CN106632236A - Method for continuously removing heavy aromatics from solvent online - Google Patents
Method for continuously removing heavy aromatics from solvent online Download PDFInfo
- Publication number
- CN106632236A CN106632236A CN201610873649.3A CN201610873649A CN106632236A CN 106632236 A CN106632236 A CN 106632236A CN 201610873649 A CN201610873649 A CN 201610873649A CN 106632236 A CN106632236 A CN 106632236A
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- CN
- China
- Prior art keywords
- solvent
- heavy
- oil
- recovery tower
- tower
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D333/00—Heterocyclic compounds containing five-membered rings having one sulfur atom as the only ring hetero atom
- C07D333/02—Heterocyclic compounds containing five-membered rings having one sulfur atom as the only ring hetero atom not condensed with other rings
- C07D333/46—Heterocyclic compounds containing five-membered rings having one sulfur atom as the only ring hetero atom not condensed with other rings substituted on the ring sulfur atom
- C07D333/48—Heterocyclic compounds containing five-membered rings having one sulfur atom as the only ring hetero atom not condensed with other rings substituted on the ring sulfur atom by oxygen atoms
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C1/00—Working-up tar
- C10C1/18—Working-up tar by extraction with selective solvents
Abstract
The invention discloses a method for continuously removing heavy aromatics from solvent online. The method includes 1), taking out solvent, accounting for smaller than 2% of total lean solvent circulation volume, from a recovery tower to perform online heavy aromatic removal; 2), mixing the collected solvent with water taken out from the recovery tower; 3), subjecting the mixture to standing and separating through a primary separator and a secondary separator; 4), separating the collected solvent through the primary separator and the secondary separator to obtain new solvent, injecting the new solvent into a wet solvent tank, and feeding de-heavy heavy component oil separated out by the secondary separator into a heavy component collection tank; 5), re-injecting the new solvent in the wet solvent tank into the recovery tower by a pump. The method has the advantages that the benzene hydrogenation solvent is subjected to continuous online de-heavy, so that solvent and product quality is guaranteed, and solvent consumption is reduced greatly; continuous online de-heavy can substitute for original regenerating tower systems, so that consumption of conduction oil and coal gas is reduced; after system operation, system operation stability and economic benefit are remarkable, and potential environment protection benefit is achieved.
Description
Technical field
The present invention relates to coal chemical technology.
Background technology
In liquid-liquid extraction process with sulfolane as solvent, in Coal Chemical Industry benzene hydrogenation industry critical role is occupied.Ring fourth
Sulfone liquid-liquid extraction is used for Aromatics Extractive Project can obtain higher aromatics yield and product quality.But the deterioration of industry park plan sulfolan
Always perplex the outstanding problem of arene extracting process.
There is deterioration in extractive process in sulfolane so as to extract ability decline, be mainly shown as sulfolane darken,
It is mingled with heavy arene and some colloidal substances body in pH value decline, solvent and forms deposit and the increase of solvent loss amount etc..Normally
During commercial scale, in addition to runtime air-tightness is definitely tight, the work of the continuous online imurity-removal of sulfolane solvent
Skill is very urgent, otherwise without high-quality solvent, benzene hydrogenation system can be affected normally to produce, and largely effects on product yield and matter
Amount.
The content of the invention
The technical problem to be solved be realize it is a kind of can in on-line continuous desolvation heavy aromatics method.
To achieve these goals, the technical solution used in the present invention is：One kind can be weighed in on-line continuous desolvation
The method of aromatic hydrocarbons：
1) take out the solvent in recovery tower less than total lean solvent circuit amount 2% and removed heavy aromatics online；
2) water for taking out solvent with take out in recovery tower is mixed；
3) by mixture by primary separator, the standing separation of second-stage separator；
4) take out solvent to isolate in novel solvent injection wet solvent groove from primary separator, second-stage separator, the second-order separation
The de- heavy component oil that device is isolated sends into heavy constituent collecting tank；
5) novel solvent in wet solvent groove notes recovery tower by blowback.
1) the middle solvent that takes out accounts for the 1% of total lean solvent circuit amount.
It is described 2) in the water that takes out in recovery tower be prepared by the following：By the oil gas after stripping in recovery tower and steam
Condensed device is delivered to oil-water separation tank, the water isolated is delivered to into pipe-line mixer and is mixed with solvent is taken out.
2) the middle water weight ratio taken out in solvent and recovery tower that takes out is 10：1.
The heavy component oil cleaning oil tower for being pumped to oil depot loading system, the oily tower of cleaning are taken off in the heavy constituent collecting tank
Interior de- heavy oil periodically delivers to coal tar distillation system with tank car.
Based on described the method for heavy aromatics equipment, recovery tower lean solvent can be continuously disengaged from on-line continuous desolvation
Outlet Jing pipeline connection lean solvent pumps, the lean solvent pump conveys lean solvent to pipe-line mixer, and the recovery tower top is arranged
Pipeline collects oil gas and steam after stripping and is delivered to condenser, and the condenser conveys mixed liquor to oil-water separation tank, institute
The separation water out Jing pipelines connection water pump of oil-water separation tank is stated, separation water is delivered to pipe-line mixer by the water pump, described
Pipe-line mixer liquid outlet is by primary separator, the standing separation of second-stage separator, the primary separator, second-stage separator
Bottom boots bucket enter in the wet solvent groove in groove area, the de- heavy component oil that second-stage separator top is isolated is delivered to again
Fraction collection groove, novel solvent is to recovery tower described in the wet solvent groove Jing novel solvent pumps.
The novel solvent pump delivery outlet Jing pipelines connect the input port of rich solvent pump, and the pipeline is connected by the first three-way valve
The liquid outlet of extraction tower, the rich solvent pump delivery outlet Jing pipelines connect recovery tower.
The liquid outlet pipeline of the lean solvent pump is provided with the second three-way valve, the second three-way valve one outlet connecting pipe
Blender, another outlet connection extraction tower.
It is an advantage of the current invention that in normal production, about 1% amount of lean solvent circuit amount is carried out into continuous online removing
Heavy arene and impurity, so that it is guaranteed that enter extraction tower lean solvent quality, improve the extraction efficiency of extraction tower, improve aromatic hydrocarbons and non-aromatic
The separation efficiency of hydrocarbon, improves aromatic hydrocarbon product and non-aromatics product quality, reduces the loss of lean solvent.Simultaneously to the heavy after de- weight
Aromatic hydrocarbons is comprehensively utilized, in cleaning oil tower when using it for entrucking, so as to also solve the live loss abnormal smells from the patient of washing oil,
Also the washing oil blockage problem of the oily tower of cleaning is solved, the unnecessary de- heavy oil of the oily tower of cleaning can be passed to tar and steam by tank car
System is evaporated, is recycled.
Description of the drawings
The content of every width accompanying drawing expression in description of the invention is briefly described below：
Fig. 1 is heavy aromatics process chart in on-line continuous desolvation.
Specific embodiment
As shown in figure 1, total lean solvent circuit amount (about 60 tons/h) that lean solvent is exported, cuts out 600kg/h (about 1%) molten
Agent enters online de- weight system, (is 1 with the ratio of solvent with 60kg/h is cut out from recovery tower exit of pump：10) system process
Separation water mixes in pipe-line mixer, and then by primary separator, the standing separation of second-stage separator, solvent is from one or two grades
The bottom boots bucket of separator is entered in the wet solvent groove in groove area, and the de- heavy component oil that second-stage separator top is isolated is (referred to as
De- heavy oil), into heavy constituent collecting tank, with the cleaning oil tower for being pumped to oil depot loading system, for clean oily tower circulation and
The benzene hydrocarbon gase of entrucking is absorbed, the de- heavy oil in the oily tower of cleaning periodically delivers to coal tar distillation system, ultimately forms coal with tank car
Tar product.
This technique enters back into system by using the technique separation water of system itself after mixing with solvent, internal system is built
Vertical water balance, is not required to increase soft water in addition.The circumscribed de- weight of solvent on-line continuous forms dynamic equilibrium with solvent make-up amount, is formed
Each groove, tower and flow are in steady statue.
Benzene hydrogenation solvent is continuously taken off online weight, it is ensured that while solvent and product quality, solvent greatly reduces
Consume, continuous online de- weight can replace original regeneration Tower System, so as to reduce the consumption of conduction oil and coal gas, the system
After operation, no matter the stability of system operation, economic benefit achieve noticeable achievement, especially also potential environmental benefit.
Indirect benefit：Not only there is it containing sulfolane due in regenerator running, needing regular deslagging, the residue
His polymer, fixed-end forces are extremely difficult and the smell is awful.After using the de- weight of on-line continuous, de- heavy oil is finally with tar product
Product form is taken out, also certain economic benefit.
Direct benefit.The de- weight system of on-line continuous achieves noticeable achievement in terms of cost efficiency.
New sulfolane solvent about 12t is saved every year, and according to 1.9 ten thousand yuan/t, then annual sulfolane solvent consumption is reduced, harvested
Direct economic benefit be：12 × 1.9=22.8 (ten thousand yuan/a).
After solvent quality is improved, arene content in non-aromatic hydrocarbon product is reduced, improve aromatics yield, according to aromatic hydrocarbons and non-
The price difference of aromatic hydrocarbon product, the direct economic benefit of results is：Non-aromatics benzene content in 2015 reduces by 12% compared with 2014 annual means,
1500 tons of non-aromatics yield, non-aromatics benzene content reduces by 180 tons, and purified petroleum benzin and non-aromatic 2000 yuan/t of hydrocarbon product price difference were (according at that time
Price difference), direct profit=180 × 0.2=36 (ten thousand yuan/a)
Obvious energy conservation after the de- weight system operation of on-line continuous.Regenerator reduces heat conduction oil heat consumption, reduces conduction oil
The gas consumption of stove, it is 50m3/h that coal gas consumption can be reduced per hour, is calculated according to horse steel 0.6 yuan/m3 of gas price, is received
The direct economic benefit for obtaining is：50 × 8000 ÷ 10000=24 of (year run time) × 0.6 (ten thousand yuan/a)
Therefore, continuously after the de- weight system operation of line and regenerative system are disabled, annual obtainable economic benefit is 82.8
Wan Yuan.
Claims (8)
1. it is a kind of can in on-line continuous desolvation heavy aromatics method, it is characterised in that：
1) take out the solvent in recovery tower less than total lean solvent circuit amount 2% and removed heavy aromatics online；
2) water for taking out solvent with take out in recovery tower is mixed；
3) by mixture by primary separator, the standing separation of second-stage separator；
4) take out solvent to isolate in novel solvent injection wet solvent groove from primary separator, second-stage separator, second-stage separator point
The de- heavy component oil for separating out sends into heavy constituent collecting tank；
5) novel solvent in wet solvent groove notes recovery tower by blowback.
2. it is according to claim 1 can in on-line continuous desolvation heavy aromatics method, it is characterised in that：It is described 1)
Middle taking-up solvent accounts for the 1% of total lean solvent circuit amount.
3. it is according to claim 2 can in on-line continuous desolvation heavy aromatics method, it is characterised in that：It is described 2)
The water taken out in middle recovery tower is prepared by the following：Oil gas after stripping in recovery tower and the condensed device of steam are delivered to
Oil-water separation tank, is delivered to the water isolated pipe-line mixer and mixes with solvent is taken out.
4. according to claim 1,2 or 3 can in on-line continuous desolvation heavy aromatics method, it is characterised in that：
2) the middle water weight ratio taken out in solvent and recovery tower that takes out is 10: 1.
5. it is according to claim 4 can in on-line continuous desolvation heavy aromatics method, it is characterised in that：It is described heavy
The heavy component oil cleaning oil tower for being pumped to oil depot loading system is taken off in Fraction collection groove, the de- heavy oil in the oily tower of cleaning is regular
Coal tar distillation system is delivered to tank car.
6. the method for heavy aromatics can be continuously disengaged from on-line continuous desolvation based on any one of claim 1-5
Equipment, it is characterised in that：Recovery tower lean solvent outlet Jing pipeline connection lean solvent pumps, the lean solvent pump conveying lean solvent is to pipe
Road blender, the recovery tower top arranges pipeline and collects oil gas and steam after stripping and be delivered to condenser, the condensation
Device conveys mixed liquor to oil-water separation tank, the separation water out Jing pipelines connection water pump of the oil-water separation tank, and the water pump will
Separation water is delivered to pipe-line mixer, and the pipe-line mixer liquid outlet is by primary separator, the standing point of second-stage separator
From the primary separator, the bottom boots bucket of second-stage separator are entered in the wet solvent groove in groove area, the second-stage separator top
The de- heavy component oil isolated is delivered to heavy constituent collecting tank, and novel solvent described in the wet solvent groove Jing novel solvent pumps is to recovery
Tower.
It is 7. according to claim 6 to be continuously disengaged from equipment, it is characterised in that：
The novel solvent pump delivery outlet Jing pipelines connect the input port of rich solvent pump, and the pipeline is by the connection extraction of the first three-way valve
The liquid outlet of tower, the rich solvent pump delivery outlet Jing pipelines connect recovery tower.
It is 8. according to claim 7 to be continuously disengaged from equipment, it is characterised in that：The liquid outlet pipeline of the lean solvent pump is provided with
Second three-way valve, the second three-way valve one outlet connecting pipe blender, another outlet connection extraction tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610873649.3A CN106632236A (en) | 2016-09-30 | 2016-09-30 | Method for continuously removing heavy aromatics from solvent online |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610873649.3A CN106632236A (en) | 2016-09-30 | 2016-09-30 | Method for continuously removing heavy aromatics from solvent online |
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| Publication Number | Publication Date |
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| CN106632236A true CN106632236A (en) | 2017-05-10 |
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| CN201610873649.3A Pending CN106632236A (en) | 2016-09-30 | 2016-09-30 | Method for continuously removing heavy aromatics from solvent online |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108379866A (en) * | 2018-03-22 | 2018-08-10 | 马鞍山钢铁股份有限公司 | Four benzene extractive distillation systems of one kind and technique |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5030737A (en) * | 1990-02-12 | 1991-07-09 | Phillips Petroleum Company | Use of a solvent for hydrogenation of sulfolene to sulfolane |
| JPH07278136A (en) * | 1994-04-12 | 1995-10-24 | Mitsubishi Chem Corp | Method for regenerating recovered sulfolane |
| US20140216915A1 (en) * | 2009-06-02 | 2014-08-07 | Uop Llc | Apparatus for removing a contaminant from a solvent separation process |
| CN105017210A (en) * | 2014-04-23 | 2015-11-04 | 上海宝钢化工有限公司 | Regeneration method of sulfolane |
| CN105237511A (en) * | 2015-10-24 | 2016-01-13 | 大连福佳·大化石油化工有限公司 | Extraction solvent recycling and reusing system |
-
2016
- 2016-09-30 CN CN201610873649.3A patent/CN106632236A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5030737A (en) * | 1990-02-12 | 1991-07-09 | Phillips Petroleum Company | Use of a solvent for hydrogenation of sulfolene to sulfolane |
| JPH07278136A (en) * | 1994-04-12 | 1995-10-24 | Mitsubishi Chem Corp | Method for regenerating recovered sulfolane |
| US20140216915A1 (en) * | 2009-06-02 | 2014-08-07 | Uop Llc | Apparatus for removing a contaminant from a solvent separation process |
| CN105017210A (en) * | 2014-04-23 | 2015-11-04 | 上海宝钢化工有限公司 | Regeneration method of sulfolane |
| CN105237511A (en) * | 2015-10-24 | 2016-01-13 | 大连福佳·大化石油化工有限公司 | Extraction solvent recycling and reusing system |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108379866A (en) * | 2018-03-22 | 2018-08-10 | 马鞍山钢铁股份有限公司 | Four benzene extractive distillation systems of one kind and technique |
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| PB01 | Publication | ||
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| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 243003 Department of intellectual property right of Hunan West Road No. 8 technology center, Ma'anshan City, Anhui Province Applicant after: Ma'anshan Iron and Steel Co., Ltd. Address before: 243003 Hunan Anhui West Road, No. 8 technology center, Intellectual Property Department Applicant before: Ma'anshan Iron and Steel Co., Ltd. |
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| CB02 | Change of applicant information | ||
| CB02 | Change of applicant information |
Address after: 243003 8 Jiuhua Road, Yushan, Ma'anshan, Anhui Applicant after: Ma'anshan Iron and Steel Co., Ltd. Address before: 243003 intellectual property department, technology center, No. 8 Hunan West Road, Yushan, Ma'anshan, Anhui Applicant before: Ma'anshan Iron and Steel Co., Ltd. |
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| CB02 | Change of applicant information | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20170510 |
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| RJ01 | Rejection of invention patent application after publication |