72.5% of the starting NO concentrations of up to 1000 ppm (a level that is typical of combustion systems) were realized over the Cu—TiO₂ and TiO₂ catalysts, respectively. These photocatalytic systems resulted in nitrous oxide formation at levels of 29% N and 12.1% N, respectively. The balance of the converted nitrogen is likely N₂ since no other features were detected in the GC-VUV spectra, and nitrogen is the only specie that cannot be detected by the VUV detector due to its very low absorbance cross section as compared to other species. The variations in the amounts of nitrous oxide formed suggest that tuning of the catalyst can occur to generate the desired nitrous oxide production. The experiments were conducted at ˜298 K and 1 atm, utilizing up to approximately 820 ppm of NO and 3-4% v of CO₂, with 70% relative humidity. Ultraviolet lamps were used to initiate the chemistry.

Cu—TiO₂ Catalyst Preparation

Copper chloride dehydrate (CuCl₂.2H₂O, >99.0%, Sigma-Aldrich) and Aeroxide® TiO₂ P25 (≥99.5%, Sigma-Aldrich) were used as the precursor and starting TiO₂ material, respectively. Aeroxide® TiO₂ P25 is a fine white powder with hydrophilic character caused by hydroxyl groups on the surface. It comprises aggregated primary particles. The aggregates are several hundred nanometers in size and the primary particles have a mean diameter of approx. 21 nm. Particle size and density of ca. 4 g/cm³ lead to a specific surface of approx. 50 m²/g.

A one-step process was used to prepare Cu-modified TiO₂ (Cu—TiO₂). The incorporation of copper into the commercial P25 TiO₂ was achieved through an incipient wet impregnation process. Accordingly, 2 grams (g) of TiO₂ nanoparticles were dispersed in 100 mL of NaOH aqueous solution. Then, 25 milliliters (mL) of CuCl₂ solution was added drop-wise under magnetic stirring. After further stirring, the precipitates were washed and centrifuged with Nanopure water (18.1 MΩ) until a pH of 7 was obtained. The resulting material was dried at 80° C. overnight. The nominal copper content was kept at 0.5 wt. % because this amount of copper can correspond to an optimum photocatalytic activity level.

GC-VUV Instrumentation and Gas Standards

Recent studies have introduced the use of gas chromatography coupled with vacuum ultraviolet (GC-VUV) detection as a means for analyzing gaseous species. This technique provides universal detection of species through rapid light absorption measurements in the 115-240 nm wavelength region. All chemical species can absorb in this wavelength region, and possess unique and distinctive absorbance features that may be used for identification and quantification. In a typical GC-VUV system, eluting analytes from the GC's column pass through a heated transfer line into the VUV system's flow cell (10 cm long×1 mm inside diameter) together with make-up gas (N₂). The source module houses a deuterium lamp, which redirects and focuses light through the flow cell. The detector module houses a parabolic mirror to redirect light onto a diffraction grating which diffracts the light onto a back-thinned charged coupled device (CCD).

In this disclosure, a Bruker 456-GC (Scion Instruments, Inc., Fremont, Calif.) was coupled to a VGA-100 VUV detector (VUV Analytics, Inc., Austin, Tex.) and used to collect data from injected gas samples. The data collection rate for the VUV was set at 9 Hz. The transfer line and VUV flow cell temperatures were set at 300° C. and 275° C., respectively, and the make-up gas (nitrogen) was set to 0.61 psi. The GC column used was a fixed fused silica Q-plot column (30 mm×0.53 mm and average thickness of 20 μm, Bruker) and it was operated at a constant column flow rate of 8.3 mL/min with helium as a carrier gas. The GC temperature program started at 40° C., held for 4 minutes, and then increased to 120° C. at a rate of 20° C./min. The final temperature was held for 2 minutes. All injections were performed manually. This work represents the first ever study wherein a GC-VUV system is utilized to analyze the stable products derived from a photocatalytic reaction.

A series of standards were prepared to identify species of interest, as well as to create calibration curves (concentration vs. peak area of analyte) for the quantification of products formed. Compressed CO₂ (99%, Air Liquide), CH₄ (99.97%, Praxair), CO (90.85%, Praxair), NO (1000 ppm balanced in helium, Praxair) and N₂O (1 ppm balanced in N₂, Supelco, Sigma-Aldrich) were used as standards for positive identification and calibration.

Reactor Experiments: Photoreduction of CO₂ in the Presence of Water and NO

In the photocatalytic reduction of CO₂, a fixed amount of catalytic material (˜0.3 g) was uniformly dispersed onto a glass fiber filter (Whatman, QMA, 4.7 cm) and placed in a 200 mL cylindrical photoreactor containing stainless steel (SS) walls and a quartz window. Quartz wool wetted with Nanopure water (18.1 MΩ) was also placed in the reactor to maintain moisture within the system. Flowing compressed CO₂ with H₂O at a relative humidity of 70% and, when applicable, NO into the reactor generated a mixture of reactants that were balanced in helium or nitrogen. After ˜25 minutes of flow, the reactor was subsequently turned to batch mode. The initial concentrations of CO₂ and NO ranged between 3.0-4.0% by volume and 610-819 ppm by volume (0.0610-0.0819% by volume), respectively.

FIG. 4 shows a schematic of an experimental setup used for testing a photocatalytic reaction system 400. The photocatalytic reaction system 400 includes: (1) 99.99% CO₂ cylinder, (2) 1000 ppm NO cylinder, (3) UHP N₂ cylinder, (4) Mass flow controller, (5) Impinger, (6) Photoreactor, (7) Bruker GC, and (8) vacuum ultraviolet detector. A photochemical reactor (Srinivasan-Griffin Rayonet) equipped with uniform UV irradiation (supplied by Rayonet, RPR-3500A UVA 315-400 nm bulbs) and proper ventilation was used to illuminate the SS-quartz reactor containing the catalytic material. During the illumination period of 2 hours, 200 μL of gas was taken at fixed intervals from the SS reactor using a gastight syringe (VICI Precision Sampling, A-2 RN, 500 μL). Gaseous samples were manually injected into the GCVUV.

A series of background tests were conducted to support the conclusion that any carbon-or nitrogen-containing species in the gaseous samples measured by the GC-VUV originated from CO₂ or NO reaction in the presence of the catalytic surface, H₂O and/or NO. Initial background experiments consisted of illuminating a mixture of reactants (CO₂, H₂O and/or NO) in the SS reactor in the absence of catalytic material. Ultra-high pure nitrogen and H₂O vapor were used as the reaction gases, and the system was tested with catalytic material loaded in the reactor. Furthermore, the interaction of NO with the catalysts was studied at room temperature to determine the yield of nitrous oxide (N₂O) in the absence of CO₂ and H₂O.

GC-VUV Analysis of Gas Standards

FIG. 5 shows the separation and detection of components of interest using the plot-Q column on the Bruker 456-GC coupled with a VUV detector. The peaks displayed in FIG. 5 were identified based on both the injection of standard samples and, when available, matched with standards in the VUV spectral library. The VUV spectral features of each respective compound are shown in FIG. 6. It was observed that all analyzed compounds exhibited significant absorptivity in the 125-160 nm wavelength region. As a result of the type of column and temperature program utilized in this study, oxygen, carbon monoxide, nitric oxide, and methane were all found to co-elute with one another to some degree. In light of this, de-convolution of the first peak shown in FIG. 3 was necessary in order to quantify the respective peak areas of each compound. De-convolution of co-eluting peaks was accomplished using the VUV Model & Analyze software, v4.7 (VUV Analytics Inc., Cedar Park, Tex.). The model absorbance spectrum where n analytes are simultaneously present in the flow cell, as is the case for chromatographic co-elution, is given by:

$\begin{array}{cc}{A}_j=\frac{1}{\ln \left(10\right)}\frac{d}{v}\sum _{i-1}^n{\sigma }_{\mathrm{ij}}N_i=\frac{1}{\ln \left(10\right)}\frac{d}{V}\left({\sigma }_{1j}N_1+{\sigma }_{2j}N_2+\dots +{\sigma }_{\mathrm{nj}}N_n\right).& \left(3\right)\end{array}$

In equation 3, d is the flow cell length and V is the flow cell length, both constants. There is one equation like this at each wavelength value j ranging from 125-240 nm. Removing the subscript j, and absorbing all constants into a single value k, allows for generalization of the wavelength dependence of absorption:

A=k(σ₁N₁+σ₂N₂+ . . . +σ_nN_n)   (4)

where A is the calculated absorbance spectrum, to be compared with A_meas, the measured absorbance spectrum. The σ_i are cross section spectra (in cm²/molecule) for each of the components present in the co-eluting peak (stored in the VGA-100 spectral library database). For each analyte, there is one term consisting of the product of the number of analyte molecules, N_i (a scalar) and the array of cross section values σ_i. The N_i are parameters to be optimized, and the factors kσ_i are the basis functions to be used in the linear optimization procedure (i.e., the fit procedure).

For this disclosure, a model was built from the analyte absorbance reference spectra, A_i,ref:

$\begin{array}{cc}A=\sum _{i=1}^nf_iA_{i,\mathrm{ref}}=\left(f_1A_{1,\mathrm{ref}}+f_2A_{2,\mathrm{ref}}+\dots +f_nA_{n,\mathrm{ref}}\right)& \left(5\right)\end{array}$

Here f_i are the fit parameters to be optimized and A_i,ref are the basis functions. The advantage of building the model this way is that the absolute cross section need not be known; only the VUV spectrum, which is directly proportional to the absolute cross section, is required. The advantage of invoking known cross sections is that they allow for the determination of the actual on-column mass of each analyte.

Regardless of whether equation 4 or 5 is used, both contain a set of known basis functions and scaling factors, which can be determined by linear optimization. The result of fitting the procedure is the set of optimal parameters N_i (Eq. 4) or f_i (Eq. 5). These optimal scaling parameters can be put back into Eq. 4 or Eq. 5, accordingly, to determine the calculated absorbance spectrum, which ideally differs from the measured spectrum only by the measurement noise. A caveat is that the reference spectra of the co-eluting analytes, i.e. σ_i in Eq. 4 or A_i,ref in Eq. 5, which are to be de-convolved must be known and distinct from one another. Typical product spectra are shown in FIG. 5, and are very distinct from each other, thus enabling de-convolution.

With analyte reference spectra, the optimized f_i reflect the amount of the ith component relative to the ith reference spectrum represented in the measure absorbance. When the model is applied to a chromatographic peak comprised of co-eluting components, new curves representing the contribution of each of these analytes to the original peak are generated. The areas of these curves were used to quantify the analyte amounts in the photocatalytic reaction experiments described herein.

CO₂/H₂O/NO Photocatalytic Experiments

The catalyst 102 comprised commercial P25 TiO₂ and the synthesized Cu—TiO₂ in the CO₂ photoreduction experiments. In the background study where the system was illuminated in the absence of catalytic material, the CO₂ and NO concentrations remained constant, and no products were observed. In the case in which the catalyst 102 was exposed to the reactants in the absence of UV illumination, no products were observed. Both studies demonstrated that CO₂ and NO conversion only commenced when the catalyst 102 was present together with the light source 104. In the system where H₂O vapor and N₂ were the only reactants, the catalyst 102 under UV illumination from the light source 104 produced no carbon-containing species. This further demonstrated that any carbon or nitrogen containing products that were produced were derived from CO₂ and/or NO in the reaction gases.

In a system where CO₂ and H₂O were the sole gaseous reactants, it was observed that illumination of the commercial P25 TiO₂ and Cu—TiO₂ surfaces resulted in a loss of gas-phase CO₂ and a corresponding increase in CO. In all conducted experiments, no CH₄ was detected, suggesting that the utilized catalysts have a higher selectivity for CO formation. In comparison to commercial P25 TiO₂, the Cu—TiO₂ photocatalyst demonstrated the best photocatalytic activity—where the highest CO production was 3.51 μmol/g-catalyst after 2 hours of illumination, as shown in FIG. 7. In particular, line 700 in FIG. 7 represents the CO formation over the commercial P25 TiO₂ photocatalyst in the presence of CO₂ and H₂O, and line 702 in FIG. 7 represents the CO formation over the Cu—TiO₂ photocatalyst in the presence of CO₂ and H₂O. Previous studies have found production rates of 0.17 μmol·g^−1·h⁻¹ and 0.35 μmol·g^−1·h⁻¹ over anatase and mixed-phase commercial P25 TiO₂, respectively.

It was established by preliminary experiments that, without UV illumination, the NO concentration in the photoreactor with a photocatalyst remains invariable. After UV light is introduced by the light source 104, the NO concentration decreases and N₂O subsequently forms. The N₂O was positively identified using its VUV spectrum. No other products of the photoreaction were observed. In the system where CO₂, H₂O, and NO were the reactants, it was observed that illumination of the commercial P25 TiO₂ surface resulted in a loss of gas-phase NO and a corresponding increase in N₂O. The system containing the Cu—TiO₂ catalyst showed favorable formation for both N₂O and CO products. Nonetheless, it was observed that the presence of NO in the system had a detrimental effect on the CO₂ photoreduction process—whereby the production of CO over Cu—TiO₂ significantly decreased to 1.80 μmol/g-catalyst, as shown in FIG. 7. In particular, line 704 in FIG. 7 represents the CO formation over the commercial TiO₂ photocatalyst in the presence of CO₂/H₂O/NO, and line 706 represents the CO formation over the Cu—TiO₂ photocatalyst in the presence of CO₂/H₂O/NO. Based on the kinetic theory of gases, it is expected that NO with a molecular weight of 30 would reach the surface faster than CO₂ with a molecular weight of 44, given that the speed of each is proportional to the (molecular mass)^−0.5. Thus, this significant decrease in CO production over both catalysts could stem from the favorable adsorption behavior of NO over titania-based materials and its ability to occupy important binding sites that are critical to reducing CO₂. However, the concentration of CO₂ in the feed is significantly higher than the concentration of NO. Therefore, a more plausible explanation is likely that the NO is interacting with the CO, thereby reducing the amount of CO that is desorbed from the surface and subsequently measured by the GC-VUV. This theory is explored subsequently in this disclosure.

FIG. 8 presents plots of the NO concentration as a function of the illumination time, by the light source 104, over the TiO₂ based photocatalysts. In particular, line 800 represents the NO concentration over the commercial P25 TiO₂ photocatalyst in the presence of NO, line 802 represents the NO concentration over the Cu—TiO₂ photocatalyst in the presence of NO, line 804 represents the NO concentration over the commercial P25 TiO₂ photocatalyst in the presence of CO₂/H₂O/NO, and line 806 represents the NO concentration over the Cu—TiO₂ photocatalyst in the presence of CO₂/H₂O/NO. The zero point corresponds to the beginning of illumination. The commercial P25 TiO₂ (line 800) catalyst is shown to exhibit more favorable NO degradation than Cu—TiO₂ (line 802) when CO₂ and H₂O are not present within the system. The lowest NO conversion was observed over the Cu—TiO₂ surface when CO₂ and H₂O are present within the system (line 806). It is proposed that this behavior may be due to CO₂ and NO competing for available electrons.

FIGS. 9 and 10 provide an account of the evolution of N₂O and O₂ from NO photoreduction over the commercial and copper modified P25 TiO₂. Specifically, FIG. 9 shows the N₂O evolution for the P25 TiO₂ photocatalyst in the presence of NO (line 900) and CO₂/H₂O/NO (line 902), and the N₂O evolution for the Cu—TiO₂ photocatalyst in the presence of NO (line 904) and CO₂/H₂O/NO (line 906). As shown in FIG. 9, favorable N₂O formation from CO₂ photoreduction in the presence of H₂O and NO over Cu—TiO₂ (line 906) can be achieved. FIG. 10 shows the O₂ evolution for the P25 TiO₂ photocatalyst in the presence of CO₂/H₂O (line 1000) and CO₂/H₂O/NO (line 1002), and the O₂ evolution for the Cu—TiO₂ photocatalyst in the presence of CO₂/H₂O (line 1004) and CO₂/H₂O/NO (line 1006).

FIGS. 9 and 10 clearly indicate that variables such as the reactant feed and type of catalyst have an effect on NO degradation to O₂ and N₂O. The reported O₂ evolution in each system reflects a cumulative production from a series of likely reactions such as H₂O splitting and NO reduction. Nitrous oxide was most prevalent in the system where CO₂ was reduced in the presence of H₂O and NO over the copper modified catalyst. This system exhibited a higher O₂ production than a system with just NO present. This trend may be due to the enhanced charge of the Cu—TiO₂ catalyst; which assists in the generation of more holes for H₂O splitting.

The calculated molar yield of N₂O and conversion of NO over the TiO₂ materials are reported in the table, below.

TABLE 1
Summary of NO molar conversion and N2O yield (expressed
as % N) over commercial P25 TiO2 and Cu—TiO2
	NO Conversion	N2O Yield
Inlet Conditions	(% N)	(% N)
Commercial P25 TiO2 + NO	76.7	15.9 ± 3.9
Commercial P25 TiO2 + CO2 + H2O + NO	72.5	12.1 ± 2.5
Cu—TiO2 + NO	74.3	7.7 ± 1.8
Cu—TiO2 + CO2 + H2O + NO	53.3	29.0 ± 3.2

The molar conversion percent of NO and molar yield percent of N₂O can be defined according to Equations 6 and 7, respectively:

$\begin{array}{cc}\mathrm{Conversion}\left(\%N\right)=\frac{n_{0,\mathrm{NO}}-n_{f,\mathrm{NO}}}{n_{0,\mathrm{NO}}}\times 100& \left(6\right)\\ N_2O\mathrm{Yield}\left(\%N\right)=\frac{2n_{f,N_2O}}{n_{0,\mathrm{NO}}-n_{f,\mathrm{NO}}}\times 100& \left(7\right)\end{array}$

where n_0,i is the number of moles of compound i at time zero, and n_f,i is the number of moles of compound i at final illumination time.

The conversion of NO was found to range between 53.3% and 76.7%. It is of interest to note that the illumination of catalytic material in the presence of CO₂, H₂O, and NO over Cu—TiO₂ results in a higher N₂O yield than a system where just NO and Cu—TiO₂ are present. However, this trend (more than a factor of 4 increase in N₂O formation) was not observed over the commercial P25 TiO₂ surface, suggesting that the presence of Cu²⁺ ions on the TiO₂ may have an effect on the surface chemistry. The CO molecule has demonstrated the ability to effectively probe TiO₂ surfaces with deposited metals. In most studies, it is observed that CO strongly adsorbs on Cu sites. In light of this, reaction 15 in Table 2, below, seems more plausible in explaining the enhanced formation of N₂O over Cu—TiO₂. Instead, the NO reduction in the presence of CO₂ and H₂O resulted in a 24 percent decrease in N₂O formation over commercial P25 TiO₂.

As shown in Table 1, the yields of N₂O (expressed as % N) from the reported photocatalytic systems do not fully account for the total amount of NO converted (% NO). The unaccounted-for converted nitrogen (N) for all four scenarios ranges between 24 and 66 percent and is hypothesized to be in the form of N₂. This hypothesis is supported by the fact that no additional products were detected by GC-VUV. The one material that is challenging to detect by VUV is N₂, given that N₂ has a very low absorbance cross section in the vacuum ultraviolet region. In addition, a published study of NO photocatalytic decomposition indicated that N₂ is a major product.

It is hypothesized that the high formation of CO over the Cu—TiO₂ surface (in comparison to P25 TiO₂) likely has a direct impact on the N₂O yield. The results provided in FIGS. 7 and 9 lend support to this hypothesis. The change in CO production in going from the CO₂/H₂O system to the CO₂/H₂O/NO system is 1.71 μmol/g catalyst at 2 hours (i.e. 3.51 μmol/g-catalyst from the CO₂/H₂O system minus 1.80 μmol/g-catalyst from the CO₂/H₂O/NO system). This change in CO is directly comparable to the production of N₂O that is seen in FIG. 9 at 2 hours, i.e., 1.70 μmol/g catalyst, suggesting a 1 to 1 mole ratio between CO consumption and N₂O production over the Cu—TiO₂ catalyst. A slightly different result appears when comparing the CO and N₂O levels in the CO₂/H₂O and CO₂/H₂O/NO systems over the P25 TiO₂ catalyst. As determined from FIGS. 7 and 9 for the P25 TiO₂ catalyst, the change in CO production in going from the CO₂/H₂O to the CO₂/H₂O/NO systems is approximately 2.1 μmol/g-catalyst (i.e. 2.1 μmol/g catalyst from the CO₂/H₂O system minus 0 μmol/g-catalyst from the CO₂/H₂O/NO system), while the N₂O production in the CO₂/H₂O/NO system is only 0.74 μmol/g-catalyst. This result suggests that the P25 TiO₂ surface is not as effective as compared to the Cu—TiO₂ surface in enhancing the CO reaction with NO to form N₂O. Instead, with the P25 TiO₂ system, a portion of the CO readily desorbs from the surface and is measured in the gas-phase. The current results are consistent with previous studies that suggest that CO assists in the reduction of NO to N₂O over commercial P25 TiO₂, but extend the previous results to the Cu—TiO₂ catalyst.

It should also be noted that in the presented reaction pathway, both Langmuir-Hinshelwood and Eley-Rideal mechanisms apply due to the reaction of adsorbed and gas-phase species. The possible reaction pathways during the CO₂ reduction process in the presence of H₂O and NO are also included in Table 2. It is purported that adsorbed CO formed from CO₂ photoreduction by H₂O initiates another reaction involving adsorbed NO molecules. Reaction (15) in Table 2 suggests that the presence of CO helps to reduce NO to N₂O. This mechanism aligns with the results displayed in FIG. 9, where the Cu—TiO₂ catalyst exhibits significant N₂O production.

TABLE 2
Photocatalyst Activation
TiO2 + hv → e− + h+              (1)
NO Photoreduction Mechanism
NO(ads) + e− → NO−(ads)          (2)
O2−(c) + h+ → O−(c)              (3)
NO−(ads) + NO(gas) → N2O(gas) + O−(cus) (4)
O−(cus) + NO(gas) + →NO2−(ads)   (5)
NO−(ads) + O−(cus) → N(ads) + O(ads) + O2−(cus) (6)
NO(ads) + N(ads) → N2O(ads)      (7)
NO(ads) + O(ads) → NO2(ads)      (8)
2O(ads) → O2(gas)                (9)
2N(ads) → N2(gas)                (10)
2NO(ads) → N2(gas) + O2(gas)     (11)
CO2 Photoreduction Mechanism
2H2O(ads) + 4h+ → 4H+ + O2(gas)  (12)
4H+ + 4e− → 2H2(gas)             (13)
CO2(ads) + 2H+ + 2e− → CO(ads) + H2O(ads) (14)
2NO(ads) + CO(ads) → N2O(gas) + CO2(gas) (15)
indicates data missing or illegible when filed

Thus, the systems and methods described herein enable the photoreduction of CO₂ and NO in post-combustion streams. Additionally, the photoreduction of CO₂ and NO can enable the generation of CO and N₂O, which may be harvested for use in other industries. The technology includes a method for simultaneous carbon dioxide and nitric oxide control that is highly efficient, particularly for nitric oxide conversion. Chemical products are created in the control process that can enable industries to enhance their efficiencies (thus addressing the new US Environmental Protection Agency's new Carbon Rule) and increase profitability while simultaneously enhancing environmental stewardship.

The technology has the potential to control NO using light and an inexpensive photocatalyst. This may result in cost savings and easier operations. One product of the NO control using the technology is nitrous oxide, a chemical that can be sold to the semiconductor industry or sold to gas companies for purification and subsequent use by the medical industry. Different amounts of the nitrous oxide can be generated based on the catalyst that is used (either TiO₂ or Cu—TiO₂). The technology can simultaneously avoid the direct release of CO₂ to the atmosphere by converting the CO₂ to CO. Advantages over current technology include: (1) light is used to activate the catalyst; (2) the chemicals are relatively inexpensive; and (3) the photocatalytic approach can also be used to treat CO₂ and convert this to CO or potentially other carbon containing species.

Although the invention has been described in considerable detail with reference to certain embodiments, one skilled in the art will appreciate that the present invention can be practiced by other than the described embodiments, which have been presented for purposes of illustration and not of limitation. Therefore, the scope of the appended claims should not be limited to the description of the embodiments contained herein.

Claims

1. A photoreduction system for a fluid stream, the fluid stream including at least carbon dioxide and nitric oxide therein, the photoreduction system comprising: a catalyst arranged such that the fluid stream flows over a surface region of the catalyst;a light source configured to illuminate the surface region of the catalyst;wherein when the light source illuminates the surface region of the catalyst, a concentration of the carbon dioxide and a concentration of the nitric oxide in the fluid stream are reduced as the fluid stream flows over the surface region.

2. The photoreduction system of claim 1, wherein when the concentration of nitric oxide is reduced as the fluid stream flows over the surface region, nitrous oxide is generated.

3. The photoreduction system of claim 1, wherein the catalyst comprises a metal oxide.

4. The photoreduction system of claim 3, wherein the metal oxide has a band gap energy between 2 and 5 eV.

5. The photoreduction system of claim 3, wherein the band gap energy of the metal oxide is between 2.5 and 4.5 eV.

6. The photoreduction system of claim 3, wherein the band gap energy of the metal oxide is between 3 and 3.5 eV.

7. The photoreduction system of claim 3, wherein the metal oxide comprises a dopant.

8. The photoreduction system of claim 3, wherein the metal oxide comprises titanium dioxide.

9. The photoreduction system of claim 5, wherein the titanium dioxide comprises a phase selected from the group consisting of anatase, brookite, rutile, and mixtures thereof.

10. The photoreduction system of claim 5, wherein the phase of the titanium dioxide comprises a mixture of anatase and rutile.

11. The photoreduction system of claim 7, wherein the dopant is a metal.

12. The photoreduction system of claim 11, wherein the metal is selected from the group consisting of copper, platinum, silver, and mixtures thereof.

13. The photoreduction system of claim 7, wherein the dopant is a non-metal.

14. The photoreduction system of claim 13, wherein the non-metal is iodine.

15. The photoreduction system of claim 1, wherein the catalyst comprises copper modified titanium dioxide.

16. The photoreduction system of claim 15, wherein the copper modified titanium dioxide is formed from reaction of a copper-containing compound and titanium dioxide particles having a mean diameter in a range of 10 to 50 nanometers.

17. The photoreduction system of claim 15, wherein the copper modified titanium dioxide is formed from reaction of a copper-containing compound and titanium dioxide particles having a mean diameter in a range of 10 to 30 nanometers.

18. The photoreduction system of claim 15, wherein the copper modified titanium dioxide has a copper content in a range of 0.01 to 5 wt. %.

19. The photoreduction system of claim 15, wherein the copper modified titanium dioxide has a copper content in a range of 0.1 to 1 wt. %.

20. The photoreduction system of claim 15, wherein the copper modified titanium dioxide has a copper content in a range of 0.2 to 0.8 wt. %.

21. The photoreduction system of claim 1, wherein the light source is configured to emit ultraviolet radiation.

22. The photoreduction system of claim 1, wherein the catalyst consists essentially of copper modified titanium dioxide.

23. The photoreduction system of claim 1, wherein the conversion of nitric oxide in the fluid stream is greater than 50%.

24. The photoreduction system of claim 1, wherein the yield of nitrous oxide in the fluid stream is greater than 4%.

25. The photoreduction system of claim 1, wherein the fluid stream includes flue gas.

26. A method for simultaneously controlling a carbon dioxide concentration and a nitric oxide concentration and generating nitrous oxide in a fluid stream, the method comprising: arranging a catalyst in the fluid stream such that the fluid stream flows over a surface region of the catalyst; andilluminating the surface region of the catalyst as the fluid stream flows over the surface region.

27. The method of claim 26, wherein the catalyst comprises titanium dioxide.

28. The method of claim 26, wherein the catalyst comprises a material selected from the group consisting of anatase titanium dioxide, brookite titanium dioxide, rutile titanium dioxide, and mixtures thereof.

29. The method of claim 26, wherein the catalyst comprises a mixture of anatase titanium dioxide and rutile titanium dioxide.

30. The method of claim 26, wherein the catalyst comprises a material selected from the group consisting of copper modified titanium dioxide, iodine modified titanium dioxide, platinum modified titanium dioxide, silver modified titanium dioxide, and mixtures thereof.

31. The method of claim 26, wherein the catalyst comprises copper modified titanium dioxide.

32. The method of claim 31, wherein the copper modified titanium dioxide is formed from reaction of a copper-containing compound and titanium dioxide particles having a mean diameter in a range of 10 to 50 nanometers.

33. The method of claim 31, wherein the copper modified titanium dioxide is formed from reaction of a copper-containing compound and titanium dioxide particles having a mean diameter in a range of 10 to 30 nanometers.

34. The method of claim 31, wherein the copper modified titanium dioxide has a copper content in a range of 0.01 to 5 wt. %.

35. The method of claim 31, wherein the copper modified titanium dioxide has a copper content in a range of 0.1 to 1 wt. %.

36. The method of claim 31, wherein the copper modified titanium dioxide has a copper content in a range of 0.2 to 0.8 wt. %.

37. The method of claim 26, wherein illuminating the surface region of the catalyst comprises: emitting ultraviolet radiation from a light source towards the surface region of the catalyst.

38. A photocatalytic reaction system comprising: a photocatalytic reactor having an interior space in fluid communication with an inlet and an outlet, the photocatalytic reactor including a light source to irradiate at least a portion of a catalyst in the interior space;a fluid separation unit in fluid communication with the outlet of the photocatalytic reactor, the fluid separation unit configured to separate at least one product of a plurality of products received from the photocatalytic reactor;an analyzer is in fluid communication with the fluid separation unit for receiving the plurality of products, the analyzer comprising a detector, a second light source, and a controller in electrical communication with the detector and a second light source; andwherein the controller executes a program stored in the controller to: (i) irradiate at least two products of the plurality of products using the second light source,(ii) generate an absorbance spectrum (Ameas) of the at least two products from electrical signals received from the detector, the absorbance spectrum including a co-eluting peak, and(iii) de-convolute the co-eluting peak to compute a concentration of one or more of the at least two products.

39. The photocatalytic reaction system of claim 38, wherein the analyzer includes a vacuum ultraviolet detector.

40. The photocatalytic reaction system of claim 38, wherein the de-convolution of the co-eluting peak includes computing a calculated absorbance spectrum (Acalc) at one or more wavelengths according to: Acalc=k(σ1N1+σ2N2+ . . . +σnNn);wherein σn are cross section spectra (cm2/molecule), and Nn is total number of molecules for the one or more of the at least two products.

41. The photocatalytic reaction system of claim 38, wherein the de-convolution of the co-eluting peak includes computing a reference spectral absorbance (A) at one or more wavelengths according to: A=(f1A1,ref+f2A2,ref+ . . . +fnAn,ref);wherein fn is a fitting parameter to be optimized, and An,ref is the absorbance from an individual reference spectrum for the one or more of the at least two products.

42. The photocatalytic reaction system of claim 38, wherein the de-convolution of the co-eluting peak includes linear optimization by using a scaling parameter to match the absorbance spectrum (Ameas) to the reference spectral dictionary (A) or the calculated absorbance spectrum (Acalc).

43. The photocatalytic reaction system of claim 42, wherein the scaling parameter is selected from the group consisting of fn and Nn.

44. The photocatalytic reaction system of claim 38, wherein the de-convolution of the co-eluting peak includes generating individual absorbance peaks for each of the at least two products.

45. The photocatalytic reaction system of claim 44, wherein the individual absorbance peaks are integrated to calculate the concentration of each of the at least two products.

46. The photocatalytic reaction system of claim 40, wherein the one or more wavelengths are between 120 and 250 nm.

47. The photocatalytic reaction system of claim 38, wherein the fluid separation unit includes a gas chromatography column.

48. The photocatalytic reaction system of claim 39, wherein a transfer line that is heated to a first temperature is configured to place the fluid separation unit in fluid communication with the analyzer.

49. The photocatalytic reaction system of claim 48, wherein the first temperature is between 250° C. to 350° C.

50. The photocatalytic reaction system of claim 48, wherein the transfer line is configured with an inert gas inlet at a first pressure.

51. The photocatalytic reaction system of claim 48, wherein the first pressure is between 0.2 to 5 psi.

52. A method for determining the concentration of at least two products of a plurality of products from a photocatalytic reaction system, the method comprising: (a) acquiring an absorbance spectrum (Ameas) of at least two products of a plurality of products using an analyzer, the absorbance spectrum including a co-eluting peak;(b) de-convoluting the co-eluting peak by generating an individual absorbance spectrum for the at least two products; and(c) computing a concentration for one or more of the at least two products based on the individual absorbance spectrums.

53. The method of claim 52, wherein the analyzer includes a vacuum ultraviolet detector.

54. The method of claim 52, wherein step (b) further includes computing a calculated absorbance spectrum (Acalc) at one or more wavelengths according to: Acalc=k(σ1N1+σ2N2+ . . . +σnNn);wherein σn are cross section spectra (cm2/molecule), and Nn is total number of molecules for the one or more of the at least two products.

55. The method of claim 52, wherein step (b) further includes computing a reference spectral absorbance (A) at one or more wavelengths according to: A=(f1A1,ref+f2A2,ref+ . . . +fnAn,ref);wherein fn is a fitting parameter to be optimized, and An,ref is the absorbance from an individual reference spectrum for the one or more of the at least two products.

56. The method of claim 52, wherein step (b) further includes linear optimization by using a scaling parameter to match the absorbance spectrum (Ameas) to the reference spectral dictionary (A) or the calculated absorbance spectrum (Acalc).

57. The method of claim 56, wherein the scaling parameter is selected from the group consisting of fn and Nn.

58. The method of claim 52, wherein step (c) further includes integrating the individual absorbance spectrums to calculate the concentration for the one or more of the at least two products.

59. A method for analyzing a sample derived from a photocatalytic reaction, the method comprising: using gas chromatography coupled with vacuum ultraviolet detection for analyzing gaseous species in the sample.

60. A method for analyzing a sample derived from a photocatalytic reaction, the method comprising: using gas chromatography coupled with thermal conductivity detection for analyzing gaseous species in the sample.