CN109957417A - A kind of the modifying process device and modifying process of delayed coking stable gasoline - Google Patents
A kind of the modifying process device and modifying process of delayed coking stable gasoline Download PDFInfo
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- CN109957417A CN109957417A CN201910276058.1A CN201910276058A CN109957417A CN 109957417 A CN109957417 A CN 109957417A CN 201910276058 A CN201910276058 A CN 201910276058A CN 109957417 A CN109957417 A CN 109957417A
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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
- C10G7/00—Distillation of hydrocarbon oils
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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
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/12—Controlling or regulating
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of modifying process device of delayed coking stable gasoline and modifying process.Modifying process device provided by the invention includes: Cutting Tap；The Cutting Tap is connected by reboiler with the stable gasoline outlet of stabilizer tower bottom in the first absorbing-stabilizing system；The first heat-exchanger rig that air inlet is connected with the tower top gas outlet of the Cutting Tap；The second heat-exchanger rig that feed inlet is connected with the tower bottom discharge port of the Cutting Tap.Using above-mentioned modifying process device provided by the invention to delayed coking stable gasoline modifying process, stable gasoline can be divided into two parts, the respectively light petrol of fulvene hydrocarbon content, the heavy petrol of rich virtue potential content, can better meet the use demand of terminator and hydrogenating materials；And the stable gasoline of same amount is divided into two parts, it is used respectively as terminator and hydrogenating materials, saves cost, improve the utility value of stable gasoline.
Description
Technical field
The present invention relates to technical field of petrochemical industry, in particular to a kind of modifying process device of delayed coking stable gasoline
And modifying process.
Background technique
A major issue in fuel production be how by the heavy distillate in crude oil even crude conversion at lightweight
Fuel product.Heavy oil conversion is light oil mainly by following approach: being 1. decomposed into lesser molecule from macromolecular: relying primarily on
Decomposition reaction (such as thermal response and catalysis reaction)；2. being converted to higher H/C composition from low H/C composition: mainly (such as molten by decarburization
Agent depitching, catalytic cracking, coke etc.) and hydrogen (being such as hydrocracked) is added to realize.Coke (referred to as " coking ") is depth heat
Cracking process, and one of the means of processing residual oil, and be the technical process that can uniquely produce petroleum coke, it is based on some industries pair
The specific demand of high-quality petroleum coke, play an important role coking always in petroleum refining industry.
Coking is with poor hydrogen heavy still bottoms (such as heavy oil, decompression residuum, cracked residue or pitch) for raw material, in high temperature
Depth heat cracking reaction is carried out under (400~500 DEG C), by cracking reaction, a part of raw material is made to be converted into carburet hydrogen and light
Matter oil product；Simultaneously because making another part of raw material be converted into coke there are condensation reaction.On the one hand due to raw material weight, contain phase
When the aromatic hydrocarbons of quantity, on the other hand, pyrogenetic reaction condition is harsher, and therefore, condensation reaction accounts for very big specific gravity, generate coke compared with
It is more.
Once used coking method includes: autoclave coking, open hearth coking, contact coking, delayed coking, sulphur in petroleum refining industry
Change coking and flexicoking etc..Wherein, delayed coking is most widely used, and is that oil plant improves yield of light oil and production petroleum
Burnt main means.The effect of delayed coking is to crack heavy oil fraction, polymerize, and generation oil gas, light oil, centre evaporate
Divide oil and coke.Its working principle is that: heavy oil feed heats in tube furnace, using high flow rate (filling the water in boiler tube) and height
Calorific intensity (heater outlet temperature be 500 DEG C), temperature needed for making feedstock oil reach pyrogenetic reaction in the short time in heating furnace,
Then coke tower is quickly entered, pyrogenetic reaction is deferred in heating furnace in coke drum and goes to carry out, therefore, is referred to as to prolong
Slow coking.Specifically, being cut in fractionating column from the oil product that coking reactor comes out, tower top produces rich tail gas of coking plant and coking
Raw gasoline, intermediate lateral line withdrawal function coker gas oil, reaction tower tower bottom output coke.
Containing more alkene in the resulting carburet hydrogen of coking and liquid oil, stability is poor, therefore often as other dresses
Become product after the processing such as the raw material set or hydrogenated purification.Absorbing-stabilizing system is the after-treatment system of delayed coking, purpose
Be using absorb and rectificating method by from fractionating column rich tail gas of coking plant and coker naphtha be separated into coking dry gas (C2Below),
Coking liquefied gas (C3、C4) and qualified stable gasoline.Absorbing-stabilizing system mainly by absorption tower, desorber, stabilizer, again inhale
It receives the ancillary equipments such as tower and corresponding heat exchanger to constitute, is the schematic diagram of absorbing-stabilizing system in the prior art referring to Fig. 1, Fig. 1.Its
Workflow is specific as follows: rich tail gas of coking plant becomes coking dry gas behind absorption tower and reabsorber and (enters oil refining gas stream pipe network
It is used as refinery itself fuel)；Coker naphtha produces coking liquefied gas after desorber and stabilizer and vapour is stablized in coking
Oil.Wherein, gained coking liquefied gas can be used as the raw material production chemical products of fuel and subsequent gas separation unit；Gained coking is stablized
A part of gasoline is back to absorption tower and uses as rich tail gas of coking plant supplement absorbent, another part as product discharger,
It can be used as the riser that terminator is sent into catalytic cracking unit, or the raw material as gasoline hydrogenation uses.
It in the prior art, is usually to be sent directly into catalytic unit as termination after obtaining the stable gasoline product of outlet
Agent uses, or uses directly as hydrogenating materials.And terminator is needed to have higher olefin(e) centent plus hydrogen former in actual use
Material has a higher arene content, however olefin(e) centent is lower in the stable gasoline of absorbing-stabilizing system discharge, arene content is higher,
Practical application request cannot preferably be met for above two purposes.
Summary of the invention
In view of this, the purpose of the present invention is to provide a kind of modifying process device of delayed coking stable gasoline and modifications
Stable gasoline can be divided into olefin(e) centent higher by technique using modifying process device provided by the invention or modifying process
Light petrol and the fragrant higher heavy petrol of potential content, better meet the use demand of terminator or hydrogenating materials.
The present invention provides a kind of modifying process devices of delayed coking stable gasoline, comprising:
Cutting Tap；The Cutting Tap is arranged by the stable gasoline of stabilizer tower bottom in reboiler and the first absorbing-stabilizing system
Outlet is connected；
The first heat-exchanger rig that air inlet is connected with the tower top gas outlet of the Cutting Tap；
The second heat-exchanger rig that feed inlet is connected with the tower bottom discharge port of the Cutting Tap.
In some embodiments of the invention, first heat-exchanger rig includes:
The air cooler that air inlet is connected with the tower top gas outlet of the Cutting Tap；
The water cooler that feed inlet is connected with the discharge port of the air cooler.
In some embodiments of the invention, second heat-exchanger rig includes:
The heating agent water- to-water heat exchanger that feed inlet is connected with the tower bottom discharge port of the Cutting Tap；
The Heat Exchanger in Circulating Water System that feed inlet is connected with the discharge port of the heating agent water- to-water heat exchanger.
In some embodiments of the invention, the Cutting Tap also with the stable gasoline outlet of the second absorbing-stabilizing system
It is connected.
In some embodiments of the invention, further includes:
The buffering return tank that feed inlet is connected with the discharge port of first heat-exchanger rig；
The buffering return tank is connected with light petrol pump；
The light petrol pump is connected to the riser of catalytic cracking unit, and is connected to the feedback outlet of the Cutting Tap.
In some embodiments of the invention, stabilizer of the discharge port of the reboiler also with the first absorbing-stabilizing system
It is connected.
The present invention also provides a kind of modifying process of delayed coking stable gasoline, the technique uses above-mentioned technical proposal
Described in modifying process device, the technique includes:
By the stable gasoline of the stabilizer tower bottom in the first absorbing-stabilizing system through reboiler boil processing again after, be sent into
Cutting Tap；Later, a part in Cutting Tap in stable gasoline is changed into gas phase, is discharged by gas outlet at the top of Cutting Tap, and pass through
First heat-exchanger rig carries out cold treatment, forms light petrol；Another part in Cutting Tap in stable gasoline flows to tower bottom by tower bottom
Discharge port discharge, and cold treatment is carried out through the second heat-exchanger rig, form heavy petrol.
In some embodiments of the invention, it is 150~160 DEG C that the stable gasoline, which is handled through reboiler to temperature,；
The column bottom temperature of the Cutting Tap is 140~145 DEG C, and tower top temperature is 60~70 DEG C.
In some embodiments of the invention, the technique includes:
By the stable gasoline of the stabilizer tower bottom in the first absorbing-stabilizing system through reboiler boil processing again after, be sent into
Cutting Tap；Meanwhile the stable gasoline sent outside from the second absorbing-stabilizing system is sent into Cutting Tap；Later, stablize in Cutting Tap
A part in gasoline is changed into gas phase, is discharged by gas outlet at the top of Cutting Tap, and carries out cold treatment, shape through the first heat-exchanger rig
At light petrol；Another part in Cutting Tap in stable gasoline flows to tower bottom and is discharged by tower bottom discharge port, and fills through the second heat exchange
Carry out cold treatment is set, heavy petrol is formed.
In some embodiments of the invention, the tower top pressure of the Cutting Tap is 0.05~0.09MPa, and tower bottom pressure is
0.09~1.1MPa；
The temperature of the stable gasoline of the stabilizer tower bottom in the first absorbing-stabilizing system is 170~210 DEG C；
The temperature of the stable gasoline sent outside from the second absorbing-stabilizing system is 100~120 DEG C.
The present invention provides a kind of modifying process devices of delayed coking stable gasoline, comprising: Cutting Tap；The Cutting Tap
It is connected by reboiler with the stable gasoline outlet of stabilizer tower bottom in the first absorbing-stabilizing system；Air inlet is cut with described
Cut the first heat-exchanger rig that the tower top gas outlet of tower is connected；Feed inlet be connected with the tower bottom discharge port of the Cutting Tap
Two heat-exchanger rigs.Using above-mentioned modifying process device provided by the invention to delayed coking stable gasoline modifying process, can incite somebody to action
Stable gasoline is divided into two parts, the respectively light petrol of fulvene hydrocarbon content, and the heavy petrol of rich virtue potential content can preferably expire
The use demand of sufficient terminator and hydrogenating materials；And the stable gasoline of same amount is divided into two parts, respectively as terminator
It is used with hydrogenating materials, saves cost, improve the utility value of stable gasoline.
Detailed description of the invention
In order to more clearly explain the embodiment of the invention or the technical proposal in the existing technology, to embodiment or will show below
There is attached drawing needed in technical description to be briefly described, it should be apparent that, the accompanying drawings in the following description is only this
The embodiment of invention for those of ordinary skill in the art without creative efforts, can also basis
The attached drawing of offer obtains other attached drawings.
Fig. 1 is the schematic diagram of absorbing-stabilizing system in the prior art；
Fig. 2 is the modifying process schematic device for the delayed coking stable gasoline that one embodiment of the present of invention provides；
Fig. 3 is that the first absorbing-stabilizing system comes into operation the schematic diagram of stable gasoline；
Fig. 4 is that the second absorbing-stabilizing system comes into operation the schematic diagram of stable gasoline.
Specific embodiment
The present invention provides a kind of modifying process devices of delayed coking stable gasoline, comprising:
Cutting Tap；The Cutting Tap is arranged by the stable gasoline of stabilizer tower bottom in reboiler and the first absorbing-stabilizing system
Outlet is connected；
The first heat-exchanger rig that air inlet is connected with the tower top gas outlet of the Cutting Tap；
The second heat-exchanger rig that feed inlet is connected with the tower bottom discharge port of the Cutting Tap.
Referring to fig. 2, Fig. 2 is that the modifying process device for the delayed coking stable gasoline that one embodiment of the present of invention provides shows
It is intended to；Wherein, 1 is Cutting Tap, and 2 be the first heat-exchanger rig, and 3 be the second heat-exchanger rig, and 4 be reboiler.
The present invention carries out the stable gasoline that absorbing-stabilizing system in the prior art generates by above-mentioned modifying process device
Processing.The present invention is not particularly limited the structure of the absorbing-stabilizing system, using routine well known to those skilled in the art
Absorbing-stabilizing system.Referring to Fig. 1, the process of absorbing-stabilizing system production stable gasoline is as follows in the prior art:
The rich gas that self-dalay coking generates enters liquid separation tank by aerostatic press, and liquid separation tank top rich gas enters rich gas compression
Condensed oil is formed on machine, bottom.Rich gas through compressor compresses to 1.5MPa, isolate after the condensed oil of part with water mixing, washing, then
It is cooled to 50 DEG C through air cooler；Rich gas after cooling is mixed with the gas phase of the rich oil at absorption tower bottom, desorption tower top through rich gas
Cooler is cooled to 40 DEG C and enters high pressure condensation oil tank.The top rich gas of the high pressure condensation oil tank enters absorption tower bottom, and bottom is solidifying
Contracting oil is extracted out by desorber feed pump, into desorber top.The raw gasoline generated from coking fractionating section enters absorption tower the
31 layers of tower tray make absorbent, and partially stabilized gasoline enters absorption the 34th layer of tower tray of tower top and makees supplement absorbent.Compress rich gas self-priming
Receive tower bottom enter, inversely contacted through 34 layers of single overflow tower tray with absorbent, set in the tower there are two middle section flow back: a middle section flow back
Oil is extracted out by one middle section reflux pump of absorption tower, is cooled to 40 DEG C of 23 layers of absorption tower of return towers through one middle section reflux cooler of absorption tower
Disk；Two middle section withdrawing oils are extracted out by two middle section reflux pump of absorption tower, are cooled to 40 DEG C of returns through two middle section reflux cooler of absorption tower
10 layers of absorption tower tower tray.The lean gas of absorption is escaped from tower top, into reabsorber；Absorbent diesel oil comes from coker gas oil water cooling
Device, into reabsorber top；Lean gas is inversely contacted through 30 layers of single overflow tower tray with diesel oil is absorbed from bottom to top, tower bottom condensed oil
To coking fractional distillation column, tower top dry gas to dry gas liquid separation tank, rich diesel oil to the coking richness that absorbs returned from reabsorber tower bottom absorbs
Oil heat exchanger.Absorption tower bottom rich oil is mixed by rich gas of the absorption tower pump extraction after air-cooled with rich gas air cooler.
High pressure condensation tank bottom condensed oil is extracted out by desorber feed pump, enters desorber through steady vapour condensation oil heat exchanger
Top.Contain C2 following components in desorber, reaching tower bottom becomes deethanization gasoline.Desorption bottom reboiler is supplied by wax tailings
To heat as full tower heat source, parses tower overhead gas and mixed with the air-cooled rear rich gas of rich gas air cooler.Tower bottom deethanization gasoline is by stablizing
The extraction of tower feed pump enters 24 layers of tower tray in the middle part of stabilizer after stabilizer feed exchanger and stable gasoline heat exchange.Stabilizer
Top evolution gaseous hydrocarbon divides two-way: entering stabilizer return tank after stabilizer is cooled to and is cooled to 40 DEG C all the way；Another way through heat by
Road regulating valve is directly into return tank of top of the tower is stablized, to control stable tower top pressure.Stablize return tank of top of the tower bottom liquefied gas by
Stablize tower top return pump extraction and divide two-way: being back to stable tower top all the way, as supplement absorbent；Another way is to desulfurization of liquefying
Tower.In brief, stabilizer reboiler makees full tower heat source by wax tailings heat supply, and deethanization gasoline is after stabilizer is fractionated, tower
Bottom removes butane following components, becomes stable gasoline.A part of stable gasoline is sent as product discharger to catalytic cracking
Device makees terminator or as hydrogenating materials, and another part sends absorption tower back to through steady vapour absorbent water cooling, as supplement absorbent.
In above-mentioned process flow, the conditional parameter of delayed coking absorbing-stabilizing system is as follows referring to table 1:
The conditional parameter of 1 delayed coking absorbing-stabilizing system of table
| Control point | Parameter | |
| 1 | Stabilizer tower top pressure, MPa | 0.9~1.2 |
| 2 | Fractionating column column bottom temperature, DEG C | 320~385 |
| 3 | Absorbing tower pressure on top surface, MPa | 0.9~1.2 |
| 4 | Desorber tower top pressure, MPa | 1.0~1.2 |
| 5 | Reabsorber tower top pressure, MPa | 0.8~1.1 |
| 6 | Absorption tower tower top temperature, DEG C | 25~45 |
| 7 | Column overhead temperatures are desorbed, DEG C | 50~70 |
| 8 | Desorber column bottom temperature, DEG C | 130~160 |
| 9 | Reabsorber tower top temperature, DEG C | 30~50 |
| 10 | Stablize column overhead temperatures, DEG C | 40~65 |
| 11 | Stabilizer column bottom temperature, DEG C | 170~210 |
| 12 | Diesel oil absorbent temperature, DEG C | 30~45 |
| 13 | Gasoline absorbent temperature, DEG C | 20~40 |
| 14 | Liquefied gas goes out unit temp, DEG C | 30~45 |
| 15 | Stable gasoline sends temperature outside, DEG C | When direct-furnish: 100~120；When commonly sending outside: 30~45 |
| 16 | Each tower and tank fill level, % | 30~60 |
The stable gasoline for passing through stabilizer tower bottom in reboiler 4 and the first absorbing-stabilizing system according to the present invention, Cutting Tap 1
Outlet is connected.The stable gasoline that first absorbing-stabilizing system generates first after reboiler provides heat source to Cutting Tap, then is sent
Enter Cutting Tap.In some embodiments of the invention, the temperature of the stable gasoline is 170 DEG C~210 DEG C, at reboiler 4
After reason, it is down to 150~160 DEG C.In some embodiments of the invention, the steam conduct of 1.0MPa can be used in the reboiler 4
Heat source.
In some embodiments of the invention, the discharge port of reboiler 4 also with the stabilizer phase of the first absorbing-stabilizing system
Connection.Referring to fig. 2, i.e., the stable gasoline of the first absorbing-stabilizing system divides two-way after reboiler 4 boils processing again: a part of conduct
Cutting Tap 1 is fed to, has not only served as segmentation raw material, but also as the heat source of Cutting Tap 1, regulate and control the temperature of Cutting Tap 1；Another part
It is back to the stabilizer tower bottom of the first absorbing-stabilizing system, as the absorbent of absorbing-stabilizing system after air-cooled water cooling, is kept
System operates normally.Referring to Fig. 3, Fig. 3 is that the first absorbing-stabilizing system comes into operation the schematic diagram of stable gasoline, wherein is inhaled first
(170 DEG C~210 DEG C) interceptions of stable gasoline for receiving stabilizer tower bottom in systems stabilisation are sent into modifying process device of the present invention
The processing of reboiler 4；Through treated the gasoline (150~160 DEG C) of reboiler 4, a part is sent into modifying process device of the present invention
Cutting Tap 1, another part return the first absorbing-stabilizing system in stabilizer, keep system operate normally.
In some embodiments of the invention, water cooler is additionally provided between reboiler 4 and Cutting Tap 1, first absorbs surely
The stable gasoline (170 DEG C~210 DEG C) for determining stabilizer bottom in system, the temperature after reboiler are 150~160 DEG C, then through water
Cooler is cooling, guarantees that feeding temperature is 115~125 DEG C, and then guarantee the thermal balance in Cutting Tap 1, guarantees that Cutting Tap is normally transported
Row.
In a preferred embodiment of the invention, Cutting Tap 1 also with the stable gasoline outlet phase of the second absorbing-stabilizing system
Connection.Referring to fig. 2, i.e. the stable gasoline that the second absorbing-stabilizing system is sent outside handles without reboiler and is sent directly into Cutting Tap 1, with
Above-mentioned reboiler treated stable gasoline collectively as Cutting Tap 1 charging, by the stable gasoline of two sets of absorbing-stabilizing systems
Cutting Tap 1 is sent into a manner of hot feed collectively as raw material.In some embodiments, referring to fig. 4, Fig. 4 is the second Vapor recovery unit
System comes into operation the schematic diagram of stable gasoline, the stable gasoline that the second absorbing-stabilizing system generates, and a part is adjusted through air-cooled, water cooling
To 100~120 DEG C of the temperature sent outside, then the Cutting Tap 1 sent into modifying process device of the present invention, and the first Vapor recovery unit is come from
System and through reboiler handle stable gasoline mixing as Cutting Tap feed；The temperature of the charging is preferably 115~125
℃.Another part water cooled can be handled, and return to the second absorbing-stabilizing system as supplement absorbent.Using two sets of stable absorption systems
System can obtain more stable gasolines parallel to obtain fulvene the hydrocarbon component and rich aromatic component, meanwhile, it is absorbed using second
The stable gasoline of systems stabilisation regulates and controls the temperature into Cutting Tap, to guarantee Cutting Tap feeding temperature for 115~125 DEG C.If only
Using the first absorbing-stabilizing system, the temperature after reboiler is 150~160 DEG C, to guarantee 115~125 DEG C of inlet temperature of stabilizer, then
It needs to increase water cooler to cool down, to guarantee the thermal balance in Cutting Tap 1, guarantees that Cutting Tap operates normally.
In some embodiments of the invention, Cutting Tap 1 is connected with the stable gasoline outlet of two sets of absorbing-stabilizing systems
When logical, the discharge port of reboiler 4 is connected with the stabilizer of the first absorbing-stabilizing system；That is the stabilization of the first absorbing-stabilizing system
Gasoline divides two-way after the processing of reboiler 4: a part has not only served as segmentation raw material, but also as cutting as Cutting Tap 1 is fed to
The heat source of tower 1 regulates and controls the temperature of Cutting Tap 1；Another portion is back to the stabilizer tower bottom of the first absorbing-stabilizing system, through air-cooled water
Absorbent after cold as absorbing-stabilizing system keeps system to operate normally.
In the present invention, after stable gasoline enters Cutting Tap 1, height evaporates an ingredient downlink and deposits to the tower bottom of Cutting Tap 1, low to evaporate
Point ingredient is heated to be changed into gas phase and along 1 uplink of Cutting Tap, i.e., by Cutting Tap 1 by the component segmentation in stable gasoline at uplink
Light petrol and downlink heavy petrol.The present invention regulates and controls the feeding temperature of stable gasoline by reboiler 4, and then controls Cutting Tap
Stable gasoline component is split by the temperature in 1.As described above, being handled in some embodiments of the present invention through reboiler 4
Stable gasoline temperature afterwards is 150~160 DEG C, 115~125 DEG C is down to by temperature after water recirculator, using the temperature
Under stable gasoline as charging, in conjunction with the size of Cutting Tap 1, the negative of cutting tower bottom reboiler 4 is reduced in a manner of hot feed
Lotus makes the column bottom temperature of Cutting Tap 1 reach 140~145 DEG C, and tower top temperature reaches 60~70 DEG C.In preferred implementation of the invention
It is 150~160 DEG C through treated the stable gasoline temperature of reboiler 4 in example；Using stable gasoline at this temperature be used as into
Material, mix with the stable gasoline of the second absorbing-stabilizing system, 115~125 DEG C of feeding temperature of control, in conjunction with the size of Cutting Tap 1,
The load that cutting tower bottom reboiler 4 is reduced in a manner of hot feed, makes the column bottom temperature of Cutting Tap 1 reach 140~145 DEG C, tower
Top temperature reaches 60~70 DEG C, thus the stable gasoline that Cutting Tap 1 will be entered in 70 DEG C of progress component segmentations, evaporate o'clock 70 DEG C with
Under constitutional changes be exhaust outlet discharge of the gas phase along the top of Cutting Tap 1, become the light petrol rich in olefinic component, can send to urging
Change cracking unit as terminator；The component evaporated o'clock at 70 DEG C or more sinks to 1 tower bottom of Cutting Tap, becomes the weight rich in the latent ingredient of virtue
Gasoline can be used as hydrogenating materials.In some implementations of the invention, the size of Cutting Tap 1 is 2200mm (diameter) × 33700mm
(height).
Why the present invention selects that treated that stable gasoline temperature is 150~160 DEG C by reboiler 4, makes Cutting Tap 1
Stable gasoline is subjected to 70 DEG C of cuttings, is that the analysis that studied for a long period of time due to applicant finds that stable gasoline contains at 70 DEG C with alkene
The optimal partition point of amount and fragrant potential content；Specifically, being absorbed respectively with the delayed coking that stable gasoline yield is 800,000 tons/year steady
Stable gasoline (being abbreviated as the steady vapour of I coking) and the yield of system production are determined for 1,000,000 tons/year of delayed coking absorbing-stabilizing system
The stable gasoline (being abbreviated as the steady vapour of II coking) of production carry out PONA analysis (above-mentioned delayed coking absorbing-stabilizing system structure referring to
Fig. 1), as a result referring to table 2.
The PONA of 2 coker gasoline of table is analyzed
As can be seen from the above table, for two sets of absorbing-stabilizing systems, though it may be due to unit scale or coking raw material etc.
Difference can make the ingredient of the stable gasoline of production slightly have difference, but its component distributing trend is consistent, and alkene contains in component before 70 DEG C
Amount is higher, and fragrant potential content is higher in component after 70 DEG C, therefore carries out component cutting to stable gasoline at 70 DEG C, obtains olefin(e) centent
Higher light petrol and the higher heavy petrol of fragrant potential content, make respectively as the terminator and hydrogenating materials of catalytic cracking unit
With.
According to the present invention, the tower top gas outlet of Cutting Tap 1 is communicated with the first heat-exchanger rig 2.It will by the first heat-exchanger rig 2
The gas phase cooling transformation being discharged at the top of Cutting Tap 1 is fluid oil.
In some embodiments of the invention, adjusting is provided in connecting pipe between Cutting Tap 1 and the first heat-exchanger rig 2
Valve, the tower top air pressure for controlling gas phase flow rate by the regulating valve, and then controlling Cutting Tap 1 are 0.05~0.09MPa, tower bottom air pressure
For 0.09~1.1MPa；Control is conducive to the dial-out of 70 DEG C of following components low energy consumption under the air pressure conditions.
In some embodiments of the invention, the first heat-exchanger rig 2 includes: that the tower top of air inlet and the Cutting Tap 1 goes out
The air cooler 2-1 that port is connected；The water cooler 2-2 that feed inlet is connected with the discharge port of the air cooler 2-1.By Cutting Tap
1 top be discharged gas phase is successively air-cooled and water cooling, be down to suitable temperature step by step.In some embodiments, air cooler 2-1 is first passed through
Gas phase temperature is down to 50~54 DEG C, most of gas phase is cooled to liquid, then 20 are further cooled to by water cooler 2-2~
40 DEG C, stable liquid light petrol is formed completely.
In some embodiments of the invention, the discharge port of first heat-exchanger rig 2 is also connected with buffering return tank 5
(referring to fig. 2), for receiving the rich olefins light petrol of storage the first heat-exchanger rig 2 discharge.
In some embodiments of the invention, the buffering return tank 5 is also connected with light petrol and pumped for 6 (referring to fig. 2), described
Light petrol pump 6 is connected to the riser of catalytic cracking unit, and is connected to the feedback outlet of the Cutting Tap.Pass through light petrol pump 6
The rich olefins light petrol in return tank will be buffered to send out, on the one hand send part light petrol to the riser of catalytic cracking unit,
As terminator, part light petrol is on the other hand recycled to Cutting Tap 1, for the temperature in assistant regulating and controlling Cutting Tap 1.
According to the present invention, the tower bottom discharge port of Cutting Tap 1 is communicated with the second heat-exchanger rig 3.It will by the second heat-exchanger rig 3
The high temperature heavy petrol of 1 tower bottom of Cutting Tap discharge is cooled to stable low temperature heavy petrol.
In some embodiments of the invention, second heat-exchanger rig 3 includes: the tower of feed inlet Yu the Cutting Tap 1
The heating agent water- to-water heat exchanger 3-1 that bottom discharge port is connected；Feed inlet is followed with what the discharge port of the heating agent water- to-water heat exchanger 3-1 was connected
Ring water- to-water heat exchanger 3-2.The high temperature heavy petrol that 1 tower bottom of Cutting Tap is discharged successively is exchanged heat, is down to suitable temperature step by step.In some realities
It applies in example, first passes through heating agent water- to-water heat exchanger 3-1 and cool the temperature to 80~90 DEG C, recycling water- to-water heat exchanger 3-2 is further cooled to
20~40 DEG C, form stable low temperature heavy petrol.
In some embodiments of the invention, it is also connected with heavy petrol pump 7 between Cutting Tap 1 and the second heat-exchanger rig 3, uses
The second heat-exchanger rig 3 is pumped in the heavy petrol that 1 tower bottom of Cutting Tap is discharged.
In some embodiments of the invention, the tower bottom discharge port of Cutting Tap 1 is also connected with the feedback outlet of reboiler 4,
Be divided into two-way from the heavy petrol that Cutting Tap bottom 1 is discharged: a part is sent to the second heat-exchanger rig 3, and another part sends reboiler 4 back to
It is handled, then sends Cutting Tap 1 back to again as heat source.
In some embodiments of the invention, it is provided with controlling valve on each connecting pipe, respective tube is realized by controlling valve
The closure conducting in road and the regulation of mass flow, those skilled in the art can be adjusted according to the demand in actual motion.
In summary, using modifying process device provided by the invention, stable gasoline can be divided into olefin(e) centent compared with
High light petrol and the higher heavy petrol of fragrant potential content, better meets the use demand of terminator and hydrogenating materials.
The present invention also provides a kind of modifying process of delayed coking stable gasoline, the technique uses above-mentioned technical proposal
Described in modifying process device, the technique includes:
By the stable gasoline of the stabilizer tower bottom in the first absorbing-stabilizing system through reboiler boil processing again after, be sent into
Cutting Tap；Later, a part in Cutting Tap in stable gasoline is changed into gas phase, is discharged by gas outlet at the top of Cutting Tap, and pass through
First heat-exchanger rig carries out cold treatment, forms light petrol；Another part in Cutting Tap in stable gasoline flows to tower bottom by tower bottom
Discharge port discharge, and cold treatment is carried out through the second heat-exchanger rig, form heavy petrol.
In the present invention, in first absorbing-stabilizing system temperature of the stable gasoline of stabilizer tower bottom be preferably 170~
210℃.After reboiler is handled, it is preferably dropped to 150~160 DEG C.The column bottom temperature of the Cutting Tap is preferably 140~145 DEG C,
Tower top temperature is preferably 60~70 DEG C.
The tower top pressure of the Cutting Tap is preferably 0.05~0.09MPa, and tower bottom pressure is preferably 0.09~1.1MPa.
Structure, cooling temperature of first heat-exchanger rig and the second heat-exchanger rig etc. is and described in above-mentioned technical proposal
Unanimously, details are not described herein.
In some embodiments of the invention, changed using the stable gasoline of two sets of absorbing-stabilizing systems as charging
Matter, technique are as follows: by the stable gasoline of the stabilizer tower bottom in the first absorbing-stabilizing system through reboiler boil processing again after,
It is sent into Cutting Tap；Meanwhile the stable gasoline sent outside from the second absorbing-stabilizing system is sent into Cutting Tap；Later, in Cutting Tap
A part in stable gasoline is changed into gas phase, is discharged by gas outlet at the top of Cutting Tap, and carries out cold place through the first heat-exchanger rig
Reason forms light petrol；Another part in Cutting Tap in stable gasoline flows to tower bottom and is discharged by tower bottom discharge port, and changes through second
Thermal carries out cold treatment, forms heavy petrol.In the present invention, the temperature for the stable gasoline that second absorbing-stabilizing system is sent outside
Preferably 100~120 DEG C.The device structure and treatment conditions etc. that remaining step uses are with described in above-mentioned technical proposal one
It causes, details are not described herein.
For a further understanding of the present invention, the preferred embodiment of the invention is described below with reference to embodiment, still
It should be appreciated that these descriptions are only further explanation the features and advantages of the present invention, rather than to the claims in the present invention
Limitation.
Embodiment 1
It, will be in the first absorbing-stabilizing system (yield be 1,000,000 tons/year) using modifying process device shown in Fig. 2
The stable gasoline (170~210 DEG C) of stabilizer tower bottom is down to 150 DEG C after the processing of reboiler 4, is sent into Cutting Tap 1, cutting
1 height of tower is having a size of 2200 × 33700mm；Meanwhile it will be sent outside from the second absorbing-stabilizing system (yield is 800,000 tons/year)
(100~120 DEG C) feeding Cutting Taps 1 of stable gasoline, the mixing of two strands of materials enters Cutting Tap 1, mixture in a manner of hot feed
Temperature is 115~125 DEG C.Later, a part in Cutting Tap 1 in stable gasoline is changed into gas phase, the row of passing through along Cutting Tap 1
Port discharge controls gas phase flow rate by the regulating valve between Cutting Tap 1 and the first heat-exchanger rig 2 on connecting pipe, and then makes
The tower top pressure of Cutting Tap 1 is 0.05~0.09MPa, and tower bottom pressure is 0.09~1.1MPa；The gas being discharged by 1 tower top of Cutting Tap
Xiang Xianjing air cooler 2-1 is cooled to 50 DEG C, then water cooled device is cooled to 30 DEG C；Into reflux surge tank 5, the as light vapour of low-temperature stabilization
Oil can be pumped by light petrol and send a part of light petrol pump 6 to the riser of catalytic cracking unit as terminator, by another portion
Divide the temperature for being pumped to Cutting Tap 1 for assistant regulating and controlling Cutting Tap 1.Meanwhile 1 tower bottom of Cutting Tap discharge stable gasoline (140~
145 DEG C) it is pumped to heating agent water- to-water heat exchanger 3-1 by heavy petrol pump 7 and is cooled to 85 DEG C, then it is cooled to 30 DEG C through Heat Exchanger in Circulating Water System 3-2,
As low-temperature stabilization heavy petrol, it can be used as hydrogenating materials.
The material of used raw material and product is distributed referring to table 3；Products obtained therefrom specification is referring to table 4.
The distribution of the material of 3 raw material of table and product
4 product specification of table
Embodiment 2
Comparative example is set: by from the first absorbing-stabilizing system (yield be 1,000,000 tons/year) stable gasoline (170~
210 DEG C) first it is cooled to 50 DEG C through air cooler 2-1, then water cooled device is cooled to 30 DEG C, obtains low temperature gasline.
The gasoline that comparative example and embodiment 1 obtain is subjected to constituent analysis respectively, as a result referring to table 5.
5 embodiment 1 of table and the gasolene ingredient of comparative example are analyzed
In the stable gasoline of absorbing-stabilizing system output it can be seen from 5 test result of table, olefin(e) centent 29.55%,
Rich potential content is 18.45%, and when terminator as catalytic unit, olefin(e) centent is lower, as hydrogenating materials in use, Fu Qian
Content is lower.And after modifying process device provided by the invention modification, stable gasoline can be divided into two parts, respectively
The light petrol of fulvene hydrocarbon content (44.77%), the heavy petrol of rich virtue potential content (21.40%), can better meet terminator
With the use demand of hydrogenating materials；And the stable gasoline of same amount is divided into two parts, respectively as terminator and plus hydrogen original
Material uses, and saves cost, improves the utility value of stable gasoline.
Used herein a specific example illustrates the principle and implementation of the invention, and above embodiments are said
It is bright to be merely used to help understand method and its core concept of the invention, including best mode, and but also this field is appointed
What technical staff can practice the present invention, including any device or system of manufacture and use, and implement the method for any combination.
It should be pointed out that for those skilled in the art, it without departing from the principle of the present invention, can also be right
Some improvement and modification can also be carried out by the present invention, and these improvements and modifications also fall within the scope of protection of the claims of the present invention.This hair
The range of bright patent protection is defined by the claims, and may include those skilled in the art it is conceivable that other implementations
Example.If these other embodiments, which have, is similar to the structural element of claim character express, or if they include with
Equivalent structural elements of the character express of claim without essence difference, are wanted then these other embodiments should also be included in right
In the range of asking.
Claims (10)
1. a kind of modifying process device of delayed coking stable gasoline characterized by comprising
Cutting Tap；The stable gasoline outlet that the Cutting Tap passes through stabilizer tower bottom in reboiler and the first absorbing-stabilizing system
It is connected；
The first heat-exchanger rig that air inlet is connected with the tower top gas outlet of the Cutting Tap；
The second heat-exchanger rig that feed inlet is connected with the tower bottom discharge port of the Cutting Tap.
2. modifying process device according to claim 1, which is characterized in that first heat-exchanger rig includes:
The air cooler that air inlet is connected with the tower top gas outlet of the Cutting Tap；
The water cooler that feed inlet is connected with the discharge port of the air cooler.
3. modifying process device according to claim 1 or 2, which is characterized in that second heat-exchanger rig includes:
The heating agent water- to-water heat exchanger that feed inlet is connected with the tower bottom discharge port of the Cutting Tap；
The Heat Exchanger in Circulating Water System that feed inlet is connected with the discharge port of the heating agent water- to-water heat exchanger.
4. modifying process device according to claim 1, which is characterized in that the Cutting Tap also with the second Vapor recovery unit system
The stable gasoline outlet of system is connected.
5. modifying process device according to claim 1 or 2, which is characterized in that further include:
The buffering return tank that feed inlet is connected with the discharge port of first heat-exchanger rig；
The buffering return tank is connected with light petrol pump；
The light petrol pump is connected to the riser of catalytic cracking unit, and is connected to the feedback outlet of the Cutting Tap.
6. modifying process device according to claim 1, which is characterized in that the discharge port of the reboiler is also inhaled with first
The stabilizer for receiving systems stabilisation is connected.
7. a kind of modifying process of delayed coking stable gasoline, which is characterized in that the technique is appointed using in claim 1~6
Modifying process device described in one, the technique include:
By the stable gasoline of the stabilizer tower bottom in the first absorbing-stabilizing system through reboiler boil processing again after, be sent into cutting
Tower；Later, a part in Cutting Tap in stable gasoline is changed into gas phase, is discharged by gas outlet at the top of Cutting Tap, and through first
Heat-exchanger rig carries out cold treatment, forms light petrol；Another part in Cutting Tap in stable gasoline flows to tower bottom and is discharged by tower bottom
Mouth discharge, and cold treatment is carried out through the second heat-exchanger rig, form heavy petrol.
8. modifying process according to claim 7, which is characterized in that the stable gasoline, which is handled through reboiler to temperature, is
150~160 DEG C；
The column bottom temperature of the Cutting Tap is 140~145 DEG C, and tower top temperature is 60~70 DEG C.
9. modifying process according to claim 7, which is characterized in that the technique includes:
By the stable gasoline of the stabilizer tower bottom in the first absorbing-stabilizing system through reboiler boil processing again after, be sent into cutting
Tower；Meanwhile the stable gasoline sent outside from the second absorbing-stabilizing system is sent into Cutting Tap；Later, stable gasoline in Cutting Tap
In a part be changed into gas phase, be discharged, and carry out cold treatment through the first heat-exchanger rig, formed light by gas outlet at the top of Cutting Tap
Gasoline；Another part in Cutting Tap in stable gasoline flows to tower bottom and is discharged by tower bottom discharge port, and through the second heat-exchanger rig into
Row cold treatment forms heavy petrol.
10. modifying process according to claim 7, which is characterized in that the tower top pressure of the Cutting Tap be 0.05~
0.09MPa, tower bottom pressure are 0.09~1.1MPa；
The temperature of the stable gasoline of the stabilizer tower bottom in the first absorbing-stabilizing system is 170~210 DEG C；
The temperature of the stable gasoline sent outside from the second absorbing-stabilizing system is 100~120 DEG C.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101302436A (en) * | 2008-06-30 | 2008-11-12 | 天津大学 | Catalytic cracking absorption stabilization system having gasoline cutting and process producing more propene and reducing alkene |
| CN101531919A (en) * | 2009-04-21 | 2009-09-16 | 天津大学 | Energy-saving device and operation process for absorption-stabilization system |
| CN107216913A (en) * | 2017-07-10 | 2017-09-29 | 中山大学 | A kind of catalytic cracking Vapor recovery unit method and its device |
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2019
- 2019-04-08 CN CN201910276058.1A patent/CN109957417B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101302436A (en) * | 2008-06-30 | 2008-11-12 | 天津大学 | Catalytic cracking absorption stabilization system having gasoline cutting and process producing more propene and reducing alkene |
| CN101531919A (en) * | 2009-04-21 | 2009-09-16 | 天津大学 | Energy-saving device and operation process for absorption-stabilization system |
| CN107216913A (en) * | 2017-07-10 | 2017-09-29 | 中山大学 | A kind of catalytic cracking Vapor recovery unit method and its device |
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