CN105087048B - A kind of method of heavy naphtha molecular sieve dehydration - Google Patents
A kind of method of heavy naphtha molecular sieve dehydration Download PDFInfo
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- CN105087048B CN105087048B CN201410219049.6A CN201410219049A CN105087048B CN 105087048 B CN105087048 B CN 105087048B CN 201410219049 A CN201410219049 A CN 201410219049A CN 105087048 B CN105087048 B CN 105087048B
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Abstract
The invention discloses a kind of method of heavy naphtha molecular sieve dehydration, including absorption, release recovery and regeneration step, molecular sieve water separation tower (1) is set, and (3) (2), two molecular sieve water separation towers series connection adsorption dewaterings, another unload and pushes back and regenerate, 3A molecular sieves and 4A molecules sieve classification are loaded in molecular sieve water separation tower, when the logistics water content of series connection first contact raw molecule sieve dehydrating tower outlet is more than 5 μ g/g, being cut out carries out release recovery and regeneration, the molecular sieve water separation tower of former second contact raw material becomes first molecular sieve water separation tower of contact raw material, standby molecular sieve water separation tower turns into second molecular sieve water separation tower of contact raw material, dehydrating effect, material loss rate and energy consumption are small.
Description
Technical field
The present invention relates to refine hydrocarbon ils with solid absorption in the absence of hydrogen, more particularly to one kind is hydrocracked weight
The method of naphtha molecular sieve dehydration.
Background technology
One of flow, its major product are stripped using water vapour more than hydrocracking unit fractionating column in refining chemical enterprise at present
The unavoidable band water of heavy naphtha is hydrocracked, general water content is 30~100 μ g/g.With the progress of society, high-knock rating gasoline
Demand with aromatic hydrocarbons further increases, and due to being hydrocracked heavy naphtha low-sulfur, low nitrogen and Gao Fangqian, is hydrocracked heavy naphtha
It is the important source material of catalytic reforming unit, and can be fed directly as catalytic reforming unit.But such as catalytic reforming unit charging
The too high chlorine that can be washed off on reforming catalyst of water content, makes the acid function of catalyst weaken and activity decrease, high temperature water high
The aggregation of platinum crystal grain on reforming catalyst can be accelerated, making the metal function of catalyst reduces.The water of catalytic reforming unit charging contains
Amount control is less than 5 × 10-6Mass content, therefore be hydrocracked before heavy naphtha enters catalytic reforming unit and need at dehydration
Reason.
Molecular sieve is a kind of alumino-silicate, the skeleton structure for constituting spaciousness is mainly connected by oxygen bridge by sial, in structure
In have the uniform duct in many apertures and the very big hole of marshalling, internal surface area.The ion in addition with relatively low containing electricity price
The water of the larger metal ion of radius and compound state.Because hydrone continuously loses after the heating, but crystal framework structure is not
Become, form many size identical cavitys, cavity there are many diameter identical micropores to be connected again, the material smaller than channel diameter
Molecular Adsorption, so that the molecule of different size shape is separated, rises in cavity inside, and the molecular repulsion bigger than duct outside
To the effect of screening molecule, thus referred to as molecular sieve.
For the operating characteristics for obtaining and life-span as long as possible, must be regenerated after molecular sieve adsorption saturation.Industrially
Usually heated with preheated regeneration gas, purging molecule is sieved to 200~315 DEG C, and takes away the adsorbate being desorbed.
According to the molecular structure and polarity and the difference of hydrone that are hydrocracked each component in heavy naphtha, it is possible to use 3A
Or 4A molecular sieves are to being hydrocracked heavy naphtha dehydration.
Molecular sieve is dehydrated for light hydrocarbon component, and particularly gas dehydration has been known technology, molecular sieve hydro carbons liquid
The phase dehydration such as pure component application such as propylene, butylene is more universal, and molecular sieve dehydration brings material loss and regenerating molecular sieve ring
The energy consumption of section, attracts attention less.
Light hydrocarbon component Liquid-Phase Molecular Sieve is dehydrated, and inert gas such as nitrogen is used regenerating medium more, and the consumption of nitrogen accounts for liquid
Phase molecule sieve dewatering unit energy consumption more than 70%, substantial amounts of regeneration gas enters factory's hydro carbons blowdown system and also factory can be produced not
Profit influence.
《Modern chemical industry》, 2003,23 (12), 38-40, using C4+ mixed light-hydrocarbon liquid-phase dehydration technologies to natural gas processing
Device carries out technological transformation, discloses using the adsorption tower that 4A molecular sieves are filled with 3, two series connection, and 1 standby to be taken off
Water, C4+ mixed light-hydrocarbons water content is less than 10 μ g/g after taking off, and the background of this article is Natural Gas Enterprises, and regeneration gas is dry gas, for refining
Changing enterprise does not have generality.
《Petrochemical industry is designed》, 2011,28 (1), 6-9, heavy naphtha product dehydration project study, disclose and use molecule
Sieve drying chamber 2, online switching.Heavy naphtha product water content is less than 5 μ g/g mass contents, and this article regeneration gas is nitrogen, not
Consider regeneration gas circulation process, instantaneous nitrogen consumption is larger during regeneration, has considerable influence to enterprise.
The content of the invention
It is 30~100 μ g/g by water content it is an object of the invention to provide a kind of method of heavy naphtha molecular sieve dehydration
Heavy naphtha carries out molecular sieve dehydration into water content less than 5 μ g/g mass, and dehydration is entered in 3A and 4A classification filling molecular sieve towers
OK, by setting pressure release recvery facility flow, setting regeneration gas circulation process, ensureing to be hydrocracked heavy naphtha dehydration indexes
On the premise of, realization is hydrocracked the material consumption of heavy naphtha molecular sieve dehydration and energy optimization.
A kind of method of heavy naphtha molecular sieve dehydration, comprises the following steps：
1) adsorb：Raw material sequentially enters molecular sieve water separation tower 1 and molecular sieve water separation tower 2 and carries out molecular sieve dehydration, after dehydration
Heavy naphtha go out device as product, when the logistics water content of the outlet of molecular sieve water separation tower 1 is more than 5 μ g/g, cut out molecular sieve
Dehydrating tower 1, into step 2), raw material sequentially enters molecular sieve water separation tower 2 and molecular sieve water separation tower 3 and carries out molecular sieve dehydration, when
Molecular sieve water separation tower 2 outlet logistics water content be more than 5 μ g/g when, molecular sieve water separation tower 2 is cut out, into step 2), raw material according to
Secondary entrance molecular sieve water separation tower 3 and molecular sieve water separation tower 1 carry out molecular sieve dehydration, when the logistics of the outlet of molecular sieve water separation tower 3 contains
When water is more than 5 μ g/g, molecular sieve water separation tower 3 is cut out, into step 2)；
2) release is reclaimed：Step 1) molecular sieve water separation tower 1,2 or 3 that cuts out opens the discharge of molecular sieve dehydration bottom of towe and lets out
Pressure valve and the pressure release atmospheric valve on the top of molecular sieve water separation tower 1,2 or 3, pressure release recycling can is drained into by the raw material in molecular sieve water separation tower
8, when molecular sieve water separation tower is with pressure release 8 pressure balance of recycling can, molecular sieve water separation tower pressure is down to close to blowdown system pressure, is closed
Discharging decompressing valve 16 and pressure release atmospheric valve 17 are closed, pressure release is completed, and molecular sieve water separation tower enters step 3), the original in pressure release recycling can
Material mixes through pump 9 with raw material 14；
3) regenerate：Regeneration gas is introduced to step 2) molecular sieve water separation tower 1,2 or 3 after pressure release, open regeneration gas heating
Device 4, regeneration gas heat exchanger 12, regeneration gas air cooler 5, regeneration gas water knockout drum 6 and regeneration gas blower fan 7, progressively heat regeneration gas
To 230~280 DEG C, after maintaining 24~36 hours, progressively lower the temperature, close regeneration hot-air heater 4, switch to cold blowing, regeneration gas wind
Machine 7 exports regeneration gas through re-generatively cooled device 10 and regeneration gas dehydrating tower 11,40 are down into molecular sieve water separation tower 1,2 or 3~
45 DEG C, close regeneration gas blower fan 7, molecular sieve water separation tower 1,2 or 3 regeneration endings, repeat step 1).
The 3A and 4A classification filling molecular sieve towers, 4A molecular sieves, top filling 3A are loaded in molecular sieve water separation tower bottom
Molecular sieve, top 3A and bottom 4A filling ratios are 2~4: 6~8.
Described heavy naphtha is to be hydrocracked heavy naphtha.
Described pressure release is reclaimed, and after molecular sieve water separation tower water suction saturation cuts out, opens relief valve 16 and pressure release atmospheric valve
17, during the raw material in molecular sieve water separation tower drained into pressure release recycling can 8, when molecular sieve water separation tower 1,2 or 3 and pressure release recycling can 8
During pressure balance, relief valve 16 and pressure release atmospheric valve 17 are closed, the raw material in recycling can 8 mixes through pump 9 with raw material 14.
Described regeneration step, 230~280 DEG C of regeneration gas temperature maintains the temperature after 24~36 hours, progressively lowers the temperature,
Regeneration hot-air heater 4 is closed, cold blowing is switched to, regeneration gas blower fan 7 exports regeneration gas and is dehydrated through re-generatively cooled device 10 and regeneration gas
Tower 11,40~45 DEG C are down into molecular sieve water separation tower 1,2 or 3, close regeneration gas blower fan 7.
The molecular sieve water separation tower for cutting out enters reproducer, slowly opens the discharging decompressing line of molecular sieve dehydration bottom of towe, together
When slowly open the pressure release drop out line of molecular sieve dehydration tower top, heavy naphtha pressure release will be hydrocracked and drains into pressure release recycling can, when
When molecular sieve water separation tower 1,2 or 3 and pressure release 8 pressure balance of recycling can, molecular sieve water separation tower 1,2 or 3 pressure are down to close
Blowdown system pressure, closes discharging decompressing valve 16 and pressure release atmospheric valve 17, and pressure release is completed.
After the completion of pressure release, regeneration gas is introduced, open regeneration hot-air heater and regeneration gas heat exchanger, regeneration gas air cooler, again
Angry water knockout drum, regeneration gas blower fan etc., realize that regeneration gas is circulated, and regeneration gas is progressively heated to 230~280 DEG C, electric heater
Outlet temperature is kept for 230~280 DEG C, after 24~36 hours, by certain rate of temperature fall, after stopping regeneration hot-air heater, and regeneration gas
Cold blowing flow is switched to, after regeneration gas fan outlet regeneration gas is through re-generatively cooled device and regeneration gas dehydrating tower, to molecular sieve water separation tower
Cold blowing, cold blowing to molecular sieve water separation tower is down to 40~45 DEG C, stops regeneration gas blower fan, and molecular sieve water separation tower cuts out regeneration gas recycle stream
Journey.
Had the beneficial effect that with a kind of method of heavy naphtha molecular sieve dehydration of prior art：
1) 3A molecular sieves and 4A molecular sieves are classified filling in heavy naphtha molecular sieve water separation tower, improve the same of dewatering efficiency
When ensure molecular sieve dehydrating effect；
2) independent pressure release recvery facility is set, C-4-fraction yield is improved, material loss is greatly reduced, material loss rate is small
In 0.01% mass percent, the operating cost of Liquid-Phase Molecular Sieve dewatering unit is advantageously reduced；
3) regeneration gas circulation process is set, the consumption of nitrogen is on the one hand greatly reduced, be conducive to the production safety of factory, together
When avoid a large amount of inert gases from entering blowdown system, on the other hand reduce the energy consumption of Molecular sieve dehydration units.
Brief description of the drawings
Fig. 1：It is a kind of heavy naphtha molecular sieve dehydration process flow diagram in ward.
Wherein：
1. molecular sieve water separation tower, 2. molecular sieve water separation tower, 3. molecular sieve water separation tower, 4. regenerates hot-air heater, 5. regeneration gas
Air cooler, 6. regeneration gas water knockout drum, 7. regeneration gas blower fan, 8. pressure release recycling can, 9. pump, 10. regenerates Gas Cooler, 11. regeneration
Qi exhaustion water tower, 12. regeneration gas heat exchangers, 13. compensation regeneration gas, 14. raw materials, 15. products, 16. discharging decompressing valves, 17. pressure releases
Atmospheric valve.
Specific embodiment
The invention will be further described below in conjunction with the accompanying drawings：
It is two series connection in normal operating using three molecular sieve water separation tower adsorption-regenerations, one standby.Grasped in series connection
One online micro-moisture analyzer is set on the outlet official road of 1# molecular sieve water separation towers 1 of work, when detecting 1# molecular sieve water separation towers 1
When the water content of outlet streams is more than 5 μ g/g, 1# molecular sieve water separation towers 1 are cut out, be changed into 3# molecular sieve water separation towers 3 and enter regeneration journey
Sequence, the 2# molecular sieve water separation towers 2 for originally operating are switched to 1# molecular sieve water separation towers 1.Standby molecular sieve water separation tower switches to 2# molecules
Sieve dehydrating tower 2.
The 3# molecular sieve water separation towers 3 for cutting out enter reproducer, slowly open the discharging decompressing at the bottom of 3# molecular sieve water separation towers 3
Line, while slowly opening the pressure release drop out line on the top of 3# molecular sieve water separation towers 3, will be hydrocracked heavy naphtha pressure release and drains into pressure release time
Closed cans 8, when 3# molecular sieve water separation towers 3 and pressure release 8 pressure balance of recycling can, molecular sieve water separation tower pressure is down to close to emptying and is
System pressure, closes discharging decompressing valve 16 and pressure release atmospheric valve 17, and pressure release is completed.Heavy naphtha is hydrocracked in pressure release recycling can
Boosted through pump 9, return is hydrocracked heavy naphtha raw material and is dehydrated again.
After the completion of pressure release, regeneration gas is introduced, open regeneration hot-air heater 4, while opening regeneration gas heat exchanger 12, regeneration gas
Air cooler 5, regeneration gas water knockout drum 6, regeneration gas blower fan 7 etc., realize that regeneration gas is circulated.By certain heating rate, by nitrogen plus
To 230~280 DEG C, regeneration hot-air heater 4 outlet temperature is kept for 230~280 DEG C to heat, after 24~36 hours, by certain cooling
Speed, after stopping regeneration hot-air heater 4, regeneration gas is switched to cold blowing flow, and regeneration gas blower fan 7 exports regeneration gas through re-generatively cooled device 10
After regeneration gas dehydrating tower 11, to the cold blowing of 3# molecular sieve water separation towers 3, cold blowing to 3# molecular sieve water separation towers 3 is down to 40~45 DEG C, stops
Regeneration gas blower fan 7,3# molecular sieve water separation towers 3 cut out regeneration gas circulation process.
After the completion of 3# molecular sieve water separation towers 3 regenerate.Through the bottom topping up stop valve topping up of 3# molecular sieve water separation towers 3, slowly open
Topping up stop valve, by the topping up of 3# molecular sieve water separation towers 3 to operating pressure, closes stop valve.3# molecular sieve water separation towers 3 are to standby shape
State.Whole reproducer is completed.
Independent pressure release recvery facility is set, and raising is hydrocracked heavy naphtha yield, material loss is greatly reduced, material is damaged
Consumption rate is less than 0.01% mass percent.
Regeneration gas circulation process is set, the consumption of nitrogen is on the one hand greatly reduced, be conducive to the production safety of factory, while
Avoid a large amount of inert gases from entering blowdown system, on the other hand reduce the energy consumption of Molecular sieve dehydration units.
Embodiment 1
It is hydrocracked heavy naphtha feedstock property and is shown in Table 1.Treating capacity is 120000kg/h, and operating flexibility is 60~110%,
Operation temperature：40 DEG C, operating pressure：1.0MPa(G).
Table 1 is hydrocracked heavy naphtha feedstock property
| Project | Bit indicator |
| Boiling range | DEG C 80~180 |
| Sulfur content (mass content) | |
| Water content (mass content) | |
| Density (20 DEG C) | |
| Viscosity | mPa.s0.28 |
Molecular sieve water separation tower middle and upper part 3A and bottom 4A filling ratios are 2: 8.The effective adsorption capacity of 3A molecular sieves takes 5%
Mass percent, the effective adsorption capacity of 4A molecular sieves takes 6% mass percent, and molecular sieve water separation tower filling ratio of height to diameter is 4: 1,
Calculated by single column switching in 7 days, molecular sieve water separation tower internal diameter is 2.5m, and molecular sieve water separation tower filling height is 10.0m.
It is two series connection in normal operating using three molecular sieve water separation tower adsorption-regenerations, one standby.Grasped in series connection
One online micro-moisture analyzer is set on the outlet official road of 1# molecular sieve water separation towers 1 of work, when detecting 1# molecular sieve water separation towers 1
When the water content of outlet streams is more than 5 μ g/g, 1# molecular sieve water separation towers 1 are cut out, be changed into 3# molecular sieve water separation towers 3 and enter regeneration journey
Sequence, the 2# molecular sieve water separation towers 2 for originally operating are switched to 1# molecular sieve water separation towers 1.Standby molecular sieve water separation tower switches to 2# molecules
Sieve dehydrating tower 2.
The 3# molecular sieve water separation towers 3 for cutting out enter reproducer, slowly open the discharging decompressing at the bottom of 3# molecular sieve water separation towers 3
Line, while slowly opening the pressure release drop out line on the top of 3# molecular sieve water separation towers 3, will be hydrocracked heavy naphtha pressure release and drains into pressure release time
Closed cans 8, when 3# molecular sieve water separation towers 3 and pressure release 8 pressure balance of recycling can, molecular sieve water separation tower pressure is down to close to emptying and is
During system pressure, pressure release is completed.The heavy naphtha that is hydrocracked in pressure release recycling can boosts through pump 9, returns and is hydrocracked heavy naphtha
Raw material is dehydrated again.
After the completion of pressure release, regeneration gas is introduced, open regeneration hot-air heater 4, while opening regeneration gas heat exchanger 12, regeneration gas
Air cooler 5, regeneration gas water knockout drum 6, regeneration gas blower fan 7 etc., realize that regeneration gas is circulated, and regeneration gas internal circulating load presses adsorption bed volume
Air speed 200h-1Design.By certain heating rate, nitrogen is heated to 270 DEG C, regeneration hot-air heater 4 outlet temperature keeps 270
DEG C, after 30 hours, by certain rate of temperature fall, after stopping regeneration hot-air heater 4, regeneration gas is switched to cold blowing flow, regeneration gas blower fan 7
After outlet regeneration gas is through re-generatively cooled device 10 and regeneration gas dehydrating tower 11, to the cold blowing of 3# molecular sieve water separation towers 3, cold blowing to 3# molecules
Sieve dehydrating tower 3 is down to 40~45 DEG C, stops regeneration gas blower fan 7, and 3# molecular sieve water separation towers 3 cut out regeneration gas circulation process.
After the completion of 3# molecular sieve water separation towers 3 regenerate.Through the bottom topping up stop valve topping up of 3# molecular sieve water separation towers 3, slowly open
Topping up stop valve, by the topping up of 3# molecular sieve water separation towers 3 to operating pressure, closes stop valve.3# molecular sieve water separation towers 3 are to standby shape
State.Whole reproducer is completed.
Independent pressure release recvery facility is set, and raising is hydrocracked heavy naphtha yield, material loss is greatly reduced, material is damaged
Consumption rate is 0.008% mass percent.
Regeneration gas circulation process is set, the consumption of nitrogen is on the one hand greatly reduced, be conducive to the production safety of factory, while
Avoid a large amount of inert gases from entering blowdown system, on the other hand reduce the energy consumption of Molecular sieve dehydration units.With regeneration gas once
By process CIMS, the energy consumption reduction by 30% of Molecular sieve dehydration units.
Embodiment 2
It is hydrocracked heavy naphtha feedstock property and is shown in Table 2.Treating capacity is 150000kg/h, and operating flexibility is 60~110%,
Operation temperature：40 DEG C, operating pressure：1.0MPa(G).
Table 2 is hydrocracked heavy naphtha feedstock property
| Title | Unit | Index |
| Boiling range | ℃ | 65-165 |
| Sulfur content (mass content) | 0.5 | |
| Water content (mass content) | 30 | |
| Density (20 DEG C) | 760 | |
| Viscosity | mPa.s | 0.26 |
Molecular sieve water separation tower middle and upper part 3A and bottom 4A filling ratios are 4: 6.The effective adsorption capacity of 3A molecular sieves takes 5%
Mass percent, the effective adsorption capacity of 4A molecular sieves takes 6% mass percent, and molecular sieve water separation tower filling ratio of height to diameter is 4: 1,
Calculated by single column switching in 7 days, molecular sieve water separation tower internal diameter is 2.0m, and molecular sieve water separation tower filling height is 8.0m.
It is two series connection in normal operating using three molecular sieve water separation tower adsorption-regenerations, one standby.Grasped in series connection
One online micro-moisture analyzer is set on the outlet official road of 1# molecular sieve water separation towers 1 of work, when detecting 1# molecular sieve water separation towers 1
When the water content of outlet streams is more than 5 μ g/g, 1# molecular sieve water separation towers 1 are cut out, be changed into 3# molecular sieve water separation towers 3 and enter regeneration journey
Sequence, the 2# molecular sieve water separation towers 2 for originally operating are switched to 1# molecular sieve water separation towers 1.Standby molecular sieve water separation tower switches to 2# molecules
Sieve dehydrating tower 2.
The 3# molecular sieve water separation towers 3 for cutting out enter reproducer, slowly open the discharging decompressing at the bottom of 3# molecular sieve water separation towers 3
Line, while slowly opening the pressure release drop out line on the top of 3# molecular sieve water separation towers 3, will be hydrocracked heavy naphtha pressure release and drains into pressure release time
Closed cans 8, when 3# molecular sieve water separation towers 3 and pressure release 8 pressure balance of recycling can, molecular sieve water separation tower pressure is down to close to emptying and is
During system pressure, pressure release is completed.The heavy naphtha that is hydrocracked in pressure release recycling can boosts through pump 9, returns and is hydrocracked heavy naphtha
Raw material is dehydrated again.
After the completion of pressure release, regeneration gas is introduced, open regeneration hot-air heater 4, while opening regeneration gas heat exchanger 12, regeneration gas
Air cooler 5, regeneration gas water knockout drum 6, regeneration gas blower fan 7 etc., realize that regeneration gas is circulated, and regeneration gas internal circulating load presses adsorption bed volume
Air speed 200h-1Design.By certain heating rate, nitrogen is heated to 260 DEG C, regeneration hot-air heater 4 outlet temperature keeps 260
DEG C, after 24 hours, by certain rate of temperature fall, after stopping regeneration hot-air heater 4, regeneration gas is switched to cold blowing flow, regeneration gas blower fan 7
After outlet regeneration gas is through re-generatively cooled device 10 and regeneration gas dehydrating tower 11, to the cold blowing of 3# molecular sieve water separation towers 3, cold blowing to 3# molecules
Sieve dehydrating tower 3 is down to 40~45 DEG C, stops regeneration gas blower fan 7, and 3# molecular sieve water separation towers 3 cut out regeneration gas circulation process.
After the completion of 3# molecular sieve water separation towers 3 regenerate.Through the bottom topping up stop valve topping up of 3# molecular sieve water separation towers 3, slowly open
Topping up stop valve, by the topping up of 3# molecular sieve water separation towers 3 to operating pressure, closes stop valve.3# molecular sieve water separation towers 3 are to standby shape
State.Whole reproducer is completed.
Independent pressure release recvery facility is set, and raising is hydrocracked heavy naphtha yield, material loss is greatly reduced, material is damaged
Consumption rate is 0.009% mass percent.
Regeneration gas circulation process is set, the consumption of nitrogen is on the one hand greatly reduced, be conducive to the production safety of factory, while
Avoid a large amount of inert gases from entering blowdown system, on the other hand reduce the energy consumption of Molecular sieve dehydration units.With regeneration gas once
By process CIMS, the energy consumption reduction by 30% of Molecular sieve dehydration units.
Embodiment 3
It is hydrocracked heavy naphtha feedstock property and is shown in Table 3.Treating capacity is 150000kg/h, and operating flexibility is 60~110%,
Operation temperature：40 DEG C, operating pressure：1.0MPa(G).
Table 3 is hydrocracked heavy naphtha feedstock property
| Title | Unit | Index |
| Boiling range | ℃ | 80-170 |
| Sulfur content (mass content) | 0.5 | |
| Water content (mass content) | 50 | |
| Density (20 DEG C) | 765 | |
| Viscosity | mPa.s | 0.27 |
Molecular sieve water separation tower middle and upper part 3A and bottom 4A filling ratios are 3: 7.The effective adsorption capacity of 3A molecular sieves takes 5%
Mass percent, the effective adsorption capacity of 4A molecular sieves takes 6% mass percent, and molecular sieve water separation tower filling ratio of height to diameter is 4: 1,
Calculated by single column switching in 7 days, molecular sieve water separation tower internal diameter is 2.2m, and molecular sieve water separation tower filling height is 8.8m.
It is two series connection in normal operating using three molecular sieve water separation tower adsorption-regenerations, one standby.Grasped in series connection
One online micro-moisture analyzer is set on the outlet official road of 1# molecular sieve water separation towers 1 of work, when detecting 1# molecular sieve water separation towers 1
When the water content of outlet streams is more than 5 μ g/g, 1# molecular sieve water separation towers 1 are cut out, be changed into 3# molecular sieve water separation towers 3 and enter regeneration journey
Sequence, the 2# molecular sieve water separation towers 2 for originally operating are switched to 1# molecular sieve water separation towers 1.Standby molecular sieve water separation tower switches to 2# molecules
Sieve dehydrating tower 2.
The 3# molecular sieve water separation towers 3 for cutting out enter reproducer, slowly open the discharging decompressing at the bottom of 3# molecular sieve water separation towers 3
Line, while slowly opening the pressure release drop out line on the top of 3# molecular sieve water separation towers 3, will be hydrocracked heavy naphtha pressure release and drains into pressure release time
Closed cans 8, when 3# molecular sieve water separation towers 3 and pressure release 8 pressure balance of recycling can, molecular sieve water separation tower pressure is down to close to emptying and is
During system pressure, pressure release is completed.The heavy naphtha that is hydrocracked in pressure release recycling can boosts through pump 9, returns and is hydrocracked heavy naphtha
Raw material is dehydrated again.
After the completion of pressure release, regeneration gas is introduced, open regeneration hot-air heater 4, while opening regeneration gas heat exchanger 12, regeneration gas
Air cooler 5, regeneration gas water knockout drum 6, regeneration gas blower fan 7 etc., realize that regeneration gas is circulated, and regeneration gas internal circulating load presses adsorption bed volume
Air speed 200h-1Design.By certain heating rate, nitrogen is heated to 250 DEG C, regeneration hot-air heater 4 outlet temperature keeps 250
DEG C, after 32 hours, by certain rate of temperature fall, after stopping regeneration hot-air heater 4, regeneration gas is switched to cold blowing flow, regeneration gas blower fan 7
After outlet regeneration gas is through re-generatively cooled device 10 and regeneration gas dehydrating tower 11, to the cold blowing of 3# molecular sieve water separation towers 3, cold blowing to 3# molecules
Sieve dehydrating tower 3 is down to 40~45 DEG C, stops regeneration gas blower fan 7, and 3# molecular sieve water separation towers 3 cut out regeneration gas circulation process.
After the completion of 3# molecular sieve water separation towers 3 regenerate.Through the bottom topping up stop valve topping up of 3# molecular sieve water separation towers 3, slowly open
Topping up stop valve, by the topping up of 3# molecular sieve water separation towers 3 to operating pressure, closes stop valve.3# molecular sieve water separation towers 3 are to standby shape
State.Whole reproducer is completed.
Independent pressure release recvery facility is set, and raising is hydrocracked heavy naphtha yield, material loss is greatly reduced, material is damaged
Consumption rate is 0.009% mass percent.
Regeneration gas circulation process is set, the consumption of nitrogen is on the one hand greatly reduced, be conducive to the production safety of factory, while
Avoid a large amount of inert gases from entering blowdown system, on the other hand reduce the energy consumption of Molecular sieve dehydration units.With regeneration gas once
By process CIMS, the energy consumption reduction by 30% of Molecular sieve dehydration units.
Claims (4)
1. a kind of method of heavy naphtha molecular sieve dehydration, comprises the following steps：
1) adsorb：Raw material sequentially enters molecular sieve water separation tower (1) and molecular sieve water separation tower (2) and carries out molecular sieve dehydration, described
3A and 4A classifications filling in molecular sieve water separation tower, 4A molecular sieves are loaded in molecular sieve water separation tower bottom, and 3A molecular sieves are loaded on top,
Top 3A and bottom 4A filling ratios are 2~4: 6~8；
Heavy naphtha after dehydration goes out device as product, and the logistics water content of molecular sieve water separation tower (1) outlet is more than 5 μ g/g
When, molecular sieve water separation tower (1) is cut out, into step 2), raw material sequentially enters molecular sieve water separation tower (2) and molecular sieve water separation tower
(3) molecular sieve dehydration is carried out, when the logistics water content of molecular sieve water separation tower (2) outlet is more than 5 μ g/g, molecular sieve dehydration is cut out
Tower (2), into step 2), raw material sequentially enters molecular sieve water separation tower (3) and molecular sieve water separation tower (1) and carries out molecular sieve dehydration,
When the logistics water content of molecular sieve water separation tower (3) outlet is more than 5 μ g/g, molecular sieve water separation tower (3) is cut out, into step 2)；
2) release is reclaimed：Opening steps 1) the discharging decompressing valve (16) of molecular sieve water separation tower (1), (2) or (3) bottom of towe that cuts out
With the pressure release balanced valve (17) of molecular sieve water separation tower (1), (2) or (3) tower top, the raw material in molecular sieve water separation tower is drained into and is let out
Closed cans (8) is pushed back, when molecular sieve water separation tower is with pressure release recycling can (8) pressure balance, molecular sieve water separation tower pressure is down to close putting
Empty system pressure, closes discharging decompressing valve (16) and pressure release atmospheric valve (17), and pressure release is completed, and molecular sieve water separation tower enters step
3), the raw material in pressure release recycling can mixes through pump (9) with raw material (14)；
3) regenerate：Regeneration gas is introduced to step 2) molecular sieve water separation tower 1,2 or 3 after pressure release, open regeneration hot-air heater
(4), regeneration gas heat exchanger (12), regeneration gas air cooler (5), regeneration gas water knockout drum (6) and regeneration gas blower fan (7), progressively will again
Anger is heated to 230~280 DEG C, after maintaining 24~36 hours, progressively lowers the temperature, and closes regeneration hot-air heater (4), switches to cold
Blow, regeneration gas blower fan (7) exports regeneration gas through re-generatively cooled device (10) and regeneration gas dehydrating tower (11), into molecular sieve water separation tower
(1), (2) or (3) are down to 40~45 DEG C, close regeneration gas blower fan (7), molecular sieve water separation tower (1), (2) or (3) regeneration knot
Beam, repeat step 1).
2. according to a kind of method of the heavy naphtha molecular sieve dehydration described in claim 1, it is characterised in that：Described scheelite brain
Oil is to be hydrocracked heavy naphtha.
3. according to a kind of method of the heavy naphtha molecular sieve dehydration described in claim 1, it is characterised in that：Described pressure release is returned
Receive, after molecular sieve water separation tower water suction saturation cuts out, open discharging decompressing valve (16) and pressure release atmospheric valve (17), molecular sieve is taken off
Raw material in water tower is drained into pressure release recycling can (8), when molecular sieve water separation tower (1), (2) or (3) and pressure release recycling can (8) pressure
During balance, discharging decompressing valve (16) and pressure release atmospheric valve (17), the raw material in pressure release recycling can (8) is through pump (9) and raw material (14)
Mixing.
4. according to a kind of method of the heavy naphtha molecular sieve dehydration described in claim 1, it is characterised in that：Described regeneration step
Suddenly, 240~280 DEG C of regeneration gas temperature, maintain the temperature 24~36 hours, progressively lower the temperature, and close regeneration hot-air heater (4), cut
Change cold blowing into, regeneration gas blower fan (7) exports regeneration gas through re-generatively cooled device (10) and regeneration gas dehydrating tower (11), into molecular sieve
Dehydrating tower (1), (2) or (3) is down to 40~45 DEG C, closes regeneration gas blower fan (7).
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1221775A (en) * | 1997-12-31 | 1999-07-07 | 中国科学院大连化学物理研究所 | Dewatering tech. for microwater in organic solvent |
| CN1748835A (en) * | 2004-09-18 | 2006-03-22 | 宁波海曙洁源气体处理工程有限公司 | Method and process flow for recovering organic matter component from organic exhaust gas |
| CN203060888U (en) * | 2013-02-19 | 2013-07-17 | 西安超滤化工有限责任公司 | Methylal deep dehydration purifying device |
-
2014
- 2014-05-20 CN CN201410219049.6A patent/CN105087048B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1221775A (en) * | 1997-12-31 | 1999-07-07 | 中国科学院大连化学物理研究所 | Dewatering tech. for microwater in organic solvent |
| CN1748835A (en) * | 2004-09-18 | 2006-03-22 | 宁波海曙洁源气体处理工程有限公司 | Method and process flow for recovering organic matter component from organic exhaust gas |
| CN203060888U (en) * | 2013-02-19 | 2013-07-17 | 西安超滤化工有限责任公司 | Methylal deep dehydration purifying device |
Non-Patent Citations (3)
| Title |
|---|
| "分子筛三塔高压脱水工艺改造应用";叶帆等;《天然气与石油》;20090228;第27卷(第1期);第41-43页 * |
| "分子筛液相脱水技术在轻烃生产中的应用";张桂香等;《河南化工》;20031231(第9期);第26-27页 * |
| 重石脑油产品脱水方案研究;沈文丽等;《石油化工设计》;20111231;第28卷(第1期);第6-9页 * |
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