The deliberate introduction of aerosols into the stratosphere as a means of solar geoengineering (SG) might reduce some climate risks. Yet physical risks and efficacy of stratospheric aerosol geoengineering are poorly constrained due to uncertainty in the climate’s response to aerosol radiative forcing and to local stratospheric processes that include stratospheric chemistry, heating, and aerosol microphysics. Uncertainties about local process can be reduced by experiments. A prior modeling study1 from our group suggested that calcium carbonate (CaCO3) might enable stratospheric geoengineering with reduced ozone loss or even ozone increase, but that study lacked measurements of important CaCO3-specific reaction rates. It assumed that uptake coefficients (the probability that a gas-phase molecule is reactively bound following collision with a solid aerosol surface) of ozone-relevant gas species on CaCO3 is independent of the fraction of CaCO3 that been consumed in the reaction. This uncertainty needs to be resolved by empirical methods.

The use of empirical tools to study solar geoengineering has been limited. Field experiments are contentious2. Modeling studies use existing experimental results for sulfate, but there have been very few laboratory studies to address uncertainties of SG using non-sulfate particles3,4. This work is among the first efforts5 to measure uptake coefficients on solid particles at stratospheric temperatures. Our purpose is reducing uncertainty about SG.

Sulfate is the most widely-studied material for stratospheric SG because of the prominence of natural sulfate aerosols in the stratosphere and the long history exploring their links to climate6. In addition, there appear to be ways to inject SO2 and likely H2SO4 based on existing technologies7,8. However, sulfate aerosols pose well-known risks such as ozone depletion and stratospheric heating. CaCO3 particles have been proposed as an alternative to sulfate, and major motivations include the potential to reduce both risks1,9,10,11,12. This work addresses the ozone depletion aspect. Many modeling studies that explore chemical impacts of potential SG deployment have shown ozone depletion effects from a range of sulfate distribution scenarios, chiefly due to their impacts on NOx (NO and NO2) and halogen species13,14,15,16. These effects could counteract the recovery of ozone under the Montreal Protocol and increase risks of SG scenarios designed to mitigate impacts of climate change.

Non-sulfate materials have been proposed to address various risks of SG. Nearly two decades ago, Teller and Wood17 proposed the use of alumina nanoparticles based on scattering considerations while cautioning about environmental impacts. Other solid particles including TiO2, SiC, ZrO2, diamond, and CaCO3 have been explored9,10,11,12. Diamond and alumina might reduce ozone depletion compared with sulfate when producing the same radiative forcing18.

CaCO3 produces much less stratospheric heating than does sulfate18, and is a plausible material given the extensive industrial-scale manufacture of micron-scale calcite particles1,19. CaCO3 could also address the risks of ozone depletion by reactive uptake of acidic species containing halogens, sulfur, and nitrogen, effectively scrubbing ozone-depleting species from the stratosphere. However, due to the competition between denoxification and dehalogenation, it is difficult to know the net effect on ozone a priori.

One important shortcoming of Keith et al.1 is uncertainty of the uptake coefficients due to lack of experimental data. Here we measure the uptake coefficients of four reactions at stratospheric temperature:

$${\mathrm{CaCO}}_3 + {\mathrm{HCl}}.$$
$${\mathrm{CaCO}}_3 + {\mathrm{HNO}}_3.$$
$${\mathrm{CaCl}}_2 + {\mathrm{HNO}}_3.$$
$${\mathrm{CaCl}}_2 + {\mathrm{ClONO}}_2.$$

These reactions are important as they directly impact the chlorine and nitrate budget in the stratosphere, which critically affect stratospheric ozone concentration20. Eqs. (1) and (2) determine the capacity of CaCO3 to sequester NOx and halogen species, and Eq. (3) and Eq. (4) release reactive halogen species back to the stratosphere. We did not include heterogeneous reactions of gaseous HBr, BrONO2 and H2SO4 with CaCO3 particles because Keith et al. showed that these reactions caused little change in background mixing ratios of BrOx or H2SO4. Uptake coefficients of Eqs. (1) and (2) have been experimentally determined, but not under stratospheric conditions21,22. Uptake coefficients of Eqs. (3) and (4) have not been studied previously. In addition, Keith et al. did not include heterogeneous catalysis on CaCO3 surfaces such as ClONO2 + HCl. Here we assess the potential impacts of these reactions. We find that exposure to gas-phase acids causes CaCO3 particles to age rapidly, reducing their reactivity. This is in stark contrast to liquid sulfuric acid particles with surfaces that are unaffected by aging. We use these data to constrain a chemical transport model of stratospheric chemistry and aerosol microphysics and find that the prior model results overestimated ozone response.


Experimental determination of uptake coefficients

Flow tube experiments have been widely used to study heterogeneous uptake coefficients for gas-solid reactions relevant to the stratosphere. For example, Molina et al. studied the uptake of ClONO2 on silica and alumina in the presence of HCl5. Davies and Cox23 studied the reaction between HNO3 and NaCl. Schmidt et al.24 studied reaction between acetone and TiO2. Figure 1a shows the schematic of our flow tube experiment, it is similar to Molina et al. with slight modifications. We synthesized ClONO2 inline using plasmonic dissociation of Cl2 and cryogenically purified it inline (more details in the method section). As there are no literature values for the uptake coefficient of ClONO2 on CaCl2, we first compare our results for the uptake coefficients of ClONO2 on NaCl with existing literature values to validate our synthesis and measurement methods. The results confirm that our experimental and analysis approach as well as our ClONO2 synthesis method produce valid results: the uptake coefficient of ClONO2 on NaCl was determined to be 5 ± 3 × 10−3 at room temperature, which is close to the values reported in literature (Gebel et al.25 reported 6.5 ± 3 × 10−3).

Fig. 1: Schematics of the experimental setup and some potentially important reaction processes.
figure 1

a Schematics of the flow tube and mass spectrometer used for the flow tube experiments. b Schematics of the important physical and chemical interactions during heterogeneous uptake of gaseous molecules.

Uptake coefficients were calculated using the method of Knopf et al.26 (details in the “method” section). Typical time series for an uptake experiment for Eqs. (1) and (4) are shown in Fig. 2a, b and more detailed uptake coefficients measured are shown in Table 1. Consistent with previous literature, the reactions all show large initial uptake which gradually decays to a slowly varying semi steady state value (uptake signal changes by <5%/min). This process demonstrates a slow deactivation of the particles’ reactivity for gaseous uptake reactions.

Fig. 2: Results from uptake experiments.
figure 2

a, b Typical uptake signal from the flow tube experiments for HCl + calcite and ClONO2 + CaCl2 reactions respectively. The baseline was subtracted and signal normalized to the background level. c, d Results from long-term uptake experiments and parametric fit results for HCl + Calcite and ClONO2 + CaCl2 respectively. Thickness-dependent uptake coefficients listed in Table 1 are extracted from these fits. Error bars in the data points in c represent systematic error from the experiment. Results from the mass spectrometer measurements are overlaid on the plots. The shadowed regions show 95% confidence intervals of the parametric fit extracted using bootstrapping as outline in the experimental section. The standard errors for fitting parameters A and n (defined in the text) are 0.18 and 0.05, and the covariance is −0.08.

Table 1 Parameterization of thickness-dependent uptake coefficients.

Uptake coefficients at the semi steady state are shown in Table 1. For Eq. (2), this level occurs after about 10 min. Immediately after the insert is retracted upstream of the injector following the uptake experiment, a small increase in the HCl signal corresponding to reversibly adsorbed HCl on the surface is observed, consistent with the uptake experiment results in literature and the observation that HCl is reversibly adsorbed on the calcite surface before irreversible uptake occurs21. For Eq. (2), the semi steady state level occurs after about 3 min. In contrast to Eq. (2), there is no desorption peak after the insert is pulled upstream of the injector, signaling that this reaction proceeded without the adsorption step as in Eq. (2). For the HNO3 uptake reactions, the initial rapid changes in uptake could not be observed because there is a prominent time-varying background uptake by the quartz insert, while the background uptake of HCl and ClONO2 are smaller and did not show time-dependent characteristics. We therefore did not extract the time-dependent uptake signal for these reactions as the case for Eq. (2) and (3), and calculated the semi steady-state uptake coefficient based on the difference in mass spectrometer (MS) signal between the background value and after the signal reaches a steady value.

Flow tube experiments measure rates of surface reactions but are not suited to explore continuous changes in the uptake coefficients after exposures on the order of days or weeks as the uptake signal decreases below the detection limit. To explore the long-duration regime we conducted a set of long-term uptake “flask experiments” to measuring reaction rates between CaCO3 particles and HCl.

Flask experiments are conducted for Eq. (1) with three HCl concentrations, and the results are shown in Fig. 2c. The result from one flow tube experiment is also displayed for comparison. The concentrations span six orders of magnitude, and for each HCl concentration, we see that the reacted layer thickness growth rates decrease with reaction time, representing decreasing reactive uptake coefficients as a function of reaction extent.

Estimating thickness-dependent uptake coefficients

Unlike liquid sulfate particles, whose surface chemical composition are not affected by gas-phase uptake, CaCO3 particles age under gaseous exposure as products accumulate on their surfaces. As a result, the uptake coefficients change with exposure. We incorporate these changes by formulating uptake coefficients that depend on the product layer thickness and refer to them as thickness-dependent uptake coefficients. This is challenging because uptake coefficient changes are affected by many processes including the changes of available CaCO3 reaction sites as a function of reaction extent, adsorption and equilibration of water on the particle surface21, diffusion of gaseous species to available reaction sites, crystallization of reaction products27, and steric changes that might cause fractures in the product layer (schematics shown in Fig. 1b). Various empirical models were used to account for these changes including a shrinking-core model28, a Crystallization and Fracture modeling framework29, a kinetic model30, and a surface solvation model31. None of these processes have been studied extensively under stratospheric conditions. We therefore posit a semi-empirical model that assumes that the gas phase uptake rate is proportional to the diffusion rate of reactive gaseous species through a surface product layer to reach available CaCO3 reaction sites. The physical intuition is that the reaction rate is dominated by a diffusion-like process where the availability of the reactant plays a dominant role after the initial surface product forms and slows further reaction. The corresponding form of the cumulative product per unit area is \(n_p = A(C^nt)^{\frac{1}{2}}\), where A is the fitting parameter to the empirical data, C is the concentration of the gas phase reactive species, t is time of reaction, and n is an empirical constant chosen differently for various reactions based on their uptake mechanisms. As discussed in the experimental result section, Eq. (2) proceeds following an initial reversible surface adsorption and dissociation of HCl on CaCO3, and n was chosen as 1/2, consistent with the argument of Huthwelker et al.32; Eq. (4) proceeds without the initial reversible adsorption, and n was set to be 1. For Eq. (2), 1/2 is also the best fit for the data when n floats in the fitting routine. The uptake mechanisms for Eqs. (2) and (3) are unknown, and we formulated the reactions based on both the 1/2th and 1st order assumptions. This expression of np was chosen as it parsimoniously captures the reaction and diffusion processes. The corresponding thickness-dependent parameterizations are shown in Table 1. We selected this model because it fits our data well and is parsimonious (with only essential parameters to ensure low model variances) considering the high uncertainties due to various kinetic processes. We attempted a few other fitting models that are either more complicated or do not explain the experimental trends as well (Supplementary Fig. S1). The 95% confidence interval shown in Fig. 2c, d are calculated using bootstrapping33 and shows higher error where data are sparse.

Modeling global ozone impact

We use a slightly updated version of the atmospheric chemistry model used in Keith et al.1, adopting the highest injection rate of 5.6 Tg/yr CaCO3 from that analysis (see “method” section). In addition to the scenario using the full thickness-dependent parameterization (thk-dep) and the 2040 baseline scenario without solar geoengineering, we studied five other scenarios: (i) thk-ind, with thickness-independent uptake coefficient (γ) values from the second column in Table 1, (ii) no psc, with the same γ values as in the thk-dep case but with polar stratospheric clouds (PSC) reactions turned off, (iii) 0 × γ, with γ values for Eqs. (1)–(4) set to 0, (iv) thk-dep + conc-dep, with thickness-dependent γ values using the alternative concentration-dependent γ values for Eqs. (2) and (3) (this captures uncertainties in the uptake mechanism of Eqs. (2) and (3) as described in the previous section), and (v) 10 × γ, with γ values set to ten times the thk-dep case. The 0 × γ and 10 × γ scenarios capture the uncertainties of calcite particle surface area density since changing the uptake coefficient is equivalent to changing the surface area density available for gas-phase uptake.

Figure 3 shows the impact of CaCO3 emissions on ozone loss rates caused by important ozone depleting species compared with Keith et al. The NOx cycles play a much more important role than ClOx for all cases, and the thk-dep case shows an increase over the baseline in the NOx-related loss rates in contrast to the results from the thk-ind scenario and Keith et al. This is consistent with the decrease in ClO and increase in NOx mixing ratio for the thk-dep case in Supplementary Fig. S2. The impact on column ozone as a function of time and latitude is shown in Fig. 2b, c. The thk-ind scenario predicts an increase in ozone columns over the baseline similar to results from Keith et al., while the thk-dep scenario negates most of these increases.

Fig. 3: Changes in important ozone depleting species and ozone compared with Keith et. al.1 estimates.
figure 3

a Annually averaged rate of ozone loss caused by NOx and ClOx catalytic cycles as a function of altitude, averaged from 60°S to 60°N. b Changes (percent) in ozone column estimates using the thk-dep parameterization compared with the baseline scenario with no solar geoengineering. Positive values indicate ozone increases. c Differences in ozone column estimates (percent) between the thk-ind scenario and the thk-dep scenario compared to the baseline outcomes. Positive values mean higher ozone estimates using the thk-ind parameterization.

Changes in important ozone depleting species and ozone are shown in Fig. 3, and annually averaged meridional ozone changes over the baseline from these scenarios are shown in Fig. 4. The thk-ind scenario results in a globally averaged column ozone increase of 5%, while the thk-dep scenario shows a 1% decrease. For both cases, the largest ozone changes occur in the southern hemisphere. The thk-ind scenario shows column ozone increase of as high as 24%, while the thk-dep scenario shows a much smaller change of up to 3% reduction.

Fig. 4: Meridional ozone changes compared to 2040 baseline assuming various parameterizations of the uptake coefficients.
figure 4

The range of results obtained from Keith et al.1 are shown in the shaded region. These correspond to thickness-independent uptake coefficients for Eqs. (1)–(4) with values between 10−4 and 1. In the case of ten times of the physical surface area (10 × γ), only heterogeneous reaction rates were varied, and not the physical coagulation processes.

This ozone change in the thk-dep scenario below the baseline are caused primarily by NOx. As Fig. 3 shows, the changes in the NOx and ClOx cycles are smaller and in the opposite direction compared with the Keith et al. estimates, and the overall effect is a decrease in the ozone column compared to the baseline. Similarity between results from the thk-dep scenario and the 0 × γ results show that these impacts are not caused by Eqs. (2)–(4) but are predominantly caused by the decrease in background sulfate from neutralization by CaCO3 particles. This causes a decrease in Cl activation and ClO concentration, which in turn results in less ClONO2. It also leads to less heterogeneous hydrolysis of N2O5. Both lead to increased NOx levels that drive ozone loss around the altitude of CaCO3 injection. Another impact of the decreased sulfate is a slight decrease in PSCs. However, the comparison between the thk-dep result and the no psc result shows that the column changes due to PSC variations do not offset the ozone decrease caused by NOx increase.


Most narrowly, this study shows that our prior work overestimated the impact of CaCO3 aerosol on ozone chemistry. The aged CaCO3 aerosol is close to unreactive with respect to gas-phase uptake reactions. As a result, these uptake coefficients produce smaller ozone response in the opposite direction than predicted in Keith et al., and thus no contribution to the restoration of column ozone. However, since CaCO3 reduces stratospheric heating and ozone depletion compared to sulfate aerosols, and since there may be methods of increasing the ozone benefit of CaCO3 by increasing surface reactivity, it is still a viable candidate for SG.

The reduced ozone response is robust under a wide range of uncertainties. To assess the impact of uncertainties in the thickness-dependent γ parameterizations, we conduct model runs assuming upper and lower limits of the thickness-dependent uptake coefficient confidence intervals shown in Fig. 2c, d. In addition, we capture uncertainties in surface area density of the CaCO3 particles with the 10-γ and 0-γ scenarios. Neither this scenario nor the inclusion of gas-phase concentration-dependent γ for Eqs. (2) and (3) (thk-dep + conc-dep) produce more than 1% ozone column differences anywhere as shown in Fig. 4. This is explained by the fact that the ozone response is dominated by changes in sulfate surface area, not uptake reactions of gas-phase species on CaCO3.

More generally, these results highlight the importance of considering changes in uptake coefficients due to gas-phase exposure when determining the impacts of solid reactive particles. Further studies should explore the uptake coefficients of other ozone related gases. The details of the physical and chemical changes from reaction with sulfate aerosols, including those that contain organics34 are also important. Finally, there is uncertainty about how reactivity depends on the details of morphology and surface chemistry, which is important because CaCO3 aerosol could be produced by a variety of technologies35.

Our work illustrates how laboratory research can address uncertainties in stratospheric aerosol geoengineering. It is likely that there will be many other examples of novel measurements that can be accomplished with well-established experimental methods and are crucial in evaluating novel proposals that address risks posed by SG. As an illustration, the following experiments are straightforward applications of existing methods yet could be important to assessing SG risks:

Other heterogeneous reactions on CaCO3

Heterogeneous reactions of ClONO2 and HOCl with water and HCl on particle surfaces present key uncertainties of ozone response to CaCO3 geoengineering. Among these, reactions with HCl could be more important since the uptake coefficients of ClONO2 in the presence of HCl was shown to be two orders of magnitude greater than in the presence of water on solid surfaces5,36. Including an uptake coefficient of 0.02 for ClONO2 + HCl (the value measured on alumina surface5) for both the thk-dep and thk-ind cases decreases global ozone column by 2–3% compared to cases without this reaction (Supplementary Fig. S3). Ozone decreases up to 15% below the baseline over the south pole in the thk-dep case. Further including an uptake coefficient of 0.1 for HOCl + HCl did not change the ozone columns by more than 0.5%. Our results modified the ozone response estimate of Keith et al.1, but some relevant reactions are still poorly constrained by experiment. A next step would be to measure reaction rates of ClONO2 + HCl on fresh and aged CaCO3 surfaces.

Optical properties of CaCO3 aerosol

The major proposed advantage of CaCO3 over sulfuric acid aerosol is that it causes less radiative heating due to less solar and IR-band absorption and thus could pose lower risk with respect to changes in dynamics, which are poorly understood9. Yet, this hypothesis is based on bulk optical properties of pure CaCO3 that may differ from aged CaCO3 aerosols in the stratosphere (e.g., surface salts could form hydrates that shift the absorption of terrestrial radiation and Ca(NO3)2 may absorb in the UV). Well-established methods could be used to measure the real and imaginary index of refraction of aged CaCO3 powder. The aging process should include a range of stratospherically relevant processes including gas-phase reactions (as we explored in the flask experiments) and exposure to UV radiations.

Ice nucleating properties

Aerosols used in SG may impact cirrus cloud formation once they descend into the upper troposphere37,38. The ice nucleating properties are important in determining impacts of the sedimented aerosols on cirrus clouds. In addition, ice may nucleate onto the CaCO3 particles in the Antarctic winter under PSC conditions, affecting PSC formation. Experiments using a variety of laboratory experimental techniques39 could test ice nucleating properties on CaCO3 powder that had been prepared under the range of conditions described in the prior paragraph. For example, Cziczo et al.4 has tested ice nucleating properties of CaCO3, CaSO4, and Ca(NO3)2 and found that they can cause significant changes to cirrus clouds absent of natural ice nucleating particles4.

This study may have lessons for management of solar geoengineering research. Sound estimates of SG’s risks and efficacy will require experiments and models. Current estimates are almost entirely based on large-scale modeling. Models are crucial, but overreliance on models may encourage overconfidence when users ignore the simplifications hidden in their assumptions. Empirical methods are needed to help reduce uncertainty. Models can explore how results depend on uncertainty in parameters to motivate experimental research which, in turn, can provide better constraints on parameters used in models. The back-and-forth between the experimental and modeling communities is essential for environmental science. The complexity of experimental results like these may serve as a useful reminder of the deep uncertainties underlying predictions about the consequences of solar geoengineering.


Gas flow system and flow tube

All gas tanks are purchased from Airgas except for the SF6 gas (Praxair, research grade). The nitrogen gas is ultra-high purity, and the HCl gas is a 1% blend in nitrogen. The nitric acid is generated from a permeation tube (KIN-TEK Trace Source Refillable permeation tube with a target emission rate of, ng/min at 50 °C). When doing experiments, we operate the permeation tube at 20 °C and calibrated the emission rate using the mass spectrometer.

The flow tube is jacketed with a length of 1 m and an inner diameter of 26 mm. The insert has an inner diameter of 22 mm, wall thickness of 1 mm, and length of 22 cm. The cooling was done by circulating an ethanol-dry ice mixture through the jacket. The temperature of the gas stream is monitored by three K-type thermocouples at the two ends and the middle of the flow tube. The temperature gradient of a typical experiment through the flow tube is 1–2 K. For all the flowtube experiments, the flowtube temperature was controlled at 215 K and the pressure was 1.7 Torr. Since only dry gas streams are used in the flowtube experiments, and the reactive gas streams pass through a ~20 cm quartz tubing at 215 K before reacting with particles, we treat the water vapor content in the experimental region to be 0.

ClONO2 Synthesis

The ClONO2 synthesis consists of three steps:

$$\quad \,\,\,\,\,{\mathrm{Cl}}_2\mathop {\longrightarrow }\limits^{{\mathrm{RF}}\;{\mathrm{plasma}}} 2{\mathrm{Cl}}.$$
$${\mathrm{Cl}} + {\mathrm{O}}_3 \to {\mathrm{ClO}}.$$
$${\mathrm{ClO}} + {\mathrm{NO}}_2 \to {\mathrm{ClONO}}_2.$$

The gas tanks are all purchased from Airgas (Ar: HP grade, O2: UHP grade, Cl2 and NO2: 1% blend in nitrogen). The RF plasma is generated by a Technical Research and Manufacturing Inc. DBS301 RF generator with a frequency range of 0.125–0.25 GHz. The Power output is measured by a Bird 43 General Purpose Wattmeter and is tuned to be between 15 and 40 W during operation. The ozone is generated from an A2Z Ozone MP 1000 ozone generator. The ozone concentration as measured by an ozone meter is 1.5%.

The synthesis conditions were simulated in a box model to guide selections of design parameters that resulted in the highest ClONO2 yield. A quartz tube acts both as an RF cavity for generating the chlorine radical and as a mixing region for the combination of ClO and NO2. The length of the quartz tube is 70 cm. The distance between the two vertical flanges is 40 cm. The outer diameter is 1/2 in. and the inner diameter is 1.01 cm. We assumed no radical remains after the cold trap because the quartz wool in the cold trap provides a large surface area for them to recombine or otherwise react.

After ClONO2 is synthesized, it is collected and purified in a cold trap cooled by a cold jacket where chilled nitrogen gas flows through. The concentration of the effluent ClONO2 is measured through absorption spectroscopy in a quartz cell with an absorption length of 99.14 cm. Absorption spectra in the 200–295 nm region were acquired using a fiber-coupled Ocean Optics USB4000 UV–Vis spectrometer (10-µm slit width, 200–400 nm 5 grating) illuminated by a Hamamatsu L2D2 deuterium lamp. The concentration of ClONO2 is then calculated based on the absorption cross section data in the JPL database40. It is determined to be about 75 ppm under typical synthesis conditions.

Material and preparation for the flow tube experiment

The calcite particles is purchased from American Elements with a manufacture-reported average diameter of 200 nm. The Brunauer–Emmett–Teller (BET) surface area of these particles is measured by a Quantacrome Monosorb instrument using N2 as the adsorption gas. The BET surface area reported was 14.8 ± 0.5 m2/g. We also measured the BET surface area of samples after processing by isopropyl alcohol (IPA) and found that IPA processing did not change the BET surface area. The NaCl particles (puriss. p.a., ≥99.5%, powder or crystals) used are purchased from Sigma Aldrich. To increase the amount of surface area per unit mass, the particles are then processed in a Retsch PM100 planetary ball mill. The BET surface area of the resulting NaCl particles is measured by a Beckman Coulter SA 3100 Surface Area Analyzer using He as the absorption gas. The BET surface area is 0.051 ± 0.005 m2/g for NaCl before milling, and 0.38 ± 0.05 m2/g after milling.

Before the experiment, the CaCO3 particles are deposited on the insert from a suspension of CaCO3 in IPA. A known volume of a suspension with known mass concentration of CaCO3 is pipetted into the insert. The insert is heated at roughly 60 °C and rotated to spread the particles evenly over the insert while the IPA evaporates. This process is repeated until a desired amount of CaCO3 is deposited on the insert. The insert is then heated in an oven at 250 °C for roughly 30 min to drive off any excess IPA. A similar deposition method has been used to prepare inserts for other flow tube experiments24. Typically, the insert is deposited with ~2.5 layers of particles. For uptake experiments on CaCl2, the CaCO3 insert is exposed to about 70 Torr of HCl vapor in the flow tube for at least 8 hrs at room temperature forming a layer of CaCl2. The insert is then used directly for the uptake experiment without being exposed to room air after the flow tube is pumped down. This method is used because CaCl2 is hygroscopic and cannot be purchased in its dehydrated form. We confirmed that this produced at least 2 nm of CaCl2 using the same procedure for determining chloride content as for the long-term uptake experiment. The NaCl particle insert was prepared in the same way as the CaCO3 insert. Before each uptake experiment, the insert is placed into the flow tube which is pumped down to ~60 mTorr for at least 2 h before an uptake experiment starts. According to Santschi and Rossi21, this is sufficient to drive off all but strongly-bound surface water. It is possible that some IPA molecules could adsorb to the CaCO3 surface even after the oven and vacuum processing. However, we expect this effect to be small since heating has been shown to be effective at removing adsorbed water from CaCO3 surfaces by Santchi and Rossi, and IPA is more volatile than water.

Flow tube experiment

The uptake experiment design follows Molina et al. but differs in two respects. First, instead of moving the injector with respect to the stationary insert and flow tube, the insert is moved relative to the stationary injector and flow tube. Four magnets attached to the injector rod and the insert allow for this configuration. This eliminates condensation on the injector when it retracts from the low temperature region of the flow tube without having to heat the injector. It also eliminates the possibility of gas leaks into the flow tube due to mechanical movement of the injector relative to the vacuum seal. Second, instead of electron impact ionization, ions are produced by chemical ionization by SF6 as outlined in Huey et al.41.

An alternative method used in the literature to measure heterogeneous uptake coefficients is the aerosol flow tube experiment, where the aerosols are dispersed in a gas stream and flow with the carrier gas42. This method eliminates issues with gas-phase diffusion limitations and gas-transfer limitations within the particle layers. However, one key disadvantage of aerosol flow tube experiment compared to our coated wall flow tube experiment is that it is difficult to extend the residence time of particles in the reaction region beyond tens of seconds. As shown in the results section, reactive uptake coefficients on CaCO3 particles continue to change for more than 10 min due to gradual surface saturation. Aerosol flow tube experiments cannot capture changes in this process. To overcome the issue with gas phase diffusion limitation with the coated wall flow tube experiments, we applied a correction to the uptake coefficients as outlined in the following section. This correction was small due to the low uptake coefficients measured in our experiments. In addition, to probe the effect of gas transfer limitations within the particle layers, we measured uptake coefficients of Eq. (2) for different CaCO3 layer thickness and found that the uptake coefficients measured at the semi steady state were 2 ± 1.5 × 10−4, 4 ± 2 × 10−4, and 3 ± 2 × 10−4 for 0.5, 1.5, and 2.5 layers of coated CaCO3 thickness on the insert. These are similar to values reported by Santschi and Rossi21 for cleaved CaCO3 marbles and did not differ with layer thickness, showing that the diffusion limitations within the particle layer was not a concern for our experiments. Another way to validate this result is to calculate the diffusion-reaction length scale. Assuming a pseudo first-order reaction and using Fick’s Second Law, we can write out the reactive concentration at steady state as where C is the concentration of the reactive gas, t is the reaction time, D is the inter-diffusion constant (45.44 cm2/s for HCl in N2 at 213 K and 1.67 Torr), and k is the pseudo first-order reaction constant. For the purpose of this calculation, k is related to the uptake coefficient γ by k = γAvω, where Av is the volume-normalized particle surface area (for calcite, 4.02 × 107 m2/m3 based on the BET surface area measurement), and ω is the average molecular velocity. Taking γ to be 5 × 10−3 (high end of the values in our measurement), the diffusion length scale is then and is calculated as 45 µm. Correcting for the porosity of the particle stack does not change the order of magnitude of this length. The length is much larger than the average particle layer thickness (<1 µm) and provides a theoretical justification for why the measured γ is not influenced by the thickness of the particle layer.

Uptake coefficient calculation

The uptake coefficients are calculated based on methods in Knopf et al.26. First, γeff, the effective uptake coefficient, is calculated from the experimental observations assuming first-order reaction kinetics as:

$$\gamma _{eff} = \frac{{D_{tube}}}{{\omega _xt}}{\mathrm{ln}}\left( {\frac{{\left[ X \right]_{g,0}}}{{\left[ X \right]_g}}} \right),$$

where Dtube is the tube diameter, ωx is the thermal molecular velocity, t is interaction time between gas and particles, [X]g,0 and [X]g are concentrations of the uptaken gas X at the entrance and exit of the inset respectively. In the experiments these are measured as concentrations before and after the insert is exposed to the reactive gas stream. [X]g,0/[X]g is the penetration ratio. The gas phase diffusion effects are then corrected to calculate the actual uptake coefficient γ as:

$$\gamma = C\frac{{\gamma _{eff}}}{{1 - \gamma _{eff}\frac{3}{{2N_{Shw}^{eff}Kn_X}}}},$$

where C is the ratio between the geometric area of the insert and the BET surface area of the particles, NeffShw is the effective Sherwood number, and KnX is the Knudsen number following the definition in Knopf et al. As outlined in Knopf et al., the gas phase correction factor (γeff/γ) decreases with increasing uptake coefficients. Under our experimental conditions, this correction factor ranges from 1 to 5%.

Uptake experiments were first performed on a blank quartz insert using the same procedure as for the uptake experiments to determine the baseline uptake. No significant uptake was observed for HCl and ClONO2. However, HNO3 showed a large uptake signature. The uptake signal of this baseline uptake at steady state was extracted from these experiments and subtracted from the uptake signals when calculating the uptake coefficients.

Flask experiment procedures

0.1 g of CaCO3 particles are deposited at the bottom of a glass vessel. A mixture of HCl gas and N2 gas controlled by upstream mass flow controllers flows through the bottle, allowing HCl vapor to react with the particles. The pressure of the bottle is controlled by a check valve at roughly ambient pressure. Before reaction starts, the vessel is secured in a box of dry ice for roughly 10 min, so its temperature equilibrates. During this time, dry nitrogen gas flows through the bottle to drive away room air left in the bottle. After the reaction process completes and the HCl gas flow is turned off, the N2 gas flow continues for an extra 10 min to allow all HCl gas metered into the flow system to pass through the reaction vessel. For longer-term reactions, the dry ice is replenished roughly twice per day to maintain the temperature of the bottle. After the reaction, the particles are suspended in 10 mL of milli-q water so the CaCl2 on the surface would dissolve in the water. The suspension is then filtered through a 20 nm syringe filter. The Cl concentration in the resulting solution is measured by a Cole–Parmer Combination Ion-Selective Electrode for chloride ions. The electrode is calibrated each time before a measurement using known concentrations of CaCl2 solutions that bracket the measured Cl concentration range. The thickness of the CaCl2 layer formed is calculated using the BET surface area, the bulk density of CaCl2, and the total amount of Cl ions reacted with the CaCO3 particles.

Error characterization

For the flow tube experiments, random errors in the uptake coefficients arise from uncertainties in various physical measurements and the MS signal noise. To first order, random errors correspond to the partial differential of uptake coefficient (γ) with respect to uncertainties of the respective factors. We considered uncertainties arising from measurements based on instrument specifications (temperature: ±5 K, pressure: ±5 mTorr, flow: ±3 sccm, and BET surface area: ±0.5 m2/g). These uncertainties correspond to roughly 30% of total uncertainties across the range of γ values we measured (the BET surface area measurements account for 90% of this uncertainty), and the MS signal noise account for the remaining 70%.

For the flask experiment measurements, random errors come mainly from the precision of the ion-selective electrode used to measure the chloride ion concentration (2% of the measured voltage). Another source of error is the dead volume in the glass vessel, which takes time for the influent HCl–N2 mixture to displace at the start of the reaction. To account for this effect, we included an uncertainty term that is equivalent to the time that the influent gas fully displaces the dead volume (~10 s). This effect is negligible for longer period reactions (>1 min) but has a significant effect for the shorter-term reactions.

Modeling method

In order to probe the impact on global stratospheric ozone, we conduct similar simulations as Keith et al.1 using the AER 2-D chemical transport-aerosol model. All model specifications follow that study except for the uptake coefficients to isolate the impact of uptake coefficients measured in this work. We investigate the highest CaCO3 emission rate in that study with 5.6 Tg yr−1 of uniform CaCO3 emission between 30°S and 30°N and between 20 and 25 km. This produces roughly 2 W m−2 of global radiative forcing (RF). CaCO3-related reactions that are included in the model consist of Eqs. (1)–(4) and coagulation of sulfate aerosols with CaCO3 particles. The coagulation was treated in the same way as Keith et al.1, assuming liquid sulfate reacts with CaCO3 to form CaSO4 instantaneously once sulfate aerosols coagulate with CaCO3 aerosols. Future atmosphere trace gases for 2040 conditions are taken from RPC 6.0, providing 2.3 ppbv of Cly in the upper stratosphere but with temperature and circulation from a 1978–2004 climatology.