Sicong
Tian
a,
Jianguo
Jiang
*abc,
Feng
Yan
a,
Kaimin
Li
a,
Xuejing
Chen
a and
Vasilije
Manovic
*d
aSchool of Environment, Tsinghua University, Beijing 100084, P. R. China. E-mail: jianguoj@tsinghua.edu.cn
bKey Laboratory for Solid Waste Management and Environment Safety, Ministry of Education of China, P. R. China
cCollaborative Innovation Center for Regional Environmental Quality, Tsinghua University, Beijing, P. R. China
dCombustion and CCS Centre, Cranfield University, Bedford, Bedfordshire, MK43 0AL, UK. E-mail: v.manovic@cranfield.ac.uk
First published on 25th April 2016
An efficient CO2 capture process has been developed by integrating calcium looping (CaL) and waste recycling technologies into iron and steel production. A key advantage of such a process is that CO2 capture is accompanied by simultaneous iron and CaO recycling from waste steel slag. High-purity CaO-based CO2 sorbents, with CaO content as high as 90 wt%, were prepared easily via acid extraction of steel slag using acetic acid. The steel slag-derived CO2 sorbents exhibited better CO2 reactivity and slower (linear) deactivation than commercial CaO during calcium looping cycles. Importantly, the recycling efficiency of iron from steel slag with an acid extraction is improved significantly due to a simultaneous increase in the recovery of iron-rich materials and the iron content of the materials recovered. High-quality iron ore with iron content of 55.1–70.6% has been recovered from waste slag in this study. Although costing nearly six times as much as naturally derived CaO in the purchase of feedstock, the final cost of the steel slag-derived, CaO-based sorbent developed is compensated by the byproducts recovered, i.e., high-purity CaO, high-quality iron ore, and acetone. This could reduce the cost of the steel slag-derived CO2 sorbent to 57.7 € t−1, appreciably lower than that of the naturally derived CaO. The proposed integrated CO2 capture process using steel slag-derived, CaO-based CO2 sorbents developed appears to be cost-effective and promising for CO2 abatement from the iron and steel industry.
Implementation of CO2 capture technologies in existing industrial sectors is urgently required, as carbon capture and storage (CCS) is the only current technology that would allow industrial sectors to realize a deep reduction in CO2 emissions.6 The development of CCS in various industrial sectors is springing up worldwide, leaving much room for deploying applicable technologies for industrial CO2 capture.7 As a promising alternative to conventional amine scrubbing and oxy-fuel combustion CO2 capture technologies, calcium looping (CaL), which relies on CaO as a regenerable CO2 sorbent upon cyclic carbonation and calcination reactions,8 has been widely investigated recently through bench- and pilot-scale demonstrations at sizes of 1 kWth–1.7 MWth.9–12 A recent techno-economic analysis of post-combustion CO2 capture technologies found that CaL is more energy-efficient and cost-effective than other emerging CO2 capture technologies, including chilled ammonia absorption, alkali–metal carbonate adsorption, and membrane separation;13 a further reduction in the CO2 capture cost can be achieved by integrating CaL with thermal energy storage.14
However, the dramatic decay in the cyclic CO2 capture performance of naturally occurring precursors-derived CaO, triggered mainly by sintering of CaCO3 during the CaL-based CO2 capture process, remains as an obstacle for the development and implementation of this technology. To overcome this limitation, various strategies have been investigated to date. Several measures, including thermal activation,15–17 steam hydration,18–21 and recarbonation,22 have been demonstrated to be effective in stabilizing the CO2 capture performance of naturally occurring sorbents. Another approach involves developing synthetic CaO-based CO2 sorbents with thermally stable surface areas and pore volumes, thereby minimizing performance deterioration for CO2 capture. This can be achieved by employing organic-carbon templates23–25 during sorbent preparation and introducing refractory supports26–28 into the CaO matrix. Broda and colleagues29 developed a highly effective MgO-stabilized, CaO-based CO2 sorbent via recrystallization of calcium and magnesium acetates in organic solvents. The as-prepared material exhibited an excellent CO2 uptake of 10.71 mmolCO2 gsorbent−1 after 10 harsh CaL cycles, with only 8 wt% of MgO required. However, the significantly increased cost for sorbent preparation due to the employment of organic acids should be considered before practical application.30,31
The iron and steel industry is the largest energy-consuming manufacturing industry in the world.32 Currently, more than 2.5 Gt of CO2 is emitted annually from the global iron and steel industry without implementation of any effective CO2 reduction measures.33 In addition to an urgent demand for CO2 abatement in the iron and steel industry, valorization of steel slag, a Ca-rich and Fe-containing industrial waste, is another challenge faced in iron and steel production. Global annual generation of steel slag is almost 200 Mt a−1, half of which is contributed by China.34 However, only 20% of the steel slag produced annually in China is utilized, and the other 80% is stockpiled in the open air.
The CaL-based CO2 capture process can be operated readily in a dual circulating fluidized bed system with regard to practical applications.10 Importantly, limestone is an essential feedstock for many energy-intensive manufacturing industries (e.g., the iron-and-steel and cement industries),32,35 making it feasible for integration into industrial processes for CO2 abatement. The potential synergy among power generation, cement production, and CO2 abatement in the cement industry has been investigated by integrating CaL into cement manufacturing processes, where spent CaO from the CaL cycle is reused directly as a “carbon-free” feedstock for cement production, resulting in almost zero sorbent cost and waste production for CO2 capture from the cement industry.35–38 However, no research on the integration of CaL into the iron and steel industry for CO2 abatement has been reported to date. Therefore, we have developed an efficient CO2 capture process (Fig. 1) by integrating CaL and waste recycling technologies into iron and steel production to help realize simultaneous CO2 abatement and steel slag minimization in the iron and steel industry. In this system, Ca and Fe in the steel slag are separated via the leaching of steel slag using acetic acid solution (acid extraction), with Ca extracted into the leachate and Fe concentrated in the residues. The Fe-rich materials can be recycled directly into the blast furnace, substituting for iron ore as the feedstock for iron production after magnetic separation. The CaO-based sorbent, derived from the precipitation of ions in the Ca-rich leachate and a subsequent dry-distillation of the resulting precipitate, is delivered to the CaL unit for CO2 capture. The spent sorbent can also be recycled into the blast furnace as a substitute for natural limestone to remove impurities in the iron ore during iron production. Such an integrated CO2 capture process is demonstrated to be highly efficient and cost-effective in this study, which is promising for application to CO2 abatement in the iron and steel industry.
![]() | ||
Fig. 1 General schematic of integrated CO2 capture and steel slag valorization process proposed for use in iron and steel industry. |
![]() | ||
Scheme 1 Sketch of operation route for preparing CaO-based CO2 sorbents and recovering iron-rich minerals from steel slag. |
Material | Acid concentration [M] | Extraction time [h] | Solid/liquid ratio [g![]() ![]() |
---|---|---|---|
1 M–0.5 h–1![]() ![]() |
1 | 0.5 | 1![]() ![]() |
1 M–2 h–1![]() ![]() |
1 | 2 | 1![]() ![]() |
2 M–0.5 h–1![]() ![]() |
2 | 0.5 | 1![]() ![]() |
2 M–2 h–1![]() ![]() |
2 | 2 | 1![]() ![]() |
3 M–2 h–1![]() ![]() |
3 | 2 | 1![]() ![]() |
5 M–2 h–1![]() ![]() |
5 | 2 | 1![]() ![]() |
The cyclic CO2 capture experiments were performed in the TGA with a precision of 0.001 mg. During each run, a small amount (∼25 mg) of sorbent was placed in a 150 μL alumina pan and heated to 900 °C at a rate of 20 °C min−1 under a N2 flow of 50 mL min−1. The temperature was held at 900 °C to calcine the sorbent for 10 min. Subsequently, the temperature was decreased to 650 °C at a rate of 50 °C min−1. Once the reaction temperature was reached, a gas flow of 75 mL min−1 containing 20 vol% CO2 and 80 vol% N2 was introduced into the reaction chamber to carbonate the sample for 10 min. Then, the reaction atmosphere was switched to a gas flow of 75 mL min−1 containing 80 vol% CO2 and 20 vol% N2, and the sample was heated to 900 °C at a rate of 50 °C min−1. After calcination at 900 °C for 5 min, a new CaL cycle was started by decreasing the reaction temperature to 650 °C under a N2 flow of 75 mL min−1. The carbonation–calcination cycle was repeated 20 times for each sorbent. The cyclic uptake of CO2, expressed in gCO2 gsorbent−1, was calculated from the continuously monitored weight change of the sample. Blank runs were performed to correct for the effects of buoyancy and change in gas density between different reaction steps.
CO2 capture characteristics of the steel slag-derived, CaO-based CO2 sorbents were also investigated by carbonating the material at 650 °C under a 20 vol% CO2/80 vol% N2 atmosphere for 120 min using TGA/DSC 2, after a pre-calcination of the sorbent at 900 °C under a N2 atmosphere for 10 min.
Fig. 3 plots the recycling efficiency of iron from the steel slag with an acid extraction, with raw steel slag included for comparison. It is shown in Fig. 3(a) that recovery of all magnetically-separated materials decreased with increasing centrifugal speed, regardless of whether raw slag or the slag with an acid extraction was employed. This is because a stronger magnetic force is required to separate phases at a higher centrifugal speed. However, there was a significant increase in the recovery of the magnetically-separated materials from the steel slag with an acid extraction compared with that from the raw slag. Increasing the dosage of acetic acid from 1 M to 3 M or 5 M during the acid extraction did not significantly increase the recovery of the magnetically-separated materials, probably because more iron was extracted into the leachate from the steel slag with higher concentrations of acetic acid as shown in Fig. 2. The iron content of the magnetically-separated materials from either the raw steel slag or the steel slag with an acid extraction increased with centrifugal speed (Fig. 3(b)); this is because the more magnetic phases could be separated at higher centrifugal speeds. Importantly, the iron content of all magnetically-separated materials from the steel slag with an acid extraction was appreciably higher than that from the raw slag, exceeding 55% at a centrifugal speed of 500 rpm. The magnetically separated materials corresponding to 2 M–0.5 h–1:
5 and 5 M–2 h–1
:
10 exhibited iron contents as high as 70.0% and 70.6%, respectively. These values were close to the theoretical iron content of 72.4% in pure magnetite, indicating that the as-separated materials could be a high-quality alternative to iron ore available for iron production. Therefore, when acid extraction of the waste steel slag is used, not only is high-purity CaO obtained for use in CO2 capture (to be discussed below) and subsequent iron production, but the recycling efficiency of iron is also improved significantly by increasing both the recovery of iron-rich materials and the iron content of the materials recovered.
The mechanism underlying the significant enhancement in the recycling efficiency of iron from steel slag was studied by characterizing the XRD patterns, as shown in Fig. 4. Ca12Al14O33 (mayenite), Ca(OH)2 (portlandite), (Ca1.92Fe1.08)Fe2(SiO4)3 (andradite ferroan), Ca2SiO4 (calcium silicate), and Mg6Fe2(OH)16CO3·4H2O (sjogrenite) were the major mineral phases in the raw steel slag sample. After acid extraction, the phases (Ca1.92Fe1.08)Fe2(SiO4)3 and Mg6Fe2(OH)16CO3·4H2O were no longer identified in the remaining steel slag residues, and a new phase, SiO2 (quartz), was present. This was likely associated with the reaction between acetic acid and these phases during the acid extraction process, where Ca and Mg were dissolved, leaving SiO2 in the residues. Upon a subsequent magnetic separation, Ca12Al14O33 became the major phase in the final steel slag solids. Fe3O4 (magnetite) and MgFe2O4 (magnesioferrite) were identified as the dominant phases in the magnetically-separated materials (at a centrifugal speed of 500 rpm), indicating that the formed Fe3O4 and MgFe2O4, with a theoretical iron content of 72.4% and 56.0%, respectively, are the Fe-rich phases available for magnetic separation from the steel slag with an acid extraction. Therefore, depending on the ratio of Fe3O4 to MgFe2O4, the iron content of the magnetically-separated materials should be 56.0–72.4%, which is in line with the results from samples at 500 rpm (Fig. 3(b)).
The change in morphology of the material 1 M–2 h–1:
10 during N2-TPD was further characterized using scanning electron microscopy (Fig. 6). The freshly dried 1 M–2 h–1
:
10 had a coarse structure with a comparatively compact surface (Fig. 6(a)). When heated to 600 °C, acetone was released due to the decomposition of calcium acetate, resulting in a slice-shaped morphology in the material (Fig. 6(b)). With subsequent decarbonation of CaCO3 before heating to 900 °C, a well-defined, porous structure, mainly comprised of fine CaO grains, formed in the freshly calcined 1 M–2 h–1
:
10 (Fig. 6(c)). XRD patterns of typical as-prepared CO2 sorbents in the freshly calcined state are shown in Fig. 7. The major phase, CaO, along with minor phases, MgO and CaS, were identified in 1 M–0.5 h–1
:
10, 1 M–2 h–1
:
10, 2 M–0.5 h–1
:
5, and 2 M–2 h–1
:
5, the materials with the same (low) mass ratio of acetic acid to steel slag during acid extraction (Fig. S2 in the ESI†). With increasing doses of acetic acid, small quantities of Ca2Fe2O5 and (MgFe)2SiO4 were detected in the 3 M–2 h–1
:
10 and 5 M–2 h–1
:
10 materials synthesized.
CO2 capture performance as a function of reaction time was compared between commercial CaO and the various CaO-based CO2 sorbents synthesized in this study (Fig. 8). Commercial CaO presented a classical two-stage CO2 capture regime under the conditions studied here.41 In the first 5 min, the commercial CaO experienced a fast and kinetically-controlled reaction stage as pores with a diameter <100 nm were filled by newly formed CaCO3. This was followed by a substantially slower reaction stage controlled by the diffusion of CO2 through the CaCO3 product layer. Alvarez and Abanades42 concluded that the transition between the two reaction stages occurs at a critical product layer thickness of ∼50 nm, which was better explained later by Li and colleagues43 through a rate equation theory they developed. The carbonation rate of the synthesized CaO-based CO2 sorbents was not as fast as that of the commercial CaO during the kinetically-controlled reaction stage. However, materials 1 M–0.5 h–1:
10, 1 M–2 h–1
:
10, 2 M–0.5 h–1
:
5, and 2 M–2 h–1
:
5 exhibited significantly faster carbonation rates than commercial CaO during the diffusion-controlled reaction stage, allowing their uptake of CO2 to surpass that of commercial CaO after a 20 min carbonation period. After 120 min, 1 M–2 h–1
:
10 achieved a CO2 uptake of 0.62 gCO2 gsorbent−1, which was 1.5 times as high as that of the commercial CaO, indicative of an activation effect of acetic acid on the CaO-based CO2 sorbents.44 Freshly calcined 1 M–0.5 h–1
:
10, 1 M–2 h–1
:
10, 2 M–0.5 h–1
:
5, and 2 M–2 h–1
:
5 exhibited similar uptakes of CO2, indicating that the extraction time and solid/liquid ratio did not influence significantly the isothermal CO2 capture performance of the steel slag-derived CO2 sorbents. This is probably because the extraction time and solid/liquid ratio had almost no effect on the elemental (Table S1†) and mineral (Fig. S2†) compositions of materials. However, the CO2 uptake experienced a significant decrease with increasing acetic acid dosage, which was likely associated with the lower CaO content in freshly calcined 3 M–2 h–1
:
10 and 5 M–2 h–1
:
10, as discussed in Fig. 2 and Table S1.†
![]() | ||
Fig. 8 Carbonation of the CO2 sorbents synthesized, with commercial CaO included for comparison, under a 20 vol% CO2/80 vol% N2 atmosphere at 650 °C for 120 min. |
The multicyclic CO2 capture performance of commercial CaO and the steel slag-derived, CaO-based CO2 sorbents synthesized in this study under realistic CaL conditions are compared in Fig. 9. The commercial CaO presented a slightly higher CO2 uptake of 0.27 gCO2 gsorbent−1 compared with the steel slag-derived sorbents 1 M–0.5 h–1:
10, 1 M–2 h–1
:
10, 2 M–0.5 h–1
:
5, and 2 M–2 h–1
:
5 in the first cycle, whereas 3 M–2 h–1
:
10 and 5 M–2 h–1
:
10 had lower CO2 uptakes of 0.16 gCO2 gsorbent−1 and 0.14 gCO2 gsorbent−1, respectively. However, the CO2 uptake of the commercial CaO experienced a drastic decrease within the first five cycles, and began to stabilize after falling to 0.07 gCO2 gsorbent−1 by the tenth cycle. For the steel slag-derived, CaO-based CO2 sorbents synthesized, two types of multicyclic CO2 capture characteristics were revealed. 3 M–2 h–1
:
10 and 5 M–2 h–1
:
10, although bearing a limited CO2 capture performance compared to commercial CaO, displayed a similar CO2 capture characteristic as the commercial CaO, i.e., the CO2 uptake dropped drastically during the first several cycles, followed by a comparatively stable uptake afterwards. However, 1 M–0.5 h–1
:
10, 1 M–2 h–1
:
10, 2 M–0.5 h–1
:
5, and 2 M–2 h–1
:
5, the materials with the same (low) mass ratio of acetic acid to steel slag during acid extraction, exhibited a different CO2 capture characteristic. A drastic decay in CO2 uptake occurred mainly between the first two cycles. Then, the CO2 uptake experienced a slow, linear decay with increasing CaL cycles. Because of this, the CO2 uptake of 1 M–0.5 h–1
:
10, 1 M–2 h–1
:
10, 2 M–0.5 h–1
:
5, and 2 M–2 h–1
:
5 exceeded that of the commercial CaO from the third cycle onward, and 1 M–2 h–1
:
10 captured almost twice as much CO2 as the commercial CaO by the end of the twentieth cycle. One would expect that the well-preserved porous structure of the cycled 1 M–2 h–1
:
10, compared to that of the commercial CaO, ensured its favorable CO2 capture characteristics (Fig. 6(c–f)). Therefore, the better carbonation reactivity (Fig. 8) and cyclic stability (Fig. 9) of the steel slag-derived, CaO-based CO2 sorbents 1 M–0.5 h–1
:
10, 1 M–2h–1
:
10, 2 M–0.5 h–1
:
5, and 2 M–2 h–1
:
5, when compared to commercial CaO, suggest that they are promising alternatives for use in CaL.
![]() | ||
Fig. 9 Multicyclic CO2 capture performance of the steel slag-derived, CaO-based sorbents synthesized, with commercial CaO included for comparison, under realistic CaL conditions. |
Material | Feedstock consumeda [t tsorbent−1] | Byproduct recovereda [t tsorbent−1] | Cost of sorbents [€ t−1] | |||
---|---|---|---|---|---|---|
Acetic acid | Limestone | CaO | Iron ore | Acetone | ||
a Prices of the components mentioned were determined according to the average price from the past 3 years in the Chinese market, i.e., 231.9 € t−1, 51.5 € t−1, 103.1 € t−1, and 450.9 € t−1 for acetic acid (≥99.8 wt%), limestone (∼90 wt%), iron ore (∼62 wt%), and acetone (≥99.5 wt%), respectively. b The component was not consumed or recovered. | ||||||
1 M–0.5 h–1![]() ![]() |
2.50 | — | 0.91 | 0.05 | 0.94 | 57.7 |
1 M–2 h–1![]() ![]() |
2.50 | — | 0.90 | 0.06 | 0.93 | 62.2 |
2 M–0.5 h–1![]() ![]() |
2.86 | — | 0.90 | 0.06 | 0.93 | 145.7 |
2 M–2 h–1![]() ![]() |
2.73 | — | 0.89 | 0.07 | 0.92 | 120.0 |
Naturally derived CaO | —b | 1.98 | — | — | — | 102.0 |
Given the enhanced CO2 capture performance of the steel slag-derived sorbents compared to naturally derived CaO, an increase in the cost of the as-prepared CO2 sorbents is acceptable as long as it remains below an upper limit, which largely depends on the CO2 capture capacity of the materials. Romeo and colleagues46 studied in detail the relationship between the increase in the maximum average CO2 capture capacity of CaO-based sorbents and the maximum acceptable investment in sorbents under different CaL operations, and proposed a useful approach to assess the availability of new CaO-based CO2 sorbents for use in CaL; we adapted this approach to assess the acceptable cost of the steel slag-derived CO2 sorbents developed in this study (Table 3). As expected, a more cost-effective CaO-based CO2 sorbent is required when CaL is performed under higher sorbent-to-CO2 ratios (R) or material make-up flows (fp), as more fresh sorbents are consumed under these operating conditions. Materials 1 M–0.5 h–1:
10 and 1 M–2 h–1
:
10 exhibited appreciable superiority over naturally derived CaO with regard to the cost of sorbents under all sorbent/CO2 ratios and material make-up flows. Material 2 M–2 h–1
:
5 was comparable with naturally derived CaO under low sorbent/CO2 ratios and material make-up flows, while the cost of material 2 M–0.5 h–1
:
5 was marginally higher than naturally derived CaO. However, it should be pointed out that the cost structure of the proposed integrated CO2 capture process was assessed here mainly based on the material flow analysis. The capital costs and variable operating costs commonly considered in practical CaL projects have not been mentioned yet at this stage. Nevertheless, the proposed integrated CO2 capture process using materials 1 M–0.5 h–1
:
10 and 1 M–2 h–1
:
10 appears to be cost-effective, which is promising for CO2 abatement applications in the iron and steel industry.
Material | X ave increasea [%] | Maximum acceptable cost of sorbents [€ t−1] | |||||
---|---|---|---|---|---|---|---|
R = 1.5 | R = 3 | R = 5 | |||||
f
p![]() |
f p = 2.5% | f p = 1% | f p = 2.5% | f p = 1% | f p = 2.5% | ||
a The subtraction of average carbonation conversion during 20 cycles between the steel slag-derived CO2 sorbent and naturally derived CaO. b The molar ratio of the CaO-based sorbent to CO2 during the CaL process. c The make-up flow (purge percentage) of fresh CaO-based sorbents in the calciner. | |||||||
1 M–0.5 h–1![]() ![]() |
3.8 | 117.2 | 109.4 | 112.6 | 109.7 | 111.4 | 108.9 |
1 M–2 h–1![]() ![]() |
7.6 | 132.3 | 116.7 | 123.3 | 117.3 | 120.8 | 115.9 |
2 M–0.5 h–1![]() ![]() |
5.9 | 125.6 | 113.4 | 118.5 | 113.9 | 116.6 | 112.8 |
2 M–2 h–1![]() ![]() |
5.4 | 123.6 | 112.5 | 117.1 | 112.9 | 115.4 | 111.8 |
Footnote |
† Electronic supplementary information (ESI) available. See DOI: 10.1039/c6gc00400h |
This journal is © The Royal Society of Chemistry 2016 |