Absorption Chemistry of Plasma-Generated NO_x Gas for Green Nitric Acid Production

Abstract

Nitric acid (HNO₃) is predominantly produced in large production plants using the Ostwald process. In view of its widespread application as synthetic fertilizer, small- scale and local production has become of interest. The chemical precursor of nitric acid is NO_x gas, which can be produced from air at percentage-level concentrations using small-scale, electrically powered warm plasma reactors. Using gas-phase plasma, the downstream conversion of NO_x into fertilizer is a crucial, but as yet understudied step. This work aims to help close this gap and support the further development of plasma-driven nitrogen fixation and subsequent NO_x scrubbing. The chemistry of NO_x absorption through gas scrubbing is investigated at a 1% NO_x concentration using a synthetic mimic of a plasma-produced NO_x stream in order to maintain maximal controllability. pH values of the scrubber solution were kept in the range of 1 to 5 and it was recirculated for up to 30 h. The kinetics of NO_x absorption were found to be strongly pH-dependent, requiring several hours of recirculation to reach steady state conditions. Once at steady state, the NO_x removal efficiency turned out to be rather pH independent and reached around 84% for experiments at pH 1–4. The formation of nitrous acid (HNO₂) byproduct reached a constant value of around 3.43 mM based on a dynamic equilibrium of its formation and decomposition. Approaches to minimize undesired nitrite and nitrous acid byproduct formation are discussed.

1. Introduction

Ammonium nitrate fertilizer, an essential element in our global food production system, is currently produced in large chemical plants [1,2]. Ammonia (NH₃), being the base chemical, is produced in the Haber–Bosch process. Ammonia synthesis, using hydrogen gas produced from fossil methane, is responsible for a significant percentage of global carbon dioxide emissions [3,4,5]. In the subsequent Ostwald process, NH₃ is catalytically oxidized with O₂ to form NO₂, which upon reaction with water forms HNO₃. The chemistry of this industrial absorption process is complex. The process entails about 40 entangled reaction steps with intermediates and by-products such as HNO₂, N₂O, N₂O₃ and N₂O₄ [6]. NO oxidation and NO₂ absorption are performed under pressures of up to 10 bar and at NO_x gas concentrations of around 10%. The commercial HNO₃ product is typically a concentrated solution containing up to 65 wt.% HNO₃ [7,8,9].

Electricity-powered plasma technology is an emerging alternative for nitric acid production with continuously improving energy efficiency [10,11,12]. In plasma, electrons and gas molecules are excited such that nitrogen and oxygen gas from atmospheric air react to NO_x [11,13]. In general, plasma reactors are divided into three groups based on gas temperature: thermal plasma, non-thermal plasma and warm plasma, which can be described as an intermediate of the former two. In warm plasma, electron temperatures are elevated, while gas molecules are also heated but not to the extent of thermal plasma gas temperatures. This creates only a partial equilibrium between the electrons and gas molecules, causing warm plasma to be the most promising type for NO_x production considering yield over energy requirement [11,14,15,16].

Plasma-based nitrogen oxidation is a strongly growing research domain. It encompasses dry or gas-phase plasma, using only air and electricity for the production of NO_x, but also plasma–liquid systems are of growing research interest for the production of plasma-activated water (PAW), rich in NO₂⁻ and NO₃⁻. In these plasma–liquid reactors, plasma discharge can be in direct or indirect contact with the liquid phase [17,18]. A large number of short-lived species (e.g., H*, OH*, H₂O₂, …) are produced when the plasma interacts with water, with the advantage of also creating oxidizing agents like H₂O₂ or O₃. This results in highly complex reaction pathways and often lowers the energy to NO_x efficiency [18,19,20,21].

Using gas-phase plasma, produced NO_x gas still needs to react with water to form HNO₃ like in the Ostwald process. This is performed afterwards in a gas–water contactor or scrubber. However, in plasma processes, NO_x is produced at concentrations in the range of a few percent, which is substantially lower than in the Ostwald processes (ca. 10%), leading to different absorption conditions [7,8,11,15].

Besides serving as a precursor for HNO₃, NO_x gas is also a known air pollutant emitted at parts-per-million levels during combustion processes [22,23]. NO_x scrubbing is also an end-of-pipe solution to eliminate it from flue gas [24,25]. Under near-ambient temperature and pressure conditions, the low aqueous solubility of NO and the slow kinetics of its spontaneous oxidation to the better-dissolving NO₂ often necessitate the use of oxidizing agents like H₂O₂ and O₃ [25,26,27,28,29,30].

The operation conditions of scrubbers for the absorption of plasma-based NO_x are in between those of the Ostwald process and NO_x emission abatement technologies. While NO_x absorption is extensively modelled, for example by Patwardhan et al. [31], only limited experimental research has been performed on NO_x to HNO₃ conversion under reaction conditions relevant to gas-phase plasma-NO_x with a downstream scrubbing unit. In order to make an estimation of the feasibility or implementation potential of plasma technology for nitrate fertilizer production, more research on the NO_x absorption step is necessary [11,32].

In this work, NOₓ absorption processes and, in particular, the formation and transformation of NO₂⁻ and NO₃⁻ in liquid-phase reactions are studied. In order to allow a more direct investigation, a NO_x-containing gas mixture is used, mimicking the NO_x gas produced from gas-phase warm plasma reactors. As plasma-NO_x production is a strongly emerging domain, NO_x concentrations of up to 5% are reported but are at the moment still on the upper end of achieved concentrations. Therefore, a NO_x concentration of 1% was chosen to represent a current, small-scale plasma reactor [11,15,33].

Insight was gained on the influence of scrubbing liquid pH on NO_x absorption kinetics, since alkaline solutions are often deemed more effective for NO_x removal compared to neutral or acidic solutions due to the acidic character of NO_x [22,34]. Also, nitrate capacities and the formation of undesired nitrous acid side products were studied without the addition of oxidizing agents for long-term recirculation.

2. Materials and Methods

2.1. Setup

The experimental setup for NO_x absorption experiments is depicted in Figure 1. A mixture of NO, O₂ and N₂ gases delivered from gas cylinders was fed to the absorption column at 3 L/h. Absorption liquid was circulated at 375 mL/min in such a way that gas and liquid were running in counter-current. A large contact area was assured between liquid and gas by filling the column with packing material consisting of glass Raschig rings with diameter and height 6 mm (Glasatelier Saillart, Meerhout, Belgium), depicted in Figure 2.

The column was kept at a constant temperature of 293 K by a cryostat. The liquid outlet of the column is connected to a round flask with openings for the gas inlet, base solution inlet, pH probe (Mettler Toledo, Zaventem, Belgium, SevenCompact) and pH control system (Hannah instruments, Temse, Belgium, HI510 and HI1006-1850). The pH of the scrubbing solution was kept constant as follows. The round flask was filled with acidified aqueous solution of H₂SO₄ (Acros Organics, Geel, Belgium, 96 wt%) or H₃PO₄ (Acros Organics, Geel, Belgium, 85 wt%) at the intended pH, in a range from pH 1 to pH 5. During operation of the absorption column, the pH was monitored and kept constant by dosing with 0.2 M KOH (Sigma-Aldrich, Hoeilaart, Belgium, ≥85%).

2.2. Gas Phase Composition and Analysis

The inlet gas mixture was composed of 1% NO, 20% O₂ and 79% N₂, and fed from gas cylinders using mass flow controllers (Bronkhorst, Olen, Belgium, EL-FLOW). The flow rate was 3 L/min. NO and NO₂ concentrations in the gas mixture were measured with a UV analyzer (ABB, Diegem, Belgium, AO2020 Limas11HW). Calculations were performed in MATLAB software (MathWorks, Natick, MA, USA, R23022b) and Excel (Microsoft 365, Redmond, WA, USA, version 2502). Before starting the absorption, the feed gas was run for 30 min in bypass mode and sent directly to the analyzer without passing through the column to allow the gas composition to stabilize and to be verified. The NO and NO₂ removal efficiency (RE) was estimated as the difference between the in- and outlet concentrations divided by the inlet concentration (Equation (1)):

$$RE(N{O}_x)\%=1-{\displaystyle \frac{{\int }_{t_{end-5min}}^{t_{end}}\left(C_{N{O}_{xout}}\right)}{{\int }_{t_{end-5min}}^{t_{end}}\left(C_{N{O}_{xbypass}}\right)}}\ast 100$$

(1)

In the bypass phase of each experiment, some NO oxidation already occurred in the gas lines, resulting in a mixture of NO and NO₂ reaching the scrubber column. The oxidation ratio (OR), defined as the ratio of the concentration of NO₂ over total NO_x, is determined according to Equation (2). Oxidation ratios were very similar for all tests with OR values of 0.56 ± 0.008.

$$OR={\displaystyle \frac{C_{N{O}_{2in}}}{C_{N{O}_{2in}}+C_{N{O}_{in}}}}$$

(2)

2.3. Liquid Phase Analysis

Liquid samples were taken every hour. Samples taken from the round flask were diluted 100 times and buffered at pH 7 using an equimolar mixture of 0.005 M NaH₂PO₄ (Merck, Hoeilaart, Belgium, >99%) and Na₂HPO₄ (Merck, Hoeilaart, Belgium 98–100%). Nitrous acid is a weak acid, being only partially deprotonated under acidic conditions. Protonation–deprotonation equilibrium of nitrous acid was considered to be established in the scrubber solution under all conditions. Estimates of the actual concentration of nitrous acid based on total nitrite analysis were made assuming a nitrous acid pK_a value of 3.20 (Equation (3)) [35,36].

$$[{HNO}_2]={\displaystyle \frac{\left[N{O}_2^{-}\right]\ast {10}^{-pH}}{{10}^{-p{K}_a}}}$$

(3)

At this pH value, nitrous acid is deprotonated, which is needed for quantification using anion chromatography. The nitrate and nitrite contents of the liquid samples were analyzed using ion chromatography (Metrohm, Kontich, Belgium, Eco IC, A Supp 5 column, 850 IC conductivity detector).

3. Results

NO_x scrubbing experiments were performed in a column with an empty bed volume (EBV) of 780 mL with 400 mL recirculation solution, of which the pH was kept fixed at values of 1, 2, 3, 4 and 5 by dosing with KOH, which not only has a pH regulating function but could also add value to the fertilizer (Figure 1). A gas mixture consisting of 1% NO, 20% O₂ and 79% N₂ entered the column in counter-current with the solution at a flow rate of 3 L/min, based on typical flow rates found for several reactor types including gliding arc [11,16,19,37]. In order to ensure sufficient contact area, the column was filled with an inert packing material. In- and outgoing NO_x gasses were analyzed in-line using a UV detector. The HNO₃, NO₂⁻ and HNO₂ content of the scrubber solution was analyzed in regularly taken samples; thereafter HNO₂ was deprotonated to NO₂⁻ by adding a buffer solution of pH 7 to enable quantification with ion chromatography. The combination of NO₂⁻ and HNO₂ will later on be referred to as total nitrite concentration. For more information see Section 2. Data of preliminary tests, to indicate reproducibility, can be found in the Supplementary Information.

3.1. Scrubber Liquid Analysis

The nitrate, nitrite and total nitrite concentrations, standing for the sum of NO₂⁻ and HNO₂ in the scrubber solution, were determined at 1 h time intervals (Figure 3). Experiments at pH 4 and 5 were run over two days. No liquid samples were taken during the night. The nitrate concentration steadily increased for all the five experiments at different pH values. At the end of the testing period, the nitrate concentration in the scrubber solution reached values of 12.6 mM at pH 1; 14.0 mM at pH 2; 10.4 mM at pH 3; 40.3 mM at pH 4; and 14.9 mM at pH 5 (Figure 3 and

Table 1. Total NO₂⁻ (sum of NO₂⁻ and HNO₂ as measured), actual NO₂⁻, HNO₂ and NO₃⁻ concentrations in the scrubber solution at the end of the experiments of Figure 3 at different pH.

pH	Time (h)	Total NO2− (mM)	NO2− (mM)	HNO2 (mM)	NO3− (mM)
1	6	3.37	0.0211	3.35	12.6
2	6	3.86	0.229	3.63	14.0
3	6	5.41	2.09	3.32	10.4
4	30	21.6	18.6	2.95	40.3
5	30	38.4	37.8	0.599	14.9

). However, it is important to note that tests at pH 4 and 5 ran for 30 h instead of 6 h.

Table 2. NO₃⁻ concentrations for tests at pH 1–5 after 6 h.

pH	Time (h)	NO3− (mM)
1	6	12.6
2	6	14.0
3	6	10.4
4	6	4.72
5	6	2.97

illustrates the NO₃⁻ concentration for tests at pH 1–5 after 6 h. After the same amount of scrubbing time, NO₃⁻ concentrations reached 12.63 mM at pH 1 while only 2.97 mM was reached at pH 5. The nitrate accumulation rate decreased with increasing pH value.

The total nitrite concentration displayed increasing values at higher pH. At pH 1, 2 and 3, the total nitrite concentration reached a plateau after 2 to 4 h (Figure 3) at ca. 3.37 mM, 3.86 mM and 5.41 mM for pH 1, 2 and 3, respectively (Table 1). At pH 4 and 5 the total nitrite concentration in the circulating solution did not reach a plateau, even when the scrubbing was prolongated to 30 h. The total nitrite concentrations rose to 21.6 and 38.4 mM, respectively, at pH 4 and 5. At pH 5, nitrite was the main NO_x-derived compound in the scrubber liquid.

After the total nitrite concentration plateau was reached at pH 1, 2 and 3, the calculated HNO₂ concentrations reached very similar concentrations of 3.35, 3.63 and 3.32 mM, respectively (Table 1). At pH 4, the HNO₂ concentration reached 2.95 mM at the end of the 30 h testing period and had not fully reached a plateau yet, suggesting it could still increase to reach a value similar to that reached in the experiments at lower pH. At pH 5 the final HNO₂ concentration reached only 0.599 mM, which is substantially below the plateau value reached at lower pH. Under this condition, it may take a very long time to reach the plateau.

3.2. Gas Phase Analysis

The NO_x concentration in the gas exiting the scrubber under the different pH conditions is presented in Figure 4a,b. In experiments at pH 1, 2 and 3, NO_x outlet concentrations initially were around 800 ppm, and increased during the experiment until a plateau value of ca. 1800 ppm was reached. The corresponding NO_x removal efficiency decreased from ca. 95% initially, to 82.5%, 83.9% and 83.0% at pH 1, 2 and 3, respectively (Figure 4c).

At pH 4 and 5, the outgoing NO_x gas concentrations were significantly lower after 7 h, and still increasing (Figure 4b). When prolonging the scrubbing to 30 h at pH 4, a plateau value of ca. 84.2% removal efficiency was reached (Figure 4c), which is in the range of the values obtained at pH 1, 2 and 3. At pH 5, even after 30 h, the removal efficiency kept on slowly decreasing. Very long times would have been needed to verify the reaching of a plateau. Gaps in the data are due to a setup malfunction leading to an artefact in the data, irrelevant for further interpretation.

4. Discussion

The reaction network of NO_x gas absorption in aqueous media is complex and involves dissolution as well as chemical reactions involving reaction intermediates and reversible and irreversible reactions, in gas as well as liquid phase. The reactions considered most important in the gas phase are presented in Equations (4)–(7) [6,38,39,40,41].

2 NO (g) + O₂ (g) → 2 NO₂ (g)

(4)

NO (g) + NO₂ (g) ⇌ N₂O₃ (g)

(5)

NO (g) + NO₂ (g) + H₂O ⇌ 2 HNO₂ (g)

(6)

2 NO₂ (g) ⇌ N₂O₄ (g)

(7)

According to Equations (4)–(6), NO gas is converted into NO₂, N₂O₃, and HNO₂, respectively, which are more water-soluble. NO₂ also dimerizes to form N₂O₄ (Equation (7)).

The main reactions in the liquid phase are given in Equations (8)–(11). Dissolved N₂O₃ and N₂O₄ are converted into either HNO₂ or a combination of HNO₂ and HNO₃ [31,40,42]. The reactions of Equations (8)–(11) are often assumed irreversible since the rate of the back reactions, being bimolecular, is considered negligible in the present diluted, aqueous solutions [38,43,44,45].

2 NO₂ (l) + H₂O → HNO₂ (l) + HNO₃ (l)

(8)

N₂O₃ (l) + H₂O → 2 HNO₂ (l)

(9)

N₂O₄ (l) + H₂O → HNO₂ (l) + HNO₃ (l)

(10)

3 HNO₂ (l) → H₂O + 2 NO (g) + HNO₃ (l)

(11)

In liquid phase, nitrous acid is prone to disproportionation, leading to HNO₃, NO and H₂O formation according to Equation (11) [31,42,46,47]. The poorly soluble NO molecules desorb from the solution and return to the gas phase, where they re-enter the reaction network [48]. The HNO₂ decomposition reaction mechanism is often assumed as described by Schwartz et al. to be fourth order in HNO₂, but accurate rate equations remain a matter of discussion [42,44,45].

The observation of a total nitrite (NO₂⁻ and HNO₂) concentration plateau in the scrubber liquid at fixed pH values of 1, 2 and 3 (Figure 3) can be understood as follows. Nitrous acid decomposition is a disproportionation reaction involving several HNO₂ molecules and a reaction order higher than 1 (Equation (11)) [44,45]. With increasing HNO₂ concentration, the HNO₂ disproportionation reaction rate will increase until it equals the rate of HNO₂ formation (Equations (8)–(10)), leading to a steady-state HNO₂ concentration. At a constant pH, this also means a steady-state NO₂⁻ concentration.

This is in agreement with what is seen in analysis of the gas phase. The decrease in NO_x removal efficiency with time at constant pH (Figure 4c,d) could be attributed to this formation of NO by HNO₂ disproportionation (Equation (11)) [41,49]. Here as well, it is noticed that once the system reaches its steady state, NO_x removal efficiencies are very similar for pH 1, 2, 3 and 4. The similar limitation of the NO_x removal efficiency is also likely to be a consequence of the similar HNO₂ concentration (Table 1) and equal rate of the HNO₂ decomposition reaction (Equation (11)).

While at steady state pH does not seem to influence removal efficiency, in the transient period, on the other hand, the pH does matter, as observed in earlier studies [24,31,34,38]. The time after which the steady state condition is reached is pH-dependent. For tests at pH 1, 2 and 3 the HNO₂ concentrations reach steady state after approximately 4, 5 and 6 h, respectively. At pH 4 and 5, the accumulation of HNO₂ in the scrubber solution progresses much more slowly due to the acid dissociation reaction (Figure 3). The higher the pH, the more HNO₂ directly dissociates into NO₂⁻ and the longer it takes for enough HNO₂ to accumulate for the dissociation reaction (Equation (11)) to balance the formation rate. Per pH unit, ten times more HNO₂ is converted to NO₂⁻, which is reflected in Table 1.

The test at pH 4 nearly reached its steady state after 30 h, but the test at pH 5 did not reach this level within the tested timespan. Notably, much of the experimental research focuses on short-duration tests, often with recirculation times for the scrubbing solution limited to an hour [38,50]. An important conclusion to draw is that running experiments for shorter timespans than necessary to reach steady state could wrongly lead to the assumption that increasing the pH of the scrubbing solution also increases removal efficiency in the long term.

Nitrate, being a strong acid and assumed to be always in its dissociated form, accumulates over time in the scrubber solution (Figure 3). In the transient period, the concentration increases more than proportionally with time. This can also be attributed to the increasing rate of the HNO₂ decomposition reaction (Equation (11)), which also forms HNO₃. Given the steady-state NO₂⁻ and HNO₂ concentrations and the ongoing NO₃⁻ accumulation, there is no point in expressing a nitrate selectivity in these tests, as it is strongly time-dependent. What can be expressed is the steady-state NO₂⁻ amount that remains present.

It is possible that the final removal efficiency is a combination of NO that was not absorbed and went directly to the outlet of the system and NO that was released during HNO₂ disproportionation. The disproportionation reaction, however, does play an important role, since HNO₂ concentrations reach a plateau value after a few hours for a constant RE while solubility limits are far from being reached [51,52]. Also, the fact that removal efficiencies for the same empty bed residence time (EBRT) and gas concentrations reach their constant value after different times depending on pH and HNO₂ concentration, is another indication that the disproportionation reaction does play a significant role in determining the removal efficiency.

In practical applications of nitrate fertilizer production, nitrite and nitrous acid are undesired side products. Even though the maximal allowed nitrite concentration in nitrogen fertilizer is in many countries not explicitly regulated, effects of nitrite toxicity are reported at concentrations starting from 0.11 mM [53,54]. Below these concentrations, nitrite is converted in soil processes into nitrate by nitrite-oxidizing bacteria [55,56]. This study hints at a few abiotic options expected to lower the steady-state HNO₂ concentration without sacrificing the NO_x removal efficiency.

A first approach to consider is to increase the liquid volume in the round bottom flask. For a constant EBRT but larger liquid volume, a slower increase in HNO₂ concentration is expected for the same absolute amount of NO_x absorbed. This means that the disproportionation reaction is also slowed down, resulting in a lower steady-state HNO₂ concentration and NO formation. In a first preliminary experiment at pH 1 with liquid volumes of 250 mL and 400 mL, similar removal efficiencies of 83.6% and 82.5% were reached, respectively. Total nitrite concentrations seemed to stagnate after 6 h at 4.07 and 3.37 mM for 250 mL circulation volume and 400 mL, respectively; 4.04 mM and 3.35 mM of this were in the form of HNO₂. Increasing the volume of the scrubbing liquid 1.6 times reduced the nitrite content by around 17%. Increasing the liquid volume as well as slowing down the disproportionation reaction also decreased the rate of NO₃⁻ formation. After 6 h, nitrate concentrations of 19.6 mM and 12.6 mM were obtained for 250 mL and 400 mL scrubbing solution. However, this could be remedied by increasing the time over which the experiment was ran. While our results indicate that larger volumes indeed reduced the nitrite concentration in the scrubbing liquid, the tested volumes were limited by the size of the instrumentation. Further validation and optimization of the effect of the scrubbing volume on the nitrite concentration is recommended when implementing this approach.

Another option would be to increase the NO_x oxidation ratio. As shown in other experimental contexts, this can increase the removal efficiency as well as nitrate selectivity over nitrite [22,49,50]. By oxidizing NO to NO₂ and forming N₂O₄ instead of N₂O₃, it is likely that the reactions of Equations (7), (8) and (10) are favored over the reactions of Equations (6) and (9), lowering in this way the HNO₂ formation and disproportionation rate. The NO_x oxidation ratio is dependent on the composition of the plasma-produced NO_x gasses but also on the oxidation reaction of NO (Equation (4)), which is a spontaneous reaction, second-order dependent on NO partial pressure and first-order dependent on O₂ partial pressure [31,57]. As is often done, pressurizing the air in or at the outlet of the plasma process will improve the NO₂ content of the NO_x, as showcased, for example, by Tsonev et al. reaching an OR of 94% [41,58,59]. Another solution would be to prolong the residence time of the gas in the scrubber, as also noted by Abdelaziz et al. [33].

A third option to further lower the nitrite content would be to store the scrubbing solution in a storage tank after the desired nitrate concentration is reached. Braida and Ong (2000) showed that the decomposition of nitrite occurs spontaneously through either the nitrous acid disproportionation reaction (Equation (11)) or its decomposition to NO and NO₂ [36]. The rate of nitrite removal is dependent on the aeration rate and favored by lower pH values. The contribution of Equation (11) becomes larger when lowering the aeration rate. In the context of also maximizing the NO₃⁻ concentration, this would be the preferred option. At 1 mM NO₂⁻ and solution pH of 2.85, 90% of the NO₂⁻ would be removed after 24 h without extra aeration [36]. Thus, at low pH values, undesired nitrite and nitrous acid are expected to be eliminated over time, producing nitric acid and NO_x gas. The gas phase enriched with NO_x could be recovered from the storage tank and again injected into the scrubber to ensure no NO_x is released to the environment.

Plasma technology is a fast-developing research domain with various reactor types, each characterized by distinct energy efficiencies and NOₓ concentration outputs. When looking at industrial applications for fertilizer production, it is important to evaluate whether it is preferable to operate at a higher energy consumption over a shorter period of time or at a lower energy consumption over a longer duration, depending on renewable energy availability. Based on this evaluation, the most suitable reactor type can be selected, along with a corresponding NOₓ absorption unit.

The Haber–Bosch process for nitrogen fixation has an energy efficiency of 0.5–0.6 MJ/mol-N. State-of-the-art plasma reactors are currently reaching energy efficiencies approaching 1 MJ/mol-N and are therefore still less energy efficient [11,14,15]. Further development of plasma reactors and NO_x absorption units is needed to make this technology for green nitrogen fixation competitive with the Haber–Bosch process.

5. Conclusions

This study provides experimental data on the NO_x absorption chemistry in aqueous solution under conditions relevant for small-scale fossil carbon-free nitric acid production based on warm plasma technology. A synthetic gas mixture containing 1% NO_x, considered a relevant concentration range for current, energy-efficient warm plasma reactors, was sent over a gas–water contactor or scrubber. The scrubbing liquid was an aqueous solution with constant pH in the range 1 to 5 and was recirculated for up to 30 h.

The NO_x removal efficiency was observed to be higher for increased pH at the onset of the experiment, yet decreased over the course of the experiment to a plateau value of ca. 83%, independent of pH. The explanation lies in a corresponding increase in the HNO₂ concentration until a plateau is reached, and a negative correlation between HNO₂ concentration and removal efficiency. The steady-state HNO₂ concentration and, therefore, the HNO₂ decomposition rate were observed to be very similar for all pH values. It is thus concluded that pH does not influence removal efficiency when running experiments sufficiently long for a steady state to be reached. However, pH does remain an important parameter concerning the NO₂⁻ concentration, as it is the determining factor in the NO₂⁻ ↔ HNO₂ equilibrium.

This paper gives a concise insight in NO_x absorption kinetics, capacities and steady state removal efficiencies at a 1% NO_x concentration. It therefore aims to contribute to bridging a gap between classical NO_x absorption research and the upcoming plasma domain.

Besides the pH value, also other NO_x concentrations, oxidation ratios, flow rates or temperature effects can be studied in further research to clarify an often overlooked area of downstream NO_x absorption for small-scale plasma-based (H)NO₃ production.