CN109679679A - A kind of heavy aromatics industrial process - Google Patents
A kind of heavy aromatics industrial process Download PDFInfo
- Publication number
- CN109679679A CN109679679A CN201910030994.4A CN201910030994A CN109679679A CN 109679679 A CN109679679 A CN 109679679A CN 201910030994 A CN201910030994 A CN 201910030994A CN 109679679 A CN109679679 A CN 109679679A
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- Prior art keywords
- oil
- solvent
- tower
- furfural
- extract
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Classifications
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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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/02—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents with two or more solvents, which are introduced or withdrawn separately
- C10G21/04—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents with two or more solvents, which are introduced or withdrawn separately by introducing simultaneously at least two immiscible solvents counter-current to each other
-
- 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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
- C10G21/12—Organic compounds only
- C10G21/16—Oxygen-containing compounds
-
- 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
- C10G2400/30—Aromatics
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- Chemical & Material Sciences (AREA)
- 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 invention discloses a kind of heavy aromatics industrial processes, it include: feedstock processing part, Aromatics Extractive Project part, Solvent recovery portion, solvent processing part and public work part, described device is that raw material carries out Aromatics Extractive Project after flashing using FCC recycle oil (slurry oil): being raffinated oil because arene content is low as the preferable raw material Returning catalyticing cracking device of quality or carrying device；Extraction oil obtains the heavy arene of high-purity after distilling, it is sold as chemical products, the device is stripped raw material using two kinds of solvents, and saturated hydrocarbons and aromatic hydrocarbons, colloid, asphalitine in FCC recycle oil (slurry oil) is made to reach optimal separating effect.
Description
Technical field
The present invention relates to a kind of heavy aromatics industrial processes, and in particular to heavy aromatics and wax oil extract isolation technics.
Background technique
For the conversion ratio for improving heavy oil, heavy oil catalytic cracking uses the mode of operation of the full freshening of recycle oil.Due to recycle oil
In heavy aromatics be coke precursor, green coke amount increases during recycle freshening, causes to burn running at full capacity, and device is transported
Row is difficult, it has to the operation of device is maintained by externally extracting oil mode.
Currently, the starting point of the project is to take out using the recycle oil in FCCU as the raw material of aromatic extraction unit through solvent
Raffinating oil after mentioning returns to FCCU as catalytically cracked material and carries out catalytic cracking reaction, and extraction oil is then used as chemical products pin
It sells, since the chemical composition and chemical property of recycle oil and slurry oil are very close, the weight virtue of green coke will be easy in recycle oil
Hydrocarbon extraction, it is possible to reduce the green coke amount of FCCU reduces the carbon-burning load of regenerator, and then cancels externally extracting oil, industrial practice industry
It was demonstrated that the processing capacity of FCCU can be improved in the case where carbon-burning load is constant after extracting aromatic hydrocarbons out by freshening oil extraction
15% or so.In order to eliminate above-mentioned bottleneck problem, the present invention develops Aromatic Extraction Process and carries out solvent separation to recycle oil, and
Extraction heavy aromatics is comprehensively utilized.
Summary of the invention
The purpose of the present invention is to overcome above-mentioned the deficiencies in the prior art, providing a kind of heavy aromatics industrial process, this
Ecology production. art provided by scheme can be realized heavy aromatics and separate with wax oil Rapid extraction, and oil product processing benefit has been greatly optimized
Use structure.
In order to achieve the above objectives, the present invention adopts the following technical scheme: a kind of heavy aromatics industrial process, comprising:
Feedstock processing part, Aromatics Extractive Project part, Solvent recovery portion, solvent processing part and public work part, the producer
Method raw material can be realized by method one and method two, and according to feedstock oil source, feedstock oil is catalytic diesel oil, FCC heavy diesel oil, returns
One or several the single composition of oil refining and lightweight slurry oil etc.,
Method one:
Raw material recycle oil and bavin fraction is urged, is mixed with natural proportion；
Method two:
Raw material recycle oil urges bavin heavy distillat and catalytic slurry to mix.
The feedstock processing part, the mixed raw material from tank field enter feedstock oil stripper, strip at reduced pressure conditions
Out after light fraction oil, enter extracting part as charging.Tower top oil gas is cold through steam jet ejector, stripping tower top condensate cooler
After solidifying cooling, into stripping return tank of top of the tower, light component is extracted out by feedstock oil stripper reflux pump, and a part send original as flowing back
Expect oil and gas stripper overhead, another part is as product tank sending area.
The extracting part: after feedstock oil stripping tower bottom material is by the pump pressurization of feedstock oil stripper, into the middle part of extraction tower,
Wet furfural pressurizes from furfural liquid separation tank furfural feed pump, into extraction tower top；Two solvents are from two solvent tank solvent feeds
After pump pressurization, it is sent into extraction tower lower part；Feedstock oil inversely contacts in tower with furfural, two solvents, carries out liquid-liquid extraction, furfural
The heavy aromatics in feedstock oil is extracted from top to bottom, and two solvents extract light aromatics and alkane in furfural extract out from bottom to top
Hydrocarbon, extracts column overhead raffinate and tower bottom Extract respectively enters Solvent recovery portion.
The solvent recovery and the raffinate for handling part exchange heat through heat exchanger to 180-230 DEG C from extracting column overhead from pressure
Afterwards, into raffinate destilling tower, steam stripping is blown by tower bottom and goes out two solvents, raffinated oil from after the pressurization of tower bottom raffinate oil pump,
It is cooled to 40-80 DEG C through pumping cooler to send to tank field, the solvent vapo(u)r flowed out from raffinate distillation tower top is steamed through raffinate
It evaporates after overhead condenser is cooled to 20-50 DEG C, into vacuum tank, condensate liquid in vacuum tank is from flowing into solvent liquid separation tank.
After the extraction tower tower bottom Extract pumps up, heated device exchanges heat to after 200-235 DEG C, steams into Extract
Tower is sent out, tower bottom liquid is from pressure after heat exchanger exchanges heat to 225-265 DEG C, and into Extract destilling tower, solvent vapo(u)r is steamed from Extract
Column overhead outflow is sent out, after Extract evaporation overhead condenser is cooled to 20-60 DEG C, into solvent liquid separation tank, the extraction oil is used
Extract out oil pump from Extract destilling tower tower bottom extraction pressurization after, through Extract-extraction oil heat exchanger, extraction oil-furfural heat exchanger,
Extraction oil cooler, which is cooled to 20-60 DEG C and send to described in tank field, to be steamed from the solvent vapo(u)r that Extract distillation tower top flows out through Extract
It evaporates after overhead condenser is cooled to 20-60 DEG C, into vacuum tank, condensate liquid in vacuum tank is from flowing into solvent liquid separation tank.
It is described into the furfural of solvent liquid separation tank, the sedimentation separation in knockout drum of two solvents and water, aqueous solution containing aldehyde gravity flow
Enter furfural liquid separation tank, the aqueous solution containing two solvents enters two solvent tanks, furfural and water and further separates in furfural liquid separation tank, water
Mutually from two solvent tanks are flowed into, furfural is sent after furfural pump pressurization to extraction tower, after two solvents and water separate in two solvent tanks, two
Solvent send to extraction tower after solvent feed pump pressurization and is recycled, and send dehydrating tower recycling design containing aqueous solvent.
The dehydration tower top enters solvent knockout drum, tower after dehydration overhead condenser is cooled to 20-80 DEG C containing solvent vapo(u)r
After bottom sewage is pressurizeed with sewage pump, the carrying device after sewage cooler is cooling.
The furfural of the recycling, two solvents are refined by solvent refining tower interruption respectively according to its quality condition,
After separating in tower into the furfural of solvent refining tower or two solvents, top gaseous phase is condensed through solvent refining overhead condenser and is cooled down
Enter furfural liquid separation tank or two solvent tanks afterwards, tower bottom heavy diesel fuel component heavy constituent pumping goes out to send to tank field, which sets built-in
Tower bottom heater and tower top cooler.
The beneficial effects of the present invention are: the device is stripped raw material using two kinds of solvents, make FCC recycle oil (oil
Slurry) in saturated hydrocarbons and aromatic hydrocarbons, colloid, asphalitine reach optimal separating effect.
Detailed description of the invention
Fig. 1 is the work flow diagram of process units of the invention；
Wherein, feedstock processing part is that raw material preprocessing device, Aromatics Extractive Project part are attached most importance to aromatics extraction unit, includes chaff
Aldehyde and two solvent extraction units, solvent recovery and processing unit subpackage contain the purification reuse unit and heavy aromatics of two solvents and furfural
It include the units such as water, electricity, gas, wind, the heat of the device with wax oil separator, public work part.
Specific embodiment
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, it is obtained by those of ordinary skill in the art without making creative efforts every other
Embodiment shall fall within the protection scope of the present invention.
A kind of heavy aromatics industrial process and the device for implementing this method, comprising: feedstock processing part, Aromatics Extractive Project portion
Divide, Solvent recovery portion, solvent processing part and public work part, the production method raw material can pass through method one and method
Two realize, according to feedstock oil source, feedstock oil be the single of catalytic diesel oil, FCC heavy diesel oil, recycle oil and lightweight slurry oil etc. or
Several compositions, the raw material oil nature are as shown in table 1.
Method one:
Raw material recycle oil and bavin fraction is urged, is mixed with natural proportion；
Method two:
Raw material recycle oil urges bavin heavy distillat and catalytic slurry to mix.
1 raw material oil nature of table
Embodiment 1:
The feedstock processing part, the mixed raw material from tank field enter feedstock oil stripper, strip at reduced pressure conditions
Out after light fraction oil, enter extracting part as charging.Tower top oil gas is cold through steam jet ejector, stripping tower top condensate cooler
After solidifying cooling, into stripping return tank of top of the tower, light component is extracted out by feedstock oil stripper reflux pump, and a part send original as flowing back
Expect oil and gas stripper overhead, another part is as product tank sending area.
The extracting part: after feedstock oil stripping tower bottom material is by the pump pressurization of feedstock oil stripper, into the middle part of extraction tower,
Wet furfural pressurizes from furfural liquid separation tank furfural feed pump, into extraction tower top；Two solvents are from two solvent tank solvent feeds
After pump pressurization, it is sent into extraction tower lower part；Feedstock oil inversely contacts in tower with furfural, two solvents, carries out liquid-liquid extraction, furfural
The heavy aromatics in feedstock oil is extracted from top to bottom, and two solvents extract light aromatics and alkane in furfural extract out from bottom to top
Hydrocarbon, extracts column overhead raffinate and tower bottom Extract respectively enters Solvent recovery portion.
The solvent recovery and the raffinate for handling part exchange heat through heat exchanger to 180-230 DEG C from extracting column overhead from pressure
Afterwards, into raffinate destilling tower, steam stripping is blown by tower bottom and goes out two solvents, raffinated oil from after the pressurization of tower bottom raffinate oil pump,
It is cooled to 40-80 DEG C through pumping cooler to send to tank field, the solvent vapo(u)r flowed out from raffinate distillation tower top is steamed through raffinate
It evaporates after overhead condenser is cooled to 20-50 DEG C, into vacuum tank, condensate liquid in vacuum tank is from flowing into solvent liquid separation tank.
After the extraction tower tower bottom Extract pumps up, heated device exchanges heat to after 200-235 DEG C, steams into Extract
Tower is sent out, tower bottom liquid is from pressure after heat exchanger exchanges heat to 225-265 DEG C, and into Extract destilling tower, solvent vapo(u)r is steamed from Extract
Column overhead outflow is sent out, after Extract evaporation overhead condenser is cooled to 20-60 DEG C, into solvent liquid separation tank, the extraction oil is used
Extract out oil pump from Extract destilling tower tower bottom extraction pressurization after, through Extract-extraction oil heat exchanger, extraction oil-furfural heat exchanger,
Extraction oil cooler, which is cooled to 20-60 DEG C and send to described in tank field, to be steamed from the solvent vapo(u)r that Extract distillation tower top flows out through Extract
It evaporates after overhead condenser is cooled to 20-60 DEG C, into vacuum tank, condensate liquid in vacuum tank is from flowing into solvent liquid separation tank.
It is described into the furfural of solvent liquid separation tank, the sedimentation separation in knockout drum of two solvents and water, aqueous solution containing aldehyde gravity flow
Enter furfural liquid separation tank, the aqueous solution containing two solvents enters two solvent tanks, furfural and water and further separates in furfural liquid separation tank, water
Mutually from two solvent tanks are flowed into, furfural is sent after furfural pump pressurization to extraction tower, after two solvents and water separate in two solvent tanks, two
Solvent send to extraction tower after solvent feed pump pressurization and is recycled, and send dehydrating tower recycling design containing aqueous solvent.
The dehydration tower top enters solvent knockout drum, tower after dehydration overhead condenser is cooled to 20-80 DEG C containing solvent vapo(u)r
After bottom sewage is pressurizeed with sewage pump, the carrying device after sewage cooler is cooling.
The furfural of the recycling, two solvents are refined by solvent refining tower interruption respectively according to its quality condition,
After separating in tower into the furfural of solvent refining tower or two solvents, top gaseous phase is condensed through solvent refining overhead condenser and is cooled down
Enter furfural liquid separation tank or two solvent tanks afterwards, tower bottom heavy diesel fuel component heavy constituent pumping goes out to send to tank field, which sets built-in
Tower bottom heater and tower top cooler, the products obtained therefrom index such as table 2 after the device.
2 product quality indicator of table
The process has the characteristics that flexible operation, can be wanted meeting user to the quality of product according to the variation in market
Under the premise of asking, by changing the operating condition of extraction tower, the yield and quality of product are adjusted.
Claims (8)
1. a kind of heavy aromatics industrial process, it is characterised in that: returned including feedstock processing part, Aromatics Extractive Project part, solvent
Receiving portions, solvent processing part and public work part, the production method raw material can pass through method one and the realization of method two, root
According to feedstock oil source, feedstock oil is one or several the single combination of catalytic diesel oil, FCC heavy diesel oil, recycle oil and lightweight slurry oil etc.
Object,
Method one:
Raw material recycle oil and bavin fraction is urged, is mixed with natural proportion；
Method two:
Raw material recycle oil urges bavin heavy distillat and catalytic slurry to mix.
2. a kind of heavy aromatics industrial process as described in claim 1, it is characterised in that: the feedstock processing part is come
Enter feedstock oil stripper from the mixed raw material of tank field, after light fraction oil is stripped off at reduced pressure conditions, enters as charging
Extract part.Tower top oil gas is after steam jet ejector, stripping tower top condensate cooler condensation are cooling, into stripping overhead reflux
Tank, light component are extracted out by feedstock oil stripper reflux pump, and a part send feedstock oil stripper overhead as reflux, and another part is made
For product tank sending area.
3. a kind of heavy aromatics industrial process as described in claim 1, it is characterised in that: the extracting part: feedstock oil
After stripping tower bottom material is by the pump pressurization of feedstock oil stripper, into the middle part of extraction tower, wet furfural from furfural liquid separation tank furfural into
Material pump pressurization, into extraction tower top；Two solvents are sent into extraction tower lower part from after the solvent feed pump pressurization of two solvent tanks；It is former
Material oil inversely contacts in tower with furfural, two solvents, carries out liquid-liquid extraction, and furfural extracts the weight in feedstock oil from top to bottom
Aromatic hydrocarbons, two solvents extract light aromatics and alkane in furfural extract out from bottom to top, extract column overhead raffinate and tower bottom is taken out
Liquid respectively enters Solvent recovery portion out, and wherein the weight ratio of feedstock oil, wet furfural and two solvent naphthas is: feedstock oil: wet furfural:
Two solvent=1: 0.4~2.5: 0.2~1.6.
4. a kind of heavy aromatics industrial process as described in claim 1, it is characterised in that: the solvent recovery and processing unit
The raffinate divided after heat exchanger exchanges heat to 180-230 DEG C, into raffinate destilling tower, is blown from extracting column overhead from pressure by tower bottom
Enter steam stripping and go out two solvents, raffinate oil from after the pressurization of tower bottom raffinate oil pump, is cooled to 40-80 DEG C through pumping cooler and send to tank
Area, the solvent vapo(u)r flowed out from raffinate distillation tower top enter after raffinate distillation overhead condenser is cooled to 20-50 DEG C
Vacuum tank, condensate liquid in vacuum tank is from flowing into solvent liquid separation tank.
5. a kind of heavy aromatics industrial process as claimed in claim 4, it is characterised in that: the extraction tower tower bottom Extract
After pumping up, heated device exchanges heat to after 200-235 DEG C, and into Extract evaporating column, tower bottom liquid exchanges heat from pressure through heat exchanger
To after 225-265 DEG C, into Extract destilling tower, solvent vapo(u)r is flowed out from Extract evaporating column tower top, through Extract evaporating column
After top condenser is cooled to 20-60 DEG C, into solvent liquid separation tank, the extraction oil is taken out with extraction oil pump from Extract destilling tower tower bottom
After pressurizeing out, it is cooled to 20-60 DEG C through Extract-extraction oil heat exchanger, extraction oil-furfural heat exchanger, extraction oil cooler and send
To the solvent vapo(u)r described in tank field from Extract distillation tower top outflow after Extract distillation overhead condenser is cooled to 20-60 DEG C,
Into vacuum tank, the condensate liquid in vacuum tank flows into solvent liquid separation tank certainly.
6. a kind of heavy aromatics industrial process as claimed in claim 4, it is characterised in that: described into solvent liquid separation tank
Furfural, the sedimentation separation in knockout drum of two solvents and water, aqueous solution containing aldehyde is from inflow furfural liquid separation tank, the aqueous solution containing two solvents
Into two solvent tanks, furfural and water further separate in furfural liquid separation tank, and water phase is pumped from two solvent tanks, furfural is flowed into through furfural
It is sent after pressurization to extraction tower, after two solvents and water separate in two solvent tanks, two solvents are sent after solvent feed pump pressurization to pumping
Stripper is recycled, and send dehydrating tower recycling design containing aqueous solvent.
7. a kind of heavy aromatics industrial process as claimed in claim 4, it is characterised in that: the dehydration tower top is steamed containing solvent
Vapour enters solvent knockout drum after dehydration overhead condenser is cooled to 20-80 DEG C, cold through sewage after tower bottom sewage is pressurizeed with sewage pump
But carrying device after device is cooling.
8. a kind of heavy aromatics industrial process as claimed in claim 4, it is characterised in that: the furfural of the recycling,
Two solvents are refined by solvent refining tower interruption respectively according to its quality condition, into the furfural or two solvents of solvent refining tower
After separating in tower, top gaseous phase enters furfural liquid separation tank or two solvent tanks after the condensation of solvent refining overhead condenser is cooling,
Tower bottom heavy diesel fuel component heavy constituent pumping goes out to send to tank field, which sets built-in tower bottom heater and tower top cooler.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2018103936416 | 2018-04-27 | ||
| CN201810393641 | 2018-04-27 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109679679A true CN109679679A (en) | 2019-04-26 |
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ID=66192163
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910030994.4A Pending CN109679679A (en) | 2018-04-27 | 2019-01-14 | A kind of heavy aromatics industrial process |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111500316A (en) * | 2020-05-09 | 2020-08-07 | 宁波博汇化工科技股份有限公司 | Method for preparing heavy aromatic hydrocarbon by extractive distillation |
| CN116355649A (en) * | 2023-04-14 | 2023-06-30 | 中国石油化工股份有限公司 | Device and method for producing light aromatic hydrocarbon and heavy aromatic hydrocarbon |
-
2019
- 2019-01-14 CN CN201910030994.4A patent/CN109679679A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111500316A (en) * | 2020-05-09 | 2020-08-07 | 宁波博汇化工科技股份有限公司 | Method for preparing heavy aromatic hydrocarbon by extractive distillation |
| CN111500316B (en) * | 2020-05-09 | 2022-05-10 | 宁波博汇化工科技股份有限公司 | Method for preparing heavy aromatic hydrocarbon by extractive distillation |
| CN116355649A (en) * | 2023-04-14 | 2023-06-30 | 中国石油化工股份有限公司 | Device and method for producing light aromatic hydrocarbon and heavy aromatic hydrocarbon |
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