1 Introduction

Pulp and paper production is one of the largest industrial energy users (IEA 2014). The raw material used in chemical pulping is mainly woody biomass. Over 80% of the carbon dioxide (CO2) emissions are from burning of residual biomass. Of the global capacity, a significant portion is at forest industry sites (Vakkilainen et al. 2013). Comparison of global capacities of plants converting biomass for energy purposes shows that recovery boiler capacity is much larger than other biomass boiler capacities (Fig. 1).

Fig. 1
figure 1

Comparison of the global capacities (petajoules, PJ) of various types of biomass plants (Vakkilainen et al. 2013). BFB and CFB refer to bubbling fluidized bed and circulating fluidized bed, respectively

Sustainability, emission trading and control, environmental regulations, corporate image, self-sufficiency of fuel supply, and the price of fossil fuels are among the many factors driving companies to reduce usage of fossil fuels. In the chemical pulp industry, a large share of energy use is already biomass-based, and in normal operations, modern kraft pulp mills are usually self-sufficient in energy, with the exception of lime kiln operations. Fossil fuels are primarily used to reduce lime mud to burnt lime. They are also used during upsets, start-up and shut-down, as well as sometimes for safety reasons, e.g., to secure non-condensable gas destruction (Vakkilainen and Kivistö 2008; Vakkilainen and Kivistö 2014). The lime kiln is typically the only unit operation utilizing fossil fuels during normal operations, and, consequently, the main source of fossil fuel-based emissions. When the woody raw material is from a sustainable origin, the mill operations can be considered carbon-neutral except for fossil fuel use. Substituting fossil fuels used in the lime kiln with renewable fuels produced at the mill, especially if existing side streams are used, would make normal kraft pulp mill operations nearly fossil fuel-free. Feasible options to integrate renewable lime kiln fuel production into the kraft pulp production process exist (Kuparinen and Vakkilainen 2017).

This study provides an assessment of the global potential of pulp and paper industry to act as site for negative CO2 emissions through biomass-based CO2 capture and storage (BECCS) and what could be the share of internally utilized CO2 (biomass-based CO2 capture and utilization, BECCU). To clarify the potential to capture CO2, an analysis of modern Nordic Softwood Kraft Pulp Mill (Kuparinen et al. 2017) and Southern Eucalyptus Kraft Pulp Mill potential with alternative sources captured and the effect to their energy production is shown and discussed. The possibility to utilize captured CO2 as raw material for further bioproducts is explored.

2 CO2 sources in kraft pulp mills

The operation of a modern Nordic Softwood Kraft Pulp Mill and a Southern Eucalyptus Kraft Pulp Mill is analyzed, to clarify the potential to capture CO2 and the effect to their energy balances is shown and discussed. The magnitude of the recovery process is often not fully appreciated. The global sulfate pulp production was 137 million tons (t) in 2016 (FAO 2017). Consequently, more than 1300 million tons of weak black liquor was processed in recovery boilers globally and 206 million tons of black liquor dry solids was combusted (Tran and Vakkilainen 2007). The global energy generation in recovery boilers was thus approximately 1.8 exajoules (EJ). Based on statistics (IEA 2018), this makes black liquor the fifth most important fuel in the world after coal, oil, natural gas, and gasoline. In the industrial sector, recovery boilers were responsible for about a quarter of the global biomass-based energy generation in 2011 (Vakkilainen et al. 2013).

Carbon dioxide capture (CC) from lime kiln flue gasses and subsequent use as calcium carbonate paper filler is a well-known and widely applied technology (Hirsch et al. 2013). It is technically possible to retrofit post-combustion CC to an existing pulp or pulp and board mill recovery boiler or biomass boiler (IEAGHG 2016). Carbon dioxide capture processes use heat and power, which affects the energy balance of the mill. The adequacy of steam and electricity needs to be estimated based on mill-specific details and the requirements of the chosen CC process. Estimation on the effects of CC process implementation can be made by analyzing example mill processes. For instance, when amine-based post-combustion CO2 capture process is used in stand-alone mills, added steam use can be covered without need for an additional boiler (Onarheim et al. 2017).

2.1 Sources of CO2

CO2 is formed in kraft pulp mills primarily during combustion, when carbon (C) in the fuel oxidizes. The primary reaction is

$$ \mathrm{C}+{\mathrm{O}}_2\to {\mathrm{CO}}_2. $$

The main CO2 sources are the recovery boiler, the biomass boiler, and the lime kiln. Non-condensable gas (NCG) destruction with several vents is also a CO2 source, but a negligible one. Of these, typically, the lime kiln is the only fossil CO2 source. A simplified process diagram of a kraft pulp mill showing the main CO2 sources is depicted in (Fig. 2).

Fig. 2
figure 2

Kraft pulp mill operations and alternative CO2-removal streams studied

2.2 Biomass boiler

Biomass residue is generated in the wood handling processes of the pulp mill, and, in addition to bark, the biomass residues contain other particles such as fines and wood lost during mill debarking. Almost all pulp mills burn this residue at site in the biomass boiler.

Biomass boiler uses fossil fuels during startup and shutdown. In many mills, additional auxiliary steam is generated with fossil fuels especially if the mill is an integrated mill. Integrated mill combines the pulp mill and the paper machine. For pulp mill, the fossil fuel usage produces at least 20 kilograms (kg) CO2 per air-dry pulp ton (ADt), but can be significantly larger.

2.3 Recovery boiler

Weak black liquor from brown stock washers after pulping is concentrated in multi-effect evaporator. Most of the water is removed, and concentrated black liquor, at 10–35% water content, is burned in a recovery boiler. The role of the recovery boiler is to burn organic residue from pulping and recover used sodium-based pulping chemicals in the black liquor. As concentrated black liquor is sprayed into the lower part of the recovery boiler, the parts of wood, not used for pulp, are burned. In the lower part of the furnace, an oxygen deficient environment is maintained so that sodium sulfide (Na2S) is preferably formed. The extent of sulfide formation over sulfate is measured by the reduction efficiency, typically over 90%. The rest of the sodium reacts to carbonate. The inorganic sodium and sulfur are recovered as a molten smelt, which consists mostly of Na2S and sodium carbonate (Na2CO3). The molten smelt enters a dissolving tank where it is dissolved in almost water-like weak white liquor to form green liquor. Carbon dioxide in the carbonate is thus from biogenic source (Kuparinen and Vakkilainen 2017). Biogenic CO2 from the recovery boiler exits from the stack of the recovery boiler with the flue gas. Typically fossil fuels are used during startup and shutdown. Occasionally due sudden and large process upsets or equipment failure fossil fuels, mostly oil and natural gas are burned. Fossil fuel usage produces 10–20 kg CO2/ADt. Biogenic CO2 produced is 1600–2400 kg CO2/ADt.

2.4 Lime kiln

The green liquor from the recovery boiler is sent to the causticizing plant, where it reacts with lime (CaO) to convert the Na2CO3 to sodium hydroxide (NaOH) following the reactions

$$ {\displaystyle \begin{array}{l}\mathrm{CaO}+{\mathrm{H}}_2\mathrm{O}\to \mathrm{Ca}{\left(\mathrm{OH}\right)}_2\\ {}{\mathrm{Na}}_2{\mathrm{CO}}_3+\mathrm{Ca}{\left(\mathrm{OH}\right)}_2\to 2\ \mathrm{NaOH}+{\mathrm{CaCO}}_3.\end{array}} $$

Conversion is measured by causticizing efficiency, typically 80 to 85%. Reaction product calcium carbonate (CaCO3) is regenerated to CaO in the lime kiln with heat from burning typically fossil fuel according to the reduction reaction:

$$ {\mathrm{CaCO}}_3+\left(\mathrm{heat}\right)\to \mathrm{CaO}+{\mathrm{CO}}_2. $$

The reduction reaction produces biogenic CO2 that exits with the flue gasses from the stack of the lime kiln. Typically, fossil fuels are used to reach the required temperature, at least 850 °C. Fossil fuel usage, mostly oil and natural gas, produces 100–250 kg CO2/ADt.

2.5 Biogas production

Liquid effluents from pulp mill are treated to high degree. Effluent flows contain small biomass particles (fiber sludge) that settle down. Separated material is called primary sludge. Very often the next step is biological treatment where remaining organics in the effluent are eaten by micro-organisms creating biosludge.

In some new mills, biosludge recovered is treated to biogas. Biogas production can be 10–15 kilowatt hours (kWh) per ADt (Metsä Group 2016). CO2 emissions from biogas production can be estimated growing, but of minor significance in relation to above-mentioned combustion processes.

2.6 Studied mills

The potential to capture CO2 within kraft pulp mill operations has been analyzed via case studies. The mass and energy balances of two reference mills were calculated and the most important CO2 sources were defined to estimate the CC potential and the effect of the implementation of the capture processes on the mill operations. The following reference mills were studied:

  • Mill A

    • A modern softwood kraft pulp mill located in Northern Europe

    • Annual pulp production 1,400,000 ADt

    • Residue from woodhandling process combusted in a power boiler

    • Integrated paper mill producing coated and uncoated paper

  • Mill B

    • A modern eucalyptus kraft pulp mill located in South America

    • Annual pulp production 1,500,000 ADt

The mills represent typical mills in their chosen location. Three hundred and fifty annual operating days was estimated for the both mills. The mill balances were calculated using an updated MillFlow program. The program includes detailed mass and energy balances and has been used to design pulp mills and to evaluate new process alternatives (Vakkilainen and Kivistö 2008; Hamaguchi et al. 2011). The Millflow balances include hundreds of calculations, which were introduced in more detail earlier (Hamaguchi et al. 2011). In the program, the pulping line is dimensioned based on the desired capacity of the mill. The wood demand is calculated based on the cooking yield and losses in the process stages, and the chemical demand is calculated from the digester balance. The program includes a black liquor calculation tool to define the inputs for the recovery boiler calculations, such as the dry solids flow, the composition, and the heating value of black liquor. The electricity generation is calculated from turbo generator balances after defining the steam flows from the recovery boiler and the biomass boiler. The electricity and heat usage in each department of the mill is used to define the steam balance. The lime kiln calculations require that inputs such as the type of make-up lime, the amount of residual lime, and the availability of burnt lime are defined. During this study, a carbon capture unit was added to calculate how carbon capture affects the balances of the reference mills.

Mill A is a large integrated pulp and paper mill located in Northern Europe. The recovery boiler and a separate biomass boiler produce steam for use in mill processes and for electricity generation in a steam turbine. The integrated paper mill is a notable steam and electricity consumer. Biomass boiler is fueled with woody residue from the wood handling process of the mill. The recovery boiler combusting black liquor and the biomass boiler produce biogenic CO2 due to biomass-based fuels. Natural gas is used as lime kiln fuel. A more detailed description of the Northern reference mill operations can be found in a previous work (Kuparinen et al. 2017).

Mill B is a South American stand-alone kraft pulp mill producing market pulp from eucalyptus (Eucalyptus globulus). Steam is generated in the recovery boiler that is able to cover the heat and electricity demand of the mill, and a separate biomass boiler is not used. Eucalyptus is typically debarked in the forest, and therefore the amount of on-site woody residue is relatively small compared with Northern mills. The lime kiln is fired with oil, which is typical when the mill is not located near the natural gas grid. Earlier studies introduced the operations of this reference mill in more detail (Kuparinen and Vakkilainen 2017; Hamaguchi et al. 2011).

Simplified block diagrams of Mill A and Mill B (Figs. 3 and 4) show the primary CO2 sources in the reference mills. The main process values of the reference mills are typical for new mills (Table 1). The biomass boiler in Mill A is assumed to combust all biomass residues generated, and the amount of CO2 is calculated accordingly. The figures represent a normal operation situation, and therefore, fossil fuels used during startups and shutdowns are not shown in the figures. The CO2 from fossil fuels used during startup and shutdown can be estimated at 10–20 kg CO2/ADt. The lime kiln produces both fossil, fuel-based CO2, and biogenic CO2 originating from the lime reburning reaction. In the reference mill cases, 64% of lime kiln CO2 is biogenic for Mill A, and 55% for Mill B.

Fig. 3
figure 3

Simplified block diagram of the operations of Mill A, a modern softwood kraft pulp mill located in Northern Europe. The values are given on hourly (h) or daily (d) basis. AD refers to air-dry, BD to bone-dry, DS to dry solids, and WL to white liquor

Fig. 4
figure 4

Simplified block diagram of the operations of Mill B, a modern eucalyptus kraft pulp mill located in South America. The values are given on hourly (h) or daily (d) basis. AD refers to air-dry, BD to bone-dry, DS to dry solids, and WL to white liquor

Table 1 The main process values and CO2 sources of the reference mills. The values are given on annual (a), daily (d), or hourly (h) basis. MW refers to megawatt

3 CO2 removal

As described above, the main CO2 emission sources in a kraft pulp mill arise from the recovery boiler, the biomass boiler (when present), and the lime kiln, from which the recovery boiler is the largest point source. CO2 removal is energy intensive and removal cost depends on removal method and process integration possibilities. Considering only carbon flows across the plant borders presented (Figs. 3 and 4), a simplified carbon balance and net CO2 emissions from the process (CO2,net) can be defined for the process as follows

$$ \mathrm{C}{\mathrm{O}}_{2,\mathrm{net}}=\left({\mathrm{C}}_{\mathrm{f}}+{\mathrm{C}}_{\mathrm{C}\mathrm{aCO}3}\right)\frac{{\mathrm{M}}_{\mathrm{C}\mathrm{O}2}}{{\mathrm{M}}_{\mathrm{C}}}-{\upeta}_{\mathrm{C}\mathrm{C}\mathrm{U}}{\upeta}_{\mathrm{C}\mathrm{C}}\mathrm{C}{\mathrm{O}}_{2,\mathrm{total}} $$

where ηCC is the share of CO2 removed from the total CO2 emissions (CO2,total) and depends on capture method and how it is applied. Most likely it is not feasible to apply CO2 removal for all possible CO2 streams, but rather to consider only the largest one(s). For example in Mill A and Mill B, the share of total emissions from the recovery boiler are 68% and 87%, respectively. If the efficiency of CO2 capture process is 90%, it follows that ηCC,A = 61% and ηCC,B = 78%. Depending on CO2 source and emissions of electricity production, in CO2 to fuel conversion emissions in CCU route may exceed the fossil emissions (Abanades et al. 2017). Net negative CO2 emissions can be reached only, if at least part of the captured CO2 will be permanently removed from the atmosphere. ηCCU gives the CO2 emission effect of selected CO2 utilization and storage route, where 100% means that all captured CO2 is permanently removed from the atmosphere, without additional emissions from the storage/utilization process. Cf and CCaCO3 are carbon flows into the plant in fossil fuel and limestone makeup streams. MCO2 and MC refer to molar masses of CO2 and C. For two studied Mill types where the capture process is applied only on recovery boiler, the net specific CO2 emission curves show substantial recovery potential for a single mill (Fig. 5). Specific emissions have large variation, depending on capture process efficiency and the CO2 emissions of the utilization route. When global potential for negative emissions is estimated roughly in Section 5, average specific emissions of − 1 t CO2/ADt is used for a general kraft pulp mill with CO2 capture and utilization.

Fig. 5
figure 5

Net CO2 emissions per produced dry ton of pulp from Mill A and Mill B for different capture efficiencies (80%, 90%, 100%), when CO2 capture is applied only on recovery boiler flue gasses. In this work, average specific emissions of − 1 t,CO2/ADt is used for a general kraft pulp mill with CO2 capture and utilization

3.1 CO2 removal methods

Different technologies based on pre-, post- or oxy-combustion processes can be utilized for CO2 capture from pulp mills. Leeson et al. (2017) recently presented techno-economic analysis and review of different CO2 removal methods applied to different industrial CO2 sources. Also, pulp and paper industries were touched and it was determined that not many detailed studies have been applied to pulp mills. It was also noticed that there is no single winning technology in terms of costs and that benchmarking is difficult due to inconsistent literature.

Amine-based post combustion CO2 capture systems are a proven technology that is commercially available. CO2 capture efficiency of monoethanolamine (MEA) process is usually between 80 and 90% and as a post combustion method, it can be applied easily to existing plants. Aqueous solution (30 percentage by weight) of MEA can be considered as a reference solvent in post combustion capture process. CO2 is absorbed at temperature 45–50 °C and flue gasses need to be cooled before amine absorption. Desorption occurs at 100–120 °C and approximately 3.7 megajoules (MJ) per kg,CO2 heat is needed for sorbent regeneration. In addition, some electricity is needed for the process, which increases own electricity use of the mill (Onarheim et al. 2015).

In recent study, Karjunen et al. (2017) studied the application of CO2 capture, transport, and intermediate storage logistics for Finnish energy system based on renewable energy sources. The cost of biogenic CO2 for utilization varied between 40 and 44 €/t,CO2 depending on applied future scenario. Costs were lowest for industrial scenario, where the largest amount of CO2 was captured from large industrial (mainly pulp and paper) point sources. In the calculations, conventional MEA capture process was taken as reference capture method. Application of more advanced capture methods could lead to lower capture costs.

Oxycombustion processes (see e.g., Stanger et al. 2015) applied to recovery boiler, bark boiler, or lime kiln are one option but require oxygen source and possibly modifications to the flue gas passages. In oxycombustion processes, reaction zones and gas atmosphere in the furnace will change, which may have implications on heat transfer and reactions that should be taken into account. Main additional cost is production of oxygen, which in case of kraft pulp mills can be quite affordable due to often preexisting equipment on site. In addition, precombustion processes based on black liquor gasification have been suggested for CO2 capture but these technologies have not yet been demonstrated successfully commercially (Onarheim et al. 2015).

Advanced hot solid looping technologies such as post-combustion calcium looping (CaL) (Martínez et al. 2016) offer also interesting possibilities for CO2 capture. In CaL, process calcium oxide is used for CO2 capture. In the case of kraft pulp mill, it has been proposed that lime mud from the lime kiln could be used as a sorbent for CO2 capture in pulp mills (Sun et al. 2013; Tynjälä et al. 2014). Even if lime mud as is would not be feasible choice for CO2 capture, there are other integration possibilities with CaL process and lime kiln, and also existing infrastructure for limestone acquisition and handling in a pulp mill, which could lead to further integration benefits. For CaL process integrated to lime kiln of a cement plant, Romano et al. (2013) estimated that the minimum cost of CO2 avoided could be as low as 27 €/t,CO2.

3.2 Effect of capture to energy use

CO2 capture processes are energy-intensive, and therefore, the effect of the process on the reference mill energy balances was estimated. MEA-based post-combustion process and capture from recovery boiler flue gas flow were chosen for the calculations. The consumption of low-pressure steam, cooling water, and electricity were estimated based on a previous study (Onarheim et al. 2015). The effect of capture process to energy use in reference mills is presented in Table 2.

Table 2 The effect of carbon capture process in the energy balances of reference mills, when MEA based post-combustion process is used to capture CO2 from recovery boiler flue gas

Due to integrated paper production, Mill A is a large energy consumer compared with a stand-alone pulp mill. Additional steam used in CO2 capture reduces electricity generation. If the energy use is limited to mill’s own production, availability of electricity sets the maximum limits for the capture process. Without additional electricity, 21% of CO2 in the recovery boiler flue gas flow can be captured without additional energy generation. This equals to 14% of the total CO2 of the mill. If carbon capture is used together with another process influencing the energy balance, such as lignin extraction, energy adequacy may become an issue.

Mill B is a stand-alone pulp mill where electricity is produced substantially in excess of own use. In this case, the limiting factor is the adequacy of steam, when steam production is limited to the recovery boiler and no additional boiler exists. The capture process consumes low-pressure steam. Based on the steam balance calculations, the maximum capture rate from recovery boiler flue gas flow is 32%, which equals to a capture rate of 28% of the total CO2 emissions of the mill. The mill steam consumption increases then by 22%. Electricity consumption increases by 12% and production decreases by 10%.

4 CO2 utilization in kraft pulp mills

The possibility to utilize captured CO2 as raw material for further bioproducts is explored. The possibilities depend on mill-specific details, such as the chosen processes and the type of wood raw material. The studied alternatives for on-site utilization of CO2 are typically occurring large streams; tall oil manufacturing, lignin extraction, and production of precipitated calcium carbonate (PCC). Tall oil manufacturing can be considered as an option in softwood mills, but in hardwood and eucalyptus mills tall oil recovery is rarely done due to low levels of extractives (Shackford 2003). Lignin extraction can be integrated in both hardwood and softwood mills. There are several uses for the separated lignin; formaldehyde resins, carbon fibers, moisture barriers in packaging materials and upgraded fuel (Tomani 2013). In the case of an integrated pulp and paper mill, CO2 can be used in PCC production (Teir et al. 2005).

4.1 Tall oil manufacture

After pulping, weak black liquor contains fatty and rosin acid extractives as foamy material called soap. Especially, coniferous trees have high extractive content. Soap in black liquor is separated and skimmed from feed and intermediate liquor tanks in the evaporation plant. Raw soap is converted to crude tall oil (CTO) by acidulation in the tall oil plant. Tall oil production varies and can be estimated as 45 kg/ADt for Nordic pine (Pinus sylvestris), 25 kg/ADt for Nordic spruce (Picea abies) and less than 20 kg/ADt for Nordic birch (Betula pendula, Betulapubescens) (Gullichsen and Lindeberg 2000). Acidulation is typically done using sulfuric acid. Acid use is 200–300 kg of sulfuric acid per ton of crude tall oil. Sometimes rest acid from chlorine dioxide (ClO2) plant can be partially used. Part of the acid can be replaced by the use of CO2. Because CO2 is weaker acid only about 50% of acid use can be replaced. CO2 use corresponds to 4–6 kg/ADt.

Due to the environmental footprint associated with the use of fossil fuels, it is of great economic importance to produce fuels from other sources. Tall oil can be converted to a renewable fuel at a low cost and offers competitive advantage against alternative biomaterials, such as vegetable oil (Aro and Fatehi 2017).

4.2 PCC production

In integrated mills, part of the coating materials for paper production can be produced by blowing, e.g., lime kiln flue gas through slurry of calcium hydroxide solution. Produced calcium carbonate is then used to whiten and smoothen the paper surface (Nanri et al. 2008).

Typically, lime kiln flue gasses are bubbled through green liquor. The amount of calcium carbonate produced is typically fixed to correspond the local demand. A possible production level could be 33 kgCaCO3/ADt corresponding to CO2 use of 20 kg/ADt.

4.3 Lignin separation

Major wood components are cellulose 40–50%, hemicellulose 23–32%, and lignin 15–30%. About half of the original wood, most of the cellulose and some hemicelluloses is converted to kraft pulp and the rest of the organics in wood are led through evaporation plant to energy production in recovery boiler.

The separation of lignin from residual black liquor is an option that is considered by the pulp mills for several reasons. Firstly, the heat transfer capacity of the recovery boiler is often a bottleneck that limits pulp production. Removing part of the lignin from the black liquor decreases the heat load on the recovery boiler and more pulp can be produced. The separated lignin could be sold or used to replace, e.g., fuel oil or natural gas in the lime kilns or be combusted in a power boiler if the energy is required. Secondly, the modern pulp mills have energy surplus and this energy surplus can be exported to other users in the form of biofuel. Thirdly, separated lignin can be used as a raw material in chemicals (Hamaguchi et al. 2013).

Typically, lignin is separated by acidifying part of the black liquor. Sulfuric acid is used for acidification. The use is 50–100 kg per ton of separated lignin. In many commercial processes, part of the acidification is done by CO2. The CO2 use is then 150–250 kg per ton of separated lignin. If lignin separation degree is 20% and the wood pulped is pine, then the CO2 use is about 35 kg/ADt.

4.4 CO2 utilization processes in the reference mills

Compared with carbon capture potential, the utilization possibilities are currently small. Considering the CO2 requirement of the above-mentioned utilization processes, required carbon capture rates at the reference mills vary from 0.2 to 21.6% depending on the chosen process/processes and CO2 source (Table 3). Tall oil production was considered only for Mill A, because in eucalyptus mills tall oil recovery is rarely done due to pulp properties. PCC production was also considered for Mill A due to integrated paper production. Lignin separation rate was chosen at 20% for both mills.

Table 3 Required CO2 capture rates to cover for selected CO2 utilization processes in reference mills A and B. Capture rates calculated for the flue gasses from the recovery boiler (RB), biomass boiler (BB), and lime kiln (LK)

The main process flows of Mills A and B with integrated CCU processes are presented in Figs. 6 and 7. For Mill A, all the three possible options are shown, although implementation of each of them would require generation or purchase of additional electricity. This results from increased electricity consumption due to new processes and decrease in steam generation in the recovery boiler due to lignin extraction. Capture from recovery boiler flue gas was chosen except for PCC production, where lime kiln flue gas is used.

Fig. 6
figure 6

The main process flows for Mill A when the studied CCU processes are implemented

Fig. 7
figure 7

The main process flows for Mill B when CO2 from the recovery boiler is utilized for lignin separation

5 Global potential

This study provides an assessment of the global potential of pulp and paper industry to act as site for negative CO2 emissions. Estimates are given based on recent production data (FAO 2017). The development trend of the global chemical wood pulp production from the year 1961 to 2016 shows almost constant growth (Fig. 8).

Fig. 8
figure 8

World wood chemical pulp production, data from FAO 2017

The estimated CO2 production of the 15 largest unbleached and bleached sulfate pulp producer countries based on production in the year 2016 is more than 300 megatons (Mt) (Fig. 9). These countries produced 93% of the global sulfate pulp production and therefore, substantial CCU potential can be expected.

Fig. 9
figure 9

CO2 production, including both biogenic and fossil-based CO2, of the largest sulfate pulp producer countries in the year 2016. Estimation based on pulp production data (FAO 2017)

The global technical potential to capture CO2 from kraft pulp mill recovery boilers, lime kilns, and biomass boilers was estimated based on chemical pulp production data from the year 2016 (FAO 2017). The estimates were made for bleached and unbleached sulfate pulp, and were about 100 and 35 MtCO2/a respectively (Table 4). Technical potential to utilize CO2 in the mill processes using above-mentioned technologies was estimated about 12 and 4 MtCO2/a respectively (Table 4).

Table 4 Global technical potential to capture CO2 from recovery boilers (RB), biomass boilers (BB), and lime kilns (LK) and on-site utilization potential, estimations based on sulfate pulp production data from the year 2016 (FAO 2017)

Technical potential to capture CO2 from pulp mills is substantial. With rather conventional assumptions presented above, total amount of about 135 MtCO2/a could be removed from the atmosphere from existing pulp mills, without additional biomass harvesting at price levels well below 50 €/t,CO2. Pulp mills alone are not answer to high negative emission targets but they can be one significant component in the palette. With currently available technologies, only a small part of produced CO2 can be utilized on-site. The potential for both capture and utilization can be estimated to increase along with technology development as well as the steady increase of pulp production capacity with new mills. Commercial potential of CO2 utilization routes was not estimated in this study.

In recent mitigation strategies for climate change, BECCS has been presented as one of the key technologies, as it offers a way to negative CO2 emissions (Fridahl and Lehtveer 2018; IPCC 2018). The global annual BECCS potential has been estimated at or below 5 gigatons (Gt) CO2 (de Coninck et al. 2018). Based on the estimation above, capture from chemical pulp industry can cover at least 3% of the global potential. Technology is not yet mature, but it is tested and used in small scale. The deployment of BECCS/CCU in the pulp industry does not affect the wood use of the mills, and therefore has no effect on forest or land use when applied to existing mills. Sociopolitical issues are the primary constraints on the way to BECCS and its large-scale use (Fridahl and Lehtveer 2018).

In addition to the investment and operational costs, the economic feasibility of BECCS/CCU is greatly dependent on the avoided CO2 costs, primarily taxes and emissions credit collected on fossil-based emissions. It should be noted that as currently, CO2 in chemicals is counted at production source; therefore, use of biogenic CO2 replacing fossil CO2 would give the mill no credits. Therefore, apart from development of carbon utilization technologies, the future of BECCS/CCU depends on political decisions. Incentives for negative emissions would be a probable way to encourage producers to adopt these processes. Utilization of biogenic CO2 in the processes of an emission producer is a novel concept, and thus unknown as a legislative issue.

6 Conclusions

This study evaluated the possibilities of CO2 capture and on-site utilization in pulp mills. Bioenergy with carbon capture and storage or utilization has been recognized as one of the key technologies in recent strategies on climate change mitigation. In kraft pulp mills, three main CO2 sources can be identified as the recovery boiler, the lime kiln, and in most mills, the biomass boiler. Large part of CO2 formed in the pulping process is biogenic, and the primary source of fossil-based CO2 is the lime kiln. Therefore, carbon capture offers pulp mills the possibility to act as site for negative CO2 emissions, if biogenic CO2 is permanently removed from the atmosphere by utilizing it as raw material for further bioproducts. The technical potential for carbon capture in pulp mills is notable, and it can be estimated to cover 3% of the global capture potential from bioenergy. Considering currently available technologies, the utilization possibilities in pulp mills are minor compared with the capture potential. Therefore, the possibilities for climate change mitigation using carbon capture in the chemical pulp industry center on carbon storage, and utilization possibilities require more research to become a notable option. The cost-effectiveness of BECCS/CCU is primarily dependent on the avoidance of cost of fossil CO2 emissions. In the future, the feasibility will depend both on technology development on CO2 utilization possibilities, and on political decision-making regarding emission taxes and possible incentives encouraging CO2-negative solutions.