APPARATUS AND METHODS FOR NANOPARTICLE GENERATION AND PROCESS INTENSIFICATION OF TRANSPORT AND REACTION SYSTEMS
원문보기
IPC분류정보
국가/구분
United States(US) Patent
공개
국제특허분류(IPC7판)
B01F-005/12
B01F-005/04
B01F-015/06
B82Y-040/00
출원번호
US-0481193
(2012-05-25)
공개번호
US-0236680
(2012-09-20)
발명자
/ 주소
PANAGIOTOU, Thomai
Mesite, Steven Vincent
Fisher, Robert John
출원인 / 주소
MICROFLUIDICS INTERNATIONAL CORPORATION
인용정보
피인용 횟수 :
0인용 특허 :
0
초록▼
Apparatus, systems and methods are provided that utilize microreactor technology to achieve desired mixing and interaction at a micro and/or molecular level between and among feed stream constituents. Feed streams are fed to an intensifier pump at individually controlled rates, e.g., based on operat
Apparatus, systems and methods are provided that utilize microreactor technology to achieve desired mixing and interaction at a micro and/or molecular level between and among feed stream constituents. Feed streams are fed to an intensifier pump at individually controlled rates, e.g., based on operation of individually controlled feed pumps. The time during which first and second feed streams are combined/mixed prior to introduction to the microreactor is generally minimized, thereby avoiding potential reactions and other constituent interactions prior to micro- and/or nano-scale interactions within the microreactor. Various microreactor designs/geometries may be employed, e.g., “Z” type single or multi-slot geometries and “Y” type single or multi-slot geometries. Various applications benefit from the disclosure, including emulsion, crystallization, encapsulation and reaction processes.
대표청구항▼
1.-15. (canceled) 16. A method for processing at least two liquid feed streams, comprising: a. feeding first and second constituents to one or more intensifier pumps at different individually actively controlled rates such that interaction is substantially prevented prior to pressurization within th
1.-15. (canceled) 16. A method for processing at least two liquid feed streams, comprising: a. feeding first and second constituents to one or more intensifier pumps at different individually actively controlled rates such that interaction is substantially prevented prior to pressurization within the one or more intensifier pumps;b. pressurizing the first and second constituents in a combined stream within the one or more intensifier pumps to an elevated pressure of at least 35 MPa;c. delivering the combined stream to a microreactor downstream from the one or more intensifier pumps, the microreactor having a minimum channel dimension of 150 microns or less, causing the first and second constituents to interact within the microreactor at a nanoscale level. 17. The method of claim 16, wherein the first and second constituents are fed to the one or more intensifier pumps in feed lines that are coaxially aligned. 18. The method of claim 16, wherein the first and second constituents are introduced to the one or more intensifier pumps through spaced ports defined by the one or more intensifier pumps. 19. The method according to claim 16, wherein the first and second constituents are fed to the at least one intensifier pump through a first feed line and a second feed line that is coaxially positioned within the first feed line so as to prevent substantial mixing of the first and second constituents prior to pressurization by the at least one intensifier pump. 20. The method of claim 16, wherein the microreactor is characterized by a geometry selected from the group consisting of: (i) a “Z” type single slot geometry, (ii) a “Y” type single slot geometry, (iii) a “Z” type multi-slot geometry; or (iv) a “Y” type multi-slot geometry. 21. The method of claim 16, further comprising recycling at least a portion of effluent from the microreactor to the one or more intensifier pumps. 22. The method of claim 16, wherein the different individually actively controlled rates for delivery of the first and second constituents to the one or more intensifier pumps are effected by individually actively controlled feed pumps for the first and second constituents. 23. The method of claim 16, wherein the different individually actively controlled rates are effective to control the ratio of first constituent to second constituent fed to the one or more intensifier pumps. 24. The method of claim 16, further comprising cooling or quenching the combined stream after interaction within the microreactor. 25. The method of claim 16, wherein the first constituent includes a solvent and wherein the second constituent includes an antisolvent, and wherein, interaction of the solvent and the antisolvent in the microreactor is effective to define a nanosuspension, the method further comprising:obtaining constituent nanoparticle crystals from the nanosuspension that define a median particle size. 26. The method of claim 25, wherein the solvent stream is selected from the group consisting of dimethyl sulfoxide (DMSO), N-Methyl-2-Purrolidone (NMP), methanol, ethanol, acetone, dichloromethane, octanol and isopropyl alcohol, and the antisolvent stream is selected from the group consisting of water, hexane and heptane. 27. The method of claim 26, wherein the solvent stream is DMSO and nanoparticles of azithromycin are obtained at a median particle size of about 50-100 nm. 28. The method of claim 26, wherein the solvent stream is DMSO and nanoparticles of oxycarbazepine are obtained at a median particle size less than 1000 nm. 29. The method of claim 26, wherein the solvent stream is DMSO or NMP and nanoparticles of loratadine are obtained at a median particle size of less than 500 nm. 30. The method of claim 25, further comprising cooling or quenching the nanosuspension after interaction within the microreactor. 31. The method of claim 16 for controlling a reaction, wherein the first constituent is a first reactant and the second constituent is a second reactant, the method further comprising: adjusting reaction selectivity by controlling interaction between the first and second reactants prior to the nanoscale level interaction within the microreactor. 32. The method of claim 31, wherein control of the interaction between the first and second reactants is effected by limiting contact between the first and second reactants prior to pressurization in the at least one intensifier pump. 33. The method of claim 31, wherein the first and second reactants are delivered to the at least one intensifier pump through spaced ports defined by the at least one intensifier pump. 34. The method of claim 31, further comprising cooling or quenching the first and second reactants after interaction within the microreactor. 35. The method of claim 31, wherein the first and second reactants react at an accelerated rate due to enhanced surface interaction between the first and second reactants within the microreactor. 36. The method of claim 35, further comprising cooling or quenching the first and second reactants after reaction within the microreactor. 37. The method of claim 16, wherein wherein interaction of the first and second constituents in the microreactor produces polymorphs, and wherein polymorph production is controlled through control of operational parameters associated with the microreactor. 38. The method of claim 37, wherein the operational parameters are selected from the group consisting of microreactor design, microreactor geometry, pressure generated by the intensifier pump, supersaturation ratio, solvents, antisolvents, temperature and combinations thereof. 39. The method of claim 37, further comprising cooling or quenching the first and second streams after interaction within the microreactor. 40-52. (canceled) 53. The method of claim 16, wherein the elevated pressure is at least about 70 MPa. 54. The method of claim 16, wherein the elevated pressure is at least about 140 MPa. 55. The method of claim 16, wherein the elevated pressure is at least about 207 MPa. 56. The method of claim 16, wherein the ratio of the flow rate of the second stream to the flow rate of the first stream is at least about 2:1. 57. The method of claim 16, wherein the ratio of the flow rate of the second stream to the flow rate of the first stream is at least about 3:1. 59. The system of claim 1, wherein the ratio of the flow rate of the second stream to the flow rate of the first stream is at least about 10:1. 60. The method of claim 16, wherein the microreactor has channels with minimum dimensions in the range of 75-150 microns. 61. The method of claim 16, wherein the average fluid velocity in microreactor channels is in the range of 300-500 m/s. 62. The method of claim 16, further comprising: effecting a sheer rate in the microreactor of at least about 1.2×106 s−1. 63. The method of claim 16, further comprising: controlling the first controlled rate with respect to the second controlled rate. 64. The method of claim 16, wherein the microreactor has a multi-slot geometry. 65. The method of claim 16, wherein the first and second feed streams enter the microreactor as impinging jets. 66. The method of claim 16, wherein at least one of the liquid feed streams includes solid particles. 67. The method of claim 25, wherein at least one of the feed streams contains seed particles. 68. The method of claim 25, wherein at least one of the feed streams contains catalyst particles. 69. The method of claim 31, wherein at least one of the feed streams contains seed particles. 70. The method of claim 31, wherein at least one of the feed streams contains catalyst particles. 71. The method of claim 31, wherein at least one of the reactants is a solid.
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