CN105272799B - Olefin catalytic cracking reaction system and method - Google Patents
Olefin catalytic cracking reaction system and method Download PDFInfo
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- CN105272799B CN105272799B CN201410350421.7A CN201410350421A CN105272799B CN 105272799 B CN105272799 B CN 105272799B CN 201410350421 A CN201410350421 A CN 201410350421A CN 105272799 B CN105272799 B CN 105272799B
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Abstract
The invention discloses an olefin catalytic cracking reaction system and method. The system includes an expansion machine unit; the expansion machine unit includes an expansion machine; a pre-hydrogenation reactor outlet pipeline is divided into two branches, one branch is connected with a pre-hydrogenation circulation pump and then is connected with a pre-hydrogenation cooler, and the other branch is connected with a pre-hydrogenation feeding and discharging heat exchanger and then is connected with a catalytic cracking feeding vaporization tank; the top of the catalytic cracking feeding vaporization tank is connected with the expansion machine, and an outlet of the expansion machine is successively connected with the catalytic cracking reaction feeding and discharging heat exchanger and a feeding heater and then is connected with a catalytic cracking reactor. The method comprises that a pre-hydrogenation reaction discharging material is directly heated and evaporated without reduction of a pressure, and after evaporation, the pressure is reduced to a catalytic cracking reaction required pressure via the expansion machine. The method of firstly heating evaporation of the pre-hydrogenation reaction discharging material and then taking the evaporated material as an expansion machine working medium for driving a machine pump is used for replacing a conventional flow method of firstly reducing the pressure and then evaporating, the pressure potential of the pre-hydrogenation reaction discharging material is used for applying work, and thus the purposes of reducing energy consumption and saving operating cost are achieved.
Description
Technical field
The present invention relates to carbon four and above heavier olefins preparing propylene by catalytic cracking, ethene technical field, further say, are to relate to
And a kind of olefins by catalytic cracking reaction system and method.
Background technology
Olefins by catalytic cracking technology is carbon four and the more heavy constituent using ethylene unit, MTO devices or oil refining apparatus by-product
As raw material, under catalyst action, contained alkene in catalytic pyrolysis raw material obtains the one of light molecular olefine propylene and ethene
The method of kind.For avoiding raw materialNote 1The carbon distribution in the catalytic cracking reaction device such as the alkadienes of middle entrainment, alkynes, causes catalyst to lose
Living, reaction time shortens, and side reaction increases, and reaction selectivity declines, and can generally arrange reaction feed pre-hydrogenator, go
Except harmful constituents such as alkadienes, alkynes.
Note 1：Described in word of the present invention, chart, raw material fingering enters the material of pre-hydrogenator, comprising device fresh feed
And recycle stock.
The typical process of the technology is as shown in Figure 1.The pre- hydrogenation units of raw material Jing, remove the harmful constituents such as alkadienes, alkynes
Afterwards, Jing pressure-reducing valves decompression, then Jing after vaporization unit is heated vaporization, into catalytic cracking reaction unit, carbon four in raw material and
More heavier olefins are converted into propylene and ethylene.
More specifically, the typical process of the technology is as shown in Figure 2.The raw material (F-1) come from upstream is hydrogenated with input and output material pre-
Heat exchanger 1 and hydrogenation reaction discharging heat exchange cooling, then Jing after pre-add hydrogen cooler 2 is cooled to hydrogenation reaction temperature, with hydrogen F-2
It is mixed into pre-hydrogenator 3.Pre-hydrogenator outlet material, a part of Jing are hydrogenated with circulating pump 4 in advance and boost, and are back to pre-
Hydrogenation cooler 2, used as pre- hydrogenation recycle stock；A part of Jing is hydrogenated with input and output material heat exchanger 1 in advance and is heated up with raw material F-1 heat exchange,
Downstream catalytic cracking unit is delivered to as pre-hydrotreating reaction discharging F-3.As olefins by catalytic cracking reaction is that molecular number increases
Reaction, therefore operating pressure is lower, is more conducive to reaction；And hydrogenation reaction typically need to be carried out at elevated pressures, therefore pre- hydrogenation
Reaction discharging F-3 needs to enter back into downstream Jing after pressure-reducing valve 5 reduces pressure.Additionally, olefins by catalytic cracking reaction is gas phase reaction again, therefore
Charging into before catalytic cracking reaction device needs first to vaporize.Therefore the pre-hydrotreating reaction discharging F-4 after decompression, deliver to catalytic pyrolysis charging
Gasifying pot 6, after feeding vaporizer 7 is heated vaporization, Jing feed superheaters 8 are heated to 104 DEG C to gas phase again.Overheated pre- hydrogenation
Reaction discharging F-5, in catalytic cracking reaction input and output material heat exchanger 10, after heating up with the discharging heat exchange of catalytic cracking reaction device, then Jing
Feed heater 11, after being heated to reaction temperature, into catalytic cracking reaction device 12.Catalytic cracking reaction device discharges and pre-add
After hydrogen reaction discharging F-5 heat exchange, downstream separation unit is delivered to as olefins by catalytic cracking reaction discharging F-6.
This typical process less energy-conservation, operating cost are higher, and reason is：Pre-hydrotreating reaction operating pressure is higher, and alkene
Hydrocarbon catalytic cracking reaction operating pressure is relatively low, and this flow process pressure-reducing valve reduces pressure, and does not make full use of the pressure potential of material.
The content of the invention
For solving produced problem in prior art, the invention provides a kind of olefins by catalytic cracking reaction system and side
Method.Take pre-hydrotreating reaction discharging heating vaporization first, be further used as the method that decompressor working medium drives pump, replace traditional process
First reduce pressure, the method for re-vaporization, the pressure potential acting discharged using pre-hydrotreating reaction are reduced energy consumption, save operating cost
Purpose.
An object of the present invention is to provide a kind of olefins by catalytic cracking reaction system.
Including:Feed pre- hydrogenation unit, feedstock vaporisation unit and catalytic cracking reaction unit；Feed pre- hydrogenation unit bag
Include：It is pre- to be hydrogenated with input and output material heat exchanger, pre-add hydrogen cooler, pre-hydrogenator and be hydrogenated with circulating pump in advance；Feedstock vaporisation unit bag
Include：Catalytic pyrolysis feedstock vaporisation tank and feeding vaporizer；Catalytic cracking reaction unit includes：Catalytic cracking reaction input and output material exchanges heat
Device, feed heater, catalytic cracking reaction device and catalytic cracking reaction discharging cooler；
The system includes decompressor unit；Decompressor unit is arranged on feedstock vaporisation unit and catalytic cracking reaction unit
Between；Decompressor unit includes decompressor；
Pre-hydrogenator outlet line is divided into two, and a connection connects pre-add hydrogen cooler after being hydrogenated with circulating pump in advance；
Another connection connects catalytic pyrolysis feedstock vaporisation tank after being hydrogenated with input and output material heat exchanger in advance；Catalytic pyrolysis feedstock vaporisation tank top connects
Decompressor is connect, expander outlet connects catalytic pyrolysis after being sequentially connected catalytic cracking reaction input and output material heat exchanger and feed heater
Reactor.
The second object of the present invention is to provide a kind of olefins by catalytic cracking reaction method.
Including：Pre-hydrotreating reaction discharging is not reduced pressure directly to be heated and is vaporized, and after vaporization, Jing decompressors are decompressed to catalytic pyrolysis
Reaction desirable pressure.
Comprise the following steps：
(1) raw material is mixed into pre-hydrogenator with hydrogen Jing after heat exchange and cooling down；
(2) pre-hydrogenator outlet material, it is a part of it is boosted after be back to pre-add hydrogen cooler, follow as pre- hydrogenation
Ring material；It is a part of to send into catalytic pyrolysis feedstock vaporisation tank Jing after being hydrogenated with input and output material heat exchanger in advance and heat up with raw material heat exchange；
(3) after feeding vaporizer is heated vaporization, catalytic pyrolysis feedstock vaporisation tank gas phase enters decompressor, expansion work
After decompression, in catalytic cracking reaction input and output material heat exchanger, heat up with the discharging heat exchange of catalytic cracking reaction device, then Jing feed heaters
Heating, into catalytic cracking reaction device；
(4) after the discharging of catalytic cracking reaction device is exchanged heat with pre-hydrotreating reaction discharging, then the discharging cooling of Jing catalytic cracking reactions
Device is cooled down, and delivers to downstream separation unit as olefins by catalytic cracking reaction discharging.
Wherein, preferably：
After the raw material elder generation, Jing pre-add hydrogen input and output material heat exchanger, pre-add hydrogen cooler, are cooled to 36-60 DEG C, send into pre-add
Hydrogen reactor.
Pre-hydrotreating reaction discharging pressure after decompressor work is 0.05-0.6MpaG.
The catalytic cracking reaction device discharging elder generation Jing catalytic cracking reaction input and output material heat exchangers are changed with pre-hydrotreating reaction discharging
Heat, then Jing catalytic cracking reactions discharging cooler, are cooled to 36-60 DEG C, send into downstream separation unit.
The process conditions of the present invention can adopt common process conditions in prior art, in the present invention, preferably：
The operating pressure of the pre-hydrogenator is 0.9-7.0MPaG, and reaction temperature is 36-60 DEG C, and reaction temperature rising is
1-50℃；
The operating pressure of the catalytic pyrolysis feedstock vaporisation tank is 0.6-6.95MPaG, and operation temperature is 40-200 DEG C；
Feed heater operating pressure 0.05-0.6MPaG, material side outlet temperature are 400-600 DEG C；
Catalytic cracking reaction device operating pressure 0.03-0.6MPaG, reaction temperature are 400-600 DEG C.
Concrete technical scheme is as follows：
System includes：Feedstock vaporisation unit and decompressor unit, the feedstock vaporisation unit include：Catalytic pyrolysis feeds vapour
Change tank and feeding vaporizer；The decompressor unit includes that decompressor, decompressor drive pump and supporting motor or the turbine of going into operation.
System upstream and downstream connects the pre- hydrogenation unit of charging and catalytic cracking reaction unit respectively；The pre- hydrogenation unit of the charging includes：In advance
It is hydrogenated with input and output material heat exchanger, pre-add hydrogen cooler, pre-hydrogenator and is hydrogenated with circulating pump in advance；The catalytic cracking reaction unit
Including：The discharging cooling of catalytic cracking reaction input and output material heat exchanger, feed heater, catalytic cracking reaction device and catalytic cracking reaction
Device.
Method includes：Pre-hydrotreating reaction discharging is not reduced pressure directly to be heated and is vaporized, and drives turbine to do as working medium after vaporization
Work(, and it is decompressed to catalytic cracking reaction desirable pressure.
Idiographic flow is as follows：The raw material (F-1) come from upstream is changed in pre- hydrogenation input and output material heat exchanger 1 and hydrogenation reaction discharging
Heat cooling, then Jing after pre-add hydrogen cooler 2 is cooled to hydrogenation reaction temperature, pre-hydrogenator is mixed into hydrogen.Pre-add
Hydrogen reactor outlet material, a part of Jing are hydrogenated with circulating pump 4 in advance and boost, and are back to pre-add hydrogen cooler 2, used as pre- hydrogenation circulation
Material；A part of Jing is hydrogenated with input and output material heat exchanger 1 in advance and is heated up with raw material F-1 heat exchange, as pre-hydrotreating reaction discharging F-3 deliver to into
Material vaporization unit catalytic pyrolysis feedstock vaporisation tank 6.After feeding vaporizer 7 is heated vaporization, gas phase F-4 ' make into decompressor 9
Do work for working medium, drive pump.Pre-hydrotreating reaction discharging F-5 after expansion work, first exchanges heat in catalytic cracking reaction input and output material
Device 10, is heated up with the discharging heat exchange of catalytic cracking reaction device, then Jing feed heaters 11, after being heated to reaction temperature, is entered and is urged
Change cracking reactor 12.Catalytic cracking reaction device is discharged after being exchanged heat with pre-hydrotreating reaction discharging F-5, then Jing catalytic cracking reactions go out
Material cooler cooling, delivers to downstream separation unit as olefins by catalytic cracking reaction discharging F-6.
Pre-hydrotreating reaction of the decompressor after vaporizing discharges as working medium, and pre-hydrotreating reaction discharging is done work in decompressor
Decompression, decompressor are connected with pump by bearing, and bearing is also connected with motor or turbine.Decompressor power output needs work(with pump
Rate is compared, and insufficient section is provided by motor or turbine, and this motor or turbine act also as the power that goes into operation when decompressor is without working medium
Source.
Each material can be exchanged heat with unclassified stores in device, to reduce public work material (such as steam, recirculated water etc.)
Consume.
As the present invention does not obtain effective profit for pre-hydrotreating reaction discharge pressure potential energy present in existing commercial plant
Multiple prior arts are optimized combination by problem, and proposition is adapted to make full use of this pressure potential and do not affect upstream and downstream
The group technology of unit operation, therefore, reaction technology, catalyst used in the present invention etc. can adopt prior art,
The enforcement of the present invention is not limited by disclosed in the present invention or undocumented technical essential, and those skilled in the art can basis
Situation is selected as appropriate for, but the present invention is definitely not these prior arts simply enumerates combination, but solves current industry
The problem that production is implicitly present in, with quite significant industrial value.
Invention olefin catalytic cracking reaction system and method has the advantage that and effect：
1. plant energy consumption is reduced
The present invention drives pump by pre-hydrotreating reaction discharging is vaporized at elevated pressures as decompressor working medium, returns
The pressure potential using material is received, it is all or part of to substitute steam or electricity needed for pump, so as to reduce plant energy consumption.
2. operating cost is reduced
, compared with conventional method, as overall utility consumption is reduced, device operating cost can be bright for the inventive method
It is aobvious to reduce；The new equipment component design condition such as boost expander and catalytic pyrolysis feedstock vaporisation tank improves increased investment, can be
Reclaim in short period, economic benefit of the present invention is obvious.
3. pre-hydrotreating reaction and catalytic cracking reaction are not affected
The inventive method, varies without pre-hydrotreating reaction and catalytic cracking reaction operating condition, on both without impact.
Description of the drawings
Fig. 1 prior art group technology schematic diagrames
The olefins by catalytic cracking system schematic of Fig. 2 prior arts
Fig. 3 group technology schematic diagrames of the present invention
Fig. 4 invention olefin catalytic cracking system schematic diagrames
Description of reference numerals：
F-1 raw materials, 1 pre- hydrogenation input and output material heat exchanger, 2 pre-add hydrogen coolers, 3 pre-hydrogenators, 4 pre- hydrogenation circulations
Pump, the discharging of F-3 pre-hydrotreating reactions, 5 pressure-reducing valves, the pre-hydrotreating reaction discharging after F-4 decompressions, F-4 ' do not reduce pressure the pre-add for first vaporizing
Hydrogen reaction discharging, 6 catalytic pyrolysis feedstock vaporisation tanks, 7 feeding vaporizers, 8 feed superheaters, 9 decompressors, F-5 reduce pressure and vaporize
Pre-hydrotreating reaction discharging afterwards, 10 catalytic cracking reaction input and output material heat exchangers, 11 feed heaters, 12 catalytic cracking reaction devices,
13 catalytic cracking reactions discharging cooler, F-6 catalytic cracking reaction products.
Specific embodiment
With reference to embodiment, the present invention is further illustrated.
Embodiment：
As shown in figure 4, a kind of olefins by catalytic cracking reaction system.
Including:Feed pre- hydrogenation unit, feedstock vaporisation unit and catalytic cracking reaction unit；Feed pre- hydrogenation unit bag
Include：Pre- hydrogenation input and output material heat exchanger 1, pre-add hydrogen cooler 2, pre-hydrogenator 3 and pre- hydrogenation circulating pump 4；Feedstock vaporisation list
Unit includes：Catalytic pyrolysis feedstock vaporisation tank 6 and feeding vaporizer 7；Catalytic cracking reaction unit includes：Catalytic cracking reaction is passed in and out
Material heat exchanger 10, feed heater 11, catalytic cracking reaction device 12 and catalytic cracking reaction discharging cooler 13；
The system includes decompressor unit；Decompressor unit includes decompressor 9；
3 outlet line of pre-hydrogenator is divided into two, and a connection connects pre-add hydrogen cooler after being hydrogenated with circulating pump 4 in advance
2；Another connection connects catalytic pyrolysis feedstock vaporisation tank 6 after being hydrogenated with input and output material heat exchanger 1 in advance；Catalytic pyrolysis feedstock vaporisation tank 6
Top connection decompressor 9, after the outlet of decompressor 9 is sequentially connected catalytic cracking reaction input and output material heat exchanger 10 and feed heater 11
Connection catalytic cracking reaction device 12.
Method includes：Pre-hydrotreating reaction discharging is not reduced pressure directly to be heated and is vaporized, and drives turbine to do as working medium after vaporization
Work(, and it is decompressed to catalytic cracking reaction desirable pressure.
Idiographic flow is as follows：
The raw material (F-1) come from upstream is hydrogenated with input and output material heat exchanger 1 and hydrogenation reaction discharging heat exchange cooling pre-, then Jing is pre-
After hydrogenation cooler 2 is cooled to hydrogenation reaction temperature, pre-hydrogenator is mixed into hydrogen.Pre-hydrogenator exports thing
Material, a part of Jing are hydrogenated with circulating pump 4 in advance and boost, and are back to pre-add hydrogen cooler 2, used as pre- hydrogenation recycle stock；A part of Jing
Pre- hydrogenation input and output material heat exchanger 1 is heated up with raw material F-1 heat exchange, is delivered to feedstock vaporisation unit as pre-hydrotreating reaction discharging F-3 and is urged
Change cracking feed gasifying pot 6.After feeding vaporizer 7 is heated vaporization, gas phase F-4 ' decompressor 9 is entered as working medium acting,
Drive pump.Pre-hydrotreating reaction discharging F-5 after expansion work, first in catalytic cracking reaction input and output material heat exchanger 10, with catalysis
Cracking reactor discharging heat exchange heats up, then Jing feed heaters 11, after being heated to reaction temperature, into catalytic cracking reaction device
12.Catalytic cracking reaction device is discharged after being exchanged heat with pre-hydrotreating reaction discharging F-5, then Jing catalytic cracking reactions discharging cooler is cold
But, downstream separation unit is delivered to as olefins by catalytic cracking reaction discharging F-6.
Each step parameter is as follows：
After the raw material elder generation, Jing pre-add hydrogen input and output material heat exchanger, pre-add hydrogen cooler, are cooled to 40 DEG C, send into pre- hydrogenation anti-
Answer device；
The operating pressure of the pre-hydrogenator is 2.9MPaG, and reaction inlet temperature is 40 DEG C, and reaction temperature rising is 9 DEG C；
The operating pressure of the catalytic pyrolysis feedstock vaporisation tank is 2.69MPaG, and operation temperature is 130 DEG C；
Pre-hydrotreating reaction of the decompressor after vaporizing discharges as working medium, and pre-hydrotreating reaction discharging is done work in decompressor
Decompression, decompressor are connected with pump by bearing, and bearing is also connected with motor or turbine.Decompressor power output needs work(with pump
Rate is compared, and insufficient section is provided by motor or turbine, and this motor or turbine act also as the power that goes into operation when decompressor is without working medium
Source；
Pre-hydrotreating reaction discharging pressure after decompressor work is 0.36MPaG；
Feed heater operating pressure 0.32MPaG, material side outlet temperature are 575 DEG C；
Catalytic cracking reaction device operating pressure 0.07MPaG, reaction temperature are 575 DEG C；
After the catalytic cracking reaction discharging elder generation, Jing catalytic cracking reaction input and output material heat exchangers, catalytic cracking reaction discharging are cold
But device, is cooled to 40 DEG C, sends into downstream separation unit；
Each material can be exchanged heat with unclassified stores in device, to reduce public work material (such as steam, recirculated water etc.)
Consume.
Each logistics composition is shown in Table 1, and reaction feed preparation system public work is consumed, and comprehensive energy consumption and operating cost are adjusted and seen
Table 3.
Comparative example：
As shown in Fig. 2 a kind of olefins by catalytic cracking system.
Including：Feed pre- hydrogenation unit, pressure-reducing valve, vaporization unit and catalytic cracking reaction unit.Raw material Jing is hydrogenated with list in advance
Unit, after removing the harmful constituents such as alkadienes, alkynes, the decompression of Jing pressure-reducing valves, then Jing after vaporization unit is heated vaporization, into catalysis
Cracking reaction unit, carbon four in raw material and more heavier olefins are converted into propylene and ethylene.
The raw material (F-1) come from upstream is hydrogenated with input and output material heat exchanger 1 and hydrogenation reaction discharging heat exchange cooling pre-, then Jing is pre-
After hydrogenation cooler 2 is cooled to hydrogenation reaction temperature, pre-hydrogenator 3 is mixed into hydrogen F-2.Pre-hydrogenator goes out
Mouth material, a part of Jing are hydrogenated with circulating pump 4 in advance and boost, and are back to pre-add hydrogen cooler 2, used as pre- hydrogenation recycle stock；One
Lease making is hydrogenated with input and output material heat exchanger 1 in advance and is heated up with raw material F-1 heat exchange, is delivered to downstream catalytic as pre-hydrotreating reaction discharging F-3 and is split
Solution unit.Pre-hydrotreating reaction discharges F-3 Jing after the decompression of pressure-reducing valve 5, delivers to catalytic pyrolysis feedstock vaporisation tank 6, in feeding vaporizer 7
After being heated vaporization, Jing feed superheaters 8 are heated to 104 DEG C to gas phase again.Overheated pre-hydrotreating reaction discharging F-5, splits in catalysis
Solution reaction input and output material heat exchanger 10, after heating up with the discharging heat exchange of catalytic cracking reaction device, then Jing feed heaters 11, it is heated to
After reaction temperature, into catalytic cracking reaction device 12.Catalytic cracking reaction device is discharged after being exchanged heat with pre-hydrotreating reaction discharging F-5,
Downstream separation unit is delivered to as olefins by catalytic cracking reaction discharging F-6.
Each step parameter is as follows：
After the raw material elder generation, Jing pre-add hydrogen input and output material heat exchanger, pre-add hydrogen cooler, are cooled to 40 DEG C, send into pre- hydrogenation anti-
Answer device；
The operating pressure of the pre-hydrogenator is 2.9MPaG, and reaction inlet temperature is 40 DEG C, and reaction temperature rising is 9 DEG C；
The pressure-reducing valve operating upstream pressure is 2.69MPaG, and operation temperature is 130 DEG C, and valve outlet pressure is
0.49MPaG；
The operating pressure of catalytic pyrolysis feed surge tank is 0.49MPaG, and operation temperature is 89 DEG C；
The feed superheater outlet temperature is 104 DEG C；
Feed heater operating pressure 0.32MPaG, material side outlet temperature are 575 DEG C；
Catalytic cracking reaction device operating pressure 0.07MPaG, reaction temperature are 575 DEG C；
After the catalytic cracking reaction discharging elder generation, Jing catalytic cracking reaction input and output material heat exchangers, catalytic cracking reaction discharging are cold
But device, is cooled to 40 DEG C, sends into downstream separation unit；
Each logistics composition is shown in Table 2, and reaction feed preparation system public work is consumed, and comprehensive energy consumption and operating cost are adjusted and seen
Table 4.
1 embodiment of the present invention analog result of table
Note：In table, logistics number represents raw material with logistics, i.e. F-1 in corresponding Fig. 4 respectively；F-2 represents hydrogen；F-3 represents pre-
Hydrogenation reaction discharges；F-4 ' represents pre-hydrotreating reaction discharging (decompressor charging) after vaporization；F-5 is represented after vaporizing and reducing pressure
Pre-hydrotreating reaction discharges (i.e. catalytic cracking reaction charging)；F-6 represents catalytic cracking reaction discharging.
2 comparative example analog result of table
Note：In table, logistics number represents raw material with logistics, i.e. F-1 in corresponding Fig. 2 respectively；F-2 represents hydrogen；F-3 represents pre-
Hydrogenation reaction discharges；F-4 represents the pre-hydrotreating reaction discharging after decompression；F-5 represents the pre-hydrotreating reaction after reducing pressure and vaporizing and goes out
Material (i.e. catalytic cracking reaction charging)；F-6 represents catalytic cracking reaction discharging.
Contrast table 1, result shown in table 2 understand that the method for the present invention will not both change pre- Hydroprocessing conditions, and also will not
Change catalytic pyrolysis feed conditions, only in the reaction feed preparation process between pre- hydrogenation and catalytic pyrolysis, the temperature of material
Pressure and phase are changed.
The public work consumption of 3 embodiment of the present invention of table, energy consumption and operating cost statistical form
Note：1 is heated using the middle pressure steam of more than 1.3MPaG, and energy reduced value presses 80kg mark oil/t vaporimeters；
The energy reduced value of 2 electricity is based on 0.26kg mark oil/kW*h.
The consumption of 4 comparative example public work of table, energy consumption and operating cost statistical form
Note：Heated using the low-pressure steam of more than 0.3MPaG, energy reduced value presses 66kg mark oil/t vaporimeters；
3,4 result of contrast table understands that the inventive method unit interval energy consumption reduces 44.15kg mark oil than comparative example；It is single
Position time operation expense can reduce by 236.4 yuan, operate count per year within 8000 hours, can save 189.12 ten thousand yuan of running cost every year.
Also can withdraw at short notice because setting up the investment increment produced by the increase of the equipment such as decompressor and feeding vaporizer wall thickness.
In sum, the method for the present invention can obviously reduce energy consumption, save running cost, with preferable economic worth and
Social effect, is suitably promoted in the industrial production.
Claims (7)
1. a kind of olefins by catalytic cracking reaction unit, including：Feed pre- hydrogenation unit, feedstock vaporisation unit and catalytic cracking reaction
Unit；Feeding pre- hydrogenation unit includes：Pre- hydrogenation input and output material heat exchanger, pre-add hydrogen cooler, pre-hydrogenator and pre- hydrogenation
Circulating pump；Feedstock vaporisation unit includes：Catalytic pyrolysis feedstock vaporisation tank and feeding vaporizer；Catalytic cracking reaction unit includes：
Catalytic cracking reaction input and output material heat exchanger, feed heater, catalytic cracking reaction device and catalytic cracking reaction discharging cooler；Its
It is characterised by：
Described device includes decompressor unit；Decompressor unit be arranged on feedstock vaporisation unit and catalytic cracking reaction unit it
Between；Decompressor unit includes decompressor；
Pre-hydrogenator outlet line is divided into two, and a connection connects pre-add hydrogen cooler after being hydrogenated with circulating pump in advance；It is another
Connect catalytic pyrolysis feedstock vaporisation tank after propping up the pre- hydrogenation input and output material heat exchanger of connection；The connection of catalytic pyrolysis feedstock vaporisation tank top is swollen
Swollen machine, expander outlet connect catalytic cracking reaction after being sequentially connected catalytic cracking reaction input and output material heat exchanger and feed heater
Device.
2. a kind of olefins by catalytic cracking method using olefins by catalytic cracking reaction unit as claimed in claim 1, its feature
It is that methods described includes：
Pre-hydrotreating reaction discharging is not reduced pressure directly to be heated and is vaporized, and after vaporization, Jing decompressors are decompressed to pressure needed for catalytic cracking reaction
Power.
3. olefins by catalytic cracking method as claimed in claim 2, it is characterised in that methods described includes：
(1) raw material is mixed into pre-hydrogenator with hydrogen Jing after heat exchange and cooling down；
(2) pre-hydrogenator outlet material, it is a part of it is boosted after be back to pre-add hydrogen cooler, as pre- hydrogenation recycle
Material；It is a part of to send into catalytic pyrolysis feedstock vaporisation tank Jing after being hydrogenated with input and output material heat exchanger in advance and heat up with raw material heat exchange；
(3) after feeding vaporizer is heated vaporization, catalytic pyrolysis feedstock vaporisation tank gas phase enters decompressor, expansion work decompression
Afterwards, in catalytic cracking reaction input and output material heat exchanger, heat up with the discharging heat exchange of catalytic cracking reaction device, then Jing feed heaters add
Heat, into catalytic cracking reaction device；
(4) after the discharging of catalytic cracking reaction device is exchanged heat with pre-hydrotreating reaction discharging, then Jing catalytic cracking reactions discharging cooler is cold
But, downstream separation unit is delivered to as olefins by catalytic cracking reaction discharging.
4. olefins by catalytic cracking method as claimed in claim 3, it is characterised in that：
After the raw material elder generation, Jing pre-add hydrogen input and output material heat exchanger, pre-add hydrogen cooler, are cooled to 36-60 DEG C, send into pre- hydrogenation anti-
Answer device.
5. olefins by catalytic cracking method as claimed in claim 3, it is characterised in that：
Pre-hydrotreating reaction discharging pressure after decompressor work is 0.05-0.6MPaG；
Pre-hydrotreating reaction of the decompressor after vaporizing discharges as working medium, and pre-hydrotreating reaction discharging is done work in decompressor and subtracted
Pressure.
6. olefins by catalytic cracking method as claimed in claim 3, it is characterised in that：
The catalytic cracking reaction device discharging elder generation Jing catalytic cracking reaction input and output material heat exchangers and pre-hydrotreating reaction discharging heat exchange, then
Jing catalytic cracking reactions discharging cooler, is cooled to 36-60 DEG C, sends into downstream separation unit.
7. the olefins by catalytic cracking method as described in one of claim 3～6, it is characterised in that：
The operating pressure of the pre-hydrogenator is 0.9-7.0MPaG, and reaction temperature is 36-60 DEG C, and reaction temperature rising is 1-50
℃；
The operating pressure of the catalytic pyrolysis feedstock vaporisation tank is 0.6-6.95MPaG, and operation temperature is 40-200 DEG C；
Feed heater operating pressure 0.05-0.6MPaG, material side outlet temperature are 400-600 DEG C；
Catalytic cracking reaction device operating pressure 0.03-0.6MPaG, reaction temperature are 400-600 DEG C.
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| US3730875A (en) * | 1971-02-16 | 1973-05-01 | Universal Oil Prod Co | Combination process for black oil conversion |
| CN101172923A (en) * | 2006-10-31 | 2008-05-07 | 中国石油化工股份有限公司 | Combination technique for producing olefin hydrocarbon with mixed C_4 |
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| FR2940313B1 (en) * | 2008-12-18 | 2011-10-28 | Inst Francais Du Petrole | HYDROCRACKING PROCESS INCLUDING PERMUTABLE REACTORS WITH LOADS CONTAINING 200PPM WEIGHT-2% WEIGHT OF ASPHALTENES |
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| US3730875A (en) * | 1971-02-16 | 1973-05-01 | Universal Oil Prod Co | Combination process for black oil conversion |
| CN101172923A (en) * | 2006-10-31 | 2008-05-07 | 中国石油化工股份有限公司 | Combination technique for producing olefin hydrocarbon with mixed C_4 |
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