Manufacturing of bupivacaine multivesicular liposomes

Abstract

The present disclosure relates to a new and improved large scale commercial manufacturing process of making bupivacaine multivesicular liposomes (MVLs) comprising DPEC, DPPG, cholesterol and tricapryl

Description

MANUFACTURING OF BUPIVACAINE MULTIVESICULAR LIPOSOMESINCORPORATION BY REFERENCE TO ANY PRIORITY APPLICATION

[0001] The present application claims the benefit of priority to U.S. Ser. Nos. 63 / 649828, 63 / 649872 and 63 / 649846, all filed May 20, 2024, each of which is incorporated by reference in its entirety.BACKGROUNDField

[0002] This disclosure relates generally to commercial manufacturing processes for making bupivacaine multivesicular liposomes.Description of the Related Art

[0003] Bupivacaine is a versatile drug that has been shown to be efficacious for a wide variety of indications, including: local infiltration, peripheral nerve block, sympathetic nerve block, and epidural and caudal blocks. It may be used in pre-, intra- and post-operative care settings. Bupivacaine encapsulated multivesicular liposomes product (Exparel®) has been approved in the US and Europe for use as postsurgical local analgesia and as an interseal ene brachial plexus nerve block to produce postsurgical regional analgesia, providing significant long- lasting pain management across various surgical procedures. Particularly, Exparel® has had great success in the market in part due to the ability to locally administer bupivacaine multivesicular liposomes (MVLs) at the time of surgery and extend the analgesic effects relative to other non- liposomal formulations of bupivacaine. Such extended release properties of bupivacaine MVLs allow patients to control their post-operative pain without or with decreased use of opioids. Given the addictive nature of opioids and the opioid epidemic that has been affecting countries around the world, there is an urgent need for new and improved commercial scale productions of Exparel® to meet the substantial and growing market demand.SUMMARY

[0004] One aspect of the present disclosure relates to a batch comprising a composition of bupivacaine encapsulated multivesicular liposomes (MVLs). the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise 1, 2-dierucoylphosphatidylcholine (DEPC), 1, 2-dipalmitoyl-sn-glycero-3-phospho-rac-(l -glycerol) (DPPG) or a salt thereof, cholesterol, and tricaprylin; andan aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL; wherein the batch has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L. about 150 to about 280 L or about 200 to about 260 L); wherein the batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from two or more aliquots of the batch using a rotator-facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date; and wherein the rate of change in the cumulative percentage release of bupivacaine of the batch at the 24-hour time point is at least 0.05% / month after storage of the aliquots at 2°C to 8°C for about 12 months.

[0005] A second aspect of the present disclosure relates to a batch comprising a composition of bupivacaine encapsulated multivesicular liposomes (MVLs), the composition comprising: bupivacaine residing inside a plurality' of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise 1, 2-dierucoylphosphatidylcholine (DEPC), 1, 2-dipalmitoyl-sn-glycero-3-phospho-rac-(l -glycerol) (DPPG) or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; and the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL; wherein the batch has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein the batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from two or more aliquots of the batch using a rotator-facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date; and wherein the rate of change in the cumulative percentage release of bupivacaine at the 48- hour time point is no less than -0.3% / month after storage of the aliquots at 2°C to 8°C for about 12 months.

[0006] A third aspect of the present disclosure relates to a batch comprising a composition of bupivacaine encapsulated multivesicular liposomes (MVLs), the composition comprising:bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise 1, 2- dierucoylphosphatidylcholine (DEPC), 1, 2-dipalmitoyl-sn-glycero-3-phospho-rac-(l- glycerol) (DPPG) or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; and the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL; wherein the batch has a volume of at least 200 liters (for example about 220 liters, 240 liters, 260 liters, 280 liters or 300 liters); wherein the batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from six aliquots of the batch using a rotator- facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date; and wherein the rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.1% / month after storage of the aliquots at 2°C to 8°C for about 12 months.

[0007] A fourth aspect of the present disclosure relates to a batch comprising a composition of bupivacaine encapsulated multi vesicular liposomes (MVLs), the composition comprising: bupivacaine residing inside a plurality' of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise 1, 2- dierucoylphosphatidylcholine (DEPC), 1, 2-dipalmitoyl-sn-glycero-3-phospho-rac-(l- glycerol) (DPPG) or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; and the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL; wherein the batch has a volume of at least 200 liters (for example about 220 liters, 240 liters, 260 liters, 280 liters or 300 liters); wherein the batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from six aliquots of the batch using a rotator- facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date; andwherein the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.25% / month after storage of the aliquots at 2°C to 8°C for about 12 months.

[0008] A fifth aspect of the present disclosure relates to a process for preparing a batch of bupivacaine encapsulated multivesicular liposomes (MVLs). the process comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water-immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water-immiscible solvent solution comprises l,2-dipalmitoyl-sn-glycero-3- phospho-rac-(l -glycerol) (DPPG) or a salt thereof, 1.2-dierucoylphosphatidylcholine (DEPC), tricaprylin and cholesterol, and wherein either the first aqueous solution or the solvent solution comprises bupivacaine;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a water-in-oil-in-water second emulsion, wherein the second aqueous solution comprises lysine and at least one an osmotic agent;(c) substantially removing the volatile water-immiscible solvent from the waterin-oil-in-water second emulsion by sparging the water-in-oil-in-water second emulsion to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is at least 190 L / min (for example, about 200 to about 400 L / min);(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow rate is at least 190 L / min (for example, about 200 to about 350 L / min); and(f) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a batch of aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from 12 mg / mL to 17 mg / mL; wherein the batch has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L): wherein the batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from two or more aliquots of the batch using a rotator-facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date; andwherein a rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.05% / month after storage of the aliquots at 2°C to 8°C for about 12 months.

[0009] A sixth aspect of the present disclosure relates to a process for preparing a batch of bupivacaine encapsulated multivesicular liposomes (MVLs). the process comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water-immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water-immiscible solvent solution comprises l,2-dipalmitoyl-sn-glycero-3- phospho-rac-(l -glycerol) (DPPG) or a salt thereof, 1.2-dierucoylphosphatidylcholine (DEPC), tricaprylin and cholesterol, and wherein either the first aqueous solution or the solvent solution comprises bupivacaine;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a water-in-oil-in-water second emulsion, wherein the second aqueous solution comprises lysine and at least one an osmotic agent;(c) substantially removing the volatile water-immiscible solvent from the waterin-oil-in-water second emulsion by sparging the water-in-oil-in-water second emulsion to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is at least 190 L / min (for example, about 200 to about 400 L / min);(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow rate is at least 190 L / min (for example, about 200 to about 350 L / min); and(f) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a batch of aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from 12 mg / mL to 17 mg / mL; wherein the batch has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L): wherein the batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from two or more aliquots of the batch using a rotator-facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date; andwherein a rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.3% / month after storage of the aliquots at 2°C to 8°C for about 12 months.

[0010] A seventh aspect of the present disclosure relates to a process for preparing a batch of bupivacaine encapsulated multivesicular liposomes (MVLs), the process comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water-immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water-immiscible solvent solution comprises bupivacaine, 1,2-dipalmitoyl-sn- glycero-3-phospho-rac-(l -glycerol) (DPPG) or a salt thereof. 1,2- dierucoylphosphatidylcholine (DEPC), tricaprylin and cholesterol;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a water-in-oil-in-water second emulsion, wherein the second aqueous solution comprises lysine and dextrose;(c) substantially removing the volatile water-immiscible solvent from the water- in-oil-in-water second emulsion by sparging the water-in-oil-in-water second emulsion to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 400 L / min);(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow rate is at least 190 L / min (e.g., about 200 to 350 L / min); and(1) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a batch of aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from 12 mg / mL to 17 mg / mL; wherein the batch has a volume of at least 200 liters (for example about 220 liters, 240 liters, 260 liters, 280 liters or 300 liters); wherein the batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from six aliquots of the batch using a rotator- facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date; andwherein the rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.1% / month after storage of the aliquots at 2°C to 8°C for about 12 months.

[0011] An eighth aspect of the present disclosure relates to a process for preparing a batch of bupivacaine encapsulated multivesicular liposomes (MVLs), the process comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water-immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water-immiscible solvent solution comprises bupivacaine, 1,2-dipalmitoyl-sn- glycero-3-phospho-rac-(l -glycerol) (DPPG) or a salt thereof. 1,2- dierucoylphosphatidylcholine (DEPC), tricaprylin and cholesterol;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a water-in-oil-in-water second emulsion, wherein the second aqueous solution comprises lysine and dextrose;(c) substantially removing the volatile water-immiscible solvent from the water- in-oil-in-water second emulsion by sparging the water-in-oil-in-water second emulsion to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 400 L / min);(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 350 L / min); and(f) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a batch of aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from 12 mg / mL to 17 mg / mL; wherein the batch has a volume of at least 200 liters (for example about 220 liters, 240 liters, 260 liters, 280 liters or 300 liters); wherein the batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from six aliquots of the batch using a rotator- facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date; andwherein the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point no less than -0.25% / month after storage of the aliquots at 2°C to 8°C for about 12 months.

[0012] A ninth aspect of the present disclosure relates to a process for preparing bupivacaine encapsulated multivesicular liposomes (MVLs), the process comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water-immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water-immiscible solvent solution comprises at least one phosphatidyl choline, at least one phosphatidyl glycerol, cholesterol, and at least one neutral lipid, and wherein either the first aqueous solution or the solvent solution comprises bupivacaine;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a water-in-oil-in-water second emulsion, wherein the second aqueous solution comprises lysine and at least one osmotic agent;(c) substantially removing the volatile water-immiscible solvent from the water- in-oil-in-water second emulsion by sparging the water-in-oil-in-water second emulsion at a temperature of about 18°C to about 20°C to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 400 L / min);(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 350 L / min); and(f) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a final aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from about 12 mg / mL to about 17 mg / rnL; wherein the final aqueous suspension of bupivacaine encapsulated MVLs has a volume of at least 100, 110 or 120 L (for example, about 120 to 300 L, about 150 to about 280 L, about 200 to about 260 L, about 320 to about 500 L, or about 350 to about 450 L); and wherein the process has a bupivacaine MVL product yield of at least about 75%.

[0013] A tenth aspect of the present disclosure relates to batches comprising compositions of bupivacaine encapsulated multivesicular liposomes (MVLs), the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise 1, 2-dierucoylphosphatidylcholine (DEPC), 1, 2-dipalmitoyl-sn-glycero-3-phospho-rac-(l -glycerol) (DPPG) or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL; wherein the batches are manufactured within a period of six months, and the batches each has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from two or more aliquots of each batch using a rotator- facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and an average rate of change in the cumulative percentage release of bupivacaine of the batches at the 24-hour time point is at least 0.05% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months; alternatively or additionally, each batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from two or more aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and an average rate of change in the cumulative percentage release of bupivacaine of the batches at the 48-hour time point is no less than -0.3% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months.

[0014] An eleventh aspect of the present disclosure relates to batches comprising compositions of bupivacaine encapsulated MVLs, the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise DEPC. DPPG or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL;wherein the batches are manufactured within a period of six months, and the batches each has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from two or more aliquots of each batch using a rotator- facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and an average change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.5% after storage of the aliquots of each batch at 2°C to 8°C for about 12 months; alternatively or additionally, each batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from two or more aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and an average change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -5% after storage of the aliquots of each batch at 2°C to 8°C for about 12 months.

[0015] A twelfth aspect of the present disclosure relates to batches comprising compositions of bupivacaine encapsulated MVLs. the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise DEPC, DPPG or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL; wherein the batches are manufactured within a period of three months, and the batches each has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from six aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.05% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months; alternatively or additionally, each batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from six aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of thealiquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.3% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months; wherein the average rate of change in the cumulative percentage release of bupivacaine is based on two to five batches, and at least one batch is manufactured 10 or more days apart from at least one other batch.

[0016] A thirteenth aspect of the present disclosure relates to batches comprising compositions of bupivacaine encapsulated MVLs. the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise DEPC, DPPG or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL; wherein the batches are manufactured within a period of three months, and the batches each has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from six aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and an average change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.5% after storage of the aliquots of each batch at 2°C to 8°C for about 12 months; alternatively or additionally, each batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from six aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and an average change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -5% after storage of the aliquots of each batch at 2°C to 8°C for about 12 months; wherein the average change in the cumulative percentage release of bupivacaine is based on two to five batches, and at least one batch is manufactured 10 or more days apart from at least one other batch.

[0017] A fourteenth aspect of the present disclosure relates to a process for preparing a plurality of batches of bupivacaine encapsulated MVLs, the process of manufacturing a batch of the plurality of batches comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water- immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water- immiscible solvent solution comprises DEPC, DPPG or a salt thereof, cholesterol, and tri caprylin, and wherein either the first aqueous solution or the solvent solution comprises bupivacaine;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a water- in-oil-in-water second emulsion, wherein the second aqueous solution comprises lysine and at least one an osmotic agent;(c) substantially removing the volatile water-immiscible solvent from the water-in-oil-in- water second emulsion by sparging the water-in-oil-in-water second emulsion to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 400 L / min);(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 350 L / min); and(1) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a batch of aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from 12 mg / mL to 17 mg / mL; manufacturing a plurality of batches according to the steps of (a)-(f); wherein the plurality of batches are manufactured within a period of six months and the batches each has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from two or more aliquots of each batch using a rotator- facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and an average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.05% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months;altematively or additionally, each batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from two or more aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.3% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months.

[0018] A fifteenth aspect of the present disclosure relates to a process for preparing a plurality of batches of bupivacaine encapsulated MVLs, the process comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water- immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water- immiscible solvent solution comprises DEPC, DPPG or a salt thereof, cholesterol, and tri caprylin, and wherein either the first aqueous solution or the solvent solution comprises bupivacaine;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a water- in-oil-in-water second emulsion, wherein the second aqueous solution comprises lysine and at least one an osmotic agent;(c) substantially removing the volatile water-immiscible solvent from the water-in-oil-in- water second emulsion by sparging the water-in-oil-in-water second emulsion to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 400 L / min);(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 350 L / min); and(f) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a batch of aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from 12 mg / mL to 17 mg / mL; manufacturing a plurality of batches according to the steps of (a)-(f); wherein the batches are manufactured within a period of six months, and the batches each has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L);wherein each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from two or more aliquots of each batch using a rotator- facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and an average change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.5% after storage of the aliquots of each batch at 2°C to 8°C for about 12 months; alternatively or additionally, each batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from two or more aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and an average change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -5% after storage of the aliquots of each batch at 2°C to 8°C for about 12 months.

[0019] A sixteenth aspect of the present disclosure relates to a process for preparing a plurality of batches of bupivacaine encapsulated MVLs, the process of manufacturing a batch of the plurality of batches comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water- immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water- immiscible solvent solution comprises bupivacaine. DEPC. DPPG or a salt thereof, cholesterol;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a water- in-oil-in-water second emulsion, wherein the second aqueous solution comprises lysine and dextrose;(c) substantially removing the volatile water-immiscible solvent from the water-in-oil-in- water second emulsion by sparging the water-in-oil-in-water second emulsion to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 400 L / min);(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 350 L / min); and(f) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a batch of aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from 12 mg / mL to 17 mg / mL;manufacturing a plurality of batches according to the steps of (a)-(f) ; wherein the plurality of batches are manufactured within a period of three months and the batches each has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from six aliquots of each batch using a rotator-facilitated in vitro release assay, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and an average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.05% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months; alternatively or additionally, each batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from six aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.3% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months; wherein the average rate of change in the cumulative percentage release of bupivacaine is based on two to five batches, and at least one batch is manufactured 10 or more days apart from at least one other batch.

[0020] A seventeenth aspect of the present disclosure relates to a process for preparing a plurality of batches of bupivacaine encapsulated MVLs, the process of manufacturing a batch of the plurality of batches comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water- immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water- immiscible solvent solution comprises bupivacaine, DPPG or a salt thereof, DEPC, tricaprylin and cholesterol, and wherein either the first aqueous solution or the solvent solution comprises bupivacaine;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a waterin-oil-in-water second emulsion, wherein the second aqueous solution comprises lysine and dextrose;(c) substantially removing the volatile water-immiscible solvent from the water-in-oil-in- water second emulsion by sparging the water-in-oil-in-water second emulsion to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 400 L / min);(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 350 L / min); and(f) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a batch of aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from 12 mg / mL to 17 mg / mL; manufacturing a plurality of batches according to the steps of (a)-(f); wherein the batches are manufactured within a period of three months, and the batches each has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from six aliquots of each batch using a rotator-facilitated in vitro release assay, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and an average change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.5% after storage of the aliquots of each batch at 2°C to 8°C for about 12 months; alternatively or additionally, each batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from six aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and an average change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -5% after storage of the aliquots of each batch at 2°C to 8°C for about 12 months; wherein the average change in the cumulative percentage release of bupivacaine is based on two to five batches, and at least one batch is manufactured 10 or more days apart from at least one other batch.

[0021] An eighteenth aspect of the present disclosure relates to a process for detecting a filter integrity failure during a process for preparing bupivacaine encapsulated multivesicular liposomes (MVLs), the process comprising: performing microfiltration and diafiltration using a crossflow filtration system that is configured to switch between microfiltration and diafiltration mode, wherein thecrossflow filtration system comprises a plurality of independently operating crossflow modules, each crossflow module comprises at least one filter array, and each filter array comprises a plurality of hollow fiber filters, wherein the crossflow filtration system further comprises at least one turbidity sensor downstream of the at least one filter array for detection of loss of filter integrity; detecting an abnormal turbidity value by the at least one turbidity sensor, wherein the abnormal turbidity value is a value above a threshold value; and testing one or more filters of the at least one filter array for a potential filter integrity failure by successively deactivating individual filters of the one or more filters and measuring turbidity by the at least one turbidity sensor while each individual filter is deactivated until a normal turbidity value is detected, wherein a normal turbidity value is a value below the threshold value.

[0022] The process can also include, in response to detecting a normal turbidity value, identifying the individual filter that was deactivated when the normal turbidity value was detected as a potentially damaged filter. The process can also include testing the potentially damaged filter by reactivating the potentially damaged filter and measuring turbidity by the at least one turbidity sensor while the potentially damaged filter is active, and in response to measuring an abnormal turbidity value when the potentially damaged filter is active after reactivation, determining that the potentially damaged filter is a damaged filter and deactivating the damaged filter.

[0023] A further aspect of the present disclosure relates to a batch comprising a composition of bupivacaine encapsulated multivesicular liposomes (MVLs), prepared by any one of the embodiments of the processes as described herein.

[0024] A further aspect of the present disclosure relates to a composition of bupivacaine encapsulated multivesicular liposomes (MVLs), prepared by any one of the embodiments of the processes as described herein.

[0025] A further aspect of the present disclosure relates to a method of treating or ameliorating pain in a subject in need thereof, comprising administering the composition of bupivacaine MVLs as described herein to the subject.

[0026] A further aspect of the present disclosure relates to batches comprising compositions of bupivacaine MVLs produced by any one of the embodiments of the processes described herein.

[0027] In addition to the features described above, additional features and variations will be readily apparent from the following descriptions of the drawings and exemplary embodiments. It is to be understood that these drawings depict typical embodiments, and are not intended to be limiting in scope.BRIEF DESCRIPTION OF THE DRAWINGS

[0028] FIG. 1A illustrates a process flow chart of the formation of an initial aqueous suspension bupivacaine MVLs and solvent removal according to an embodiment of the manufacturing process described herein.

[0029] FIG. IB illustrates a process flow chart of additional steps of concentration, diafiltration and solvent removal, and additional concentration of the initial aqueous suspension of bupivacaine MVLs according to an embodiment of the manufacturing process described herein.

[0030] FIG. 2 A illustrates a schematic diagram as an embodiment of a system for performing a manufacturing process.

[0031] FIG. 2B illustrates a schematic diagram of a portion of the system of Figure 2A depicting a crossflow module having an alternative arrangement of turbidity sensors.

[0032] FIG. 2C illustrates a process flow chart of detecting filter integrity failures and adjusting operation of the filtration system according to an embodiment of the manufacturing process described herein.

[0033] FIG. 3A is a line chart illustrating the average rate of change in cumulative percentage release of bupivacaine at 24-hour time point as a function of time, comparing batch samples according to certain embodiments of the present disclosure with batch samples manufactured by two known processes.

[0034] FIG. 3B is a line chart illustrating the average rate of change in cumulative percentage release of bupivacaine at 48-hour time point as a function of time, comparing bupivacaine MVLs batch samples according to certain embodiments of the present disclosure with bupivacaine MVLs batch samples manufactured by two known processes.

[0035] FIG. 4A is a line chart illustrating the average cumulative percentage release of bupivacaine at 24-hour time point at 0 and 12 months, comparing bupivacaine MVLs batch samples according to certain embodiments of the present disclosure with bupivacaine MVLs batch samples manufactured by two known processes.

[0036] FIG. 4B is a line chart illustrating the average cumulative percentage release of bupivacaine at 48-hour time point at 0 and 12 months, comparing bupivacaine MVLs batch samples according to certain embodiments of the present disclosure with bupivacaine MVLs batch samples manufactured by two known processes.

[0037] FIGs. 5A through 5F is a table illustrating the cumulative percentage release of bupivacaine at 24-hour and 48-hour after storage of bupivacaine MVLs samples at 5 °C for 12 months, and the samples were produced by the 45 L process.

[0038] FIG. 6 is a table illustrating the cumulative percentage release of bupivacaine at 24-hour and 48-hour after storage of bupivacaine MVLs samples at 5 °C for 12 months, and the samples were produced by the UK 200 L process.

[0039] FIG. 7 is a table illustrating the cumulative percentage release of bupivacaine at 24-hour and 48-hour after storage of bupivacaine MVLs samples at 5 °C for 12 months, and the samples were produced by the new process as described according to certain embodiments of the present disclosure.DETAILED DESCRIPTION

[0040] Embodiments of the present disclosure relate to new and improved commercial scale manufacturing processes for making bupivacaine encapsulated MVLs. The newly developed processes provide for an increased product yield as compared to prior processes used for the manufacturing of Exparel®, which are disclosed in U.S. Patent No. 9,585,838, also referred to as the “45 L process”), and U.S. Patent No. 1 1,033,495 (also referred to as the “UK 200 L process”), and U.S. Patent Application Publication No. 2022 / 0304932, each of which is incorporated by reference in its entirety7. The 45 L process was approved by the FDA in 2012, has an average yield of about 75% and produces about 2.4K of vials of Exparel® product in 2023. The UK 200 L process was approved by the FDA in 2021, has an average yield of about 73% and produces about 1 OAK vials of Exparel® product. As described in detail herein, certain embodiments of the present disclosure relate to a new and improved commercial process of making bupivacaine MVLs, has an average of about 82% yield, and produces up to 14.4K vials of Exparel® product, which is a 37% increase of production from the UK 200 L process. Additional embodiments of the present disclosure relate to additional process improvements and optimizations which may result in at least 8 folds increase in manufacturing scale compared to the 45 L process.

[0041] Furthermore, batches of Exparel® produced by the improved commercial processes have demonstrated improved stability based on a rotator facilitated in vitro release assay (IVRA) test during stability studies conducted at about 5°C for at least 12 months. Currently, Exparel® US product has a shelf life of 24 months based on the IVRA test performed at 5°C at the following seven time points: 0 months, 3 months, 6 months, 9 months, 12 months, 18 months and 24 months. At each time point, the IVRA test detects at least the 24-hour and 48-hour cumulative percentage release of bupivacaine. For commercial lots, the IVRA test also detects the 4-hour and 168-hour cumulative percentage release of bupivacaine. The Exparel® product specification requires that the average cumulative percentage release of bupivacaine is 46%-7I% at 24-hour and 60%-85% at 48-hour. It has been observed that during stability studies, the average cumulative percentage release of bupivacaine at 24-hour usually has a more pronounced decreasein the first 12 months, in particularly the first 6 months. Then the rate of decrease slows down during the second 12 months. It is important that the IVRA test results remain within the product specification during the shelf life of the product. As such, the flatter the trend line illustrating the rate of change in the cumulative percentage release of bupivacaine during the first 12 months, the more likely that the product will meet the IVRA specification during the entire 24 months. It has been observed that batches containing compositions of bupivacaine MVLs produced by the new process described herein have a flatter trend line illustrating the rate of change in the cumulative percentage release of bupivacaine during the first 12 months, as compared to the trend lines of the products produced by the 45L process and the UK 200L process. This surprising and unexpected observation may even allow Exparel® produced by the new process to surpass and extend the currently approved shelf life by the FDA.Definitions

[0042] The section headings used herein are for organizational purposes only and are not to be construed as limiting the subject matter described.

[0043] As used herein, the terms “bupivacaine encapsulated multivesicular liposomes’', “bupivacaine-MVLs” or “bupivacaine MVLs” refer to a multivesicular liposome composition encapsulating bupivacaine. In some embodiments, the composition is a pharmaceutical formulation, where the bupivacaine encapsulated multivesicular liposome particles are suspended in a liquid suspending medium to form a suspension. In some such embodiments, the BUP-MVL suspension may also include free or unencapsulated bupivacaine. In some cases, the free or unencapsulated bupivacaine may be less than about 8%, 7%, 6%. 5%, 4%, 3%, 2%, 1%, 0.5%, 0.2% or 0.1%, by weight of the total amount of the bupivacaine in the composition, or in a range defined by any of the two preceding values. In some embodiment, the free bupivacaine may be about 5% or less by weight of the total amount of the bupivacaine in the composition. In further embodiments, the free bupivacaine may be about 8% or less during the shelf life of the product (i.e.. up to 2 years when stored at 2-8 °C).

[0044] As used herein, the term “encapsulated” means that bupivacaine is inside a liposomal particle, for example, the MVL particles. In some instances, bupivacaine may also be on an inner surface, or intercalated in a membrane, of the MVLs.

[0045] As used herein, the term “unencapsulated bupivacaine” or “free bupivacaine” refers to bupivacaine outside the liposomal particles, for example the MVL particles. For example, unencapsulated bupivacaine may reside in the suspending solution of these particles.

[0046] As used herein, the term “median particle diameter” refers to volume weighted median particle diameter of a suspension.

[0047] As used herein, a '‘pH adjusting agent” refers to a compound that is capable of modulating the pH of an aqueous phase.

[0048] As used herein, the terms “tonicity” and “osmolality ” are measures of the osmotic pressure of two solutions, for example, a test sample and water separated by a semi- permeable membrane. Osmotic pressure is the pressure that must be applied to a solution to prevent the inward flow of water across a semi-permeable membrane. Osmotic pressure and tonicity7are influenced only by solutes that cannot readily cross the membrane, as only these exert an osmotic pressure. Solutes able to freely cross the membrane do not affect tonicity’ because they will become equal concentrations on both sides of the membrane. An osmotic pressure provided herein is as measured on a standard laboratory’ vapor pressure or freezing point osmometer.

[0049] As used herein, the term “sugar” as used herein denotes a monosaccharide or an oligosaccharide. A monosaccharide is a monomeric carbohydrate which is not hydrolysable by acids, including simple sugars and their derivatives, e.g., amino sugars. Examples of monosaccharides include sorbitol, glucose, fructose, galactose, mannose, sorbose, ribose, deoxyribose, dextrose, neuraminic acid. An oligosaccharide is a carbohydrate consisting of more than one monomeric saccharide unit connected via glycosidic bond(s) either branched or in a chain. The monomeric saccharide units within an oligosaccharide can be the same or different. Depending on the number of monomeric saccharide units the oligosaccharide is a di-, tri-, tetra-, penta- and so forth saccharide. In contrast to polysaccharides, the monosaccharides and oligosaccharides are water soluble. Examples of oligosaccharides include sucrose, trehalose, lactose, maltose and raffinose.

[0050] As used herein, the term “amphipathic lipids” include those having a net negative charge, a net positive charge, and zwitterionic lipids (having no net charge at their isoelectric point).

[0051] As used herein, the term “neutral lipid” refers to oils or fats that have no vesicle-forming capabilities by themselves, and lack a charged or hydrophilic “head” group. Examples of neutral lipids include, but are not limited to, glycerol esters, glycol esters, tocopherol esters, sterol esters which lack a charged or hydrophilic “head” group, and alkanes and squalenes.

[0052] Unless defined otherwise, all technical and scientific terms used herein have the same meaning as is commonly understood by one of ordinary’ skill in the art. All patents, applications, published applications and other publications referenced herein are incorporated byreference in their entirety unless stated otherwise. In the event that there are a plurality of definitions for a term herein, those in this section prevail unless stated otherwise. As used in the specification and the appended claims, the singular forms “a,” “an” and “the” include plural referents unless the context clearly dictates otherwise. Unless otherwise indicated, conventionalmethods of mass spectroscopy, NMR, HPLC, protein chemistry, biochemistry, and pharmacology are employed. The use of “or” or “and” means “and / or” unless stated otherwise. Furthermore, use of the term “including” as well as other forms, such as “include”, “includes,” and “included,” is not limiting. As used in this specification, whether in a transitional phrase or in the body of the claim, the terms “comprise(s)” and “comprising” are to be interpreted as having an open-ended meaning. That is, the terms are to be interpreted synonymously with the phrases “having at least” or “including at least.” When used in the context of a process, the term “comprising” means that the process includes at least the recited steps, but may include additional steps. When used in the context of a compound, composition, or device, the term “comprising” means that the compound, composition, or device includes at least the recited features or components, but may also include additional features or components.Manufacturing Processes

[0053] Some embodiments of the present application relate to a commercial scale manufacturing process for preparing bupivacaine encapsulated multivesicular liposomes. The process comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water-immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water-immiscible solvent solution comprises at least one phosphatidyl choline, at least one phosphatidyl glycerol, cholesterol, and at least one neutral lipid, and wherein either the first aqueous solution or the volatile water-immiscible solvent solution comprises bupivacaine;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a water-in-oil-in-water second emulsion;(c) substantially removing the volatile w ater-immiscible solvent from the water- in-oil-in-water second emulsion by sparging the water-in-oil-in-water second emulsion to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is at least 190 L / min;(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow rate is at least 190 L / min; and(f) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a final aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from about 12 mg / mL to about 17 mg / mL; wherein the final aqueous suspension of bupivacaine encapsulated MVLs has a volume of, or at least of 100 L, 110 L. 120 L. 125 L, 150 L, 175 L. 200 L. 225 L, 250 L, 275 L or 300 L, or a range defined by any two of the proceeding values. In some embodiments, the sparging in step (c) is conducted at a temperature of about 18°C to about 20°C. In some embodiments, the process has a bupivacaine encapsulated MVLs product yield of at least about 75%.

[0054] In some further embodiments, the process has a bupivacaine MVL product yield of about, or at least about 76%, 77%, 78%, 79%, 80%, 81%, 82%, 83%, 84% or 85%. As described herein, the yield of bupivacaine MVLs is calculated as the following: (bupivacaine concentration in the final aqueous suspension x volume of the final aqueous suspension) / (the amount of bupivacaine in the first water-in-oil emulsion).

[0055] In some embodiments of the process, the volatile water-immiscible solvent solution comprises bupivacaine, l,2-dipalmitoyl-sn-glycero-3-phospho-rac-(l-glycerol) (DPPG) or a salt thereof (e g., a sodium salt), 1,2-dierucoylphosphatidylcholine (DEPC), tricaprylin and cholesterol. Other non-limiting exemplary phosphatidyl cholines include dioleyl phosphatidyl choline (DOPC), 1,2-di decanoy l-sn-glycero-3-phosphocholine (DDPC), 1,2-dilinoleoyl-sn- glycero-3-phosphocholine (DLOPC), l,2-dilauroyl-sn-glycero-3-phosphocholine (DLPC), 1,2- dimyristoyl-sn-glycero-3 -phosphocholine (DMPC), l,2-dipalmitoyl-sn-glycero-3- phosphocholine (DPPC), l,2-distearoyl-sn-glycero-3-phosphocholine (DSPC). l-myristoyl-2- palmitoyl-sn-glycero 3 -phosphocholine (MPPC), l-myristoyl-2-stearoyl-sn-glycero-3- phosphocholine (MSPC), l-palmitoyl-2-myristoyl-sn-glycero-3-phosphocholine (PMPC), 1- palmitoyl-2-oleoyl-sn-glycero-3-phosphocholine (POPC), l-palmitoyl-2-stearoyl-sn-glycero-3- phosphocholine (PSPC), l-stearoyl-2-myristoyl-sn-glycero-3-phosphocholine (SMPC). 1- stearoyl-2-oleoyl-sn-glycero-3-phosphocholine (SOPC), or l-stearoyl-2-palmitoyl-sn-glycero-3- phosphocholine (SPPC). Other non-limiting examples of phosphatidyl glycerols include 1,2- di erucoyl-sn-glycero-3-phospho-rac-(l -glycerol) (DEPG), l,2-dilauroyl-sn-glycero-3-phospho- rac-(l -glycerol) (DLPG), l,2-dimyristoyl-sn-glycero-3-phospho-rac-(l-glycerol) (DMPG), 1,2- dioleoyl-sn-glycero-3-phospho-rac-(l-glycerol) (DOPG), L2-distearoyl-sn-glycero-3-phospho- rac-(l -glycerol) (DSPG), l-palmitoyl-2-oleoyl-sn-glycero-3-phospho-rac-(l-glycerol) (POPG), or salts thereof, for example, the corresponding sodium salts, ammonium salts, or combinations of the salts thereof. Other non-limiting exemplary' neutral lipids may include but are not limited to triglycerides, propylene glycol esters, ethylene glycol esters, and squalene. Non-limitingexemplary triglycerides are triolein (TO), tripalmitolein, trimyristolein, trilinolein, tributyrin, tricaproin, tricaprylin (TC), and tricaprin. The fatty acid chains in the triglycerides useful in the present application can be all the same, or not all the same (mixed chain triglycerides), or all different. In some embodiments, the concentration of bupivacaine in the solvent solution is from about 5 mg / mL to about 100 mg / mL, from about 10 mg / mL to about 75 mg / mL, or from about 20 mg / mL to about 50 mg / mL. In some embodiments, the concentration of DEPC in the solvent solution is from about 1 mg / mL to about 30 mg / mL, from about 5 mg / mL to about 20 mg / mL, or from about 10 mg / mL to about 15 mg / mL. In some embodiments, the concentration of cholesterol in the solvent solution is from about 1 mg / mL to about 30 mg / mL, from about 2 mg / mL to about 15 mg / mL, or from about 5 mg / mL to about 10 mg / mL. In some embodiments, the concentration of DPPG in the solvent solution is from about 0.1 mg / mL to about 20 mg / mL, from about 0.5 mg / mL to about 10 mg / mL, or from about 1 mg / mL to about 5 mg / mL. In some embodiments, the concentration of tri caprylin in the solvent solution is from about 0. 1 mg / mL to about 20 mg / mL, from about 0.5 mg / mL to about 10 mg / mL, or from about 1 mg / mL to about 5 mg / mL. In further embodiments, DEPC and DPPG in the solvent solution are in a mass ratio of about 4: 1, 5: 1, 6: 1, 7: 1, 8:1, 9: 1, or 10: 1.

[0056] In some embodiments of the process described herein, the volatile water- immiscible organic solvent comprises or is methylene chloride (CH2CI2). In other embodiments, the volatile water-immiscible organic solvent comprises or is chloroform (CHCh).

[0057] In some embodiments of the process described herein, the second aqueous solution comprises a basic pH adjusting agent and at least one osmotic agent. Suitable organic bases that can be used as a basic pH adjusting agent include, but are not limited to histidine, arginine, lysine, tromethamine (Tris), etc. Suitable inorganic bases that can be used as a basic pH adjusting agent include, but are not limited to sodium hydroxide, calcium hydroxide, magnesium hydroxide, potassium hydroxide, etc. In some further embodiments, the basic pH adjusting agent comprises lysine. Non-limiting exemplary osmotic agents include monosaccharides (e.g., glucose, and the like), disaccharides (e.g., sucrose and the like), polysaccharide or polyols (e.g., sorbitol, mannitol. Dextran, and the like), or amino acids. In some further embodiments, the at least one osmotic agent is selected from dextrose, sorbitol, sucrose, or combinations thereof. In some further embodiments, the osmotic agent comprises dextrose. In some further embodiments, the second aqueous solution contains lysine and dextrose.Processes of Making Batches of Bupivacaine MVLs with Improved In Vitro Release Profile

[0058] Additional embodiment the present disclosure relates to a process for preparing a batch of bupivacaine encapsulated multivesicular liposomes (MVLs). the process comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water- immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water- immiscible solvent solution comprises l,2-dipalmitoyl-sn-glycero-3-phospho-rac-(l-glycerol) (DPPG) or a salt thereof, 1,2-dierucoylphosphatidylcholine (DEPC), tricaprylin and cholesterol, and wherein either the first aqueous solution or the solvent solution comprises bupivacaine;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a waterin-oil-in-water second emulsion, wherein the second aqueous solution comprises lysine and at least one an osmotic agent;(c) substantially removing the volatile water-immiscible solvent from the water-in-oil-in- water second emulsion by sparging the water-in-oil-in-water second emulsion to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 400 L / min);(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 350 L / min); and(f) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a batch of aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from 12 mg / mL to 17 mg / mL. In some embodiments, bupivacaine is in the solvent solution. In some embodiments, the second aqueous solution comprises lysine and dextrose. In some embodiments, the sparging in step (c) is conducted at a temperate from about 18°C to about 20°C.

[0059] In some embodiments, the batch has a volume of at least 100 liters. In some further embodiments, the batch has a volume of at least 100 liters. 1 10 liters, 120 liters. 125 liters, 150 liters, 175 liters, 200 liters, 225 liters, 250 liters, 275 liters or 300 liters, or a range defined by any two of the preceding values. In some such embodiments, the batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from two or more aliquots of the batch using a rotator-facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date; and the rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.05% / month after storage of the aliquots at 2°C to 8°C for about 12 months. In some further embodiments, the rate of change in the cumulative percentage release of bupivacaine atthe 24-hour time point is, or is s at least 0.06% / month, 0.07% / month, 0.08% / month, 0.09% / month, 0.10% / month, 0.11% / month, 0.12% / month, 0.13% / month, 0.14% / month, 0.15% / month, 0.16% / month, 0.17% / month, 0.18% / month, 0.19% / month, or 0.20% / month after storage of the aliquots at 2°C to 8°C for about 12 months. In some embodiments, the rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is 0.08% / month to 0.5% / month, or 0.1% / month to 0.5% / month, for example, 0. 1% / month to 0.4% / month, 0.15% / month to 0.45% / month, 0.20% / month to 0.40% / month, or 0.25% / month to 0.35% / month. In some embodiments, the cumulative percentage release of bupivacaine for the batch is based on two aliquots, three aliquots, four aliquots, five aliquots, or six aliquots.

[0060] In some embodiments, the batch has a cumulative percentage release of bupivacaine from 60% to 85% at the 48-hour time point, measured from two or more aliquots of the batch using a rotator-facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date, and the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.3% / month. In some further embodiments, the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is, is no less than, or is at least -0.25% / month, -0.20% / month, -0.18% / month, -0.15% / month, -0.12% / month, -0.10% / month, -0.08% / month, -0.05% / month. no change (0% / month). 0.02% / month, 0.05% / month, 0.08% / month, 0.10% / month, 0.12% / month, 0.15% / month, 0.18% / month, 0.20% / month, 0.22% / month, or 0.25% / month, or a range defined by any two of the preceding values, after storage of the aliquots at 2°C to 8°C for about 12 months. In some further embodiments, the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.2% / month. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -0.12% / month to 0.33% / month, for example, -0.12% / month to 0.30% / month, -0.12% / month to 0.28% / month, -0.10% / month to 0.25% / month, -0.08% / month to 0.22% / month, -0.05% / month to 0.20% / month, or 0% / month to 0.15% / month. In some embodiments, the cumulative percentage release of bupivacaine for the batch is based on two aliquots, three aliquots, four aliquots, five aliquots, or six aliquots.

[0061] In some further embodiments, the batch has a volume of at least 200 L, 210 L, 220 L, 230 L, 240 L. 250 L, 260 L, 270 L. 280 L, 290 L, or 300 L, or a range defined by any two of the proceeding values. In some embodiments, the batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from six aliquots of the batch using a rotator-facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date; and the rate of change in thecumulative percentage release of bupivacaine at the 24-hour time point is at least 0. 1% / month after storage of the aliquots at 2°C to 8°C for about 12 months. In some further embodiments, the rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0. 13% / month. In some further embodiments, the rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is 0.08% / month to 0.5% / month, or 0. 1% / month to 0.5% / month, for example, 0.1% / month to 0.4% / month, 0.15% / month to 0.5% / month, from 0.20% / month to 0.40% / month, or 0.25% / month to 0.35% / month. In some embodiments, the batch has a cumulative percentage release of bupivacaine from 60% to 85% at the 48-hour time point, measured from six aliquots of the batch using a rotator-facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date, and the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.25% / month. In some further embodiments, the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is, is no less than, or is at least -0.25% / month, -0.20% / month, -0.18% / month, -0.15% / month, -0.12% / month,-0.10% / month, -0.08% / month, -0.05% / month, no change (0% / month), 0.02% / month, 0.05% / month, 0.08% / month, 0.10% / month, 0.12% / month, 0.15% / month, 0.18% / month, 0.20% / month, 0.22% / month, or 0.25% / month, or a range defined by any two of the preceding values. In some further embodiments, the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.2% / month. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -0.12% / month to 0.33% / month, for example, -0.12% / month to 0.30% / month, -0.12% / month to 0.28% / month, -0.10% / month to 0.25% / month, -0.08% / month to 0.22% / month, -0.05% / month to 0.20% / month, or 0% / month to 0.15% / month.

[0062] Additional embodiment the present disclosure relates to a process for preparing a plurality of batches of bupivacaine encapsulated MVLs, the process of manufacturing a batch of the plurality of batches comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water- immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water- immiscible solvent solution comprises DEPC, DPPG or a salt thereof, cholesterol, and tricaprylin, and wherein either the first aqueous solution or the solvent solution comprises bupivacaine;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a water- in-oil-in-water second emulsion, wherein the second aqueous solution comprises lysine and at least one an osmotic agent;(c) substantially removing the volatile water-immiscible solvent from the water-in-oil-in- water second emulsion by sparging the water-in-oil-in-water second emulsion to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow' rate is at least 190 L / min;(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow' rate is at least 190 L / min; and(f) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a batch of aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from 12 mg / mL to 17 mg / mL; and manufacturing a lurality of batches according to the steps of (a)-(f). In some embodiments, bupivacaine is in the solvent solution. In some embodiments, the second aqueous solution comprises lysine and dextrose.

[0063] In some embodiments of the process of manufacturing a plurality of batches, the plurality of batches are manufactured within a period of six months and the batches each has a volume of, or at least of 100 liters, 110 liters, 120 liters, 125 liters, 150 liters, 175 liters, 200 liters, 225 liters, 250 liters, 275 liters, or 300 liters, or a range defined by any two of the preceding values. In some further embodiments, the batches are manufactured within a period of 3 months. In some other embodiments, the batches are manufactured within a period of 2 months. In some embodiments, the batches are manufactured within a period of 30 days. In some embodiments, the batches are manufactured within a period of 3 months, each having a volume of at least 200 liters, for example about 220 liters, 240 liters, 260 liters, 280 liters or 300 liters. In some embodiments, the batches are manufactured within a period of 2 months, each having a volume of at least 200 liters. In some embodiments, the batches are manufactured within a period of 30 days, each having a volume of at least 200 liters, for example about 220 liters, 240 liters, 260 liters, 280 liters or 300 liters. In some embodiments, the sparging in step (c) is conducted at a temperate from about 18°C to about 20°C.

[0064] In some embodiments of the process of manufacturing a plurality of batches, each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from tw o or more aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date; and an average rate of change in the cumulativepercentage release of bupivacaine at the 24-hour time point is at least 0.05% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is, or is at least 0.06% / month, 0.07% / month. 0.08% / month, 0.09% / month, 0. 10% / month, 0.11% / month, 0.12% / month. 0.13% / month, 0.14% / month, 0.15% / month, 0.16% / month, 0. 17% / month, 0.18% / month, 0.19% / month, or 0.20% / month, or a range defined by any two of the preceding values, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.08% / month. In some embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is 0.08% / month to 0.5% / month, or 0.1% / month to 0.5% / month, for example, 0.1% / month to 0.4% / month, 0.15% / month to 0.45% / month, 0.20% / month to 0.40% / month, or 0.25% / month to 0.35% / month. In some embodiments, the average rate of change in the cumulative percentage release of bupivacaine is based on three batches, and one batch is manufactured at least 7 days apart (e.g., 7, 8, 9, or 10 or more days apart) from at least one other batch. In some other embodiments, the average rate of change in the cumulative percentage release of bupivacaine is based on two batches, and one batch is manufactured at least 7 days apart (e.g., 7. 8, 9, or 10 or more days apart) from the other batch. In some embodiments, the cumulative percentage release of bupivacaine for each batch is based on two aliquots, three aliquots, four aliquots, five aliquots, or six aliquots.

[0065] In some embodiments of the process of manufacturing a plurality of batches, each batch has a cumulative percentage release of bupivacaine from 60% to 85% at the 48-hour time point, measured from two or more aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date, and the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.3% / month after storage of the aliquot of each batch at 2°C to 8°C for about 12 months. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is, is no less than, or is at least -0.25% / month, -0.20% / month, -0.18% / month, -0.15% / month, -0.12% / month, -0.10% / month, -0.08% / month, -0.05% / month, no change (0% / month). 0.02% / month, 0.05% / month, 0.08% / month, 0. 10% / month, 0.12% / month, 0. 15% / month, 0. 18% / month, 0.20% / month, 0.22% / month, or 0.25% / month, or a range defined by any two of the preceding values, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.2% / month. In some furtherembodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -0.18% / month to 0.33% / month, for example, -0. 15% / month to 0.30% / month, -0.12% / month to 0.28% / month, -0.10% / month to 0.25% / month, -0.08% / month to 0.22% / month, -0.05% / month to 0.20% / month. or 0% / month to 0. 15% / month. In some embodiments, the average rate of change in the cumulative percentage release of bupivacaine is based on three batches, and one batch is manufactured at least 7 days apart (e.g., 7, 8, 9, or 10 or more days apart) from at least one other batch. In some other embodiments, the average rate of change in the cumulative percentage release of bupivacaine is based on two batches, and one batch is manufactured at least 7 days apart (e.g.. 7, 8, 9, or 10 or more days apart) from the other batch. In some embodiments, the cumulative percentage release of bupivacaine for each batch is based on two aliquots, three aliquots, four aliquots, five aliquots, or six aliquots.

[0066] In some embodiments of the process of manufacturing a plurality of batches, each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from two or more aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date; and wherein an average change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.5% after storage of the aliquots of each batch at 2°C to about 8°C for 12 months. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 24-hour time point is, or is at least 0.6%, 0.7%, 0.8%, 0.9%, 1.0%, 1.1%, 1.2%, 1.3%, 1.4%, 1.5%, 1.6%, 1.7%, 1.8%, 1.9% or 2.0% after storage of the aliquots of each batch at 2°C to about 8°C for 12 months. In some embodiments, the average change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 1%. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 24-hour time point is 1% to 5%, for example, 1.5% to 4.5%, 2.0% to 4.0%, or 2.5% to 3.5%. In some embodiments, the average change in the cumulative percentage release of bupivacaine is based on three batches, and one batch is manufactured at least 7 days apart (e.g.. 7, 8, 9. or 10 or more days apart) from at least one other batch. In some other embodiments, the average change in the cumulative percentage release of bupivacaine is based on two batches, and one batch is manufactured at least 7 days apart (e.g., 7, 8, 9, or 10 or more days apart) from the other batch. In some embodiments, the cumulative percentage release of bupivacaine for each batch is based on two aliquots, three aliquots, four aliquots, five aliquots, or six aliquots.

[0067] In some embodiments of the process of manufacturing a plurality' of batches, each batch has a cumulative percentage release of bupivacaine from 60% to 85% at the 48-hour time point, measured from two or more aliquots of each batch using a rotator-facilitated in vitrorelease assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date; and an average change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -5% after storage of the aliquots of each batch at 2°C to 8°C for about 12 months. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 48-hour time point is, or is no less than -4.5%, -4.0%, -3.5%, -3.0%, -2.5%, -2.0%, -1.5%, -1.0%, -0.5%, no change (0%), 0.5%, 1.0%, 1.5%, 2.0% or 2.5% after storage of the aliquots of each batch at 2°C to about 8°C for 12 months. In some embodiments, the average change in the cumulative percentage release of bupivacaine at the 48-hour time point is, or is no less than -4%. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 48- hour time point is from -4% to 6%, for example, -3.5% to 5.5%, -3.0% to 5.0%, -2.5% to 4.5%, -2.0% to 4.0%, -1.5% to 3.5%, or -1.0% to 3.0%. In some embodiments, the average change in the cumulative percentage release of bupivacaine is based on three batches, and one batch is manufactured at least 7 days apart (e.g., 7, 8, 9, or 10 or more days apart) from at least one other batch. In some other embodiments, the average change in the cumulative percentage release of bupivacaine is based on two batches, and one batch is manufactured at least 7 days apart (e.g., 7, 8, 9, or 10 or more days apart) from the other batch. In some embodiments, the cumulative percentage release of bupivacaine for each batch is based on two aliquots, three aliquots, four aliquots, five aliquots, or six aliquots.

[0068] In some embodiments, the cumulative percentage release of bupivacaine of each batch is measured as the average of three aliquots from each batch. In other embodiments, the cumulative percentage release of bupivacaine of each batch is measured as the average of six aliquots from each batch. In some further embodiments, the cumulative percentage release of bupivacaine is measured using the rotator-facilitated in vitro release assay. In some embodiments, the in vitro release assay is run for about 48 hours. In some other embodiments, the in vitro release assay is run for about 168 hours. In some embodiments, each aliquot has a cumulative percentage release of bupivacaine from 36% to 81% at the 24-hour time point. In some embodiments, each aliquot has a cumulative percentage release of bupivacaine from 50% to 95% at the 48-hour time point. In some embodiments, the cumulative percentage release of bupivacaine is measured after storage of the aliquots of each batch at about 5°C for about 365 days from batch manufacture date.

[0069] In some embodiments, the batches are manufactured within a period of 3 months, each having a volume of at least 200 liters, for example, 210 L, 220 L, 230 L, 240 L, 250 L, 260 L, 270 L, 280 L, 290 L, or 300 L, or a range defined by any two of the proceeding values. In some further embodiments, the batches are manufactured within 30 days. In some such embodiments, each batch has a cumulative percentage release of bupivacaine from 46% to 71%at a 24-hour time point, measured from six aliquots of each batch using a rotator-facilitated in vitro release assay, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date; wherein an average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.05% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months; and wherein the average rate of change in the cumulative percentage release of bupivacaine is based on two to five batches, and at least one batch is manufactured 10 or more days apart from at least one other batch. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is, or is at least 0.06% / month, 0.07% / month. 0.08% / month, 0.09% / month, 0.10% / month, 0.11% / month, 0.12% / month, 0.13% / month, 0.14% / month, 0.15% / month, 0. 16% / month, 0.17% / month, 0.18% / month, 0.19% / month, or 0.20% / month, or a range defined by any two of the preceding values, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months. In some embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0. 1% / month. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is 0.08% / month to 0.5% / month, or 0. 1% / month to 0.5% / month, for example, 0.1% / month to 0.4% / month, or 0.15% / month to 0.5% / month. In some embodiments, the in vitro release assay is run for about 48 hours. In some other embodiments, the in vitro release assay is run for about 168 hours. In some embodiments, each batch has a cumulative percentage release of bupivacaine from 60% to 85% at the 48-hour time point, and the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.25% / month after storage of the aliquot of each batch at 2°C to 8°C for about 12 months. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is, is no less than, or is at least -0.25% / month, -0.20% / month, -0.18% / month, -0.15% / month, -0.12% / month, -0.10% / month, -0.08% / month, -0.05% / month, no change (0% / month), 0.02% / month, 0.05% / month, 0.08% / month, 0.10% / month, 0.12% / month, 0. 15% / month, 0. 18% / month, 0.20% / month, 0.22% / month, or 0.25% / month, or a range defined by any two of the preceding values, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months. In some embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.2% / month. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -0.18% / month to 0.33% / month, for example, -0.15% / month to 0.30% / month, -0.12% / month to 0.28% / month, -0.10% / month to 0.25% / month, -0.08% / month to 0.22% / month, -0.05% / month to 0.20% / month, or 0% / month to 0.15% / month. In some embodiments, the average rate of change in the cumulative percentage release of bupivacaine isbased on three batches, and one batch is manufactured 10 or more days (e.g., 10, 15, 20, 25 or 30 days) apart from at least one other batch. In some other embodiments, the average rate of change in the cumulative percentage release of bupivacaine is based on two batches, and one batch is manufactured 10 or more days (e.g., 10, 15, 20, 25 or 30 days) apart from the other batch.

[0070] In some embodiments, the batches are manufactured within a period of 3 months, each having a volume of at least 200 liters, for example, 210 L, 220 L, 230 L, 240 L, 250 L, 260 L, 270 L, 280 L, 290 L, or 300 L, or a range defined by any two of the proceeding values. In some further embodiments, the batches are manufactured within 30 days. In some such embodiments, each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from six aliquots of each batch using a rotator-facilitated in vitro release assay, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date; wherein an average change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.5% after storage of the aliquots of each batch at 2°C to 8°C for about 12 months; and wherein the average rate of change in the cumulative percentage release of bupivacaine is based on two to five batches, and at least one batch is manufactured 10 or more days apart from at least one other batch. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 24-hour time point is, or is at least O.6%. 0.7%, 0.8%, 0.9%, 1.0%. 1.1%, 1.2%, 1.3%. 1.4%, 1.5%, 1.6%, 1.7%. 1.8%, 1.9% or 2.0% after storage of the aliquots of each batch at 2°C to about 8°C for 12 months. In some embodiments, the average change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 1%. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 24-hour time point is 1% to 5%. In some embodiments, the in vitro release assay is run for about 48 hours. In some other embodiments, the in vitro release assay is run for about 168 hours. In some embodiments, each batch has a cumulative percentage release of bupivacaine from 60% to 85% at the 48-hour time point, and an average change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -5% after storage of the aliquot of each batch at 2°C to 8°C for about 12 months. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 48-hour time point is, or is no less than -4.5%, -4.0%, -3.5%, -3.0%, -2.5%, -2.0%, -1.5%, -1.0%, -0.5%, no change (0%), 0.5%, 1.0%, 1.5%, 2.0% or 2.5% after storage of the aliquots of each batch at 2°C to about 8°C for 12 months. In some embodiments, the average change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -4%. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -4% to 6%. In some embodiments, the average change in the cumulative percentage release of bupivacaine is based on three batches, and onebatch is manufactured 10 or more days (e.g., 10, 15, 20, 25 or 30 days) apart from at least one other batch. In some other embodiments, the average change in the cumulative percentage release of bupivacaine is based on two batches, and one batch is manufactured 10 or more days (e.g., 10, 15, 20, 25 or 30 days) apart from the other batch.

[0071] As described herein with respect to any of the time points (e.g., 24-hour, 48- hour or 168-hour) in which cumulative percentage release of bupivacaine is tested, each time point is within ±15 minutes of the scheduled time points.

[0072] As described herein with respect to the rate of change in the cumulative percentage release of bupivacaine, each aliquot is measured at the following five time points: a first time point is within 30 days from batch manufacture date, a second time point is about 3 months from the batch manufacture date, a third time point which is about 6 months from the batch manufacture date, a fourth time point which is about 9 months from the batch manufacture date, and a fifth time point which is about 12 months from the batch manufacture date. Each time point of actual measurement is within ± 30 days of the scheduled time point.

[0073] As described herein with respect to the change in the cumulative percentage release of bupivacaine after storage of the aliquots of each batch at 2°C to 8°C for about 12 months, the change is calculated as: % release of bupivacaine at about 12 months from batch manufacture date - % release of bupivacaine shortly after manufacturing (e.g., within 30 days from batch manufacture date when the batch product is filled into individual vials). Batch product is usually filled into individual vials within 7 days from the manufacture date.

[0074] In some embodiments of the processes described herein, the mixing in step (a) is performed using a first mixer at a high shear speed. In some embodiments, the high shear speed is from about 1100 rpm to about 1300 rpm. For example, in some embodiments, the high shear speed is about 1100 rpm, about 1110 rpm, about 1120 rpm, about 1130 rpm, about 1140 rpm, about 1150 rpm, about 1160 rpm, about 1170 rpm, about 1180 rpm, about 1190 rpm, about 1200 rpm, about 1210 rpm, about 1220 rpm, about 1230 rpm, about 1240 rpm, about 1250 rpm. about 1260 rpm, about 1270 rpm, about 1280 rpm, about 1290 rpm. about 1300 rpm, or a range defined by any of the two preceding values. In some embodiment, the high shear speed is about 1200 rpm to about 1250 rpm. In some such embodiments, the mixing in step (a) is performed for about 65 minutes to about 75 minutes, for example, about 65, 66, 67, 68, 69, 70, 71, 72, 73, 74 or 75 minutes, or a range defined by any two of the preceding values. In some further embodiments, the mixing in step (a) is performed at the high speed from about 1200 rpm to about 1250 rpm or about 1225 rpm for about 70 minutes.

[0075] Proper mixing rate is important for forming the first emulsion droplets in a proper size range, which is important to the final product yield, the MVL particle stability andrelease properties. It was observed that when the mixing speed is too low or too high, the droplets formed in the first emulsion were either too big or too small. In some embodiments, mixing temperature and / or time may also affect the size of the droplet formed. In some further embodiments, the first mixer used in step (a) of the process has a blade diameter of about 8 inches to about 15 inches (e.g., about 8. 9, 10, 11, 12. 13. 14 or 15 inches). In some further embodiment, the first mixer has an 11 -inch blade diameter. In some embodiments, two or more mixers may be used in step (a). In further embodiments, the first mixer used in step (a) of the process is not a static mixer. In other embodiments, the first mixer used in step (a) of the process is a static mixer. In further embodiments, the mixing in step (a) is performed at a temperature of about 20 °C to about 23 °C. In some embodiments, the mixing in step (a) is performed at a temperature of about 21.5 °C. In some further embodiments, the water-in-oil first emulsion has a volume of about 200L to about 260L, or from about 200L to about 240L, such as 200L, 205L, 210L, 215L, 220L, 225L, 230L, 235L or 240L.

[0076] In some embodiments of the processes described herein, the mixing in step (b) is performed using a second mixer at a low shear speed. In some embodiments, the low shear speed is from about 445 rpm to about 680 rpm. In some embodiments, the low shear speed is for example, about 445 rpm, about 450 rpm, about 460 rpm, about 470 rpm, about 480 rpm. about490 rpm. about 500 rpm, about 510 rpm, about 520 rpm, about 530 rpm, about 540 rpm. about550 rpm, about 560 rpm, about 570 rpm, about 580 rpm, about 590 rpm, about 600 rpm, about610 rpm, about 620 rpm, about 630 rpm, about 640 rpm, about 650 rpm, about 660 rpm, about670 rpm, about 680 rpm, or a range defined by any of the two preceding values. In some further embodiments, the low shear speed is from about 615 rpm to about 650 rpm, or about 630 rpm. In some embodiments, the mixing in step (b) is performed for about 60 and about 85 seconds. In some embodiments, the mixing in step (b) is performed for about 69 seconds, about 70 seconds, about 71 seconds, about 72 seconds, about 73 seconds, about 74 seconds, about 75 seconds, about 76 seconds, about 77 seconds, about 78 seconds, about 79 seconds, about 80 seconds, about 81 seconds, about 82 seconds, about 83 seconds, about 84 seconds, or about 85 seconds, or a range defined by any two of the preceding values. In some further embodiments, the mixing in step (b) is performed at the low speed from about 615 rpm to about 650 rpm for about 70 seconds. In some other embodiments, the mixing in step (b) is performed with both the first mixer at a high speed from about 800 rpm to about 1000 rpm and a second mixer at a low speed from about 450 rpm to about 550 rpm for about 60 to 75 seconds. In some further embodiments, the second mixer used in step (b) of the process has a blade diameter of about 8 inches to about 15 inches, for example, about 8, 9, 10, 11, 12, 13, 14 or 15 inches. In some further embodiment, the second mixer has an 11 -inch blade diameter. In some embodiments, the second mixer used in step (b) of the process isnot a static mixer. In other embodiments, the second mixer used in step (b) of the process is a static mixer.

[0077] In some embodiments of the processes described herein, the second aqueous solution is stored at a temperature of about 18 °C to about 22 °C prior to the mixing in step (b). In some further embodiments, the mixing in step (b) is performed at a temperature of from about 18°C to about 22°C, or from about 18°C to about 20°C. In some embodiments, the mixing in step (b) is performed at a temperature of about 20 °C or less. For example, in some embodiments, the mixing in step (b) is performed at a temperature of about 19 °C to about 20 °C. The water-in-oil- in water (w / o / w) second emulsion is not as stable as the first emulsion. As such, a low shear speed is used in the mixing step to reduce the disruption of the spherules formed in this step. In addition, the mixing time, speed, and temperature in step (b) are also important to yield the final MVL particles in the target diameters and have the desired release properties. If mixing time is too short, it leads to a larger particle size. In some embodiments, the volume ratio of the first emulsion to the second emulsion is about 1 : 1, 1 : 1.5, 1:2, 1 :2.5, 1:3, 1:3.5, 1 :4, 1:4.5 or 1 :5. In one embodiment, the volume ratio of the first emulsion to the second emulsion is about 1 :3.5. In further embodiment, additional second aqueous solution is added to dilute the second emulsion prior to the sparging step such that the final volume ratio of the first emulsion to the diluted second emulsion is about l: 10 to about 1:30. for example, about 1: 10. 1: 12, 1: 14, 1 : 16, 1 : 18, 1:20, 1 :22, 1 :24, 1 :26, 1:28 or 1 :30. In one embodiment, the volume ratio of the first emulsion to the diluted second emulsion is about 1:20. The second aqueous solution comprises lysine and an osmotic agent such as dextrose. In some embodiments, the concentration of lysine in the second aqueous solution is from about 0. 1 mg / mL to about 10 mg / mL, from about 0.5 mg / rnL to about 5 mg / mL. from about 1 mg / mL to about 2.5 mg / mL, or from about 1.5 mg / mL to about 2.0 mg / mL. In some further embodiments, the concentration of dextrose in the second aqueous solution is from about 5 mg / mL to about 100 mg / mL, from about 10 mg / mL to about 80 mg / mL, from about 20 mg / mL to about 60 mg / mL, from about 30 mg / mL to about 40 mg / mL, or about 32 mg / mL to about 35 mg / mL.

[0078] In some embodiments of the processes described herein, substantially removing the volatile water-immiscible solvent from the water-in-oil-in-water second emulsion comprises exposing the second emulsion to a gas atmosphere. Organic solvent may be substantially removed by blowing a gas over the second emulsion, or sparging gas in the second emulsion. In some further embodiments, substantially removing the volatile water-immiscible solvent may comprise bubbling a sparging gas through the second emulsion or the diluted second emulsion. In some embodiments, the sparging gas is nitrogen.

[0079] In some embodiments of the processes described herein, sparging is performed at a temperature of about 18 °C to about 22 °C, about 18 °C to about 21 °C, or about 18 °C toabout 20 °C. In some embodiments, sparging is performed at a temperature of about 19 °C. In some embodiments, sparging is performed at a temperature of about 19 °C or less. For example, in some embodiments, sparging is performed at a temperature of about 18 °C to about 19 °C. It was observed that sparging performed at lower temperatures can provide less product breakage (MVL particle breakage) and consequently improved product yield. For example, it was observed that sparging performed at lower temperatures is correlated with lower conductivity values in the aqueous suspension. Lower conductivity values can be representative of less product breakage due to less release of the contents inside of internal aqueous chambers of the MVLs, and consequently higher product yield. Accordingly, sparging performed at a temperature of about 20 °C, about 19 °C, about 19 °C or less, from about 18 °C to about 20 °C, or from about 18 °C to about 19 °C can beneficially provide an improved product yield in comparison to higher temperatures. In some embodiments, sparging performed at a temperature of about 19 °C, about 19 °C or less, or from about 18 °C to about 19 °C can provide improved product yield in comparison to sparging performed at above 20 °C (e.g., at about 21°C or 22°C).

[0080] In addition, the sparging time also impacts the product yield. Longer sparging time usually results in lower product yield at least due to increased product breakage. In some embodiments, the sparging is performed for about 15 minutes to about 30 minutes, for example, about 15. 16. 17, 18, 19, 20, 21, 22, 23, 24, 25, 26. 27. 28. 29 or 30 minutes, or a range defined by any two of the preceding values. In some further embodiments, sparging is performed for about 19 minutes to about 25 minutes, or about 22 minutes at a temperature of about 19 °C. In some further embodiments, sparging the water-in-oil-in-water second emulsion comprises sparging at a sparging gas flow rate of about 1500 to about 3000 SLPM, about 1750 SLPM to about 2750 SLPM, or about 1874 SLPM to about 2500 SLPM. In some further embodiments, sparging the water-in-oil-in-water second emulsion is at a sparging gas flow rate of about 2400 SLPM for about 22 minutes.

[0081] In some embodiments, conductivity values of the aqueous suspension can be measured to determine that sparging is complete. Additionally or alternatively, the pH of the aqueous suspension may also be measured to determine whether sparging is complete. For example, a drop in pH can be observed during the sparing process, at least partially due to the release of the phosphoric acid from the internal aqueous chambers of the MVLs.

[0082] It may be advantageous for the pre-sparging second emulsion (e.g., diluted second emulsion) to be at a desired temperature at the beginning of sparging. In certain embodiments, the mixing in step (b) prior to sparging may occur for a relatively short period of time (e.g., 65 to 85 seconds). In such embodiments, it may be desirable for the components of the second emulsion to be at or near a desired temperature during the mixing in step (b). In suchembodiments, the desired temperature may be provided by providing the second aqueous solution at or near the desired temperature. For example, the second aqueous solution can be provided at a temperature of about 19 °C, about 19 °C or less, about 18 °C to about 19 °C, or about 18 °C to about 20 °C.

[0083] In certain embodiments, it was observed that sparging temperatures may affect particle size and / or particle size distribution (e.g., median particle size and / or particle size distribution). While lower temperatures (e.g., about 19 °C, about 19 °C or less, about 18 °C to about 19 °C, or about 18 °C to about 20 °C) may provide improved product yield, it was observed that lower temperatures may result in an increased median particle size and / or an increased particle size distribution. In certain embodiments, it was observed that the shear speed of mixing, the mixing temperature, and / or the mixing time in step (b) may affect median particle size and / or particle size distribution. In certain embodiments, the shear speed of the mixing, the mixing temperature, and / or the mixing time in step (b) can be selected to counteract the effects of the lower sparging temperatures on median particle size and / or particle size distribution. In certain embodiments, it was observed that higher mixing speeds can result in smaller median particle sizes and / or particle size distributions than lower mixing speeds. In some embodiments in which sparging is performed at lower temperatures (e.g., about 19 °C, about 19 °C or less, from about 18 °C to about 19 °C, or from about 18 °C to about 20 °C), the mixing speeds for the mixing in step (b) can be about 520 rpm, at least about 520 rpm, about 535 rpm, at least about 535 rpm, about 575 rpm, at least 575 rpm, about 630 rpm, at least about 630 rpm, or from 615 rpm to 680 rpm. In some embodiments in which sparging is performed at lower temperatures (e.g., about 19 °C. about 19 °C or less, from about 18 °C to about 19 °C. or from about 18 °C to about 20 °C), a mixing time of about 68 seconds to 72 seconds or about 70 seconds can be used. In some embodiments, a particular ramp rate may be used to increase the speed of the mixer to the desired mixing speed. A ramp rate is how quick the mixer reaches the target mixing speed. The ramp rate impacts the duration the mixer takes to reach the target mixing speed, and thereby increases or decreases the total amount of mixing energy utilized for the mixing step for a given mixing time.

[0084] In some embodiments of the processes described herein, when sparging is performed at a temperature of about 19°C, a mixing speed of 630 rpm and a mixing time of 70 seconds may be used with a particular ramp rate. In some embodiments, other combinations of mixing speeds, ramp rates, and / or mixing times may be selected to provide similar results, such as, for example, lower mixing speeds with faster ramp rates, lower mixing speeds with longer mixing times, or faster mixing speeds with shorter mixing times.

[0085] Exparel® product specification includes the following particle size (volume- weighted diameter) requirements: dio is no larger than 12.0 pm, dso (median) is from 24 pm to31.0 pm, and dsxi is no larger than 62.0 gm during the shelf life of the product. The products manufactured by the 45L process in 2022 (n = 144) have a dso of 24.6 pm to 27. 1 pm and a ds>o of 46.2 pm to 52.2 pm. In contrast, the products manufactured by the 200L UK process (n = 75) have a dso of 25.3 pm to 28.9 pm and a d90 of 52.2 pm to 61.8 pm, while the products dio manufactured by both processes is about 13.5 pm to 15.0 pm. It was observed that when the manufacturing scale was substantially increased from 45L to 200L, the MVL products had a wider particle size distribution (the difference between dgo and dio). As the MVL particles have the tendency to agglomerate during storage and results in larger d9o value overtime, it is important that the product has a narrower particle size distribution and smaller d9o at the initial release to ensure that the dgo is within the product specification during the entire shelf life, and also allow for a wide range of median particle size (dso) to be achieved without failing the d o particle size specification. It was unexpectedly observed that higher microfiltration feed flow rates in step (d) can result in smaller particle size distribution than lower microfiltration feed flow rates. In some instance, higher microfiltration feed flow rates in step (d) can result in smaller particle size distribution without substantial reduction in median particle size (dso). Higher feed flow rates may also reduce the overall time of the microfiltration in step (d), for example, by allowing for higher permeate flow rates and consequently less processing time. Reduced overall time of step (d) may be preferable, for example, because the suspension is less stable during step (d). In some embodiments, higher microfiltration feed flow rates can reduce the risk of filters clogging. In some embodiments, the more diluted the suspension, the less shear is imparted at the same flow rate. When the suspension is initially diluted, high feed flow rates may be used and then reduced linearly over the course of step (d) until an end target level of concentration is reached.

[0086] In some embodiments of the processes described herein, the first microfiltration is conducted with a beginning first microfiltration feed flow rate from about 190 L / min to about 400 L / min, or from about 200 L / min to about 350 L / min, and an end first microfiltration feed flow rate from about 190 L / min to about 310 L / min. In some embodiments, the microfiltration feed flow rate in step (d) can decrease during the microfiltration in step (d). For example, in some embodiments, at the start of the microfiltration in step (d), the feed flow rate can be from about 290 L / min to about 350 L / min. In some embodiments, at the start of the microfiltration in step (d), the feed flow rate can be about 320 L / min to about 340 L / min. In some embodiments, at the end of the microfiltration in step (d). the feed flow rate can be about 190 L / min to about 310 L / min. In some embodiments, at the end of the microfiltration in step (d), the feed flow rate can be about 300 L / min or from about 280 L / min to about 300 L / min. In some embodiments, the feed flow rate can decrease linearly or approximately linearly in relation to the level of liquid in the sparging vessel or the concentration of bupivacaine MVLs during themicrofiltration in step (d). In some embodiments, decreasing the feed flow rate during the microfiltration of step (d) can prevent product breakage as the aqueous suspension of bupivacaine encapsulated multivesicular liposomes becomes less diluted.

[0087] In some further embodiments, in which sparging is performed at lower temperatures (e.g.. about 19 °C, about 19 °C or less, about 18 °C to about 19 °C, or about 18 °C to about 20 °C), higher microfiltration feed flow rates, such as feed flow rates of about 340 L / min or from about 340 L / min to about 350 L / min at the start of microfiltration and / or about 300 L / min or from about 300 L / min to about 310 L / min at the end of microfiltration can be used.

[0088] In some embodiments of the processes described herein, wherein step (e) is performed using two sets of filtration modules, wherein each set of the filtration modules operate independently of the other. In further embodiments, each set of the filtration module comprises three, four, five, six or more hollow fiber filters, each having a membrane pore size from about 0. 1 pm to about 0.2 pm. One embodiment of the filtration modules is illustrated in FIG. 2A.

[0089] In some embodiments of processes described herein, the diafiltration step (e) is performed until the aqueous suspending medium of the second aqueous suspension is substantially replaced with the saline solution multiple times (e.g., at least 2.0, 2.5, 3.0, 3.5, 4.0, 4.5 or 5.0 times volume exchanges). It was unexpectedly observed that higher diafiltration feed flow rates can result in smaller particle size distributions than lower diafiltration feed flow rates. In some instance, it was observed that higher diafiltration feed flow rates can result in smaller particle size distributions than lower diafiltration feed flow rates without impacting product yield or the percentage of free bupivacaine. As yield was not impacted by the higher recirculation rates, without being bound by a particular theory, this observation suggests that higher diafiltration feed flow rates do not destroy particles but may operate by another mechanism, such as reducing agglomeration. Higher diafiltration feed flow rates may also reduce the overall time of the diafiltration, for example, by allowing for higher permeate flow rates without fouling or clogging the filters. In some embodiment, the different diafiltration feed flow rates can be used at different stages throughout diafiltration. For example, in some embodiments, during a first stage of diafiltration (e.g., first volume exchange), the feed flow rate can be about 190 L / min to about 310 L / min. In some embodiments, during the first stage of diafiltration, the feed flow rate can be about 250 L / min to about 310 L / min, or about 300 L / min. In some embodiments, it was observed that higher diafiltration feed flow rates at later stages of the diafiltration process can reduce product yield. Accordingly, in some embodiments, the diafiltration feed flow rate is reduced during the second stage of diafiltration to maintain a desired product yield. In some embodiments, the diafiltration feed flow rate can be reduced during the second stage of diafiltration to maintain a desired product yield while maximizing the reduction in particle size distribution. In someembodiments, during a second stage of diafiltration. the feed flow rate can be about 190 L / min to about 265 L / min. In some embodiments, during the second stage of diafiltration (e.g., additional volume exchanges), the feed flow rate can be about 245 L / min to about 265 L / min, or about 255 L / min.

[0090] In some further embodiments, in which sparging is performed at lower temperatures (e.g., about 19 °C, about 19 °C or less, about 18 °C to about 19 °C, or about 18 °C to about 20 °C), higher diafiltration feed flow rates, such as feed flow rates of about 290 L / min to about 310 L / min or about 300 L / min in the first stage, and / or about 245 L / min to about 265 L / min or about 255 L / min in the second stage can be used.

[0091] In some embodiments of the processes described herein, the second microfiltration is conducted with a beginning second microfiltration feed flow rate of about 190 L / min to about 265 L / min. In some embodiments, the second microfiltration feed flow rate in step (!) can decrease during the microfiltration in step (f). For example, in some embodiments, at the start of the second microfiltration in step (f), the feed flow rate can be about 245 L / min to about 265 L / min, or about 255 L / min. In some embodiments, at the end of the second microfiltration in step (f), the feed flow rate can be about 120 L / min to about 190 L / min. In some embodiments, at the end of the second microfiltration in step (f), the feed flow rate can be about 170 L / min to about 190 L / min or about 180 L / min. In some embodiments, the feed flow rate can decrease linearly or approximately linearly during step (f) in relation to the concentration vessel liquid level or the MVL concentration in the third aqueous suspension in the concentration vessel. In some embodiments, decreasing the feed flow rate during the microfiltration of step (f) can prevent filter clogging and / or product damage as the aqueous suspension of bupivacaine encapsulated multivesicular liposomes becomes less dilute. Higher microfiltration feed flow rates may also reduce the overall time of the microfiltration in step (1).

[0092] In some embodiments of processes described herein, step (f) may be performed until a target concentration of bupivacaine MVLs is reached, for example, a target bupivacaine concentration in the final aqueous suspension can be from about 12 mg / mL to about 17 mg / mL. In some further embodiments, the final aqueous suspension of bupivacaine encapsulated multivesicular liposomes is transferred to a bulk product vessel, and subsequently filled into individual vials.

[0093] A further aspect of the present disclosure relates to a process for preparing bupivacaine encapsulated multivesicular liposomes (MVLs), the process comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water-immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water-immiscible solvent solution comprises bupivacaine, 1,2-dipalmitoyl-sn-glycero-3-phospho-rac-(l -glycerol) (DPPG) or a salt thereof, 1,2- dierucoylphosphatidylcholine (DEPC), tricaprylin and cholesterol, and wherein the first emulsion has a volume of at least 200 L;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a water-in-oil-in-water second emulsion, wherein the second aqueous solution comprises lysine and dextrose;(c) substantially removing the volatile water-immiscible solvent from the waterin-oil-in-water second emulsion by sparging the water-in-oil-in-water second emulsion to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume, wherein the sparging is performed at a temperature of 18°C to 20°C for no more than 25 minutes;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated MVLs by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is about 190 L / min to about 400 L / min or about 200 L / min to about 400 L / min;(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow rate is from about 190 L / min to about 350 L / min or about 200 L / min to about 350 L / min; and(!) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a final aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from about 12 mg / mL to about 17 mg / mL; wherein the final aqueous suspension of bupivacaine encapsulated MVLs has a volume of at least about 200 L (for example, 210 L, 220 L, 230 L, 240 L, 250 L, 260 L, 270 L, 280 L, 290 L. or 300 L, or a range defined by any two of the proceeding values); and wherein the process has a bupivacaine MVL product yield of at least about 75%. In some further embodiments, the final aqueous suspension of bupivacaine encapsulated MVLs has a volume of at least about 250 L. In still further embodiments, the process has a bupivacaine MVL product yield of at least about 76%, 77%, 78%, 79%, 80%, 81%, 82%, 83%, 84% or 85%, or a range defined by any two of the preceding values (for example, about 76% to about 85%, or about 78% to about 83%).

[0094] In any embodiments of the processes described herein, the volume ratio of the first emulsion to the second emulsion is about L I, 1 : 1.5, 1:2, 1 :2.5, 1:3, 1:3.5, 1 :4, 1 :4.5 or 1:5.In one embodiment, the volume ratio of the first emulsion to the second emulsion is about 1 :3.5. In further embodiment, additional second aqueous solution is added to dilute the second emulsion prior to the sparging step such that the final volume ratio of the first emulsion to the diluted second emulsion is about 1: 10 to about 1:30. or about 1 :20. In some embodiments, the first microfiltration is conducted with a beginning first microfiltration feed flow rate from about 290 L / min to about 350 L / min, and an end first microfiltration feed flow rate from about 250 L / min to about 310 L / min, decreasing approximately linearly in relation to the level of liquid in the sparging vessel or the bupivacaine MVL concentration in the first aqueous suspension. In some such embodiments, the beginning first microfiltration feed flow rate is about 340 L / min, and the end first microfiltration feed flow rate is about 300 L / min. In some embodiments, the filtration feed flow rate during a first stage of diafiltration is about 250 L / min to about 310 L / min, and the filtration feed flow rate during a second stage of diafiltration is about 245 L / min to about 265 L / min. In some further embodiments, the filtration feed flow rate during a first stage of diafiltration is about 300 L / min, and the filtration feed flow rate during a second stage of diafiltration is about 255 L / min. In some embodiments, sparging the water-in-oil-in-water second emulsion is performed at a temperature of about 19 °C. In some embodiments, the mixing in step (a) is performed using a first mixer at a high speed from about 1100 rpm to about 1300 rpm for about 65 minutes to about 75 minutes. In some further embodiments, the mixing in step (a) is performed at the high speed from about 1200 rpm to about 1250 rpm for about 70 minutes. In some further embodiments, the water-in-oil first emulsion has a volume of about 200L to about 260L or about 200L to about 240L. In some embodiments, the mixing in step (b) is performed at a low speed from about 445 rpm to about 680 rpm for about 60 to 85 seconds. In some further embodiments, the mixing in step (b) is performed at the low speed from about 615 rpm to about 650 rpm for about 70 seconds.

[0095] In any embodiments of the processes described herein, steps (d), (e) and (f) are conducted with a crossflow filtration system that is configured to switch between microfiltration and diafiltration mode, wherein the crossflow filtration system comprises a plurality of independently operating crossflow modules. In some embodiments, each crossflow module comprises at least one filter array, and each filter array comprises a plurality of hollow fiber filters. In some further embodiments, each crossflow module comprises two filter arrays, and each filter array comprises six hollow fiber filters. In some further embodiments, the crossflow filtration system comprises four filter arrays, and each filter array comprises six hollow fiber filters. In some embodiments, the crossflow filtration system further comprises at least one turbidity sensor dow nstream of the filter array for detection of loss of filter integrity during active manufacture.

[0096] FIGs. 1A-1B are process flow charts, each depicting a portion of the bupivacaine MVLs manufacturing process 100 according to some embodiments described herein. The circled A symbol indicates the connection point between FIG. 1 A and FIG. IB. As shown in FIGs. 1A-1B, bupivacaine MVLs is produced via an aseptic double-emulsion process. The bulk manufacturing system is a closed, sterilized system into which all process solutions are sterile- filtered through 0.2 pm filters.

[0097] As shown in FIG. 1A, the process 100 includes step 102, wherein DEPC, DPPG, cholesterol, tricaprylin, and bupivacaine are dissolved in methylene chloride to form a lipid / drug solution 102. At step 103, the lipid solution is filtered through a 0.2 pm membrane filter into a sterilized vessel. At step 104, phosphoric acid is dissolved in WFI (water for injection) to form a H3PO4 solution (first aqueous solution). At step 105, the H3PO4 solution is filtered through a 0.2 pm membrane filter into a sterilized vessel. Under aseptic conditions, the filtered lipid / drug solution is combined ith the filtered H3PO4 solution in a volume ratio of 1: 1 at an emulsification step 106 using agitation to produce a w / o emulsion (i.e., first emulsion). High shear mixing of the lipid / drug solution with the phosphoric acid solution is performed, wherein bupivacaine is ionized by the phosphoric acid and partitions into the internal aqueous phase. This forms a water-in-oil first emulsion. In some embodiments, the volume of this water in oil first emulsion can be about 200L to about 260L. In some embodiments, the volume of the water in oil first emulsion is about 200L, 210L, 220L, 230L, or 240L. In some alternative embodiments, bupivacaine may be present in the first aqueous solution additionally or alternatively to being present in the lipid / drug solution.

[0098] At step 107, lysine and dextrose are combined in WFI to form a dextrose / lysine solution (second aqueous solution). In certain embodiments, the dextrose / lysine solution may be kept at a temperature of about 19 °C, about 19 °C or less, about 18 °C and about 19 °C, or about 18 °C to about 20 °C.

[0099] At step 108, the dextrose / lysine solution is filtered through a 0.2 pm membrane filter into a sterilized vessel (e g., a sparging vessel). In certain embodiments, the dextrose / lysine solution in the sterilized vessel may be kept at a temperature of about 19 °C, about 19 °C or less, about 18 °C to about 19 °C, or about 18 °C to about 20 °C. Under aseptic conditions, the filtered dextrose / lysine solution is added to the w / o emulsion in a volume ratio of approximately 2.5: 1 at an emulsification step 109 using agitation to produce a water-in-oil-in-water emulsion (i.e., second emulsion).

[0100] At emulsification step 109, agitation is performed at lower shear, producing a water-in-oil-in-water (w / o / w) second emulsion with the majority of the bupivacaine resident in the internal aqueous phase. In some embodiments, the volume of this second emulsion can be from about 700 L to about 860 L. Additional filtered dextrose / lysine solution is added to the w / o / wemulsion at a dilution step 110 to form a diluted water-in-oil-in-water emulsion of MVLs and bringing the final volume ratio to approximately 20: 1 (dextrose / lysine solution to water-in-oil emulsion) with mixing. In some embodiments, the volume of the diluted water-in-oil-in-water second emulsion can be from about 4000 L to about 5200 L or from about 4200 L to about 5040 L. The diluted w / o / w second emulsion can have a temperature of from about 18 °C to about 22 °C. In some embodiments, the diluted w / o / w second emulsion can have a temperature of about 19 °C, about 19 °C or less, about 18 °C to about 19 °C, or about 18 °C and about 20 °C (e.g., due to the temperature of the dextrose / lysine solution).

[0101] At step 111, the diluted water-in-oil-in-water emulsion of MVLs is sparged wi th sterile nitrogen to remove at least a portion of the methylene chloride. In some embodiments, the sparge gas flow rate, liquid temperature, and dimensions of the sparge vessel have been found to impact the sparging process. In some embodiments, the duration of sparge, size and number of sparge tubes, vessel heating capacity’, number of sparge holes, size of sparge holes, and location of sparge tubes have been found to impact the sparging process. In some embodiments, the sparge vessel comprises a vertical cylindrical vessel with a diameter to height ratio of about 0.6, 0.7, 0.8, 0.9 or 1.0, or any ratio therebetween. In some embodiments, the diameter to height ratio is about 0.8. This relatively taller and reduced diameter sparge vessel (as compared to the sparge vessel used in the UK 200 L process) results in increased sparge efficiency for substantially removing methylene chloride. In some embodiments, the relatively taller and reduced diameter sparge vessel in combination with the number and location of sparge tubes results in increased sparge efficiency for substantially removing methylene chloride. In some embodiments, sparging comprises bubbling nitrogen through the diluted emulsion at sparge gas flow rate of about 1874 SLPM (standard liters per minute) to about 2500 SLPM. In some embodiments, the sparge gas flow rate can be about 2400 SLPM.

[0102] In some embodiments, sparging is performed for about 19 minutes to about 25 minutes. In some embodiments, sparging is performed for about 19 minutes, about 20 minutes, about 21 minutes, about 22 minutes, about 23 minutes, about 24 minutes, about 25 minutes, or any value therebetween. In some embodiments, sparging is performed for about 22 minutes. If sparging is not performed for a sufficiently long period of time, too much volatile solvent may remain in the diluted w / o / w emulsion of MVLs. If sparging is performed for too long of a period of time, excess MVL breakage can occur. In some embodiments, excess MVL breakage can hurt the product yield. In some embodiments, excess MVL breakage can cause an excessive pH decrease, which may result in bupivacaine in the second aqueous solution to crystalize and cause batch manufacture failure. In some embodiments, pH may be monitored to determine whensparging is complete. In some embodiments, conductivity values can be monitored to determine when sparging is complete.

[0103] It was observed that in some embodiments, a lower sparge gas flow' rate such as 1874 SLPM with a longer sparge time such as 25 minutes, or a higher sparge gas flow rate such as 2500 SLPM with a shorter sparge time such as 20 minutes, can each be sufficiently effective at substantially removing methylene chloride. Between the two approaches, the higher sparge gas flow' rate and shorter sparge time approach were observed to result in improved product yield, increasing production capacity for bupivacaine encapsulated MVLs (e.g.. due to reduced bupivacaine encapsulated MVL destruction during sparging).

[0104] In certain embodiments, it has been found that sparging at a lower temperature (e.g., a temperature of about 19 °C, about 19 °C or less, about 18 °C to about 19 °C, or about 18 °C to about 20 °C) is effective at increasing yield in comparison to a higher temperature. In some embodiments, the temperature of the diluted second emulsion during the sparge process is about 19 °C. In some embodiments, the second aqueous solution is supplied and / or maintained at a lower temperature such that the diluted second emulsion is at the lower temperature. In some embodiments, the second aqueous solution is supplied and / or maintained at a temperature of about 19 °C, about 19 °C or less, about 18 °C to about 19 °C, or about 18 °C to about 20 °C.

[0105] Sparging the diluted emulsion to remove at least a portion of the methylene chloride forms a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume. In some embodiments, the first volume can be about 4000 L to about 5000 L.

[0106] As descried herein, in some embodiments in which sparging is performed at lower temperatures (e.g.. about 19 °C, about 19 °C or less, about 18 °C and about 19 °C, or about 18 °C to about 20 °C), higher shear mixing speeds can be used at step 109, such as shear mixing speeds of about 520 rpm, at least about 520 rpm, about 535 rpm, at least about 535 rpm, about 575 rpm, at least about 575 rpm, about 630 rpm, at least about 630 rpm or from 520 rpm to about 680 rpm.First Microfiltration

[0107] FIG. IB depicts additional steps of process 100. After sparging at step 111, the diluted suspension of bupivacaine MVLs is concentrated via aseptic microfiltration at step 112. In some embodiments, the diluted suspension is concentrated to a bupivacaine concentration of about 4.0 mg / mL to about 6.7 mg / mL or approximately 4.5 mg / mL. This first microfiltration reduces the first volume of the first aqueous suspension to form a second aqueous suspension having a second volume. In some embodiments, the second volume includes about 200 L to 480 L in the sparge vessel, as well as about 400 L to about 550 L in the tangential flow filtration (TFF)filters and the connecting piping to the sparge vessel. In some embodiments, the first volume is reduced by about 75% - 90%.

[0108] In some embodiments, the first microfiltration comprises circulating the first aqueous suspension past at least one tangential flow filter, thereby reducing the first volume as a portion of the first aqueous suspension that is less than a membrane pore size (e.g., less than about 0.2 microns) of the tangential flow filter(s) passes through the tangential flow filter(s) as permeate, and a portion not removed as permeate is recirculated. The tangential flow filter(s) can be arranged in tangential flow filtration modules, as described with respect to FIG. 2A below. It was observed that increasing the feed flow rate of the first aqueous suspension during this first microfiltration can provide smaller particle size distribution of MVLs in the final product. The feed flow rate of the first microfiltration is summed across the input streams of all filter modules to describe a total first microfiltration feed flow rate. In some embodiments, as described herein, the total first microfiltration feed flow rate can be about 190 L / min to about 350 L / min or about 250 L / min to about 350 L / min per TFF array.

[0109] As described herein, in some embodiments, the feed flow rate of the first microfiltration decreases (e.g., linearly or approximately linearly) between the start and end of the first microfiltration in relation to the level of liquid in the sparging vessel or the bupivacaine MVLs concentration in the aqueous suspension. In some embodiments, the total first microfiltration feed flow rate can be about 340 L / min or about 290 L / min to about 350 L / min at the start of microfiltration for each TFF array. In some embodiments, the total first microfiltration feed flow rate can be about 300 L / min or from about 250 L / min to about 310 L / min per TFF array. As described in any embodiments of the present disclosure, the feed flow rate of the first microfiltration step refers to the total feed flow rate per TFF array.Diafiltration

[0110] At step 113, a NaCl solution is formed by dissolving sodium chloride in WFI. At step 114, the NaCl solution (i.e., sahne solution) is filtered through a 0.2 pm membrane filter.[OHl] Under aseptic conditions, the bupivacaine MVLs concentrate (second aqueous suspension) formed at step 112 is subjected to diafiltration in step 115. In some embodiments, diafiltration crossflow filtration by at least four volumes or at least 4.5 volumes of the filtered NaCl solution through introduction of the filtered NaCl solution into a filtration apparatus or system through multiple 0.2 pm hollow fiber filter membrane unit filters at a diafiltration step 115. Diafiltration step 115 is used to remove unencapsulated bupivacaine, lysine, dextrose and residual methylene chloride. This diafiltration step exchanges a portion of the second aqueous suspension that is less than a membrane pore size (e.g., less than about 0.2 microns) of the tangential flowfilter(s) with a saline solution to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume. In some embodiments, the third volume can be about 675 L to about 945 L.

[0112] It was observed that increasing the feed flow rate of the second aqueous suspension during diafiltration can lower the particle size distribution of MVLs in the final product. The feed flow rate of the diafiltration process is summed across the input streams of each array of filters (e.g., six filters / array) to describe a total diafiltration feed flow rate. In some embodiments, the total diafiltration feed flow rate is about 190 L / min to about 310 L / min for each TFF array.

[0113] In some embodiments, the diafiltration is performed at at least two stages comprising an initial stage and a later stage. The initial stage may comprise a higher total diafiltration feed flow rate than the later stage. In some embodiments, the diafiltration process may begin with the initial stage, then continues with the initial stage until it begins the later stage, then continues with the later stage until the diafiltration is complete. The total diafiltration feed flow rate can be described for these two stages as an initial stage total diafiltration feed flow rate and a later stage total diafiltration feed flow rate.

[0114] In some embodiments, an initial or first stage total diafiltration feed flow rate is about 190 L / min to about 310 L / min for each TFF array. In some embodiments, the initial stage total diafiltration flow rate is about 300 L / min per TFF array. In some embodiments, the later or second stage total diafiltration feed flow rate is about 190 L / min to about 265 L / min per TFF array. In some embodiments, the later stage total diafiltration feed flow rate is about 255 L / min per TFF array. As described in any embodiments of the present disclosure, the feed flow rate of the diafiltration step refers to the total feed flow rate per TFF array.

[0115] At step 116, sterile nitrogen is used to flush the headspace of the crossflow filtration apparatus or system to further reduce residual methylene chloride content and final product pH. In some embodiments, step 116 can be performed in parallel with step 115.Second Microfiltration

[0116] At step 117, the third aqueous suspension is subjected to a second microfiltration, reducing the third volume of the third aqueous suspension and providing a final aqueous suspension of bupivacaine encapsulated MVLs having a target concentration. In some embodiments, the solution is concentrated via aseptic microfiltration in concentrate step 117 to form an initial bulk suspension of MVLs at a target weight / volume that corresponds to a bupivacaine concentration of 12.3-16.6 mg / mL.

[0117] In some embodiments, the second microfiltration comprises circulating the third aqueous suspension past at least one tangential flow filter, thereby reducing the third volume as a portion of the third aqueous suspension that is less than a membrane pore size (e g., less than about 0.2 microns) of the tangential flow filter(s) passes through the tangential flow filter(s) as permeate, and a portion not removed as permeate is recirculated. The tangential flow filter(s) can be arranged in tangential flow filtration modules, as described in the section below. The feed flow rate of the second microfiltration is summed across the input streams of all filter modules to describe a total second microfiltration feed flow rate. In some embodiments, the total second microfiltration feed flow rate is about 120 L / min to about 265 L / min for each TFF array.

[0118] As described herein, in some embodiments, the feed flow rate of the second microfiltration decreases (e.g., linearly or approximately linearly) between the start and end of the second microfiltration in relation to the level of liquid in the concentration vessel or the bupivacaine MVLs concentration in the aqueous suspension. In some embodiments, the total second microfiltration feed flow rate can be about 255 L / min or from about 190 L / min to about 265 L / min at the start of microfiltration per TFF array. In some embodiments, the total second microfiltration feed flow rate can be about 180 L / min or from about 120 L / min to about 190 L / min at the end of microfiltration per TFF array. As described in any embodiments of the present disclosure, the feed flow rate of the second microfiltration step refers to the total feed flow rate per TFF array.

[0119] The bulk product is then transferred into a sterilized holding vessel. The initial bulk suspension of MVLs is sampled and bupivacaine concentration is measured. In certain embodiments, the product yield can be about 75% to about 83%, where the product yield is calculated by dividing the total amount of bupivacaine in the bulk suspension of MVLs by a total amount of bupivacaine in the first emulsion vessel (excluding transfer hold up loss). In some embodiments, the product yield is, or is at least about 75%, 76%, 77%, 78%, 79%, 80%, 81%, 82%, 83%, 84% or 85%. or a range defined by any two of the preceding values.

[0120] Optionally, if the initial bulk suspension of MVLs is designated to be filled as an individual lot, the initial bulk suspension of MVLs is concentrated further via sedimentation (gravitational settling) and / or decantation to a bupivacaine concentration of approximately 13.3 mg / mL, or alternatively diluted with a filtered NaCl solution to a bupivacaine concentration of approximately 13.3 mg / mL at a decantation and / or dilution step 120 to form an adjusted bulk suspension of MVLs. The saline solution that is optionally used at step 120 can be formed by dissolving sodium chloride in WFI at step 118 and filtered through a 0.2 pm membrane filter at step 119.Example of Additional Process for Increased Final Product Volume and Yield

[0121] Additional embodiments of the present application relate to an improved process for producing large batches of bupivacaine encapsulated multivesicular liposomes (MVLs) with an increased final product volume and / or yield, as compared to the process described above with up to 300 L final batch volume with lower initial concentrations of bupivacaine, lipid components, and components of the second aqueous solution.

[0122] It was observed that increasing the initial concentration of the components of the first aqueous solution, second aqueous solution and the volatile water-immiscible solvent solution can result in a larger final product volume, while maintaining the same particle composition and substantially the same particle size as bupivacaine MVLs produced by the manufacturing process using lower initial concentrations of MVL and second aqueous solution components. This process relies on generating a first emulsion particle with higher concentrations of bupivacaine and lipid components with higher osmotic pressure (e.g., at least 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, 70% or 75% more osmotic pressure than the process described previously with up to 300 L final batch volume.

[0123] An example process for increased final product volume and yield may include:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water-immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water-immiscible solvent solution comprises at least one phosphatidyl choline, at least one phosphatidyl glycerol, cholesterol, and at least one neutral lipid, and wherein either the first aqueous solution or the volatile water-immiscible solvent solution comprises bupivacaine;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a water-in-oil-in-water second emulsion;(c) substantially removing the volatile water-immiscible solvent from the water- in-oil-in-water second emulsion by sparging the water-in-oil-in-water second emulsion to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 400 L / min);(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLshaving a third volume, wherein the diafiltration feed flow rate is at least 190 L / min (e.g., about 200 to about 350 L / min); and(f) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a final aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from about 12 mg / mL to about 17 mg / mL; wherein the final aqueous suspension of bupivacaine encapsulated MVLs has a volume of about, or at least about 300 L, 350 L, 400 L, 450 L, 500 L, 550 L, 600 L, 650 L, 700 L, 750 L, 800 L, 850 L, 900 L, 950 L or 1000 L; and wherein the process has a bupivacaine encapsulated MVLs product yield of at least at least about 75% (for example, about 75, 76, 77, 78, 79, 80, 81, 82, 83, 84, 85, 86, 87, 88 or 89%, or a range defined by any two of the preceding values). In some embodiments, the sparging in step (c) is conducted at a temperature of about 18°C to about 20°C.

[0124] Unless otherwise specified herein, the steps for the process for increased final product volume and yield, for example, steps (a), (b), (c), (d), (e) and (f), may be performed in the same or substantially similar manner as previously described herein (e.g., with respect to Figures 1A-1B). Additionally, any other features, parameters, or conditions associated with these steps may be the same or substantially similar to those described above, unless otherwise specified.

[0125] In some embodiments, the concentration of bupivacaine in the solvent solution is from about 20 mg / mL to about 160 mg / mL, from about 30 mg / mL to about 140 mg / mL, from about 40 mg / mL to about 80 mg / mL, from about 50 mg / mL to about 70 mg / mL, from about 60 mg / mL to about 100 mg / mL, from about 75 mg / mL to about 95 mg / mL, from about 80 mg / mL to about 90 mg / mL, or from about 110 mg / mL to about 130 mg / mL. In some embodiments, the concentration of DEPC in the solvent solution is from about 10 mg / mL to about 90 mg / mL, from about 20 mg / mL to about 80 mg / mL, from about 25 mg / mL to about 35 mg / mL, from about from about 30 mg / mL to about 45 mg / mL, from about 35 mg / mL to about 50 mg / ml, or from about 40 mg / mL to about 55 mg / mL. In some embodiments, the concentration of cholesterol in the solvent solution is from about 5 mg / mL to about 50 mg / mL, from about 10 mg / mL to about 40 mg / mL, from about 15 mg / mL to about 35 mg / mL, from about 20 mg / mL to about 25 mg / mL, from about 25 mg / mL to about 30 mg / mL, or from about 30 mg / mL to about 35 mg / mL. In some embodiments, the concentration of DPPG in the solvent solution is from about 0.5 mg / mL to about 30 mg / mL. from about 1 mg / mL to about 20 mg / mL, from about 2 mg / mL to about 10 mg / mL, from about 2.5 mg / mL to about 4 mg / mL, from about 3 mg / mL to about 5 mg / mL, or from about 6 mg / mL to about 8 mg / mL. In some embodiments, the concentration of tricaprylin in the solvent solution is from about 0.5 mg / mL to about 40 mg / mL, from about 1 mg / mL to about 30 mg / mL, from about 2 mg / mL to about 20 mg / mL, from about 3 mg / mL to about 15 mg / mL, from about 4mg / mL to about 7 mg / mL, from about 8 mg / mL to about 10 mg / mL, or from about 12 mg / mL to about 15 mg / mL.

[0126] A higher concentration of initial components (e.g. bupivacaine, DPPG, DEPC, tricaprylin and cholesterol), a greater amount of initial components can be provided in the same volume as with a lower concentration of initial components. Beginning with a greater amount of the initial components of the solvent solution (e.g., bupivacaine, DPPG, DEPC, tricaprylin and cholesterol) and greater concentration of the second aqueous components (e.g., lysine and dextrose), can allow for generation of more first emulsion droplets and more second emulsion spherules, resulting in a greater number of particles in the final product, and thereby an increase the final product volume as compared to the process described above with up to 300 L final batch volume. The second aqueous solution comprises lysine and an osmotic agent such as dextrose. In some embodiments, the concentration of lysine in the second aqueous solution is from about 0.2 mg / mL to about 20 mg / mL, from about 1 mg / mL to about 10 mg / mL, from about 2 mg / mL to about 8 mg / mL, from about 2.5 mg / mL to about 5 mg / mL, or from about 5 mg / mL to about 7 mg / mL. In some further embodiments, the concentration of dextrose in the second aqueous solution is from about 10 mg / mL to about 150 mg / mL, from about 20 mg / mL to about 100 mg / mL, from about 30 mg / mL to about 80 mg / mL, from about 40 mg / mL to about 70 mg / mL, about 45 mg / mL to about 60 mg / mL, or about 70 mg / mL to about 90 mg / mL.

[0127] Increasing the initial concentration of the components of the solvent solution can lead to a higher osmotic pressure of the solvent solution. Osmotic pressure is the minimum pressure which needs to be applied to a solution to prevent the inward flow of its pure solvent across a semipermeable membrane. To account for the increased osmotic pressure, the first emulsion droplet size and the second emulsion spherule size may be adjusted. In certain embodiments, a smaller first emulsion droplet size and a smaller second emulsion spherule size may be desired. In some embodiments, the mixing speed and / or mixing time in step (a) can be selected to provide a desired first emulsion droplet size. In some embodiments, the mixing speed and / or mixing time in step (b) can be selected to provide a desired spherule size. Smaller first emulsion droplets and second emulsion spherules can be obtained by using a higher shear speed compared to the shear speed used when lower initial concentrations are used. The particle size of bupivacaine MVLs in the final product may be the same or similar to the particle size in the final product produced by the manufacturing process described above when using lower initial concentrations. The bupivacaine MVLs composition may remain the same as the final product produced by the manufacturing process described above.

[0128] In some embodiments of the process for increased final product volume and yield described herein, the mixing in step (a) is performed using a first mixer at a high shear speed.In some embodiments, the high shear speed is from about 1000 rpm to about 1600 rpm. For example, in some embodiments, the high shear speed is about 1000, about 1100 rpm, about 1120 rpm, about 1140 rpm, about 1160 rpm, about 1180 rpm, about 1200 rpm, about 1220 rpm, about 1240 rpm, about 1260 rpm, about 1280 rpm, about 1300 rpm, about 1320 rpm, about 1340 rpm, about 1360 rpm, about 1380 rpm, about 1400 rpm, about 1420 rpm, about 1440 rpm, about 1460 rpm, about 1480 rpm, about 1500 rpm, about 1520 rpm, about 1540 rpm, about 1560 rpm, about 1580 rpm, about 1600 rpm, or a range defined by any of the two preceding values. In some embodiment, the high shear speed is about 1300 rpm to about 1380 rpm. In some further embodiments, the high shear speed is from about 1320 rpm to about 1360 rpm, about 1330 rpm, or about 1350 rpm. In some such embodiments, the mixing in step (a) is performed for about 45 minutes to about 100 minutes, for example, about 45, 46, 47, 48, 49, 50, 51, 52, 53, 54, 55, 56, 57, 58, 59, 60, 61, 62, 63, 64, 65, 66, 67, 68, 69, 70, 71, 72, 73, 74, 75, 76, 77, 78, 79, 80, 81, 82, 83, 84, 85, 86, 87, 88, 89, 90, 91, 92, 93. 94. 95, 96, 97, 98, 99 or 100 minutes, or a range defined by any two of the preceding values.

[0129] In some embodiments of the process for increased final product volume and yield described herein, the mixing in step (b) is performed using a second mixer at a low shear speed. In some embodiments, the low shear speed is from about 500 rpm to about 1000 rpm. In some embodiments, the low shear speed is for example, about 500 rpm. about 520 rpm. about 540 rpm, about 560 rpm, about 580 rpm, about 600 rpm, about 620 rpm, about 640 rpm, about 660 rpm, about 680 rpm, about 700 rpm, about 720 rpm, about 740 rpm, about 760 rpm, about 780 rpm, about 800 rpm, about 820 rpm, about 840 rpm, about 860 rpm, about 880 rpm, about 900 rpm, about 920 rpm, about 940 rpm, about 960 rpm, about 980 rpm, about 1000 rpm, or a range defined by any of the two preceding values. In some further embodiments, the low shear speed is from about 715 rpm to about 750 rpm, or about 730 rpm. In some embodiments, the mixing in step (b) is performed for about 45 to about 120 seconds, from about 55 to about 100 seconds, or from about 65 to about 80 seconds, or about 70 seconds. In some embodiments, the mixing in step (b) is performed for about 45, 46, 47, 48, 49, 50, 51, 52. 53. 54. 55. 56, 57, 58, 59, 60, 61, 62, 63, 64, 65, 66, 67, 68, 69, 70, 71, 72, 73, 74, 75, 76, 77, 78, 79, 80, 81, 82, 83, 84, 85, 86, 87, 88, 89 or 90, 91, 92, 93, 94, 95, 96, 97, 98, 99, 100, 101, 102, 103, 104, 105, 106, 107, 108, 109, 110, 111, 112, 113, 114, 115, 116, 117, 118, 119, 120 seconds, or a range defined by any two of the preceding values.

[0130] In certain embodiments, a manufacturing process as described herein using a solvent solution having components with a concentration of about 1.5 times those of reference solvent solution can result in a final product having a volume of about or at least about 1.5 times greater than that of a process performed using the reference solvent solution. In someembodiments, a manufacturing process as described herein using a solvent solution having components with a concentration of about 2 times those of reference solvent solution can result in a final product having a volume of about or at least about 2 times greater than that of a process performed using the reference solvent solution. In some embodiments, a manufacturing process as described herein using a solvent solution having components with a concentration of about 2.5 or 3 times those of reference solvent solution can result in a final product having a volume of about or at least about 2.5 or 3 times greater than that of a process performed using the reference solvent solution.

[0131] In some embodiments of the process for increased final product volume and yield described herein, the final aqueous suspension of bupivacaine encapsulated multi vesicular liposomes has a volume of at least about 300 L. In one embodiment, the final aqueous suspension of bupivacaine encapsulated multi vesicular liposomes has a volume of about 400 L to about 600 L. In one embodiment, the final aqueous suspension of bupivacaine encapsulated multivesicular liposomes has a volume of about 450 L to about 550 L. In some embodiment, the final aqueous suspension of bupivacaine encapsulated multivesicular liposomes has a volume of about 400 L to about 1000 L, e.g., about 400, 410, 420, 430, 440, 450, 460, 470, 480, 490, 500, 510, 520, 530, 540, 550, 560, 570, 580. 590, 600, 610. 620, 630, 640. 650, 660, 670. 680, 690, 700, 710, 720, 730, 740, 750, 760, 770. 780, 790, 800. 810, 820, 830. 840, 850, 860. 870, 880, 890. 900, 910, 920, 930, 940, 950, 960, 970, 980, 990, or 1000 L, or a range defined by any two of the preceding values. In some such embodiments, the target concentration of the bupivacaine in the final aqueous suspension (i.e., bulk product suspension) is from about 12 mg / mL to about 17 mg / mL, or from about 12.3 mg / mL to about 16.6 mg / mL.

[0132] The process for increased final product volume and yield can also increase the product yield by increasing the initial concentration of the components of the solvent solution and adjusting other processing conditions, for example, the mixing speed and mixing time for forming the first and second emulsions. In some embodiments, the product yield is. or is at least about 80%. 81%. 82%. 83%. 84%. 85%. 86%.87%, 88%, 89% or 90%.Tangential Flow Filtration Modules

[0133] Some embodiments of the present application relates to a crossflow filtration system comprising: a diafiltration vessel; and a plurality of independently operating crossflow modules, each crossflow module of the plurality of independently operating crossflow modules comprising at least one filter array, each filter array comprising a plurality of hollow fiber filters, wherein each crossflow module of the plurality of independently operating crossflow modules is connected to a retentate conduit, a permeate conduit, and a rotary lobe pump. In someembodiments, the crossflow filtration system may be used in the microfiltration and / or diafiltration step of the commercial process described herein.

[0134] In some embodiments, each crossflow module comprises two filter array s. In some embodiments, each crossflow module comprises at least five hollow fiber filters or at least six follow fiber filters. In some such embodiments, each filter array comprises at least two. three, four, five or six hollow fiber filters.

[0135] In some embodiments, the plurality of independently operating crossflow modules comprises a first crossflow module and a second crossflow module, wherein the first crossflow module is coupled to a first rotary lobe pump and the second crossflow module is coupled to a second rotary lobe pump operating independently of the first rotary lobe pump. In some further embodiments, the first crossflow module is coupled to the diafiltration vessel by a first retentate conduit to facilitate flow of retentate from the first crossflow module to the diafiltration vessel, and wherein the second crossflow module is coupled to the diafiltration vessel by a second retentate conduit to facilitate flow of retentate from the second crossflow module to the diafiltration vessel. In some further embodiments, the first rotary lobe pump comprises a fluid outlet coupling the first rotary lobe pump to the first crossflow module, and wherein the second rotary lobe pump comprises a fluid outlet coupling the second rotary lobe pump to the first crossflow module. In some further embodiments, the first rotary lobe pump comprises a fluid inlet coupling the first rotary lobe pump to the diafiltration vessel, and wherein the second rotary lobe pump comprises a fluid inlet coupling the second rotary lobe pump to the diafiltration vessel.

[0136] In some embodiments, the first crossflow module operates independently from the second crossflow module. In some such embodiments, only one of the first crossflow module and the second crossflow module is in use during the operation of the crossflow filtration system. In other embodiments, both the first crossflow module and the second crossflow module are in use during the operation of the crossflow filtration system.

[0137] In some embodiments, each of the plurality of independently operating crossflow modules comprises a microfiltration mode and a diafiltration mode.

[0138] In some embodiments, the crossflow filtration system further comprises a nitrogen flushing module to blow a stream nitrogen over the retentate in the diafiltration vessel.

[0139] Some further embodiments of the present application relate to a process of manufacturing bupivacaine encapsulated multivesicular liposomes using the crossflow module described herein, the process comprising: reducing a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume by microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume;exchanging a portion of the second aqueous suspension that is less than a membrane pore size (e.g., less than about 0.2 microns) of the tangential flow filter(s) with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume; and further reducing the third volume of the third aqueous suspension by microfiltration to provide a final aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine.

[0140] In some embodiments, the process further comprises blowing a stream of nitrogen over the second aqueous suspension during the diafiltration / saline exchange step. In some further embodiments, the diafiltration include at least 3, 3.5, 4, 4.5, or 5 exchange volumes of the saline solution such that the aqueous supernatant of the second aqueous suspension is substantially (e.g., at least 95%, 96%, 97%, 98%, 99%) replaced by the saline solution. In some embodiments, the diafiltration includes 4.5 exchange volumes.

[0141] FIG. 2A depicts an embodiment of a system 200 including components for performing embodiments of a manufacturing process as described herein.

[0142] In certain embodiments, the system 200 can include a preparation vessel 220. In certain embodiments, the vessel 220 can be used for a lipid / drug solution formation step of a commercial scale manufacturing process as described herein, such as step 102 of the process 100. In certain embodiments, DEPC, DPPG, cholesterol, tricaprylin, WFI, bupivacaine, and methylene chloride added to the vessel 220 and mixed to form a lipid / drug solution within the vessel 220.

[0143] In certain embodiments, the system 200 can include a preparation vessel 222. In certain embodiments, the vessel 222 can be used in a first aqueous solution formation step of a commercial scale manufacturing process as described herein, such as step 104 of the process 100. In certain embodiments, phosphoric acid and WFI can be mixed within the preparation vessel 222 to form the first aqueous solution.

[0144] In certain embodiments, the system 200 can include an emulsification vessel 224. In certain embodiments, the vessel 224 can be used in a w / o emulsion step of a commercial scale manufacturing process as described herein, such as step 106 of the process 100. In certain embodiments, the lipid / drug solution from vessel 220 and the first aqueous solution from vessel 222 can be transferred to the emulsification vessel 224 and mixed to form a w / o first emulsion.

[0145] In certain embodiments, the system 200 can include a preparation vessel 226. In certain embodiments, the vessel 226 can be used in a dextrose / lysine solution formation step of a commercial scale manufacturing process as described herein, such as step 107 of the process 100. In certain embodiments, lysine, dextrose, and WFI can be added to the vessel 226 and mixed until dissolved to form a dextrose / lysine solution.

[0146] In certain embodiments, the system 200 can include a sparge / diafiltration vessel 228. In certain embodiments, the dextrose / lysine solution can be transferred to the vessel 228 after formation.

[0147] In certain embodiments, the vessel 224 can be used in a w / o / w second emulsion step of a commercial scale manufacturing process as described herein, such as step 109 of the process 100. In certain embodiments, a predetermined amount of the dextrose lysine solution can be transferred from the vessel 228 to the vessel 224 and mixed with the w / o emulsion to form a w / o / w emulsion within the vessel 224.

[0148] In certain embodiments, the vessel 228 can be used for a step of forming a diluted suspension of a commercial scale manufacturing process as described herein, such as step 110 of the process 100. In certain embodiments, the w / o / w emulsion from vessel 224 can be transferred to vessel 228 containing the remaining volume of the dextrose / lysine solution.

[0149] In certain embodiments, the vessel 228 can be used in a sparging step of a commercial scale manufacturing process as described herein, such as step 1 10 of the process 100. Sparging with nitrogen can then be performed in the vessel 228 to substantially remove methylene chloride to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume.

[0150] In certain embodiments, the system 200 can include a crossflow filtration system 250 (tangential flow filter). The filtration system 250 can be used in microfiltration and / or diafiltration steps of a commercial scale manufacturing process as described herein, such as steps 115, 116, and / or 117 of the process 100.

[0151] In certain embodiments, the filtration system 250 can be used in a concentration step of a commercial scale manufacturing process as described herein, such as step 112 of the process 100. In certain embodiments, the crossflow filtration system 250 can be used in a microfiltration mode to reduce the total volume of the first aqueous suspension of bupivacaine encapsulated MVLs to form a second suspension of bupivacaine encapsulated MVLs having a second volume.

[0152] In certain embodiments, vessel 226 can be used in a saline solution formation step of a commercial scale manufacturing process as described herein, such as step 113 of the process 100. In certain embodiments, sodium chloride and WFI can be added to the vessel 226 and mixed to form a saline solution.

[0153] In certain embodiments, the filtration system 250 can be used in a diafiltration step of a commercial scale manufacturing process as described herein, such as step 115 of the process 100. In certain embodiments, the crossflow filtration system 250 can be used in adiafiltration mode to undergo several volume exchanges with the saline solution to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume.

[0154] In certain embodiments, the filtration system 250 can be used in a nitrogen flushing step of a commercial scale manufacturing process as described herein, such as step 116 of the process 100. In certain embodiments, the head space of the crossflow filtration system 250 or portions thereof can be flushed with nitrogen to reduce pH and methylene chloride content during diafiltration.

[0155] In certain embodiments, the filtration system 250 can be used in a concentration step of a commercial scale manufacturing process as described herein, such as step 117 of the process 100. In certain embodiments, the crossflow filtration system 250 can be used in microfiltration mode to provide a final suspension of bupivacaine encapsulated multivesicular liposomes having a target concentration of bupivacaine. In some embodiments, the system 200 can include a concentration vessel 230. In certain embodiments, the vessel 230 can be used in a concentration step of a commercial scale manufacturing process as described herein, such as step 117 of the process 100. In some embodiments, during this microfiltration, the dilute product can be transferred to the concentration vessel 230, where microfiltration can be continued until the volume is reduced to the target volume.

[0156] In certain embodiments, the system 200 can include a final product vessel 232 that can receive the final suspension after reduction to the target volume.

[0157] The filtration system 250 includes independently operating crossflow modules 202a and 202b. Crossflow module 202a includes a filter array 204a and a filter array 204b. Crossflow module 202b includes a filter array 204c and a filter array 204d. Each filter array 204a- d may include two or more hollow fiber filters. In some embodiments, each filter array includes five or more or six or more hollow fiber filters.

[0158] As shown in Figure 2A, the system may be connected to a sparge / diafiltration vessel 228. Retentate can flow from the crossflow module 202a to the vessel 228 via a retentate return conduit 208a. For example, the retentate return conduit 208a can be in fluid communication with both the filter array 204a and the filter array 204b (e.g., via a transfer panel) to receive retentate flowing therefrom. Retentate can flow from the crossflow module 202b to the vessel 228 via a retentate return conduit 208b. For example, the retentate return conduit 208b can be in fluid communication with both the filter array 204c and the filter array 204d (e.g., via a transfer panel) to receive retentate flowing therefrom. Similarly, retentate can flow from the crossflow' module 202a to the concentration vessel 230 via the retentate return conduit 208a and retentate can flow from the crossflow module 202b to the concentration vessel 230 via the retentate return conduit 208b.

[0159] Permeate can flow from the crossflow module 202a for removal from the filtration system 250 via a permeate conduit 210a. For example, the permeate conduit 210a can be in fluid communication with both the filter array 204a and the filter array 204b (e.g., via a transfer panel) to receive permeate flowing therefrom. Permeate can flow from the crossflow module 202b for removal from the filtration system 250 via a permeate conduit 210b. For example, the permeate conduit 210b can be in fluid communication with both the filter array 204c and the filter array 204d (e.g., via a transfer panel) to receive permeate flowing therefrom.

[0160] The filtration system 250 may include or be used in conjunction with two independently operating rotary lobe pumps 212a and 212b. The pump 212a includes a fluid inlet 214a and a fluid outlet 216a. The pump 212b includes a fluid inlet 214b and a fluid outlet 216b. The pump 212a is connected to the vessel 228 via the inlet 214a and connected to crossflow module 202a via the outlet 216a. The pump 212b is connected to the vessel 228 via the inlet 214b and connected to the crossflow module 202b via the outlet 216b. The pump 212a is also connected to the vessel 230 via the inlet 214a. The pump 212b is connected to the vessel 230 via the inlet 214b.

[0161] In some embodiments of the processes described herein, the crossflow filtration system utilizes two independent rotary lobe pumps providing retentate flow to independent arrays of five or six hollow fiber filter housings. This configuration allows for smaller pipe diameters. Smaller pipe diameters can minimize the volume within the cross-flow filtration system 250 to allow for concentration to the target volume. Smaller pipe diameters may also allow for cleaning using lower flow rates than higher pipe diameters. In addition, the filtration module design allows for two filter arrays to be in-use during bulk operation while two filter arrays are being cleaned and sterilized in preparation for the next bulk production run. This configuration allows for shorter cycle times and increased manufacturing capacity. Furthermore, the improved filtration module design allows for independent hollow fiber filter housing isolation. This functionality automatically detects and isolates individual filter integrity failures, allowing the bulk cycle to proceed without offline testing and recleaning. In some further embodiments, the process may further comprise an additional product recovery step from one of the two filter array and / or a saline flush step, to allow for nearly complete product recovery from the transfer lines and thereby increasing product yield.

[0162] As described herein, during each of the microfiltration and diafiltrations steps when performed under normal operating conditions of the crossflow filtration system, a portion of the relevant aqueous suspensions (first, second, and third aqueous suspension) that is less than a membrane pore size (e.g., less than about 0.2 microns) of the tangential flow filter(s) passes through the tangential flow filter(s) as permeate, and a portion not removed as permeate isrecirculated. Filter integrity failures can lead to leakage of particles having a size greater than the membrane pore size during microfiltration and / or diafiltration, which may lead to clogging of downstream sterile boundary filter(s) (e.g., sterile boundary filter 242a, sterile boundary filter 242b). Filter clogging may prevent proper diafiltration and may lead to batch failure. Tangential flow filter integrity failures can be caused by high concentrations of methylene chloride, heating, and / or pressure fluctuations. Filter integrity failures can lead to leakage during microfiltration and / or diafiltration.

[0163] In some embodiments, the crossflow- filtration system comprises at least one turbidity sensor disposed on a permeate outlet stream to monitor the turbidity of the stream. In some embodiments of the commercial-scale process described herein, a turbidity sensor disposed on a permeate outlet stream of a tangential flow filter is used to monitor the turbidity of the permeate. Leakage of particles larger than the membrane pore size can result in change in turbidity of the permeate. By sensing sudden changes in permeate turbidity, the turbidity sensor can be used to detect tangential flow filter breakthroughs during microfiltration and diafiltration steps. Should the turbidity change suddenly, the system can identify which filter is not integral and automatically turn off the permeate flow from the identified filter. Adding this capability to the commercial-scale process described herein can decrease the failure rate of bupivacaine encapsulated MVL batch failures, increasing production and allowing increased usage of the filters.

[0164] In some embodiments, a turbidity sensor can be positioned dow nstream of the filter array to detect when a filter has lost its integrity. The filter that has lost its integrity can be identified and automatically disqualified. This approach can reduce the risk of batch failure due to filter breakage. Sensing by this turbidity’ sensor for loss of filter integrity may be performed during microfiltration and / or diafiltration.

[0165] In some embodiments, a turbidity sensor may be positioned downstream of each crossflow module 202a, 202b along a permeate outflow to measure turbidity in the permeate. As shown in FIG. 2A, a turbidity sensor 240a may be positioned along the permeate conduit 210a. A turbidity sensor 240b may be positioned along the permeate conduit 210b. In some embodiments, a single filter array of each crossflow- module may be in-use during a bulk operation. For example, the filter array 204a and the filter array 204c may be in use while the filter array 204b and the filter array 204d may be inactive. In such embodiments, the turbidity sensors measure the turbidity' in the permeate from only the in-use filter arrays. For example, the turbidity sensor 240a may measure the turbidity- of the permeate from the filter array 204a, and the turbidity sensor 240b may measure the turbidity- from the permeate of only the filter array 204c. In other embodiments, if both filter arrays within a crossflow module are in-use the related turbidity sensorcan measure the turbidity of the permeate from both filter arrays of the crossflow module. In other embodiments, each filter array (e.g., filter arrays 204a, 204b, 204c, and / or 204d) may have its own turbidity7sensor. For example, Figure 2B depicts an example of an alternative embodiment of a crossflow module 202a having a turbidity7sensor 240d for measuring turbidity in the permeate from the filter array 204a and a turbidity sensor 240e for measuring turbidity in the permeate from the filter array 204b. As shown, permeate from the filter array 204a may flow through a permeate conduit 21 la to the permeate conduit 210a. Permeate from the filter array 204b may flow through a permeate conduit 211b to the permeate conduit 210a. The turbidity sensor 240d may be positioned along the permeate conduit 211a. The turbidity sensor 240e may be positioned along the permeate conduit 211b. As shown in Figure 2B, retentate may flow from the filter array 204a through a retentate conduit 209a to the retentate return conduit 208a. Retentate may flow from the filter array 204b through a retentate conduit 209b to the retentate return conduit 208a.

[0166] In some embodiments, the crossflow module 202b may have any of the same and / or similar features and / or functions as the crossflow module 202a.

[0167] In some embodiments, each filter of a filter arrays (e.g., filter arrays 204a, 204b, 204c, and / or 204d) may have its own turbidity7sensor. For example, a distinct turbidity7sensor may be positioned to measure turbidity7of permeate from each filter.

[0168] In certain embodiments, a turbidity sensor may be used to identify a filter experiencing filter integrity failure so that the identified filter may be deactivated during a bulk operation. In some embodiments, each filter may have a distinct waste stream valve that may be closed to deactivate the filter and opened to reactivate the filter. In embodiments having a distinct turbidity sensor for each filter, a filter may be deactivated in response to an abnormal reading from its associated turbidity sensor (e.g., by closing its distinct waste stream valve).

[0169] In embodiments having a distinct turbidity7sensor for each filter array (as shown for example, in FIG. 2B), in response to an abnormal reading from a turbidity7sensor associated with a filter array, the filter of the filter array experiencing a filter integrity failure can be identified by deactivating the filters within the filter array one by one and measuring the resulting turbidity. If an abnormal turbidity value is detected when a particular filter is active but is not detected when that particular filter is inactive, the system 200 may determine that the particular filter is experiencing a filter integrity failure, and may deactivate the particular filter.

[0170] In embodiments having a distinct turbidity7sensor for each crossflow module (as shown for example, in FIG. 2A), in response to an abnormal reading from a turbidity sensor associated with the crossflow7module, the filter of the crossflow^ module experiencing a filter integrity7failure can be identified by deactivating the filters within a filter array (if only one filter array of a crossflow module is in-use) or the filters of the crossflow module (if both filter arraysof the crossflow module are in use) one by one and measuring the resulting turbidity. If an abnormal turbidity value is detected when a particular filter is active but is not detected when that particular filter is inactive, the system 200 may determine that the particular filter is experiencing a filter integrity failure, and may deactivate the particular filter.

[0171] In some embodiments, filters may be tested in groups (e.g., of two filters, three filters, four filters, etc.) in addition to or alternatively to testing filters one by one to detect any group of filters experiencing filter integrity failures. This may be performed, for example, if an abnormal turbidity reading occurs, but no single filter is determined to be the filter causing the abnormal turbidity reading (e.g., no single filter is determined to be experiencing filter integrityfailure) using the processes described herein. In some embodiments, if no single filter is determined to be the filter causing the abnormal turbidity reading, groups of two filters may be tested, and if no group of two filters is determined to be causing the abnormal turbidity reading, groups of three filters may be tested and so on.

[0172] FIG. 2C is a process flow chart depicting a process 300 for detecting filter integrity failures and adjusting the operation of the filtration system according to some embodiments described herein. The process 300 may be performed for any crossflow module or filter array within the manufacturing system.

[0173] As described above, the systems described herein may monitor turbidity of a permeate outflow stream from a crossflow module (e.g., crossflow module 202a, 202b). The turbidity may be monitored by a turbidity sensor (e.g., turbidity sensor 240a, turbidity sensor 240b) positioned along the permeate conduit (e.g., permeate conduit 210a, permeate conduit 210b) receiving permeate from the crossflow module (e.g., crossflow module 202a, crossflow module 202b). In other embodiments, the turbidity may be monitored by a turbidity sensor (e.g., turbidity sensor 240d, turbidity sensor 240e) positioned along the permeate conduit (e.g., permeate conduit 21 la, permeate conduit 21 lb) receiving permeate from a distinct filter array (e.g., filter array 204a, filter array 204b. filter array 204c, filter array 204d) Monitoring of turbidity may be performed throughout the manufacturing processes described herein or may be initiated at the onset of microfiltration and / or diafiltration.

[0174] The process 300 includes a step 302 at which an abnormal turbidity is detected. The abnormal turbidity value may be a value outside of a range of normal operating turbidity values expected to occur during operation of the manufacturing system (e.g., system 200). The abnormal turbidity value may be a turbidity value beyond a threshold value. The abnormal turbidity value may indicate potential filter integrity failure of one of the filters (or in some embodiments, multiple filters). The abnormal turbidity value may be detected by the turbiditysensor (e.g., sensor 240a, sensor 240b) and / or a control system, computer system, or processing circuit in communication with the turbidity sensor.

[0175] After an abnormal turbidity value is detected, a series of steps may be performed to identify the particular filter experiencing a filter integrity failure. At step 304, a "‘next7’ filter of the plurality of filters within a filter array (or within a crossflow module if both filter arrays of the crossflow module are in use) is selected and tested to determine a filter integrity failure. The first time step 304 is performed, the “next” filter is a first filter of a set of currently active filters (e.g., of a filter array or crossflow module associated with the turbidity sensor). If step 304 is performed additional times during the process 300, the “next” filter will be an active filter that has not yet been tested. The order of testing may be predefined or randomized. To test a particular filter, the filter is turned off (e.g., by a control system, computer system, or processing circuit of the system 200) and a defined amount of permeate is allowed to flow through the permeate conduit to ensure that any permeate from the particular filter has passed the turbidity probe. The defined amount of permeate may be based on the distance of the turbidity sensor from the filter array (or crossflow module) and the volume of the permeate conduit.

[0176] In some embodiments, the flow rate through the filter array (or crossflow module) may be reduced prior to turning off a particular filter to prevent an undesired increase in pressure within the other filters of the filter array (or crossflow module) after the particular filter is turned off. The decrease in flow rate may be proportional to the number of filters in-use in the filter array (or the crossflow module if both filter arrays of the crossflow module are in use) prior to turning off the particular filter. For example, if a single filter array has six active filters is in- use within a crossflow module, the flow rate may be decreased by 1 / 6 in advance of turning off a particular filter.

[0177] After the defined amount of permeate has flowed through the permeate conduit, the turbidity7is measured and a determination is made at step 306 if a normal operational turbidity value has been detected.

[0178] If a normal turbidity value is detected at step 306, the particular filter being tested may be identified as the potential filter experiencing filter integrity failure at step 308. If a normal turbidity value is not detected at step 306, the particular filter being tested may be reactivated, and a determination is made if all of the active filters have been tested at step 307. If all of the active filters have been tested, the process may end, without a filter experiencing filter integrity failure being determined and deactivated. In some embodiments, an alert may be provided to a user that an abnormal turbidity value was detected but no filter experiencing filter integrity failure was determined. A user may choose to proceed with a bulk operation or to end the operation. As one example, all of the filters may be tested without achieving a normal turbidityreading at step 306 if multiple filters are experiencing a filter integrity failure at the same time. In some alternative embodiments, sets of multiple filters (e.g., two filters, three filters, four filters, etc.) may be tested in groups using a process that is the same as or generally similar to the process 300 to determine and / or deactivate a group of filters experiencing filter integrity failures. In some embodiments, testing in groups may be performed after testing each active filter individually without achieving a normal turbidity reading at step 306.

[0179] If all the active filters have not yet been tested at step 307, the process may return to step 304, at which a next filter of the filter array (or of the crossflow module if both filter arrays of the crossflow module are in use) is tested. In this way, steps 304, 306, and 307 may be repeated with each active filter of the filter array (or crossflow module) until a particular filter is identified as the potential filter experiencing filter failure or no filter is identified as the filter experiencing filter failure.

[0180] After a particular filter is identified as the potential filter experiencing filter integrity failure at step 306, an additional test may be run to confirm the identified filter is the filter experiencing filter integrity failure at step 310. The test can include reactivating the identified filter and monitoring the turbidity sensor to detect if an abnormal turbidity value is again detected. If an abnormal turbidity value is detected, the identified filter is confirmed as the filter experiencing a filter integrity failure. The identified filter may then be turned off for the remainder of the manufacturing process at step 314. The identified filter and / or its corresponding filter array may be removed and replaced after completion of the manufacturing process. If an abnormal turbidity value is not detected at step 312, the process may move to step 313 where a determination is made if all of the active filters have been tested. If all of the active filters have been tested, the process may end. If all of the active filters have not been tested, the process may return to step 304.

[0181] In certain embodiments, one or more additional turbidity sensor having different wavelengths may be used to determine product concentration. For example, in certain embodiments, a turbidity sensor 240c can be positioned to determine or measure turbidity within the concentration vessel. When a final product target concentration is detected by the sensor 240c, the system may step further concentration of the product.

[0182] In some embodiments, the system comprises at least one inline mesh screen for filtering foreign debris. In some embodiments, an inline steel screen is used to filter foreign debris from MVL solutions or suspensions. In some embodiments, this screening step is performed when transferring the final aqueous suspension to a holding vessel after step (I), when transferring the final aqueous suspension from the holding vessel to an aseptic fill line, or any combination thereof. The mesh screen can be placed inline such that the process fluids flow through it during theprocess, catching foreign debris such as plastic from shedding gaskets from process equipment. Then, the inline mesh screen can be removed between batches or when cleaning to inspect for foreign debris and remove foreign debris enmeshed and / or replaced between batches.

[0183] In any embodiments of the processes described herein, the final aqueous suspension of bupivacaine encapsulated multivesicular liposomes produced by the process described herein has a volume of at least about 150 L. In one embodiment, the final aqueous suspension of bupivacaine encapsulated multivesicular liposomes has a volume of about 200 L to about 300 L, e.g., about 200, 210, 220, 230, 240, 250, 260, 270, 280, 290 or 300 L. In another embodiment, the final aqueous suspension of bupivacaine encapsulated multivesicular liposomes has a volume of about 225 L to about 300 L. In another embodiment, the final aqueous suspension of bupivacaine encapsulated multivesicular liposomes has a volume of about 225 L to about 250 L or 260 L to about 300 L. In further embodiments, when using the process described herein with improved final product volume, the final aqueous suspension of bupivacaine encapsulated multivesicular liposomes has a volume of about 310 L to about 350 L, from about 350 L to about 400 L, from about 400 L to about 450 L, from about 450 L to about 500 L, from about 500 L to about 600 L, from about 600 L to about 700 L, from about 700 L to about 800 L, or from about800 L to about 900 L. In some such embodiments, the target concentration of the bupivacaine in the final aqueous suspension (i.e., bulk product suspension) is from about 12 mg / mL to about 17 mg / mL, or from about 12.3 mg / mL to about 16.6 mg / mL. In further embodiments, the final product target concentration of the bupivacaine in the aqueous suspension is about 13.3 mg / mL. In some embodiments, the percent packed particle volume (% PPV) of the bupivacaine encapsulated MVLs in the composition is about 32% to about 44% (e.g.. about 35%, 36%, 37%, 38%, 39% or 40%). In some embodiments, the final aqueous suspension of bupivacaine MVLs comprises less than 5%, 4%, 3%, 2% or 1% unencapsulated bupivacaine, wherein the amount of unencapsulated bupivacaine is calculated based on the total weight of the bupivacaine in the aqueous suspension. In some embodiments, the volume weighted mean dso of the multivesicular liposomes in the final aqueous suspension is about 24 pm to about 28 pm. In some embodiments, the dso of the multivesicular liposomes in the final aqueous suspension is about 25 pm, about 26 pm or about 27 pm. In some embodiments, the volume weighted mean dio of the multivesicular liposomes in the final aqueous suspension is about 13 pm to about 15 pm, or about 13.5 pm to about 14.5 pm. In some embodiments, the volume weighted mean d9o of the multivesicular liposomes in the final aqueous suspension is about 46 pm to about 57 pm, about 47 pm to about 54 pm, or about 48 pm to about 52 pm.Bupivacaine In Vitro Release Assay (IVRA) Test

[0184] Topologically, multivesicular liposomes are defined as having multiple non- concentric chambers within each particle, resembling a “foam-like’' or “honeycomb-like'’ matrix. The individual chambers are separated by lipid bilayer membranes composed of synthetic and naturally occurring lipids. The presence of internal membranes distributed as a network throughout multivesicular liposomes may serve to confer increased mechanical strength to the vesicle. The multivesicular nature of multivesicular liposomes also indicates that, unlike for unilamellar vesicles, a single breach in the external membrane of multivesicular vesicles will not result in total release of the internal aqueous contents. Exparel® has an extended release profile of bupivacaine up to 72 hours. The Exparel® product specification requires that the average cumulative percentage release of bupivacaine is 10%-35% at 4-hour, 46%-71% at 24-hour, 60%- 85% at 48-hour, and no less than 80% at 168-hour, using a rotator-facilitated test also referred to as in vitro release assay (IVRA) test.

[0185] The IVRA test is based on mechanical disruption of MVL particles via physical impact of mixing in the presence of an air bubble of a specific size. An aliquot of a batch of bupivacaine MVLs prepared by the process described herein is diluted 17-fold in a media containing 0.5% bovine serum albumin (BSA) / 50 mM pH 7 phosphate buffered saline (PBS) and 0.05% sodium azide. Then, 1.8 mL of the diluted bupivacaine MVLs composition is transferred to a 2 mL Simport polypropylene microcentrifuge tube, or 1.94 mL of the diluted bupivacaine MVLs composition is transferred to a 2 mL VWR crew-cap polypropylene microcentrifuge tube. For each aliquot, a set of five microcentrifuge tubes are used for measurement at the five time points: 0 hour, 4-hour, 24-hour, 48-hour, and 168-hour. For each lot. six aliquots of bupivacaine MVLs are used to calculate the cumulative percentage release of bupivacaine at each time points (i.e., an average of six aliquots). These tubes are rotated at 37°C at a speed of 12 rpm. The tubes are rotated for 168 hours and sampled at the 4-hour, 24-hour, 48-hour, and 168-hour time points. At each time point, six sample tubes are removed and tested for bupivacaine content in the supernatant; the sample tubes are centrifuged at 14.000 g for 10 minutes. Without disturbing the MVL pellet, 350 pL of the supernatant is pipetted into a 1.5 mL tube, combined with 700 pL acetonitrile and vortexed at high speed for 10 seconds, then the 1.5 mL tube is incubated at room temperature for 30 minutes to precipitate BS A / lipids. Then about 700 pL of supernatant from each 1.5 mL tube is transferred into a HPLC vial for analysis. The bupivacaine in the supernatant (released from the MVL particles) is determined by isocratic reversed-phase HPLC (column: Cl 8, 5 pm, 3.0 mm x 150 mm, Zorbax Extend) with UV detection at 263 nm, using bupivacaine HC1 as reference standard (about 0.1 mg / mL in 40% IP A). The flow rate is 0.7 mL / min, and theinjection volume is 10 pL. The mobile phase is composed of 65% Acetonitrile: 35% Phosphate Buffer (pH 6.8). The pH of the mobile phase is 7.7 ± 0.2.

[0186] Percent release is determined from the bupivacaine concentration in the supernatant and the labeled concentration of bupivacaine in the product (which is 13.3mg / mL). The data is presented as a cumulative percentage release of bupivacaine against time. All of the six individual replicate bupivacaine percentage released results for each sample must be not more than 10% outside the specification window for t = 4-hour, 24-hour and 48-hour time points (e.g., the individual % released results should be from 36% to 81% at the 24-hour time point from 50% to 95% at the 48-hour time point). The six individual replicate % released results must be not more than 10% below the specification limit for t = 168-hour (i.e. the individual % released results must be no less than 70%.).Bupivacaine Multivesicular Liposomes

[0187] Some embodiments of the present disclosure relate to a batch comprising a composition of bupivacaine encapsulated multivesicular liposomes (MVLs), the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise 1, 2-dierucoylphosphatidylcholine (DEPC), 1, 2-dipalmitoyl-sn-glycero-3-phospho-rac-(l -glycerol) (DPPG) or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL; wherein the batch has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein the batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from two or more aliquots of the batch using a rotator-facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date; and wherein the rate of change in the cumulative percentage release of bupivacaine at the 24- hour time point is at least 0.05% / month after storage of the aliquots at 2°C to 8°C for about 12 months.

[0188] In some embodiments of the batch described herein, the batch has a volume of at least 200 liters (e.g., 225 liters, 250 liters, 275 liters or 300 liters). In some embodiments, the cumulative percentage release of bupivacaine at a 24-hour time point is measured from two, three,four, five or six aliquots of the batch. In some further embodiments, the rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0. 1% / month. In some further embodiments, the rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is, or is at least 0.06% / month, 0.07% / month, 0.08% / month, 0.09% / month, 0.10% / month. 0.11% / month, 0.12% / month, 0.13% / month, 0.14% / month, 0. 15% / month, 0.16% / month, 0. 17% / month, 0. 18% / month, 0.19% / month, or 0.20% / month after storage of the aliquots of the batch at 2°C to 8°C for about 12 months. In some embodiments, the rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is 0. 1% / month to 0.5% / month, for example, 0. 15% / month to 0.45% / month, 0.20% / month to 0.40% / month, or 0.25% / month to 0.35% / month. In some further embodiments, the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than - 0.3% / month after storage of the aliquot of each batch at 2°C to 8°C for about 12 months. In some further embodiments, the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.2% / month, for example, from -0. 18% / month to 0.33% / month, -0.15% / month to 0.30% / month, -0.12% / month to 0.28% / month, -0.10% / month to 0.25% / month, -0.08% / month to 0.22% / month, -0.05% / month to 0.20% / month, or 0% / month to 0.15% / month.

[0189] Some additional embodiments of the present disclosure relate to a batch comprising a composition of bupivacaine encapsulated multivesicular liposomes (MVLs), the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise 1, 2-dierucoylphosphatidylcholine (DEPC), 1, 2-dipalmitoyl-sn-glycero-3-phospho-rac-(l -glycerol) (DPPG) or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; and the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL; wherein the batch has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein the batch has a cumulative percentage release of bupivacaine from 60% to 85% at the 48-hour time point, measured from two or more aliquots of the batch using a rotator- facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date; andwherein the rate of change in the cumulative percentage release of bupivacaine at the 48- hour time point is no less than -0.3% / month after storage of the aliquot of each batch at 2°C to 8°C for about 12 months.

[0190] In some embodiments of the batch described herein, the batch has a volume of at least 200 liters (e.g.. about 220 liters, 225 liters. 240 liters, 250 liters. 260 liters, 275 liters. 280 liters or 300 liters). In some embodiments, the cumulative percentage release of bupivacaine at a 48-hour time point is measured from two, three, four, five or six aliquots of the batch. In some further embodiments, the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.2% / month. In some further embodiments, the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is, is no less than, or is at least -0.25% / month, -0.20% / month, -0. 18% / month, -0. 15% / month, -0.12% / month, -0.10% / month, -0.08% / month, -0.05% / month. no change (0% / month), 0.02% / month, 0.05% / month, 0.08% / month. 0.10% / month, 0.12% / month, 0. 15% / month, 0.18% / month, 0.20% / month, 0.22% / month, or 0.25% / month, or a range defined by any two of the preceding values,, after storage of the aliquots of the batch at 2°C to 8°C for about 12 months. In some further embodiments, the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -0.12% / month to 0.33% / month, for example, -0.12% / month to 0.30% / month, -0.12% / month to 0.28% / month. -0.10% / month to 0.25% / month. -0.08% / month to 0.22% / month, -0.05% / month to 0.20% / month, or 0% / month to 0. 15% / month.

[0191] Some embodiments of the present disclosure relate to batches comprising compositions of bupivacaine encapsulated multivesicular liposomes (MVLs), the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise DEPC, DPPG or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; and the total bupivacaine concentration in the composition is from 12 mg / rnL to 17 mg / mL; wherein the batches are manufactured within a period of six months, and the batches each has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from two or more aliquots of each batch using a rotator- facilitated in vitro release assay, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date; andwherein an average rate of change in the cumulative percentage release of bupivacaine of the batches at the 24-hour time point is at least 0.05% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is, or is at least 0.06% / month, 0.07% / month. 0.08% / month, 0.09% / month, 0.10% / month, 0. 11% / month,0.12% / month, 0.13% / month, 0.14% / month, 0.15% / month, 0.16% / month, 0.17% / month,0.18% / month, 0.19% / month, or 0.20% / month, or a range defined by any two of the preceding values, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.08% / month. In some embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is 0. 1% / month to 0.5% / month, for example, 0.15% / month to 0.45% / month, 0.20% / month to 0.40% / month, or 0.25% / month to 0.35% / month. In some further embodiments, the IVRA test is performed for at least 48 hours, and each batch has a cumulative percentage release of bupivacaine from 60% to 85% at the 48-hour time point, and the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.3% / month after storage of the aliquot of each batch at 2°C to 8°C for about 12 months. For example, the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.2% / month, for example, from -0.18% / month to 0.33% / month, 0.15% / month to 0.30% / month, -0.12% / month to 0.28% / month, -0.10% / month to 0.25% / month, -0.08% / month to 0.22% / month, -0.05% / month to 0.20% / month, or 0% / month to 0.15% / month.

[0192] Some embodiments of the present disclosure relate to batches comprising compositions of bupivacaine encapsulated multivesicular liposomes (MVLs), the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise DEPC, DPPG or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; and the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL; wherein the batches are manufactured within a period of six months, and the batches each has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein each batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from two or more aliquots of each batch using a rotator-facilitated in vitro release assay, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date; and wherein an average rate of change in the cumulative percentage release of bupivacaine of the batches at the 48-hour time point is no less than -0.3% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is, is no less than, or is at least -0.25% / month, -0.20% / month, -0. 18% / month, -0. 15% / month, -0.12% / month, -0.10% / month, -0.08% / month. -0.05% / month, no change (0% / month), 0.02% / month, 0.05% / month, 0.08% / month. 0.10% / month, 0.12% / month, 0. 15% / month, 0.18% / month, 0.20% / month, 0.22% / month, or 0.25% / month, or a range defined by any two of the preceding values, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.2% / month. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -0.18% / month to 0.33% / month, for example, -0. 15% / month to 0.30% / month, -0.12% / month to 0.28% / month, -0.10% / month to 0.25% / month, -0.08% / month to 0.22% / month, -0.05% / month to 0.20% / month, or 0% / month to 0.15% / month.

[0193] In some embodiments of the batches described herein, the average rate of change in the cumulative percentage release of bupivacaine is based on three batches, and one batch is manufactured at least 7 days apart (e.g., 7, 8, 9, or 10 or more days apart) from at least one other batch. In some other embodiments, the average rate of change in the cumulative percentage release of bupivacaine is based on two batches, and one batch is manufactured at least 7 days apart (e.g., 7, 8, 9, or 10 or more days apart) from the other batch. In some embodiments, the cumulative percentage release of bupivacaine of each batch is measured as the average of two aliquots, three aliquots, four aliquots, five aliquots, or six aliquots from each batch. In further embodiments, the cumulative percentage release of bupivacaine of each batch is measured as the average of six aliquots from each batch.

[0194] Some embodiments the present disclosure relate to batches comprising compositions of bupivacaine encapsulated MVLs, the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise DEPC. DPPG or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; and the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL;wherein the batches are manufactured within a period of six months, and the batches each has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from two or more aliquots of each batch using a rotator- facilitated in vitro release assay, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date; and wherein an average change in the cumulative percentage release of bupivacaine at the 24- hour time point is at least 0.5% after storage of the aliquots of each batch at 2°C to 8°C for about 12 months. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 24-hour time point is, or is at least 0.6%, 0.7%, 0.8%, 0.9%, 1.0%, 1.1%, 1.2%, 1.3%, 1.4%, 1.5%, 1.6%, 1.7%, 1.8%, 1.9% or 2.0%, or a range defined by any two of the preceding values, after storage of the aliquots of each batch at 2°C to about 8°C for 12 months. In some embodiments, the average change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 1%. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 24-hour time point is 1% to 5%, for example, 1.5% to 4.5%, 2.0% to 4.0%, or 2.5% to 3.5%. In some further embodiments, the IVRA test is performed for at least 48 hours, and each batch has a cumulative percentage release of bupivacaine from 60% to 85% at the 48-hour time point, and an average change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -5% after storage of the aliquots of each batch at 2°C to 8°C for about 12 months. In some embodiments, the average change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -4%. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -4% to 6%, for example, -3.5% to 5.5%, -3.0% to 5.0%, -2.5% to 4.5%, -2.0% to 4.0%, -1.5% to 3.5%, or -1.0% to 3.0%.

[0195] Some embodiments the present disclosure relate to batches comprising compositions of bupivacaine encapsulated MVLs. the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise DEPC, DPPG or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; and the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL;wherein the batches are manufactured within a period of six months, and the batches each has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein each batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from two or more aliquots of each batch using a rotator- facilitated in vitro release assay, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date; and wherein an average change in the cumulative percentage release of bupivacaine at the 48- hour time point is no less than -5% after storage of the aliquots of each batch at 2°C to 8°C for about 12 months. In some embodiments. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 48-hour time point is, or is no less than -4.5%, -4.0%, -3.5%, -3.0%, -2.5%, -2.0%, -1.5%, -1.0%, -0.5%, no change (0%), 0.5%, 1.0%, 1.5%, 2.0% or 2.5% after storage of the aliquots of each batch at 2°C to about 8°C for 12 months. In some embodiments, the average change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -4%. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -4% to 6%, for example, -3.5% to 5.5%, -3.0% to 5.0%, -2.5% to 4.5%, -2.0% to 4.0%, -1.5% to 3.5%, or -1.0% to 3.0%.

[0196] In some embodiments of the batches described herein, the average change in the cumulative percentage release of bupivacaine is based on three batches, and one batch is manufactured at least 7 days apart (e.g., 7, 8, 9, or 10 or more days apart) from at least one other batch. In some other embodiments, the average change in the cumulative percentage release of bupivacaine is based on two batches, and one batch is manufactured at least 7 days apart (e.g., 7, 8, 9, or 10 or more days apart) from the other batch. In some embodiments, the cumulative percentage release of bupivacaine of each batch is measured as the average of two aliquots, three aliquots, four aliquots, five aliquots, or six aliquots from each batch. In some further embodiments, the cumulative percentage release of bupivacaine of each batch is measured as the average of six aliquots from each batch.

[0197] In some embodiments of batches described herein, the batches each has a volume of at least 100 liters, 110 liters, 120 liters, 125 liters, 150 liters, 175 liters, 200 liters. 225 liters, 250 liters, 275 liters or 300 liters, or a range defined by any two of the preceding values. In some further embodiments, the batches are manufactured within a period of 3 months. In some other embodiments, the batches are manufactured within a period of 2 months. In some embodiments, the batches are manufactured within a period of 30 days. In some embodiments, the batches are manufactured within a period of 3 months, each having a volume of at least 200liters, for example about 220 liters, 240 liters, 260 liters, 280 liters or 300 liters. In some embodiments, the batches are manufactured within a period of 2 months, each having a volume of at least 200 liters, for example about 220 liters, 240 liters, 260 liters, 280 liters or 300 liters. In some embodiments, the batches are manufactured within a period of 30 days, each having a volume of at least 200 liters, for example about 220 liters, 240 liters. 260 liters, 280 liters or 300 liters.

[0198] Some further embodiments of the present disclosure relate to batches comprising compositions of bupivacaine encapsulated MVLs, the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise DEPC, DPPG or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; and the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL; wherein the batches are manufactured within a period of three months, and the batches each has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from six aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date; wherein the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.05% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months, and wherein the average rate of change in the cumulative percentage release of bupivacaine is based on two to five batches, and at least one batch is manufactured 10 or more days apart from at least one other batch. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is, or is at least 0.06% / month, 0.07% / month, 0.08% / month, 0.09% / month, 0.10% / month, 0.11% / month, 0.12% / month,0.13% / month, 0.14% / month. 0.15% / month, 0.16% / month, 0.17% / month, 0.18% / month,0. 19% / month, or 0.20% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months. In some embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least 0.1% / month. In some further embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is 0.15% / month to 0.5% / month, for example, 0.15% / month to 0.45% / month. 0.20% / monthto 0.40% / month, or 0.25% / month to 0.35% / month. In some embodiments, the average rate of change in the cumulative percentage release of bupivacaine is based on three batches, and one batch is manufactured 10 or more days (e.g., 10, 15, 20, 25 or 30 days) apart from at least one other batch. In some other embodiments, the average rate of change in the cumulative percentage release of bupivacaine is based on two batches, and one batch is manufactured 10 or more days (e.g., 10, 15, 20, 25 or 30 days) apart from the other batch. In some further embodiments, the batches are manufactured within 30 days.

[0199] Some further embodiments of the present disclosure relate to batches comprising compositions of bupivacaine encapsulated MVLs, the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise DEPC, DPPG or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; and the total bupivacaine concentration in the composition is from 12 mg / rnL to 17 mg / mL; wherein the batches are manufactured within a period of three months, and the batches each has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein each batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from six aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date; wherein the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.3% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months, and wherein the average rate of change in the cumulative percentage release of bupivacaine is based on two to five batches, and at least one batch is manufactured 10 or more days apart from at least one other batch. In some embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is, is no less than, or is at least-0.25% / month, -0.20% / month, -0. 18% / month, -0.15% / month, -0.12% / month, -0.10% / month,-0.08% / month. -0.05% / month, no change (0% / month), 0.02% / month, 0.05% / month, 0.08% / month, 0.10% / month, 0.12% / month, 0. 15% / month, 0. 18% / month, 0.20% / month,0.22% / month, or 0.25% / month, or a range defined by any two of the preceding values. In some embodiments, the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.2% / month. In some further embodiments, the averagerate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -0. 18% / month to 0.33% / month, for example, -0. 15% / month to 0.30% / month, -0. 12% / month to 0.28% / month, -0. 10% / month to 0.25% / month, -0.08% / month to 0.22% / month, -0.05% / month to 0.20% / month, or 0% / month to 0. 15% / month. In some embodiments, the average rate of change in the cumulative percentage release of bupivacaine is based on three batches, and one batch is manufactured 10 or more days (e.g., 10, 15, 20, 25 or 30 days) apart from at least one other batch. In some other embodiments, the average rate of change in the cumulative percentage release of bupivacaine is based on two batches, and one batch is manufactured 10 or more days (e g., 10, 15, 20, 25 or 30 days) apart from the other batch. In some further embodiments, the batches are manufactured within 30 days.

[0200] Additional embodiments of the present disclosure relate to batches comprising compositions of bupivacaine encapsulated MVLs, the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise DEPC, DPPG or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; and the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL; w herein the batches are manufactured within a period of three months, and the batches each has a volume of at least 100, 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from six aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date; wherein an average change in the cumulative percentage release of bupivacaine at the 24- hour time point is at least 0.5% after storage of the aliquots of each batch at 2°C to 8°C for about 12 months; and wherein the average rate of change in the cumulative percentage release of bupivacaine is based on two to five batches, and at least one batch is manufactured 10 or more days apart from at least one other batch. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 24-hour time point is, or is at least 0.6%, 0.7%, 0.8%, 0.9%, 1.0%, 1.1%, 1.2%, 1.3%, 1.4%, 1.5%, 1.6%, 1.7%, 1.8%, 1.9% or 2.0% after storage of the aliquots of each batch at 2°C to about 8°C for 12 months. In some embodiments, the average change in the cumulative percentage release of bupivacaine at the 24-hour time point is at least1%. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 24-hour time point is 1% to 5%, for example, 1.5% to 4.5%, 2.0% to 4.0%, or 2.5% to 3.5%. In some embodiments, the average change in the cumulative percentage release of bupivacaine is based on three batches, and one batch is manufactured 10 or more days (e.g., 10, 15. 20, 25 or 30 days) apart from at least one other batch. In some other embodiments, the average change in the cumulative percentage release of bupivacaine is based on two batches, and one batch is manufactured 10 or more days (e.g., 10, 15, 20, 25 or 30 days) apart from the other batch. In some further embodiments, the batches are manufactured within 30 days.

[0201] Additional embodiments of the present disclosure relate to batches comprising compositions of bupivacaine encapsulated MVLs, the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise DEPC, DPPG or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; and the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL; wherein the batches are manufactured within a period of three months, and the batches each has a volume of at least 100. 110 or 120 liters (for example, about 120 to 300 L, about 150 to about 280 L or about 200 to about 260 L); wherein each batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from six aliquots of each batch using a rotator-facilitated in vitro release assay for at least about 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date; wherein an average change in the cumulative percentage release of bupivacaine at the 48- hour time point is no less than -5% after storage of the aliquots of each batch at 2°C to 8°C for about 12 months; and wherein the average change in the cumulative percentage release of bupivacaine is based on two to five batches, and at least one batch is manufactured 10 or more days apart from at least one other batch. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 48-hour time point is, or is no less than -4.5%. -4.0%, -3.5%, -3.0%, -2.5%, -2.0%, -1.5%, -1.0%, -0.5%, no change (0%), 0.5%, 1.0%. 1.5%, 2.0% or 2.5% after storage of the aliquots of each batch at 2°C to about 8°C for 12 months. In some embodiments, the average change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -4%. In some further embodiments, the average change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -4% to 6%, for example,-3.5% to 5.5%, -3.0% to 5.0%, -2.5% to 4.5%, -2.0% to 4.0%, -1.5% to 3.5%, or -1.0% to 3.0%. In some embodiments, the average change in the cumulative percentage release of bupivacaine is based on three batches, and one batch is manufactured 10 or more days (e.g., 10, 15, 20, 25 or 30 days) apart from at least one other batch. In some other embodiments, the average change in the cumulative percentage release of bupivacaine is based on two batches, and one batch is manufactured 10 or more days (e.g., 10, 15, 20, 25 or 30 days) apart from the other batch. In some further embodiments, the batches are manufactured within 30 days.

[0202] In some embodiments of batches described herein, the batches each has a volume of at least 100 liters. 110 liters, 120 liters. 125 liters, 150 liters. 175 liters, 200 liters. 220 liters, 225 liters, 240 liters, 250 liters, 260 liters, 275 liters, 280 liters or 300 liters. In some embodiments, the batches are manufactured within a period of 2 months. In some embodiments, the batches are manufactured within a period of 30 days. In some embodiments, the batches are manufactured within a period of 2 months, each having a volume of at least 200 liters, for example about 220 liters, 240 liters, 260 liters, 280 liters or 300 liters. In some embodiments, the batches are manufactured within a period of 1.5 months, each having a volume of at least 200 liters. In some embodiments, the batches are manufactured within a period of 30 days, each having a volume of at least 200 liters, for example about 220 liters, 240 liters, 260 liters, 280 liters or 300 liters.

[0203] In any embodiments of the batch or batches described herein, the cumulative percentage release of bupivacaine is measured using the rotator-facilitated in vitro release assay for up to 168 hours. In some embodiments, the in vitro release assay is run for about 48 hours. In some other embodiments, the in vitro release assay is run for about 168 hours. In some embodiments, each aliquot has a cumulative percentage release of bupivacaine from 36% to 81% at the 24-hour time point. In some embodiments, each aliquot has a cumulative percentage release of bupivacaine from 50% to 95% at the 48-hour time point. In some embodiments, the cumulative percentage release of bupivacaine is measured after storage of the aliquots of each batch at about 5°C for about 365 days from batch manufacture date.

[0204] In any embodiments of the batch or batches described herein, the total bupivacaine concentration in the composition is 12.0 to 14.6 mg / mL, or about 13.3 mg / mL. In some further embodiments, the % PPV of the bupivacaine encapsulated MVLs in the composition is about 32% to about 44%. In some embodiments, the shelf-life of the bupivacaine MVL product is at least 24 months (e.g., 24, 25, 26, 27, 28, 29 or 30 months). In some further embodiments, the aliquot of each batch(es) is in a Type I clear glass vial with ETFE-faced gray butyl stopper and aluminum flip-off cap and polypropylene (PP) flip disc, or gray plug stopper and white aluminum flip tear up seal.

[0205] As described herein with respect to any of the time points (e.g., 24-hour, 48- hour or 168-hour) in which cumulative percentage release of bupivacaine is tested, each time point is within ±15 minutes of the scheduled time points.

[0206] As described herein with respect to the rate of change in the cumulative percentage release of bupivacaine, each aliquot is measured at the following five time points: a first time point is within 30 days from batch manufacture date, a second time point is about 3 months from the batch manufacture date, a third time point which is about 6 months from the batch manufacture date, a fourth time point which is about 9 months from the batch manufacture date, and a fifth time point which is about 12 months from the batch manufacture date. Each time point of actual measurement is within ± 30 days of the scheduled time point.

[0207] As described herein with respect to the change in the cumulative percentage release of bupivacaine after storage of the aliquots of each batch at 2°C to 8°C for about 12 months, the change is calculated as: % release of bupivacaine at about 12 months - % release of bupivacaine shortly after manufacturing (e.g., within 30 days from batch manufacture date when the batch product is filled into individual vials). Batch product is usually filled into individual vials within 7 days from manufacture date.

[0208] Some further embodiments relate to a composition of bupivacaine encapsulated multivesicular liposomes prepared by the process utilizing the crossflow filtration system described herein. In some embodiments, the bupivacaine concentration in the composition is about 12.0 mg / mL to about 14.6 mg / mL. In one embodiment, the bupivacaine concentration in the composition is about 13.3 mg / mL. In some embodiments, the percent packed particle volume (% PPV) of the composition of bupivacaine encapsulated MVLs is about 32%, 33%, 34%, 35%, 36%, 37%, 38%, 39%, 40%, 41%, 42%, 43% or 44%. In further embodiments, the % PPV of the bupivacaine MVLs is about 36% to about 38%. %PPV is calculated as 100% - (supernatant volume of the composition / total volume of the composition). In further embodiments, the composition comprises less than 5%, 4%, 3%, 2% or 1% unencapsulated bupivacaine, wherein the amount of unencapsulated bupivacaine is calculated based on the total weight of the bupivacaine in the composition. In some further embodiments, the bupivacaine encapsulated MVLs have an average / mean dgo volume-weighted particle diameter less than about 54 pm, 53 pm or 52 pm when measured shortly after manufacture (e.g., after storage of the composition at 2 to 8 °C for less than 1 week, 2 weeks. 3 weeks or 1 month). In further embodiments, the bupivacaine encapsulated MVLs have an average / mean volume-weighted particle diameter span (d9o - dio) of less than about 38, 37, 36, 35, or 34 pm when measured shortly after manufacture (e.g., after storage of the composition at 2 to 8 °C for less than 1 week, 2 weeks, 3 weeks or 1 month).

[0209] In some further embodiments, the composition of bupivacaine encapsulated MVLs may have a volume of 1 mL, 4 mL, 5 rnL, 10 mL or 20 mL for a single dose administration. In any embodiments of the bupivacaine encapsulated MVLs described herein, the bupivacaine may be present in the salt form as bupivacaine phosphate.Methodology

[0210] To determine total bupivacaine concentration, a sample of bupivacaine MVLs composition is dissolved / diluted 25-fold in 100% methanol, then analyzed by isocratic reversed- phase HPLC with UV detection at 263 nm. Bupivacaine concentration is determined on the basis of peak area, using an external bupivacaine hydrochloride standard.

[0211] To determine free bupivacaine (i.e., unencapsulated bupivacaine), a sample of freshly suspended bupivacaine MVLs composition is transferred to a microfuge tube which is centrifuged at 13,000 rpm in the Eppendorf microfuge model # 5415) for 10 minutes at room temperature, then an aliquot of the supernatant diluted 5-fold in 100% methanol and the bupivacaine concentration assayed by HPLC. The volume fraction of external (i.e., extraliposomal) phase is assessed by placing a sample of bupivacaine MVLs composition in a capillary tube and centrifuging. The volume fraction of external phase is determined from the relative height of the supernatant compared to that of the total sample. Free bupivacaine (as a % of the total bupivacaine in the sample) is determined from the bupivacaine concentration in the supernatant and the volume fraction of external phase. The identity of bupivacaine is determined by comparing retention time of the bupivacaine peak in the sample with the bupivacaine hydrochloride reference standard peak.

[0212] To determine the particle size distribution of bupivacaine MVLs, a sample of bupivacaine MVLs suspension is diluted in 0.9% Sodium chloride (pH adjusted normal saline) and the particle size distribution is measured by laser light scattering (by HORIBA Laser Scattering Particle Size Distribution Analyzer LA-950 and LA-960 (or equivalent)), using Mie scattering theory. Three measurements are conducted for each sample.Methods of Administration

[0213] Some embodiments of the present application are related to methods for treating, ameliorating pain comprising administering a pharmaceutical composition comprising bupivacaine MVLs as described herein, to a subject in need thereof. In some further embodiments, the pain is post-surgical pain.

[0214] In some embodiments of the methods described herein, the administration is parenteral. In some further embodiments, the parenteral administration may be selected from thegroup consisting of subcutaneous injection, tissue injection, intramuscular injection, intraarticular, spinal injection, intraocular injection, epidural injection, intrathecal injection, intraotic injection, perineural injection, and combinations thereof. In particular embodiments, the parenteral administration is subcutaneous injection or tissue injection. In some further embodiments, the instant pharmaceutical compositions can be administered by bolus injection, e.g.. subcutaneous bolus injection, intramuscular bolus injection, intradermal bolus injection and the like. In one embodiment, the administration is via local infiltration to a surgical site to provide local analgesia. In another embodiment, the administration is via interscalene brachial plexus nerve block or femoral nerve block to provide regional analgesia. In another embodiment, the administration is via an adductor canal block to provide regional analgesia. In yet another embodiment, the administration is via a sciatic nerve block in the popliteal fossa to provide regional analgesia. For pediatric subjects between the age of 6 and 17 years old, the administration of bupivacaine MVL composition described herein may be weight based, at about 4 mg / kg and up to 233 mg of bupivacaine. In some embodiments, the bupivacaine MVL composition has a volume of 1 mL, 2 rnL, 4 mL, 5mL, 10 mL or 20 mL for a single-dose administration.

[0215] Administration of the instant bupivacaine MVL composition may be accomplished using standard methods and devices, e.g., pens, injector systems, needle and syringe, a subcutaneous injection port delivery system, catheters, and the like. The administration of the bupivacaine MVLs composition may be used in conjunction with Pacira’s handheld cryoan algesia device.EXAMPLES

[0216] The following examples, including experiments and results achieved, are provided for illustrative purposes only and are not to be construed as limiting the present application.Example 1: Sample comparison - average rate of change in cumulative percentage release of bupivacaine

[0217] In this example, five batches (Batch Nos. 1-5) of Exparel® (bupivacaine MVLs) produced by the new process according to certain embodiment of the present disclosure were stored at 5 °C for about 12 months after batch manufacture date. An IVRA test was performed at 0 month, about 3 months, about 6 months, about 9 months and about 12 months. The average rate of change in cumulative percentage release of bupivacaine at 24-hour and 48-hour were compared to that of 134 batches of Exparel® produced by the 45 L process described herein, and 9 batches Exparel® produced by the UK 200 L process described herein. The results are summarized in Table 1.Table 1. Average rate of change in % bupivacaine release comparison* Only batches with complete IVRA data at all five time points (0 month, about 3 months, about 6 months, about 9 months and about 12 months) during the 12 months storage at 5°C were included in the calculation.**Only 126 batches produced by the 45 L process had 48-hour IVRA data at all five time points during the 12 months storage at 5°C.

[0218] FIG. 3A is a line chart illustrating the average rate of change in cumulative percentage release of bupivacaine at 24-hour time point as a function of time over 12 months, comparing 5 batch samples produced by the present process with 134 batch samples manufactured by the 45 L process and 9 batch samples produced by the UK 200 L process. FIG. 3B is a line chart illustrating the average rate of change in cumulative percentage release of bupivacaine at 48-hour time point as a function of time over 12 months, comparing 5 batch samples produced by the present process with 126 batch samples manufactured by the 45 L process and 9 batch samples produced by the UK 200 L process. Error bars in FIGs. 3A and 3B represent a 95% confidence interval (CI), with values generated using the 95% CI and the standard error of the mean (SEM). The average cumulative percentage release of bupivacaine used to generate FIGs. 3A-3B are illustrated in Tables 2A, 2B and 2C, using the data presented in FIGs. 5A-5F, 6 and 7.

[0219] It was observed that the slope lines for the batches generated by the current process are either flat (48-hour) or trending slightly upw ard (24 hour). In contrast, the slope lines for the batches generated by both the 45 L process and the UK 200 L process are trending downward at both 24-hour and 48-hour. These figures suggest that the batches generated by the current process have improved IVRA stability profiles as compared to those produced by the 45 L and UK 200 L processes. In prior stability' studies, it has been observed that the average % release of bupivacaine at 24-hour usually has a more pronounced decrease in the first 12-month, in particularly the first 6 months. Then the % release of bupivacaine continues to decrease during the second 12-month but the rate of decrease slows down. Because the IVRA test results need to remain within the product specification during the entire shelf life of the product, the flatter the trend line illustrating the rate of change in the cumulative percentage release of bupivacaine in the first 12 months, the more likely that the product will meet the IVRA specification during the entire 24 months. Furthermore, a slope line that trends upwards in the first 12-month can also compensate for or counteract the expected decrease in the % release in the second 12-month.Table 2A. Batch % release of bupivacaine produced by the current processTable 2B. Batch % release of bupivacaine produced by the 45 L processTable 2C. Batch % release of bupivacaine produced by the UK 200 L processExample 2: Sample comparison - average change in cumulative percentage release of bupivacaine

[0220] In this example, 8 batches (Batch Nos. 1-8) of Exparel® (bupivacaine MVLs) produced by the new process according to certain embodiment of the present disclosure were stored at 5 °C for about 12 months after batch manufacture date. An IVRA test was performed at 0 month and about 12 months. The average change in cumulative percentage release of bupivacaine at 24-hour and 48-hour were compared to that of 140 batches of Exparel® produced by the 45 L process described herein, and 9 batches Exparel® produced by the UK 200 L process described herein. The results are summarized in Table 3.Table 3. Average change in % bupivacaine release comparison* Only 132 batches produced by the 45 L process had 48-hour IVRA data at both 0 and 12 months during the 12 months storage at 5°C.

[0221] FIG. 4A is a line chart illustrating the average cumulative percentage release of bupivacaine at 24-hour time point at 0 and 12 months, comparing 8 batch samples produced by the present process with 140 batch samples manufactured by the 45 L process and 9 batch samples produced by the UK 200 L process. FIG. 4B is a line chart illustrating the average cumulative percentage release of bupivacaine at 48-hour time point at 0 and 12 months, comparing 8 batch samples produced by the present process with 132 batch samples manufactured by the 45 L process and 9 batch samples produced by the UK 200 L process. Error bars in FIGs. 4A and 4B represent a 95% confidence interval (CI), with values generated using the 95% CI and the standard error of the mean (SEM). The average cumulative percentage release of bupivacaine used to generate FIGs. 4A-4B are illustrated in Tables 4A, 4B and 4C, using the data presented in FIGs. 5A-5F, 6 and 7. Consistent with the observation in the average rate of change in % bupivacaine release, the figures suggest that the batches generated by the current process have an improved IVRA profile as compared to those produced by the 45 L and UK 200 L processes.Table 4A. Batch % release of bupivacaine produced by the current processTable 4B. Batch % release of bupivacaine produced by the 45 L processTable 4C. Batch % release of bupivacaine produced by the UK 200 L process

[0222] FIGs. 5A-5F is a table illustrating the cumulative percentage release of bupivacaine at 24-hour and 48-hour after storage of the bupivacaine MVLs samples produced by the 45 L process at about 5 °C for about 0 months, 3 months. 6 months, 9 months and 12 months from manufacture date. FIG. 6 is a table illustrating the cumulative percentage release of bupivacaine at 24-hour and 48-hour after storage of the MVLs samples produced by the UK 200 L process at about 5 °C for about 0 months, 3 months, 6 months, 9 months and 12 months from manufacture date. FIG. 7 is a table illustrating the cumulative percentage release of bupivacaine at 24-hour and 48-hour after storage of the MVLs samples produced by process described hereinat about 5 °C for about 0 months, 3 months, 6 months, 9 months and 12 months from manufacture date.

[0223] While the present application has been described with reference to the specific embodiments thereof, it should be understood by those skilled in the art that various changes may be made and equivalents may be substituted without departing from the true spirit and scope of the invention. In addition, many modifications may be made to adapt a particular situation, material, composition of matter, process, process step or steps, to the objective, spirit and scope of the present invention. All such modifications are intended to be within the scope of the claims appended hereto.

Claims

WHAT IS CLAIMED IS:

1. A batch comprising a composition of bupivacaine encapsulated multivesicular liposomes (MVLs), the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise I, 2- dierucoylphosphatidylcholine (DEPC), 1, 2-dipalmitoyl-sn-glycero-3-phospho-rac-(l- glycerol) (DPPG) or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL; wherein the batch has a volume of at least 100 liters; wherein the batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from two or more aliquots of the batch using a rotator-facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date; and wherein the rate of change in the cumulative percentage release of bupivacaine of the batch at the 24-hour time point is at least 0.05% / month after storage of the aliquots at 2°C to 8°C for about 12 months.

2. The batch of claim 1, the rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is from 0.05% / month to 0.5% / month or from 0.08% / month to 0.5% / month.

3. The batch of claim 1 or 2, wherein the rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is from 0.1% / month to 0.5% / month, or from 0. 1% / month to 0.4% / month.

4. The batch of any one of claims 1 to 3, wherein the batch has a cumulative percentage release of bupivacaine from 60% to 85% at the 48-hour time point, and the rate of change in the cumulative percentage release of bupivacaine of the batch at the 48-hour time point is no less than -0.3% / month after storage of the aliquots at 2°C to 8°C for about 12 months.

5. The batch of claim 4, wherein the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -0.3% / month to 0.33% / month or from -0.2% / month to 0.30% / month.

6. The batch of claim 4 or 5, wherein the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -0.18% / month to 0.33% / month or from -0.12% / month to 0.28% / month.

7. A batch comprising a composition of bupivacaine encapsulated multivesicular liposomes (MVLs), the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise 1, 2- dierucoylphosphatidylcholine (DEPC). 1, 2-dipalmitoyl-sn-glycero-3-phospho-rac-(l- glycerol) (DPPG) or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL; wherein the batch has a volume of at least 100 liters; wherein the batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from two or more aliquots of the batch using a rotator-facilitated in vitro release assay for at least 48 hours, after storage of the aliquots at 2°C to 8°C for about 12 months from batch manufacture date; and wherein the rate of change in the cumulative percentage release of bupivacaine of the batch at the 48-hour time point is no less than -0.3% / month after storage of the aliquots at 2°C to 8°C for about 12 months.

8. The batch of claim 7, wherein the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -0.3% / month to 0.33% / month or from - 0.2% / month to 0.30% / month.

9. The batch of claim 7 or 8, wherein the rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -0.18% / month to 0.33% / month or from -0.12% / month to 0.28% / month.

10. Batches comprising compositions of bupivacaine encapsulated multivesicular liposomes (MVLs), the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise 1, 2- dierucoylphosphatidylcholine (DEPC), 1, 2-dipalmitoyl-sn-glycero-3-phospho-rac-(l- glycerol) (DPPG) or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL;wherein the batches are manufactured within a period of six months, and each of the batches has a volume of at least 100 liters; wherein each batch has a cumulative percentage release of bupivacaine from 46% to 71% at a 24-hour time point, measured from two or more aliquots of each batch using a rotator-facilitated in vitro release assay for at least 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date; and wherein an average rate of change in the cumulative percentage release of bupivacaine of the batches at the 24-hour time point is at least 0.05% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months.

11. The batches of claim 10, wherein the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is from 0.05% / month to 0.5% / month or from 0.08% / month to 0.5% / month.

12. The batches of claim 10 or 11, wherein the average rate of change in the cumulative percentage release of bupivacaine at the 24-hour time point is from 0.1% / month to 0.5% / month, or from 0.1% / month to 0.4% / month.

13. The batches of any one of claims 10 to 12, wherein each batch has a cumulative percentage release of bupivacaine from 60% to 85% at the 48-hour time point, and the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is no less than -0.3% / month.

14. The batches of claim 13, wherein the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -0.3% / month to 0.33% / month or from -0.2% / month to 0.30% / month.

15. The batches of claim 13 or 14, wherein the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -0. 18% / month to 0.33% / month or from -0.12% / month to 0.28% / month.

16. Batches comprising compositions of bupivacaine encapsulated multivesicular liposomes (MVLs), the composition comprising: bupivacaine residing inside a plurality of internal aqueous chambers of MVLs separated by lipid membranes, wherein the lipid membranes comprise 1, 2- dierucoylphosphatidylcholine (DEPC), 1, 2-dipalmitoyl-sn-glycero-3-phospho-rac-(l- glycerol) (DPPG) or a salt thereof, cholesterol, and tricaprylin; and an aqueous medium in which the bupivacaine encapsulated MVLs are suspended, wherein the aqueous medium also comprises unencapsulated bupivacaine; the total bupivacaine concentration in the composition is from 12 mg / mL to 17 mg / mL;wherein the batches are manufactured within a period of six months, and each of the batches has a volume of at least 100 liters; wherein each batch has a cumulative percentage release of bupivacaine from 60% to 85% at a 48-hour time point, measured from two or more aliquots of each batch using a rotator-facilitated in vitro release assay for at least 48 hours, after storage of the aliquots of each batch at 2°C to 8°C for about 12 months from batch manufacture date; and wherein an average rate of change in the cumulative percentage release of bupivacaine of the batches at the 48-hour time point is no less than -0.3% / month after storage of the aliquots of each batch at 2°C to 8°C for about 12 months.

17. The batches of claim 16, wherein the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -0.3% / month to 0.33% / month or from -0.2% / month to 0.30% / month.

18. The batches of claim 16 or 17, wherein the average rate of change in the cumulative percentage release of bupivacaine at the 48-hour time point is from -0. 18% / month to 0.33% / month or from -0. 12% / month to 0.28% / month.

19. The batches of any one of claims 10 to 18, wherein the batches are manufactured within a period of 3 months.

20. The batches of any one of claims 10 to 19, wherein the batches are manufactured within a period of 30 days.

21. The batches of any one of claims 10 to 20, wherein the average rate of change in the cumulative percentage release of bupivacaine is based on three batches, and one batch is manufactured 10 or more days apart from at least one other batch.

22. The batches of any one of claims 10 to 20, wherein the average rate of change in the cumulative percentage release of bupivacaine is based on two batches, and one batch is manufactured 10 or more days apart from the other batch.

23. The batch or batches of any one of claims 1 to 22. wherein the cumulative percentage release of bupivacaine of each batch is measured as the average of six aliquots from each batch.

24. The batch or batches of any one of claims 1 to 23, wherein each aliquot has a cumulative percentage release of bupivacaine from 36% to 81% at the 24-hour time point, and a cumulative percentage release of bupivacaine from 50% to 95% at the 48-hour time point.

25. The batch or batches of any one of claims 1 to 24, wherein the total bupivacaine concentration in the composition is about 13.3 mg / mL.

26. The batch or batches of any one of claims 1 to 25, w herein each batch has a volume of about 120 L to about 300 L. or about 150 L to about 280 L, or about 200 L to about 260 L.

27. The batch of any one of claims 1 to 9 and 23 to 26, prepare by a process comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water-immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water-immiscible solvent solution comprises l,2-dipalmitoyl-sn-glycero-3- phospho-rac-(l -glycerol) (DPPG) or a salt thereof, 1.2-dierucoylphosphatidylcholine (DEPC), tricaprylin and cholesterol, and wherein either the first aqueous solution or the volatile water-immiscible solvent solution comprises bupivacaine;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a water-in-oil-in-water second emulsion, wherein the second aqueous solution comprises lysine and at least one osmotic agent;(c) substantially removing the volatile water-immiscible solvent from the waterin-oil-in-water second emulsion by sparging the water-in-oil-in-water second emulsion to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is about 200 L / min to about 400 L / min;(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow rate is about 200 L / min to about 350 L / min; and(f) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a batch of aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from 12 mg / mL to 17 mg / mL.

28. The batches of any one of claims 10 to 26, wherein each batch is prepared by a process comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water-immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water-immiscible solvent solution comprises l,2-dipalmitoyl-sn-glycero-3- phospho-rac-(l -glycerol) (DPPG) or a salt thereof, 1,2-dierucoylphosphatidylcholine (DEPC), tricaprylin and cholesterol, and wherein either the first aqueous solution or the volatile water-immiscible solvent solution comprises bupivacaine;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a water-in-oil-in-water second emulsion, wherein the second aqueous solution comprises lysine and at least one osmotic agent;(c) substantially removing the volatile water-immiscible solvent from the water- in-oil-in-water second emulsion by sparging the water-in-oil-in-water second emulsion to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is about 200 L / min to about 400 L / min;(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow rate is about 200 L / min to about 350 L / min; and(f) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a batch of aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from 12 mg / mL to 17 mg / mL.

29. A process for preparing bupivacaine encapsulated multivesicular liposomes (MVLs), the process comprising:(a) mixing a first aqueous solution comprising phosphoric acid with a volatile water-immiscible solvent solution to form a water-in-oil first emulsion, wherein the volatile water-immiscible solvent solution comprises at least one phosphatidyl choline, at least one phosphatidyl glycerol, cholesterol, and at least one neutral lipid, and wherein either the first aqueous solution or the solvent solution comprises bupivacaine;(b) mixing the water-in-oil first emulsion with a second aqueous solution to form a water-in-oil-in-water second emulsion, wherein the second aqueous solution comprises lysine and at least one osmotic agent;(c) substantially removing the volatile water-immiscible solvent from the water- in-oil-in-water second emulsion by sparging the water-in-oil-in-water second emulsion at a temperature of about 18°C to about 20°C to form a first aqueous suspension of bupivacaine encapsulated MVLs having a first volume;(d) reducing the first volume of the first aqueous suspension of bupivacaine encapsulated multivesicular liposomes by a first microfiltration to provide a second aqueous suspension of bupivacaine encapsulated MVLs having a second volume, wherein the first microfiltration feed flow rate is at least 190 L / min;(e) exchanging the second aqueous suspension medium with a saline solution by diafiltration to provide a third aqueous suspension of bupivacaine encapsulated MVLs having a third volume, wherein the diafiltration feed flow rate is at least 190 L / min; and(f) reducing the third volume of the third aqueous suspension by a second microfiltration to provide a final aqueous suspension of bupivacaine encapsulated MVLs having a target concentration of bupivacaine from about 12 mg / mL to about 17 mg / mL; wherein the final aqueous suspension of bupivacaine encapsulated MVLs has a volume of at least 100 L; and wherein the process has a bupivacaine MVL product yield of at least about 75%.

30. The process of claim 29, wherein the volatile water-immiscible solvent solution comprises bupivacaine, l,2-dipalmitoyl-sn-glycero-3-phospho-rac-(l-glycerol) (DPPG) or a salt thereof, 1,2-dierucoylphosphatidylcholine (DEPC), tricaprylin and cholesterol.

31. The process of claim 29 or 30, wherein the second aqueous solution comprises lysine and dextrose.

32. The process of any one of claims 29 to 31, wherein the mixing in step (a) is performed at a high speed from about 1100 rpm to about 1300 rpm for about 65 minutes to about 75 minutes.

33. The process of claim 32, wherein the mixing in step (a) is performed at the high speed from about 1200 rpm to about 1250 rpm for about 70 minutes.

34. The process of any one of claims 29 to 31, wherein the mixing in step (a) is performed at a high speed from about 1300 rpm to about 1500 rpm for about 70 minutes to about 90 minutes.

35. The process of claim 34, wherein the mixing in step (a) is performed at the high speed from about 1330 rpm to about 1350 rpm for about 70 minutes.

36. The process of any one of claims 29 to 35, wherein the water-in-oil first emulsion has a volume of about 200 L to about 260 L.

37. The process of any one of claims 29 to 36, wherein the mixing in step (b) is performed at a low speed from about 445 rpm to about 680 rpm for about 60 to 85 seconds.

38. The process of claim 37, wherein the mixing in step (b) is performed at the low speed from about 615 rpm to about 650 rpm for about 70 seconds.

39. The process of any one of claims 29 to 38, wherein the mixing in step (b) is performed at a low speed from about 680 rpm to about 800 rpm for about 65 to 85 seconds.

40. The process of claim 39, wherein the mixing in step (b) is performed at the low speed from about 720 rpm to about 740 rpm for about 70 seconds.

41. The process of any one of claims 29 to 40, wherein step (b) is performed at a temperature of about 18 °C to about 20 °C.

42. The process of any one of claims 29 to 41, wherein volume ratio of the first emulsion to the second emulsion is about 1 : 1 to 1 :5.

43. The process of any one of claims 29 to 42, wherein sparging the water-in-oil-in-water second emulsion is performed at a temperature of about 19 °C for about 19 minutes to about 25 minutes.

44. The process of claim 43, wherein sparging the water-in-oil-in-water second emulsion comprises sparging at a sparging gas flow rate of about 1874 SLPM to about 2500 SLPM, or at a sparging gas flow rate of about 2400 SLPM for about 22 minutes.

45. The process of any one of claims 29 to 44, wherein the first microfiltration is conducted with a beginning first microfiltration feed flow rate of about 220 L / min to about 350 L / min, and an end first microfiltration feed flow rate of about 190 L / min to about 310 L / min.

46. The process of claim 45, wherein the first microfiltration feed flow rate decreases approximately linearly in relation to the MVL concentration in the first aqueous suspension, and wherein the beginning first microfiltration feed flow rate is about 340 L / min, and the end first microfiltration feed flow rate is about 300 L / min.

47. The process of any one of claims 29 to 46, wherein a diafiltration feed flow rate during a first stage of the diafiltration is about 190 L / min to about 310 L / min, and a diafiltration feed flow rate during a second stage of the diafiltration is about 190 L / min to about 265 L / min.

48. The process of claim 47, wherein the diafiltration feed flow rate during the first stage of diafiltration is about 300 L / min. wherein the diafiltration feed flow rate during the second stage of diafiltration is about 255 L / min.

49. The process of any one of claims 29 to 48, wherein the second microfiltration is conducted with a beginning second microfiltration feed flow rate of about 190 L / min to about 265 L / min, and an end second microfiltration feed flow rate of about 120 L / min to about 190 L / min.

50. The process of claim 49, wherein the second microfiltration feed flow rate decreases approximately linearly in relation to the MVL concentration in the third aqueous suspension, and wherein the beginning second microfiltration feed flow rate is about 255 L / min, and the end second microfiltration feed flow rate is about 180 L / min.

51. The process of any one of claims 29 to 50, wherein steps (d). (e) and (f) is conducted with a crossflow filtration system that is configured to switch between microfiltration and diafiltration mode, wherein the crossflow filtration system comprises a plurality of independently operating crossflow modules, each crossflow module comprises at least one filter array, and each filter array comprises a plurality of hollow fiber filters.

52. The process of claim 51, wherein the crossflow filtration system comprises two filter arrays, and each filter array comprises six hollow fiber filters.

53. The process of claim 51 or 52, wherein the crossflow filtration system further comprises at least one turbidity sensor downstream of the at least one filter array for detection of loss of filter integrity .

54. The process of claim 53, further comprising: detecting an abnormal turbidity value by the at least one turbidity sensor, wherein the abnormal turbidity value is a value above a threshold value; and testing one or more filters of the at least one filter array for a potential filter integrity failure by successively deactivating individual filters of the one or more filters and measuring turbidity by the at least one turbidity sensor while each individual filter is deactivated until a normal turbidity value is detected, wherein a normal turbidity value is a value below the threshold value.

55. The process of claim 54, wherein, in response to detecting a normal turbidity value, the process comprises identifying the individual filter that was deactivated when the normal turbidity value was detected as a potentially damaged filter.

56. The process of claim 55, further comprising: testing the potentially damaged filter by reactivating the potentially damaged filter and measuring turbidity by the at least one turbidity sensor while the potentially damaged filter is active; and in response to measuring an abnormal turbidity value when the potentially damaged filter is active after reactivation, determining that the potentially damaged filter is a damaged filter and deactivating the damaged filter.

57. The process of any one of claims 29 to 56, wherein the batch has a volume of about 120 L to about 300 L, about 150 L to about 280 L, about 200 L to about 260 L, about 320 L to about 500 L, or about 350 to about 450 L58. The process of any one of claims 29 to 57, wherein the process has a bupivacaine MVL product yield of at least about 80%.

59. A composition of bupivacaine encapsulated multivesicular liposomes (MVLs), prepared by the process of any one of claims 29 to 57.

60. A batch comprising a composition of bupivacaine encapsulated multivesicular liposomes (MVLs), prepared by the process of any one of claims 29 to 57.

61. A method of treating or ameliorating pain in a subject in need thereof, comprising administering the composition of any one of claims 1 to 28 and 59 to 60 to the subject.

62. The method of claim 61, wherein the administration is via local infiltration to a surgical site to provide local analgesia.

63. The method of claim 61, wherein the administration is via interscalene brachial plexus nen e block or femoral nerve block to provide regional analgesia.

64. The method of claim 61, wherein the administration is via an adductor canal block or via a sciatic nerve block in the popliteal fossa to provide regional analgesia.

65. The method of any one of claims 61 to 64. wherein the composition has a volume of about 10 mL or 20 mL for a single-dose administration.

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