CN107880929A - The atmospheric and vacuum distillation technique and system of a kind of floating bed hydrogenation product - Google Patents
The atmospheric and vacuum distillation technique and system of a kind of floating bed hydrogenation product Download PDFInfo
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- CN107880929A CN107880929A CN201610874771.2A CN201610874771A CN107880929A CN 107880929 A CN107880929 A CN 107880929A CN 201610874771 A CN201610874771 A CN 201610874771A CN 107880929 A CN107880929 A CN 107880929A
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- oil
- atmospheric
- floating bed
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- bed hydrogenation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
Abstract
The present invention relates to coal chemical industry and technical field of petrochemical industry, discloses a kind of atmospheric and vacuum distillation technique of floating bed hydrogenation product, comprises the following steps：Thermal high separation is carried out to floating bed hydrogenation product, collects hot high score oil；Heat low separation is carried out to the hot high score oil again, obtains hot low point of oil；Distillation processing is carried out to described low point of oil of heat under normal pressure, collects 150 DEG C~250 DEG C cuts and the cut more than 250 DEG C respectively；It will be evaporated under reduced pressure after the heating of the cut more than 250 DEG C in above-mentioned steps, obtain diesel oil, wax oil and subtract slag；Also disclose the atmospheric and vacuum distillation system of above-mentioned technique.It can make that decompression heater outlet temperature is up to standard, each cut quality of vacuum tower is qualified using above-mentioned technique and system, manufactured pitch rank is higher.
Description
Technical field
The invention belongs to coal chemical industry and technical field of petrochemical industry, and in particular to a kind of Atmospheric vacuum of floating bed hydrogenation product
Distillation technique and system.
Background technology
In existing heavy oil hydrocracking technique, it is anti-to enter floating bed hydrogenation by pretreated heavy raw oil
Answer device, the liquid phase that the reaction product of generation is formed by the gas phase that high pressure hot separator is separated after supercooling, decompression again
Into stripper, while the liquid-solid phase material separated from high pressure hot separator enters thermal low-pressure separators after decompression, heat
The gas phase that low pressure separator is separated is fractionated to obtain naphtha into stripper；Due to the difference of raw material oil nature, heat low
Liquid-solid phase material in separator can contain a certain proportion of heavy naphtha fraction, and this part heavy naphtha is by vacuum furnace
When will largely vaporize so that the outlet temperature of vacuum furnace does not reach the design feeding temperature of vacuum tower.Then, when largely vaporizing
After heavy naphtha fraction enters vacuum tower, it will also cause the apparatus for vacuum producing overload operation of Top of Vacuum Tower, so that Top of Vacuum Tower
Do not reach the vacuum of design so that vacuum tower can not stable operation, ultimately result in vacuum tower each side line oil product kick the beam and
Bottom of towe residue can not meet the requirement of asphalt moulding because being mixed with a certain amount of light oil.In addition, thermal low-pressure separators bottom is flowed
Because containing substantial amounts of colloid and catalyst solid particle in the liquid-solid phase material gone out, thus vacuum furnace tube coking will be caused to block up
Plug, so as to influence the normal operating of vacuum furnace.
Therefore, how the separation link in existing suspension bed hydrogenation process is improved, to overcome present in it
Depressurize that heater outlet temperature is up to standard, the high deficiency of lightweight oil content in each cut of vacuum tower, this for those skilled in the art and
Speech is a technical barrier urgently to be resolved hurrily.
The content of the invention
The technical problem to be solved in the present invention is present in the separation link in existing suspension bed hydrogenation process is overcome
The defects of decompression heater outlet temperature is up to standard, lightweight oil content is high in each cut of vacuum tower, and then one kind is provided can make decompression
The atmospheric and vacuum distillation technique and system for the floating bed hydrogenation product that heater outlet temperature is up to standard, each cut quality of vacuum tower is qualified.
In order to solve the above technical problems, the technical solution adopted by the present invention is as follows：
A kind of atmospheric and vacuum distillation technique of floating bed hydrogenation product of the present invention, comprises the following steps：
(1) thermal high separation is carried out to floating bed hydrogenation product, collects hot high score oil；Heat is carried out to the hot high score oil again
Low pressure separates, and obtains hot low point of oil；
(2) distillation processing is carried out to described low point of oil of heat under normal pressure, collects 150 DEG C~250 DEG C cuts respectively and more than 250
DEG C cut；
(3) it will be evaporated under reduced pressure after the heating of the cut more than 250 DEG C in step (2), obtain diesel oil, wax oil and subtract
Slag.
Alternatively, the operation temperature that the thermal high separates is 350~460 DEG C, operating pressure is 18~21MPa.
Alternatively, 350~460 DEG C of operation temperature, the operating pressure of the heat low separation are 0.5~2MPa.
Alternatively, 380~400 DEG C of the operation temperature of the vacuum distillation, operating pressure are 0.003~0.005MPa.
Alternatively, in addition to being more than the step of 250 DEG C of cuts carry out purified treatment in step (2), it is specially：
It is more than 250 DEG C of cuts by described and contacts with adsorbent to remove colloid therein and hydrogenation catalyst, forms purification
Oil and paste, then the purification oil is heated and is evaporated under reduced pressure successively.
Alternatively, the adsorbent is semi-coke and/or carclazyte.
Alternatively, the paste is adhesive.
A kind of system for carrying out atmospheric and vacuum distillation to suspension bed air inlet product using above-mentioned technique, including：
High pressure hot separator, its import and the hydrogenation products outlet of floating bed hydrogenation reactor；
Thermal low-pressure separators, its import connect the oil-out of the high pressure hot separator；
Vacuum tower, its import connect the oil discharge outlet of the thermal low-pressure separators by vacuum furnace, in the tower of the vacuum tower
Diesel oil outlet, wax oil outlet are from top to bottom disposed with wall and subtracts slag outlet；
Also include：
Atmospheric tower, it is arranged between the oil discharge outlet of the thermal low-pressure separators and the vacuum furnace, in the atmospheric tower
Bottom be provided with the outlet of normal slag, the often slag outlet is connected with the vacuum furnace；The row of being provided with the top of the atmospheric tower
Gas port, the exhaust outlet connect heavy naphtha oil sump tank.
Alternatively, in addition to be arranged at it is described often slag outlet the vacuum furnace between adsorbent equipment.
Alternatively, in addition to the slag outlet that subtracts the asphalt moulding device set is connected.
Technical solution of the present invention, have the following advantages that：
1. the atmospheric and vacuum distillation technique of floating bed hydrogenation product provided in an embodiment of the present invention, fully takes into account suspension bed and adds
Contained heavy naphtha component is to negative shadow caused by follow-up heating and decompression distillation system in the hot low point of oil of hydrogen product
Ring (depressurize heater outlet temperature is up to standard, lightweight oil content is high in each cut of vacuum tower), thus it is initiative first to low point of heat
Oil carries out air-distillation to remove 150 DEG C therein~250 DEG C cuts, that is to say heavy naphtha, then will be greater than 250 DEG C again
It is evaporated under reduced pressure after cut heating, thus first heavy naphtha can be avoided largely to be vaporized in vacuum furnace so that vacuum furnace
Outlet temperature does not reach the design feeding temperature of vacuum tower；Second heavy naphtha can be also avoided to enter in vacuum tower and cause to depressurize
Each side line oil product of tower kicks the beam and bottom of towe residue can not meet the requirement of asphalt moulding, so as to efficiently solve existing suspension
The decompression heater outlet temperature present in separation link in bed hydroprocessing technique is not up to standard, lightweight oil content is high in each cut of vacuum tower
The defects of so that floating bed hydrogenation product can obtain bavin best in quality after atmospheric and vacuum distillation PROCESS FOR TREATMENT of the present invention
Oil, wax oil and pitch；Simultaneously diesel oil obtained above, wax oil enter downstream fixed bed reactors refine that hydrogenation reduces need not
The energy consumption and cost wanted.
2. the atmospheric and vacuum distillation technique of floating bed hydrogenation product provided in an embodiment of the present invention, by using adsorbent to heat
The cut more than 250 DEG C in low point of oil carries out purified treatment, so as to remove colloid therein and hydrogenation catalyst, to avoid
Above-mentioned substance enters vacuum furnace and causes tube coking or even worn out, and then ensures the continual and steady operation of vacuum furnace.
Further, technique of the present invention by using semi-coke and/or carclazyte as adsorbent so that be adsorbed with glue
The paste of matter and hydrogenation catalyst can use as industry adhesive, so as to be advantageous to increase the economic effect of present invention process
Benefit.
3. the atmospheric and vacuum distillation system of floating bed hydrogenation product provided in an embodiment of the present invention, only need to be in existing segregative line
Set up between thermal low-pressure separators and vacuum tower in system an atmospheric tower can overcome decompression heater outlet temperature it is not up to standard, decompression
The defects of lightweight oil content is high in each cut of tower, thus have the advantages that equipment investment is small, stable, output benefit is high.
Brief description of the drawings
, below will be to specific in order to illustrate more clearly of the specific embodiment of the invention or technical scheme of the prior art
The required accompanying drawing used is briefly described in embodiment or description of the prior art, it should be apparent that, in describing below
Accompanying drawing is some embodiments of the present invention, for those of ordinary skill in the art, before creative work is not paid
Put, other accompanying drawings can also be obtained according to these accompanying drawings.
Fig. 1 is the atmospheric and vacuum distillation process chart of floating bed hydrogenation product of the present invention；
Wherein, reference is as follows：
10- floating bed hydrogenation reactors；20- high pressure hot separators；30- thermal low-pressure separators；40- atmospheric towers；
41- Atmospheric Tower air water coolers；42- Atmospheric Tower return tanks；43- Atmospheric Tower pumps；44- normal pressure column bottoms pumps；45- is normal
Press bottom of towe profit cooler；50- vacuum towers；51- vacuum furnaces；52- vacuum 1st side cut pumps；53- vacuum 1st side cut condensers；54- second line of distillation
Pump；55- second line of distillation coolers；56- VACUUM TOWER BOTTOM pumps；60- adsorbent equipments.
Embodiment
The present invention can be embodied in many different forms, and should not be construed as limited to embodiment set forth herein.
Conversely, there is provided these embodiments so that the disclosure will be thorough and complete, and the design of the present invention will be fully conveyed to
Those skilled in the art, the present invention will only be defined by the appended claims.
Embodiment 1
A kind of atmospheric and vacuum distillation system of floating bed hydrogenation product is present embodiments provided, including：
Floating bed hydrogenation reactor 10, its top are provided with hydrogenation products outlet；
High pressure hot separator 20, its import and hydrogenation products outlet, are set out in the bottom of high pressure hot separator 20
Hydraulic fluid port；
Thermal low-pressure separators 30, its import connect the oil-out of high pressure hot separator 20；
Atmospheric tower 40, it is arranged between the oil discharge outlet of thermal low-pressure separators 30 and vacuum furnace 51, at the bottom of atmospheric tower 40
Portion is provided with normal slag outlet, and normal slag outlet is connected with vacuum furnace 51；Heavy naphtha output group is provided with the top of atmospheric tower 40
Part；Specially atmospheric tower 40 pushes up elder generation and is connected with Atmospheric Tower air water cooler 41, through normal pressure return tank of top of the tower 42, Atmospheric Tower pump 43
Atmospheric tower 40 is back to, heavy naphtha export pipeline connects with the output end of Atmospheric Tower pump 43.
Vacuum tower 50, its import connects the oil discharge outlet of thermal low-pressure separators 30 by vacuum furnace 51, in the tower of vacuum tower 51
Diesel oil outlet, wax oil outlet are from top to bottom disposed with wall and subtracts slag outlet；Subtract the asphalt moulding that slag outlet connection is set
Device.
In the present embodiment, vacuum tower outlet obtains diesel oil by vacuum 1st side cut pump 52 and vacuum 1st side cut cooler 53, by subtracting two
Line pump 54 and second line of distillation cooler 55 obtain wax oil, and above-mentioned diesel oil and wax oil are solid through diesel oil output line and wax oil output line and subsequently
Fixed bed hydrogenation reactor connects, and further refines hydrogenation；Vacuum tower bottoms are connected through VACUUM TOWER BOTTOM pump 56 with asphalt moulding unit.
In the present embodiment, adsorbent equipment 60 is set between the outlet of normal slag and vacuum furnace.Normal slag outlet and adsorbent equipment 60
Between be additionally provided with atmospheric tower pump 44 and atmospheric tower base oil water cooler 45.
Embodiment 2
As shown in figure 1, the present embodiment provides a kind of atmospheric and vacuum distillation technique of floating bed hydrogenation, comprise the following steps：
S1. high temperature coal-tar is sent into floating bed hydrogenation reactor, floating bed hydrogenation production is obtained after series reaction
Thing；
S2. floating bed hydrogenation product enters in high pressure hot separator, under 460 DEG C, 18MPa isolated hot high score oil and
Hot gas separated by high pressure separator, hot gas separated by high pressure separator enter cold high pressure separator, and hot high score oil then enters thermal low-pressure separators, divide under 460 DEG C, 2MPa
From obtaining low point of oil of heat and hot low point of gas, hot low point of gas enters fractionating device, and hot low point of oil then enter in atmospheric tower distill with
Remove the heavy naphtha of 150 DEG C~250 DEG C cuts；
S3. the remaining cut for being more than 250 DEG C is re-fed into vacuum tower after vacuum furnace is heated to 400 DEG C in step S2,
It is evaporated under reduced pressure under 0.005MPa, respectively obtains diesel oil, wax oil and subtract slag, it is final will then subtracts slag feeding asphalt moulding unit again
Pitch is made.
Embodiment 3
As shown in figure 1, the present embodiment provides a kind of atmospheric and vacuum distillation technique of floating bed hydrogenation, comprise the following steps：
S1. high temperature coal-tar is sent into floating bed hydrogenation reactor, floating bed hydrogenation production is obtained after series reaction
Thing；
S2. floating bed hydrogenation product enters in high pressure hot separator, under 350 DEG C, 21MPa isolated hot high score oil and
Hot gas separated by high pressure separator, hot gas separated by high pressure separator enter cold high pressure separator, and hot high score oil then enters thermal low-pressure separators, under 350 DEG C, 0.5MPa
Isolated low point of oil of heat and hot low point of gas, hot low point of gas enter fractionating device, and hot low point of oil is then into distilling in atmospheric tower
To remove the heavy naphtha of 150 DEG C~250 DEG C cuts；
S3. it is remaining in step S2 to be more than 250 DEG C of cuts and be re-fed into after vacuum furnace is heated to 380 DEG C in vacuum tower, in
It is evaporated under reduced pressure under 0.003MPa, respectively obtains diesel oil, wax oil and subtract slag, will be then subtracted slag feeding asphalt moulding unit again and finally make
Obtain pitch.
Embodiment 4
As shown in figure 1, the present embodiment provides a kind of atmospheric and vacuum distillation technique of floating bed hydrogenation, comprise the following steps：
S1. high temperature coal-tar is sent into floating bed hydrogenation reactor, floating bed hydrogenation production is obtained after series reaction
Thing；
S2. floating bed hydrogenation product enters in high pressure hot separator, under 380 DEG C, 19MPa isolated hot high score oil and
Hot gas separated by high pressure separator, hot gas separated by high pressure separator enter cold high pressure separator, and hot high score oil then enters thermal low-pressure separators, under 380 DEG C, 1.0MPa
Isolated low point of oil of heat and hot low point of gas, hot low point of gas enter fractionating device, and hot low point of oil is then into distilling in atmospheric tower
To remove the heavy naphtha of 150 DEG C~250 DEG C cuts；
S3. the remaining cut for being more than 250 DEG C is re-fed into vacuum tower after vacuum furnace is heated to 390 DEG C in step S2,
It is evaporated under reduced pressure under 0.004MPa, respectively obtains diesel oil, wax oil and subtract slag, it is final will then subtracts slag feeding asphalt moulding unit again
Pitch is made.
Embodiment 5
As shown in figure 1, the present embodiment provides a kind of atmospheric and vacuum distillation technique of floating bed hydrogenation, comprise the following steps：
S1. high temperature coal-tar is sent into floating bed hydrogenation reactor, floating bed hydrogenation production is obtained after series reaction
Thing；
S2. floating bed hydrogenation product enters in high pressure hot separator, under 400 DEG C, 20MPa isolated hot high score oil and
Hot gas separated by high pressure separator, hot gas separated by high pressure separator enter cold high pressure separator, and hot high score oil then enters thermal low-pressure separators, under 400 DEG C, 1.5MPa
Isolated low point of oil of heat and hot low point of gas, hot low point of gas enter fractionating device, and hot low point of oil is then into distilling in atmospheric tower
To remove the heavy naphtha of 150 DEG C~250 DEG C cuts；
S3. it is remaining in step S2 to be more than 250 DEG C of cuts and be re-fed into after vacuum furnace is heated to 380 DEG C in vacuum tower, in
It is evaporated under reduced pressure under 0.003MPa, respectively obtains diesel oil, wax oil and subtract slag, will be then subtracted slag feeding asphalt moulding unit again and finally make
Obtain pitch.
Embodiment 6
As shown in figure 1, the present embodiment provides a kind of atmospheric and vacuum distillation technique of floating bed hydrogenation, comprise the following steps：
S1. high temperature coal-tar is sent into floating bed hydrogenation reactor, floating bed hydrogenation product is obtained after series reaction；
S2. floating bed hydrogenation product enters in high pressure hot separator, the isolated hot high score oil under 450 DEG C, 18.5MPa
With hot gas separated by high pressure separator, hot gas separated by high pressure separator enters cold high pressure separator, and hot high score oil then enters thermal low-pressure separators, in 450 DEG C, 1.7MPa
Under isolated low point of oil of heat and hot low point of gas, hot low point of gas enters fractionating device, and hot low point of oil is then into steaming in atmospheric tower
Evaporate to remove the heavy naphtha of 150 DEG C~250 DEG C cuts；
S3. remove the cut after heavy naphtha and carry out purified treatment, specially will be greater than 250 DEG C of cuts and contacted with adsorbent
To remove colloid therein and hydrogenation catalyst, purification oil and paste are formed, then purification oil is heated and depressurized successively
Distillation, and adhesive can be further made in paste；
Adsorbent can be selected as the mixture of semi-coke or carclazyte or both；
S4. purify oil distillate in step S3 to be re-fed into vacuum tower after vacuum furnace is heated to 400 DEG C, under 0.005MPa
It is evaporated under reduced pressure, respectively obtains diesel oil, wax oil and subtract slag, will then subtracts slag again and be sent into asphalt moulding unit finally obtained pitch.
Comparative example 1
The present embodiment provides a kind of atmospheric and vacuum distillation technique of floating bed hydrogenation, comprises the following steps：
S1. high temperature coal-tar is sent into floating bed hydrogenation reactor, floating bed hydrogenation product is obtained after series reaction；
S2. floating bed hydrogenation product enters in high pressure hot separator, under 460 DEG C, 18MPa isolated hot high score oil and
Hot gas separated by high pressure separator, hot gas separated by high pressure separator enter cold high pressure separator, and hot high score oil then enters thermal low-pressure separators, divide under 460 DEG C, 2MPa
From low point of oil of heat and hot low point of gas is obtained, hot low point of gas enters fractionating device；
S3. the hot low point of oil in step S2 is fed through in vacuum tower, is evaporated under reduced pressure under 0.005MPa, is respectively obtained bavin
Oil, wax oil and subtract slag, will then subtract slag again and be sent into asphalt moulding unit pitch is finally made.
Experimental example
The diesel oil of 2~embodiment of above-described embodiment 6 and the gained of comparative example 1, wax oil and subtract slag property it is as shown in the table：
Table：
Data above shows, compared with comparative example 1, the diesel oil of the gained of 2~embodiment of embodiment 6, wax oil density are higher, say
The bright diesel oil obtained using above-mentioned technique and system and wax oil are not mixed with light oil, and quality is more preferable；Meanwhile 2~embodiment of embodiment 6
Gained subtracts slag and is made that the needle penetration of pitch, ductility are small compared to comparative example 1, and softening point is big compared with comparative example 1, illustrate obtained by subtract slag more tacky
It is thick, pitch is made and is easier to shape, quality is higher.
Obviously, above-described embodiment is only intended to clearly illustrate example, and is not the restriction to embodiment.It is right
For those of ordinary skill in the art, can also make on the basis of the above description it is other it is various forms of change or
Change.There is no necessity and possibility to exhaust all the enbodiments.And the obvious change thus extended out or
Among changing still in the protection domain of the invention.
Claims (10)
1. a kind of atmospheric and vacuum distillation technique of floating bed hydrogenation product, it is characterised in that comprise the following steps：
(1) thermal high separation is carried out to floating bed hydrogenation product, collects hot high score oil；Heat low is carried out to the hot high score oil again
Separation, obtain hot low point of oil；
(2) distillation processing is carried out to described low point of oil of heat under normal pressure, collects 150 DEG C~250 DEG C cuts respectively and evaporated more than 250 DEG C
Point；
(3) being more than after 250 DEG C of cuts heat in step (2) is evaporated under reduced pressure, obtains diesel oil, wax oil and subtract slag.
2. the atmospheric and vacuum distillation technique of floating bed hydrogenation product according to claim 1, it is characterised in that the thermal high
The operation temperature of separation is 350~460 DEG C, operating pressure is 18~21MPa.
3. the atmospheric and vacuum distillation technique of floating bed hydrogenation product according to claim 1 or 2, it is characterised in that the heat
350~460 DEG C of operation temperature, the operating pressure of low pressure separation are 0.5~2MPa.
4. the atmospheric and vacuum distillation technique of the floating bed hydrogenation product according to claim 1-3, it is characterised in that the decompression
380~400 DEG C of operation temperature, the operating pressure of distillation are 0.003~0.005MPa.
5. the atmospheric and vacuum distillation technique of the floating bed hydrogenation product according to claim 1-4, it is characterised in that also include pair
It is more than the step of 250 DEG C of cuts carry out purified treatment in step (2), is specially：
Be more than 250 DEG C of cuts by described and contact with adsorbent to remove colloid therein and hydrogenation catalyst, formed purification oil and
Paste, then the purification oil is heated and is evaporated under reduced pressure successively.
6. the atmospheric and vacuum distillation technique of floating bed hydrogenation product according to claim 5, it is characterised in that the adsorbent
For semi-coke and/or carclazyte.
7. the atmospheric and vacuum distillation technique of floating bed hydrogenation product according to claim 6, it is characterised in that the paste
For adhesive.
8. a kind of system for carrying out atmospheric and vacuum distillation to suspension bed air inlet product using any one of the claim 1-4 techniques,
Including：
High pressure hot separator, its import and the hydrogenation products outlet of floating bed hydrogenation reactor；
Thermal low-pressure separators, its import connect the oil-out of the high pressure hot separator；
Vacuum tower, its import connect the oil discharge outlet of the thermal low-pressure separators by vacuum furnace, in the tower wall of the vacuum tower
From top to bottom it is disposed with diesel oil outlet, wax oil outlet and subtracts slag outlet；
Characterized in that, also include：
Atmospheric tower, it is arranged between the oil discharge outlet of the thermal low-pressure separators and the vacuum furnace, at the bottom of the atmospheric tower
Portion is provided with normal slag outlet, and the often slag outlet is connected with the vacuum furnace；Exhaust outlet is provided with the top of the atmospheric tower,
The exhaust outlet connects heavy naphtha oil sump tank.
9. system according to claim 8, it is characterised in that also include being arranged at the often slag outlet and the vacuum furnace
Between adsorbent equipment.
10. system according to claim 8 or claim 9, it is characterised in that also include and the drip for subtracting slag outlet connection and setting
Blue or green shaped device.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201610874771.2A CN107880929B (en) | 2016-09-30 | 2016-09-30 | Atmospheric and vacuum distillation process and system for hydrogenation product of suspension bed |
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| CN201610874771.2A CN107880929B (en) | 2016-09-30 | 2016-09-30 | Atmospheric and vacuum distillation process and system for hydrogenation product of suspension bed |
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101376068A (en) * | 2008-09-17 | 2009-03-04 | 天津大学 | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer |
| CN104449824A (en) * | 2014-12-05 | 2015-03-25 | 北京石油化工工程有限公司 | Separation and pressure reduction combining system for suspended bed hydrocracking reaction products |
-
2016
- 2016-09-30 CN CN201610874771.2A patent/CN107880929B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101376068A (en) * | 2008-09-17 | 2009-03-04 | 天津大学 | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer |
| CN104449824A (en) * | 2014-12-05 | 2015-03-25 | 北京石油化工工程有限公司 | Separation and pressure reduction combining system for suspended bed hydrocracking reaction products |
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