CN106147833A - A kind of high activity Multifunctional heavy method for transformation and device - Google Patents
A kind of high activity Multifunctional heavy method for transformation and device Download PDFInfo
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- CN106147833A CN106147833A CN201510182518.6A CN201510182518A CN106147833A CN 106147833 A CN106147833 A CN 106147833A CN 201510182518 A CN201510182518 A CN 201510182518A CN 106147833 A CN106147833 A CN 106147833A
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Abstract
A kind of high activity Multifunctional heavy method for transformation, belongs to petrochemical industry, utilization of resources equipment technical field, is used for reducing coke, dry gas yied, improves light oil yield, processing coked waxy oil, producing more propylene.Enter with regenerative agent including mink cell focus, mix and contact, cracking reaction and rear conversion reaction occur, it is characterized in that: design millisecond residual oil cracking reactor and high intensity mixing conversion reactor, two reactors in series also feed low temperature high activity catalyst betwixt；Improve millisecond residual oil cracking reactor oil ratio, charging mixing temperature promotes mink cell focus in millisecond reactor very short time cracking, avoids overcracking to improve yield of light oil, improve mixing conversion reactor catalyst activity and response strength simultaneously, promote rear portion conversion reaction Olefin decrease or cracking wax tailings or producing more propylene.For RFCC, heavy oil alkene, it is particularly suited for existing apparatus transformation.
Description
Technical field
The invention belongs to petrochemical industry, utilization of resources equipment technical field, particularly to a kind of high activity Multifunctional heavy conversion side
Method and device.
Background technology
Conventional catalytic cracking device riser length 35～45 meters, oil gas response time 3～4 seconds.Modern molecular sieve catalyst is lived
Property is the highest, and macromole crack materials generally can become in very short time light diesel fuel, gasoline component, if the response time is long, and can
Further for light diesel fuel component cracking is generated LPG, dry gas and coke, especially dry gas, the too high meeting of coke yield directly result in gently
Matter oil yield reduces, and reduction dry gas, coke yield are one of process optimization ultimate aim.For current catalytic cracking unit by
Determine that obviously there are overcracking phenomenon in riser length 35～45 meters, oil gas response time 3～4 seconds in structure of reactor pattern,
If being intended to reduce dry gas and coke yield, raising yield of light oil further, catalytic cracking unit structure of reactor pattern need to be improved.
Foreign study and develop millisecond catalytic cracking technique before several years, it is important to develop response time extremely short millisecond reactor and
Supporting settler and regenerator, can reduce overcracking reaction to greatest extent, reduce dry gas yied and coke, raising light oil
Yield, and built demonstration plant.Domestic also carrying out millisecond catalytic cracking research, day by day become due to catalytically cracked stock weight,
The reasons such as social desirability improves constantly, through engineering approaches show that millisecond catalytic cracking technology is the most not mature enough, can not meet current social and want
Ask.The content of olefin in gasoline produced such as millisecond catalytic cracking technique is higher than Conventional catalytic cracking, and current social requires gasoline alkene
Hydrocarbon content is low；And for example millisecond catalytic cracking recycle oil cracking capability is not strong, and current petroleum chemical enterprise raw oil becomes weight day by day, needs
Want higher recycle oil cracking capability；The most currently also has the social desirability such as processing coked waxy oil, producing more propylene.
Summary of the invention
It is an object of the invention to provide a kind of high activity Multifunctional heavy method for transformation, make mink cell focus at high temperature, high solvent-oil ratio, pre-
Phase very short time cracked, reduces overcracking to greatest extent, reduces dry gas and coke yield, raising yield of light oil, simultaneously
Realize rear portion high activity, high intensity reaction environment effectively facilitates rear portion conversion reaction Olefin decrease or cracking wax tailings or producing more propylene,
Adapt to current multiple social desirability.
The present invention solves the method that its technical problem used: include that mink cell focus enters with regenerative agent, mixes and contact, occur
Cracking reaction and rear conversion reaction, is characterized in that: design millisecond residual oil cracking reactor and high intensity mixing conversion reactor, two is anti-
Answer device series connection and feed low temperature high activity catalyst betwixt；Improve millisecond residual oil cracking reactor oil ratio, charging mixing temperature
Promote mink cell focus in millisecond reactor very short time cracking, avoid overcracking to improve yield of light oil, improve mixing simultaneously and convert
Reactor catalyst activity and response strength, promote rear portion conversion reaction Olefin decrease or cracking wax tailings or producing more propylene.
Further, high intensity mixing conversion reactor is made up of gas-solid mixing facility, one section or two sections of fast beds or conveying bed.
Further, it is also possible on millisecond residual oil cracking reactor top, wax tailings adsorption section or terminator Injection Section are set.
A kind of high activity Multifunctional heavy reforming unit, including regenerator, reacting-settler, stripping section, fast point, outlet,
Regenerative agent pipe, external warmer, cooler, pre-riser, feed zone, millisecond oil pipe are anti-, linkage section, mixing conversion reaction
Device, low temperature high activity catalyst pipe, the anti-front end of millisecond oil pipe is connected with feed zone, pre-riser, and rear end is connected with linkage section；
Mixing conversion reactor lower end is connected with linkage section upper end, and upper end is connected with outlet lower end, and outlet is from settler bottom cone
Or stripping section top stretches into and upwardly extends and be connected with dividing soon；Regenerative agent pipe lower end is connected with pre-riser, feed zone, upper end with
Regenerator connects；Low temperature high activity catalyst pipe lower end is connected with linkage section or mixing conversion reactor bottom, upper end and cooler
Or external warmer connects.
Further, millisecond oil pipe is counter is that level millisecond oil pipe is anti-, or vertical millisecond oil pipe is anti-, or inverted L-shaped millisecond
Oil pipe is anti-.
Further, mixing conversion reactor includes three-dimensional mixing distributor, one section or two sections of fast beds or transport bed reactor.
Further, it is also possible on millisecond oil pipe anti-top, wax tailings adsorption section or terminator Injection Section are set.
Further, it is also possible to outlet stretches into from side, settler middle and upper part and is connected with dividing soon, or stretches into upwards bottom stripping section
Extend and be connected with fast point.
Further, it is also possible in external warmer, cooler bottom, stripping facility is set.
Innovative point of the present invention and good effect:
Innovative point of the present invention is: design millisecond residual oil cracking reactor and high intensity mixing conversion reactor, two reactors in series are also
Feed low temperature high activity catalyst betwixt；Improve millisecond residual oil cracking reactor oil ratio, charging mixing temperature promotes mink cell focus
In millisecond reactor very short time cracking, avoid overcracking to improve yield of light oil, improve mixing conversion reactor catalysis simultaneously
Agent activity and response strength, promote rear portion conversion reaction Olefin decrease or cracking wax tailings or producing more propylene.
Good effect of the present invention is: 1, realize mink cell focus in high temperature, high solvent-oil ratio, expection very short time cracked, to greatest extent
Reducing overcracking, dry gas yied can reduce by 30%～40%, coke yield can reduce by 0.5～1 percentage point, yield of light oil can
Improve 1～3 percentage points；2, realize rear portion high activity, high intensity reaction environment effectively facilitates rear portion conversion reaction, reduces gasoline
Olefin(e) centent or cracking wax tailings or producing more propylene；3, existing apparatus transformation it is particularly suited for.
Accompanying drawing explanation
Fig. 1 is a kind of high activity Multifunctional heavy method for transformation and device schematic diagram.
1-pushes up rotation, and 2-divides soon, 3-settler, 5-fast bed, 6A-solid mixing distributor, 7-linkage section, 8-cooler, 9-
Outlet, 10-thermocatalyst pipe, 11-low temperature high activity agent pipe, 13A-bed regenerator, 16-regenerative agent pipe, 17-regenerates sliding
Valve, 18-feed nozzle, 19-feed zone, 20-millisecond oil pipe is anti-.
Fig. 2 is another kind of high activity Multifunctional heavy method for transformation and device schematic diagram.
1-pushes up rotation, and 2-divides soon, 3-settler, 4-stripping section, and 5-two-stage nitration conveying bed, 6-mono-section carries bed, 7-linkage section, 8-
Cooler, 9-outlet, 10-thermocatalyst pipe, 11-low temperature high activity agent pipe, 12-pre-riser, 13D-fast bed regenerator,
14-wax tailings adsorption section, 15-wax tailings nozzle, 16-regenerative agent pipe, 17-regenerates guiding valve, 18-feed nozzle, and 19-enters
Material section, 20-millisecond oil pipe is anti-.
Fig. 3 is another kind of high activity Multifunctional heavy method for transformation and device schematic diagram.
1-pushes up rotation, and 2-divides soon, 3-settler, 4-stripping section, and 5-two-stage nitration conveying bed, 6-mono-section carries bed, 7-linkage section, 8-
Cooler, 9-outlet, 10-thermocatalyst pipe, 11-low temperature high activity agent pipe, 12-pre-riser, 13B-the first regenerator,
13C-Second reactivator, 16-regenerative agent pipe, 17-regenerates guiding valve, 18-feed nozzle, 19-feed zone, and 20-millisecond oil pipe is anti-.
Fig. 4 is another kind of high activity Multifunctional heavy method for transformation and device schematic diagram.
1-pushes up rotation, and 2-divides soon, 3-settler, and 5-two-stage nitration conveying bed, 6-mono-section carries bed, 7-linkage section, 8-cooler, 9-
Outlet, 10-thermocatalyst pipe, 11-low temperature high activity agent pipe, 12-pre-riser, 13B-the first regenerator, 13C-second is again
Raw device, 16-regenerative agent pipe, 17-main regeneration guiding valve, 18-feed nozzle, 19-feed zone, 20-millisecond oil pipe is anti-.
Fig. 5 is another kind of high activity Multifunctional heavy method for transformation and device schematic diagram.
1-pushes up rotation, and 2-divides soon, 3-settler, 4-stripping section, and 5-two-stage nitration conveying bed, 6-mono-section carries bed, 7-linkage section, 8-
Cooler, 9-outlet, 10-thermocatalyst pipe, 11-low temperature high activity agent pipe, 12-pre-riser, 13B-the first regenerator,
13C-Second reactivator, 14-wax tailings adsorption section, 15-wax tailings nozzle, 16-regenerative agent pipe, 17-regenerates guiding valve, 18-
Feed nozzle, 19-feed zone, 20-millisecond oil pipe is anti-.
Detailed description of the invention
Seeing Fig. 1, anti-20 front ends of millisecond oil pipe are connected with feed zone 19, and rear end is connected with linkage section 7, regenerative agent pipe 16 times
Regeneration guiding valve 17 is installed in portion, and lower end is connected with feed zone 19, upper end is connected with bed regenerator 13A, and feed zone 19 is installed into
Material nozzle 18.The internally installed three-dimensional mixing distributor 6A of fast bed 5, its lower end is connected with linkage section 7 upper end, upper end and outlet
Pipe 9 lower end connects, and outlet 9 top is stretched into internal and fast point 2 in the middle part of settler 3 and is connected, and fast point 2 is connected with top rotation 1.
Cooler 8 top is connected with bed regenerator 13A through thermocatalyst pipe 10, and bottom is through low temperature high activity agent pipe 11 and linkage section
7 connect.
Seeing Fig. 2, anti-20 lower ends of millisecond oil pipe are connected with feed zone 19, upper end is connected with wax tailings adsorption section 14, charging
Section 19 is provided with feed nozzle 18 and is connected with pre-riser 12, wax tailings adsorption section 14 be provided with wax tailings nozzle 15 and with
Linkage section 7 connects.Two-stage nitration conveying one section, bed 5 lower end conveying bed 6 is connected with linkage section 7 upper end, outlet 9 lower end and two
Section conveying bed 5 upper end connects, and outlet 9 top is bored section bottom settler 3 and stretched into inside and upwardly extend and divide 2 to be connected soon.
Regeneration guiding valve 17 is installed in regenerative agent pipe 16 bottom, and lower end is connected with pre-riser 12, and upper end is connected with fast bed regenerator 13D.
Cooler 8 bottom is connected with linkage section 7 through low temperature high activity agent pipe 11, and top is through thermocatalyst pipe 10 and fast bed regenerator
13D connects.
Seeing Fig. 3, Fig. 4, anti-20 lower ends of millisecond oil pipe are connected with pre-riser 12 through feed zone 19, upper end and linkage section 7
Connecting, feed zone 19 is provided with feed nozzle 18.Two-stage nitration conveying one section, bed 5 lower end conveying bed 6 is connected with linkage section 7 upper end,
Outlet 9 lower end is connected with two-stage nitration conveying bed 5 upper end, and Fig. 3 outlet 9 top is bored section bottom settler 3 and stretched into inside (figure
4 stretch into inside in the middle part of settler 3) it is connected with fast point 2.Regenerative agent pipe 16 bottom install regeneration guiding valve 17, lower end with carry in advance
Rising device 12 to connect, upper end is connected with Second reactivator 13C.Cooler 8 bottom is through low temperature high activity agent pipe 11 and linkage section 7
Connecting, top is connected with Second reactivator 13C through thermocatalyst pipe 10.
Seeing Fig. 5, anti-20 lower ends of millisecond oil pipe are connected with feed zone 19, upper end is connected with wax tailings adsorption section 14, charging
Section 19 is provided with feed nozzle 18 and is connected with pre-riser 12, wax tailings adsorption section 14 be provided with wax tailings nozzle 15 and with
Linkage section 7 connects.Two-stage nitration conveying one section, bed 5 lower end conveying bed 6 is connected with linkage section 7 upper end, outlet 9 lower end and two
Section conveying bed 5 upper end connects, and outlet 9 top is stretched into inside bottom stripping section 4 and upwardly extended and divide 2 to be connected soon.Regeneration
Regeneration guiding valve 17 is installed in agent pipe 16 bottom, and lower end is connected with pre-riser 12, and upper end is connected with Second reactivator 13C.Cooling
Device 8 bottom is connected with linkage section 7 through low temperature high activity agent pipe 11, and top is through thermocatalyst pipe 10 and the first regenerator 13B even
Connect.
Seeing Fig. 1,680～720 DEG C of high temperature regeneration agent draw to enter through regenerative agent pipe 16, regeneration guiding valve 17 from bed regenerator 13A
Entering feed zone 19, mink cell focus enters after feed nozzle 18 is atomized, and contacts mixing, vaporization entrance millisecond weight with high temperature regeneration agent
There are catalytic cracking reaction, control reaction temperature 500～550 DEG C in oil pipe anti-20, is melted into light oil in very short time implosion and keeps away
Exempt from overcracking, generate a small amount of dry gas and coke, reaction oil gas and spent agent simultaneously and exit into from anti-20 rear ends of millisecond oil pipe
Linkage section 7.680～720 DEG C of high temperature regeneration agent are drawn from bed regenerator 13A and are entered cooler 8 through thermocatalyst pipe 10, temperature
Degree drops to 300～550 DEG C and is transported to linkage section 7 through low temperature high activity agent pipe 11.In linkage section 7, two strands of catalyst and oil gas converge
Close and control temperature 470～550 DEG C, flow up and enter fast bed 5, two strands of catalyst and oil gas through three-dimensional mixing distributor 6A and mix
Closing and uniformly carry out rear portion conversion reaction Olefin decrease or cracking wax tailings or producing more propylene, final reaction oil gas and spent agent are from outlet
Pipe 9 is discharged, and after fast point 2 and top rotation 1 gas solid separation, oil gas discharges system, and spent agent removes bed regenerator 13A through stripping section.
Good effect is: dry gas yied reduces by 30%～40%, and coke yield reduces by 0.5～1 percentage point, and yield of light oil improves 1～3
Percentage point, content of olefin in gasoline 20%～30%；Or producing more propylene, productivity of propylene 10%～20%.
Seeing Fig. 2,680～720 DEG C of high temperature regeneration agent are drawn from fast bed regenerator 13D top and are slided through regenerative agent pipe 16, regeneration
Valve 17 enters pre-riser 12, boosted entrance feed zone 19, and mink cell focus enters and high temperature regeneration after feed nozzle 18 is atomized
Agent contacts mixing, vaporization, enters millisecond oil pipe anti-20 and cracking reactions, control reaction temperature 500～550 DEG C occur, make weight
Matter oil, at very short time implosion chemical conversion light oil avoid overcracking, generates a small amount of dry gas and coke simultaneously, reaction oil gas and treating
Raw agent exits into wax tailings adsorption section 14 from upper end, and wax tailings enters after wax tailings nozzle 15 is atomized, and makes coking
Nitride is also adsorbed on spent agent by wax oil vaporization, and reaction oil gas and spent agent continue up and flow into linkage section 7.680～
720 DEG C of high temperature regeneration agent are drawn from fast bed regenerator 13D top and are entered cooler 8 through thermocatalyst pipe 10, and temperature drops to
300～550 DEG C are transported to linkage section 7 through low temperature high activity agent pipe 11.Two strands of catalyst and oil gas merging control in linkage section 7
470～550 DEG C, continue up the blended allotter of flowing and enter one section of conveying bed 6, two-stage nitration conveying bed 5, two strands of catalyst and oil
Gas mix homogeneously carry out rear portion conversion reaction Olefin decrease or cracking wax tailings or producing more propylene, final reaction oil gas and spent agent from
Outlet 9 is discharged, and after fast point 2 and top rotation 1 gas solid separation, oil gas discharges system, and spent agent removes fast bed through stripping section 4
Regenerator 13D bottom.Good effect is: 1, can processing coked waxy oil；2, dry gas yied reduces by 30%～40%, coke yield
Reducing by 0.5～1 percentage point, yield of light oil improves 1～3 percentage points, content of olefin in gasoline 20%～30%；Or producing more propylene,
Productivity of propylene 10%～20%.
Seeing Fig. 3, Fig. 4,680～720 DEG C of high temperature regeneration agent are drawn from Second reactivator 13C and are slided through regenerative agent pipe 16, regeneration
Valve 17 enters pre-riser 12, boosted entrance feed zone 19, and mink cell focus enters and high temperature regeneration after feed nozzle 18 is atomized
Agent contacts mixing, vaporization, enters millisecond oil pipe anti-20 and cracking reactions occur, and control reaction temperature 500～550 DEG C, in pole
Short time implosion chemical conversion light oil also avoids overcracking, generates a small amount of dry gas and coke, reaction oil gas and spent agent from milli simultaneously
Second anti-20 rear ends of oil pipe exit into linkage section 7.680～720 DEG C of high temperature regeneration agent are drawn from Second reactivator 13C and are urged through heat
Agent pipe 10 enters cooler 8, and temperature drops to 300～550 DEG C and is transported to linkage section 7 through low temperature high activity agent pipe 11.Even
Two strands of catalyst and oil gas merging control temperature 470～550 DEG C in the section of connecing 7, flow up blended allotter and enter one section
Conveying bed 6, two-stage nitration conveying bed 5, two strands of catalyst and air-fuel mixture uniformly carry out rear portion conversion reaction Olefin decrease or cracking coking wax
Oil or producing more propylene, final reaction oil gas and spent agent are discharged from outlet 9, after fast point 2 and top rotation 1 gas solid separation, and oil
Gas discharges system, and spent agent removes the first regenerator 13B through stripping section 4.Good effect is: dry gas yied reduces by 30%～40%,
Coke yield reduces by 0.5～1 percentage point, and yield of light oil improves 1～3 percentage points, content of olefin in gasoline 20%～30%；Or it is many
Produce propylene, productivity of propylene 10%～20%.
Seeing Fig. 5,680～720 DEG C of high temperature regeneration agent draw to enter through regenerative agent pipe 16, regeneration guiding valve 17 from Second reactivator 13C
Entering pre-riser 12, boosted entrance feed zone 19, mink cell focus enters after feed nozzle 18 is atomized and contacts with high temperature regeneration agent
Mixing, vaporization, enter millisecond oil pipe anti-20 and cracking reaction, control reaction temperature 500～550 DEG C occur, make mink cell focus exist
Very short time implosion chemical conversion light oil also avoids overcracking, generate simultaneously a small amount of dry gas and coke, reaction oil gas and spent agent from
Upper end exits into wax tailings adsorption section 14, and wax tailings enters after wax tailings nozzle 15 is atomized, and makes wax tailings vapour
Changing and adsorbed on spent agent by nitride, reaction oil gas and spent agent continue up and flow into linkage section 7.680～720 DEG C
High temperature regeneration agent is drawn from the first regenerator 13B and is entered cooler 8 through thermocatalyst pipe 10, and temperature drops to 300～550 DEG C through low
Temperature high reactivity reagent pipe 11 is transported to linkage section 7.Two strands of catalyst and oil gas merging control 470～550 DEG C in linkage section 7, continue
The continuous entrance of blended allotter one section of conveying bed 6, two-stage nitration of flowing up carries bed 5, and two strands of catalyst and air-fuel mixture are uniformly carried out
Rear portion conversion reaction Olefin decrease or cracking wax tailings or producing more propylene, final reaction oil gas and spent agent are discharged from outlet 9,
After fast point 2 and top rotation 1 gas solid separation, oil gas discharges system, and spent agent removes the first regenerator 13B through stripping section 4.Actively
Effect is: 1, can processing coked waxy oil；2, dry gas yied reduces by 30%～40%, and coke yield reduces by 0.5～1 percentage point,
Yield of light oil improves 1～3 percentage points, content of olefin in gasoline 20%～30%；Or producing more propylene, productivity of propylene 10%～20%.
Claims (9)
1. a high activity Multifunctional heavy method for transformation, enters with regenerative agent including mink cell focus, mixes and contact, cracking occurs
Reaction and rear conversion reaction, is characterized in that: design millisecond residual oil cracking reactor and high intensity mixing conversion reactor, two reactors
Series connection also feeds low temperature high activity catalyst betwixt；Improve millisecond residual oil cracking reactor oil ratio, charging mixing temperature promotes
Mink cell focus millisecond reactor very short time cracking, avoid overcracking improve yield of light oil, simultaneously improve mixing conversion reaction
Device catalyst activity and response strength, promote rear portion conversion reaction Olefin decrease or cracking wax tailings or producing more propylene.
High activity Multifunctional heavy method for transformation the most according to claim 1, is characterized in that: high intensity mixing conversion reaction
Device is made up of gas-solid mixing facility, one section or two sections of fast beds or conveying bed.
High activity Multifunctional heavy method for transformation the most according to claim 1, is characterized in that: can also split at millisecond heavy oil
Change reactor top and wax tailings adsorption section or terminator Injection Section are set.
4. a high activity Multifunctional heavy reforming unit, including regenerator, reacting-settler, stripping section, fast point, outlet,
Regenerative agent pipe, external warmer, cooler, pre-riser, feed zone, millisecond oil pipe are anti-, linkage section, mixing conversion reaction
Device, low temperature high activity catalyst pipe, the anti-front end of millisecond oil pipe is connected with feed zone, pre-riser, and rear end is connected with linkage section；
Mixing conversion reactor lower end is connected with linkage section upper end, and upper end is connected with outlet lower end, and outlet is from settler bottom cone
Or stripping section top stretches into and upwardly extends and be connected with dividing soon；Regenerative agent pipe lower end is connected with pre-riser, feed zone, upper end with
Regenerator connects；Low temperature high activity catalyst pipe lower end is connected with linkage section or mixing conversion reactor bottom, upper end and cooler
Or external warmer connects.
High activity Multifunctional heavy reforming unit the most according to claim 4, is characterized in that: millisecond oil pipe is counter is level
Millisecond oil pipe is anti-, or vertical millisecond oil pipe is anti-, or inverted L-shaped millisecond oil pipe is anti-.
High activity Multifunctional heavy reforming unit the most according to claim 4, is characterized in that: mixing conversion reactor includes
Three-dimensional mixing distributor, one section or two sections of fast beds or transport bed reactor.
High activity Multifunctional heavy reforming unit the most according to claim 4, is characterized in that: can also be at millisecond oil pipe
Anti-top arranges wax tailings adsorption section or terminator Injection Section.
High activity Multifunctional heavy reforming unit the most according to claim 4, is characterized in that: can be with outlet from sedimentation
Side, device middle and upper part is stretched into and is connected with dividing soon, or stretches into upwardly extend bottom stripping section and be connected with dividing soon.
High activity Multifunctional heavy reforming unit the most according to claim 4, is characterized in that: can also external warmer,
Cooler bottom arranges stripping facility.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108300508A (en) * | 2018-04-17 | 2018-07-20 | 中国石油大学(华东) | Heavy oil millisecond is classified gas phase catalysis and cracks producing light olefins coupling device |
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2015
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108300508A (en) * | 2018-04-17 | 2018-07-20 | 中国石油大学(华东) | Heavy oil millisecond is classified gas phase catalysis and cracks producing light olefins coupling device |
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Application publication date: 20161123 |