WO2014193289A1 - A method for the treatment of spent pulping liquor for the removal and production of a lignin containing product - Google Patents
A method for the treatment of spent pulping liquor for the removal and production of a lignin containing product Download PDFInfo
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- WO2014193289A1 WO2014193289A1 PCT/SE2014/050572 SE2014050572W WO2014193289A1 WO 2014193289 A1 WO2014193289 A1 WO 2014193289A1 SE 2014050572 W SE2014050572 W SE 2014050572W WO 2014193289 A1 WO2014193289 A1 WO 2014193289A1
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- lignin
- stream
- filtration
- recovered
- depolymerisation
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Classifications
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- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C11/00—Regeneration of pulp liquors or effluent waste waters
- D21C11/0007—Recovery of by-products, i.e. compounds other than those necessary for pulping, for multiple uses or not otherwise provided for
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07G—COMPOUNDS OF UNKNOWN CONSTITUTION
- C07G1/00—Lignin; Lignin derivatives
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08H—DERIVATIVES OF NATURAL MACROMOLECULAR COMPOUNDS
- C08H6/00—Macromolecular compounds derived from lignin, e.g. tannins, humic acids
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C11/00—Regeneration of pulp liquors or effluent waste waters
- D21C11/04—Regeneration of pulp liquors or effluent waste waters of alkali lye
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/26—Nature of the water, waste water, sewage or sludge to be treated from the processing of plants or parts thereof
- C02F2103/28—Nature of the water, waste water, sewage or sludge to be treated from the processing of plants or parts thereof from the paper or cellulose industry
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C3/00—Pulping cellulose-containing materials
- D21C3/02—Pulping cellulose-containing materials with inorganic bases or alkaline reacting compounds, e.g. sulfate processes
Definitions
- the present invention relates to a method for treating spent pulping liquor for the removal and production of a lignin containing product and/or a stream of depolymerised lignin.
- US2008/0051566 said method being directed to precipitating lignin from a lignin containing liquid/slurry, such as black liquor, and comprising addition of 0 one or more compounds comprising sulphate or sulphate ions, or a mixture comprising said compound, to said liquid/slurry, adjustment of the pH level of the said liquid/slurry by acidifying using CO2 wherein the pH level is adjusted, and dewatering of said liquid/slurry so that a lignin product, or an intermediate lignin product, is obtained.
- a 5 method for separating lignin from black liquor said method also comprising precipitating lignin by acidifying, preferably by using carbon dioxide.
- WO2010/143997 there is disclosed a method for separation of lignin from original black liquor, the method comprising precipitation of lignin by a first acidification stage of the original black liquor, 0 followed by dewatering while forming a first filter cake with high content of lignin, suspending the first lignin filter cake in a second acidification stage, wherein a second lignin suspension is obtained, dewatering of the second lignin suspension forming a second filter cake with high content of lignin, washing the second filter cake water and finally dewatering of the washed 5 second lignin cake obtaining a lignin product.
- carbon dioxide is a preferred acidifying agent to use, in this case in the first acidification stage.
- US2010/0041879 there is disclosed a method for recovering a low sodium content lignin from spent kraft cooking liquor without the use of a strong mineral acid for acidulation, said method comprising the steps of acidulating a spent kraft cooking liquor with carbon dioxide gas to a pH below about 10.5, precipitating at least a portion of the lignin forming lignin agglomerates and lignin particles in the spent kraft cooking liquor and recovering a low water and low sodium content lignin product comprising calcium or magnesium compounds bound to said lignin.
- One objective of the present invention is to provide an effective method for treating spent pulping liquor / black liquor, which method overcomes the problems disclosed above, i.e. a method which permits the recovery and separation of lignin from kraft pulping liquor without concomitant loss of active alkali in the form of hydrogen sulphide and hydroxide ions and which substantially avoids the need of re-alkalization of the spent cooking liquor.
- Another objective of the present invention is to provide an integrated process for the efficient recovery of lignin from spent kraft pulping liquor and concomitant production of depolymerised lignin for use in fine chemicals production or as precursor for production of renewable fuels.
- a method for the treatment of spent pulping liquor for the removal and production of organic substances and recovering or recycling of aqueous cooking chemicals comprising: passing a spent pulping liquor flow from a digester or an evaporator, or from any other step in between the digester and the
- one aspect of the present invention is directed to a process comprising at least two filtration steps before the acid treatment instead of a pre-treatment comprising an acidifying step such as disclosed in all of US2008/0051566, US2008/0047674, WO2010/143997 and
- the lignin is precipitated after the first acidification with carbon dioxide, then the lignin is separated and the acidified remaining liquor is exposed to an alkali treatment to increase the pH value again so that it may be returned to the process again.
- the filtration steps enable to separate lignin without using an early acidification step.
- the present process is very cost-effective in terms of savings in additives like carbon dioxide and importantly, it preserves the major portion of active cooking chemicals in the form of hydroxide ions and hydrosulphide ions in the black liquor.
- the method disclosed in US2010/0041879, which is directed to ion exchanging the lignin is not preserving the active cooking chemicals, while the disadvantage in using acidulation for lignin precipitation is avoided.
- the present invention is directed to a process involving several filtration steps and, in order to preserve hydrogen sulphide in its active form, no carbon dioxide or other acid is added prior to final precipitation of lignin from a concentrated lignin stream, i.e. acid treatment is performed only after the filtration and separation steps are performed.
- the present invention is directed to the recovery of lignin and the concomitant recycling of cooking chemicals in its active form, including both alkali and different sulphuric compounds, which is a key feature with respect to the mill chemical balance hence the overall economy of a lignin recovery process.
- Diafiltration does not show or hint such recovery or recycling of active cooking chemicals. Secondly, the filtration steps disclosed are not performed in the same manner. In accordance with "Purification of Lignin Fuel from Kraft Black Liquor by Diafiltration” article it is suggested that the filtration of the solution after lignin precipitation is very difficult to perform. The filtration step according to "Purification of Lignin Fuel from Kraft Black Liquor by
- Diafiltration is performed at room temperature, which is outside the temperature range of the filtration steps of the present invention.
- the purpose of the work described in "Purification of Lignin Fuel from Kraft Black Liquor by Diafiltration” is to provide a lignin with a low ash content, while the present invention is related to the recovery of a lignin product, which optionally may be depolymerized, concomitant with the recycling of active cooking chemicals to the spent cocking liquor stream.
- the present invention provides an effective method in terms of lignin yield (whether the lignin is depolymerised or not) and recirculation and recovery of active aqueous cooking chemicals distinguishing itself from the prior art.
- aqueous cooking chemicals i.e. hydroxide ions, hydrosulphide ions
- active aqueous cooking chemicals i.e. hydroxide ions, hydrosulphide ions
- At least 80%, such as up to or even above 90%, of the total input of aqueous cooking chemicals is recovered or recycled without having been subjected to acidulation treatment.
- the expression "recovered or recycled” implies that the aqueous stream comprising cooking chemicals may be both directly and indirectly used in other parts of the process involved. As an example, recycling may imply recycling the aqueous stream comprising cooking chemicals to a pulp mill recovery cycle.
- the filtration step involving water addition may also be called diafiltration.
- a catalytic lignin depolymerisation step is integrated in the lignin recovery system of the present invention.
- Fig. 1 shows one possible process flow set-up according to one embodiment of the present invention.
- Fig. 2 shows one possible process flow set-up according to another embodiment of the present invention.
- Fig. 3 shows the set-up during the trials disclosed below for
- Fig.4 shows a process flow set-up according to another embodiment of the present invention, wherein a catalytic depolymerisation step is integrated in the lignin recovery plant.
- Fig. 5 shows yet another process flow set-up and embodiment directed to a basic catalytic depolymerisation step integrated in the lignin plant
- the lignin containing spent pulping liquor starting material used in the process of the invention may be of different types mainly depending on the pulping process and the wood raw material fed to the pulp mill.
- the spent pulping liquor is a kraft black liquor or a spent cellulose liquor originating from a soda pulping process.
- the spent pulping liquor contains spent cooking chemicals which chemicals needs to be recycled and reformed to fresh cooking chemicals within the pulp mill .
- a kraft black liquor is highly alkaline and has a pH value between 1 1 and 13.
- the black liquor contains both sodium hydroxide and sodium sulphide which both are active kraft cooking chemicals.
- the total content of inorganic salts dissolved in the kraft black liquor including the active cooking chemicals varies between 15 and 30 % by weight of the black liquor solids. The variation is mainly due to wood raw material and pulp product from the mill. It is a key objective of the present invention to recycle a major portion of these dissolved inorganic salts to the pulp mill chemicals recovery cycle prior to any substantial change in pH of the black liquor stream by addition of acid. Furthermore, it is of great importance to ensure that the pH value in streams charged or recycled to a chemicals recovery cycle of a kraft pulp mill always is kept above about 1 1 in order to minimize evolution of toxic and odorous hydrogen sulphide gas.
- the filter types used in the process may also be of different type, however membrane filters are preferred. Therefore, according to one specific embodiment of the present invention, at least one of the filtration steps is based on using membranes. According to yet another embodiment, both filtration steps are based on using membranes. It should be noted that the process according to the present invention may comprise more filtration steps than two, which is further discussed below, and such added steps may also be in the form of membrane filtration. Furthermore, modules may be used comprising more filters connected so that at least one filter may be bypassed during washing or maintenance of that filter.
- the membrane filtration(s) is nanofiltration and/or ultrafiltration. Both of these techniques and types of filters, i.e. ultrafilters and nanofilters, and the difference thereof are known. Nanofiltration and or ultrafiltration is
- the parameter cut-off which is a measure of the density of the membrane.
- Typical values for the cut-off of an ultrafilter are in the range of 10 - 100 kg/mol.
- the cut-off is normally in the range 0.1 - 15 kg/mol.
- the method also comprises at least one additional filtration step performed before the acid treatment, said filtration step involving a separation of the input stream into one aqueous stream comprising cooking chemicals being recovered or recycled and one stream having a concentrated content of organic substances.
- the method also comprises a pre-filtration step, said pre-filtration step involving a separation of the input stream of spent pulping liquor flow into one stream with large undesired molecules and one stream intended to be further filtrated.
- a filter may be the first one presented in the set-up example shown in fig. 2.
- Such a pre-filtration step is of special importance when the spent pulping liquor is based on hardwood (deciduous wood) as the hardwood liquor normally comprise a relatively high content of large polysaccharide molecules that may be separated from the liquor in such pre- treatment step.
- such pre-filtration removing undesired large molecules including polysaccharides and particles is an ultrafiltration.
- the solid/liquid separation step in which a solid lignin containing product is separated and recovered comprises at least one filter pressing step.
- this solid/liquid separation comprises a decanting step or a centrifugation step.
- the solid/liquid separation step is shown in both fig. 1 and fig. 2 after the acid treatment step.
- the solid/liquid separation step may be performed in one or more stages.
- the solid/liquid separation step comprises more than one filtration step wherein at least one filtration step involves the addition of water and acid. This addition is performed for washing performance reasons. Sulphuric acid can
- sulphuric acid is used in kraft mills and any sulphates can be recycled to the chemicals recovery cycle.
- acids can also be used for acidulation including mineral acids and organic acids.
- the lignin product obtained after acidic treatment and subsequent lignin precipitation besides ash also may contain more or less organic compounds originating from the celluloses in the wood.
- One such component following the lignin is hemicellulose. Therefore, according to one embodiment, organic product substances are at least lignin and hemicellulose, and wherein both are separated and present in the lignin product.
- the conditions used during filtration and lignin precipitation may differ depending on the spent pulping liquor treated and also the type of set-up according to the present invention.
- the water content in the feed to the filtration step in which water is added is up to 40 wt% when measured in relation to the feed of spent pulping liquor to the filtration.
- the temperature in at least one of the filtration steps is held above 85°C, e.g. above 90°C and preferably above 100°C. Temperatures well above 100°C, such as up to 150°C are fully feasible using ceramic membranes. For instance, a temperature in the range of 100-140°C may suitably be employed in an ultra and/or nanofiltration step, e.g. 120°C.
- the temperature is held in the range of 30 - 100°C in the acid treatment for precipitation of at least lignin.
- the temperature used in the acid treatment step is normally lower than in the filtration steps.
- the temperature in the acidulation step is selected based on the properties of the feed to the acidulation step as pH,
- a suitable temperature range for the acidulation step is e.g. 50 - 90°C for many embodiments according to the present invention.
- other parameters are important in the acid treatment, especially the pH value.
- the pH value is held below 10 in the acid treatment for precipitation of at least lignin.
- a pH value of from 3 - 8 may be used, e.g. 3 - 6, e.g. around a pH value of 4.
- the pH value is held in the range of 3-8 in the acid treatment for precipitation of at least lignin.
- the pH range in the acidulation step is adjusted by the addition of acid targeting a pH range of from 4-5.
- the process according to present invention is not directed to the use of several different acids or other additives for the recovery of lignin. Besides water and selected acid, no other or at least no other considerable additives are needed.
- the present invention is also related to a system configuration.
- the present invention is directed to a system for the treatment of spent pulping liquor for the removal and production of organic substances and recovering or recycling of aqueous inorganic cooking chemicals, said system comprising:
- a filter unit arranged to separate a spent pulping liquor flow from a digester or an evaporator, or from any other step in between the digester and the evaporator in a pulp mill, into one aqueous stream comprising a major portion of the cooking chemicals present in the spent pulping liquor being recovered or recycled and one stream having a concentrated content of organic substances;
- a subsequent filter unit said filter unit involving water adding capabilities and being arranged to separate the stream having a concentrated content of organic substances into one aqueous stream comprising cooking chemicals being recovered or recycled and one stream having a concentrated content of organic substances;
- a solid/liquid separation unit arranged to separate precipitated lignin from brine in order to produce a solid lignin containing product.
- At least one of the filter units is a membrane filtration unit.
- the set-up may comprise several membrane filters in series and/or parallel, also filters of different type, e.g. both ultrafilters and nanofilters. As alluded to hereinabove the set-up may have extra filtration units only intended to uphold the availability of the system, so that washing and maintenance cycles may be performed when the system is operating.
- the system also comprises at least one additional filter unit positioned before the acidulation step, said filter unit arranged for a separation of the input stream into one aqueous stream comprising cooking chemicals being recovered or recycled and one stream having a concentrated content of organic substances.
- the system may also comprise a pre-filter unit, said pre-filter unit arranged for a separation of the spent pulping liquor feed into one stream with large undesired molecules and one stream being further filtrated.
- This pre- filter may e.g. be an ultrafilter.
- the solid/liquid separation unit may be configured in different ways.
- the solid/liquid separation unit comprises at least one filter press.
- the solid/liquid separation unit comprises at least one filter press.
- the solid/liquid separation unit comprises at least one decanter or centrifuge.
- a lignin depolymerisation step is preferably performed on the retentate (concentrated stream of organic substances from a spent cooking liquor filtration unit) discharged from a first filtration step wherein the permeate (an aqueous solution comprising a major portion of the cooking chemicals, such as sodium and sulphur compounds) have been separated and recycled to the chemicals recover cycle.
- the retentate may be charged directly without prior concentration to the depolymerisation step and any alkali and sulphur compounds present in the retentate may act as catalysts in the depolymerisation step.
- the lignin concentration in the feed stream charged to a lignin depolymerisation step is considerably increased relative to the concentration of lignin in the spent cooking liquor.
- One or more catalysts may be added to the depolymerisation step in order to promote breakdown of the lignin macromolecule to smaller fragments.
- the catalyst may be composed of the inorganic chemicals present in the retentate only (sodium and sulphur salts, hydroxide ions).
- alkali in the form of potassium carbonate can be added to present in the depolymerisation step.
- one or more heterogeneous catalysts may also be present during catalyzed depolymerisation of the lignin in a depolymerisation step.
- a capping agent or a solvent may be present in the depolymerisation step.
- solvents include recycled depolymerized lignin product, phenols, vinyl acetate, butyl acetate, ethyl acetate, turpentine, cresol, light gasoil and BTX solvent recovered from nafta cracking.
- furans such as THF, organic acid rich hydrolysates from separation of hemicellulose from wood or C1 -C4 alcohols may be present during depolymerisation of lignin in a depolymerisation step.
- the depolymerisation step may be performed in continuous or batch reactors, preferably tubular reactors or CSTRs
- Preferred solvents present during depolymerisation of the retentate stream includes one or more of water, liquid carbon dioxide, hydrolysates, turpentine and/or methanol recovered in a chemical pulp mill or chemical dissolving pulp mill. It is particularly
- heterogeneous and sulphur tolerant catalysts that may be added to promote lignin depolymerisation( and partial deoxygenation) include Ni based catalysts supported on Al and/or Si supports, calcium compounds and Zr, Mo (M0S 2 ) and Cu compounds on support. Potassium carbonate is a preferred homogeneous catalyst.
- the heterogeneous catalysts can be separated from the lignin streams by for example magnetic separation or filtration and be recycled to the reactor with or without reactivation (decoking)
- reaction temperature in the catalytic step ranges from about 200 C to 375°C.
- the liquid hourly space velocity in a depolymerisation reactor is from 0.5 to 6 hours.
- Gases formed in a depolymerisation reactor may be removed from time to time or continuously from the reactor.
- Depolymerised lignin which is discharged from the reactor with the solvent may be concentrated by any or more of liquid-liquid extraction with a solvent, acidulation with an acid such as carbon dioxide or a mineral acid, membrane separation or centrifugation.
- the depolymerised lignin is recovered in the form of a pumpable liquid . Any lignin rich solids or aqueous streams comprising salts are recycled to the spent cooking liquor stream charged to the evaporators/recovery boiler. Acidic streams can be discharged to a crude tall oil acidulation plant or be neutralized and charged to the spent cooking liquor stream.
- Depolymerised lignin (coming from a molecular weight of 10 000 or more in the spent liquor down to about 300-500 g/mol after the depolymerisation step) may be further upgraded by treatment with hydrogen donor solvents or hydrogen in one or more catalytic steps in order to form components suitable for use in
- renewable diesel or renewable gasoline are renewable diesel or renewable gasoline.
- a lignin depolymerisation step consisting of one or more reactors in order to produce a stream of depolymerised lignin.
- one or more catalysts are added to be present during depolymerisation step.
- one or more solvents are added to be present during the depolymerisation step.
- depolymerised lignin is discharged from the depolymerisation reactor and directly or indirectly charged ton extraction step in which step a solvent is added dissolving the depolymerized lignin.
- the process disclosed above relating to forming a stream of depolymerised lignin may also involve one or more filtration steps after the depolymerisation step. Therefore, according to one embodiment of the present invention, the stream of depolymerised lignin being discharged from a depolymerisation reactor and/or a lignin containing stream from a subsequent extraction and/or acidulation step is passed through a subsequent filtration step in which water is added and in which the stream is separated into one aqueous stream comprising cooking chemicals being recovered or recycled and one stream having a content of organic substances.
- a stream of organic substances originating in lignin obtained by any of the procedures described herein may be purified by for example an acid treatment step, optionally in the presence of a solvent.
- a stream of depolymerised lignin is discharged from the depolymerisation reactor and separated from inorganic compounds in a subsequent separation step in order to form a purified liquid lignin product.
- the lignin product can advantageously be treated with hydrogen or hydrogen donor solvents in order to provide a fully deoxygenated lignin material.
- the spent cooking liquor is a kraft black liquor or origin from a kraft pulping process.
- At least one of the filtration step and/or the subsequent filtration step is a membrane filtration step.
- both of the filtration step and the subsequent filtration step are membrane filtrations.
- the membrane filtration(s) may be e.g. nanofiltration and/or ultrafiltration.
- the method also comprises at least one additional filtration step being performed before any acid treatment, said filtration step involving a separation of the input stream into one aqueous stream comprising cooking chemicals being recovered or recycled and one stream having a concentrated content of organic
- the solid/liquid separation step in which a solid lignin containing product is separated and recovered comprises at least one filter press step.
- the water content in the filtration step in which water is added may be up to 40 wt% when measured in relation to the input stream of spent pulping liquor flow.
- the temperature in at least one of the filtration step and/or the subsequent filtration step is held above 85°C.
- the temperature is held in the range of 30 - 100°C in any acid treatment step.
- the pH value is held below 10, such as in the range of 3-8, in an acid treatment step.
- Fig. 1 shows one possible process flow set-up according to the present invention.
- a spent pulping liquor stream is processed by subjecting it to a first filtration step involving fine ultrafiltration / nanofiltration (shown as FUF/NF).
- FUF/NF fine ultrafiltration / nanofiltration
- this step there is a separation of one stream comprising cooking chemicals being recovered or recycled and a second stream having a concentrated content of organic substances, such as lignin and hemicellulose.
- This second stream is then further processed by subjecting it to a diafiltration step (marked as DF) which involves the addition of water.
- DF diafiltration step
- this step there is separated one aqueous stream comprising cooking chemicals being recovered or recycled and another stream having a further concentrated content of organic substances (lignin / hemicellulose, etc.).
- the stream having a further concentrated content of organic substances is subjected to an acid treatment involving addition of acid and water.
- a precipitate comprising lignin, etc. is directed to solid/liquid separation, in this case a filtration, suitably passed through a filter press, for the final separation and recovery of a solid lignin containing product.
- the set-up arrangement shown in fig. 1 is suitable for a spent pulping liquor based on coniferous wood (softwood), but is not limited to such starting material.
- the set-up shown is only an example and may e.g. comprise further filtration steps, e.g. similar to the ones disclosed or e.g. pre-filtration steps of another type.
- the final filtration step may instead consist of a centrifuge or another separation equipment type.
- Fig. 2 shows another possible process flow arrangement according to the present invention.
- a pre-filtration step involving ultrafiltration (marked as UF) is incorporated as the first step.
- This step implies a
- Fig. 1 shows the steps shown in fig. 1 .
- This set-up embodiment shown in fig. 2 is suitable for a spent pulping liquor based on deciduous wood (hardwood) where a pre-filtration step sometimes is preferred or necessary.
- Fig. 3 shows the set-up during the trials disclosed below for
- Fig.4 shows a process configuration for lignin separation including an integrated lignin depolymerisation step.
- a spent cooking liquor discharged from a digester or an evaporator, or discharged from any other step treating spent cooking liquor in between the digester and the evaporator is passed through a filtration step in which the spent cooking liquor is separated into one aqueous stream comprising cooking chemicals being recovered or recycled and one stream having a concentrated content of lignin.
- the retentate from the filtration step concentrated with respect to lignin is passed directly without prior drying to a depolymerisation reactor in order to produce a stream of depolymerised lignin for export in liquid form to for example a petroleum refinery.
- Fig. 5 shows another possible process flow set-up and embodiment also directed to depolymerisation of lignin integrated in a lignin filtration plant.
- one stream of depolymerized lignin is discharged from a separation step following a nanofiltration step.
- a portion of the lignin discharged from the depolymerisation reactor (such as larger lignin particles), is passed via at least one filtration step in which water is added to then further exposed to an acid treatment for precipitation of lignin. After subsequent filtration, a solid lignin containing product is obtained.
- the set-up comprised two temperature controlled tanks in parallel having a volume of 200 liters each, a membrane module (for the ultrafiltration a M1 from A-tech Innovations GmbH, Gladbeck, Germany, was used, and for the nanofiltration a K01 from Orelis Environ réelle SAS, Salwears, France, was used) in which the ceramic membrane was installed, and two pumps of which one was used to pressurize the circuit and the second one was used to circulate the flow.
- the pressure was regulated with valves on the permeate side and the retentate side, respectively.
- TMP transmembrane pressure
- the cross-flow velocity was changed with the pump flow by means of a frequency converter (CD3100, Lust Antriebstechnik GmbH, Germany) and the flux was determined by means of weighing the permeate flow on an electrical balance (PL6001 -S, Mettler-Toledo Inc., Columbus, OH).
- One of the tanks was used only when washing and cleaning, the other functioned as the feeding tank.
- the flow was measured with an electromagnetic flow meter (Fischer&Porter Co. Ltd., Gottingen, Germany) and the pressure in the feed stream, retentate stream and permeate stream with a pressure indicator (dTrans p02, Jumo AB, Helsingborg, Sweden).
- a schematic view of the setup is shown in figure 3.
- the trials with polymeric membranes were conducted using a somewhat smaller set-up facility, based on the same principals.
- Two temperature controlled tanks in parallel having a volume of 90 liters each were used. One of them was used only for cleaning and the start-up sequence, the other one was used as a feeding tank.
- Three membrane modules (diameter 0.5 inch, length 1 m) in series, where the polymeric membranes were installed and a pump were used. The pressure was controlled with a valve on the retentate side and was registered with two pressure indicators. The flow was measured with a vortex flow meter
- the retention of hemicellulose was about 86% and 95%, respectively, for the ceramic membrane and the polymeric membrane. As such, a large amount of the hemicellulose was found in the retentate together with the lignin when both membranes were used.
- a polymeric membrane obtained an average flux of about 161 l/m 2 h and reached a volume reduction of about 84% at the concentrating step, while the ceramic membrane obtained a flux of about 250 l/m 2 h and a volume reduction of about 95%.
- a high flux and volume reduction may be desirable, and the ceramic membrane showed good results in that aspect.
- the retention of lignin was about 90% for the polymeric membrane, but almost 75% for the ceramic alternative. As such, the different membranes have different advantages when being compared to one another.
- Precipitation and filtration trials at different pH values and temperatures of different retentates have been performed.
- the trials were performed in a bench-scale equipment consisting of a heat-controlled stirred tank reactor with a volume of approximately one liter and a feed system to ensure a well- controlled addition of 6M sulphuric acid.
- the temperatures investigated varied between 35 ° C and 100 ° C. Different stirring rates and feeding rates of sulphuric acid were also studied.
- the addition of acid continued until the desired pH-value of 2 - 7 was reached whereupon the solution was either passed through a filter of 40 - 100 pm or submitted to after-treatment before filtered.
- the filtration unit consisted of a Buchner funnel connected to vacuum or a Larox lab unit (Labox 25, Larox, Lappeenranta, Finland). After filtration, the filter cake was subjected to a washing liquor of water and acid in order to reduce the sodium content of the lignin containing solid product.
- Precipitation and filtration of deciduous wood was also studied.
- the trials of nanofiltrated black liquor showed sufficient results in the temperature range of 40 ° C - 60 ° C.
- Precipitation and filtration of nanofiltrated black liquor pre-treated with ultrafiltration shows good results in a temperature interval of 40 ° C - 50 ° C. At 60 ° C sufficient results were obtained at the higher pH- values.
- Precipitation and filtration trials using retentate from membrane filtration of black liquor have been performed.
- the retentate from the membrane filtration was subjected to a lignin depolymerisation step involving base-catalytic heat-treatment before precipitation and filtration. No additional catalyst beyond the basic salts present in the retentates added.
- the depolymerisation was conducted during 2 hours at a temperature of 250 °C.
- the lignin average molecular weight was decreased by approximately 50 %.
- the precipitation was performed in a bench-scale heat-controlled stirred tank reactor with a volume of approximately one litre. Concentrated sulphuric acid was kept in a burette to ensure a controlled addition to the black liquor solution. The experiment was started when the target
- the precipitated solution was kept at the same temperature for a certain period of time ranging from 0 min to 1 .5 hours.
- the filtration unit consisted of a pressurized vessel with a volume of about 0.6 litres.
- the filter used had a mesh size of 60 pm.
- the pressure used was 0.5 bar. After filtration the filter cake was washed with washing liquor consisting of distilled water and acid in order to wash out some of the sodium in the lignin. Results of the precipitation and filtration
- the base-catalysed retentate had different properties compared to the original retentate since a depolymerisation occurred during the treatment.
- Both the lignin molecules and the hemicelluloses had smaller molecular weight distributions, which changed the properties of the lignin.
- the extracted lignin both had a different odor and colour compared to the lignin that was precipitated from concentrated black liquor alone.
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Priority Applications (8)
Application Number | Priority Date | Filing Date | Title |
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BR112015029859A BR112015029859A2 (en) | 2013-05-29 | 2014-05-09 | method for treating residual pulping liquor for the removal and production of a lignin-containing product |
SE1751100A SE540451C2 (en) | 2013-05-29 | 2014-05-09 | A method for the treatment of spent pulping liquor for the production of a stream of depolymerized lignin |
US14/893,739 US20160130752A1 (en) | 2013-05-29 | 2014-05-09 | Method for the treatment of spent pulping liquor for the removal and production of a lignin containing product |
CA2913852A CA2913852A1 (en) | 2013-05-29 | 2014-05-09 | A method for the treatment of spent pulping liquor for the removal and production of a lignin containing product |
SE1551720A SE1551720A1 (en) | 2013-05-29 | 2014-05-09 | A method for the treatment of spent pulping liquor for the removal and production of a ligning containing product |
EP14804698.0A EP3004455A4 (en) | 2013-05-29 | 2014-05-09 | A method for the treatment of spent pulping liquor for the removal and production of a lignin containing product |
SE1550127A SE1550127A1 (en) | 2013-05-29 | 2014-05-09 | A method for the treatment of spent pulping liquor for the production of a stream of liquid depolymerized lignin |
SE1550117A SE1550117A1 (en) | 2013-05-29 | 2014-05-09 | A method for the treatment of spent pulping liquor for the removal and production of a lignin containing product |
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SE1350648 | 2013-05-29 | ||
SE1350648-0 | 2013-05-29 | ||
SE1351587-9 | 2013-12-30 | ||
SE1351587 | 2013-12-30 |
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WO2014193289A1 true WO2014193289A1 (en) | 2014-12-04 |
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PCT/SE2014/050572 WO2014193289A1 (en) | 2013-05-29 | 2014-05-09 | A method for the treatment of spent pulping liquor for the removal and production of a lignin containing product |
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US (1) | US20160130752A1 (en) |
EP (1) | EP3004455A4 (en) |
BR (1) | BR112015029859A2 (en) |
CA (1) | CA2913852A1 (en) |
SE (4) | SE540451C2 (en) |
WO (1) | WO2014193289A1 (en) |
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WO2017095316A1 (en) | 2015-12-01 | 2017-06-08 | Ren Fuel K2B Ab | Depolymerized lignin in hydrocarbon oil |
AT519059A1 (en) * | 2016-09-02 | 2018-03-15 | Andritz Ag Maschf | Method for separating hemicelluloses from biomass digestion process water or spent alkalis |
WO2018226147A1 (en) * | 2017-06-05 | 2018-12-13 | Suncarbon Ab | Catalytic conversion of lignin |
WO2019164447A1 (en) | 2018-02-23 | 2019-08-29 | Ren Fuel K2B Ab | Composition of esterified lignin in hydrocarbon oil |
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EP3693508A1 (en) * | 2019-02-08 | 2020-08-12 | Scitech-service OY | Method for lignin production |
US11279643B2 (en) | 2016-03-31 | 2022-03-22 | Technion Research & Development Foundation Limited | Method for separation of magnesium and calcium ions from saline water, for improving the quality of soft and desalinated waters |
US11802183B2 (en) * | 2017-05-09 | 2023-10-31 | Fpinnovations | Lignin depolymerization process using chemicals recoverable by the kraft recovery cycle |
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CA2605672A1 (en) * | 2005-05-02 | 2006-11-09 | University Of Utah Research Foundation | Processes for catalytic conversion of lignin to liquid bio-fuels |
BRPI0520735B1 (en) * | 2005-12-07 | 2017-05-09 | Antonio Rodriguez Rivera Jose | "Method for processing lignocellulosic material and its apparatus". |
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EP2334625A1 (en) * | 2008-09-08 | 2011-06-22 | Basf Se | Method for the integrated production of cellulose and low-molecular-weight reusable materials |
CN103154097B (en) * | 2010-06-03 | 2017-01-18 | Fp创新研究中心 | method for separating lignin from black liquor |
US20140163245A1 (en) * | 2011-05-26 | 2014-06-12 | Michael A. Lake | Process for producing furfural from black liquor |
PT2726671T (en) * | 2011-06-28 | 2016-08-17 | Valmet Oy | Method for lignin separation from black liquor comprising removal of sulphur compounds from formed water effluent |
-
2014
- 2014-05-09 SE SE1751100A patent/SE540451C2/en not_active IP Right Cessation
- 2014-05-09 SE SE1550117A patent/SE1550117A1/en not_active Application Discontinuation
- 2014-05-09 SE SE1550127A patent/SE1550127A1/en not_active Application Discontinuation
- 2014-05-09 US US14/893,739 patent/US20160130752A1/en not_active Abandoned
- 2014-05-09 CA CA2913852A patent/CA2913852A1/en not_active Abandoned
- 2014-05-09 SE SE1551720A patent/SE1551720A1/en not_active Application Discontinuation
- 2014-05-09 WO PCT/SE2014/050572 patent/WO2014193289A1/en active Application Filing
- 2014-05-09 EP EP14804698.0A patent/EP3004455A4/en not_active Withdrawn
- 2014-05-09 BR BR112015029859A patent/BR112015029859A2/en not_active Application Discontinuation
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WO2018226147A1 (en) * | 2017-06-05 | 2018-12-13 | Suncarbon Ab | Catalytic conversion of lignin |
WO2019164447A1 (en) | 2018-02-23 | 2019-08-29 | Ren Fuel K2B Ab | Composition of esterified lignin in hydrocarbon oil |
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Also Published As
Publication number | Publication date |
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SE1551720A1 (en) | 2015-12-29 |
BR112015029859A2 (en) | 2017-07-25 |
SE540451C2 (en) | 2018-09-18 |
EP3004455A1 (en) | 2016-04-13 |
CA2913852A1 (en) | 2014-12-04 |
US20160130752A1 (en) | 2016-05-12 |
SE1550127A1 (en) | 2015-02-05 |
SE1550117A1 (en) | 2015-02-04 |
EP3004455A4 (en) | 2017-01-18 |
SE1751100A1 (en) | 2017-09-11 |
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