NZ712768B2 - Process and system for preparing dry milk formulae - Google Patents
Process and system for preparing dry milk formulae Download PDFInfo
- Publication number
- NZ712768B2 NZ712768B2 NZ712768A NZ71276814A NZ712768B2 NZ 712768 B2 NZ712768 B2 NZ 712768B2 NZ 712768 A NZ712768 A NZ 712768A NZ 71276814 A NZ71276814 A NZ 71276814A NZ 712768 B2 NZ712768 B2 NZ 712768B2
- Authority
- NZ
- New Zealand
- Prior art keywords
- originating
- retentate
- permeate
- whey
- module
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims abstract description 115
- 230000008569 process Effects 0.000 title claims abstract description 91
- 235000013336 milk Nutrition 0.000 title description 24
- 239000008267 milk Substances 0.000 title description 24
- 210000004080 milk Anatomy 0.000 title description 24
- 239000000203 mixture Substances 0.000 claims abstract description 304
- 239000012466 permeate Substances 0.000 claims abstract description 197
- 108010046377 Whey Proteins Proteins 0.000 claims abstract description 193
- 239000012465 retentate Substances 0.000 claims abstract description 191
- 239000007788 liquid Substances 0.000 claims abstract description 181
- 102000007544 Whey Proteins Human genes 0.000 claims abstract description 159
- 239000005862 Whey Substances 0.000 claims abstract description 136
- 239000012528 membrane Substances 0.000 claims abstract description 116
- 238000002156 mixing Methods 0.000 claims abstract description 106
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 104
- 235000020183 skimmed milk Nutrition 0.000 claims abstract description 88
- 235000018102 proteins Nutrition 0.000 claims abstract description 84
- 102000004169 proteins and genes Human genes 0.000 claims abstract description 84
- 108090000623 proteins and genes Proteins 0.000 claims abstract description 84
- 241001465754 Metazoa Species 0.000 claims abstract description 71
- 239000005018 casein Substances 0.000 claims abstract description 59
- BECPQYXYKAMYBN-UHFFFAOYSA-N casein, tech. Chemical compound NCCCCC(C(O)=O)N=C(O)C(CC(O)=O)N=C(O)C(CCC(O)=N)N=C(O)C(CC(C)C)N=C(O)C(CCC(O)=O)N=C(O)C(CC(O)=O)N=C(O)C(CCC(O)=O)N=C(O)C(C(C)O)N=C(O)C(CCC(O)=N)N=C(O)C(CCC(O)=N)N=C(O)C(CCC(O)=N)N=C(O)C(CCC(O)=O)N=C(O)C(CCC(O)=O)N=C(O)C(COP(O)(O)=O)N=C(O)C(CCC(O)=N)N=C(O)C(N)CC1=CC=CC=C1 BECPQYXYKAMYBN-UHFFFAOYSA-N 0.000 claims abstract description 59
- 235000021240 caseins Nutrition 0.000 claims abstract description 59
- 235000021119 whey protein Nutrition 0.000 claims abstract description 57
- 235000009508 confectionery Nutrition 0.000 claims abstract description 52
- 239000002253 acid Substances 0.000 claims abstract description 35
- 150000002500 ions Chemical class 0.000 claims description 272
- 238000001728 nano-filtration Methods 0.000 claims description 133
- GUBGYTABKSRVRQ-QKKXKWKRSA-N Lactose Natural products OC[C@H]1O[C@@H](O[C@H]2[C@H](O)[C@@H](O)C(O)O[C@@H]2CO)[C@H](O)[C@@H](O)[C@H]1O GUBGYTABKSRVRQ-QKKXKWKRSA-N 0.000 claims description 98
- 239000008101 lactose Substances 0.000 claims description 98
- 239000000047 product Substances 0.000 claims description 66
- 238000001035 drying Methods 0.000 claims description 56
- 239000000843 powder Substances 0.000 claims description 40
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 38
- 238000000909 electrodialysis Methods 0.000 claims description 36
- 235000016709 nutrition Nutrition 0.000 claims description 30
- 238000001556 precipitation Methods 0.000 claims description 28
- 150000003839 salts Chemical class 0.000 claims description 28
- 238000007599 discharging Methods 0.000 claims description 27
- 238000012545 processing Methods 0.000 claims description 21
- 238000001223 reverse osmosis Methods 0.000 claims description 19
- -1 based on dry weight Substances 0.000 claims description 7
- 230000035764 nutrition Effects 0.000 claims description 6
- 238000009928 pasteurization Methods 0.000 claims description 5
- 238000004659 sterilization and disinfection Methods 0.000 claims description 4
- 230000001954 sterilising effect Effects 0.000 claims description 3
- 239000007787 solid Substances 0.000 description 51
- 102000011632 Caseins Human genes 0.000 description 50
- 108010076119 Caseins Proteins 0.000 description 50
- 239000011734 sodium Substances 0.000 description 39
- 229910052500 inorganic mineral Inorganic materials 0.000 description 38
- 235000010755 mineral Nutrition 0.000 description 38
- 239000011707 mineral Substances 0.000 description 38
- 239000011575 calcium Substances 0.000 description 37
- 239000011777 magnesium Substances 0.000 description 34
- 239000002244 precipitate Substances 0.000 description 30
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 26
- 229910052708 sodium Inorganic materials 0.000 description 26
- 239000012141 concentrate Substances 0.000 description 25
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 24
- 229910052791 calcium Inorganic materials 0.000 description 24
- 235000008504 concentrate Nutrition 0.000 description 24
- 229910019142 PO4 Inorganic materials 0.000 description 22
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 22
- 239000010452 phosphate Substances 0.000 description 22
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 21
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 20
- 235000013350 formula milk Nutrition 0.000 description 20
- 239000011591 potassium Substances 0.000 description 20
- 229910052700 potassium Inorganic materials 0.000 description 20
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 19
- 235000021125 infant nutrition Nutrition 0.000 description 19
- 229910052749 magnesium Inorganic materials 0.000 description 19
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 18
- 239000004615 ingredient Substances 0.000 description 17
- 238000010438 heat treatment Methods 0.000 description 16
- 238000004519 manufacturing process Methods 0.000 description 15
- 238000005342 ion exchange Methods 0.000 description 14
- 238000001914 filtration Methods 0.000 description 12
- 239000012530 fluid Substances 0.000 description 12
- 230000001965 increasing effect Effects 0.000 description 11
- 239000000463 material Substances 0.000 description 11
- 241000283690 Bos taurus Species 0.000 description 10
- 235000013365 dairy product Nutrition 0.000 description 10
- 230000002829 reductive effect Effects 0.000 description 9
- 239000007858 starting material Substances 0.000 description 9
- 235000020244 animal milk Nutrition 0.000 description 8
- 238000001704 evaporation Methods 0.000 description 8
- 230000008020 evaporation Effects 0.000 description 8
- 238000002360 preparation method Methods 0.000 description 8
- 239000000243 solution Substances 0.000 description 8
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 6
- 238000005115 demineralization Methods 0.000 description 6
- 239000008247 solid mixture Substances 0.000 description 6
- 239000007921 spray Substances 0.000 description 6
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 5
- 239000001506 calcium phosphate Substances 0.000 description 5
- 229910000389 calcium phosphate Inorganic materials 0.000 description 5
- 235000011010 calcium phosphates Nutrition 0.000 description 5
- 235000013351 cheese Nutrition 0.000 description 5
- 235000020256 human milk Nutrition 0.000 description 5
- 210000004251 human milk Anatomy 0.000 description 5
- 239000011574 phosphorus Substances 0.000 description 5
- 229910052698 phosphorus Inorganic materials 0.000 description 5
- QORWJWZARLRLPR-UHFFFAOYSA-H tricalcium bis(phosphate) Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O QORWJWZARLRLPR-UHFFFAOYSA-H 0.000 description 5
- 235000013343 vitamin Nutrition 0.000 description 5
- 229930003231 vitamin Natural products 0.000 description 5
- 239000011782 vitamin Substances 0.000 description 5
- 229940088594 vitamin Drugs 0.000 description 5
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 4
- 239000001110 calcium chloride Substances 0.000 description 4
- 229910001628 calcium chloride Inorganic materials 0.000 description 4
- 238000011026 diafiltration Methods 0.000 description 4
- 238000010790 dilution Methods 0.000 description 4
- 239000012895 dilution Substances 0.000 description 4
- 238000009826 distribution Methods 0.000 description 4
- 230000004907 flux Effects 0.000 description 4
- 238000009472 formulation Methods 0.000 description 4
- 230000036961 partial effect Effects 0.000 description 4
- 230000002441 reversible effect Effects 0.000 description 4
- 230000009469 supplementation Effects 0.000 description 4
- 102000014171 Milk Proteins Human genes 0.000 description 3
- 108010011756 Milk Proteins Proteins 0.000 description 3
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- 238000010793 Steam injection (oil industry) Methods 0.000 description 3
- 230000001580 bacterial effect Effects 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 3
- 239000000920 calcium hydroxide Substances 0.000 description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 3
- 239000000919 ceramic Substances 0.000 description 3
- 239000000470 constituent Substances 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 150000002632 lipids Chemical class 0.000 description 3
- 235000021239 milk protein Nutrition 0.000 description 3
- 235000015097 nutrients Nutrition 0.000 description 3
- 235000013406 prebiotics Nutrition 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 239000011347 resin Substances 0.000 description 3
- 229920005989 resin Polymers 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 229910001415 sodium ion Inorganic materials 0.000 description 3
- 238000001694 spray drying Methods 0.000 description 3
- YBJHBAHKTGYVGT-ZKWXMUAHSA-N (+)-Biotin Chemical compound N1C(=O)N[C@@H]2[C@H](CCCCC(=O)O)SC[C@@H]21 YBJHBAHKTGYVGT-ZKWXMUAHSA-N 0.000 description 2
- GHOKWGTUZJEAQD-ZETCQYMHSA-N (D)-(+)-Pantothenic acid Chemical compound OCC(C)(C)[C@@H](O)C(=O)NCCC(O)=O GHOKWGTUZJEAQD-ZETCQYMHSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 108091003079 Bovine Serum Albumin Proteins 0.000 description 2
- 102000004407 Lactalbumin Human genes 0.000 description 2
- 108090000942 Lactalbumin Proteins 0.000 description 2
- 108010063045 Lactoferrin Proteins 0.000 description 2
- 102000010445 Lactoferrin Human genes 0.000 description 2
- 102000008192 Lactoglobulins Human genes 0.000 description 2
- 108010060630 Lactoglobulins Proteins 0.000 description 2
- 108010023244 Lactoperoxidase Proteins 0.000 description 2
- 102000045576 Lactoperoxidases Human genes 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 125000000129 anionic group Chemical group 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 229940098773 bovine serum albumin Drugs 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 159000000007 calcium salts Chemical class 0.000 description 2
- 150000001720 carbohydrates Chemical class 0.000 description 2
- 235000014633 carbohydrates Nutrition 0.000 description 2
- 229940071162 caseinate Drugs 0.000 description 2
- 125000002091 cationic group Chemical group 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000002255 enzymatic effect Effects 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- OVBPIULPVIDEAO-LBPRGKRZSA-N folic acid Chemical compound C=1N=C2NC(N)=NC(=O)C2=NC=1CNC1=CC=C(C(=O)N[C@@H](CCC(O)=O)C(O)=O)C=C1 OVBPIULPVIDEAO-LBPRGKRZSA-N 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 238000005304 joining Methods 0.000 description 2
- CSSYQJWUGATIHM-IKGCZBKSSA-N l-phenylalanyl-l-lysyl-l-cysteinyl-l-arginyl-l-arginyl-l-tryptophyl-l-glutaminyl-l-tryptophyl-l-arginyl-l-methionyl-l-lysyl-l-lysyl-l-leucylglycyl-l-alanyl-l-prolyl-l-seryl-l-isoleucyl-l-threonyl-l-cysteinyl-l-valyl-l-arginyl-l-arginyl-l-alanyl-l-phenylal Chemical compound C([C@H](N)C(=O)N[C@@H](CCCCN)C(=O)N[C@@H](CS)C(=O)N[C@@H](CCCNC(N)=N)C(=O)N[C@@H](CCCNC(N)=N)C(=O)N[C@@H](CC=1C2=CC=CC=C2NC=1)C(=O)N[C@@H](CCC(N)=O)C(=O)N[C@@H](CC=1C2=CC=CC=C2NC=1)C(=O)N[C@@H](CCCNC(N)=N)C(=O)N[C@@H](CCSC)C(=O)N[C@@H](CCCCN)C(=O)N[C@@H](CCCCN)C(=O)N[C@@H](CC(C)C)C(=O)NCC(=O)N[C@@H](C)C(=O)N1CCC[C@H]1C(=O)N[C@@H](CO)C(=O)N[C@@H]([C@@H](C)CC)C(=O)N[C@@H]([C@@H](C)O)C(=O)N[C@@H](CS)C(=O)N[C@@H](C(C)C)C(=O)N[C@@H](CCCNC(N)=N)C(=O)N[C@@H](CCCNC(N)=N)C(=O)N[C@@H](C)C(=O)N[C@@H](CC=1C=CC=CC=1)C(O)=O)C1=CC=CC=C1 CSSYQJWUGATIHM-IKGCZBKSSA-N 0.000 description 2
- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 description 2
- 235000021242 lactoferrin Nutrition 0.000 description 2
- 229940078795 lactoferrin Drugs 0.000 description 2
- 229940057428 lactoperoxidase Drugs 0.000 description 2
- 235000014666 liquid concentrate Nutrition 0.000 description 2
- 238000005374 membrane filtration Methods 0.000 description 2
- 238000001471 micro-filtration Methods 0.000 description 2
- 230000007935 neutral effect Effects 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 238000010979 pH adjustment Methods 0.000 description 2
- 238000002203 pretreatment Methods 0.000 description 2
- LXNHXLLTXMVWPM-UHFFFAOYSA-N pyridoxine Chemical compound CC1=NC=C(CO)C(CO)=C1O LXNHXLLTXMVWPM-UHFFFAOYSA-N 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 235000020209 toddler milk formula Nutrition 0.000 description 2
- NLZUEZXRPGMBCV-UHFFFAOYSA-N Butylhydroxytoluene Chemical compound CC1=CC(C(C)(C)C)=C(O)C(C(C)(C)C)=C1 NLZUEZXRPGMBCV-UHFFFAOYSA-N 0.000 description 1
- GHOKWGTUZJEAQD-UHFFFAOYSA-N Chick antidermatitis factor Natural products OCC(C)(C)C(O)C(=O)NCCC(O)=O GHOKWGTUZJEAQD-UHFFFAOYSA-N 0.000 description 1
- KRKNYBCHXYNGOX-UHFFFAOYSA-K Citrate Chemical compound [O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O KRKNYBCHXYNGOX-UHFFFAOYSA-K 0.000 description 1
- RFSUNEUAIZKAJO-ARQDHWQXSA-N Fructose Chemical class OC[C@H]1O[C@](O)(CO)[C@@H](O)[C@@H]1O RFSUNEUAIZKAJO-ARQDHWQXSA-N 0.000 description 1
- 102000006395 Globulins Human genes 0.000 description 1
- 108010044091 Globulins Proteins 0.000 description 1
- 108060003951 Immunoglobulin Proteins 0.000 description 1
- 239000005913 Maltodextrin Substances 0.000 description 1
- 229920002774 Maltodextrin Polymers 0.000 description 1
- 235000013382 Morus laevigata Nutrition 0.000 description 1
- 244000278455 Morus laevigata Species 0.000 description 1
- OVBPIULPVIDEAO-UHFFFAOYSA-N N-Pteroyl-L-glutaminsaeure Natural products C=1N=C2NC(N)=NC(=O)C2=NC=1CNC1=CC=C(C(=O)NC(CCC(O)=O)C(O)=O)C=C1 OVBPIULPVIDEAO-UHFFFAOYSA-N 0.000 description 1
- 101100070542 Podospora anserina het-s gene Proteins 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 229930003451 Vitamin B1 Natural products 0.000 description 1
- 239000003957 anion exchange resin Substances 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 229960002685 biotin Drugs 0.000 description 1
- 235000020958 biotin Nutrition 0.000 description 1
- 239000011616 biotin Substances 0.000 description 1
- FNAQSUUGMSOBHW-UHFFFAOYSA-H calcium citrate Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O.[O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O FNAQSUUGMSOBHW-UHFFFAOYSA-H 0.000 description 1
- 239000001354 calcium citrate Substances 0.000 description 1
- 239000003729 cation exchange resin Substances 0.000 description 1
- 229940023913 cation exchange resins Drugs 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 229960001231 choline Drugs 0.000 description 1
- OEYIOHPDSNJKLS-UHFFFAOYSA-N choline Chemical compound C[N+](C)(C)CCO OEYIOHPDSNJKLS-UHFFFAOYSA-N 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 235000020247 cow milk Nutrition 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000010908 decantation Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000002542 deteriorative effect Effects 0.000 description 1
- 235000013325 dietary fiber Nutrition 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000002036 drum drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000011552 falling film Substances 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 229960000304 folic acid Drugs 0.000 description 1
- 235000019152 folic acid Nutrition 0.000 description 1
- 239000011724 folic acid Substances 0.000 description 1
- 238000004108 freeze drying Methods 0.000 description 1
- 239000013529 heat transfer fluid Substances 0.000 description 1
- 238000004128 high performance liquid chromatography Methods 0.000 description 1
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 description 1
- 102000018358 immunoglobulin Human genes 0.000 description 1
- 229940072221 immunoglobulins Drugs 0.000 description 1
- 239000013072 incoming material Substances 0.000 description 1
- 238000001802 infusion Methods 0.000 description 1
- 239000003014 ion exchange membrane Substances 0.000 description 1
- 239000004310 lactic acid Substances 0.000 description 1
- 235000014655 lactic acid Nutrition 0.000 description 1
- 150000002597 lactoses Chemical class 0.000 description 1
- 229940035034 maltodextrin Drugs 0.000 description 1
- 229910000000 metal hydroxide Inorganic materials 0.000 description 1
- 150000004692 metal hydroxides Chemical class 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 235000019198 oils Nutrition 0.000 description 1
- 229920001542 oligosaccharide Polymers 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 229940055726 pantothenic acid Drugs 0.000 description 1
- 235000019161 pantothenic acid Nutrition 0.000 description 1
- 239000011713 pantothenic acid Substances 0.000 description 1
- 238000000247 postprecipitation Methods 0.000 description 1
- 239000006041 probiotic Substances 0.000 description 1
- 235000018291 probiotics Nutrition 0.000 description 1
- 102000004196 processed proteins & peptides Human genes 0.000 description 1
- 108090000765 processed proteins & peptides Proteins 0.000 description 1
- RADKZDMFGJYCBB-UHFFFAOYSA-N pyridoxal hydrochloride Natural products CC1=NC=C(CO)C(C=O)=C1O RADKZDMFGJYCBB-UHFFFAOYSA-N 0.000 description 1
- 238000011110 re-filtration Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229940108461 rennet Drugs 0.000 description 1
- 108010058314 rennet Proteins 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 230000001932 seasonal effect Effects 0.000 description 1
- 210000002966 serum Anatomy 0.000 description 1
- KISFEBPWFCGRGN-UHFFFAOYSA-M sodium;2-(2,4-dichlorophenoxy)ethyl sulfate Chemical compound [Na+].[O-]S(=O)(=O)OCCOC1=CC=C(Cl)C=C1Cl KISFEBPWFCGRGN-UHFFFAOYSA-M 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 229960003495 thiamine Drugs 0.000 description 1
- DPJRMOMPQZCRJU-UHFFFAOYSA-M thiamine hydrochloride Chemical compound Cl.[Cl-].CC1=C(CCO)SC=[N+]1CC1=CN=C(C)N=C1N DPJRMOMPQZCRJU-UHFFFAOYSA-M 0.000 description 1
- 239000011573 trace mineral Substances 0.000 description 1
- 235000013619 trace mineral Nutrition 0.000 description 1
- 235000013337 tricalcium citrate Nutrition 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
- 235000010374 vitamin B1 Nutrition 0.000 description 1
- 239000011691 vitamin B1 Substances 0.000 description 1
- 239000011726 vitamin B6 Substances 0.000 description 1
- 235000019158 vitamin B6 Nutrition 0.000 description 1
- 229940011671 vitamin b6 Drugs 0.000 description 1
- 150000003722 vitamin derivatives Chemical class 0.000 description 1
- 239000003039 volatile agent Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 235000021241 α-lactalbumin Nutrition 0.000 description 1
Classifications
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; MAKING THEREOF
- A23C2210/00—Physical treatment of dairy products
- A23C2210/25—Separating and blending
- A23C2210/252—Separating a milk product in at least two fractions followed by treatment of at least one of the fractions and remixing at least part of the two fractions
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; MAKING THEREOF
- A23C9/00—Milk preparations; Milk powder or milk powder preparations
- A23C9/14—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment
- A23C9/142—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by dialysis, reverse osmosis or ultrafiltration
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; MAKING THEREOF
- A23C9/00—Milk preparations; Milk powder or milk powder preparations
- A23C9/14—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment
- A23C9/142—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by dialysis, reverse osmosis or ultrafiltration
- A23C9/1422—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by dialysis, reverse osmosis or ultrafiltration by ultrafiltration, microfiltration or diafiltration of milk, e.g. for separating protein and lactose; Treatment of the UF permeate
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; MAKING THEREOF
- A23C9/00—Milk preparations; Milk powder or milk powder preparations
- A23C9/14—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment
- A23C9/142—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by dialysis, reverse osmosis or ultrafiltration
- A23C9/1425—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by dialysis, reverse osmosis or ultrafiltration by ultrafiltration, microfiltration or diafiltration of whey, e.g. treatment of the UF permeate
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; MAKING THEREOF
- A23C9/00—Milk preparations; Milk powder or milk powder preparations
- A23C9/15—Reconstituted or recombined milk products containing neither non-milk fat nor non-milk proteins
- A23C9/1512—Reconstituted or recombined milk products containing neither non-milk fat nor non-milk proteins containing isolated milk or whey proteins, caseinates or cheese; Enrichment of milk products with milk proteins in isolated or concentrated form, e.g. ultrafiltration retentate
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
- A23L33/00—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof
- A23L33/10—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof using additives
- A23L33/17—Amino acids, peptides or proteins
- A23L33/19—Dairy proteins
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
- A23L33/00—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof
- A23L33/40—Complete food formulations for specific consumer groups or specific purposes, e.g. infant formula
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
- A23V2002/00—Food compositions, function of food ingredients or processes for food or foodstuffs
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/06—Specific process operations in the permeate stream
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/08—Specific process operations in the concentrate stream
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/10—Temperature control
- B01D2311/103—Heating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2623—Ion-Exchange
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2642—Aggregation, sedimentation, flocculation, precipitation or coagulation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2692—Sterilization
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2317/00—Membrane module arrangements within a plant or an apparatus
- B01D2317/04—Elements in parallel
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/027—Nanofiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
-
- B01D61/142—
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/58—Multistep processes
Abstract
The invention relates to a process for treating animal skim milk and sweet whey and/or acid whey, comprising: (a) ultrafiltration (UF1) of a first liquid composition comprising animal skim milk with 70 -90 wt% casein and 10 -30 wt% whey proteins, based on total protein, over a first ultrafiltration membrane having a molecular weight cut-off of 2.5 -25 kDa using a volume concentration factor of 1.5 -6 to obtain a retentate (UFR1) and a permeate (UFP1); (b) ultrafiltration (UF2) of a second liquid composition comprising sweet whey and/or acid whey over a second ultrafiltration membrane having a molecular weight cut-off of 2.5 -25 kDa using a volume concentration factor of 2 -15 to obtain a retentate (UFR2) and a permeate (UFP2); and (c) mixing the UF retentate originating from step (a) with the UF retentate originating from step (b) to obtain a mixture of UF retentates. membrane having a molecular weight cut-off of 2.5 -25 kDa using a volume concentration factor of 1.5 -6 to obtain a retentate (UFR1) and a permeate (UFP1); (b) ultrafiltration (UF2) of a second liquid composition comprising sweet whey and/or acid whey over a second ultrafiltration membrane having a molecular weight cut-off of 2.5 -25 kDa using a volume concentration factor of 2 -15 to obtain a retentate (UFR2) and a permeate (UFP2); and (c) mixing the UF retentate originating from step (a) with the UF retentate originating from step (b) to obtain a mixture of UF retentates.
Description
WO 63494
Process and system for preparing dry milk formulae
FIELD OF THE ION
The present invention relates to an advanced process for the cture of dairy products,
ably for the manufacture of dry milk formulae such as infant milk formulae and other
nutritional products for infants, as well as to intermediary products able by said
process, uses of said intermediary products and a system for implementing said process.
OUND OF THE INVENTION
Human milk is considered the ‘golden standard’ for infant nutrition. Processing animal milk,
for example cows’ milk, to more resemble the composition of human milk is known in the
art. Such processing is known in the art as ‘humanizing’ animal milk. The process of
humanizing animal milk involves changing the ratio of casein:whey ns as found in
animal milk (e.g. approximately 80:20 for cow’s milk) to the desired ratio for infant
nutrition, as found in human milk (preferably n 75:25 and 30:70). In addition, the
mineral t of animal milk is typically higher that the content found in human milk.
Thus humanization of animal milk requires the reduction of the mineral content.
Preparation of products suitable for use in infant nutrition typically involves blending of
various individually purified components in the appropriate ratios, either wet or dry. Current
manufacturing processes require multiple dairy ingredients from intermediate suppliers,
including skim milk or a concentrate f (including skim milk powder), ralised
whey or a concentrate thereof (including demineralised whey powder), whey protein
concentrates or isolates (normally as powders), and pure grade lactose (typically in powder
form) to formulate a nutritionally balanced infant formula.
WO 96/08155 describes a process for treating skim milk for the manufacture of cheese and
milk powders, wherein whey proteins are removed from skim milk by microfiltration and
further treatment includes ultraflltration.
US 5,503,865 discloses a process for treating skim milk, comprising microfiltration or
ultraflltration. The permeate thereof may be demineralised by for example ion exchange
and/or electrodialysis in order to make it le to be used in baby products.
US 4497836 discloses a process wherein whey is ted to ultraflltration, and the
te thereof is subjected to electrodialysis or ion exchange.
discloses a process wherein milk serum is subjected to lltration, and
the permeate thereof is subjected to diaflltration. The ultraflltration retentate is combined
with the diaflltration retentate in the production of infant milk formulae, by mixing the
combined product with milk powder.
EP 8 describes a process wherein animal milk is subjected to microflltration through
a membrane having a porosity of 0.1 — 0.2 micrometer, after which the ltration
permeate sing whey proteins is demineralised by electrodialysis. The mineral content
of the electrodialyzed microflltration permeate is very low, and subsequent fortification with
ls and trace elements is required to obtain an infant formula.
SUlVflVIARY OF THE INVENTION
The inventors have designed an improved method for the production of dairy ts, in
particular for the production of dry (milk) powders, preferably dry (milk) powders for use in
nutritional infant formulations, in which process more optimal use is made of filtration and
2O separation technologies. In this s, a first liquid composition comprising 70 — 90 wt%
casein and 10 — 30 wt% whey proteins, based on total protein, preferably animal skim milk,
and a second liquid composition sing sweet whey and/or acid whey are first subjected
to separation by ultrafiltration, thereby reducing the need for (significant) polyvalent and/or
monovalent ion removal from the casein and/or whey protein containing liquid
compositions. The present invention thus preferably relates to a process for treating animal
skim milk and whey, comprising the steps of ultraflltrating animal skim milk and
ultraflltrating whey, preferably combined with softening and removal of monovalent ions of
the lactose enriched ultraflltration permeate streams and ing the obtained permeate
and retentate streams.
t day manufacturers of dry powder (infant) nutritional compositions largely rely on
supply and use of highly purified ingredients, such as purif1ed lactose, demineralized whey
proteins and casein proteins to produce said itions by mixing said ingredients. The
2014/050203
present inventors have designed a process of treating animal skim milk and whey for
cturing a dry (milk) powder that y circumvents buying such high-grade, pure
ingredients from third parties. The advantages of the present process of the ion over
such ng methods of producing dry (milk) powders are numerous; e.g. the loss in
lactose during the processing of skim milk and whey is d, complications related to
fouling of membranes are reduced, the use of (externally added) chemicals is reduced and
waste water is recycled in the process to a large extent and thus overall the process has a
lower environmental impact. More in particular, whereas lactose yield in conventional
purification methods for the production of nutritional powders lies around 83-85%, yield can
be improved to over 90% in the process of the present invention.
More in particular, the present invention relates to a process for treating animal skim milk
and whey, ably for the manufacture of a dry powder, such as a dry powder that can be
further sed into an infant milk formula and other nutritional products for infants. The
present process involves ultraflltration of animal skim milk and ultraflltration of whey
followed by mixing of the ultraflltration retentates, which are enriched in milk proteins and
whey proteins respectively. Adding whey to animal skim milk alters the n ition
of the skim milk, allowing the humanizing of skim milk to more le the protein
composition of human milk. Both animal skim milk and whey typically contain too high
levels of polyvalent ions, the content of which needs to be reduced in order to make the
animal skim milk a suitable source of nutrients that can be used for feeding human s.
The process according to the present invention employs ultraflltration for the removal of
said polyvalent ions from animal skim milk and whey. As such, neither the animal skim
milk nor whey need to be softened to the extent which is ordinarily done in the art. The
process according to the invention circumvents the need for using (significantly) softened
and/or demineralized whey proteins for the manufacture of dry powder formulations that are
suitable for infant nutrition preparation, by ultrafiltration of animal skim milk and whey. In
an especially preferred ment, the lactose that is removed from both the skim milk and
whey as lltration permeate is softened or even demineralized, meaning the amounts of
polyvalent ions and monovalent ions is reduced compared to the incoming material, after
which the permeate is used to supplement the resulting dry powder formulations, by adding
the demineralized lactose to either before, during or after mixing of the ultraflltration
retentates. As such, the mineral content of the resulting formulae is sufficiently low to
enable infant nutrition preparation according to regulatory bodies (e.g. EU directive
/EEC or EU directive 2006/141/EC, US Food and Drug Administration 21 CFR Ch 1
part 107).
More in particular, the present ion relates to a process for treating animal skim milk
and sweet whey and/or acid whey, comprising:
(a) ultraflltration (UFl) of a first liquid composition sing animal skim milk with
70 — 90 wt% casein and 10 — 30 wt% whey proteins, based on total n, over a first
ultraflltration membrane having a molecular weight cut-off of 2.5 — 25 kDa using a volume
concentration factor of 1.5 — 6 to obtain a retentate (UFRl) and a permeate (UFPl),
(b) ultraflltration (UF2) of a second liquid ition comprising sweet whey and/or
acid whey over a second ultraflltration membrane having a molecular weight cut-off of 2.5 —
kDa using a volume concentration factor of 2 — 15 to obtain a retentate (UFR2) and a
permeate , and
(c) mixing the UF retentate originating from step (a) with the UF retentate originating
from step (b) to obtain a mixture of UF retentates.
In alternative wording, the present invention relates to a process for treating animal skim
2O milk and sweet whey and/or acid whey, comprising:
(a) ultraflltration (UFl) of a first liquid composition comprising animal skim milk with
70 — 90 wt% casein and 10 — 30 wt% whey proteins, based on total protein, over a first
ultraflltration membrane having a molecular weight cut-off of 2.5 — 25 kDa to obtain a
retentate (UFRl) comprising 35 — 65 wt% proteins and 20 — 50 wt% lactose, based on dry
weight, and a permeate (UFPl) sing 0 — 5 wt% proteins and 70 — 98 wt% lactose,
based on dry weight,
(b) lltration (UF2) of a second liquid composition comprising sweet whey and/or
acid whey over a second lltration membrane having a molecular weight cut-off of 2.5 —
kDa to obtain a retentate (UFR2) comprising 15 — 55 wt% proteins and 35 — 65 wt%
lactose, based on dry weight, and a permeate (UFP2) comprising 0 — 5 wt% proteins and 70
— 98 wt% lactose, based on dry weight, and
(c) mixing the UF retentate originating from step (a) with the UF retentate originating
from step (b) to obtain a mixture of UF retentates.
In a preferred embodiment, the process of the invention further comprises:
(d) removing polyvalent ions from the UP permeate originating from step (a), and/or
from the UP permeate originating from step (b) or from a mixture of the UP permeates
originating from step (a) and (b), to obtain a softened UF permeate, and
(e) mixing a softened UF permeate from (d) with a UF ate originating from step (a)
and/or the UP retentate originating from step (b) or the mixture of UP retentates originating
from step (c), preferably the mixture of UP retentates originating from step (c). Preferably,
the UP permeate is ed by one polyvalent ion removal step, wherein calcium,
ium and ate are removed, ably to a icant extent. lent ion
removal preferably takes place by a combination of nanof11tration, salt itation,
ultraf11tration and electrodialysis, most preferably following the sequence of nanof11tration,
salt precipitation, ultraf11tration and electrodialysis.
In a preferred embodiment, the UP permeate originating from step (a) and the UP permeate
originating from step (b) are ed or mixed in a volume ratio of between 10:1 and 1:20,
preferably 5:1 and 1:15, more preferably 1:1 and 1:10, most preferably 1:2 and 1:6. Said
combining or mixing can take place before or after softening, but preferably before
softening.
In a preferred embodiment, mixing in step (c) involves mixing UFRl and UFR2 in a volume
ratio of between 20:1 and 1:20, preferably 10:1 and 1:10, more preferably 6:1 and 1:6, most
preferably 3:1 and 1:3 or wherein the concentrated UFRl (from step j1)) is combined or
mixed with the concentrated UFR2 (from step (jl)) in a volume ratio of between 20:1 and
1:20, preferably 10:1 and 1:10, more preferably 6:1 and 1:6, most preferably 3:1 and 1:3.
In a red embodiment, the process of the invention further comprises:
(f) ng monovalent ions from at least one of the softened UF permeates of step
(d), preferably before mixing in step (e). ably, the softened UF permeate is subjected
to at most one or at most two monovalent ion removal steps, wherein sodium, chloride and
potassium are removed, preferably to a significant extent. Preferably, all of the softened UF
permeates of (d) are subjected to monovalent ion removal. Most preferably, the UP
permeates of step (a) and (b) are first mixed into a single UF te composition which is
subsequently softened and subjected to lent ion removal.
In a preferred ment, the process of the invention further ses:
(g) subjecting at least one of the softened UF permeates of (d) to a concentration step,
ably by reverse osmosis and/or nanoflltration, preferably prior to mixing in step (e).
Preferably, the UF permeates are subjected to at most one or at most two concentration
steps.
In a preferred embodiment, l of polyvalent ions is accomplished by electrodialysis,
ion exchange and/or salt precipitation, and removal of monovalent ions is lished by
nanoflltration or diaflltration. More preferably, polyvalent ion removal preferably takes
place by a combination of nanoflltration, salt precipitation, ultraflltration and electrodialysis,
most preferably following the sequence of nanoflltration, salt precipitation, ultraflltration
and electrodialysis.
In a preferred embodiment, the process of the invention further comprises:
(h) drying of the UF retentate originating from step (a), the UF retentate originating from
step (b) or the mixture of UP retentates originating from step (c), preferably after mixing
with the ed UF te in step (a), to obtain a dry powder. Preferably, the UP
retentate originating from step (a) and/or (b) or (c) is subjected to a concentration step and/or
monovalent ion removal step prior to drying. This drying is step is preferably performed
after mixing with the softened UFPl permeate, which may be ted to a monovalent ion
removal step, the softened UFP2 permeate, which may be subjected to a lent ion
removal step, or the softened UFPl/UFP2 combined permeate, which may be subjected to a
monovalent ion removal step, to obtain a dry powder. In a preferred embodiment, the drying
of step h) takes place after mixing step (e).
In a preferred embodiment, the drying takes place after mixing step (c).More preferably,
drying involves drying of a softened UF permeate composition originating from steps (a)
and (b) which is mixed with a UF retentate originating from (c) which UF retentate is
ted to monovalent ion removal and/or a concentration step. Most preferably, the UP
retentate is subjected to monovalent ion removal and/or a concentration step prior to mixing
them together, followed by mixing with the softened UF permeate ition which
originates from steps (a) and (b).
In a preferred embodiment, the process of the invention further comprises:
(i) a terilization or rization step of the mixture of UP retentates originating
from step (c), preferably after step (e) and prior to step (h). ably, said heat-sterilization
comprises a -steam injection (DSI) step.
In a preferred embodiment, the process of the invention further comprises:
(jl) monovalent ion removal and/or concentrating of the UP retentate originating from
step (a) and/or the UP retentate originating from step (b), prior to step (c), (e) or (h),
preferably by reverse osmosis and/or nanoflltration, or
(jZ) monovalent ion removal and/or concentrating of the mixture of UP retentates
originating from step (c) prior to step (h), preferably by reverse s and/or
nanoflltration. Preferably, at least one or preferably all of the UP retentates of step (jl) or
(jZ) are subjected to at most one or at most two monovalent ion and/or concentration steps.
In a preferred embodiment, the mixture of UP retentates originating from step (c) is further
processed into a nutritional product for providing nutrition to s. In another preferred
embodiment, further ingredients are added prior to, after or during step (c) or added prior to,
after or during step (e), added prior to, after or during drying step (h). Such further
ingredients preferably se (suitable amounts of) oils, vitamins, minerals, carbohydrates
(such as lactose or maltodextrin where required), dietary fibers (such as o-
oligosaccharides and/or fructo-oligosaccharides).
In a preferred embodiment, such an amount of the UP retentate originating from step (b) is
mixed in step (c) with the UP retentate originating from step (b), that the mixture of UP
retentates originating from step (c) is characterized by a casein to whey protein weight ratio
between 75:25 and 30:70. Preferably this ratio lies between 70 to 30 and 36 to 64, more
preferably between 65 to 35 and 45 to 55.
In a preferred embodiment, water which originates from a concentration step, preferably
reverse s and/or nanoflltration, performed on the UP retentate originating from step
(a), the UF retentate originating from step (b), the mixture of UP ates originating from
step c), or from the UF te originating from step (a) and/or from the UF permeate
originating from step (b) or the softened UF permeate, is added to the first liquid
composition and/or the second liquid composition. Such a feed back of water usage
stemming from a concentration step reduces the need for addition of external water supplies.
Such water obtained from a concentration step can for example be used to reconstitute
animal skim milk and/or whey powder into liquid compositions that can subsequently be
ted to ultraflltration according to the invention.
In a preferred embodiment, the second liquid composition of step (b) ses at least 50
wt% sweet whey of the total whey, on total weight basis, preferably at least 60 wt%, more
preferably at least 70 wt% or 80 wt%, most preferably at least 90 wt%.
In a preferred embodiment, the invention s to a process for ng animal skim milk
and animal whey, for the manufacture of dairy products, preferably dry formulae, more
preferably dry infant milk powders and other nutritional products for s.
In a preferred embodiment, the process according to the invention ably operates with
500 — 2500 kg, more preferably 800 — 1800 kg, most preferably 1000 — 1400 kg dry matter
of the first liquid composition, preferably of animal skim milk, incoming per hour. The
process according to the invention preferably operates with 1500 — 5000 kg, more preferably
2200 — 4000 kg, most preferably 2600 — 3000 kg dry matter of the second liquid
composition, preferably of animal whey, ng per hour. The process according to the
invention preferably operates with 750 — 4000 kg, more preferably 1000 — 3000 kg, most
preferably 1500 — 2000 kg UF retentate obtained per hour from the ultraflltration of both
incoming streams combined. The process according to the invention preferably operates
with 1000 — 5000 kg, more preferably 1500 — 4000 kg, most preferably 2000 — 2500 kg UF
te obtained per hour from the ultraflltration of both incoming streams combined.
ED DESCRIPTION OF THE INVENTION
Process according to the present invention
The present invention relates to a process for treating animal skim milk and sweet whey
and/or acid whey, comprising:
(a) ultrafiltration (UFl) of a first liquid composition comprising animal skim milk with
70 — 90 wt% casein and 10 — 30 wt% whey proteins, based on total protein, over a first
ultrafiltration membrane having a molecular weight cut-off of 2.5 — 25 kDa using a volume
concentration factor of 1.5 — 6 to obtain a retentate (UFRl) and a permeate ,
(b) ultrafiltration (UF2) of a second liquid composition comprising sweet whey and/or
acid whey over a second ultrafiltration membrane having a molecular weight cut-off of 2.5 —
kDa using a volume concentration factor of 2 — 15 to obtain a retentate (UFR2) and a
permeate (UFP2), and
(c) mixing the UF retentate originating from step (a) with the UF retentate ating
from step (b) to obtain a mixture of UF retentates.
In alternative wording, the present invention relates to a process for treating animal skim
milk and sweet whey and/or acid whey, comprising:
(a) ltration (UFl) of a first liquid composition comprising animal skim milk with
2O 70 — 90 wt% casein and 10 — 30 wt% whey proteins, based on total protein, over a first
ultrafiltration membrane having a molecular weight cut-off of 2.5 — 25 kDa to obtain a
retentate (UFRl) comprising 35 — 65 wt% proteins and 20 — 50 wt% lactose, based on dry
weight, and a te (UFPl) comprising 0 — 5 wt% proteins and 70 — 98 wt% lactose,
based on dry weight,
(b) ultrafiltration (UF2) of a second liquid composition comprising sweet whey and/or
acid whey over a second ultrafiltration ne having a molecular weight cut-off of 2.5 —
kDa to obtain a retentate (UFR2) comprising 15 — 55 wt% proteins and 35 — 65 wt%
lactose, based on dry weight, and a permeate (UFP2) sing 0 — 5 wt% proteins and 70
— 98 wt% lactose, based on dry , and
(c) mixing the UF retentate originating from step (a) with the UF ate originating
from step (b) to obtain a mixture ofUF retentates.
The process according to the ion uses at least two sources of protein; the first is a
liquid composition comprising animal skim milk with 70 — 90 wt% casein and 10 — 30 wt%
whey proteins, based on total protein. Preferably, the first liquid ition comprises or is
animal skim milk with a 80:20 casein to whey protein content ratio. ably, the second
liquid composition comprises or is sweet whey and/or acid whey. More ably the
second liquid composition comprises or is sweet whey.
In the process according to the invention, the first liquid composition and the second liquid
composition are each subjected to ultrafiltration (UF, steps (a) and (b)) to obtain two UF
retentates (UFRl and UFR2) and two UF permeates (UFPl and UFPZ). In a preferred
embodiment, any of the first liquid composition, the second liquid composition and the
mixture of UF retentates originating from UF of the first and second liquid compositions
may be subjected to various processing steps before the final diary product is obtained.
In a preferred embodiment, the UFPl permeate originating from step (a) is first mixed with
the UFP2 permeate originating from step (b) (for example by collection in a single
collection/storage tank) before removal of polyvalent ions in step (d) takes place. The
softened FP2 combined permeate (i.e. the mixed UFPl/UFP2 permeate that
originate from the UFl/UF2 step which contains reduced polyvalent ions levels) is
subsequently mixed with the UFRl retentate that originates from UFl, the UFR2 retentate
that originates from UF2, or preferably with the mixture of UP retentates of step (c). In a
more preferred option, the UFRl retentate that originates from (a), the UFR2 retentate that
originates from (b), or preferably the mixture of UP retentates of step (c) is first subjected to
a tration step, preferably by reverse osmosis or nanofiltration, after which these more
concentrated liquid itions is/are ed with the softened UFPl/UFP2 combined
permeate. An advantage of first mixing the UFPl permeate that originates from UFl with
the UFP2 permeate that originates from UF2 is that polyvalent ions are removed from a
single liquid composition (1’. e. the UFPl/UFP2 permeate mixture) instead of that removing
polyvalent ions involves removal from two separate liquid itions.
In yet another preferred embodiment, the s of the invention ses step (jl) or (jZ).
, preferably the UF retentate originating from step (a) and/or the UF retentate
originating from step (b) is/are subjected to a monovalent ion removal and/or concentrating
step, prior to step (c), (e) or (h), preferably by reverse osmosis and/or nanoflltration.
Preferably, said UF retentates are separately subjected o. Alternatively, the mixture of
UP retentates originating from step (c) is subjected to monovalent ion removal and/or
concentration thereof, prior to step (h), preferably by reverse osmosis and/or ltration.
Preferably, at least one or both of the UP retentates of step (a) and (b) or the UP retentate of
step (c) is/are subjected to at most one or at most two monovalent ion and/or concentration
steps.
In another red embodiment, the UFRl retentate originating from UFl is enriched in
casein and whey proteins, the UFRZ retentate originating from UF2 is enriched in whey
proteins, the mixture ofUP retentates of step (c) is enriched in casein and whey protein, the
UFPl and UFP2 permeates originating from UFl and UF2, respectively, are enriched in
lactose. Furthermore, the mixture of UP retentates of step (c) is characterized by a casein to
whey protein ratio that is shifted from the 80:20 weight ratio as observed in cows’ skim milk
s higher whey protein levels. Preferably, the casein n to whey protein weight
ratio thereof lies between 75 to 35 and 30 to 70.
The process according to the invention provides sufficient l of polyvalent ions and
preferably monovalent ions, by virtue of the ultraflltration of step (a) and (b) and optionally
the softening of step (d), so that all minerals are on or below their required level for infant
nutrition. In case the content of a certain mineral is below the required level, preferably that
mineral is added. As the level of phosphate and sodium are ularly high in animal skim
milk, the process ing to the invention is designed as such that the content of
phosphate and sodium is ently reduced to enable infant nutrition preparation. Other
ions may be removed to a greater extent and preferably are supplemented again to the final
product.
In a preferred ment, the present invention relate to a process for obtaining an infant
formula, wherein, irrespective of the combining of the lactose in the softened UF permeate
originating from step (d) with any of the UP retentates originating from step (a) and (b),
additional mentation of lactose may be desired to fillfill the requirements for infant
nutrition.
Ullraflltralion steps (a) and (b)
In the process according to the invention, the first and second liquid compositions are
subjected to an ultraflltration step (a) and (b), wherein the liquid and small solutes permeate
through the membrane and end up in the UF permeate (UFPl/UFP2), while the UF retentate
(UFRl/UFR2) comprise substantially all n, in a d volume when compared to the
incoming liquid composition.
Ultrafiltration is readily performed using any ultrafiltration means known in the art,
including ceramic membranes, tubular and organic spiral wound membranes, preferably the
UF membrane is an organic spiral wound membrane. The UF membranes employed have a
molecular weight cut-off (MWCO) of that enables proteins (e. g. whey proteins and casein)
to remain in the retentate, and small solutes (e.g. solutes having a molecular weight of at
most 25 kDa, preferably at most 10 kDa) to permeate through the membrane. Preferably, UP
is performed with a UF ne having a MWCO of at most 25 kDa, more preferably at
most 10 kDa, and preferably of at least 2.5 kDa, more preferably at least 5 kDa. UF of step
(a) preferably es with a volume tration factor (VCF) of 1.5 — 6, more ably
1.6 — 3, most preferably 1.7 — 2.5. UF of step (b) preferably operates with a VCF of 2 — 15,
more preferably 3 — 10, most preferably 4 — 7. The UF is preferably med below 40 0C,
more preferably n 3 oC and 30 oC, even more preferably n 5 oC and 20 oC,
most preferably between 8 and 14 0C.
Using such processing parameters, the UF retentate (UFRl) of step (a) typically comprises
— 65 wt%, preferably 40 — 60 wt% more preferable 45 — 55 wt% proteins, based on total
dry weight of UFRl. ably, the protein content of UFRl has not changed with respect
to the incoming first liquid composition. Thus, it is preferred that UFRl comprises 70 — 90
wt% casein and 10 — 30 wt% whey proteins, based on total n. The UFRl ably
has a total solid content of 5 — 20 %, more preferably 8 — 17 %, most preferably 10 — 15 %.
The UFRl comprises lactose, preferably 20 — 50 wt% lactose, more preferably 30 — 42 wt%
lactose. The UFRl comprises monovalent ions and polyvalent ions. Typically, the UFRl
comprises 0.1 — 1 wt%, preferably 0.2 — 0.5 wt% sodium, 0.5 — 2.5 wt%, preferably 1.2 —
1.8 wt% potassium, 0.2 — 1.5 wt%, preferably 0.4 — 1 wt% chloride, 0.4 — 2.5 wt%,
preferably 0.8 — 1.8 wt% phosphorus, 0.5 — 3 wt%, preferably 1.2 — 2 wt% calcium and 0.01
— 0.5 wt%, preferably 0.05 — 0.2 wt% magnesium, all based on total dry weight of UFRl.
2014/050203
The total ash content of UFRl is preferably 2 — 15 wt%, more ably 6 — 10 wt%, based
on total dry weight of UFRl.
Using such processing parameters, the UF permeate (UFPl) of step (a) typically comprises
mainly lactose, preferably 70 — 98 wt% e, more preferably 80 — 92 wt% lactose. The
UFPl typically comprises 0 — 5 wt%, preferably 0 — 1 wt% proteins, based on total dry
weight of UFPl. The UFPl preferably has a total solid t of 2 — 15 %, more preferably
3.5 — 10 %, most preferably 4.5 — 6 %. The UFPl comprises monovalent ions and
polyvalent ions. Typically, the UFPl comprises 0.2 — 2 wt%, preferably 0.5 — 1 wt%
sodium, 1 — 5 wt%, preferably 2 — 3.5 wt% potassium, 0.5 — 3.5 wt%, preferably 1.2 — 2.5
wt% de, 0.2 — 2.0 wt%, ably 0.5 — 1.5 wt% phosphorus, 0.1 — 2 wt%, preferably
0.25 — 1 wt% calcium and 0.01 — 0.5 wt%, preferably 0.05 — 0.2 wt% magnesium, all based
on total dry weight of the UFPl. The total ash content of UFPl is preferably 4 — 17 wt%,
more preferably 7 — 12 wt%, based on total dry weight of the UFP1.In a preferred
embodiment, the VCF of the UP of step (a) is selected to produce a UFRl and UFPl with
the characteristics as described above.
Using such processing parameters, the UF retentate (UFR2) of step (b) typically comprises
— 55 wt%, preferably 25 — 45 wt% more preferable 30 — 40 wt% whey proteins, based on
total dry weight of UFR2. Preferably, the n content of UFR2 has not changed with
respect to the incoming second liquid ition. Thus, it is red that UFR2
comprises at most 10 wt%, preferably 0 — 2 wt% casein and at least 90 wt%, preferably 98 —
100 wt% whey proteins, based on total protein. The UFR2 preferably has a total solid
content of 3 — 18 %, more ably 6 — 14 %, most preferably 8 — 11 %. The UFR2
comprises lactose, preferably 35 — 65 wt%, more preferably 45 — 55 wt% lactose. The UFR2
comprises monovalent ions and polyvalent ions. Typically, the UFR2 comprises 0.1 — 1.5
wt%, preferably 0.3 — 0.8 wt% sodium, 0.5 — 4 wt%, preferably 1.5 — 2.5 wt% potassium,
0.2 — 2.5 wt%, preferably 0.6 — 1.3 wt% chloride, 0.1 — 1.5 wt%, preferably 0.4 — 0.8 wt%
phosphorus, 0.2 — 1.5 wt%, preferably 0.4 — 1 wt% calcium and 0.01 — 0.5 wt%, preferably
0.05 — 0.2 wt% magnesium, all based on total dry weight of UFR2. The total ash content of
UFR2 is preferably 1 — 15 wt%, more preferably 5 — 9 wt%, based on total dry weight of
UFR2.
Using such processing parameters, the UF permeate (UFP2) of step (b) typically comprises
mainly lactose, preferably 70 — 98 wt% lactose, more preferably 80 — 92 wt% lactose. The
UFP2 typically comprises 0 — 5 wt%, preferably 0 — 1 wt% ns, based on total dry
weight of UFP2. The UFP2 preferably has a total solid content of 2 — 15 %, more preferably
3.5 — 10 %, most preferably 4.5 — 6 %. The UFP2 comprises monovalent ions and
polyvalent ions. Typically, the UFPl comprises 0.2 — 2 wt%, preferably 0.5 — 1 wt%
sodium, 1 — 5 wt%, preferably 2 — 3.5 wt% potassium, 0.5 — 3.5 wt%, preferably 1.2 — 2.5
wt% chloride, 0.2 — 2.0 wt%, preferably 0.5 — 1.5 wt% orus, 0.l — 2 wt%, preferably
0.25 — 1 wt% calcium and 0.01 — 0.5 wt%, preferably 0.05 — 0.2 wt% magnesium, all based
on total dry weight of the UFP2. The total ash content of UFP2 is preferably 4 — 17 wt%,
more preferably 7 — 12 wt%, based on total dry weight of the UFP2. In a preferred
embodiment, the VCF of the UP of step (b) step is selected to e a UFR2 and UFP2
with the characteristics as bed above.
The UFRl and UFR2 having the above characteristics are especially suitable to be
combined, as the combination renders a composition, having the majority of ingredients,
especially the minerals (monovalent and polyvalent ions) on or below their required level for
infant nutrition, for the preparation of a nutritional product suitable for providing nutrition to
an infant, according to governmental regulations.
Both UFPs are rich in lactose, which is a le product for multiple purposes, for
example it can optionally be reintroduced into the process at a later stage in a softened form
which may also be subjected to a lent ion removal step. In an especially preferred
embodiment, the lactose comprising UF te(s) is/are ed with the UF retentate
originating from UF of step (a), with the UF ate originating from UF of step (b) or
with the a mixture of the UF retentates originating from UF of steps (a) and (b).
Mixing step (c)
In the process according to the invention, the UP retentate originating from UF of step (a) is
combined and/or mixed with the UF retentate originating from UF of step (b).
The t or volume) ratio in which the UP retentate originating from step (a), preferably
sing the protein material originating from animal skim milk, and the UF retentate
WO 63494
originating from step (b), comprising whey proteins, are mixed is dependent on the protein
composition of the incoming first liquid composition (e.g. animal milk is a nature product
and the composition thereof may vary somewhat depending on seasons, or what the s
had been fed) but is mainly determined by the desired protein composition in the resulting
dairy product. The skilled person is able to determine the protein composition and
concentration of the incoming animal skim milk by methods known in the art, e.g. by the
method according to FT001/IDF 20-3 (for total protein, N * 6.38), IDF29-l/ISOl7997-
1:2004 (for casein) and FT003 (for whey, NCN, sein en * 6.38).
In a red ment, the (weight or volume) ratio in which the UF retentate
originating from step (a), is mixed or ed with the UP retentate originating from step
(b) lies between 10:1 and 1:10, more preferably
In a particularly preferred embodiment, the dry (milk) formula is further processed into a
nutritional product for human infants such as infant ae, weaning infant formulae,
follow up milk or formulae, growing-up milk, toddler milk. In this respect, the resulting
weight ratio of caseinzwhey protein after mixing of UF ates originating from steps (a)
and (b) is preferably between 75:25 and 30:70, more preferably between 70 to 30 and 36 to
64, more preferably between 65 to 35 and 45 to 55.
The mixing of step (c) may be performed on liquid s, e.g. the liquid UF retentate
originating from step (a) can be mixed with the liquid UF retentate originating from step (b),
giving a liquid UF retentate mixture comprising casein and whey proteins. Alternatively,
one or both of the UF retentates originating from step (a) and (b) are dried prior to the
mixing of step (c), and a liquid and a solid composition are mixed (e.g. by dissolving the
solid in the liquid), giving a liquid mixed stream, or two solid streams are mixed (by dry
blending), giving a solid mixed stream. In case drying is med prior to mixing, it is
preferred that both the skim milk UFRl retentate stream and the retentate stream of the
mixture comprising casein, sweet whey and/or acid whey are dried prior to mixing, and the
resulting solids are dry blended. Preferably, the dried streams are powders. In an especially
preferred embodiment, both retentate streams are liquid during mixing and the drying step is
performed on the mixed retentate stream after the mixing step.
WO 63494
The mixing of step (c) may be accomplished by any means known in the art, such as “in
pipe” (i.e. by the joining of two incoming pipes into one single outgoing pipe), in a ce)
tank or vessel, in an agitated vessel or by any industrial mixer or blender known in the art. In
case two liquid streams are mixed, dynamic mixing or static mixing may be employed. In
case two dried streams (e. g. two powders) are mixed, a dry blender such as a ribbon blender,
a paddle blender, a tumble blender and a vertical blender, may be ed. Preferably, the
mixing step is performed on two liquid streams, preferably “in pipe” or in a balance tank.
The ratio in which the UF retentate originating from step (a) is mixed with the UF retentate
originating from step (b) is conveniently influenced by controlling the flow rate of the
ng itions.
Optionalfurlher processing steps on the UF retentates prior to or after mixing ofslep (0)
Prior to the mixing of step (c), each of the UF retentates obtained in step (a) and (b) may be
subjected to further processing steps, more preferably each of the UF retentates ed in
step (a) and (b) are subjected to further sing steps, prior to ting them to mixing
in step (c). Such further processing steps include, preferably are limited to, concentrating the
liquid composition in step (g) (i.e. increasing the protein/water weight ratio, e.g. via (partial)
evaporation or ion techniques such as nanoflltration or reverse osmosis), drying the
liquid composition in step (h), heat treatment in step (i) (e. g. pasteurization (such as HTST,
ESL or UHT) or ization (dry heat or moist heat) and/or supplementation of additional
water or other components. It is especially preferred that the optional further processing
steps of each of the UF retentates obtained in step (a) and (b) are limited to concentrating the
liquid composition in step (g) (i.e. increasing the protein/water weight ratio, e.g. via (partial)
evaporation or filtration techniques such as nanoflltration or reverse s).
In a preferred embodiment, the UF retentates originating from step (a) and/or (b) or step (c)
is/are concentrated in step (jl) and (jZ), respectively, using reverse osmosis (R0) or
nanofiltration (NF), preferably nanoflltration, prior to the executing step (c), (e) and/or (h).
The concentration of step (jl) is typically performed over an NF ne having a
molecular weight cut-off of at most 500 Da, preferably at most 300 Da, and of at least 100
Da, preferably at least 150 Da, and typically operates with a VCF of 1.5 — 5, preferably 1.8 —
3. Alternatively, the VCF of the NF of step (jl) is preferably chosen as such, that the NFR
has a total solid content of 5 — 3O %, more preferably 10 — 25 %, most preferably 16 — 20 %.
WO 63494
The concentration of step (jl) is preferably performed below 40 0C, more preferably
between 3 oC and 30 oC, even more preferably between 5 oC and 20 oC. ltration may
be enhanced with diaflltration, 1'. e. at least once an additional volume of water is added to the
thus treated permeate, and this diluted permeate is ted to NF again.
The NF or R0 ate, preferably the NF retentate, of the concentration of step (jl) of the
animal skim milk composition originating from step (a) is a liquid composition lly
comprising 30 — 75 wt% proteins (preferably 40 — 65 wt%, more preferable 45 — 60 wt%),
— 50 wt% lactose (preferably 30 — 38 wt%), 0.1 — 0.5 wt% sodium (preferably 0.15 — 0.4
wt%), 0.3 — 2 wt% ium (preferably 0.7 — 1.2 wt%), 0.01 — 0.5 wt% magnesium
(preferably 0.05 — 0.2 wt%), 0.5 — 3 wt% calcium (preferably 1.2 — 2 wt%), 0.05 — 1 wt%
chloride (preferably 0.1 — 0.4 wt%), 0.4 — 2.5 wt% phosphate (preferably 0.8 — 1.8 wt%),
based on total dry weight of the composition, has a total ash content of ably 2 — 13
wt%, more preferably 5 — 9 wt%, based on total dry weight of the composition, and has a
total solid content of 5 — 30 %, more preferably 10 — 25 %, most ably 16 — 20 %.
The NF or R0 retentate, preferably the NF retentate, of the concentration of step (jl) of the
whey composition originating from step (b) is a liquid composition typically comprising 15
— 55 wt% proteins (preferably 25 — 45 wt%, more preferable 30 — 40 wt%), 35 — 65 wt%
lactose (preferably 45 — 55 wt%), 0.1 — 1 wt% sodium (preferably 0.15 — 0.5 wt%), 0.3 — 2
wt% potassium (preferably 0.6 — 1 wt%), 0.01 — 0.5 wt% magnesium (preferably 0.05 — 0.2
wt%), 0.2 — 3 wt% m (preferably 1.2 — 2 wt%), 0.05 — 1 wt% chloride (preferably 0.1
— 0.4 wt%), 0.1 — 1.5 wt% phosphate (preferably 0.4 — 0.8 wt%), based on total dry weight
of the composition, has a total ash content of preferably 1 — 13 wt%, more preferably 5 — 9
wt%, based on total dry weight of the composition, and has a total solid content of 5 — 30 %,
more preferably 10 — 25 %, most preferably 16 — 20 %.
In an especially preferred embodiment, both the UF retentate originating from step (a) and
the UF retentate originating from step (b) are subjected to concentration step (j 1) prior to the
mixing of step (c) and the optionally drying of step (h). It is also possible to concentrate the
mixture of UF retentates originating from step (c) in step (j2).
Preferably, the UF retentate originating from step (a), (b) and/or (c) is/are not subjected to a
polyvalent ion removal step after ultraflltration. Preferably, these UF retentates are not
ted to electrodialysis, ion exchange and/or salt precipitation since a sufficient amount
of the polyvalent ions are ed into the UF permeates.
At least one of the UF retentates obtained in step (a), (b) and/or (c), optionally after the
concentration of steps (jl) or (jZ), may also be dried in step (h) prior to the mixing of step
(c). As such, the UF retentate originating from step (a) and the UF retentate originating from
step (b) are each dried tely, both preferably into a powder. Alternatively, drying may
also occur prior to the mixing of step (c) on only one of the UF retentates, after which the
dried UF retentate, preferably in the form of a powder, is mixed with the non-dried UF
retentate. In the latter case, an additional drying step is preferably needed to dry the mixture
of the UP ates originating from step (c) in order to obtain a dry (milk) formula.
In a preferred embodiment, the mixture of UP retentates originating from step (c) are dried
in step (h), and each of the UF retentate originating from step (a) and the UF retentate
originating from step (b) are not dried prior to the mixing of step (c). Preferably, the drying
of step (h) dries the mixture of UP retentates originating from step (c) into a powder,
preferably by spray-drying. When the drying of step (h) occurs after the mixing of step (c),
the least amount of drying steps is required, namely only involving the mixture of UF
retentates ating from step (c).
As alternative to drying, the mixture of UF retentates originating from step (c) may remain
liquid, optionally after concentration and/or dilution. This liquid mixed product may also be
further processed into liquid nutritional ts, ably products suitable for feeding
infants, e.g. as ready-to-use infant formulae.
After the mixing of step (c) and optionally the drying of step (h), the process according to
the invention yields a dairy product, preferably a dry (milk) formula, preferably in the form
of a powder. Preferably, this dry (milk) formula is further sed into a ional
product suitable for providing nutrition to a human infant, in particular an infant between 0
and 36 months of age. r processing typically comprises addition of further ingredients
as known in the art to the dairy product, in particular one or more selected from vitamins,
2014/050203
minerals, lipids, prebiotics, probiotics, lactose. Where appropriate, those ingredients may
also be added to a liquid composition (either prior to the drying of step (h), or in case no
drying step is performed), such as any of the UF ate originating from step (a) and (b)
and optionally to the ed UF permeate originating from step (d), or even to any of the
incoming first and second liquid compositions. The skilled person is well aware of the
beneficial ingredients for infant nutrition, and how they are best blended with the protein
fraction.
The drying of step (h) may be accomplished by any means known in the art, e.g. spray
drying, zed) bed drying, drum drying, freeze drying, roller drying, etc. In an especially
preferred embodiment, drying is accomplished using spray , optionally preceded by
partial evaporation of the liquid (e. g. by nanoflltration, reverse s, evaporation).
Optionalfurther process steps on the UFpermeates
Ultraflltration of the first liquid composition in step (a) and of the second liquid composition
in step (b) s two ultraflltration permeates (UFPl and UFPZ) that each comprise
lactose. In a preferred embodiment, at least one of, preferably both of, these UF permeates
is/are further processed and combined in step (e) with one of the UP retentates originating
from step (a) or (b), or to the mixture of the UF retentates originating from step (c). The UF
permeate originating from step (a) and from step (b) may be combined prior to further
processing, or the further processing is performed on only one of the UF permeates, or each
of the permeates separately. Preferably, the UP permeates originating from step (a) and (b)
are first ed, after which the combined UF permeates, which are ed to as the
“combined UFPl/UFP2” is further processed as described herein.
Preferably, the UF permeate originating from step (a), (b) and/or the combined UFPl/UFPZ,
has one further treatment before it is mixed with the UF retentate originating from
step (a) and/or (b), or the mixture or UF retentates originating from step (c). Such further
ent preferably comprises subjecting any of these permeates to softening or polyvalent
ion removal in optional step (d). Softening of any of the permeates s a softened UF
te. It is noted here that the “softened UF permeate” refers to a lactose comprising
(preferably lactose enriched) composition that originates from the UF of step (a) and/or (b)
as a permeate from which polyvalent and optionally monovalent ions have been removed
e.g. by step (f).
Softening of at least one of the UF permeates ating from step (a) and/or (b) is
preferably accompanied with or followed by the removal of monovalent ions. l of
monovalent ions of at least one of the UF permeates originating from step (a) and/or (b) is
especially preferred in case the dairy product obtained by the process ing to the
invention is further processed into a nutritional product suitable for infant nutrition.
Polyvalent ion removal, monovalent ion removal and/or concentration (e. g. step (d), (f), (g)
and jZ)) may be accomplished using any technique known in the art, such as
electrodialysis, ion exchange, salt precipitation, lactose crystallization, membrane filtration
techniques such as nanoflltration, optionally enhanced with diaflltration, or combinations
thereof. In the context of the t invention, polyvalent ion removal, ally ed
with monovalent ion removal, also includes the crystallisation of lactose from a liquid UF
permeate ating from step (a) and/or (b) and simultaneously keeping (significant
amounts of) the polyvalent ions and preferably (significant amounts of) the monovalent ions
in solution. The obtained crystalline lactose is regarded to be a softened UF permeate in the
context of the present ion, as it originates from the UP of step (a) and has (significant
amounts of) the polyvalent ions removed.
In an especially red ment, removal of polyvalent ions of step (d), removal of
monovalent ions of step (f) and concentration of step (g) is performed by a ation of
steps sing nanoflltration, salt precipitation and precipitate removal. Preferably, this
combination of steps also comprises electrodialysis. More preferably, removal of polyvalent
ions is performed in the following order: nanoflltration, salt precipitation and precipitate
removal. Preferably, the precipitate removal is followed by a r ltration step
(preferably enhanced with diaflltration) or by electrodialysis, most preferably it is followed
by electrodialysis. Thus, it is preferred that the process of the invention involves the steps of
subjecting the UF permeate originating from step (a), (b) and/or the combined UFPl/UFP2
to nanoflltration, subjecting the nanoflltration retentate to salt precipitation and subsequently
removal of the precipitates therefrom (preferably by ultrafiltration), and subjecting the
precipitate-depleted composition to electrodialysis rably enhanced with diaflltration).
WO 63494
Alternatively, it is preferred that the process of the ion involves the steps of subjecting
the UF te originating from step (a), (b) and/or the combined UFPl/UFP2 to
nanof11tration, subjecting the nanofiltration retentate to salt precipitation and subsequently
removal of the precipitates therefrom (preferably by ultrafiltration), and subjecting the
precipitate-depleted ition to a further nanof11tration step (preferably enhanced with
diaf11tration).
The step of subjecting the UF permeate originating from step (a), and/or of the UF permeate
originating from step (b) or of a mixture of the UF permeates originating from step (a) and
(b) to nanof11tration, as part of this embodiment, mainly accomplishes monovalent ion
l and concentration. Thus, nanof11tration may be regarded the monovalent ion
removal of step (f) combined with the concentration of step (g). Nanof11tration is preferably
performed using at least one NF membrane, more ably at least one spiral wound
membrane, wherein the membrane preferably has a molecular-weight cut-off of 10 — 600
Da, more preferably 100 — 400 Da, y the VCF is typically chosen such that the total
solid content of the NF retentate is in the range of 15 - 35 wt%, preferably in the range of 20
- 25 wt%, most preferably about 22 wt%. NF is preferably operated at a VCF of 2 — 8, more
preferably 3 — 6. NF of step (dl) is preferably performed below 40 0C, more preferably in
the range of3 oC — 30 OC, even more preferably in the range of 5 OC — 20 oC.
The NF retentate is subsequently ted to salt precipitation, which is mainly aimed at
2O removal of polyvalent ions, in particular phosphate ions such as calcium phosphate. It is
especially desirably to lower the phosphate content of the ng animal skim milk and
animal whey when the process of the invention is used to manufacture infant nutrition or a
base for infant nutrition. The salt itation may thus be regarded as part of the
polyvalent ion removal of step (d), and can be achieved by creating suitable conditions
under which polyvalent ions precipitate from the lactose-enriched liquid. These conditions
include on of a strong base, such as sodium hydroxide, pH adjustment to a neutral pH,
such as between 6 and 9, preferably between 6.8 and 9.0, and increasing the temperature to
between 70 and 90 0C, which is preferably followed by decreasing the temperature to
between 5 and 30 oC. Salt precipitation preferably is accomplished by heating the NF
retentate to a temperature of 70 °C — 90 °C, preferably of 75 °C — 88 0C, most preferably of
80 °C — 85 °C. At such temperatures, at least part of the calcium phosphate precipitates,
which is visible as a white precipitate. Higher atures are generally unsuitable, as they
may cause rable enzymatic browning. Heating may occur by any means known in the
art, and is preferably accomplished by steam injection into the NF retentate or by using a
heat exchanger (e.g. a plate heat exchanger). Calcium ate precipitation may be
enhanced, meaning that a greater fraction of the calcium ate precipitates, by
sing the pH of the heated NF retentate to a value above 6.5, preferably in the range of
6.8 — 9.0, more preferably in the range of 6.8 — 7.4, and/or by adding other m salts
such as calcium chloride. The NF retentate typically has a pH of 6.0 - 6.5, and increasing
this to above 6.5, preferably in the range of 6.8 - 9.0, more preferably in the range of 6.8 -
7.4, can be accomplished by addition of a base, preferably an aqueous solution of a metal
hydroxide, such as sodium hydroxide, potassium hydroxide and/or calcium hydroxide.
ably, a concentrated solution sodium hydroxide is used, more preferably a 20 — 35 %
(w/v) solution of NaOH in water. Only little of the base solution is needed, as the
components that may act as buffer are removed by NF. As ce, typically about 0.1 — 1
wt% based on the total weight of the NF ate, preferably 0.3 — 0.5 wt% based on the
total weight of the NF retentate, of a solution of about 30 % (w/v) NaOH in water is used.
The skilled person is capable to adjust this value for variations in pH of the NF retentate,
different types of base and different concentrations. As the calcium content should not
necessarily be reduced as much as the phosphate content of the UF permeate originating
from step (a), and/or of the UF permeate originating from step (b) or of a mixture of the UF
permeates originating from step (a) and (b), in order to prepare infant nutrition with both
calcium and phosphate on or below d values, some additional calcium, preferably in
the form of calcium chloride, calcium citrate, calcium e, calcium hydroxide, or
mixtures thereof, preferably calcium chloride, can be added to the heated NF retentate,
which induces the precipitation of more calcium phosphate. Using calcium hydroxide
preferably achieves both the pH increase and addition of a calcium salt, but its suitability is
slightly ed by its low solubility. Thus, in a preferred embodiment, a mixture of
calcium chloride and sodium hydroxide is added to the NF retentate to enhance calcium
phosphate precipitation. As such, the softened UFP will have a phosphate t which is
further reduced compared to the calcium content. Suitably, the NF retentate is subsequently
cooled to a temperature below 30 °C, ably in the range of 5 °C — 30 0C, more
preferably in the range of 8 °C — 25 °C, most preferably in the range of 8 °C — 15 °C, before
the precipitate is removed from the NF retentate. Rapidly cooling the NF retentate is
ally preferred, to reduce the chances on rable bacterial growth and to minimize
the resolubilization of m phosphate. Although less preferred, the precipitate may also
be removed from the NF retentate at an elevated temperature, for example at a temperature
above 25 °C.
Subsequently, the precipitates may be removed by any technique known in the art (e.g.
centrifugal separation, decantation in a settling tank, ion, for example microflltration or
ultraflltration). Preferably, the precipitate removal step is performed by filtration, more
preferably by ultrafiltration, which permeates the lactose and soluble minerals and s
the precipitate which predominantly comprises calcium phosphate. The primary aim of this
precipitate removal is thus to remove precipitates and not to fractionate any other material,
and may thus be regarded as part of the polyvalent ion removal of step (d). Any UF
membrane as known in the art may be used, but also a UF bed. Preferably, at least one UF
membrane with a lar-weight cut-off of preferably 1 kDa — 50 kDa, more preferably 5
— 20 Da is used. UF preferably operates at a VCF of 5 — 40, more preferably 7 — 35, most
preferably 10 — 30. Good results are obtained using a VCF of about 10, but lactose yields in
the outflowing softened UFP may be further increased without deteriorating the efficacy of
process by increasing the VCF to up to 40. Thus, the UF permeate comprises substantially
all e as originally present in the incoming UF permeate(s) originating from step (a)
and/or (b). The NF retentate which has been subjected to precipitate removal (e.g. the UF
permeate) is referred to in the t of this embodiment as the precipitate-depleted UF
permeate(s).
2O It is preferred that the resulting precipitate-depleted UF permeate(s) is/are further desalted in
a r nanoflltration step and/or an odialysis step, most preferably in an
electrodialysis step. The electrodialysis (ED) step as part of this embodiment may be
regarded part of the lent ion removal of step (d) and part of the monovalent ion
removal of step (f), and is preferably med on an incoming flow comprising between
18 and 24 % w/w solids content. ED is preferably operated until the conductivity of the
outflowing (lactose ed) liquid reaches a value below 4 mS, preferably below 2 mS,
even more preferably below 1 mS and/or until the ash content reaches a value of below 3
wt%, more preferably below 2 wt%, most preferably below 1 wt%, based on total weight of
the outflowing liquid. The skilled person understands how to adjust the electrodialysis
settings to achieve this goal. In case a r nanofiltration step is employed, NF is
preferable conducted using the parameters (i.e. membrane type and porosity, VCF and
temperature) as described above for the NF step on the incoming UF te(s) originating
from step (a) and/or (b). Preferably, the NF is enhanced with diaflltration, i.e. at least once
an additional volume of water is added to the NF permeate, and this diluted thus treated
permeate is ted to NF again. The NF is preferably performed such that the NF
retentate has a total solid content of 16 — 28 wt%, preferably 18 — 22 wt%.
The resulting lactose-enriched outflowing liquid of this preferred sequence of steps for the
combined removal of polyvalent ions of step (d), removal of monovalent ions of step (f) and
concentration of step (g), i.e. the precipitate-depleted UF permeate (preferably obtained as a
UF te) obtained in the precipitate removal step, the outflowing liquid obtained in the
ED step or the NF retentate obtained in the further NF step, preferably the outflowing liquid
of the ED step, is referred to as the softened UF permeate in step (d) and can be used in step
(e).
The polyvalent ion removal of step (d) enables the removal of significant amounts of the
polyvalent ions. Preferably at least 50 wt%, more preferably at least 70 wt% or at least 80
wt%, most preferably at least 90 wt% of the polyvalent ions are removed. The weight
tage (wt%) of polyvalent ion removal is determined by comparing the total weight of
lent ions present after step (b) to the total weight of polyvalent ions present prior to
step (d). Likewise, a monovalent ion l step enables the removal of significant
amounts of the lent ions. Preferably, at least 20 wt% of the monovalent ions are
removed, more preferably at least 35 wt% or at least 50 wt%, most preferably at least 60
2O wt% of the monovalent ions are removed. Thus, the softened UF permeate preferably
comprises at least 20 wt% less monovalent ions, preferably at least 35 wt% less, more
preferably at least 50 wt% less, most preferably at least 60 wt% less monovalent ions, when
compared to the incoming UF permeate ating from step (a).
Each of the UF permeates originating from the UF of step (a) and (b), either separately or as
mixture, may o further processing steps prior to being subjected to the polyvalent ion
removal of step (d). Such optional further processing steps include, preferably are limited to,
concentrating the liquid stream (i.e. increasing the lactose/water weight ratio) by any
le means known in the art (e. g. by (partial) ation or flltration techniques such as
reverse osmosis), heat treatment (e.g. pasteurization (such as HTST, ESL or UHT) or
sterilization (dry heat or moist heat)) and/or supplementation of additional water or other
components. tration may also be accomplished during the removal of monovalent
ions, e. g. during nanoflltration, optionally enhanced with diaflltration.
In an especially preferred embodiment, removal of monovalent ions from the UF permeate
originating from step (a) and/or (b), or the combined UFPl/UFP2 is performed on any
softened permeate originating from step (d) by nanofiltration (NF). Using this sequence of
steps, the nanoflltration retentate (NFR) is considered to be the softened UF permeate (as
this is enriched in lactose), which may then be combined with any of the UF retentates in
step (e). During the ion exchange of step (d), the polyvalent ions (e. g. Mg2+, Ca2+, PO43) are
replaced by monovalent ions (typically Na+, K+, Cl'), and during nanofiltration these
monovalent ions permeate h the nanoflltration ne. Preferably, nanoflltration is
ed with diaflltration, 1'. e. at least once an additional volume of water is added to this
permeate, and this diluted thus d permeate is ted to NF again. Conveniently, the
NF permeate which comprises monovalent ions and is substantially free of e, may be
used to regenerate the ion exchange column(s).
Nanoflltration of the (softened) UF permeate originating from step (a) and/or step (b), or of
the combined UFPl/UFP2, may be performed using a spiral wound membrane having a
molecular weight cut-off of at most 500 Da, preferably at most 300 Da, and of at least 100
Da, ably at least 150 Da, is used. The NF step typically operates with a VCF of 1.1 —
, preferably 1.2 — 4, more preferably at 1.4 to 3. Alternatively, the VCF of the NF step is
2O preferably chosen as such, that the NFR has a total solid content of 14 — 35 %, more
preferably 20 — 3O %. The NF step is preferably performed below 40 0C, more preferably
n 3 oC and 30 oC, even more preferably between 5 oC and 20 oC.
Preferably, ltration is enhanced with diaflltration. One or more additional volumes of
water, typically 50 — 100 vol% of the volume of the incoming stream of the NF step
(outgoing stream of the ion exchange step), preferably 60 — 80 vol%, are added to the NFR,
which is subsequently pushed through the NF membrane er with residual monovalent
ions from the NFR. Preferably, at least two additional volumes of water are added to the
NFR. An additional advantage of using NF is that large amounts of water can be removed by
this cost-effective membrane tion technique, t the need for evaporation.
The composition of the UF permeate originating from step (a) and/or the UF permeate
originating from step (b), or the composition of the combined UFPl/UFP2 may vary to a
2014/050203
d extent depending on the exact composition of the first liquid composition (e. g. what
type of animal skim milk is used, which animal, seasonal variations). For example, new
season bovine milk comprises somewhat higher levels of sodium compared to bovine milk
from later in the season. Typically, the UF permeate originating from step (a) and/or the UF
permeate originating from step (b), or the ed UFPl/UFP2 prior to softening is a
liquid composition typically comprising 70 — 98 wt% lactose (preferably 80 — 92 wt%), 0.2
— 2 wt% sodium (preferably 0.5 — 1 wt%), 1 — 5 wt% potassium (preferably 2 — 3.5 wt%),
0.01 — 0.5 wt% magnesium (preferably 0.05 — 0.2 wt%), 0.1 — 2 wt% calcium (preferably
0.25 — 1 wt%), 0.5 — 3.5 wt% chloride rably 1.2 — 2.5 wt%), 0.2 — 2 wt% phosphorous
(preferably 0.5 — 1.5 wt%), based on total dry weight of the composition, has a total ash
content of preferably 4 — 17 wt%, more preferably 7 — 12 wt%, based on total dry weight of
the composition, and preferably has a total solid content of 2 — 15 %, more ably 3.5 —
%, most preferably 4.5 — 6 %. In addition to lactose and minerals, the UF permeate
originating from step (a) and/or the UF permeate originating from step (b), or the
ition of the combined UFPl/UFP2 stream may comprise some small proteinaceous
material (e.g. peptides), organic acids (e.g. citric acid, lactic acid) and non-protein nitrogen
material (NPN).
After softening of step (d), the softened UF permeate, preferably comprises at least 90 % of
the lactose present prior to softening, preferably at least 95 %. The softened UF permeate
obtained after softening, or preferably after monovalent ion removal most preferably after
ion exchange of step (d) and uent ltration, is a liquid composition typically
comprising 75 — 100 wt% lactose (preferably 90 — 100 wt%, more preferable 95 — 99 wt%),
at most 1.5 wt% sodium (preferably 0.2 — 0.7 wt%), at most 1 wt% potassium (preferably
0.1 — 0.5 wt%), at most 0.1 wt% magnesium (preferably at most 0.02 wt%), at most 0.2 wt%
calcium (preferably at most 0.1 wt%), at most 1.5 wt% chloride rably 0.3 — 1 wt%), at
most 0.5 wt% phosphate (preferably at most 0.3 wt%), based on total dry weight of the
composition, has a total ash content of preferably at most 5 wt%, more preferably 1 — 4
wt%, based on total dry weight of the composition, and preferably has a total solid content
of 7 — 35 %, more preferably 10 — 30 %, most preferably 18 — 28 %. Each of the ions
mentioned here is preferably substantially absent from these softened UF permeate after
ing or monovalent ion removal.
In case the total solid content of any of the softened UF permeate is vely low, e.g.
below 10 % or below 15 %, the softened UF permeate may be concentrated to achieve a
total solid content of preferably 10 — 3O %, more preferably 18 — 28 %, before being
combined in step (e). Concentration may be accomplished by any means known in the art.
Preferably, tration is accomplished using reverse osmosis.
In case the softened UF permeate is obtained by ion exchange of step (d) and nanof11tration,
the NF permeate is a liquid ition typically comprising at most 25 wt% lactose
(preferably at most 15 wt%), 10 — 50 wt% sodium (preferably 20 — 30 wt%), 5 — 30 wt%
potassium (preferably 8 — 12 wt%), 0 — 10 wt% magnesium (preferably 0.1 — 5 wt%), 0 — 10
wt% m (preferably 0.1 — 5 wt%), 20 — 70 wt% chloride (preferably 35 — 55 wt%), 0 —
wt% phosphate (preferably 0.1 — 5 wt%), based on total dry weight of the composition,
has a total ash t of preferably at least 50 wt%, more preferably 65 — 85 wt%, based on
total dry weight of the composition, and preferably has a total solid content of 7 — 35 %,
more ably 10 — 3O %, most ably 18 — 28 %.
The softened UF permeate originating from step (d), having the above teristics, is
y suited to be added to the UF retentate originating from step (a) and/or the UP
retentate originating from step (b), or preferably to be added to the mixture of UP retentates
2O originating from step (c), for the ation of dairy products, preferably (dry) milk
formulae, in particular for the preparation of a nutritional product for providing nutrition to
infants. Thus, in a preferred embodiment of the process according to the ion, the
softened UF permeate originating from step (d) is combined in step (e) with the UF retentate
originating from step (a) and/or the UF retentate originating from step (b), or to the mixture
of UP retentates originating from step (c). Most preferably the softened UF permeate
originating from step (d) is combined in step (e) during or after the mixing of step (c), thus
either with the mixture of UP retentates in step (c), or with the mixture of UF retentates
originating from step (c).
In a preferred embodiment, at least 80 wt%, more preferably at least 90 wt% or even at least
95 wt%, most preferably at least 98 wt% of the lactose that is obtained in the UP permeates
originating from step (a) and (b) is combined in step (e) with the UP retentates originating
from step (a) and (b). The lactose content in a liquid ition can readily be determined
by skilled person, e.g. enzymatically or by HPLC.
The process according to the invention s residual water at several points, e. g. from the
drying step, the optionally as nanoflltration permeates and/or the reverse osmosis permeates.
In a preferred embodiment, this residual water, optionally after further purification by e.g.
reverse osmosis, is recycled in the process ing to the invention, e. g. used to dilute or
reconstitute the first liquid composition (preferably the animal skim milk) and/or the second
liquid composition comprising sweet whey and/or acid whey starting material, or as
diaflltration water.
Definitions
The term “sweet whey” herein refers to the liquid (whey protein ning) by-product of
the cheese manufacture industry which makes use of enzymatic cheese curd formation (e. g.
based on casein precipitation using rennet), which material is y accessible in the
commercial market. Typically, whey proteins present in sweet whey include, i.a. beta-
lactoglobulin, lactalbumin, bovine serum albumin, immunoglobulins, lactoferrin,
lactoperoxidase and glycomacroprotein
Conversely, the term “acid whey” herein refers to the liquid (whey protein containing) by-
product of the cheese cture industry which makes use of (edible) acids for cheese
curd formation (e.g. based on casein precipitation using acids such as citric acid), which
material is readily accessible in the commercial market. Typically, whey proteins present in
acid whey include, i.a. beta-lactoglobulin, alpha-lactalbumin, bovine serum albumin,
globulins, lactoferrin and lactoperoxidase
The term "casein" herein refers to casein or caseinate proteins as found in animal skim milk,
such as bovine skim milk, more in ular cows' skim milk. Preferably, casein or
caseinate is in substantially intact, non-hydrolyzed form.
As used herein, the term “polyvalent ions” refers to ions having a ve or negative
charge of two or more. More in particular, this term refers to Mg”, Ca2+ and polyvalent
phosphate anions (e.g. , PO43'). The term “monovalent ions” refers to ions having a
positive or negative charge of one, in particular Na+, K+, Cl'.
The term “removal of polyvalent ions” means that said lent ions are removed from
the UP permeate ition which is subjected to the polyvalent ion l step (step
(d)). Preferably, the term “removal of polyvalent ions” indicates that at least 10 or 20 wt%
of the polyvalent ions that are present in said UF permeate (on dry weight basis thereof) is
d, preferably at least 50 wt%, 60 wt%, more preferably 70 wt% or at least 80 wt%,
most preferably at least 90 wt%. The weight percentage (wt%) of polyvalent ion removal is
determined by comparing the total weight of polyvalent ions present after step (c) to the total
weight of polyvalent ions present prior to step (c). Likewise, the term “softening” is used to
denote the removal of polyvalent ions. Hence, herein “softening” and “removal of
polyvalent ions” is used interchangeably. Analogously, the term “softened” is used to refer
to a composition from which polyvalent ions have been removed. “Signif1cant polyvalent
ion removal” denotes the removal of at least 70 wt% of the polyvalent ions, preferably at
least 85 wt%, more preferably at least 95 wt% or even at least 99 wt% of the polyvalent
ions. lent ion removal or softening may be accompanied with lent ion
removal, either in the same step or in a separate step. Preferably, polyvalent ion removal
refers to removal of at least or all of calcium, ium and/or phosphate species to the
extent as defined in this paragraph.
The term “removal of monovalent ions” means that said monovalent ions are removed from
the composition which is subjected to the monovalent ion removal step (preferably a
softened UF permeate and/or any UF retentate). In case not indicated otherwise, preferably
at least 10 or 20 wt% (on dry weight basis) of the monovalent ions is removed from the
composition which was subjected to a lent ion removal step, more preferably at least
wt% or 50 wt%, most preferably at least 60 wt%. Removal of monovalent ions is
particularly preferred in case the process according to the invention aims to manufacture dry
powder formulations intended for use as infant nutrition. “Signif1cant monovalent ion
removal” denotes the removal of at least 70 wt% of the monovalent ions, preferably at least
85 wt%, more preferably at least 95 wt% or even at least 99 wt% of the monovalent ions.
Preferably, monovalent ion removal refers to l of at least or all of sodium, potassium
and/or chloride to the extent as defined in this paragraph.
As used herein, the term “enriched” herein refers to the situation wherein the amount of a
certain constituent of a (liquid) composition (as wt% based on dry weight) is higher after a
process step, when compared to the content of the same ingredient in the (liquid)
composition before said process step. ably, the dry weight percentage of an ingredient
that is enriched has a content in a stream discharged from the process step of at least 110 %,
more preferably at least 125%, most preferably at least 150 %, based on the dry weight
percentage of said ingredient in the incoming stream of said s step. Exemplary is the
ultraflltration of skim milk, wherein the milk proteins are retained in the retentate while
water and small s permeate through the ultraflltration membrane. As such, any UF
retentate is enriched in casein and whey ns, as the content thereof in the retentate, as
wt% based on dry weight of the composition, is increased compared to the wt% thereof in
skim milk, as less small solutes are present. Likewise, the permeate is enriched in small
solutes (e.g. enriched in lactose), as the amount of proteins is significantly reduced in the
te, and lactose tutes by far the largest part of the dry weight of the permeate.
The “total solid content” of a liquid composition denotes the weight percentage of solids
present in the composition, based on the total weight of the ition. Solids include all
non-volatiles, typically everything except water.
The e concentration factor” or “VCF” is the factor at which a liquid composition is
concentrated upon flltration, i.e. the total volume of the incoming stream prior to filtration
divided by the total volume of the retentate after filtration, irrespective of the total solid
content. Thus, when 5 L of a liquid composition is fractionated over an ultraflltration
membrane into a permeate of 4 L and a retentate of l L, this UF process operates with a
VCF of5/l = 5.
By a “UF retentate originating from” is meant the liquid retentate composition that is
(directly) obtained from ultraflltration steps (a) and (b). The term also refers to the UP
ates that are mixed in step (c) to obtain the mixture of UF retentates. ective of
whether between the obtaining of the UF retentate from step (a) and (b) and the mixing in
step (c) or step (e) or drying in step (h), the UF retentate is subjected to a concentration step,
such as reverse osmosis or nanofiltration, the term UF retentate still applies to this UF
fraction. Thus, the term UF retentate is meant to denote the (protein enriched) fraction that is
processed according to the steps of the invention from the ultraflltration step up to the point
where it is (re)combined with a UF permeate.
Similarly, the term “UF permeate originating from” herein means the liquid permeate
composition that is (directly) ed from ultraflltration steps (a) and (b). The term also
refers to the UP permeates that are conveyed as (liquid) compositions from the ultraflltration
step to the polyvalent ion removal module for execution of step (d), or to the monovalent ion
removal module for execution of step (f) and/or any al concentration step or module
to eventually obtain the combined permeate/retentate product of step (e) or to obtain the dry
powder in step (h). Irrespective of whether between the obtaining of the UP permeate from
step (a) and (b) and the mixing in step (e) or drying in step (h), the UP permeate is subjected
to a sing step (e. g. a polyvalent ion removal step, a concentration step, reverse
osmosis and/or nanoflltration), within the context of the present invention the term UF
permeate still applies to this UF fraction. Thus, the term UF te is meant to denote the
(lactose enriched) fraction that is sed according to the steps of the invention from the
ultraflltration step up to the point where it is (re)combined with a UF retentate.
In the context of the present invention, a dry a has a water content of at most 6 wt%,
2O preferably 1 — 4 wt%, more preferably 2 — 3 wt%, based on total weight of the ition.
The dry formula may be further processed into nutritional products, ably products
suitable for feeding human infants.
Preferredfirst and second liquid itions ofthe invention
The first liquid composition comprises animal skim milk which comprises milk ns and
lactose. It comprises amounts of minerals that are typical for animal skim milk. The protein
on thereof comprises 70 — 90 wt% casein and 10 — 30 wt% whey proteins, preferably
75 — 85 wt% casein and 15 — 25 wt% whey protein, based on dry total weight of the protein
fraction. Preferably, it comprises 20 — 60 wt% protein, more ably 25 — 50 wt% protein
based on total dry weight of the first liquid composition. Preferably, the first liquid
composition comprises 25 — 75 wt% lactose, more preferably 40 — 60 wt% lactose, based on
total dry weight of the first liquid composition. Preferably, the first liquid composition
comprises 3 — 15 wt% minerals, more preferably 5 — 10 wt% minerals, based on total dry
weight of the first liquid composition. Preferably, the first liquid composition comprises 25
— 75 wt% monovalent ions, more ably 30 — 60 wt% monovalent ions, and 25 — 75 wt%
polyvalent ions, more preferably 40 — 70 wt% polyvalent ions, based on total dry weight of
the minerals. Preferably, the first liquid composition has a total solid t between 3 and
%, more preferably between 6 and 11 %, most preferably between 7.5 and 10 %. The fat
content of the animal skim milk is typical for animal skim milk and lies well below that of
non-skim milk. In particular, the fat content lies below 3 wt% (g/lOOg animal skim milk),
preferably below 2 wt%, more preferably below 1 wt%, most preferably below 0.5 wt%.
In an especially preferred embodiment, the first liquid composition comprises animal skim
milk or is animal skim milk. Animal skim milk (i.e. non-human skim milk), preferably from
bovine animals, and may be used as such, in diluted or concentrated form, as (optionally
diluted) skim milk concentrate or as reconstituted skim milk powder. Most ably, the
first liquid composition is cows’ skim milk. The animal skim milk may be pretreated before
it is subjected to the process according to the invention. Such pre-treatment comprises or
consists of a heat-treatment step (e.g. rization) and/or flltration step to reduce the
bacterial load of the animal skim milk. Preferably, the animal skim milk is not pre-treated
with the aim to change the mineral t or profile thereof. In particular, the animal skim
milk is ably not (significantly) softened or subjected to monovalent ion removal before
2O it enters the present ultrafiltration process.
The second liquid ition of the ion is a sweet whey and/or acid whey
comprising composition which comprises n, lactose and amounts of ls that are
typical for this type of whey (in the form of monovalent and polyvalent ions). The protein
fraction of the liquid whey composition comprises 0 — 25 wt% casein and 75 — 100 wt%
whey proteins, preferably 0 — 10 wt% casein and 90 — 100 wt% whey protein, most
preferably 0 — 5 wt% casein and 95 — 100 wt% whey protein, based on dry total weight of
the protein fraction. Preferably, the second composition comprises 5 — 40 wt% n, more
preferably 7 — 17 wt% protein based on total dry weight of the second liquid composition.
Preferably, it comprises 40 — 90 wt% lactose, more preferably 60 — 80 wt% lactose, based on
total dry weight of the second liquid composition. Preferably, the second composition
ses 3 — 15 wt% minerals, more preferably 6 — 12 wt% minerals, based on total dry
weight of the second liquid composition. Preferably, the second composition comprises 40 —
90 wt% monovalent ions, more preferably 60 — 85 wt% lent ions, and 10 — 60 wt%
polyvalent ions, more preferably 15 — 40 wt% polyvalent ions, based on total dry weight of
the minerals. Preferably, it has a total solid t between 1 and 15 %, more preferably
between 3 and 10 %, most preferably between 4 and 8 %.
In an ally preferred embodiment, the second liquid composition is sweet whey and/or
acid whey. The sweet and/or acid whey may be used as such, in d or concentrated
form, as (optionally diluted) whey concentrate and as reconstituted whey from a powder.
Both sweet whey and acid whey are suitable as liquid animal whey composition for use in
the invention. Most preferably, the second liquid composition is sweet whey. The animal
whey as used may be pretreated before it is subjected to an ultraflltration step of the process
according to the invention. Pre-treatment of the animal whey comprises or consists of heat-
treatment (preferably pasteurization) and/or filtration to reduce the bacterial load of the
animal whey. Preferably, the animal whey is not pre-treated with the aim to change the
mineral t or profile thereof. In particular, the animal whey is not (significantly)
softened or subjected to monovalent ion removal before it enters the present process.
Preferably, the second liquid composition comprises sweet whey, or the whey t
therein ts of sweet whey or said whey comprises at least 20 wt% sweet whey of the
total whey (on total weight basis of the whey present in the second liquid composition), or at
least 40 wt% sweet whey, or at least 60 wt% sweet whey, or at least 80 wt% sweet whey, or
even at least 90 wt% sweet whey. In such cases, the remainder of the whey comprises acid
whey.
Intermediary products obtainable during execution ofthe process
The present invention also relates to intermediary products obtained during execution of the
process according to the ion.
In a first aspect, the intermediary products of the invention relate to a liquid composition
obtainable by the nanofiltration of the UP retentate originating from UF of the first liquid
composition in step (jl), i.e. the nanoflltration retentate obtained by NF of the UP retentate
originating from UF of the animal skim milk composition. The liquid composition according
to this first aspect comprises:
(a) 30 — 75 wt% proteins, preferably 40 — 65 wt% ns, more able 45 — 60 wt%
proteins, based on total dry weight of the composition,
(b) 20 — 50 wt% lactose, preferably 30 — 38 wt% lactose, based on total dry weight of the
composition, and
(c) minerals in the form of monovalent and polyvalent ions.
The protein on (a) preferably is not changed with t to the protein fraction as
present in animal skim milk. Thus, the protein fraction (a) preferably comprises 70 — 90 wt%
casein and 10 — 30 wt% whey protein, ably 75 — 85 wt% casein and 15 — 25 wt% whey
protein, based on total protein. The monovalent ions of fraction (c) preferably comprise
sodium, more preferably 0.1 — 0.5 wt% sodium, most preferably 0.15 — 0.4 wt% sodium,
based on total dry weight of the composition. The monovalent ions of fraction (c) preferably
comprise potassium, more preferably 0.3 — 2 wt% potassium, most preferably 0.7 — 1.2 wt%
potassium, based on total dry weight of the composition. The monovalent ions of fraction (c)
preferably comprise chloride, more preferably 0.05 — 1 wt% de, most preferably 0.1 —
0.4 wt% de, based on total dry weight of the composition. The polyvalent ions of
fraction (c) preferably se magnesium, more preferably 0.01 — 0.5 wt% magnesium,
most preferably 0.05 — 0.2 wt% magnesium, based on total dry weight of the composition.
The polyvalent ions of fraction (c) preferably comprise calcium, more preferably 0.5 — 3
wt% calcium, most preferably 1.2 — 2 wt% calcium, based on total dry weight of the
ition. The polyvalent ions of fraction (c) preferably comprise phosphate, more
preferably 0.4 — 2.5 wt% phosphate, most preferably 0.8 — 1.8 wt% phosphate, based on
total dry weight of the composition. The total mineral content of fraction (c) preferably adds
up to a total ash content of 2 — 13 wt%, more preferably 5 — 9 wt%, based on total dry
weight of the composition. The composition preferably has a total solid content of 5 — 30 %,
more preferably 10 — 25 %, most ably 16 — 20 %.
In a second , the intermediary products of the invention relate to a liquid composition
obtainable by the nanof11tration of the UF retentate originating from UF of the sweet whey
and/or acid whey comprising composition in step (jl), i.e. the nanof11tration ate
obtained by NF of the UF retentate originating from UF of the second liquid composition.
The liquid composition according to this second aspect comprises:
(a) 15 — 55 wt% proteins, preferably 25 — 45 wt% proteins, more preferable 30 — 40 wt%
proteins, based on total dry weight of the composition,
(b) 35 — 65 wt% lactose, preferably 45 — 55 wt% lactose, based on total dry weight of the
composition, and
(c) minerals in the form of monovalent and polyvalent ions.
The protein fraction (a) preferably is not changed with respect to the protein on as
present in sweet whey and/or acid whey. Thus, the protein fraction (a) preferably comprises
0 — 25 wt% casein and 75 — 100 wt% whey protein, preferably 0 — 10 wt% casein and 90 —
100 wt% whey protein, most preferably 0 — 5 wt% casein and 95 — 100 wt% whey protein.
The monovalent ions of fraction (c) preferably comprise sodium, more preferably 0.1 — 1
wt% sodium, most preferably 0.15 — 0.5 wt% sodium, based on total dry weight of the
composition. The monovalent ions of on (c) preferably comprise potassium, more
preferably 0.3 — 2 wt% potassium, most ably 0.6 — 1 wt% potassium, based on total
dry weight of the composition. The monovalent ions of fraction (c) preferably comprise
chloride, more preferably 0.05 — 1 wt% chloride, most preferably 0.1 — 0.4 wt% chloride,
based on total dry weight of the composition. The polyvalent ions of on (c) ably
comprise magnesium, more preferably 0.01 — 0.5 wt% magnesium, most preferably 0.05 —
0.2 wt% magnesium, based on total dry weight of the composition. The polyvalent ions of
fraction (c) preferably se calcium, more preferably 0.2 — 1.5 wt% calcium, most
preferably 0.4 — 1 wt% calcium, based on total dry weight of the composition. The
lent ions of fraction (c) preferably se phosphate, more preferably 0.1 — 1.5
wt% phosphate, most preferably 0.4 — 0.8 wt% phosphate, based on total dry weight of the
composition. The total mineral content of fraction (c) preferably adds up to a total ash
content of 1 — 13 wt%, more preferably 5 — 9 wt%, based on total dry weight of the
composition. The composition preferably has a total solid content of 5 — 30 %, more
preferably 10 — 25 %, most ably 16 — 20 %.
In a third aspect, the intermediary products of the invention relate to a liquid composition
obtainable by the nanoflltration of step (j2), i.e. the nanoflltration retentate obtained by NF
of the ed UF permeate originating from the ed UF permeates of the first and
second liquid compositions. The liquid composition ing to this third aspect comprises:
WO 63494
(a) at most 5 wt% proteins, preferably at most 1 wt% proteins, based on total dry weight of
the composition,
(b) 75 — 100 wt% lactose, preferably 90 — 100 wt% lactose, most preferably 95 — 99 wt%
lactose, based on total dry weight of the composition, and
(c) at most 5 wt% minerals in the form of monovalent and polyvalent ions, preferably at
most 1 wt% minerals, based on total dry weight of the composition.
Preferably, the composition is substantially depleted from polyvalent ions, i.e. the
composition preferably comprises at most 1 wt% lent ions, more preferably at most
0.5 wt% polyvalent ions, most preferably at most 0.35 wt% polyvalent ions. The lent
ions of fraction (c) preferably comprise at most 1.5 wt% sodium, more preferably 0.2 — 0.7
wt% sodium, based on total dry weight of the composition. The monovalent ions of fraction
(c) preferably comprise at most 1 wt% potassium, more preferably 0.1 — 0.5 wt% potassium,
based on total dry weight of the composition. The monovalent ions of on (c) preferably
comprise at most 1.5 wt% chloride, more preferably 0.3 — 1 wt% de, based on total dry
weight of the composition. The polyvalent ions of fraction (c) preferably comprise at most
0.1 wt% magnesium, more preferably at most 0.02 wt% magnesium, based on total dry
weight of the composition. The polyvalent ions of fraction (c) preferably comprise at most
0.2 wt% m, more preferably at most 0.1 wt% calcium, based on total dry weight of the
composition. The lent ions of fraction (c) preferably comprise at most 0.5 wt%
phosphate, more preferably at most 0.3 wt% phosphate, based on total dry weight of the
ition. The total mineral content of fraction (c) preferably adds up to a total ash
content of at most 5 wt%, more preferably 1 — 4 wt%, based on total dry weight of the
composition. The composition preferably has a total solid content of 7 — 35 %, more
preferably 10 — 30 %, most preferably 18 — 28 %.
In a fourth aspect, the intermediary products of the ion relate to a liquid composition
obtainable by the miXing of step (c), i.e. the e of UP retentates obtained by UF of the
first and second liquid compositions. The liquid composition according to this fourth aspect
comprises: a protein content of n 40 and 52 wt%, wherein casein and whey are
present in a weight ratio which lies between 70:30 and 30:70, lactose in an amount of
between 35 and 50 wt%, and the following minerals: magnesium in an amount of between
0.01 and 0.30 wt%, calcium in an amount of between 0.80 and 1.70 wt%, phosphorus in an
amount of between 0.60 and 1.50 wt%, sodium in an amount of between 0.10 and 0.60 wt%,
de in an amount of between 0.05 and 0.60 wt% and potassium in an amount of
n 0.60 and 1.50 wt%, all based on dry weight of the intermediary product.
In a fifth aspect, the intermediary products of the invention relate to a liquid ition
obtainable by the combining of step (e), i.e. the mixture of UF retentates obtained by UF of
the first and second liquid compositions and the softened UF permeate ating from the
ed UF permeates of the first and second liquid compositions. The liquid composition
according to this fifth aspect ses: a protein content of between 16 and 24 wt%,
wherein casein and whey are present in a weight ratio which lies between 70:30 and 30:70,
lactose in an amount of between 65 and 80 wt%, and the following minerals: magnesium in
an amount of between 0.01 and 0.25 wt%, m in an amount of between 0.20 and 0.80
wt%, phosphorus in an amount of between 0.40 and 0.80 wt%, sodium in an amount of
between 0.20 and 0.80 wt%, chloride in an amount of between 0.30 and 0.90 wt% and
potassium in an amount of n 0.30 and 0.90 wt%.
Use ofintermediary products obtainable by the process of the invention
The present ion also relates to uses of the intermediary products according to the
invention, obtainable during execution of the s as described above, especially the use
of those products in the preparation of nutritional products suitable for feeding human
infants, or bases for such nutritional products. Likewise, the present invention also relates to
processes for the preparation of nutritional products le for feeding human infants, or
bases for such nutritional products using one or more of the intermediary products according
to the invention, obtainable during execution of the process as described above.
In the context of the t invention, a base for nutritional products suitable for feeding
human s denotes a dairy product, preferably a powder, in which all ingredients are on
or below their required level for infant nutrition. Some of the required or beneficial
ingredients, such as lipids, prebiotics, vitamins and minerals, may be below the required
level, and need to be supplemented to the base, in order to prepare nutritional products
suitable for feeding human infants. The skilled person is aware of bases for nutritional
products suitable for feeding human infants, and knows which ingredients may need
supplementation and how such supplementation is accomplished.
In particular, the present invention relates to a process for making infant nutrition or a base
for infant nutrition, able from the intermediary products, comprising:
(I) mixing the liquid composition according to the first aspect with a source of lactose,
preferably the liquid composition according to the third aspect, and a source of whey
proteins, preferably the liquid composition according to the second aspect, or
(II) mixing the liquid composition according to the fourth aspect with a source of lactose,
preferably the liquid composition according to the third aspect, or
(III) providing the liquid composition according to the fifth aspect, and
(IV) optionally adding further ingredients to the (mixed) product of step (I), (II) or (III), or
to the dried product of step (V),
(V) drying the product of step (I), (II), (III) or (IV).
The further ients that may be added in step (IV) are known in the art, and preferably
include, more preferably are selected from, lipids, vitamins, minerals, prebiotics, tics
and/or onal e.
FIGURES
Here and below in the Figures, l ments of the system according to the
invention are depicted. With reference to the included Figures, the system according to the
invention is described as follows.
Systemfor executing the process according to the invention
The present invention also relates to an apparatus or system specifically designed to
implement the process according to the invention. The system according to the invention is
preferably a modular system, in which three or more modules are in fluid connection with
each other. Herein, each module may be a separate unit or two or more modules may be
ated as a single unit. Preferably, each module is a separate unit and is distinguishable
as such in the system.
The system according to the invention is arranged to e two incoming liquid
compositions (e.g. animal skim milk, and a liquid ition comprising sweet whey
and/or acid whey), and to discharge a solid composition. In addition thereto, r liquid
and/or solid compositions may be received by the system or discharged from the system.
The system according to the invention comprises a first ultrafiltration module (1) comprising
an ultrafiltration membrane (lb). The first module is designed to receive the first liquid
composition, in particular animal skim milk as via a first inlet (la) to a first side of the UF
membrane (lb). For executing the process according to the invention, the first liquid
composition is preferably the animal skim milk as meant herein. In addition, the first module
(1) comprises a first outlet (lc) for rging an ultrafiltration retentate (UFRl) from the
first side of the UF membrane (lb) and a second outlet (ld) for discharging an ultrafiltration
te (UFPl) from the second side of the UF membrane he UF membrane (lb)
has two sides, one for receiving the incoming first liquid composition and rging the
UFRl, and one for discharging the UFPl. The UFPl thus comprises only material that has
ted through the UF membrane (lb). The UF membrane (lb) employed in the first
module can be any UF membrane known in the art, including ceramic membranes and
organic spiral wound membranes. The UF membrane (lb) has a molecular weight cut-off of
that enables proteins, such as whey proteins and casein, to remain in the retentate.
Preferably, the molecular weight cut-off is at most 25 kDa, more preferably at most 10 kDa,
and preferably of at least 2.5 kDa, more preferably at least 5 kDa.
The system according to the invention comprises a second ultrafiltration module (2),
2O comprising a ltration membrane (2b). The second ultrafiltration module (2) is
designed to receive the second liquid ition comprising sweet whey and/or acid whey
via a first inlet (2a) to a first side of the second UF membrane (2b). In addition, the second
ultrafiltration module (2) comprises a first outlet (2c) for discharging an ultrafiltration
retentate (UFR2) from the first side of the second UF membrane (2b) and a second outlet
(2d) for discharging an ultrafiltration permeate (UFP2) from the second side of the second
UF membrane (2b). The UF membrane (2b) employed in the ultrafiltration module (2) can
be any UF membrane known in the art, including ceramic membranes and organic spiral
wound membranes, preferably UF membrane (2b) is an c spiral wound membrane. UF
membrane (2b) has a molecular weight cut-off that s proteins, such as whey ns
and casein, to remain in the retentate. Preferably, the molecular weight cut-off is at most 25
kDa, more ably at most 10 kDa, and preferably of at least 2.5 kDa, more preferably at
least 5 kDa.
The system according to the invention comprises a mixing module (3) for mixing at least
two liquid streams, at least two solid streams (e. g. powders) or at least one liquid stream and
at least one solid stream, preferably for mixing at least two liquid streams. The mixing
module (3) preferably enables mixing of the UP retentate originating from ultraflltration
module (1), the UF retentate originating from ultraflltration module (2) and ally the
softened UFP originating from the polyvalent ion l unit (5).
The mixing module (3) is designed to receive the UF retentate ating from
ultraflltration module (1) via a first inlet (3a) and to receive the UF retentate originating
from ultraflltration module (2) via a second inlet (3b). The second module comprises an
outlet (3c) for discharging the mixture of UP retentates. In a preferred ment, the
mixing module (3) comprises a third inlet (3d) designed to receive the softened UFP
originating from the polyvalent ion removal unit (5), and the outlet (3c) is for discharging
the mixture of UP ates and the softened UFP, referred to as the combined product.
Alternatively, mixing of the mixture of UF retentates originating from mixing module (3)
with the softened UFP originating from the polyvalent ion removal unit (5) may be
accomplished in a te mixing module, which is ed to discharge the combined
product.
2O Mixing may be accomplished by merely combining the two or three incoming composition,
but preferably the mixing module (3) further comprises mixing means (3d). The mixing
means (3d) may be any means suitable for mixing two or three compositions known in the
art, such as “in pipe” (i.e. by the joining of two or three incoming pipes into one single
outgoing pipe), in a (balance) tank or vessel, in an agitated vessel, or by any industrial mixer
or blender known in the art. Suitable mixing means include means for mixing two or three
liquid compositions, e. g. c mixing or static mixing, or for mixing two or three solid
compositions (e.g. two powders), e.g. a dry blender such as a ribbon r, a paddle
blender, a tumble blender and a vertical blender, or at least one liquid composition and at
least one solid ition, preferably for mixing two or three liquid compositions. In an
especially preferred embodiment, the mixing means is “in pipe” or in a balance tank.
The mixing module (3) is arranged in the system after the first ultraflltration module (1) and
the second ultraflltration module (2). Outlet (lc) of the first ultraflltration module (1) is in
fluid connectivity with inlet (3a) of the mixing module (3) and outlet (2c) of the second
ultraflltration module (2) is in fluid connectivity with inlet (3b) of the mixing module (3)
The system according to the invention may comprise further modules or further features as
described here below.
The system according to the invention preferably ses a drying module (4) for drying
at least one liquid ition, preferably for drying the combined product. Drying module
(4) is designed to receive a liquid composition (e. g. the combined product) via an inlet (4a)
to a drying means (4b), and to discharge a solid composition via an outlet (4c) from the
drying means (4b). The drying means (4b) may be any means suitable for drying a liquid
ition known in the art, e.g. a spray dryer, a zed) bed dryer, a drum dryer, a
freeze dryer, a roller dryer, etc. In an especially preferred embodiment, the drying means
(4b) is a spray dryer.
The drying module (4) may be arranged in the system before the mixing module (3) or after
the mixing module (3), as long as it is arranged after the first ultraflltration module (1) and
the second ultraflltration module (2). In case the drying module (4) is arranged in between
the f1rstultraf11tration module (1) and/or the second ultraflltration module (2) and the mixing
2O module (3) at least one of the ultraflltration retentates ating from ltration module
(1) and/or (2) is dried prior to mixing. In case the third module is arranged after the mixing
module (3), the ultraflltration retentates are first mixed and then the mixture of the UP
retentates originating from mixing module (3) is dried.
Optionally, the system according to the invention comprises further drying module(s), each
for drying at least one liquid stream. Each drying module is designed to receive a liquid
composition via an inlet to a drying means, and to discharge a solid composition via an
outlet from the drying means. The drying means may be any means suitable for drying a
liquid composition known in the art, e.g. a spray dryer, a (fluidized) bed dryer, a drum dryer,
a freeze dryer, a roller dryer, etc. In an ally preferred embodiment, the drying means is
a spray dryer. A further drying module may be arranged in the system before the mixing
module (3) and after the second ultraflltration module (2), preferably in case the first drying
module (4) is arranged before the mixing module (3) and after the f1rstultraf11tration module
(1). As such, the ultrafiltration retentates discharged from both ultrafiltration modules (1)
and (10) are dried prior to mixing in the mixing module (3).
In a preferred ment, the system according to the invention comprises a polyvalent ion
removal module (5) for removing polyvalent ions from one or more ultrafiltration tes
(UFPs). The polyvalent ion removal module (5) comprises an inlet (5a) for receiving the one
or more UFPs, a polyvalent ion removal unit (5b), and an outlet (SC) for rging a
softened UFP. The polyvalent ion removal unit (5b) may comprise a means for removing
(significant amounts of) polyvalent ions (i.e. ions having a positive or negative charge of
two or more) and optionally for removing (significant amounts of) monovalent ions. The
means for ng ficant amounts of) monovalent ions may be joined with the
polyvalent ion removal unit (5b), or may be present in a separate monovalent ion removal
module (6). In case means for removing (significant amounts of) lent ions and means
for removing (significant amounts of) monovalent ions are present, those means may be a
single unit, capable of removing both polyvalent and monovalent ions, or preferably two
separate such units, one capable of removing polyvalent ions and one capable of removing
monovalent ions. The two separate such units are preferably present in two distinct modules,
a polyvalent ion l module (5) and a monovalent ion l module (6), wherein an
outlet (5c) of the polyvalent ion removal module (5) is in fluid connectivity with an inlet
(6a) of the monovalent ion removal module (6). The monovalent ion removal module (6)
ses an inlet (6a) for receiving the softened UFP, a monovalent ion removal unit (6b),
and an outlet (6c) for discharging a softened UFP, from which monovalent ions are
removed.
Any technique known in the art for removing polyvalent and for removing monovalent ions
may be used as means for removing polyvalent ions (5b) and means for removing
lent ions (6b). Conveniently, the monovalent ion removal unit(s) is/are selected from
an electrodialysis set-up (comprising ion exchange membranes and means for applying an
electric potential difference), an ion exchange set-up ising at least one column filled
with anionic and/or cationic resins), a salt itation set-up, a nanofiltration ne or
a diafiltration ne, or combinations thereof. In an preferred embodiment, polyvalent
ion removal module (5) comprises at least one ion exchange column comprising anion
and/or cation exchange resins as polyvalent ion removal unit (5b) and the monovalent ion
l module (6) comprises a nanofiltration membrane as monovalent ion removal unit
(6b). In case the monovalent ion removal module (6) comprises a tration membrane
as monovalent ion removal unit (6b), the monovalent ion removal module (6) is ed to
receive the softened UFP via a first inlet (6a) to a first side of the NF membrane (6b). In
on, the monovalent ion removal module (6) comprises a first outlet (6c) for
discharging a nanofiltration retentate from the first side of the NF membrane (6b) and a
second outlet (6d) for rging a nanofiltration permeate from the second side of the NF
membrane (6b). The NF membrane (6b) employed in the monovalent ion removal module
(6) can be any NF ne known in the art. Typically, a spiral wound membrane having
a molecular weight cut-off of at most 500 Da, preferably at most 300 Da, and of at least 100
Da, preferably at least 150 Da, is used. Preferably, the monovalent ion removal module (6)
ses means for enhancing nanofiltration with diafiltration, preferably this means is an
additional inlet (6e) for receiving diafiltration water.
In an especially preferred embodiment, the polyvalent ion removal module (5) a monovalent
ion removal module (6) together comprise three or preferably four modules, i.e. a
nanofiltration module (6-i) as monovalent ion l module (6), a salt precipitation
module (5-i) and a precipitate removal module (5-ii) as polyvalent ion removal modules (5)
and preferably a second nanofiltration module (6-ii) and/or an electrodialysis module (5-iii),
more preferably an electrodialysis module (5-iii). It is preferred that these modules are
arranged in such a way that:
- the nanofiltration module (6-i) is capable of receiving the one or more UFPs, removing
monovalent ions by ion through a nanofiltration membrane, and discharging a
nanofiltration te to the salt precipitation module (5-i),
- the salt precipitation module (5-i) is capable of receiving the nanofiltration permeate from
module (6-i), causing itation of salts, in particular salts sing polyvalent ions,
and discharging a liquid stream containing precipitates to the precipitate removal module
(5-ii),
- the precipitate removal module (5-ii) is capable of receiving the liquid stream containing
precipitates from module (5-i), removing the precipitates, preferably by filtration through
an ultrafiltration membrane, and discharging a ed UFP, preferably to the
electrodialysis module (5-iii),
- and preferably the electrodialysis module (5-iii) is e of receiving the softened UFP
from module (5-ii), removing monovalent and/or lent ions from the softened UFP
and rging a softened UFP.
The salt precipitation module (5-i) comprises means for causing precipitation of salts, in
particular salts sing polyvalent ions. Any que known in the art may be used as
means for causing precipitation of salts. Preferably, the technique for causing precipitation
of salts is selected from the addition of a strong base, such as sodium ide, pH
adjustment to a neutral pH, such as between 6 and 8, and increasing the temperature to
between 70 and 90°C, followed by sing the ature to a between 5 and 30°C. The
skilled person knows how to arrange the salt precipitation module (5-i) in order to perform
these techniques. The precipitate removal module (5-ii) is preferably an lltration
module, e of removing the precipitates from the liquid stream by ultraflltration, in
which the softened UFP may be discharged as ultraflltration permeate. The electrodialysis
module (5-iii) may comprise any electrodialysis set-up as known in the art. Within the
context of this embodiment, the electrodialysis module (5-iii) may be replaced by a second
nanofiltration module (6-ii), which is capable of receiving the softened UFP from module
(5-ii), removing lent ions from the softened UFP and discharging a softened UFP.
The outlet for discharging the softened UFP from module (5-ii), (5-iii) or (6-ii) is preferably
in fluid connectivity with inlet (3 d) of the mixing module (3).
In the system according to the invention, the polyvalent ion removal module (5) is
preferably arranged in between the first ultraflltration module (1) and/or the second
ultraflltration module (2) and the mixing module (3), more preferably the polyvalent ion
removal module (5) is arranged in between the first ultraflltration module (1) and/or the
second ultraflltration module (2) and the monovalent ion removal module (6), and the
monovalent ion removal module (6) is arranged in between the polyvalent ion removal
module (5) and the mixing module (3). Outlet (1d) of the f1rstultraf11tration module (1) and
outlet (2d) of the second ultraflltration module (2) are in fluid connectivity with inlet (5a) of
the polyvalent ion removal unit (5), and outlet (5c) of the polyvalent ion removal unit (5) is
in fluid connectivity with inlet (3d) of the mixing module (3), or more ably outlet (5c)
of the polyvalent ion removal unit (5) is in fluid connectivity with inlet (6a) of the
monovalent ion removal module (6) and outlet (6c) of the monovalent ion removal module
(6) is in fluid connectivity with inlet (3 d) of the mixing module (3).
In a further red embodiment, the system according to the invention ses one or
more concentration modules for concentrating (a) liquid stream(s), preferably at least two
concentration modules, one tration module (7) for concentrating the UF retentate
ating from the first ultrafiltration module (1) and one concentration module (8) for
concentrating the UF ate originating from the second ultrafiltration module (2).
Concentration module (7) comprises an inlet (7a) for receiving the UF retentate originating
from the first ultrafiltration module (1) to a means for concentrating (7b), a means for
concentrating (7b) and an outlet (7c) for discharging a concentrated UF retentate. Any
concentration technique known in the art may be used as means for concentrating (7b).
iently, the means for concentrating (7b) is selected from an evaporation set-up (e.g.
by increasing the temperature and/or ng the pressure) or a membrane filtration set-up
(e. g. a reverse osmosis membrane or a nanofiltration membrane), most preferably the means
for concentrating (7b) is a nanofiltration membrane. In case the concentration module (7)
comprises a nanofiltration membrane as means for concentrating (7b), the concentration
module (7) is designed to receive the UF retentate via a first inlet (7a) to a first side of the
NF membrane (7b). In addition, the concentration module (7) comprises a first outlet (7c)
for discharging a trated UF retentate as NF retentate from the first side of the NF
2O membrane (7b) and a second outlet (7d) for discharging a nanofiltration permeate from the
second side of the NF membrane (7b). The NF membrane (7b) employed in the
concentration module (7) can be any NF membrane known in the art. Typically, a spiral
wound membrane having a molecular weight cut-off of at most 500 Da, preferably at most
300 Da, and of at least 100 Da, preferably at least 150 Da, is used.
Concentration module (8) comprises an inlet (8a) for receiving the UF retentate originating
from the second ultrafiltration module (2) to a means for concentrating (8b), a means for
concentrating (8b) and an outlet (SC) for discharging a concentrated UF ate. Any
concentration technique known in the art may be used as means for concentrating (8b).
Conveniently, the means for concentrating (8b) is selected from an evaporation set-up (e.g.
by increasing the temperature and/or reducing the pressure) or a membrane ion set-up
(e. g. a reverse osmosis membrane or a nanofiltration membrane), most preferably the means
for concentrating (8b) is a tration ne. In case the concentration module (8)
comprises a nanofiltration membrane as means for trating (8b), the concentration
module (8) is designed to receive the UF retentate via a first inlet (8a) to a first side of the
NF membrane (8b). In addition, the tration module (8) comprises a first outlet (SC)
for discharging a concentrated UF retentate as NF retentate from the first side of the NF
membrane (8b) and a second outlet (8d) for discharging a nanofiltration permeate from the
second side of the NF membrane (8b). The NF membrane (8b) employed in the
concentration module (8) can be any NF membrane known in the art. Typically, a spiral
wound membrane having a molecular weight cut-off of at most 500 Da, preferably at most
300 Da, and of at least 100 Da, preferably at least 150 Da, is used.
In a further preferred embodiment, the system according to the invention ses means
for recycling (residual) water from outgoing streams to incoming streams. Residual water
may be obtained in the drying module (4), in the monovalent ion removal module (6) (e. g. as
nanofiltration permeate) and in each of the tration modules (7) and (8) (e.g. as
nanofiltration permeate). Preferably, at least one of the drying module (4), the monovalent
ion removal module (6) and the concentration modules (7) and (8) r comprises an
(additional) outlet for rging water from the module, more preferably, at least one of
the concentration s (7) and (8) comprises such an outlet. Most preferably, the drying
module (4), the lent ion removal module (6) and the concentration modules (7) and
(8) each comprise such an outlet. The residual water may be used to dilute any of the
incoming liquid itions, e.g. the first liquid composition and/or the second liquid
composition, or may be used as diafiltration water, e.g. in the monovalent ion removal
module (6). Preferably, the first ultrafiltration module (1) and/or the second ultrafiltration
module (2) and/or the monovalent ion removal module (6) further comprise an additional
inlet for receiving al water. The skilled person iates that the outlets for
discharging residual water are in fluid connectivity with the inlets for ing residual
water by a conduit, wherein optionally one or more collection tanks or further purification
means (e. g. reverse osmosis membranes) are integrated.
In a further preferred embodiment, the system according to the ion comprises means
for heat treating (9) and (10) a liquid composition. Any of the liquid compositions which are
led through the system according to the invention may suitably be heat treated, using any
heat treatment technique known in the art. Conveniently, the system according to the
invention comprises at least one of an eighth module for heat treating a liquid composition.
Such a heat treatment module comprises an inlet for receiving a liquid ition to a
means for heat treatment (9), a means for heat treatment and an outlet for discharging a heat
treated liquid composition. Any heat treatment technique known in the art may be used as
means for heat treatment, such as pasteurization or sterilization set-up. Preferably, a plate
heat exchanger (9, PHE) and/or a direct steam injection/infusion (10, D81) is used as heat
treatment means. Means for heat treating (13) the combined product originating from mixing
module (3) are installed before the drying module (4), which enables the heat ent of
the combined product originating from mixing module (3). Preferably the means for heat
ent (13) is a direct steam injector operating at a temperature of about 120 oC.
The system according to the invention may further comprise chilling means, preferably to
enable the system to operate at a temperature below 40 0C, more preferably between 3 oC
and 30 oC, most preferably between 5 oC and 20 oC. Each module may have a separate
chilling means, or a central chilling means may be installed to te the ature in
the entire system. ably, the chilling means are selected from cooling tower, heat
exchanger (plate or tubular, preferably in connection with the PHE used for heat treatment),
cooling by coolant (heat transfer fluid), pumpable ice technique.
Means for chilling (l l) the nanofiltration retentate originating from the first tration
module (7) are installed before the mixing module (3), which enables chilling of the
nanofiltration retentate originating from the first concentration module (7). Preferably the
means for chilling (l l) is a plate heat exchanger operating at a temperature of about 4 oC.
Means for chilling (12) the nanoflltration retentate ating from the second tration
module (8) are installed before the mixing module (3), which enables chilling of the
nanoflltration retentate originating from the second concentration module (8). Preferably the
means for chilling (12) is a plate heat exchanger operating at a ature of about 4 0C. It
is highly red that the plate heat exchangers that are used as heat treatment means (e.g.
operating at a temperature of about 80 0C) are in thermal connectivity with the plate heat
gers that are used as chilling means (e.g. operating at a temperature of about 4 oC).
ltration and diaflltration both require the presence of a nanofiltration membrane. To
accomplish diaflltration, the module requires an additional inlet for receiving water to the
first side of the nanofiltration membrane, as such enabling dilution and re-filtration of the
nanofiltration retentate.
All filtration modules preferably comprise means to facilitate the permeations of the solvent
and optionally small solutes through the membrane. Any means known in the art may be
used to accomplish easy permeation, such as using y or the application of
transmembrane pressure (TMP). TMP may be accomplished by pressurizing the first side of
the membrane (i.e. the ate side) or by depressurizing the second side of the membrane
(i.e. the permeate side). Suitably, a pump using tatic pressure to re the first side
of the membrane and/or a pump generating suction at the second side of the membrane is
used. Suitable pumps include centrifugal pumps and positive displacement pumps,
preferably centrifugal pumps are used.
In the system according to the invention, the different s are interconnected, i.e. the
outlet of one module is in fluid connectivity with the inlet of another module, preferably
using a conduit.
The system according to the invention preferably operates with 500 — 2500 kg, more
preferably 800 — 1800 kg, most preferably 1000 — 1400 kg dry matter of the first liquid
composition, ably of animal skim milk, incoming per hour. The system according to
the invention preferably operates with 1500 — 5000 kg, more preferably 2200 — 4000 kg,
most preferably 2600 — 3000 kg dry matter of the second liquid composition, preferably of
animal whey, ng per hour. The system according to the ion preferably es
with 750 — 4000 kg, more preferably 1000 — 3000 kg, most preferably 1500 — 2000 kg UF
retentate discharged from the ultrafiltration module(s) per hour from both incoming streams
combined. The process according to the invention preferably operates with 1000 — 5000 kg,
more preferably 1500 — 4000 kg, most preferably 2000 — 2500 kg UF permeate discharged
from the ultrafiltration module(s) per hour from both incoming streams combined.
The invention will now be rated by several examples which are not meant to limit the
invention in any manner.
EXAMPLES
Example I
400 kg of pasteurized cows’ skim milk with a casein to whey protein weight ratio of 80:20
was subjected to ultrafiltration over a Synder ST3 838 UF membrane having a MWCO of 10
kDa. Ultrafiltration was performed at a temperature between 8 and 10 0C, with a
transmembrane pressure of 2 bar and a VCF of about 2. The te was collected in a
flow rate of up to 260 L/h. 208 kg of a UF permeate (UFPl) and 211 kg of a UF retentate
(UFRl) was obtained. The compositions of the incoming skim milk and the products of the
ultrafiltration are given in table 1. The slight se in total weight of the final products
(UFRl and UFPl) compared to the incoming skim milk can be attributed to dilution of the
plant dead volume during the changeover from product to water during plant flushing. As
can be seen from the data of table 1, the UF retentate is enriched in proteins, s the UF
permeate is enriched in lactose.
Table I: Compositions ofexample I (in wi% based on total dry weight)
Component Cows’ skim milk UFRl UFPl
protein 36.2 51.7 0.0
Lactose 51.8 36.5 87.6
ash 8.7 8.4 9.1
- Na 0.46 0.35 0.70
- K 1.83 1.40 2.69
- Cl 1.13 0.66 1.61
- P 1.16 1.32 0.76
- Ca 1.37 1.67 0.80
- Mg 0.12 0.12 0.13
Example 2
1000 kg of rized sweet whey with whey proteins as the sole protein source was
subjected to ultrafiltration over a Synder ST3838 UF membrane having a MWCO of 10
kDa. Ultrafiltration was performed at a temperature between 10 and 12 0C, and with a
transmembrane pressure of 2 bar and a VCF of about 5. The permeate was collected in a
flow rate of up to 400 L/h. 818 kg of a UF permeate (UFP2) and 195 kg of a UF retentate
(UFR2) was obtained. The compositions of the incoming sweet whey and the products of the
ultraflltration are given in table 2. The slight increase in total weight of the final products
(UFRl and UFPl) compared to the incoming sweet whey can be attributed to dilution of the
plant dead volume during the changeover from product to water during plant flushing.
Table 2.‘ Compositions ofexample 2 (in wi% based on total dry weight)
Component Sweet whey UFR2 UFP2
n 9.7 35.1 0.0
e 76.9 50.0 87.4
ash 8.6 6.7 9.3
- Na 0.67 0.49 0.74
- K 2.58 1.92 2.84
- Cl 1.44 0.95 1.69
- P 0.82 0.58 0.73
- Ca 0.81 0.69 0.86
-Mg 0.14 0.10 0.15
Example 3
The UFPl of example 1 and the UFP2 of example 2 were ed in a weight ratio of
20/80 to obtain 799 kg of a combined UFP. The combined UFP was subjected to ion
exchange to produce a softened UFP, and subsequently to nanofiltration enhanced with
diaflltration. Ion ge employed an anionic resin charged with chloride ions and a
cationic resin charged with sodium ions, to exchange the lent ions for sodium and
chloride. Ion ge operated at a pH between 2.4 and 4.3 and a temperature between 5
and 10 oC. Nanoflltration employed a Synder NFX 3838 NF membrane having MWCO of
150 — 300 Da, operated at a temperature between 8 and 22 0C, and with a transmembrane
pressure of 2 bar. The te was collected in a flow rate of up to 400 L/h. Two
tration volumes of, 200 L of water were added sequentially when the retentate total
solids content reached 20%. The softened UFP was concentrated to a final total solid content
of about 20 %. 178 kg of a softened UFP concentrate was obtained as a nanofiltration
retentate (NFRl), together with 1225 kg of a nanofiltration permeate (NFPl). The
compositions of the incoming combined UFP and the products of the nanofiltration are
given in table 3. The great majority of the polyvalent ions were removed during ion
exchange and the great ty of the monovalent ions ended up in the NFPl. The softened
UFP concentrate (NFRl) contained almost exclusively lactose.
Table 3 .' Compositions ofexample 3 (in wi% based on total dry weight)
component Combined UFP NFRl softened UFP concentrate
(NFP1)
protein 0.0 0.0 0.0
lactose 86.8 97.2 11.2
ash 9.2 2.4 74.7
-Na 0.71 0.61 24.7
- K 2.66 0.32 9.8
- Cl 1.70 0.84 44.9
- P 0.75 0.23 0.34
- Ca 0.84 0.06 0.36
- Mg 014 0.00 0.00
Example 4
The UFRl of example 1 was concentrated and subjected to monovalent ion l by
nanofiltration over a Synder NFX 3838 NF membrane having MWCO of 150 — 300 Da.
Nanofiltration operated at a temperature between 8 and 20 0C, and with a transmembrane
re of 2 bar and VCF of about 2. The permeate was collected in a flow rate of up to 220
L/h. 108 kg of an UFRl concentrate as nanofiltration retentate (NFR2) was obtained,
together with 149 kg of a tration permeate (NFP2). Using nanofiltration, the UFRl is
concentrated to a total solid content of about 18 %. The composition of the NFR2 product of
the nanofiltration is given in table 4.
Table 4: Composition ofexample 4 (in wt% based on total dry weight)
component NFR2
protein 55.6
lactose 33.4
ash 7.8
- Na 0.26
- K 1.06
- Cl 0.27
- P 1.33
- Ca 1.70
- Mg 0.12
Example 5
The UFR2 of example 2 was concentrated and subjected to monovalent ion removal by
nanofiltration over a Synder NFX 3838 NF membrane having MWCO of 150 — 300 Da.
Nanofiltration operated at a temperature between 8 and 20 0C, and with a transmembrane
pressure of 2 bar. The permeate was ted in a flow rate of up to 400 L/h. 73 kg of an
UFR2 concentrate as nanofiltration retentate (NFR3) was obtained, together with 148 kg of
a nanofiltration permeate (NFP3). Using nanofiltration, the UFR2 is concentrated to a total
solid content of about 18 %. The composition of the NFR3 product of the tration is
given in table 5.
Table 5 .' Composition ofexample 5 (in wt% based on total dry )
ent NFR3
protein 35.8
lactose 51.0
ash 5.6
- Na 0.35
- K 0.82
- Cl 0.26
- P 0.64
- Ca 0.66
- Mg 0.11
Example 6
The aim is to e a mixture with a caseinzwhey ratio of 40:60. To this end, the UFRl
trate of example 4 (NFR2) is mixed with the UFR2 concentrate of example 5 (NFR3)
in a weight ratio of 59 kg:87.62 kg (based on a liquid composition) or in a weight ratio of
.59 kg: 16.45 kg (based on a dry composition) respectively, to e a mixture of UFRl
and UFR2. Besides the in table 6 mentioned constituents, the NFR2/NFR3 mixture
comprises NPN at 2.82 wt% and fat at 3.08 wt%.
Table 6: Composition ofexample 6 (in wt% based on total dry weight)
component NFR2/NFR3 mixture
protein 43.6
lactose 44.1
ash 6.5
- Na 0.32
- K 0.91
- Cl 0.27
- P 0.91
- Ca 1.07
- Mg 0.12
ing the UFRl concentrate of example 4 (NFR2) with the UFR2 concentrate of
example 5 (NFR3) in another selected weight ratio allows to obtain a mixture which
comprises casein to whey proteins in a desired ratio that falls within the claimed range.
Addition of a softened and optionally concentrated UF permeate (which is substantially free
from proteins) allows one to increase the amount of lactose to a desired level. The obtained
mixture can be spray-dried into a dry milk formula. For instance, addition of le
amounts of required nutrients and minerals, where needed, allows one to obtain a g-
up a with a 40:60 casein to whey protein ratio. Alternative mixtures of UFRl and
UFR2 were made to produce other mixtures of UFRl and UFR2 that comprised a 50:50 and
60:40 casein to whey ratio.
A softened UFP concentrate was recombined with the mixture of UFRl and UFR2 to
produce a composition with a 60:40 casein to whey n ratio. The softened UFP
concentrate was combined with the mixture of UFRl and UFR2. The UFRl concentrate of
example 4 (NFRZ), the UFR2 concentrate of example 5 (NFR3) and the softened UFP
concentrate (NFRl) of example 3 are mixed in a weight ratio of 88.51 kg:43.81 kg:188.77
kg (based on a liquid composition) or in a weight ratio of 15.88 3 kg:38.57 kg (based
on a dry composition) respectively, to produce a mixture of UFRl, UFR2 and softened UFP.
Besides the in table 7 mentioned constituents, the NFRl/NFRZ/NFR3 mixture comprises
NPN at 1.67 wt% and fat at 1.01 wt%.
Table 7.‘ Composition ofexample 7 (in wt% based on total dry weight)
component NFRl/NFRZ/NFR3 mixture
protein 18.8
lactose 74.9
ash 4.2
- Na 0.49
- K 0.58
- Cl 0.62
- P 0.56
- Ca 0.55
- Mg 0.05
Combining the softened UFP concentrate with the mixture of UFRl and UFR2 in other
selected weight ratios allows obtaining a mixture which comprises casein to whey ns
in a desired ratio that falls within the claimed range. The on of the softened and
optionally concentrated UF permeate (which is substantially free from ns) allows to
increase the amount of lactose to a higher levels as shown. The obtained mixture can be
dried into a dry milk formula. For instance, on of suitable amounts of required
nutrients and minerals, where needed, allows one to obtain a growing-up formula with a
60:40 casein to whey protein ratio. Alternative mixtures where made in a similar fashion to
obtain compositions that comprised a 50:50 and 40:60 casein to whey ratio.
Fractionation of reconstituted skim milk powder (SMP) and reconstituted sweet whey
powder (SWP) according to the invention was med using a combination of unit
operations, to prepare three types of infant nutrition base products. Reconstituted SMP and
reconstituted SWP were each subjected to UF (step 1), the retentates (UFRs) were subjected
to NF (step 2) and the permeates (UFPs) to poly- and monovalent ion removal (step 3).
Subsequently, the NF retentates (NFRs) from step 2 and the ed UFPs from step 3 are
combined in step 4. The compositions of SMP and SWP are given in table 8. Each step of
the process operated in steady state conditions for 4 — 10 h, during which an acceptable
average flux was achieved throughout the entire production sequence. Concentration factors
for the membrane ion steps are given in “mass concentration factor” (MCF), which are
calculated in the same way as a VCF, but using weight instead of volume. It can be assumed
that MCF = VCF, since all densities are close to that of water (1000 kg/m3) and all solids
present in the incoming stream end up in the retentate and permeate s. Over time,
slight ions were observed for the MCFs. Here below, the MCF range is given or the
deviation from the given value was less than 10 % at all times.
Table 8: Compositions ofSMP and SWP (per 100 gpowder)
Component SMP SWP
Protein (g) 35.2 13.5
Lactose (g) 53.3 76.6
ash (g) 7.83 8.38
- Na (mg) 397 666
- K (mg) 1690 3040
- Cl (mg) 979 1500
- P (mg) 1130 722
- Ca (mg) 1260 614
- Mg (mg) 106 130
-Zn (mg) 4.8 0.17
Step 1: Fractionation of reconstituted SMP and reconstituted SWP was performed using two
3838 10 kDa ultraf11tration membranes in series (Synder Filtration), to separate the feed
als into a protein enriched retentate and a lactose/milk salts enriched permeate at 10
°C . The reconstituted skim milk feed al (~2800 kg) at a total solids content of 8.64 %
w/w solid, pH of 6.9 at 5.8 °C, was fractionated using a mass concentration factor of 2,
while the reconstituted sweet whey feed material (~3 500 kg) at a total solids content of 6.1
% w/w solid, pH of 6.63 at 6.8 °C was fractionated using a mass concentration factor of 5.5
The macronutritional and mineral distribution of the liquid retentate and permeate streams
from UF1 and UF2 are presented in table 9. The permeates were collected with an average
flux of 10.54 kg/mZ/h (for SM) and 20.21 kg/mZ/h (for SW).
Table 9: Compositions of UFRS and UFPS (per 100 g)
Component UFRl (SM) UFPl (SM) UFR2 (SW) UFP2 (SW)
Total solids (g) 11.57 5.29 9.00 5.32
Protein (g) 6.36 0.14 3.47 0.16
Lactose (g) 4.14 4.68 4.57 4.71
ash (g) 0.97 0.48 0.66 0.44
- Na (mg) 38.5 34.0 38.2 32.6
-K(mg) 162.4 142.3 117.9 99.8
— Cl (mg) 79.1 91.7 91.7 107.9
— P (mg) 142.3 37.5 77.9 30.4
— Ca (mg) 190.5 32.8 79.1 19.2
— Mg (mg) 13.7 6.0 10.0 6.1
— Mn (mg) 0.004 0.00 0.001 0.00
— Fe (mg) 0.042 0.10 0.051 0.072
- Cu (mg) 0.014 0.07 0.033 0.010
-Zn (mg) 0.80 0.16 0.032 0.010
M: Post ultrafiltration of the reconstituted skim milk and sweet whey powder streams,
the uent retentates UFRl and UFR2 were concentrated and partially demineralised
using a 3838 0 Da nanofiltration (NF) membrane (GEA Filtration, Denmark). For
concentration and demineralisation of ~ 500 kg of UFRl (pH 6.82 at 6 °C) to 26 % w/w
solids content, NF1 used two NF membranes in series, while for tration and
demineralisation of ~ 640 kg UFR2 (pH 5.88 at 6.5 °C) to 28 % w/w solids content a single
NF membrane was used in NF2. NF1 operated within a mass concentration factor range of
WO 63494
1.8 — 2.2 while NF2 operated within a mass concentration factor range of 2.6 — 3. Both NFl
and NF2 were operated within the temperature range of 13-14 °C. The permeates were
collected with an average flux of 1.64 kg/mZ/h (for UFRl) and 9.64 kg/mZ/h (for UFR2).
The macronutritional and mineral distribution of the liquid retentate and permeate streams
from NFl and NF2 are presented in table 10. The process yielded for NFRl and NFR2 milk
protein concentrate (MPC50) and whey protein concentrate (WPC3 5) powders respectively.
Table 10: Compositions ofNFRS andNFPS (per 100 g)
Component NFRl (SM) NFPl (SM) NFR2 (SW) NFP2 (SW)
Total solids (g) 24.30 0.36 24.63 0.35
Protein (g) 12.8 0.08 9.45 0.08
Lactose (g) 9.67 0.05 13.65 0.05
ash (g) 1.66 0.23 1.29 0.28
- Na (mg) 51.2 23.6 51.7 52.7
- K (mg) 222.8 92.3 168.7 156.6
— Cl (mg) 55.3 92.9 109.4 87.4
- P (mg) 273.1 13.0 203.8 103.6
— Ca (mg) 381.2 2.02 210.6 79.0
— Mg (mg) 27.7 0.23 26.6 24.1
— Mn (mg) 0.008 0.00 0.002 0.00
— Fe (mg) 0.061 0.00 0.12 0.019
- Cu (mg) 0.021 0.007 0.068 0.009
— Zn (mg) 1.61 0.013 0.067 0.011
Sig: Milk and whey permeates from UFl and UF2 respectively were concentrated and
partially demineralised separately by NF3 using two 3838 150-300 Da nanofiltration (NF)
membranes in series (GEA Filtration, Denmark). For concentration and ralisation
~1000 kg of UFPl (pH 5.9 at 6.9 °C) was concentrated to 22 % w/w solids t. For
tration and demineralisation ~1000 kg of UFP2 (pH 5.6 at 6 °C) was concentrated to
22 % w/w solids content. For tration of both UFPl and UFP2, NF3 operated within a
mass concentration factor range of 3.5 — 4 at a ature of 10 °C. Average permeate
fluxes amounted to 9.73 kg/mZ/h (for UFPl) and 10.9 kg/mZ/h (for UFP2). The
macronutritional and mineral distribution of the liquid retentate and permeate streams from
NF3 are presented in table 11.
Post concentration and demineralisation of UFPl and UFP2 by NF3, both retentates were
subsequently indirectly heated to 82 °C using an indirect plate heat exchanger feeding a 250
L jacketed ess steel vessel. Once the retentate from NF3 was in the storage vessel the
pH was ed to 7.2 (at 82 °C) using a 30 % w/w NaOH solution, causing the
precipitation of calcium salts ily of phosphate and citrate. The precipitated solution
was held at 82 °C for 20 minutes to maXimise the precipitation reaction ed by g
to 20 °C using an indirect plate heat exchanger feeding a second 250 L jacketed stainless
steel vessel. The precipitated material was removed from the NF3 retentate stream (post
precipitation) by UF3 using two 3838 10 kDa ultraflltration nes in series (Synder
Filtration). UF3 operated within a mass concentration factor of 10 at a temperature of 20 °C.
The macronutritional and mineral distribution of the liquid retentate streams from UF3 are
presented in table 12. The process according to the invention yielded ~50 %
demineralisation in the UF3 retentates compared to UFPl and UFP2 on a dry matter basis.
The liquid retentate streams from UF3 were combined in a stainless steel vessel at 40 °C.
The compounded batch (65 kg total mass) constituted the UFR3 from skim milk and the
UFR3 from sweet whey in a mass ratio of 20:80 tively. The batch was subsequently
demineralised using a pilot electrodialysis plant (Pl EDR—Y, MemBrain). The endpoint of
the ralisation was determined based on the relationship between conductivity of the
demineralised lactose and the ash t therein (endpoint: conductivity < 1 ms; ash
t < 0.75 wt% based on dry matter). Once the endpoint of the demineralisation was
reached, the demineralised lactose concentrate stream was cooled to 5 °C followed by
determination of total solids content of the ED product as 16.62 % w/w.
Table I]: Compositions ofNFR3s andNFP3s (per 100 g)
ent NFR3 (SM) NFP3 (SM) NFR3 (SW) NFP3 (SW)
Total solids (g) 20.67 0.32 23.55 0.42
Protein (g) 0.33 0.09 0.37 0.09
Lactose (g) 19.28 0.00 18.59 0.00
ash (g) 1.07 0.24 1.08 0.30
-Na (mg) 58.6 24.0 65.59 33.41
-K(mg) 253.8 94.9 255.94 118.96
- Cl (mg) 68.0 106.9 80.05 132.15
-P(mg) 133.4 5.68 115.36 10.61
- Ca (mg) 125.4 1.80 100.31 1.06
- Mg (mg) 22.9 0.16 27.69 0.16
- Mn (mg) 0.0002 0.0002 0.0002 0.000
- Fe (mg) 0.00 0.0005 0.0231 0.0212
- Cu (mg) 0.006 0.007 0.0075 0.0078
- Zn (mg) 0.023 0.012 0.0402 0.016
Table 12: Compositions of UFR3s and UFP3s (per 100 g)
Component UFP3 (SM) UFP3 (SW) ED product
Total solids (g) 17.95 19.26 16.62
Protein (g) 0.30 0.35 0.33
Lactose (g) 16.78 17.98 16.17
ash (g) 0.87 0.93 0.12
- Na (mg) 159.9 142.2 18.4
- K (mg) 226.7 230.3 3.0
- Cl (mg) 64.9 79.5 2.4
-P(mg) 66.5 71.5 19.5
- Ca (mg) 15.0 36.9 7.9
- Mg (mg) 16.3 19.8 0.0
- Mn (mg) 0.00 0.00 0.00
- Fe (mg) 0.00 0.0204 0.00
- Cu (mg) 0.016 0.0078 0.00
- Zn (mg) 0.020 0.0168 0.00
Sip—4: The final phase in the process was the production of nutritionally balanced
infant/toddler nutrition using the materials prepared in the preceding steps (1 — 3). As such
the lactose concentrate solution produced in step 3 (ED product) was used as the liquid
stream to which the NFRl and NFR2 were added, giving the desired (legally required)
content and ratio of protein (casein/whey) and lactose for first-stage infant milk (IF), follow
on milk (F0) and growing up milk ). The streams were blended in the ratios
mentioned in table 13. At this stage the liquid concentrate stream comprising demineralised
lactose (from ED t), MPC (from NFRl) and WPC (from NFR2) was pre-heated to 50
°C followed by dosing of oil and GOS to meet the nutritional requirements. The liquid
concentrate infant formula streams were then heated treated at 85 °C for 5 min in an indirect
r heat exchanger (Mircothermics), homogenised ream from the heat treatment
at first and second stage pressures of 125 and 25 bar tively (at 60 °C), followed by
evaporation to 55 % w/w solids content in a single effect falling film evaporator, operating
at 55 °C, and spray drying using a single stage spray dryer equipped with 2 fluid nozzle
atomisation operating at an inlet and outlet temperature of 175 °C and 90 °C respectively.
The nutritional composition of the IF, F0 and GUTVI powders produced is outlined in Table
Note that all components mentioned in table 14, except for the fat and part of the
ydrates (GOS) originate from the skim milk and sweet whey ng materials. All
2O components in table 14 are either within the acceptable ranges for that component, or are
below those acceptable ranges. For those components who’s content is below acceptable,
fortification would be required to increase their content to within acceptable ranges. It is
important to note that none of the ned components, not even the polyvalent ions, are
present above their acceptable range, which would be unacceptable as taking out is
impossible, while adding one or a few components may happen straightforward. The
possibility of preparing different infant nutritional ts, all according to legal standards,
trates the versatility and flexibility of the s according to the invention.
Table 13: Blending ratios, expressed in kg ofliquid concentrate per 100 kg ofdry powder
Streams IF FO GUTVI
I\FR1 (kg) 43.49 55.74 56.33
I\FR2 (kg) 61.72 47.47 47.97
ED product (kg) 191.83 215.90 208.86
Table 14: Compositions ofIF, FO andCWpowders (per 100 g)
Component IF FO GU1V1
Moisture (g) 1.26 1.68 2.38
Protein (g) 11.5 11.69 11.56
Carbohydrate (g) 56.62 59.23 63
Fat (g) 28.71 25.49 21.3
Ash (g) 1.91 1.91 1.76
- Na (mg) 192 156 171
- K (mg) 290 278 240
- C1 (mg) 88.5 83.5 109.5
- P (mg) 310 300 285
- 804 (mg) 36 33 38
- 1 (mg) 37 36 37
- Se (Hg) 7.7 8.4 6.7
-Ca(mg) 354 351 318
_ Mg (mg) 41 39 34
-211 (mg) 1 1.1 1.06
Carnite (mg) 21.3 23.6 23.8
Choline (mg) 216 231 235
ol (mg) 39.9 47.4 50.4
Biotin (Hg) 10.7 11.4 11
Folic acid (Hg) 41.4 38.8 32.1
Pantothenic acid (mg) 231 288 284
Vitamin B1 (mg) 0.17 0.17 0.17
Vitamin 312 (Mg) 1.38 1.39 1.29
Bitamin B2 (mg) 1.23 1.2 1.27
Vitamin B6 (mg) 0.1205 0.1140 0.1288
Claims (23)
1. Process for treating animal skim milk and sweet whey and/or acid whey, comprising: (a) ultrafiltration (UFl) of a first liquid composition comprising animal skim milk with 70 — 90 wt% casein and 10 — 30 wt% whey proteins, based on total protein, over a first ltration ne haVing a molecular weight cut-off of 2.5 — 25 kDa using a volume concentration factor of 1.5 — 6 to obtain a retentate (UFRl) and a te (UFPl), (b) ultrafiltration (UF2) of a second liquid composition comprising sweet whey and/or acid whey over a second ultrafiltration membrane haVing a molecular 10 weight cut-off of 2.5 — 25 kDa using a volume concentration factor of 2 — 15 to obtain a retentate (UFR2) and a permeate , and (C) mixing the UF retentate originating from step (a) with the UP retentate ating from step (b) to obtain a mixture of UF retentates. 15 2. Process for treating animal skim milk and sweet whey and/or acid whey, comprising: (a) ultrafiltration (UFl) of a first liquid composition comprising animal skim milk with 70 — 90 wt% casein and 10 — 30 wt% whey proteins, based on total protein, over a first ultrafiltration membrane haVing a molecular weight cut-off of 2.5 — 25 kDa to obtain a retentate (UFRl) sing 35 — 65 wt% proteins and 20 — 2O 50 wt% lactose, based on dry weight, and a permeate (UFPl) comprising 0 — 5 wt% proteins and 70 — 98 wt% lactose, based on dry weight, (b) ultrafiltration (UF2) of a second liquid composition comprising sweet whey and/or acid whey over a second ultrafiltration membrane haVing a molecular weight cut-off of
2.5 — 25 kDa to obtain a retentate (UFR2) comprising 15 — 55 25 wt% proteins and 35 — 65 wt% lactose, based on dry weight, and a permeate (UFP2) sing 0 — 5 wt% proteins and 70 — 98 wt% lactose, based on dry weight, and (C) mixing the UF retentate originating from step (a) with the UP retentate originating from step (b) to obtain a mixture of UF retentates.
3. The process according to claim 1 or 2, wherein the animal skim milk of the first liquid composition comprises 75 — 85 wt% casein and 15 — 25 wt% whey proteins, based on total protein, ably about 80 wt% casein and 20 wt% whey protein, more preferably the animal skim milk composition comprises or is animal skim milk.
4. The process ing to any one of claims 1 — 3, n the sweet and/or acid whey 5 composition of the second liquid composition comprises 0 — 20 wt% casein and 80 — 100 wt% whey proteins, based on total protein, preferably 0 — 10 wt% casein and 90 — 100 wt% whey ns, more preferably 0 — 5 wt% casein and 95 — 100 wt% whey proteins, most preferably the whey composition ses or is sweet whey and/or acid whey.
5. The process according to any one of claims 1 — 4, further comprising: (d) removing polyvalent ions from the UFPl permeate originating from step (a), from the UFP2 permeate originating from step (b) or from a mixture of the UF permeates originating from step (a) and (b), to obtain at least one softened UP 15 permeate, and (e) mixing the at least one softened UF permeate from (d) with the UFRl retentate originating from step (a) and/or the UFRZ retentate originating from step (b) or the mixture of UF ates originating from step (c), preferably the mixture of UF retentates originating from step (c).
6. The process according to claim 5, further comprising: (f) removing monovalent ions from at least one of the softened UF permeates of step (d), preferably before mixing in step (e). 25
7. The process according to claim 5 or 6, further comprising (g) subjecting at least one of the softened UF permeates of (d) to a concentration step, preferably by reverse osmosis and/or nanofiltration, preferably prior to mixing in step (e). 30
8. The process according any one of claims 5 — 7, n the removal of polyvalent ions is accomplished by electrodialysis, ion ge and/or salt precipitation, and removal of monovalent ions is accomplished by nanoflltration or diaflltration.
9. The process according to any one of claims 1 — 8, further comprising: (h) drying of the UFRl ate originating from step (a), the UFR2 retentate originating from step (b) or the mixture of UP retentates originating from step (c), optionally before, during or after mixing with the softened UF permeate in 5 step (e), to obtain a dry powder.
10. The process according to claim 9, wherein the drying takes place before, during or preferably after mixing step (c). 10
11. The process according to any one of claims 1 — 10, further comprising: (i) a (heat) sterilization or pasteurization step of the mixture of UF retentates originating from step (c), preferably after step (e) and prior to step (h).
12. The process according to any one of claims 1 — 11, further comprising 15 (jl) monovalent ion removal and/or concentrating of the UFRl retentate originating from step (a) and/or the UFR2 retentate originating from step (b), prior to step (c), (e) or (h), preferably by reverse osmosis and/or nanoflltration, or (j2) monovalent ion l and/or trating of the mixture of UP retentates originating from step (c) prior to step (h), preferably by e osmosis and/or 20 nanoflltration.
13. The process according to any one of claims 1 — 10, wherein the mixture of UF retentates originating from step (c) is further processed into a nutritional product for providing nutrition to s.
14. The process according to any one of claims 1 — 13, wherein such an amount of the UFRl retentate originating from step (a) is mixed in step (c) with the UFR2 ate originating from step (b), that the mixture of UF retentates of step (c) is characterized by a casein to whey n weight ratio between 75 :25 and 30:70.
15. The process according to any one of claims 5 — 14, wherein water which originates from a tration step, preferably reverse osmosis and/or nanoflltration, performed on the UFRl retentate originating from step (a), the UFR2 retentate originating from step (b), the mixture of UF retentates originating from step c), or from the UFP1 permeate originating from step (a) and/or from the UFP2 permeate originating from step (b) or the softened UF permeate, is added to the first liquid composition and/or the second liquid composition.
16. The process according to any one of claims 5 – 15, wherein the softened UF permeate of step (d) comprises less than 40% of the polyvalent ions of the UFP1 permeate originating from step (a) and/or the UFP2 permeate originating from step (b), on dry weight basis, preferably less than 30%, more preferably less than 20%, most preferably 10 less than 10%.
17. The process according to any one of claims 5 – 16, wherein the ed UF permeate of step (d) comprises less than 80% of the monovalent ions of the UFP1 permeate ating from step (a) and/or the UFP2 permeate originating from step (b), on dry 15 weight basis, preferably less than 70%, more preferably less than 60%, most ably less than 50% and/or the UFR1 retentate comprises less than 80% of the monovalent ions of the UFR1 retentate originating from step (a) and/or the UFR2 retentate originating from step (b), on dry weight basis, preferably less than 70%, more preferably less than 60%, most ably less than 50%.
18. The process according to any one of claims 1-17, wherein the second liquid ition comprises at least 50 wt% sweet whey of the total whey, on total weight basis, preferably at least 60 wt%, more preferably at least 70 wt% or 80 wt%, most preferably at least 90 wt%.
19. A modular system, comprising: (1) a first ultrafiltration (UF) module, comprising (1a) an inlet for receiving a first liquid composition comprising 70 – 90 wt% casein and 10 – 30 wt% whey proteins, based on total protein, to a first 30 side of a first ultrafiltration membrane, (1b) the first ultrafiltration membrane, (1c) a first outlet for discharging an ultrafiltration ate (UFR1) from the first side of the first iltration membrane, and (1d) a second outlet for discharging an ultrafiltration permeate (UFPl) from the second side of the first ltration membrane; (2) a second ultrafiltration (UF) module, comprising (2a) an inlet for ing a second liquid composition sing sweet whey and/or acid whey to a first side of a second ultrafiltration membrane, (2b) the second ultrafiltration membrane, (2c) a first outlet for rging an ultrafiltration retentate (UFR) from the first side of the second ultrafiltration membrane, and (2d) a second outlet for discharging an ultrafiltration permeate (UFP) from the 10 second side of the second ultrafiltration membrane, (3) a mixing module, comprising (3 a) a first inlet for receiving the UF retentate originating from the first ultrafiltration module (1), (3b) a second inlet for receiving the UF retentate originating from the second 15 ultrafiltration module (2), and (3 c) an outlet for rging a mixture of UF retentates.
20. The modular system according to claim 19, further comprising: (5) a polyvalent ion removal module, comprising 2O (5a) an inlet for receiving the UFP originating from the ultrafiltration module (1), receiving the UFP originating from the ultrafiltration module (2), or a mixture f, (5b) means for removing polyvalent ions, and (5c) an outlet for discharging a softened UF permeate, and 25 (6) a monovalent ion removal , comprising (6a) an inlet for receiving the softened UFP originating from the polyvalent ion removal module (5) to a first side of the nanofiltration membrane, (6b) a nanofiltration membrane, (6c) a first outlet for discharging a nanofiltration retentate (NFR) from the first 30 side of the nanofiltration membrane, and (6d) a second outlet for discharging a nanofiltration permeate (NFP) from the second side of the nanofiltration membrane, wherein the mixing module (3) further comprises (3d) a third inlet for receiving the NF retentate originating from the lent ion removal module (6).
21. A process according to claim 1, substantially as herein described or exemplified with 5 reference to the accompanying drawings.
22. A process according to claim 2, ntially as herein described or exemplified with reference to the accompanying drawings. 10
23. A system according to claim 19, substantially as herein described or exemplified with reference to the anying drawings. WO 63494
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/NL2013/050249 WO2014163486A1 (en) | 2013-04-03 | 2013-04-03 | Process and system for preparing dry milk formulae |
NLPCT/NL2013/050249 | 2013-04-03 | ||
PCT/NL2014/050203 WO2014163494A1 (en) | 2013-04-03 | 2014-04-03 | Process and system for preparing dry milk formulae |
Publications (2)
Publication Number | Publication Date |
---|---|
NZ712768A NZ712768A (en) | 2021-02-26 |
NZ712768B2 true NZ712768B2 (en) | 2021-05-27 |
Family
ID=
Similar Documents
Publication | Publication Date | Title |
---|---|---|
AU2014250177B2 (en) | Process and system for preparing dry milk formulae | |
AU2014250178B2 (en) | Process and system for preparing dry milk formulae | |
US10674739B2 (en) | Method for processing animal skim milk | |
ES2782473T3 (en) | Method to produce a starting formula base | |
EP2825058B1 (en) | Process for the humanization of animal skim milk and products obtained thereby | |
NZ712768B2 (en) | Process and system for preparing dry milk formulae | |
NZ712773B2 (en) | Process and system for preparing dry milk formulae |