U.S. patent application number 14/893483 was filed with the patent office on 2016-03-31 for falling bed reactor.
The applicant listed for this patent is BATTELLE MEMORIAL INSTITUTE. Invention is credited to Zia Abdullah, Michael A. O'Brian, Slawomir Winecki, Kevin Yugulis.
Application Number | 20160090535 14/893483 |
Document ID | / |
Family ID | 50983196 |
Filed Date | 2016-03-31 |
United States Patent
Application |
20160090535 |
Kind Code |
A1 |
Abdullah; Zia ; et
al. |
March 31, 2016 |
FALLING BED REACTOR
Abstract
Methods and apparatuses are provided for pyrolysis using a
falling bed reactor. The falling bed reactor may result in
effective mixing between a heat carrier and biomass, and may reduce
or eliminate inert gas requirements.
Inventors: |
Abdullah; Zia; (Columbus,
OH) ; O'Brian; Michael A.; (Columbus, OH) ;
Winecki; Slawomir; (Dublin, OH) ; Yugulis; Kevin;
(Columbus, OH) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
BATTELLE MEMORIAL INSTITUTE |
Columbus |
OH |
US |
|
|
Family ID: |
50983196 |
Appl. No.: |
14/893483 |
Filed: |
May 23, 2014 |
PCT Filed: |
May 23, 2014 |
PCT NO: |
PCT/US14/39443 |
371 Date: |
November 23, 2015 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
|
|
61826989 |
May 23, 2013 |
|
|
|
Current U.S.
Class: |
201/4 ; 201/12;
202/108 |
Current CPC
Class: |
B01J 8/388 20130101;
B07B 11/04 20130101; B01J 2208/00513 20130101; B01J 8/087 20130101;
C10B 49/18 20130101; B01J 2208/00292 20130101; B07B 4/02 20130101;
B01J 2208/00168 20130101; Y02E 50/14 20130101; C10B 49/16 20130101;
B01J 8/12 20130101; B01J 8/082 20130101; C10B 53/02 20130101; B01J
8/002 20130101; B01J 2208/0084 20130101; C10B 3/00 20130101; Y02E
50/10 20130101 |
International
Class: |
C10B 49/18 20060101
C10B049/18; C10B 53/02 20060101 C10B053/02; C10B 3/00 20060101
C10B003/00 |
Claims
1. A falling bed reactor 100, comprising: a reactor conduit 102
defining a flow axis 104; an inlet 106 operatively coupled to
receive a heat carrier particulate into the reactor conduit 102; an
outlet 108 operatively coupled to direct the heat carrier
particulate out of the reactor conduit 102; one or more baffles 114
mounted in the reactor conduit 102.
2. The falling bed reactor 100 of claim 1, comprising: the reactor
conduit 102 defining the flow axis 104; the inlet 106 operatively
coupled to receive the heat carrier particulate into the reactor
conduit 102; the outlet 108 operatively coupled to direct the heat
carrier particulate out of the reactor conduit 102; a pyrolysis
substrate inlet 110 operatively coupled to receive a pyrolysis
substrate into the reactor conduit 102; a pyrolysis product outlet
112 operatively coupled to direct a pyrolysis product out of the
reactor conduit 102; and the one or more baffles 114 mounted in the
reactor conduit 102, each baffle in the one or more baffles 114
comprising a baffle surface 116, at least a portion of each baffle
surface 116 being at an oblique angle 118 with respect to the flow
axis 104.
3. The falling bed reactor 100 of claim 1, configured to be mounted
such that at least a portion of the flow axis 104 is parallel or
oblique to a vertically downwards direction.
4. The falling bed reactor 100 of claim 2, configured to be mounted
such that at least a portion of the flow axis 104 is parallel or
oblique to a vertically downwards direction, and at least a portion
of each baffle surface 116 is at the oblique angle 118 with respect
to the vertically downwards direction.
5. The falling bed reactor 100 of claim 1, mounted to orient the
flow axis 104 in a substantially vertically downwards
direction.
6. The falling bed reactor 100 of claim 1, a cross section of the
reactor conduit 102 comprising a shape that is one of: polygonal,
rounded polygonal, elliptical, circular, or a combination or
composite thereof.
7. The falling bed reactor 100 of claim 1, a cross section of the
reactor conduit 102 comprising a shape that is one of: rectangular,
rounded rectangular, elliptical, circular, or a combination or
composite thereof.
8. The falling bed reactor 100 of claim 1, a cross section of the
reactor conduit 102 being square.
9. The falling bed reactor 100 of claim 1, one or both of the inlet
106 and the outlet 108 being substantially parallel with one or
both of the reactor conduit 102 and the flow axis 104.
10. The falling bed reactor 100 of claim 1, the inlet 106 being
operatively coupled to the reactor conduit 102 upstream of the
outlet 108 with respect to the flow axis 104.
11. The falling bed reactor 100 of claim 1, the inlet 106 being
operatively coupled to receive a pyrolysis substrate into the
reactor conduit 102.
12. The falling bed reactor 100 of claim 1, the outlet 108 being
operatively coupled to direct a pyrolysis product out of the
reactor conduit 102.
13. The falling bed reactor 100 of claim 1, further comprising: a
pyrolysis substrate inlet 110 operatively coupled to receive a
pyrolysis substrate into the reactor conduit 102; and a pyrolysis
product outlet 112 operatively coupled to direct a pyrolysis
product out of the reactor conduit 102.
14. The falling bed reactor 100 of claim 13, further comprising a
fine particulate separator 202, an input 204 of the fine
particulate separator 202 operatively coupled to the pyrolysis
product outlet 112 of the falling bed reactor 100 and the fine
particulate separator 202 comprising a particulate outlet 206 and a
gas or vapor outlet 208.
15. The falling bed reactor 100 of claim 14, the fine particulate
separator 202 comprising one or more of: a settling chamber, a
baffle chamber, a cyclonic particle separator, an electrostatic
precipitator, a filter, or a scrubber.
16. The falling bed reactor 100 of claim 13, the pyrolysis
substrate inlet 110 being operatively coupled to the reactor
conduit 102 upstream of the pyrolysis product outlet 112 with
respect to the flow axis 104.
17. The falling bed reactor 100 of claim 13, the pyrolysis
substrate inlet 110 being operatively coupled to the reactor
conduit 102 upstream of the pyrolysis product outlet 112 with
respect to the flow axis 104.
18. The falling bed reactor 100 of claim 13, the pyrolysis
substrate inlet 110 being operatively coupled to the reactor
conduit 102 at a same level or downstream of the pyrolysis product
outlet 112 with respect to the flow axis 104.
19. The falling bed reactor 100 of claim 13, the pyrolysis
substrate inlet 110 being coincident with the inlet 106.
20. The falling bed reactor 100 of claim 13, the pyrolysis product
outlet 112 being coincident with the inlet 106 or the outlet
108.
21. The falling bed reactor 100 of claim 1, the one or more baffles
114 extending from an inside wall 130 of the reactor conduit 102
into the reactor conduit 102.
22. The falling bed reactor 100 of claim 21, the one or more
baffles 114 extending from the inside wall 130 to define a
cantilevered geometry in the reactor conduit 102.
23. The falling bed reactor 100 of claim 21, the one or more
baffles 114 extending across at least a portion of the reactor
conduit 102 between a first portion of the inside wall 130 and a
second portion of the inside wall 130.
24. The falling bed reactor 100 of claim 21, each of the one or
more baffles 114 comprising a form of one or more of a rod, a
plate, a funnel, a cone, a screen, or a protrusion.
25. The falling bed reactor 100 of claim 21, each of the one or
more baffles 114 comprising a form of a rod, the rod having a
cross-sectional geometry that is at least in part polygonal,
rounded polygonal, circular, elliptical, or a combination or
composite thereof.
26. The falling bed reactor 100 of claim 21, each of the one or
more baffles 114 comprising a baffle surface 116 positioned to
intersect at least a portion of the reactor conduit 102 with
respect to the flow axis 104, at least a portion of the baffle
surface 116 comprising a geometry that is one or more of flat or
convex.
27. The falling bed reactor 100 of claim 21, each of the one or
more baffles 114 comprising a baffle surface 116, at least a
portion of the baffle surface 116 being horizontal with respect to
the flow axis 104.
28. The falling bed reactor 100 of claim 21, each of the one or
more baffles 114 comprising a baffle surface 116, at least a
portion of the baffle surface 116 being at an oblique angle 118
with respect to the flow axis 104.
29. The falling bed reactor 100 of claim 28, the one or more
baffles 114 being mounted to place at least the portion of each
baffle surface 116 at the oblique angle 118 with respect to the
flow axis 104 such that the one or more baffles 114 form a
staggered or alternating pattern in the reactor conduit 102.
30. The falling bed reactor 100 of claim 29, the staggered or
alternating pattern of the one or more baffles 114 intersecting the
flow axis 104 to provide a tortuous flow path through the one or
more baffles 114.
31. The falling bed reactor 100 of claim 21, each baffle in the one
or more baffles 114 being mounted to an inside wall 130 of the
reactor conduit 102 to define a free edge 120 of each baffle
surface 116 and a mounted edge 122 of each baffle surface 116.
32. The falling bed reactor 100 of claim 21, each baffle surface
116 in the one or more baffles 114 is substantially at the oblique
angle 118 with respect to the flow axis 104.
33. The falling bed reactor 100 of claim 21, the oblique angle 118
being between about 30.degree. and about 60.degree. with respect to
the flow axis 104 such that for each baffle surface 116, a free
edge 120 of the baffle surface 116 is further downstream along the
flow axis 104 compared to a mounted edge 122 of the baffle surface
116.
34. The falling bed reactor 100 of claim 21, further comprising an
agitator mechanism 126 configured to agitate at least a portion of
the one or more baffles 114 effective to dislodge a particulate on
at least a portion of the one or more baffles 114.
35. The falling bed reactor 100 of claim 1, further comprising a
heater 128 configured to cause pyrolysis of a substrate in the
falling bed reactor 100 by heating one or both of the falling bed
reactor 100 and a heat carrier to be fed into the falling bed
reactor 100.
36. The falling bed reactor 100 of claim 1, being configured to
employ the heat carrier comprising one or more of: a metal, a
glass, a ceramic, a mineral, or a polymeric composite.
37. The falling bed reactor 100 of claim 1, being configured to
employ sand as the heat carrier.
38. The falling bed reactor 100 of claim 1, being configured to
employ a particulate catalyst as the heat carrier.
39. A pyrolysis system 200, comprising: a falling bed reactor 100,
comprising: a reactor conduit 102 defining a flow axis 104; an
inlet 106 operatively coupled to receive a heat carrier particulate
into the reactor conduit 102; an outlet 108 operatively coupled to
direct the heat carrier particulate out of the reactor conduit 102;
one or more baffles 114 mounted in the reactor conduit 102; and a
cross-flow classifier 3100, comprising: a separator conduit 3102; a
flow input 3104 and a flow output 3106 in fluidic communication
with the separator conduit 3102, the separator conduit 3102
extending between the flow input 3104 and the flow output 3106 to
define a flow axis 3108 along at least a portion of the separator
conduit 3102, the flow input 3104 being located upstream of the
flow output 3106 with respect to the flow axis 3108; and a
cross-flow input 3114 and a cross-flow output 3116 in fluidic
communication with the separator conduit 3102 between the flow
input 3104 and the flow output 3106, the cross-flow input 3114
being located upstream of the cross-flow output 3116 with respect
to the flow axis 3108, the cross-flow input 3114 defining a
cross-flow axis 3118 intersecting the flow axis 3108 at a
cross-flow angle 3120 between about 70.degree. and about
180.degree. with respect to the flow axis 3108, wherein: the outlet
108 of the falling bed reactor 100 is operatively coupled to the
flow input 3104 of the cross-flow classifier 3100; and the flow
output 3106 of the cross-flow classifier 3100 is operatively
coupled to the inlet 108 of the falling bed reactor 100.
40. The pyrolysis system 200 of claim 39, comprising: the falling
bed reactor 100, comprising: the reactor conduit 102 defining a
flow axis 104; the inlet 106 operatively coupled to receive a heat
carrier particulate into the reactor conduit 102; the outlet 108
operatively coupled to direct the heat carrier particulate out of
the reactor conduit 102; a pyrolysis substrate inlet 110
operatively coupled to receive a pyrolysis substrate into the
reactor conduit 102; a pyrolysis product outlet 112 operatively
coupled to direct a pyrolysis product out of the reactor conduit
102; the one or more baffles 114 mounted in the reactor conduit
102, each baffle in the one or more baffles 114 comprising a baffle
surface 116, at least a portion of each baffle surface 116 being at
an oblique angle 118 with respect to the flow axis 104; and the
cross-flow classifier 3100, comprising: the separator conduit 3102;
the flow input 3104 and the flow output 3106 in fluidic
communication with the separator conduit 3102, the separator
conduit 3102 extending between the flow input 3104 and the flow
output 3106 to define the flow axis 3108 along at least a portion
of the separator conduit 3102, the flow input 3104 being located
upstream of the flow output 3106 with respect to the flow axis
3108; and the cross-flow input 3114 and the cross-flow output 3116
in fluidic communication with the separator conduit 3102 between
the flow input 3104 and the flow output 3106, the cross-flow input
3114 being located upstream of the cross-flow output 3116 with
respect to the flow axis 3108, the cross-flow input 3114 defining
the cross-flow axis 3118 intersecting the flow axis 3108 at a
cross-flow angle 3120 between about 70.degree. and about
180.degree. with respect to the flow axis 3108, wherein: the outlet
108 of the falling bed reactor 100 is operatively coupled to the
flow input 3104 of the cross-flow classifier 3100; and the flow
output 3106 of the cross-flow classifier 3100 is operatively
coupled to the inlet 108 of the falling bed reactor 100.
41. The pyrolysis system 200 of claim 39, the outlet 108 of the
falling bed reactor 100 being operatively coupled to the flow input
3104 of the cross-flow classifier 3100 via an auger or conveyor
230.
42. The pyrolysis system 200 of claim 39, the flow output 3106 of
the cross-flow classifier 3100 being operatively coupled to the
inlet 108 of the falling bed reactor 100 via an auger or conveyor
232.
43. The pyrolysis system 200 of claim 39, further comprising a fine
particulate separator 202, an input 204 of the fine particulate
separator 202 operatively coupled to the pyrolysis product outlet
112 of the falling bed reactor 100 and the fine particulate
separator 202 comprising a particulate outlet 206 and a gas or
vapor outlet 208.
44. The pyrolysis system 200 of claim 43, the fine particulate
separator 202 comprising one or more of: a settling chamber, a
baffle chamber, a cyclonic particle separator, an electrostatic
precipitator, a filter, or a scrubber.
45. The pyrolysis system 200 of claim 39, further comprising a
coarse particulate separator 212, an input 214 of the coarse
particulate separator 212 operatively coupled to the cross-flow
output 3116 of the cross-flow classifier 3100 and the coarse
particulate separator 212 comprising a particulate outlet 216 and a
gas outlet 218.
46. The pyrolysis system 200 of claim 45, the coarse particulate
separator 212 comprising one or more of: a settling chamber, a
baffle chamber, a cyclonic particle separator, an electrostatic
precipitator, a filter, or a scrubber.
47. The pyrolysis system 200 of claim 39, further comprising a gas
recycle conduit 220, the gas recycle conduit operatively coupled to
receive recycled gas from the gas outlet 218 and the gas recycle
conduit 220 operatively coupled to direct the recycled gas to the
cross-flow input 3114 of the cross-flow classifier 3100.
48. The pyrolysis system 200 of claim 47, the gas recycle conduit
comprising a fan 222, the fan 222 configured to draw the recycled
gas from the gas outlet 218 via the gas recycle conduit 220 and the
fan 222 configured to flow the recycled gas to the cross-flow input
3114 of the cross-flow classifier 3100 via the gas recycle conduit
220.
49. The pyrolysis system 200 of claim 39, the falling bed reactor
100 comprising the falling bed reactor of any of claims 1-38.
50. The pyrolysis system 200 of claim 39, one or both of the flow
input 3114 and the flow output 3116 being substantially aligned
with the flow axis 3108 of the separator conduit 3102.
51. The pyrolysis system 200 of claim 39, the cross-flow input 3114
being operatively coupled to the separator conduit 3102
substantially opposite to the cross-flow output 3116 with respect
to the flow axis 3108.
52. The pyrolysis system 200 of claim 39, being mounted such that
the flow axis 3108 points downward at a flow angle 3110.
53. The pyrolysis system 200 of claim 52, the flow angle 3110 being
less than 60.degree. from vertically down.
54. The pyrolysis system 200 of claim 39, the separator conduit
3102 comprising a first flow diameter 3122 between the flow input
3104 and the cross-flow input 3114, and the separator conduit 3102
comprising a second flow diameter 3124 downstream of the cross-flow
input 3114, the first flow diameter 3122 being greater than the
second flow diameter 3124.
55. The pyrolysis system 200 of claim 54, the separator conduit
3102 comprising a transition 3126 between the first flow diameter
3122 and the second flow diameter 3124, the transition 3126 being
substantially aligned with the cross-flow angle 3120.
56. The pyrolysis system 200 of claim 54, the separator conduit
3102 comprising a transition 3126 between the first flow diameter
3122 and the second flow diameter 3124, the transition 3126 being
substantially perpendicular with respect to the flow axis 3108.
57. The pyrolysis system 200 of claim 39, the flow input 3104 being
configured to accept a plurality of particulates, at least a first
particulate in the plurality of particulates being characterized by
a first average density and at least a second particulate in the
plurality of particulates being characterized by a second average
density greater than the first average density.
58. The pyrolysis system 200 of claim 57, the flow output 3106
being configured to convey at least a portion of the first
particulate characterized by the first density out of the separator
conduit 3102.
59. The pyrolysis system 200 of claim 58, the cross-flow output
3116 being configured to convey at least a portion of the second
particulate characterized by the second density greater than the
first density out of the separator conduit 3102.
60. The pyrolysis system 200 of claim 39, the cross-flow input 3114
defining a first convergent nozzle 3132 comprising a first nozzle
throat 3134.
61. The pyrolysis system 200 of claim 60, a cross section of the
first nozzle throat 3134 comprising at least two dissimilar
axes.
62. The pyrolysis system 200 of claim 61, the first nozzle throat
3134 comprising an elliptical cross section, a circular cross
section, a rectangular cross section, or a rounded corner
rectangular cross section.
63. The pyrolysis system 200 of claim 60, the first nozzle throat
3134 being operatively coupled to a nozzle exit zone, at least a
portion of the nozzle exit zone comprising a transition 3126
between a first flow diameter 3122 of the flow conduit 3108 and the
first nozzle throat 3134.
64. The pyrolysis system 200 of claim 63, at least a portion of the
nozzle exit zone comprising a second flow diameter 3124 of the
separator conduit 3108, the transition 3126 being located at an
upstream side of the first nozzle throat 3134 and the second flow
diameter 3124 being located at a downstream side of the first
nozzle throat 3134.
65. The pyrolysis system 200 of claim 64, the first nozzle throat
3134 being located at the second flow diameter 3124 of the
separator conduit 3108.
66. The pyrolysis system 200 of claim 60, the convergent nozzle
3132 of the cross-flow input 3114 comprising a second nozzle throat
3138, the first nozzle throat 3134 being located at the cross-flow
input 3114 between the second nozzle throat 3138 and the separator
conduit 3108.
67. The pyrolysis system 200 of claim 39, the cross-flow output
3116 defining a second convergent nozzle 3142 comprising a third
nozzle throat 3144.
68. The pyrolysis system 200 of claim 67, a cross section of the
third nozzle throat 3144 comprising at least two dissimilar
axes.
69. The pyrolysis system 200 of claim 68, the third nozzle throat
3144 comprising an elliptical cross section, a circular cross
section, a rectangular cross section, or a rounded corner
rectangular cross section.
70. The pyrolysis system 200 of claim 68, the third nozzle throat
3144 being operatively coupled to a nozzle entrance zone 3146, at
least a portion of the nozzle entrance zone 3146 comprising a
transition 3148 between a second flow diameter 3124 of the flow
conduit 3108 and the third nozzle throat 3144.
71. The pyrolysis system 200 of claim 68, at least a portion of the
nozzle entrance zone 3146 comprising an entrance vane 3150, the
entrance vane 3150 extending into the separator conduit 3102 with
respect to the second flow diameter 3124.
72. The pyrolysis system 200 of claim 71, at least a portion of the
entrance vane 3150 extending into the separator conduit 3102 at
least partly in an upstream direction with respect to the flow axis
3108.
73. The pyrolysis system 200 of claim 68, the third nozzle throat
3144 being operatively coupled through a nozzle collector zone to
an exit conduit 3154, one or both of the nozzle collector zone and
the conduit 3154 comprising an elliptical cross section.
74. The pyrolysis system 200 of claim 68, the third nozzle throat
3144 being operatively coupled through a nozzle collector zone to
an exit conduit 3154, one or both of the nozzle collector zone and
the exit conduit 3154 comprising a circular cross section.
75. The pyrolysis system 200 of claim 68, the third nozzle throat
3144 being operatively coupled to an exit conduit 3154, the exit
conduit 3154 defining an exit conduit axis 3156, the exit conduit
axis 3156 intersecting the flow axis 3108 at an exit angle 3158,
the exit angle 3158 being greater than 0.degree. and less than
180.degree..
76. The pyrolysis system 200 of claim 75, the exit angle 3158 being
between about 90.degree. and less than 180.degree..
77. The pyrolysis system 200 of claim 76, the exit conduit axis
3156 being within about 30.degree. of vertical.
78. A method 400 for pyrolyzing a substrate, comprising: 402
feeding a heat carrier to a gravity-fed baffled conduit; 404
feeding a pyrolysis substrate to the gravity-fed baffled conduit
such that the heat carrier and the pyrolysis substrate mix to form
a pyrolysis mixture; and 406 heating the heat carrier and/or the
gravity-fed baffled conduit to pyrolyze the pyrolysis substrate in
the pyrolysis mixture to form a pyrolysis product mixture.
79. The method of claim 78, the pyrolysis product mixture
comprising a gas or vapor pyrolysis product and a fine char
pyrolysis product, further comprising directing the gas or vapor
pyrolysis product and the fine char pyrolysis product out of the
gravity-fed baffled conduit.
80. The method of claim 79, the pyrolysis product mixture
comprising the heat carrier and a coarse char pyrolysis product,
further comprising directing the heat carrier and the coarse char
pyrolysis product out of the gravity-fed baffled conduit.
81. The method of claim 80, further comprising directing the gas or
vapor pyrolysis product and the fine char pyrolysis product out of
the gravity-fed baffled conduit at the same level as the heat
carrier and the coarse char pyrolysis product.
82. The method of claim 81, further comprising directing the gas or
vapor pyrolysis product and the fine char pyrolysis product out of
the gravity-fed baffled conduit upstream compared to the heat
carrier and the coarse char pyrolysis product.
83. The method of claim 81, further comprising directing the gas or
vapor pyrolysis product and the fine char pyrolysis product out of
the gravity-fed baffled conduit downstream compared to the heat
carrier and the coarse char pyrolysis product.
84. The method of claim 78, the pyrolysis product mixture
comprising the heat carrier and a coarse char pyrolysis product,
further comprising directing the heat carrier and the coarse char
pyrolysis product out of the gravity-fed baffled conduit.
85. The method of claim 78, feeding the heat carrier to the
gravity-fed baffled conduit comprises feeding the heat carrier and
the pyrolysis substrate to the same level in the gravity-fed
baffled conduit.
86. The method of claim 78, feeding the heat carrier to the
gravity-fed baffled conduit comprises feeding the heat carrier to
the gravity-fed baffled conduit upstream of the pyrolysis
substrate.
87. The method of claim 78, feeding the heat carrier to the
gravity-fed baffled conduit comprises feeding the heat carrier to
the gravity-fed baffled conduit downstream of the pyrolysis
substrate.
88. The method of claim 78, the pyrolysis product mixture
comprising a gas or vapor pyrolysis product and a fine char
pyrolysis product, the method further comprising: directing the gas
or vapor pyrolysis product and the fine char pyrolysis product out
of the gravity-fed baffled conduit; and separating the gas or vapor
pyrolysis product from the fine char pyrolysis product
89. The method of claim 78, the pyrolysis product mixture
comprising the heat carrier and a coarse char pyrolysis product,
the method further comprising: directing the heat carrier and the
coarse char pyrolysis product out of the gravity-fed baffled
conduit; and separating the heat carrier from the coarse char
pyrolysis product.
90. The method of claim 78, further comprising: recycling the heat
carrier to form a recycled heat carrier; and feeding the recycled
heat carrier to the gravity-fed baffled conduit.
91. The method of claim 78, wherein separating the heat carrier
from the coarse char pyrolysis product comprises: directing a flow
comprising a plurality of particulates along a flow axis; and
separating at least a portion of a first particulate from the
plurality of particulates to form a separated portion of the first
particulate by directing a gas jet along a cross-flow axis, the
cross-flow axis intersecting the flow axis at a cross-flow angle,
the cross-flow angle being between about 70.degree. and about
180.degree., wherein: the plurality of particulates comprises the
heat carrier and the coarse char pyrolysis product; and the first
particulate comprises the coarse char pyrolysis product
92. The method of claim 91, the cross-flow angle being between
about 80.degree. and about 100.degree..
93. The method of claim 91, the cross-flow axis and the flow axis
being substantially perpendicular.
94. The method of claim 91, the gas jet comprising a gas
temperature of between about 300.degree. C. and about 700.degree.
C.
95. The method of claim 91, the gas jet comprising a gas density in
kilograms per cubic meter of between about 0.4 and about 1.4.
96. The method of claim 91, the gas jet comprising a gas viscosity
in kilograms per meter-second of between about 1.times.10.sup.-6
and about 1.times.10.sup.-4.
97. The method of claim 91, the gas jet comprising a gas flow rate
of less than 25 cubic feet per minute.
98. The method of claim 91, the gas jet comprising a gas pressure
drop of less than 5 inches of water.
99. The method of claim 91, wherein separating at least the portion
of the first particulate from the plurality of particulates to form
the separated portion of the first particulate further comprises:
directing the separated portion of the first particulate away from
the cross-flow axis to a surface of a separator conduit; and
directing the separated portion of the first particulate along the
surface for a distance.
100. The method of claim 99, wherein directing the separated
portion of the first particulate along the surface comprises
directing the separated portion of the first particulate
substantially parallel to the flow axis.
101. The method of claim 99, wherein directing the separated
portion of the first particulate along the surface comprises using
the Coand{hacek over (a)} effect.
102. The method of claim 91, further comprising diverting the
separated portion of the first particulate along the surface away
from the surface to a cross-flow output.
103. The method of claim 102, wherein diverting the separated
portion of the first particulate along the surface away from the
surface and through the cross-flow output comprises using the
Coand{hacek over (a)} effect.
104. The method of claim 102, wherein diverting the separated
portion of the first particulate along the surface away from the
surface and through the cross-flow output comprises contacting the
separated portion of the first particulate along the surface with
an entrance vane, the entrance vane being in fluidic communication
with the cross-flow output.
105. The method of claim 91, wherein separating at least the
portion of the first particulate from the plurality of particulates
comprises substantially separating the first particulate from the
plurality of particulates.
106. The method of claim 91, wherein separating at least the
portion of the first particulate from the plurality of particulates
comprises separating at least about 99% by weight of the first
particulate from the plurality of particulates.
107. The method of claim 91, the first particulate comprising a
pyrolysis product.
108. The method of claim 91, the first particulate comprising one
or more of a biomass or a biomass pyrolysis product.
109. The method of claim 91, the first particulate comprising
char.
110. The method of claim 91, the first particulate being
characterized by a first average density in kilograms per cubic
meter of between about 100 and about 2,000.
111. The method of claim 91, the first particulate being
characterized by a first average diameter in millimeters of between
about 0.1 and about 10.
112. The method of claim 91, the first particulate comprising an
average flow rate in kilograms per second of between about 0.0012
and about 0.0023.
113. The method of claim 91, the first particulate being
characterized by a first average density and the plurality of
particulates comprising at least a second particulate characterized
by a second average density greater than the first average
density.
114. The method of claim 113, the second particulate comprising one
or more of a metal, a glass, a ceramic, a mineral, or a polymeric
composite.
115. The method of claim 113, the second particulate comprising one
or more of: steel, stainless steel, cobalt (Co), molybdenum (Mo),
nickel (Ni), titanium (Ti), tungsten (W), zinc (Zn), antimony (Sb),
bismuth (Bi), cerium (Ce), vanadium (V), niobium (Nb), tantalum
(Ta), chromium (Cr), manganese (Mn), rhenium (Re), iron (Fe),
platinum (Pt), iridium (Ir), palladium (Pd), osmium (Os), rhodium
(Rh), ruthenium (Ru), nickel, copper impregnated zinc oxide
(Cu/ZnO), copper impregnated chromium oxide (Cu/Cr), nickel
aluminum oxide (Ni/Al.sub.2O.sub.3), palladium aluminum oxide
(PdAl2O3), cobalt molybdenum (CoMo), nickel molybdenum (NiMo),
nickel molybdenum tungsten (NiMoW), sulfided cobalt molybdenum
(CoMo), sulfided nickel molybdenum (NiMo), or a metal carbide.
116. The method of claim 113, the second average density of the
second particulate in kilograms per cubic meter being between about
3,000 and about 23,000.
117. The method of claim 113, the second average density of the
second particulate divided by the first average density of the
first particulate being a ratio between about 1.5:1 and about
230:1.
118. The method of claim 113, the second particulate being
characterized by a first average diameter in millimeters of between
about 1 and about 10.
119. The method of claim 113, the second particulate comprising a
spherical, rounded or ellipsoid morphology
120. The method of claim 113, the second particulate comprising a
flow rate in kilograms per second of about 0.4 to about 1.4 per
each ton per day of biomass processed.
121. The method of claim 113, the first particulate having a first
terminal velocity and the second particulate having a second
terminal velocity, the first and second particulates being
characterized by a ratio of second terminal velocity to first
terminal velocity of at least about 5:1.
122. The method of claim 113, the first particulate having a first
terminal velocity and the second particulate having a second
terminal velocity, the first and second particulates being
characterized by a ratio of second terminal velocity to first
terminal velocity of at least about 10:1.
123. The method of claim 113, the first particulate having a first
terminal velocity and the second particulate having a second
terminal velocity, the first and second particulates being
characterized by a ratio of second terminal velocity to first
terminal velocity of at least about 20:1.
124. The method of claim 91, further comprising separating at least
a portion of a second particulate in the plurality of particulates
from the first particulate.
125. The method of claim 91, further comprising separating
substantially all of a second particulate in the plurality of
particulates from the first particulate.
126. The method of claim 91, further comprising separating at least
a portion of a second particulate in the plurality of particulates
from the first particulate in a direction substantially aligned
with the flow axis.
127. The method of claim 91, further comprising directing the flow
axis downward at a flow angle.
128. The method of claim 127, the flow angle being less than
90.degree. from vertically downward.
129. The method of claim 127, the flow angle being less than
60.degree. from vertically downward.
130. The method of claim 91, further comprising forming the gas jet
by flowing a gas through a first convergent nozzle comprising a
first nozzle throat.
131. The method of claim 91, a cross section of the first nozzle
throat comprising at least two dissimilar axes.
132. The method of claim 91, the first nozzle throat comprising an
elliptical cross section, a circular cross section, a rectangular
cross section, or a rounded corner rectangular cross section.
133. The method of claim 91, further comprising: adapting the flow
upstream of the gas jet to a first flow diameter; and adapting the
flow downstream of the gas jet to a second flow diameter, the first
flow diameter being greater than the second flow diameter.
134. The method of claim 133, further comprising adapting the flow
between the first flow diameter and the second flow diameter using
a transition between the first flow diameter and the second flow
diameter, the transition being substantially aligned with the
cross-flow angle.
135. The method of claim 134, further comprising adapting the flow
using a transition between the first flow diameter and the second
flow diameter, the transition being substantially perpendicular
with respect to the flow axis.
136. The method of claim 134, further comprising adapting the flow
using a transition between the first flow diameter and the second
flow diameter, the transition extending between at least a portion
of the first flow diameter and at least a portion of the first
nozzle throat.
137. The method of claim 134, at least a portion of the second flow
diameter coinciding with at least a portion of the first nozzle
throat.
138. The method of claim 137, the first nozzle throat being located
at the second flow diameter of the separator conduit.
139. The method of claim 134, forming the gas jet further comprises
flowing the gas through a second nozzle throat upstream of the
first nozzle throat.
140. The method of claim 134, separating at least the portion of
the first particulate from the plurality of particulates further
comprises extending an entrance vane into a portion of the flow
defined by the second flow diameter.
141. The method of claim 140, further comprising extending at least
a portion of the entrance vane into the flow at least partly in an
upstream direction with respect to the flow axis.
142. The method of claim 91, wherein separating at least the
portion of the first particulate from the plurality of particulates
comprises directing the separated portion of the first particulate
away from the flow axis substantially opposite to the gas jet along
the cross-flow axis with respect to the flow axis.
143. The method of claim 91, wherein separating at least the
portion of the first particulate from the plurality of particulates
comprises directing the separated portion of the first particulate
away from the flow axis substantially opposite to the gas jet along
the cross-flow axis with respect to the flow axis.
144. The method of claim 91, wherein separating at least the
portion of the first particulate from the plurality of particulates
further comprises directing a separated portion of the first
particulate away from the flow axis through a third nozzle
throat.
145. The method of claim 144, a cross section of the third nozzle
throat comprising at least two dissimilar axes.
146. The method of claim 144, the third nozzle throat comprising an
elliptical cross section, a circular cross section, a rectangular
cross section, or a rounded corner rectangular cross section.
147. The method of claim 144, wherein separating at least the
portion of the first particulate from the plurality of particulates
further comprises directing the separated portion of the first
particulate away from the third nozzle throat through an elliptical
cross section.
148. The method of claim 144, wherein separating at least the
portion of the first particulate from the plurality of particulates
further comprises directing the separated portion of the first
particulate away from the third nozzle throat through a circular
cross section.
149. The method of claim 144, wherein separating at least the
portion of the first particulate from the plurality of particulates
further comprises directing the separated portion of the first
particulate away from the third nozzle throat via an exit conduit
axis, the exit conduit axis intersecting the flow axis at an exit
angle, the exit angle being greater than 0.degree. and less than
180.degree..
Description
CROSS-REFERENCE TO RELATED APPLICATIONS
[0001] This application claims priority from U.S. Provisional
Patent Application No. 61/826,989, filed on May 23, 2013, which is
incorporated by reference herein in its entirety.
BACKGROUND
[0002] Biomass pyrolysis is conventionally conducted using bubbling
fluid beds, circulating fluid bed transport reactors, rotating cone
reactors, ablative reactors or auger reactors. Fluidized bed
designs such as bubbling fluid bed reactors and circulating fluid
bed reactors may provide high heat transfer rates to the substrate,
e.g., biomass, and these high heat transfer rates may result in
high yield of bio-oil. A disadvantage of fluidized bed systems is
that a significant flow rate of inert gas may be needed, which may
lead to undesirable parasitic losses. Other designs, such as
rotating cone reactors and auger reactors may not require
significant inert gas flow, but mixing between the heat carrier and
biomass may not be as effective as with fluidized beds, which may
lead to lower reaction yields, of bio-oil from bio-mass pyrolysis.
The present application appreciates that biomass pyrolysis may be a
challenging endeavor.
SUMMARY
[0003] In one embodiment, a falling bed reactor is provided. The
falling bed reactor may include a reactor conduit defining a flow
axis. The falling bed reactor may include an inlet operatively
coupled to receive a heat carrier particulate into the reactor
conduit. The falling bed reactor may also include an outlet
operatively coupled to direct the heat carrier particulate out of
the reactor conduit. The falling bed reactor may also include one
or more baffles mounted in the reactor conduit, e.g., a plurality
of baffles.
[0004] In another embodiment, a falling bed reactor is provided.
The falling bed reactor may include a reactor conduit defining a
flow axis. The falling bed reactor may include an inlet operatively
coupled to receive a heat carrier particulate into the reactor
conduit. The falling bed reactor may also include an outlet
operatively coupled to direct the heat carrier particulate out of
the reactor conduit. The falling bed reactor may further include a
pyrolysis substrate inlet operatively coupled to receive a
pyrolysis substrate into the reactor conduit. The falling bed
reactor may include a pyrolysis product outlet operatively coupled
to direct a pyrolysis product out of the reactor conduit. The
falling bed reactor may also include one or more baffles mounted in
the reactor conduit, e.g., a plurality of baffles. Each baffle in
the one or more baffles may include a baffle surface. At least a
portion of each baffle surface may be at an oblique angle with
respect to the flow axis.
[0005] In one embodiment, a pyrolysis system is provided. The
pyrolysis system may include a falling bed reactor and a cross-flow
classifier. The falling bed reactor may include a reactor conduit
defining a flow axis. The falling bed reactor may include an inlet
operatively coupled to receive a heat carrier particulate into the
reactor conduit. The falling bed reactor may also include an outlet
operatively coupled to direct the heat carrier particulate out of
the reactor conduit. The falling bed reactor may further include a
pyrolysis substrate inlet operatively coupled to receive a
pyrolysis substrate into the reactor conduit. The falling bed
reactor may include a pyrolysis product outlet operatively coupled
to direct a pyrolysis product out of the reactor conduit. The
falling bed reactor may also include one or more baffles mounted in
the reactor conduit. Each baffle in the one or more baffles may
include a baffle surface. At least a portion of each baffle surface
may be at an oblique angle with respect to the flow axis.
[0006] The cross-flow classifier may include a separator conduit.
The cross-flow classifier may also include a flow input and a flow
output in fluidic communication with the separator conduit. The
separator conduit may extend between the flow input and the flow
output to define a flow axis along at least a portion of the
separator conduit. The flow input may be located upstream of the
flow output with respect to the flow axis. The cross-flow
classifier may include a cross-flow input and a cross-flow output
in fluidic communication with the separator conduit between the
flow input and the flow output. The cross-flow input may be located
upstream of the cross-flow output with respect to the flow axis.
The cross-flow input may define a cross-flow axis intersecting the
flow axis at a cross-flow angle between about 70.degree. and about
180.degree. with respect to the flow axis. Further with respect to
the pyrolysis system, the outlet of the falling bed reactor may be
operatively coupled to the flow input of the cross-flow classifier.
Also, the flow output of the cross-flow classifier may be
operatively coupled to the inlet of the failing bed reactor.
[0007] In one embodiment, a pyrolysis method is provided. The
pyrolysis method may include feeding a heat carrier to a
gravity-fed baffled conduit. The pyrolysis method may include
feeding a pyrolysis substrate to the gravity-fed baffled conduit
such that the heat carrier and the pyrolysis substrate mix to form
a pyrolysis mixture. The pyrolysis method may include heating the
heat carrier and/or the gravity-fed baffled conduit to pyrolyze the
pyrolysis substrate in the pyrolysis mixture to form a pyrolysis
product mixture. The "gravity-fed baffled conduit" may include, for
example, the falling bed reactor.
BRIEF DESCRIPTION OF THE DRAWINGS
[0008] The accompanying figures, which are incorporated in and
constitute a part of the specification, illustrate example methods
and apparatuses, and are used merely to illustrate example
embodiments.
[0009] FIG. 1 depicts an example falling bed reactor;
[0010] FIG. 2 depicts an example pyrolysis system that includes an
example falling bed reactor and an example cross-flow particle
classifier;
[0011] FIG. 3 is a block diagram of an example cross-flow particle
classifier; and
[0012] FIG. 4 is a flow diagram of an example method for
pyrolysis.
DETAILED DESCRIPTION
[0013] FIG. 1 depicts an example falling bed reactor 100. Falling
bed reactor 100 may include a reactor conduit 102 defining a flow
axis 104. Flow axis 104 may have a downstream end, indicated by the
arrowhead, and an upstream end, indicated by the shaft end of the
arrow. Falling bed reactor 100 may include an inlet 106 operatively
coupled to receive a heat carrier particulate into reactor conduit
102. Falling bed reactor 100 may also include an outlet 108
operatively coupled to direct the heat carrier particulate out of
reactor conduit 102. Falling bed reactor 100 may further include a
pyrolysis substrate inlet 110 operatively coupled to receive a
pyrolysis substrate into reactor conduit 102. Falling bed reactor
100 may include a pyrolysis product outlet 112 operatively coupled
to direct a pyrolysis product out of reactor conduit 102. Falling
bed reactor 100 may also include one or more baffles 114, e.g.; a
plurality of baffles, mounted in reactor conduit 102. Each baffle
in one or more baffles 114 may include a baffle surface 116. At
least a portion of each baffle surface 116 may be at an oblique
angle 118 with respect to flow axis 104.
[0014] As used herein, the "heat carrier" may be a particulate
including one or more of: a metal, a glass, a ceramic, a mineral,
or a polymeric composite. For example, the heat carrier may be
sand. The heat carrier may include a particulate catalyst. For
example, the heat carrier may include a fluid catalytic cracking
(FCC) catalyst. The heat carrier may include a spent particulate
catalyst. For example, the heat carrier may include a spent FCC
catalyst. The heat carrier may be in the form of metal shot, for
example, steel shot. In various embodiments, the heat carrier, when
employed with the cross flow particle classifier, is of a density
effective to provide separation between the heat carrier and the
char to be separated in the cross flow particle classifier.
[0015] As used herein, an "oblique angle" is any angle that is not
an integer multiple of a right angle. For example, an oblique angle
excludes 0.degree., 90.degree., and 180.degree., but includes
angles between 0.degree. and 90.degree., and angles between
90.degree. and 180.degree..
[0016] In various embodiments, falling bed reactor 100 may be
configured to be mounted such that at least a portion of flow axis
104 is parallel or oblique to a vertically downward direction.
Failing bed reactor 100 may be configured to be mounted such that
at least a portion of each baffle surface 116 is at an oblique
angle 118 with respect to the vertically downward direction.
Failing bed reactor 100 may be mounted to orient flow axis 104 in a
substantially vertically downward direction. In this manner,
falling bed reactor 100 may be gravity-fed or gravity operated, at
Feast in part. For example, the pyrolysis substrate may enter
falling bed reactor 100 at pyrolysis substrate inlet 110, and the
heat carrier particulate may enter falling bed reactor 100 at inlet
106. The pyrolysis substrate and the heat carrier particulate may
fall through falling bed reactor 100, and may be intermittently
diverted from flow axis 104 by one or more baffles 114, for
example, as indicated by a path 105.
[0017] In some embodiments, a cross section of reactor conduit 102
may include a shape that may be one of: polygonal, rounded
polygonal, circular, elliptical, or a combination or composite
thereof. A cross section of reactor conduit 102 may include a shape
that may be one of: rectangular, rounded rectangular, circular,
elliptical, or a combination or composite thereof. For example,
reactor conduit 102 may be square in cross section.
[0018] In several embodiments, one or both of inlet 106 and outlet
108 may be substantially parallel with one or both of reactor
conduit 102 and flow axis 104. Inlet 106 may be operatively coupled
to reactor conduit 102 upstream of outlet 108 with respect to flow
axis 104.
[0019] In some embodiments, falling bed reactor 100 may include a
pyrolysis substrate inlet 110 operatively coupled to receive a
pyrolysis substrate into reactor conduit 102. Falling bed reactor
100 may include a pyrolysis product outlet 112 operatively coupled
to direct a pyrolysis product out of reactor conduit 102.
[0020] Pyrolysis substrate inlet 110 may be operatively coupled to
reactor conduit 102 upstream of pyrolysis product outlet 112 with
respect to flow axis 104. Pyrolysis substrate inlet 110 may be
operatively coupled to reactor conduit 102 upstream of pyrolysis
product outlet 112 with respect to flow axis 104. Pyrolysis
substrate inlet 110 may be operatively coupled to reactor conduit
102 at a same level or downstream of pyrolysis product outlet 112
with respect to flow axis 104. Pyrolysis substrate inlet 110 may be
coincident with inlet 106. Pyrolysis product outlet 112 may be
coincident with inlet 106 or outlet 108.
[0021] In various embodiments, the one or more baffles 114 may
extend from an inside wall 130 of the reactor conduit 102 into the
reactor conduit 102. For example, the one or more baffles 114 may
extend from the inside wall 130 to define a cantilevered geometry
in the reactor conduit 102. The one or more baffles 114 may extend
across at least a portion of the reactor conduit 102 between a
first portion of the inside wall 130 and a second portion of the
inside wall 130. Each of the one or more baffles 114 may include a
form of one or more of a rod, a plate, a screen, or a protrusion.
Each of the one or more baffles 114 may include a form of a rod.
The rod may include a cross-sectional geometry that is at least in
part polygonal, rounded polygonal, circular, elliptical, or a
combination or composite thereof.
[0022] In some embodiments, each of the one or more baffles 114 may
include a baffle surface 116. The baffle surface 116 may be
positioned to intersect at least a portion of the reactor conduit
102 with respect to the flow axis 104. At least a portion of the
baffle surface 116 may include a geometry that is one or more of
flat or convex. At least a portion of the baffle surface 116 may be
horizontal with respect to the flow axis 104. At least a portion of
the baffle surface 116 may be at an oblique angle 118 with respect
to the flow axis 104.
[0023] In various embodiments, one or more baffles 114 may be
mounted to place at least the portion of each baffle surface 116 at
oblique angle 118 with respect to flow axis 104 such that one or
more baffles 114 may form a staggered or alternating pattern in
reactor conduit 102. Each baffle in one or more baffles 114 may be
mounted to an inside wall 130 of reactor conduit 102 to define a
free edge 120 of each baffle surface 116 and a mounted edge 122 of
each baffle surface. In some embodiments, one or more baffles 114
may be configured as an alternating sequence of funnels and cones,
the funnels aligned with the flow axis 104 and the cones aligned
antiparallel to the flow axis 104, each of the funnels and cones
may include a free edge 120 at a downstream extremity of each of
the funnels and cones. In some embodiments, the staggered or
alternating pattern of one or more baffles 114 intersecting flow
axis 104 to provide a tortuous flow path through one or more
baffles 114. Each baffle surface 11 in one or more baffles 114 may
be substantially at oblique angle 118 with respect to flow axis
104. For example, oblique angle 118 may be between about 30.degree.
and about 60.degree. with respect to flow axis 104 such that for
each baffle surface 116, a flee edge 120 of baffle surface 116 may
be further downstream along flow axis 104 compared to a mounted
edge 122 of baffle surface 116.
[0024] In several embodiments, falling bed reactor 100 may include
an agitator mechanism 126 configured to agitate at least a portion
of one or more baffles 114 effective to dislodge a particulate on
at least a portion of one or more baffles 114. Falling bed reactor
100 may include a heater 128. Heater 128 may be configured cause
pyrolysis of a substrate in falling bed reactor 100 by heating one
or both of falling bed reactor 100 and a heat carrier to be fed
into falling bed reactor 100.
[0025] FIG. 2 depicts an example pyrolysis system 200. Pyrolysis
system 200 may include falling bed reactor 100 and a cross-flow
classifier 3100. Falling bed reactor 100 may include a reactor
conduit 102 defining flow axis 104. Flow axis 104 may have a
downstream end, indicated by the arrowhead, and an upstream end,
indicated by the shaft end of the arrow. Falling bed reactor 100
may include an inlet 106 operatively coupled to receive a heat
carrier particulate into reactor conduit 102. Falling bed reactor
100 may also include an outlet 108 operatively coupled to direct
the heat carrier particulate out of reactor conduit 102. Falling
bed reactor 100 may further include a pyrolysis substrate inlet 110
operatively coupled to receive a pyrolysis substrate into reactor
conduit 102. Falling bed reactor 100 may include a pyrolysis
product outlet 112 operatively coupled to direct a pyrolysis
product out of reactor conduit 102. Falling bed reactor 100 may
also include one or more baffles 114 mounted in reactor conduit
102. Each baffle in one or more baffles 114 may include a baffle
surface 116. At least a portion of each baffle surface 116 may be
at an oblique angle 118 with respect to flow axis 104.
[0026] Cross-flow classifier 3100 may include a separator conduit
3102. Cross-flow classifier 3100 may also include a flow input 3104
and a flow output 3106 in fluidic communication with separator
conduit 3102. Separator conduit 3102 may extend between flow input
3104 and flow output 3106 to define a flow axis 3108 along least a
portion of separator conduit 3102. Flow input 3104 may be located
upstream of flow output 3106 with respect to flow axis 3108.
Cross-flow classifier 3100 may include a cross-flow input 3114 and
a cross-flow output 3116 in fluidic communication with separator
conduit 3102 between flow input 3104 and flow output 3106.
Cross-flow input 3114 may be located upstream of cross-flow output
3116 with respect to flow axis 3108. Cross-flow input 3114 may
define a cross-flow axis 3118 intersecting flow axis 3108 at a
cross-flow angle 3120 between about 70.degree. and about
180.degree. with respect to flow axis 3108. Further with respect to
pyrolysis system 200, outlet 108 of falling bed reactor 100 may be
operatively coupled to flow input 3104 of cross-flow classifier
3100. Also, flow output 3106 of cross-flow classifier 3100 may be
operatively coupled to inlet 106 of filling bed reactor 100.
[0027] In various embodiments, outlet 108 of falling bed reactor
100 may be operatively coupled to flow input 3104 of cross-flow
classifier 3100 via an auger or conveyor 230. Flow output 3106 of
cross-flow classifier 3100 may be operatively coupled to inlet 106
of falling bed reactor 100 via an auger or conveyor 232.
[0028] In some embodiments, pyrolysis system 200 may include a fine
particulate separator 202. An input 204 of fine particulate
separator 202 may be operatively coupled to pyrolysis product
outlet 112 of falling bed reactor 100. Fine particulate separator
202 may include a particulate outlet 206 and a gas or vapor outlet
208. For example, fine particulate separator 202 may include one or
more of: a settling chamber, a baffle chamber, a cyclonic particle
separator, an electrostatic precipitator, a filter, or a
scrubber
[0029] In several embodiments, pyrolysis system 200 may include a
coarse particulate separator 212. An input 214 of coarse
particulate separator 212 may be operatively coupled to cross-flow
output 3116 of cross-flow classifier 3100. Coarse particulate
separator 212 may include a particulate outlet 216 and a gas outlet
218. For example, coarse particulate separator 212 may include one
or more of: a settling chamber, a baffle chamber, a cyclonic
particle separator, an electrostatic precipitator, a filter, or a
scrubber
[0030] In various embodiments, pyrolysis system 200 may include a
gas recycle conduit 220. Gas recycle conduit 220 may be operatively
coupled to receive recycled gas from gas outlet 218. Gas recycle
conduit 220 may be operatively coupled to direct the recycled gas
to cross-flow input 3114 of cross-flow classifier 3100. In some
embodiments, gas recycle conduit 220 may include a fan 222. Fan 222
may be configured to draw the recycled gas from gas outlet 218 via
gas recycle conduit 220. Fan 222 may be configured to flow the
recycled gas to cross-flow input 3114 of cross-flow classifier 3100
via gas recycle conduit 220.
[0031] In further embodiments, falling bed reactor 100 in pyrolysis
system 200 may include any aspect of falling bed reactor 100
described herein.
[0032] FIGS. 3A and 3B depict aspects of cross-flow classifier 3100
that may be used in example pyrolysis system 200. For example, in
various embodiments, one or both of flow input 3114 and flow output
3116 may be substantially aligned with flow axis 3108 of separator
conduit 3102. In some embodiments, cross-flow input 3114 may be
operatively coupled to separator conduit 3102 substantially
opposite to cross-flow output 3116 with respect to flow axis
3108.
[0033] In some embodiments, cross-flow classifier 3100 may be
mounted such that flow axis 3108 points downward at a flow angle
3110. For example, flow angle 3110 may be less than 90.degree. from
vertically downward. In some embodiments, flow angle 3110 may be
less than 60.degree. from vertically downward.
[0034] As used herein, "downward" means any direction represented
by a vector having a non-zero component parallel with respect to a
local gravitational acceleration direction. As used herein,
"upward" means any direction represented by a vector having a
non-zero component antiparallel with respect to the local
gravitational acceleration direction. As used herein, "vertical"
means parallel or antiparallel with respect to the local
gravitational acceleration direction. "Vertically downward" means
parallel with respect to the local gravitational acceleration
direction, indicated in FIG. 1 by arrow 3101. "Vertically upward"
means antiparallel with respect to the local gravitational
acceleration direction. As used herein, "horizontal" means
perpendicular to the local gravitational acceleration
direction.
[0035] In several embodiments, separator conduit 3102 may include a
first flow diameter 3122 between flow input 3104 and cross-flow
input 3114. Separator conduit 3102 may include a second flow
diameter 3124 downstream of cross-flow input 3114. First flow
diameter 3122 may be greater than second flow diameter 3124.
Separator conduit 3102 may include a transition 3126 between first
flow diameter 3122 and second flow diameter 3124. Transition 3126
may be substantially aligned with cross-flow angle 3120. For
example, transition 3126 may be substantially perpendicular with
respect to flow axis 3108.
[0036] In various embodiments, flow input 3104 may be configured to
accept a plurality of particulates. At least a first particulate in
the plurality of particulates may be characterized by a first
average density. At least a second particulate in the plurality of
particulates may be characterized by a second average density
greater than the first average density. Flow output 3106 may be
configured to convey at least a portion of the first particulate
characterized by the first density out of separator conduit 3102.
Cross-flow output 3116 may be configured to convey at least a
portion of the second particulate characterized by the second
density greater than the first density out of separator conduit
3102.
[0037] As used herein, a "particulate" refers to a plurality,
collection, or distribution of individual particles. The individual
particles in the particulate may have in common one or more
characteristics, such as size, density, material composition, heat
capacity, particle morphology, and the like. The characteristics of
the particles in the particulate may be the same among the
particles, or may be characterized by a distribution. For example,
particles in a particulate may all be made of the same composition,
e.g., a ceramic, a metal, or the like. In another example,
particles in a particulate may be characterized by a distribution
of particle sizes, for example, a Gaussian distribution.
[0038] In some embodiments, cross-flow input 3114 may define a
first convergent nozzle 3132. First convergent nozzle 3132 may
include a first nozzle throat 3134. A cross section of first nozzle
throat 3134 may include at least two dissimilar axes. For example,
first nozzle throat 3134 may include an elliptical cross section, a
circular cross section, a rectangular cross section, a rounded
corner rectangular cross section, a polygonal cross section, a
composite or combination thereof, or the like.
[0039] In several embodiments, the first nozzle throat 3134 may be
operatively coupled to a nozzle exit zone. At least a portion of
the nozzle exit zone may include a transition 3126 between a first
flow diameter 3122 of flow conduit 3108 and first nozzle throat
3134. In some embodiments, at least a portion of the nozzle exit
zone may include a second flow diameter 3124 of separator conduit
3108. Transition 3126 may be located at an upstream side of first
nozzle throat 3134. Second flow diameter 3124 may be located at a
downstream side of first nozzle throat 3134. First nozzle throat
3134 may be located at second flow diameter 3124 of separator
conduit 3108.
[0040] In various embodiments, convergent nozzle 3132 of cross-flow
input 3114 may include a second nozzle throat 3138. First nozzle
throat 3134 may be located at cross-flow input 3114 between second
nozzle throat 3138 and separator conduit 3108. Cross-flow output
3116 may define a second convergent nozzle 3142.
[0041] In some embodiments, second convergent nozzle 3142 may
include a third nozzle throat 3144. A cross section of third nozzle
throat 3144 may include at least two dissimilar axes. For example,
third nozzle throat 3144 may include an elliptical cross section, a
circular cross section, a rectangular cross section, a rounded
corner rectangular cross section, a polygonal cross section, a
composite or combination thereof, or the like. Third nozzle throat
3144 may be operatively coupled to a nozzle entrance zone 3146. At
least a portion of nozzle entrance zone 3146 may include a
transition 3148 between a second flow diameter 3124 of flow conduit
3108 and third nozzle throat 3144. In some embodiments, at least a
portion of nozzle entrance zone 3146 may include an entrance vane
3150. Entrance vane 3150 may extend into separator conduit 3102,
for example, with respect to second flow diameter 3124. At least a
portion of entrance vane 3150 may extend into separator conduit
3102 at least partly in an upstream direction with respect to flow
axis 3108.
[0042] In several embodiments, third nozzle throat 3144 may be
operatively coupled through a nozzle collector zone to an exit
conduit 3154. One or both of the nozzle collector zone and conduit
3154 may include an elliptical cross section. For example, one or
both of the nozzle collector zone and exit conduit 3154 may include
a circular cross section. Third nozzle throat 3144 may be
operatively coupled to an exit conduit 3154. Exit conduit 3154 may
define an exit conduit axis 3156. Exit conduit axis 3156 may
intersect flow axis 3108 at an exit angle 3158. Exit angle 3158 may
be greater than 0' and less than 180.degree.. For example, exit
angle 3158 may be between about 90.degree. and less than
180.degree.. In some embodiments, exit conduit axis 3156 may be
within about 30.degree. of vertical.
[0043] FIG. 4 is a flow diagram describing an example pyrolysis
method 400. Pyrolysis method 400 may include feeding a heat carrier
to a gravity-fed baffled conduit (step 402). Pyrolysis method 400
may include feeding a pyrolysis substrate to the gravity-fed
baffled conduit such that the heat carrier and the pyrolysis
substrate mix to form a pyrolysis mixture (step 404). Pyrolysis
method 400 may include heating the heat carrier and/or the
gravity-fed baffled conduit to pyrolyze the pyrolysis substrate in
the pyrolysis mixture to form a pyrolysis product mixture (step
406). The gravity-fed baffled conduit may include, for example, the
falling bed reactor 100 described herein.
[0044] In various embodiments of pyrolysis method 400, the
pyrolysis product mixture may include a gas or vapor pyrolysis
product and a fine char pyrolysis product. The method may include
directing the gas or vapor pyrolysis product and the fine char
pyrolysis product out of the gravity-fed baffled conduit. The
pyrolysis product mixture may include the heat carrier and a coarse
char pyrolysis product. The method may further include directing
the heat carrier and the coarse char pyrolysis product out of the
gravity-fed baffled conduit. In some examples, the method may
include directing the gas or vapor pyrolysis product and the fine
char pyrolysis product out of the gravity-fed baffled conduit at
the same level as the heat carrier and the coarse char pyrolysis
product. The method may include directing the gas or vapor
pyrolysis product and the fine char pyrolysis product out of the
gravity-fed baffled conduit upstream compared to the heat carrier
and the coarse char pyrolysis product. The method may include
directing the gas or vapor pyrolysis product and the fine char
pyrolysis product out of the gravity-fed baffled conduit downstream
compared to the heat carrier and the coarse char pyrolysis
product
[0045] In some embodiments, the pyrolysis product mixture may
include the heat carrier and a coarse char pyrolysis product. The
method may include directing the heat carrier and the coarse char
pyrolysis product out of the gravity-fed baffled conduit.
[0046] In several embodiments, feeding the heat carrier to the
gravity-fed baffled conduit may include feeding the heat carrier
and the pyrolysis substrate to the same level in the gravity-fed
baffled conduit. Feeding the heat carrier to the gravity-fed
baffled conduit may include feeding the heat carrier to the
gravity-fed baffled conduit upstream of the pyrolysis substrate.
Feeding the heat carrier to the gravity-fed baffled conduit may
include feeding the heat carrier to the gravity-fed baffled conduit
downstream of the pyrolysis substrate.
[0047] In various embodiments, the pyrolysis product mixture may
include a gas or vapor pyrolysis product and a fine char pyrolysis
product. The method may also include directing the gas or vapor
pyrolysis product and the fine char pyrolysis product out of the
gravity-fed baffled conduit. The method may also include separating
the gas or vapor pyrolysis product from the fine char pyrolysis
product. The pyrolysis product mixture may include the heat carrier
and a coarse char pyrolysis product. The method may include
directing the heat carrier and the coarse char pyrolysis product
out of the gravity-fed baffled conduit. The method may also include
separating the heat carrier from the coarse char pyrolysis product.
The method may include recycling the heat carrier to form a
recycled heat carrier. The method may also include feeding the
recycled heat carrier to the gravity-fed baffled conduit.
[0048] In several embodiments of the method, separating the heat
carrier from the coarse char pyrolysis product may include
directing a flow comprising a plurality of particulates along a
flow axis. The method may also include separating at least a
portion of a first particulate from the plurality of particulates
to form a separated portion of the first particulate by directing a
gas jet along a cross-flow axis, the cross-flow axis intersecting
the flow axis at a cross-flow angle, the cross-flow angle being
between about 70.degree. and about 180.degree.. As used herein, the
plurality of particulates may include the heat carrier and the
coarse char pyrolysis product. As used herein, the first
particulate may include the coarse char pyrolysis product
[0049] In various embodiments, the gas jet may include a gas
temperature of between about 300.degree. C. and about 700.degree.
C. The gas temperature may be a temperature in .degree. C. of about
300, 320, 340, 360, 380, 400, 420, 440, 460, 480, 500, 520, 540,
560, 580, 600, 620, 640, 660, 680, or 700, or any range between any
two of the preceding temperature values.
[0050] In some embodiments, the gas jet may include a gas density
(in kilograms per cubic meter) of between about 0.4 and about 1.4.
The gas density may have a value (in kilograms per cubic meter) of
about 0.4, 0.5, 0.6, 0.7, 0.8, 0.9, 1, 1.1, 1.2, 1.3, or 1.4, or
any range between any two of the preceding density values.
[0051] In several embodiments, the gas jet may include a gas
viscosity (in kilograms per meter-second) of between about
1.times.10.sup.-6 and about 1.times.10.sup.-4. For example, the gas
viscosity may have a value in 10.sup.-5 kilograms per meter-second
of about 0.1, 0.2, 0.3, 0.4, 0.5, 0.6, 0.7, 0.8, 0.9, 1, 1.2, 1.3,
1.4, 1.5, 1.6, 1.7, 1.8, 1.9, 2, 2.2, 2.4, 2.6, 2.8, 3, 3.25, 3.5,
3.75, 4, 4.5, 5, 5.5, 6, 6.5, 7, 7.5, 8, 8.5, 9, 9.5, or 10, or any
range between any two of the preceding gas viscosity values.
[0052] In various embodiments, the gas jet may include a gas flow
rate of less than 25 cubic feet per minute. The gas jet may include
a gas pressure drop of less than 5 inches of for example, about 1.5
inches of water or less.
[0053] In several embodiments of method 400, separating at least
the portion of the first particulate from the plurality of
particulates to form the separated portion of the first particulate
further may include directing the separated portion of the first
particulate away from the cross-flow axis to a surface of a
separator conduit. Method 400 may also include directing the
separated portion of the first particulate along the surface for a
distance. Directing the separated portion of the first particulate
along the surface may include directing the separated portion of
the first particulate substantially parallel to the first
directional flow axis. Directing the separated portion of the first
particulate along the surface may include using the Coand{hacek
over (a)} effect. Some embodiments may include diverting the
separated portion of the first particulate along the surface away
from the surface to a cross-flow output. Diverting the separated
portion of the first particulate along the surface away from the
surface and through the cross-flow output may include using the
Coand{hacek over (a)} effect. Diverting the separated portion of
the first particulate along the surface away from the surface and
through the cross-flow output may include contacting the separated
portion of the first particulate along the surface with an entrance
vane. The entrance vane may be in fluidic communication with the
cross-flow output.
[0054] In various embodiments of method 400, separating at least
the portion of the first particulate from the plurality of
particulates may include substantially separating the first
particulate from the plurality of particulates. Separating at least
the portion of the first particulate from the plurality of
particulates may include separating at least about 90%, 95%, 97%,
98%, 99%, 99.1%, 99.2%, 993%, 99.4%, 99.5%, 99.6%, 99.7%, 99.8%,
99.9%, 99.95%, 99.99%, 99.995%, or 99.999% by weight of the first
particulate from the plurality of particulates. For example,
separating at least the portion of the first particulate from the
plurality of particulates may include separating at least about 99%
by weight of the first particulate from the plurality of
particulates.
[0055] In some embodiments, the first particulate may include one
or more of a biomass or a pyrolysis product, for example, a biomass
pyrolysis product. For example, the first particulate may include
char. The first particulate may comprise a first average density
(in kilograms per cubic meter) of between about 100 and about
2,000. For example, the first average density (in kilograms per
cubic meter) may be about 100, 200, 300, 400, 500, 600, 700, 800,
900, 1000, 1100, 1200, 1300, 1400, 1500, 1600, 1700, 1800, 1900, or
2000, or between any two of the preceding density values. For
example, the first average density may be about 374 kilograms per
cubic meter.
[0056] In several embodiments, the first particulate may be
characterized by a first average diameter (in millimeters) of
between about 0.1 and about 10. For example, the first average
diameter (in millimeters) may be about 0.1, 0.2, 0.3, 0.4, 0.5,
0.6, 0.7, 0.8, 0.9, 1, 1.2, 1.4, 1.6, 1.8, 7, 2.25, 2.5, 2.75, 3,
3.25, 3.5, 3.75, or 4, or between any two of the preceding average
diameter values.
[0057] In various embodiments, the first particulate may include an
average flow rate (in kilograms per second) of between about 0.0012
and about 0.0023. For example, the average flow rate (in kilograms
per second) may be about 0.0012, 0.0013, 0.0014, 0.0015, 0.0016,
0.0017, 0.0018, 0.0019, 0.0020, 0.0021, 0.0022, or 0.0023, or
between any two of the preceding flow rate values.
[0058] In some embodiments, the first particulate may include a
first average density and the plurality of particulates may include
at least a second particulate. The second particulate may be
characterized by a second average density greater than the first
average density. The second particulate may be, for example, a heat
carrier suitable for use in an auger pyrolyzer. The second
particulate may include one or more of a metal, a glass, a ceramic,
a mineral, or a polymeric composite. For example, the second
particulate may include one or more of: steel, stainless steel,
cobalt (Co), molybdenum (Mo), nickel (Ni), titanium (Ti), tungsten
(W), zinc (Zn), antimony (Sb), bismuth (Bi), cerium (Ce), vanadium
(V), niobium (Nb), tantalum (Ta), chromium (Cr), manganese (Mn),
rhenium (Re), iron (Fe), platinum (Pt), iridium (Ir), palladium
(Pd), osmium (Os), rhodium (Rh), ruthenium (Ru), nickel, copper
impregnated zinc oxide (Cu/ZnO), copper impregnated chromium oxide
(Cu/Cr), nickel aluminum oxide (Ni/Al.sub.2O.sub.3), palladium
aluminum oxide (PdAl.sub.2O.sub.3), cobalt molybdenum (CoMo),
nickel molybdenum (NiMo), nickel molybdenum tungsten (NiMoW),
sulfided cobalt molybdenum (CoMo), sulfided nickel molybdenum
(NiMo), or a metal carbide.
[0059] In several embodiments, the second average density of the
second particulate (in kilograms per cubic meter) may be between
about 3,000 and about 23,000, for example, about 3,000, 4,000,
5,000, 6,000, 7,000, 8,000, 9,000, 10,000, 11,000, 12,000, 13,000,
14,000, 15,000, 16,000, 17,000, 18,000, 19,000, 20,000, 21,000,
22,000, or 23,000, or between about any two of the preceding
density values. For example, the second particulate may be steel or
stainless steel at a density of about 7,500 kilograms per cubic
meter.
[0060] In various embodiments, the second average density of the
second particulate divided by the first average density of the
first particulate may be a ratio between about 1.5:1 and about
230:1. For example, the ratio may be about 1.5:1, 2:1, 5:1, 10:1,
15:1, 20:1, 25:1, 50:1, 75:1, 100:1, 125:1, 150:1, 175:1, 200:1,
225:1, 230:1, or a range between about any two of the preceding
ratios.
[0061] In some embodiments, the second particulate may be
characterized by a first average diameter (in millimeters) of
between about 0.1 and about 25, for example, about 0.1, 0.2, 0.3,
0.4, 0.5, 0.6, 0.7, 0.8, 0.9, 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11,
12, 13, 14, 15, 16, 17, 18, 19, 20, 21, 22, 23, 24, 25, or a range
between about any two of the preceding average diameter values, for
example, between about 1 mm and about 10 mm.
[0062] In some embodiments, the second particulate may include a
spherical, rounded, or ellipsoid morphology. In some embodiments,
the second particulate may include a substantially spherical
morphology.
[0063] In several embodiments, the second participate may include a
flow rate (in kilograms per second per each ton per day of biomass
processed) of about 0.4 to about 1.4, for example, about 0.4, 0.5,
0.6, 0.7, 0.8, 0.9, 1, 1.1, 1.2, 1.3, 1.4, or a range between any
two of the preceding flow rates.
[0064] In some embodiments, the first particulate may be
characterized by a first terminal velocity and the second
particulate may be characterized by a second terminal velocity. The
first and second particulates may be characterized by a ratio of
the second terminal velocity to the first terminal velocity of at
least about 5:1, 10:1, 15:1, 20:1, 25:1, 30:1, or 35:1.
[0065] In various embodiments, method 400 may also include
separating at least a portion of a second particulate in the
plurality of particulates from the first particulate. For example,
method 400 may include separating substantially all of a second
particulate in the plurality of particulates from the first
particulate. Method 400 may include separating at least a portion
of a second particulate in the plurality of particulates from the
first particulate in a direction substantially aligned with the
first directional flow axis. The method may also include directing
the flow axis downward at a flow angle. The flow angle may be less
than 90.degree. from vertically downward. The flow angle may be
less than 60.degree. from vertically downward.
[0066] In several embodiments, method 400 may include forming the
gas jet by flowing a gas through a first convergent nozzle. The
first convergent nozzle may include a first nozzle throat. A cross
section of the first nozzle throat may include at least two
dissimilar axes. For example, the first nozzle throat may include
an elliptical cross section, a circular cross section, a
rectangular cross section, a rounded corner rectangular cross
section, a polygonal cross section, a composite or combination
thereof, or the like.
[0067] In various embodiments, method 400 may also include adapting
the flow upstream of the gas jet to a first flow diameter and
adapting the flow downstream of the gas jet to a second flow
diameter. The first flow diameter may be greater than the second
flow diameter. The method may also include adapting the flow
between the first flow diameter and the second flow diameter using
a transition between the first flow diameter and the second flow
diameter. The transition may be substantially aligned with the
cross-flow angle. For example, the transition may be substantially
perpendicular with respect to the flow axis. The transition may
extend between at least a portion of the first flow diameter and at
least a portion of the first nozzle throat. At least a portion of
the second flow diameter may coincide with at least a portion of
the first nozzle throat. The first nozzle throat may be located at
the second flow diameter of the separator conduit.
[0068] In some embodiments, forming the gas jet may also include
flowing the gas through a second nozzle throat upstream of the
first nozzle throat.
[0069] In several embodiments, separating at least the portion of
the first particulate from the plurality of particulates may also
include extending an entrance vane into a portion of the flow
defined by the second flow diameter. The method may include
extending at least a portion of the entrance vane into the flow at
least partly in an upstream direction with respect to the first
directional flow axis.
[0070] In various embodiments of method 400, separating at least
the portion of the first particulate from the plurality of
particulates may include directing the separated portion of the
first particulate away from the flow axis. The method may include
directing the separated portion of the first particulate away from
the flow axis substantially opposite to the gas jet along the
cross-flow axis with respect to the first directional flow
axis.
[0071] In several embodiments, method 400 may include directing a
separated portion of the first, articulate away from the flow axis
through a third nozzle throat. A cross section of the third nozzle
throat may include at least two dissimilar axes. For example, the
third nozzle throat pray include an elliptical cross section, a
circular cross section, a rectangular cross section, a rounded
corner rectangular cross section, a polygonal cross section, a
composite or combination thereof, or the like. Separating at least
the portion of the first particulate from the plurality of
particulates may also include directing the separated portion of
the first particulate away from the third nozzle throat through an
elliptical cross section. For example, the method may include
directing the separated portion of the first particulate away from
the third nozzle throat through a circular cross section.
[0072] In some embodiments, separating at least the portion of the
first particulate from the plurality of particulates further may
include directing the separated portion of the first particulate
away from the third nozzle throat via an exit conduit axis. The
exit conduit axis may intersect the flow axis at an angle. The
angle may be greater than 0.degree. and less than 180.degree.. For
example, the angle may be between about 90.degree. and less than
180.degree.. In some examples, the conduit axis may be within about
30.degree. of vertical.
Prophetic Example
[0073] Heated spherical steel shot, about 1 mm in diameter, may be
added via inlet 106 into reactor conduit 102. Ground particulate
bio-mass (e.g., a mixture of corn stover and wood particulate) may
be added via pyrolysis substrate inlet 110 into reactor conduit
102. The reactor conduit 102 and the steel shot may be heated to a
desired pyrolysis temperature, e.g., 500.degree. C. The heated
steel shot and the bio-mass may fall through the one or inure
baffles 114 mounted in reactor conduit 102. The heated steel shot
and the bio-mass may mix, and the bio-mass may pyrolyze to form a
pyrolysis mixture including gas or vapor of bio-oil, bio-char, and
the heated steel shot. A mixture of fine bio-char and the gas or
vapor of bio-oil may be collected at pyrolysis product outlet 112.
A mixture of coarse bio-char and the steel shot may be collected at
outlet 108. The falling bed reactor described in this Example may
exhibit effective mixing between the steel shot heat carrier and
the bio-mass, similar to the mixing observed in fluidized bed
reactors. The falling bed reactor described in this Example may
also operate without needing inert gas, similar to the operation of
auger reactors.
[0074] To the extent that the term "includes" or "including" is
used in the specification or the claims, it is intended to be
inclusive in a manner similar to the term "comprising" as that term
is interpreted when employed as a transitional word in a claim.
Furthermore, to the extent that the term "or" is employed (e.g., A
or B) it is intended to mean "A or B or both." When the applicants
intend to indicate "only A or B but not both" then the term "only A
or B but not both" will be employed. Thus, use of the term "or"
herein is the inclusive, and not the exclusive use, See Bryan A.
Garner, A Dictionary of Modern Legal Usage 624 (2d. Ed. 1995).
Also, to the extent that the terms "in" or "into" are used in the
specification or the claims, it is intended to additionally mean
"on" or "onto." To the extent that the term "selectively" is used
in the specification or the claims, it is intended to refer to a
condition of a component wherein a user of the apparatus may
activate or deactivate the feature or function of the component as
is necessary or desired in use of the apparatus. To the extent that
the terms "coupled" or "operatively connected" are used in the
specification or the claims, it is intended to mean that the
identified components are connected in a way to perform a
designated function. To the extent that the term "substantially" is
used in the specification or the claims, it is intended to mean
that the identified components have the relation or qualities
indicated with degree of error as would be acceptable in the
subject industry.
[0075] As used in the specification and the claims, the singular
forms "a," "an," and "the" include the plural unless the singular
is expressly specified. For example, reference to "a compound" may
include a mixture of two or more compounds, as well as a single
compound.
[0076] As used herein, the term "about" in conjunction with a
number is intended to include .+-.10% of the number. In other
words, "about 10" may mean from 9 to 11.
[0077] As used herein, the terms "optional" and "optionally" mean
that the subsequently described circumstance may or may not occur,
so that the description includes instances where the circumstance
occurs and instances where it does not.
[0078] In addition, where features or aspects of the disclosure are
described in terms of Markush groups, those skilled in the art will
recognize that the disclosure is also thereby described in terms of
any individual member or subgroup of members of the Markush group.
As will be understood by one skilled in the art, for any and all
purposes, such as in terms of providing a written description, all
ranges disclosed herein also encompass any and all possible
sub-ranges and combinations of sub-ranges thereof. Any listed range
can be easily recognized as sufficiently describing and enabling
the same range being broken down into at least equal halves,
thirds, quarters, fifths, tenths, and the like. As a non-limiting
example, each range discussed herein can be readily broken down
into a lower third, middle third and upper third, and the like. As
will also be understood by one skilled in the art all language such
as "up to," "at least," "greater than," "less than," include the
number recited and refer to ranges which can be subsequently broken
down into sub-ranges as discussed above. Finally, as will be
understood by one skilled in the art, a range includes each
individual member. For example, a group having 1-3 cells refers to
groups having 1, 2, or 3 cells. Similarly, a group having 1-5 cells
refers to groups having 1, 2, 3, 4, or 5 cells, and so forth. While
various aspects and embodiments have been disclosed herein, other
aspects and embodiments will be apparent to those skilled in the
art.
[0079] As stated above, while the present application has been
illustrated by the description of embodiments thereof, and while
the embodiments have been described in considerable detail, it is
not the intention of the applicants to restrict or in any way limit
the scope of the appended claims to such detail. Additional
advantages and modifications will readily appear to those skilled
in the art, having the benefit of the present application.
Therefore, the application, in its broader aspects, is not limited
to the specific details, illustrative examples shown, or any
apparatus referred to. Departures may be made from such details,
examples, and apparatuses without departing from the spirit or
scope of the general inventive concept.
[0080] The various aspects and embodiments disclosed herein are for
purposes of illustration and are not intended to be limiting, with
the true scope and spirit being indicated by the following
claims.
* * * * *