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    • 专利摘要:
    2090918SE (57) Abstract The present invention relates to a method and apparatusfor purifying crude tall oil. The purification method com-prises a first purification step (2) for separating at least sol-ids (8) from the crude tall oil and producing solids freecrude tall oil, and after the first purification step (2) a sec-ond purification step (4) for separating water (14) from thesolids free crude tall oil. The purification apparatus com-prises at least one solids separator (3, 5') for separating atleast solids (8) from the crude tall oil and producing solidsfree crude tall oil, and at least one water separator (5, 9)arranged downstream of the solids separator (3, 5') in theflow direction of the crude tall oil for separating at leastwater (14) from the solids free crude tall oil. (Figure 1)
    公开号:SE1150085A1
    申请号:SE1150085
    申请日:2011-02-07
    公开日:2011-08-09
    发明作者:Matti Ristolainen；Jaacko Nousiainen
    申请人:Upm Kymmene Corp；
    IPC主号:
    专利说明:

    [1] [0001] The present invention relates to purifying crude tall oil andparticularly to a method according to the preamble of claim 1. The present in-vention further relates to an apparatus according to the preamble of claim 17.
    [2] [0002] Tall oil is a by-product of kraft pulping of coniferous trees. ltcomprises resins acids, fatty acids and unsaponifiables. Tall oil is recoveredfrom black liquor that is formed as a result of pulping coniferous trees in alka-line cooking liquor form black liquor. The black liquor contains cooking chemi-cals, Iignin and other substances separated from the wood. The black liquor isthen concentrated and left to settle. Tall oil soap rises on the surface of theblack liquor and can be separated from it. The soap is acidulated by addingacid, such as sulphuric acid to the soap and crude tall oil is produced. Thecrude tall oil (CTO) may further be distilled for producing distilled tall oil (DTO).
    [3] [0003] CTO can be used for different purposes, for example for pre-paring soap, pine soap, cosmetic products or carbonaceous fuel components.The carbonaceous fuel components are produced by catalytic hydrodeoxy-genation (HDO) and/or hydroisomerization (Hl) of CTO, as is described for ex-ample in document WO2008/O58664. One problem when using CTO as feed-stock for fuel components is that metals in the CTO tend to deactivate thecatalysts used in these catalytic processes. The metals in the CTO poison thecatalysts active sites thus preventing the catalysts from functioning properly.Furthermore, the Iignin residues in the CTO clogs the pores of the catalyst alsodeactivating the catalyst. Consequently, when preparing fuel components fromCTO, it is purified before the HDO and/or Hl steps to remove impurities, suchas metals, residue Iignin and/or carbohydrate derived material and possibleother substances.
    [4] [0004] Document WO2008/058664 describes a process in whichfeedstock, vegetable oil or animal oil, is treated before HDO step to remove al-kaline metals and alkaline earth metals from the feedstock. This treatment isconducted by washing the feedstock with slightly acidic media or absorbing themetals on a suitable material, for example using ion exchange resins.
    [5] [0005] Document EP 1741768 describes a process in which thefeedstock, bio oil or fat, is degummed before HDO step. ln degumming phos- 2090918SE phorous compounds are removed from the feedstock and it is performed bywashing the feedstock with H3PO4, NaOH and soft water and separating theformed gums. Most of the metal components in the feedstock are removedduring degumming.
    [6] [0006] After the metal components removal, lignin and possibleother residues are separated from the feedstock by e.g. decanting.
    [7] [0007] One of the problems associated with the prior art vegetableoil based feedstock purification methods is that they are slow and inefficientthus making them difficult to be used in processes for producing biofuels. lf thefeedstock is CTO, it comprises metals such as copper, iron, sodium, phospho-rus, silicon and also some aluminium, calcium, potassium and lead. Washingbased methods for removing metals do not decrease the metal content of thefeedstock sufficiently to prevent deactivation of the catalytic agent used in theHDO and Hl steps. Furthermore a considerable amount of feedstock, CTO, islost together with the separated lignin when decanting the feedstock for ligninand possible other residues. This decreases the yield of the process such thatless biofuel is obtained from a specific volume of feedstock.
    [8] [0008] An object of the present invention is to provide a method andan apparatus so as to overcome the above prior art problems. The objects ofthe invention are achieved by a method according to the characterizing portionof claim 1, which method is characterized in that purifying comprises a first pu-rification step for separating at least solids from the crude tall oil and producingsolids free crude tall oil, and after the first purification step a second purificationstep for separating water from the solids free crude tall oil by phase separation.The objects of the invention are further achieved by an apparatus according tothe characterizing portion of claim 17, which apparatus is characterized in thatthe apparatus comprises at least one solids separator for separating at leastsolids from the crude tall oil and producing solids free crude tall oil, and at leastone water separator arranged downstream of the solids separator in the flowdirection of the crude tall oil for separating at least water from the solids freecrude tall oil by phase separation.
    [9] [0009] The preferred embodiments of the invention are disclosed inthe dependent claims.
    [10] [0010] The invention is based on the idea of purifying crude tall oil inat least in two consecutive steps such that first the crude tall oil is subjected to 2090918SE a purification treatment where mostly solids are separated from the CTO andafter that to a purification treatment where essentially water is separated fromthe solids free CTO by phase separation. ln the first purification step the crudetall oil is filtered or subjected to phase separation in which most of the solidsare removed from the crude tall oil. ln the second purification step the crudetall oil is subjected to phase separation in which water is removed from thecrude tall oil. The phase separation in the second purification step may com-prise, for example, decantation, centrifugation, a liquid coalescing process orany combination thereof for removing water from the crude tall oil.
    [11] [0011] An advantage of the present invention is that it provides anefficient and fast solution for removing unwanted metals and residue ligninfrom the CTO. ln the present invention the residue lignin precipitates togetherwith the metals in the CTO. The precipitation may be further enhanced by ad-justing the pH-value of the CTO, preferably it is set between 0.5 and 6. Theprecipitated lignin and metals are separated together from the CTO and thusthe quality of the CTO is improved and the yield of the CTO process for pro-ducing biofuel components increases. After the most solids have been sepa-rated from the CTO, it is further subjected to water removal step in which es-sentially water and possible residue metals and metals dissolved into the waterare removed. The purification method of the present invention is fast and pro-vides an efficient solution for purification of tall oil to be used efficiently in theprocess for preparlng fuel components from CTO. This means, that the cata-lysts will not be poisoned or clogged by the impurities and the lifetime of thecatalysts used in fuel manufacturing processes is much longer than beforewhen prior art purification methods of the feedstock have been used.
    [12] [0012] ln the following the invention will be described in greater de-tail by means of preferred embodiments with reference to the attached draw-ings in which
    [13] [0013] Figure 1 is a schematic flow diagram showing the purificationof CTO according to the present invention;
    [14] [0014] Figures 2 to 5 show schematic flow diagrams showing em-bodiments of the apparatus of the present invention. 2090918SE Definitions
    [15] [0015] ln the present description and claims, the following termshave the meanings defined below.
    [16] [0016] The term “CTO” or “crude tail oil” refers to a by-product of theKraft process of wood pulp manufacture. CTO contains generally both satu-rated and unsaturated oxygen-containing organic compounds such as rosins,unsaponifiables, sterols, resin acids, fatty acids, fatty alcohols and other alkylhydrocarbon derivatives as well as inorganic ímpurities. CTO also contains lig-nin, metals and small particles such as fibers and fines.
    [17] [0017] The term "solids free CTO" refers to crude tall oil that hasbeen purified in the first purification step. Most of the solid matter and metalshave been removed from it, but it may still contain minor amounts of lignin,metals and other small particles.
    [18] [0018] The term "purified CTO" refers to crude tall oil that has beenpurified both in a first purification step and after that in a second purificationstep. Lignin, solid matter, metals and water has been removed from it in suchan extent that the purified CTO can be used in different end applications, forexample for fuel component production.
    [19] [0019] “Phase separation” refers to a separation process that isbased on gravity and different densities of the components to be separated.
    [20] [0020] Figure 1 shows a schematic flow diagram of the purificationarrangement of CTO according to the present invention. ln the figures 1 to 5same features are denoted with same reference numerals. The purification ar-rangement comprises a first purification step 2 for separating solids from thecrude tall oil and after the first purification step 2 a second purification step 4for separating water from the crude tall oil. The second purification step 4 is ar-ranged after the first purification step 2 in the direction of the CTO flow. CTOproduced by pulping of coniferous trees, is first conducted to the first purifica-tion step 2 through conduit 16. ln the first purification step 2 at least solids 8are separated by at least one solids separator from the CTO and removedfrom the first purification step along conduit 20. The solids free CTO from thefirst purification step 2 is further conducted along conduit 18 to second purifica-tion step 4, where at least one water separator separates at least water 14from the solids free CTO. The separated water 14 is removed from the second 2090918SE purification step along conduit 26. Alternatively the solids free CTO may beconducted from the first purification step 2 via an intermediate storage tank 6to second purification step 4, which is shown in figure 6 by dotted line. The sol-ids separator may be a filter, two phase separator or a three phase separatoror any other means capable of separating solids from CTO. The water separa-tor may be for example a two phase separator, three phase separator, de-canter apparatus, centrifuge, liquid coalescing apparatus, any combinationthereof or any other means for separating water from CTO where the separa-tion is based on gravity and different densities of the components to be sepa-rated. After the second purification step 4 the purified CTO is conducted astorage tank 10 along conduit 24. From the storage tank 10 the purified CTOmay be conducted to catalytic hydrodeoxygenation (HDO) and/or hydroisom-erization (HI) for preparing carbonaceous fuel components, such as biofuel.
    [21] [0021] The present invention is based on the idea using two-steppurification for crude tall oil in such a way that first most of the solids are re-moved from the CTO and then water is removed from the CTO. The first purifi-cation step 2 may be conducted by filtering or by phase separation for separat-ing solids from the CTO. The second purification step 4 may be conducted byphase separation, for example by decantation, centrifugation, liquid coalescingprocess or by any combination thereof. ln the following some preferable em-bodiments of the apparatus of the present invention are described referring tofigures 2 to 5.
    [22] [0022] Figure 2 shows one embodiment of the present invention inwhich the first purification step 2 is carried out by filtering the CTO to removeprecipitated lignin, metals and other possible solids 8. The filtering is preferablycarried out by pressure filtering using one or more pressure filters 3. A pres-sure filter usually comprises a filter cloth or membrane through which the me-dium to be filtered is forced by. aid of pressure. During filtering a filtering cake isformed on the filter cloth or filter membrane from the precipitated metals, ligninand possible other solid impurities. This filtering cake retains and absorbs alsometals and alkali metals still remaining in the CTO. Pressure filters and the fil-tering process using them are well known and will thus not be discussed herein detail. The first purification step 2 therefore removes most of the solids, met-als and precipitated lignin from the CTO. During filtering step the temperatureof the CTO is between 20 to 120°C, preferably between 50 to 100°C, and morepreferably about 90°C. 2090918SE
    [23] [0023] The filtering may be enhanced by adding filtration aid by fil-tration aid supply means 15 along conduit 27 to the CTO before the one ormore filters 3. Filtration aid 15 is added to prevent solids or other precipitates inthe CTO forming a sticky impermeable filter cake. The cake properties and fil-tering efficiency are enhanced by maintaining the permeability of the accumu-lating cake by using the filtration aid 15. The filtration aid 15 is removed fromthe CTO during the filtering in the filter 3. Cellulose, cellulose containingchemical agents, chemical pulp or combination thereof may be used as filtra-tion aid 15. Also other suitable filtration aid material can be used. The filtercake may be periodically removed from the filter. The removed filter cake com-prising llgnin and possibly also fibres may be burned for producing energy.
    [24] [0024] From the first purification step 2 the solids free CTO is con-ducted to the second purification step 4 via conduit 18. The second purificationstep comprises one or more phase separators 5, in which both water 14 andremaining solids 12 are separated from the solids free CTO. As phase separa-tors, two or three phase separators can be used. ln a phase separator, theCTO separates from the water and solids thus producing purified CTO. Phaseseparators and their operating principles are well known and will thus not bediscussed here in detail. The separated water 14 is removed from the one ormore separators 5 through conduit 26 and the removed solids 12 are removedthrough conduit 28. The purified CTO that is conducted to the storage tank 10through conduit 24 has therefore both solids 8, 12 and water 14 separatedfrom it. i
    [25] [0025] To enhance the separation of llgnin, metals and possibleother impurities which may be dissolved into the CTO, the apparatus also con-tains washing means for washing the CTO. Washing the crude tall oil with wa-ter is carried out before the first purification step 2. Alternatively or additionallythe solids free CTO is washed with water between the first purification step 2and the second purification step 4. Washing is carried out in the first and/or thesecond purification steps 2, 4, before the purification means 3 and/or 4. ln theembodiment presented in Fig 2, there is a first washer 13 before the one ormore filters 3 for washing the CTO and a second washing means 17 before theone or more phase separators 5 for washing the solids free CTO. TheCTO/solids free CTO is preferably washed with hot water but also cold watermay be used. Washing with water may be conducted in any know method andapparatus, such as washing column. ln the case where several purification 2090918SE means are used in a purification step, the washer may also be arranged be-tween the different purification means in the same step.
    [26] [0026] pH-value of the CTO has an important effect on the precipita-tion of lignin, metals and other possible impurities in the CTO. Low pH-value ofthe CTO causes the residue lignin, possible residue fibres or other impurities toprecipitate in the CTO. The pH-value of the CTO has to be under 7, preferablyunder 4 so that the precipitation of lignin, metals and possible other impuritiesis sufficient. ln a preferred embodiment the pH-value of the CTO is between0.5 and 6 and more preferably between 1 and 3. The pH-value of the CTO maybe already in the preferred range when the CTO is conducted from the soapseparation to the purification, but this is not always the case. When the pH-value of the CTO is not in the preferred range, it has to be adjusted. The pH-value of the crude tall oil is preferably adjusted before the first purification step,i.e. filter 3 or any other solids separator, but it may also be conducted beforethe second purification means, i.e. phase separator 5 or any other water sepa-rator. Thus adjusting the pH-value of the crude tall oil is carried out before thefirst purification step 2. Alternatively or additionally adjusting the pH-value iscarried out by adjusting pH-value of the solids free crude tall oil between thefirst purification step 2 and the second purification step 4.The pH-value of theCTO is adjusted to be under 7, preferably under 6, more preferably between0.5 to 6 and most preferably between 1 to 3 for enhancing the precipitation oflignin, metals and possible other impurities in the CTO effectively. The adjust-ing of the pH-value of the crude tall oil is normally carried out by lowering thepH-value of the CTO or solids free CTO. Lowering the pH-value of the CTO orsolids free CTO may be carried out with acid washing or acidificatlon usingsulphuric acid, formlc acid, acetic acid or lactic acid. The acid washing may beconducted by the first washer 13 or by the second washer 17, as shown in fig-ure 2. The acid washing may be conducted in an acid washing column or ves-sel in any known washing method. The acid washing column is preferably ar-ranged to provide counter current acid wash. Acidification of the CTO may alsobe conducted by mixing acid or acidic water to CTO or solids free CTO in aconduit in which the CTO/solids free CTO is conducted or in an acidificatlonvessel or the like. The acid washing or acidification removes metals, alkalimetals, phospholipids and other impurities from the CTO/solids free CTO.Temperature of the CTO/solids free CTO during acid washing is between 40 to120°C, preferably between 50 to 100°C, and more preferably 90°C. During 2090918SE acid washing or acidification the pH-value of the CTO/solids free CTO de-creases in response to the used acid and the dosage of the used acid. lnsummary, adjusting the pH-value of the CTO may be carried cut in any loca-tion before purification step in which solids are separated from the CTO.
    [27] [0027] The pH-value of the CTO/ solids free CTO is controlled by apH control unit 30. There are several pH measurement means (not shown inthe Figure) in the apparatus that measure the pH of the CTO or solids freeCTO. The pH can be measured either from the washers 13 and/or 17 or fromthe conduits transferring the CTO/solids free CTO. The pH measurement sig-nal 31 from the first washer 13 and /or the pH measurement signal 32 meas-ured from the conduit 16 is transmitted to the control unit 30. Also the pHmeasurement signal 33 from the second washer 17 and /or the pH measure-ment signal 34 measured from the conduit 22 is transmitted to the control unit30. The control unit calculates the amount of acid needed for achieving thesuitable pH range and transmits this information to acid controller 25 whichcontrols the amount of acid that is supplied to the process. The acid is addedthrough conduit 35 to one or more of the following parts of the process: to thefirst washer 13, conduit 16, second washer 17 and conduit 22, depending onthe pH value of the corresponding purification step and the purification meansused in the step. As can be realized from above, the pH value of the washingwater in the washers 13 and/or 17 can be controlled by the control unit 30. Al-ternatively the pH-value of the CTO/solids free CTO can be carried out inde-pendently and separately from the washers 13, 17.
    [28] [0028] The embodiment shown in figure 3 presents the apparatus,where the second purification step 4 comprises a water separator 9 whichdoes not substantially separate solids from the CTO. The water separator 9separates mainly water 14 which is removed from the separator 9 via conduit26. As solids are not separated from the solids free CTO in the second purifi-cation step, there is no need to adjust the pH-value before the second purifica-tion means, i.e. water separator 9. The water separation in the second purifica-tion step 4 may be carried out by decantation, centrifugation, liquid coalescingor by any combination thereof. The mentioned methods for separating waterfrom the solids free CTO in the second purification step may be carried out byusing one or more water separators 9 for decantation, centrifugation, and liq-uid coalescing. ln the embodiment of figure 3, the first purification step 2 issimilar to the first purification step 2 of the embodiment shown in Figure 2. 2090918SE Thus the first purification step 2 is carried out by filtering the CTO to removeprecipitated lignin, metals and other possible solids 8. The filtering is preferablycarried out by pressure filtering using one or more pressure filters 3. The filter-ing may be enhanced by adding filtration aid by filtration aid supply means 15along conduit 27 to the CTO before the one or more filters 3. From the first pu-rification step 2 the solids free CTO is conducted via conduit 18 to the secondpurification step 4. The CTO is washed in a first washer 13 before it is fed tothe filter 3. The pH of the washing water and/or the pH of the CTO can be con-trolled by a pH controller 30 in similar way as was explained in connection ofFigure 2.
    [29] [0029] Figure 4 shows a schematic flow diagram of the purificationapparatus according to another embodiment of the present invention. ln theembodiment of figure 4 both the first purification step 2 and the second purifi-cation step 4 are carried out by using at least one phase separator 5', 5. Asphase separators, two or three phase separators can be used. The separatedwater 19 from the separators 5' in the first purification step 2 is removed viaconduit 21 and the removed solids 8 are removed via conduit 20. From thesecond purification step 4, the separated water 14 is removed from the separa-tors 5 through conduit 26 and the removed solids 12 are removed through con-duit 28.
    [30] [0030] Washing CTO and/or the solids free CTO as well as adjust-ing the pH-value of the CTO/solids free CTO are carried out in the same man-ner as in the embodiment of figure 2.
    [31] [0031] Figure 5 shows yet another embodiment of the present in-vention in which the first purification step 2 comprises one or more phaseseparators 5' and the second purification step 4 comprises one or more waterseparation equipments 9 that provide water separation by decantation, cen-trifugation, liquid coalescing or by any combination thereof. Therefore the em-bodiment of figure 5 corresponds the embodiment of figure 3, but the filtering 3is replaced with three phase separation 5”. Thus, in the embodiment of figure 5the first purification step 2 is carried out by using at least one phase separator5”. As phase separators, two or three phase separators can be used. The sep-arated water 19 from the separators 5' in the first purification step 2 is removedvia conduit 21 and the removed solids 8 are removed via conduit 20. Washingthe CTO as well as adjusting the pH-value of the CTO are carried out in thesame manner as in the embodiment of figure 4 or 2. 2090918SE
    [32] [0032] The purified CTO conducted to storage tank 10 may be thensubjected to HDO and/or Hl steps carried out in HDO and/or HI sections. lfonly HDO step is used, the product received from HDO step may further besubjected to isomerisation for producing biofuel. The purified CTO may also beconducted to any other known process for preparing fuel components or otherproducts from the purified CTO.
    [33] [0033] According to the above mentioned the apparatus andmethod of the present invention is based on purifying the CTO in two subse-quent purification steps and in at least two subsequent purification means. lnthe first purification step 2 most of the solids are separated from the CTO. Thesolids separation may be carried out with one or more filters 3 or one or morethree phase separators 5', which also separate water from the CTO. After thefirst purification step 2, the solids free CTO is subjected to a second purifica-tion step 4 for essentially separating water from the solids free CTO. The sec-ond purification step 4 may be carried out using one or more phase separators5, which also separate remaining solids from the solids free CTO, for exampleby decantation, centrifugation, liquid coalescing or by any combination thereof.
    [34] [0034] lt will be obvious to a person skilled in the art that, as thetechnology advances, the inventive concept can be implemented in variousways. The invention and its embodiments are not limited to the examples de-scribed above but may vary within the scope of the claims.
    权利要求:
    Claims (32)
    [1] 1. A method for purifying crude tall oil, c h a r a c te r i z e d in thatthe purifying comprises a first purification step (2) for separating at least solids(8) from the crude tall oil and producing solids free crude tall oil, and after thefirst purification step (2) a second purification step (4) for separating water (14)from the solids free crude tall oil by phase separation.
    [2] 2. A method according to claim 1, c h a r a c t e r i z e d in that sol-ids (8) are separated from the crude tall oil in the first purification step (2) byfiltering.
    [3] 3. A method according to claim 2, c h a ra c te r i z e d in that fil-tering is carried out by pressure filtration.
    [4] 4. A method according to claim 2 or 3, c h a ra cte rize d byadding filtration aid to the crude tall oil before the filtering of the crude tall oil.
    [5] 5. A method according to claim 4, c h a r a c t e r i z e d in that fil-tration aid is selected from the following: cellulose, cellulose containing chemi-cal agent, chemical pulp and a combination thereof.
    [6] 6. A method according to claim 1, c h a r a c t e r i z e d in that sol-ids are separated from the crude tall oil in the first purification step (2) byphase separation.
    [7] 7. A method according to claim 6, c h a ra c t e r i z e d in that thephase separation is carried out by a three phase separator or by a two phaseseparator separating both solids (8) and water (19) from the crude tall oil.
    [8] 8. A method according to claim 1, c h a ra cte r i z e d in that thephase separation is carried out with a three phase separator or a two phaseseparator separating both remaining solids (12) and water (14) from the solidsfree crude tall oil.
    [9] 9. A method according to claim 1, c h a r a c t e r i z e d in that wa-ter (14) is separated from the solids free crude tall oil in the second purificationstep (4) by one of the following phase separation methods: decantation, cen-trifugation, liquid coalescing process and any combination thereof.
    [10] 10. A method according to claim 1, c h a r a c t e r i z e d by adjust-ing the pH-value of the crude tall oil before separating solids (8, 12) from thecrude tall oil. 2090918SE 12
    [11] 11. A method according to claim 1, c h a r a c t e r i z e d by adjust-ing the pH-value of the crude tall oil before the first purification step (2) and/orby adjusting the pH-value of the solids free crude tall oil between the first puri-fication step (2) and the second purification step (4).
    [12] 12. A method according to claim 10 or 11, c ha racte rized byadjusting the pH-value of the crude tall oil or solids free crude tall oil between0.5 to 6.
    [13] 13. A method according to claim 10 or 11, c h a racte rized byadjusting pH-value of the crude tall oil or solids free crude tall oil between 1 to 3.
    [14] 14. A method according to claim 10 or 11, c h a ra cte rize d byIowering the pH-value of the crude tall oil or solids free crude tall oil by acidwashing or acidification.
    [15] 15. A method according to claim 14, c h a ra c te r i z e d in thatthe acid washing or acidification is performed using sulphuric acid, formic, ace-tic acid or lactic acid _
    [16] 16. A method according to claim 10 or 11, c h a ra cte rize d bywashing the crude tall oil with water before the first purification step (2) and/orby washing the solids free crude tall oil with water between the first purificationstep (2) and the second purification step (4).
    [17] 17. An apparatus for purifying crude tall oil, c h a r a c t e r i z e d inthat the apparatus comprises at least one solids separator (3, 5') for separatingat least solids (8) from the crude tall oil and producing solids free crude tall oil,and at least one water separator (5, 9) arranged downstream of the solidsseparator (3, 5') in the flow direction of the crude tall oil for separating at leastwater (14) from the solids free crude tall oil by phase separation.
    [18] 18. An apparatus according to claim 17, c h a r a c t e r i z e d inthat the solids separator (3, 5') comprises at least one filter (3) for separatingsolids (8) from the crude tall oil.
    [19] 19. An apparatus according to claim 18, c h a r a c t e r i z e d inthat the filter (3) is a pressure filter.
    [20] 20. An apparatus according to claim 18, c h a r a c t e r i z e d inthat the filter is provided with a chargeable filter cloth or filter membrane forremoving metals from the crude tall oil.
    [21] 21. An apparatus according to claim 18, c h a r a c te r i z e d inthat the apparatus further comprises supply means (15) for supplying filtrationaid to the crude tall oil before the filter (3). 2090918SE 13
    [22] 22. An apparatus according to claim 21, c h a r a c t e r i z e d inthat the filtration aid is one of the following: cellulose, cellulose containingchemical agent or combination thereof.
    [23] 23. An apparatus according to claim 17, c h a r a c te r i z e d inthat the solids separator (3, 5') comprises one or more three phase or twophase separators (5') for separating solids (8) and water (19) from the crudetall oil.
    [24] 24. An apparatus according to claim 17, c h a r a c t e r i z e d inthat that the water separator (5, 9) comprises one or more three phase or twophase separators (5) for separating water (14) and remaining solids (12) fromthe solids free crude tall oil.
    [25] 25. An apparatus according to claim 17, c h a r a c t e r i z e d inthat that the water separator (9) is one of the following: decanter apparatus,centrifuge, liquid coalescing apparatus or any combination thereof.
    [26] 26. An apparatus according to claim 17, c h a r a c t e r i z e d inthat the apparatus comprises a first washer (13) before the solids separator (3,5') for washing the crude tall oil with water or with acidic water.
    [27] 27. An apparatus according to claim 17, c h a r a c t e r i z e d inthat the apparatus comprises a second washer (17) between the solids sepa-rator (3, 5') and the water separator (5, 9) for washing the solids free crude talloil with water or with acidic water.
    [28] 28. An apparatus according to claim 17, c h a r a c t e r i z e d inthat the apparatus further comprises - a control unit (30) for adjusting the pH-value of the crude tall oil orsolids free crude tall oil, - an acid reservoir (25) and - a conduit (35) connected thereto for adding the amount of acid de-termined by the control unit (30) to one of the following: the first washer (13),the second washer (17), the crude tall oil and the solids free crude tall oil.
    [29] 29. An apparatus according to claim 28, c h a r a c t e r i z e d inthat the control unit (30) is arranged to calculate the amount of acid to beadded according to measurement signals (31, 32, 33, 34) measured from oneof the following locations: the first washer (13), the second washer (17), beforethe solids separator (3,5') and before the water separator (5, 9). 2090918SE 14
    [30] 30. An apparatus according to claim 28, c h a r a c t e r i z e d inthat the control unit (30) is arranged to adjust the pH-value of the crude tall oilor solids free crude tall oil between 0.5 to 6.
    [31] 31. An apparatus according to claim 28, c h a r a c t e r i z e d inthat the control unit (30) are arranged to adjust the pH-value of the crude tall oilor solids free crude tall oil between 1 to 3.
    [32] 32. Use of two step purification of crude tall oil for preparing fuelcomponents from it, in which two step purification solids are first separatedform the crude tall oil and solids free crude tall oil is produced, and then wateris removed from the solids free crude tall oil.
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    同族专利:
    公开号 | 公开日
    FI123968B|2014-01-15|
    FI20105121A0|2010-02-08|
    CA2731326A1|2011-08-08|
    US20110213169A1|2011-09-01|
    US8816105B2|2014-08-26|
    FI20105121A|2011-08-09|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2358004A|1940-03-11|1944-09-12|Russell G Dressler|Treatment of tall oil|
    FI66296C|1983-01-11|1984-10-10|Linotek Oy|CONTAINER SEPARATIONSANORDNING OCH FOERFARANDE FOER SEPARERING AV I EN VAETSKEBLANDNING INGAOENDE LAETTA OCH TUNGA VAETSKEFORMIGA FRAKTIONER|
    US20060264684A1|2005-05-19|2006-11-23|Petri John A|Production of diesel fuel from biorenewable feedstocks|
    DK1741768T3|2005-07-04|2015-10-26|Neste Oil Oyj|A process for the preparation of dieselcarbonhydrider|
    ITMI20062193A1|2006-11-15|2008-05-16|Eni Spa|PROCESS FOR PRODUCING HYDROCARBURAL FRACTIONS FROM MIXTURES OF BIOLOGICAL ORIGIN|
    US7982076B2|2007-09-20|2011-07-19|Uop Llc|Production of diesel fuel from biorenewable feedstocks|
    WO2009131510A1|2008-04-21|2009-10-29|Sunpine Ab|Conversion of crude tall oil to renewable feedstock for diesel range fuel compositions|
    CN101445742A|2008-12-30|2009-06-03|浙江工业大学|Method for preparing biodiesel by utilizing stratified and graded esterified deacidification of high acid value oil|
    FI124508B|2009-02-27|2014-09-30|Upm Kymmene Oyj|Method and apparatus for making fuel components from crude tall oil|FI126819B|2012-02-13|2017-06-15|Upm-Kymmene Corp|Method for Concentrating Fibril Pulp and Fibril Pulp Product|
    FI126505B|2015-07-08|2017-01-13|Upm-Kymmene Corp|Method and system for reducing residual sludge in crude tall oil|
    法律状态:
    2014-09-30| NAV| Patent application has lapsed|
    优先权:
    申请号 | 申请日 | 专利标题
    FI20105121A|FI123968B|2010-02-08|2010-02-08|Process and apparatus for cleaning crude oil|
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