biorefinería forestal y su aplicación en la industria de pulpa y papel

8/10/2019 Biorefinera Forestal y Su Aplicacin en La Industria de Pulpa y Papel

1/10

The forest biore nery and its implementation in the pulpand paper industry: Energy overview

Maryam Moshkelani * , Mariya Marinova, Michel Perrier, Jean ParisDepartment of Chemical Engineering, cole Polytechnique de Montral, C.P.6079, Succ. Centre-ville Montral (Quebec), Canada H3C3A7

a r t i c l e i n f o

Article history:Received 1 June 2011Accepted 20 December 2011Available online 11 January 2012

Keywords:Integrated forest biore neryEnergy ef ciencyPulp and paper industryProgressive implementationGreen integration

a b s t r a c t

Incorporating a biore nery unit to an operating Kraft pulping process has signi cant technological,economic and social advantages over the construction of a grassroot biore nery. Also, the conversion of a Kraft mill from total pulp making to complete biore nery can be done in a stepwise fashion and so givea company that envisages such transformation the opportunity to master the new technologies, evaluateoptions and develop an appropriate business plan. In all cases however, the road to conversion presentsserious challenges. As components of the wood such as lignin or hemicelluloses are withdrawn from theKraft pulp line, the heat production capacity from the recovery boiler where they are currently burnt isdiminished. At the same time the operation of the added biore nery unit increases the steam demand. Inorder to avoid fossil fuel dependency, the total site must be highly integrated and optimized. Theapplication of an intensive and innovative energy optimization methodology to actual case studies hasshown that the green, low GHG emissions biore nery is feasible. The economics can be attractive fora site combining specialty wood pulp and bio-product, biomass gasi cation, power cogeneration andheat upgrading by optimally positioned and designed absorption heat cycles. The methodology has beenapplied to biore ning technologies for lignin and hemicelluloses extraction and valorisation, bothtechnologies being coupled with gasi cation of wood residue.

2012 Elsevier Ltd. All rights reserved.

1. Introduction

Biore ning has been de ned by the International Energy Agency(Biore nery, task 42) as the sustainable processing of biomass intoa spectrum of marketable products and energy [1]. The potential of implementing any biore nery is assessed in the context of availablefeedstock, applicable technological processes and market demand.Lignocellulosic crops or residues of forestry sector are attractivefeedstocks for biore neries specially when integrated into a pulpand paper mill because it does not compete with agricultural cropsfor fertile land and relies on larger biomass yields [2] . The forestbiore nery has received much attention from the pulp and papersector in industrially mature countries primarily in North Americaand Western Europe as a potential way to diversify its product mixand generate new revenues. The industry has been in a precariouseconomic situation for some time because large and modernproducing facilities established in countries with abundant fast

growing resources, and low manufacturing costs have createda competitive environment. This has driven traditionalmanufacturing countries like Canada to take a fresh look at theirrenewable resources and seek alternatives to convert intosustainedand pro table businesses [3] .

The Integrated forest biore nery (IFBR) consists of implement-ing biore nery units into existing pulping mill called receptor Kraft.TheKraft process is a receptor process of choice. It entails treatmentof wood chips with a mixture of sodium hydroxide and sodiumsul de (the white liquor), to convert wood into pulp and steam [4].A simpli ed schematic of the Kraft process is shown in Fig. 1. Woodchips are cooked in a digester where lignin and hemicelluloses aredegraded into fragments and dissolved in the strongly basicdeligni cation liquor. The discharge from the deligni cation stageconsists of cellulose ber in suspension in residual digestion liquor.The bers are cleaned and separated from liquor in a series of washers and bleached to remove the residual traces of lignin andother impurities. Bleached pulp is then dried with steam and hotair. To recover the active cooking agents, the residual black liquor isconcentrated in evaporators and burned in a recovery boiler togenerate process steam and yield an inorganic smelt. The smelt isdissolved, recausti ed by live lime produced onsiteand returned tothe digester as white liquor.

* Corresponding author. KSH Solutions Inc., 1 Place Alexis Nihon, Tour Xerox,3400 de Maisonneuve O., Bureau 1600, Montral, Qubec H3Z 3B8. Tel.: 1 514 9324611x5884; fax: 1 514 932 9700.

E-mail address: [email protected] (M. Moshkelani).

Contents lists available at SciVerse ScienceDirect

Applied Thermal Engineering

j o u rn a l h o mep ag e : www.e l sev i e r. co m/ l o ca t e / ap t h e rmen g

1359-4311/$ e see front matter 2012 Elsevier Ltd. All rights reserved.

doi: 10.1016/j.applthermaleng.2011.12.038

Applied Thermal Engineering 50 (2013) 1427 e 1436
mailto:[email protected]://www.sciencedirect.com/science/journal/13594311http://www.elsevier.com/locate/apthermenghttp://dx.doi.org/10.1016/j.applthermaleng.2011.12.038http://dx.doi.org/10.1016/j.applthermaleng.2011.12.038http://dx.doi.org/10.1016/j.applthermaleng.2011.12.038http://dx.doi.org/10.1016/j.applthermaleng.2011.12.038http://dx.doi.org/10.1016/j.applthermaleng.2011.12.038http://dx.doi.org/10.1016/j.applthermaleng.2011.12.038http://www.elsevier.com/locate/apthermenghttp://www.sciencedirect.com/science/journal/13594311http://crossmark.dyndns.org/dialog/?doi=10.1016/j.applthermaleng.2011.12.038&domain=pdfmailto:[email protected]


2/10


3/10

consumption. Modi ed Norden ef ciency factor and equivalentdisplacement ratiohave been computedand compared with typicaloperation values for 5 washers in the mill. It was found thatreplacing the three vacuum drum washers with a wash press,preheating bleaching agents and reutilizing ef uents from papermachine in washers not only saves water and energy but alsoresults in discharging a cleaner pulp for bleaching. Fig. 3 illustratesthe analysis of washing section and potential of energy and water

savings are presented in Table 1 .

2.1.1.2. Evaporators train. Evaporators are important steamconsumers in the mill, 12.5 (t/hr), and they concentrate blackliquor to be burnt in the recovery boiler. Studying evaporationsection showed that preheating the black liquor entering themulti effect evaporator train will be concentrated and hot blackliquor exiting the train will increase the economy. Moreover

recompressing the steam used for evaporation increases thepotential of live steam saving. The analysis and benchmarking of evaporation train is presented in Fig. 4 and Table 2 shows theenergy saving potential.

2.1.1.3. Boiler area. Steam is produced in boiler area. Boiler inef -ciency lowers the potential of steam quality and production. Thereference mill has one recovery boiler and four power boilers. They

were analysed and potential steam savings recognized. Resultsshow that reducing heat loss from the recovery boiler results inincreasing the steam production capacity and ashing the blowdown to preheat the boiler makeup water leads to steam saving.The results of analysis and energy improvement are presented inFig. 5 and Table 3 .

2.1.2. System performance analysis (SPA)To evaluate the system energy ef ciency, the global KPIs of the

process such as steam production and utilization, waterconsumption and ef uent production are identi ed and computedbefore developing energy enhancement measures. Then they arecompared with a wide number of mills and best current practice of the industry to assess inef ciencies [10] . There are tools and tech-

niques which lead to targeting the energy and water for the processand better understanding the constraints levels in the mills.Thermal pinch is the process integration technique to targetminimum heating and cooling requirements of the process andextent of internal heat recovery. Water pinch targets the potentialof water and ef uent reutilization in the process. Combinedthermal and consistency pro le of pulp depicts dilution and non

Fig. 2. Stepwise intensive energy optimization approach.

Fig. 3. Washing section analysis of the reference mill.

Table 1Steam and water saving potential in washing section.

Water saving (m 3/adt) 3.1Mill water reduction% 3.4Steam saving (GJ/adt) 0.64Mill steam saving% 1.8

M. Moshkelani et al. / Applied Thermal Engineering 50 (2013) 1427 e 1436 1429


4/10

isothermal mixing points along the pulp line. There are severalcomposite curves that represent the different aspects of the watersystem in the mill. The composite curves for process water, waterheat exchanger network, and water tanks, analyse the energyinef ciencies in the water system [11] . Constraint analysisis the keyaspect of SPA by distinguishing between the different levels of energy saving projects with their incorporated economic aspects; itgives the mill the opportunity to choose the extent of the energysaving projects (retro t or grassroot) with respect to the invest-ment cost. The results forapplying constraint analysisto an existingKraft mill are presented in Table 4 .

2.1.3. System interaction analysis (SIA)The energy ef ciency of the Kraft process is strongly related to

the proper management of water and steam which must take intoaccount their strong interactions. The combined water and energyoptimization approach proposes the fresh water reduction pathwith the highest energy saving response from the point of demandback to the source. For the reference mill six water reductionprojects are recognized and presented in Table 5 . Ef uents aremostly reutilized in these projects to reduce fresh waterconsumption without necessity of a heat exchanger.

Applying the intensive energy optimization approach for thereference mill saves 21 e 34% of total steam consumption (highersaving by means of higher investments e.g. compressor) and 27% of mill fresh water consumption. Several techniques are applied onthe utility or process side to maximize the energy performance andaddress the synergetic or counter action effects of different projects[12] . The SIA maximizes the potential for steam and water savings,for heat upgrading by means of absorption heat pumps and, forheat and power production by co- and tri-generation within themill ( Fig. 6). Upgrading the low energy level of some hot streams inthe process using a heat pump can increase the steam saving andpower production. It is reported by Marinova et al. that imple-mentation of a tri-generation unit consisting of a back pressuresteam turbine and absorption heat pump could reduce the coolingdemand of the process by 17% and increase the steam productionby 30% while 2.2 MW of electrical power is produced [13] .

2.2. Selected biore nery options for Kraft process

Lignocellulosic biomass has three major components: cellulose,hemicellulose and lignin. Cellulose is a complex carbohydrate,(C6H10O5)n, that is composed of glucose units and forms the mainconstituent of the cell wall of vascular plants. It is the majorcomponent of many manufactured products such as paper,specialty products e.g. nanocrystalline cellulose, viscose and rayonas well as paperboard, packaging and building materials. Hemi-cellulose (C 5H8O5)n has a random, amorphous structure with littlestrength to hydrolysis or heat and contains a mix of C6 and C5sugars which can be converted into value-added products. LigninC9H10O2(OCH3)n, a phenolic polymer, is a complex chemicalcompound; it is an integral part of the secondary cell walls of plants which can be chemically extracted from residual pulpingliquors by acid precipitation. Wood also contains a large number of

other organic components in small quantities that can be trans-formed into high value special products (pharmaceutical or foodadditives). Typical compositions of wood biomass are given inTable 6 .

In the Kraft pulping process only 42 e 44% of woody biomass isconverted into pulp and the rest (mainly lignin and hemicelluloses)is combusted in the recovery boiler. This portion can be betterutilized to increase the revenue margin of the mills, by beingconverted into higher marketable products such as biofuels, syn-tethic gas, chemicals, heat and power through various technolog-ical paths. This possibility along with the vicinity to sources of biomass and accessible existing infrastructures make Kraft millsexcellent candidates as biore nery receptors. The biore nery basedon Kraft process is composed of two sides e upstream and down-

stream ( Fig. 7). The upstream side, which is the Kraft process itself,is well de ned in terms of technology, energy and materialrequirements, water utilization and products. However, the de -nition of the downstream side is a challenge and it is essential toappropriately assess the feedstock, product options, pathways, andenergy and material requirements.

5

5.2

5.4

5.6

5.8

6

6.2

6.4

6.6

Economy Consumed thermal energy

Reference Mill

Average Canadian

Economy (t/t): evaporated water per used steamConsumed thermal energy (GJ/adt): steam consumption per produced pulp

Fig. 4. Evaporation section analysis of the reference mill.

Table 2Energy saving potential in evaporators.

Potential of improvement Economy Steam saving %

Black liquor preheating 6.2 0.5Steam recompression 5.9 8.2

0

10

20

30

40

50

60

70

80

90

RB PB1 PB2 PB3 PB4

Referrence mill Mediane Canadian Best practice

RB: Recovery boiler PB: Power boiler

Fig. 5. Steam production analysis of the reference mill, boiler ef ciency.

Table 3Energy saving potential in boiler area.

Potential of improvement Increase in steamproduction capacity %

Steamsaving %

RB maintenance improvement 6.4 eBlow down heat recovery e 3.1



5/10

The biore nery options selected for integration into Kraftprocess are [15] :

Hemicelluloses extraction from wood chips prior to pulpingand their conversion into polymers, fuels and chemicals. In thisstudy particular attention is paid to two product options:ethanol as a biofuel, a high volume but a low pro t product andfurfural as an intermediate feedstock for further synthesiswhich is a small volume product but high in pro t.

Extraction of lignin from black liquor by precipitation followedby washing and drying. Lignin can be further transformed intovaluable chemicals such as phenol, road additives, and surfaceactive dispersants or even carbon bers;

Gasi cation of wood residues to produce synthetic gas asa source of heat, power, fuels or chemicals.

The technological paths for selective transformation are ther-mochemical, biochemical, or chemical. The hydrolysis of hemi-celluloses and acid precipitation of lignin fall in chemical processpathway. Fermenting sugar constituents of hemicelluloses toproduce ethanol requires biochemical process at close to ambienttemperature. On the other hand gasi ying biomass is a thermo-chemical conversion.

2.2.1. Hemicelluloses extractionThe extraction of hemicelluloses from wood chips prior to

pulping and their conversion into value-added products is a keybiore ning technology. The ef ciency of the technology stronglydepends on the pre-treatment operation, the challenge being toextract a signi cant amount of hemicelluloses without a negativeimpact on pulp quality and quantity [16,17] . Mao and et al. haveproposed the near-neutral extraction process integrated within anexisting hardwood Kraft mill [18] . The near-neutral process usesgreen liquor, composed primarily of Na 2CO3 and Na 2S, in the wood

extraction stage. In the study conducted by Mao and co-authors,a portion of the hemicelluloses is extracted from wood prior topulping and converted into acetic acid and ethanol while using theextracted wood chips for pulp production. The biore nery istreated as an adjunct to the base Kraft process, which maintainsthe pulp production. The implementation of the near-neutral

process modi es the energy balance of the Kraft pulp mill.Approximately 10% of the wood, mainly hemicelluloses and lignin,are extracted during chips pre-treatment. Nevertheless, the calo-ri c value of the hemicelluloses is low (about 13 MJ/kg) comparedto that of lignin (25 MJ/kg) and the impact on the black liquorcombustibility is less than in the case of lignin extraction.However, the transformation of the hemicelluloses sugars intovalue added products requires energy intensive operations.

Ethanol and furfural are two attractive product options; theirproduction paths are shown in Figs. 8 and 9 . The potential worldmarket for ethanol is 65 billion L/a with a price ranging from 0.7 to0.9 $/L. It is mostly used as biofuel requiring high processing and

capital cost due to the complexity and ef ciency of the process. Onthe contrary, furfural has smaller global market of 250,000 t/a, buthigh market price of 1000 $/t. It is used mostly as extractive solvent,adhesive, bleaching agent and feedstock for other products.

The incorporation of the hemicellulose extraction stage prior toKraft pulping and its subsequent conversion affects the energybalance of the mill. Marinova et al. have shown that the imple-mentation of the near-neutral process into a typical CanadianKraft pulp mill increases the base case steam demand by 15.5%. Anapproach for energy optimization is proposed to face the energyshortage of the modi ed process. A combination of severalmeasures reduces the steam demand of the Kraft process andsatis es the increased energy requirement of the biore nery.Energy optimization should be an integral part of any attempt to

successfully convert a conventional Kraft pulp mill into a bio-re nery [15] .The hemicelluloses biore nery requires new operations, some

of them non typical for the pulp and paper industry and implieshigh investment costs. The concept of the biore nery cluster is an

Table 4Energy saving project types and constraints.

Level of modi cation Steam saving %

Minor Adjustments (Retro t-Low) Direct and indirect steam heat exchangers

11

Major adjustments (Retro t-High) Direct and indirect steam heat exchangers Pinch violations

Non isothermal mixing points

16

Restructuring existing network (Grassroot) Direct and indirect steam heat exchangers Pinch violations Non isothermal mixing points Restructuring water network

17

Table 5Combined water and energy saving projects.

Type of project Watersaving %

Steamsaving %

Replacing grinder fresh water withpaper machine ef uent

16.4 0

Replacing bleaching fresh waterwith paper machine ef uent

2.3 2.7

Reducing vacuum pump fresh waterby ltering and reutilizing the ef uents

0.7 0

Reutilizing vacuum pump ef uentin paper machine

1.1 0

Reutilizing bleaching ef uent inrecausti cation

1.6 3.1

Reducing washing fresh water byreutilizing washer ef uent

1.5 2.9

Total 23.6 8.7

Fig. 6. System interaction analysis.

Table 6Typical components of wood (%) [14] .

Component Softwood Hardwood

Cellulose 40 e 50 40 e 50Hemicelluloses 15 e 20 20 e 35Lignin 23 e 33 16 e 25Other organics 1 e 5 1e 2Inorganic as ash 0.2 e 0.5 0.2 e 0.5



6/10

opportunity to address this major economic concern. Several pulpmills could be involved in the initiative, offering to the participantsa mutually bene cial venture by sharing investment and operatingcosts. Each of the pulp mills will supply feedsock, e.g. concentratedpre-hydrolysate; and one of them serves as the centre of the clusterwhere the hemicelluloses transformation is carried out. A simpli-

ed representation of a biore nery cluster is illustrated in Fig. 10.Several parameters should be optimized in order to establish

a pro table biore nery cluster based on hemicelluloses extractionand transformation; those parameters are: concentration of thepre-hydrolysate, distance between the mills, transportation costs,energy and material use. The participants in the initiative shouldagree to collaborate and share the required investments costs as

well as the pro ts. Then the cluster concept could be a pro tableoption for the pulp and paper industry.

2.2.2. Lignin extractionThe advantage of extracting lignin from black liquor is to reduce

the load on the recovery boiler which is the bottleneck for pulpproduction. It also increases pro t margin by generating energy orvalue-added products such as carbon bers, phenol, road additives,surface active agent and dispersants in secondary processes. Lignin

extraction is possible through acid precipitation, electrolysis andultra ltration. Acid precipitation is the technique which hasreached the most advanced state of development and imple-mentation [19] and is presented in Fig. 11. Black liquor at 30%dissolved solids concentration is withdrawn from the evaporatortrain and precipitated in acidic condition. The acidi cation agentused to lower the pH for precipitation is CO 2. After ltering, thelignin cake is washed in acidic conditions (sulfuric acid, pH 4) andwash ltrates are returned to the evaporation section of the Kraftprocess [20] . Integration of lignin extraction units into Kraft processincreases the opportunity of water and chemicals saving. Filtratefrom pulp drying can be used for lignin washing. Recovering CO 2from the stack gases of mill boilers or lime kiln creates CO 2 sinkswhich results in GHG emission reduction. Sulfuric acid for washingmay be available onsite from the ClO 2 making plant (ClO 2 isproduced onsite and used as a bleaching agent).

However, such integration has evident impact on energydemand of the global site ( Fig. 12). Extracting lignin from blackliquor decreases the steam production capacity of the referencemill recovery boiler. At equal extraction rate, the energy impact of lignin extraction on the recovery boiler will be signi cantly largerthan in the hemicelluloses case because of its higher speci c heatcontent. Moreover reutilizing biore nery weak ltrate in the Kraftevaporation section increases the demand for live steam. Theenergy implication of biore nery units is mostly to heat upchemicals and water and adds to the energy demand of the inte-grated site. The evaporation section generally accounts for almost92% of increase in steam demand. This de cit in steam is partiallycompensated by increasing the feed rate of chips to Kraft process. Itis reported by Perin-Levasseur et al. that a 10% increase in pulpproduction results in 20% increase in total steam demand [21] .Since the recovery boiler capacity is the limiting factor inincreasing the production, optimizing the energy ef ciency of theintegrated site is the ultimate solution to address its energyrequirement.

2.2.3. Biomass gasi cationThe Kraft process consumes large quantities of energy, 26% of

the total energy used by the Canadian industry sector, which isgenerated from several types of fuels (black liquor, wood residuesor fossil). Expensive fossil fuel is consumed in lime kiln and powerboilers to satisfy the energy demand of the process while contrib-uting to CO 2 emissions to the higher atmosphere. Biomass, which isgenerally combusted for steam production, can be used more ef -ciently in poly-generation pathways to generate high value

Fig. 7. Upstream and downstream sides of a biore nery based on the Kraft process.

Fig. 8. Pathway for ethanol production from wood chips.



7/10


8/10

Fig. 14 shows the integrated green biore nery into a Kraft millreceptor. The bio-products are ethanol, furfural or lignin whereasenergy demand (steam and power) is provided by biomass gasi -cation. The produced syngas is utilized in combined heat andpower cyclesto generategreenpowerand satisfy thesteamdemandof the mill. Simultaneously it can re the lime kiln to eliminate thefossil fuel consumption and reduce CO 2 emission. Intensive energyoptimization is applied to improve the energy ef ciency of indi-vidual receptor Kraft, biore nery units and global integrated site.

4. Strategy for progressive implementation of GIFBR

The forestry sectors in industrially mature countries must revisetheir traditional business models to develop new sources of reve-nues in order to regain pro tability and remain competitive inglobal market. In order to manage the risk that is associated withsuch conversion, progressive implementation is proposed in thispaper. The advantage of this approach is to permit the mill to havethe pulp line in production in order to keep its revenue throughoutthe transformation period. It also increases the chance forcombining different technology pathways, and diversi es theproduct mix. Decision making to choose among various pathways,products and conversion policies is selective and uniquely tailoredfor every individual Kraft mill considering its constraints, availablesources, and business plan. For instance, as a converted mill,

maintaining the Kraft production line may be a necessity when thebio-product is a low price commodity such as biofuel [25] , but inhigh value specialty production scenarios, total conversion to bio-re nery might be more advantageous. Consequently there could beKraft mills partially be converted into biore neries while keepingthe pulp line in operation, mills completely converted into bio-re neries, or others that choose to produce value added pulp andpaper derivatives such as:

Bio-sensitive papers, intelligent papers Composite packaging materials, construction materials Rayon from dissolving pulp

However, irrespective of the conversion path selected by the

mill, optimizing the energy demand of the receptor Kraft mill is therst and critical step of the conversion process. An intensive energyoptimization methodology, such as the one presented in this paper,provides a road map for the mill to save energy and water withindifferent investment levels. Then the liberated energy productioncapacity can be made available to support the demand of the otherrevenue generating initiatives such as: biore nery, tri-generation,steam sale, and power generation. The next step is to select thebiore nery technology, identify the energy implications and opti-mize its energy ef ciency. Integrating a biore nery unit intoa receptor Kraft mill creates interactions within the overall site.Therefore intensive energy and material integration is highly rec-ommended. Implementing gasi cation units completes theconcept of green integrated site by eliminating fossil fuel

consumption and increases the possibility to upgrade the steamproduction rate for cogeneration. Fig. 15 presents the strategy forprogressive implementation of GIFBR.

Nevertheless, the implementation strategy raises a number of unusual challenges such as:

Making appropriate choices among various production path-ways and mastering new technologies

Managing the implementation for manufacturing high value-added products but limited in tonnage to avoid over-saturation of the market

Achieving the integration of downstream processing chainwith the chemical and petro-chemical industries

Ensuring the durability of new operations within a context of sustainable development

Fig. 11. Lignin extraction from Kraft black liquor.

Fig. 12. Energy impact of different lignin extraction rate on total site (reference

mill

biore nery).



9/10

Pulp line

Recovery loop

Hemicellulose or

lignin biorefinery

units

Biomass

gasification units

By-products

Heat

Water

Wood

chips

Water

Bio-products

Pulp

Co-generation unitsWood

waste

Syngas

Syngas Steam & electricity

Steam &

electricity

Sludge &

Treated effluent

Fig. 14. Green integrated forest biore nery concept (GIFBR).

Fig. 13. Gasi cation biore nery units with CHP.

Development of integration platforms1- Definitio and intensive nergy optimization of the receptor mill2- Development of biorefinery configurations and identifying their energy requirements3- Selection of the most appropriate biorefinning technology with optimized energy consumption

Developement & analysis of integrated forest biorefinery1- Integration of Kraft and biorefinery platforms2- Intensive energy and material integration3- Applying enviromental analysis to evaluate the fossil fuel depencancy and GHG emissions

Implementation of green integrated forest biorefinery1- Development and integration of biomass gasification units to mitigate the inviromental impacts2-Econonic analysis and project prioritization3- Progress implemenation

Fig. 15. GIFBR progressive implementation.



10/10

5. Conclusions

The pulp and paper sector of mature industrial countries havethe potential to transform into more diversi ed and pro tablebusinesses. Developing a single road map for the entire industry isnot a desirable since there are various possible products withdifferent market demand and value. The transformation pathways,product mix, suitable conversion technologies, market uncertaintyevaluations, and sustainable development are challenges to betackled. Successful conversion will require progressive imple-mentation of new business plans to give companies the opportu-nity to master the new technologies, minimize the risks andincrease pro tability. The sustainability of the conversion willdepend upon the successful implementation of intensive energyintegration and optimization measures.

Acknowledgements

This work was supported by a grant from the R&D cooperativeprogram of the Natural Science and Engineering Research Councilof Canada. The authors need to also thank all the students who have

contributed to this synthesis work. We are also indebted to thepartners who have supported the work in many ways: FPInnova-tions, CanmetENERGY, Hydro-Quebec, Green eld Ethanol andseveral Canadian Kraft mills.

References

[1] IEA, in: IEA Bioenergy Task 42 on Biore neries: Co-production of Fuels, Chem-icals, Power and Materials from Biomass, Minutes of the Third Task Meeting,Copenhagen, Denmark, 2007. http://www.biore nery.nl/ieabioenergy-task42 .

[2] F. Cherubini, The biore nery concept: using biomass instead of oil forproducing energy and chemicals, Energy Conversion Manage. 51 (2010)1412 e 1421.

[3] M. Towers, T. Browne, P. Stuart, J. Paris, in: Biore ning: The Pulp and PaperIndustry in Transition, 6th International World Energy System Conference,Turin, Italy, July 10 e 12, 2006, pp. 55 e 62.

[4] G. Smook, Handbook for Pulp and Paper Technologists, third ed. Angus Wilde,Vancouver, 2002.[5] E. Mateos-Espejel, M. Moshkelani, M.J. Keshtkar, J. Paris, in: Sustainability of

Green Integrated Forest Biore nery: Question of Energy, Annual Conference of the Canadian Pulp and Paper Industry, Montreal, Canada, February 1 e 3, 2011,pp. 139 e 143.

[6] E. Mateos-Espejel, L. Savulescu, J. Paris, Base case process development forenergy ef ciency improvement, application to a Kraft pulping mill. Part I:de nition and characterization, Chem. Eng. Res. Des. 89 (6) (2011) 742 e 752.

[7] E. Mateos-Espejel, L. Savulescu, F. Marchal, J. Paris, Uni ed methodology forthermal energy ef ciency improvement: application to Kraft process, Chem.Eng. Sci. 66 (2011) 135 e 151.

[8] CETC, CanmetENERGY e Pinch Analysis: For Ef cient Use of Energy, Water &Hydrogen, Catalogue M39 e 96/2003E, 2003.

[9] P. Navarri, S. Bdard, Part II: Assessing Water and Energy Consumption andDesigning Strategies for Their Reduction, Handbook of Water and EnergyManagement in Food Processing, Woodhead Publishing Limited, Cambridge,UK, 2008.

[10] E. Mateos-Espejel, L. Savulescu, F. Marchal, J. Paris, Base case process devel-

opment for energy ef ciency improvement, application to a Kraft pulping mill.Part II: benchmarking analysis, Chem. Eng. Res. Des. 89 (6) (2011) 729 e 741.

[11] A. Alva-Argaez, L. Savulescu, Water reuse project selection. A retro t path towaterand energy savings, Chem.Engineering Transactions 18 (2009)403 e 409.

[12] E. Mateos-Espejel, L. Savulescu, F. Marchal, J. Paris, Systems interactionsanalysis for the energy ef ciency improvement of a Kraft Process, Energy 35(12) (2010) 5132 e 5142.

[13] M. Marinova, E. Mateos-Espejel, B. Bakhtiari, J. Paris, in: A New Methodologyfor the Implementation of Trigeneration in Industry: Application to the KraftProcess, 1st European Conference on Polygenration, Tarragona, Spain, October16 e 17, 2007, pp. 1 e 20.

[14] M. Towers, Y. Boluk, J. Paris, T. Browne, in: The Biore nery: A Vision forCanadian Pulp and Paper Industry, World Congress on Industrial Biotech-nology and Bioprocessing, Toronto, Canada, July 11 e 14, 2006.

[15] M. Marinova, E. Mateos-Espejel, N. Jemaa, J. Paris, Addressing the increasedenergy demand of a Kraft mill biore nery: the hemicellulose extraction case,Chem. Eng. Res. Des 87 (2009) 1269 e 1275.

[16] H. Huang, S. Ramaswamy, U.W. Tschirner, B.V. Ramarao, A review of separa-tion technologies in current and future biore neries, Sep. Purif. Technol. 62(1) (2008) 1 e 21.

[17] B. Kamm, M. Kamm, Principles of biore neries, Appl. Microbiol. Biotechnol. 64(2) (2004) 137 e 145.

[18] H.Mao, J.M. Genco,S.H.Yoon,A. VanHeiningen,H. Pendse, Technicaleconomicevaluation of a hardwood biore nery using the near-neutral hemicellulosespre-extraction process, J. Biobased Mater. Bioenergy 2 (2) (2008) 177 e 185.

[19] M. Davy, V. Uloth, J. Cloutier, Econimic evaluation of black liquor treatmentprocesses for incremental Kraft pulping production, Pulp Paper Can. 99 (2)(1998) 35 e 39.

[20] F. Ohman, Precipitation and separation of lignin from Kraft black liquor, PhDthesis, Department of chemical and biological engineering, ChalmersUniversity Technology, 2006.

[21] Z. Perin-Lavasseur, L. Savulescu, M. Benali, in: Lignin Production and Pro-cessing Path Assessment: Energy, Water and Chemicals Integration Perspec-tive, Annual Conference of the Canadian Pulp and Paper Industry, Montreal,Canada, February 1 e 3, 2011, pp. 87 e 90.

[22] M. Moshkelani, E. Mateos-Espejel, W. Kamal, J. Paris, in: Integration of a Gasi cation Unit Into a Kraft Process: Energy and Economic Feasibility,

Annual Conference of the Canadian Pulp and Paper Industry, Montreal,Canada, February 1 e 3, 2011, pp. 238 e 241.[23] Earth System Research Laboratory, Global Monitoring Division, http://www.

esrl.noaa.gov/gmd/ccgg/trends/ .[24] F. Meunier, Domestiquer l effect de serre nergies et changement climatique,

second ed. (2008) Dunod, Paris.[25] T. Browne, in: Economics of Commodity Chemicals and Fuel From Forest

Biomass, Annual Conference of the Canadian Pulp and Paper Industry, Mon-treal, Canada, February 1 e 3, 2011, pp. 30 e 33.

http://www.biorefinery.nl/ieabioenergy-task42http://www.biorefinery.nl/ieabioenergy-task42http://www.biorefinery.nl/ieabioenergy-task42http://www.biorefinery.nl/ieabioenergy-task42http://www.esrl.noaa.gov/gmd/ccgg/trends/http://www.esrl.noaa.gov/gmd/ccgg/trends/http://www.esrl.noaa.gov/gmd/ccgg/trends/http://www.esrl.noaa.gov/gmd/ccgg/trends/http://www.esrl.noaa.gov/gmd/ccgg/trends/http://www.biorefinery.nl/ieabioenergy-task42

biorefinería forestal y su aplicación en la industria de pulpa y papel

Documents