CN104593052A - Solvent refining equipment and method for inferior coker gas oil - Google Patents
Solvent refining equipment and method for inferior coker gas oil Download PDFInfo
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- CN104593052A CN104593052A CN201510024802.0A CN201510024802A CN104593052A CN 104593052 A CN104593052 A CN 104593052A CN 201510024802 A CN201510024802 A CN 201510024802A CN 104593052 A CN104593052 A CN 104593052A
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- 239000002904 solvent Substances 0.000 title claims abstract description 190
- 238000007670 refining Methods 0.000 title claims abstract description 140
- 238000000034 method Methods 0.000 title claims abstract description 40
- 239000000284 extract Substances 0.000 claims abstract description 223
- 238000000605 extraction Methods 0.000 claims abstract description 178
- 238000001704 evaporation Methods 0.000 claims abstract description 48
- 230000008020 evaporation Effects 0.000 claims abstract description 45
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 claims abstract description 40
- 235000011194 food seasoning agent Nutrition 0.000 claims description 28
- 238000001035 drying Methods 0.000 claims description 10
- 238000004807 desolvation Methods 0.000 claims description 8
- 238000009835 boiling Methods 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 239000011259 mixed solution Substances 0.000 claims description 3
- 238000005373 pervaporation Methods 0.000 claims description 2
- 239000002994 raw material Substances 0.000 abstract description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 10
- 238000004517 catalytic hydrocracking Methods 0.000 abstract description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 6
- 150000004945 aromatic hydrocarbons Chemical class 0.000 abstract description 6
- 238000004523 catalytic cracking Methods 0.000 abstract description 6
- 239000007788 liquid Substances 0.000 abstract description 6
- 229930195734 saturated hydrocarbon Natural products 0.000 abstract description 6
- 239000000203 mixture Substances 0.000 abstract description 5
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 5
- 238000005336 cracking Methods 0.000 abstract description 3
- 239000007789 gas Substances 0.000 abstract description 3
- 238000002156 mixing Methods 0.000 abstract description 3
- 239000013064 chemical raw material Substances 0.000 abstract 1
- 239000011593 sulfur Substances 0.000 abstract 1
- 229910052717 sulfur Inorganic materials 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 210
- 238000004064 recycling Methods 0.000 description 8
- 238000000638 solvent extraction Methods 0.000 description 8
- 239000004215 Carbon black (E152) Substances 0.000 description 6
- 229930195733 hydrocarbon Natural products 0.000 description 6
- 150000002430 hydrocarbons Chemical class 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 239000005864 Sulphur Substances 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 5
- 238000000746 purification Methods 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 4
- 238000004939 coking Methods 0.000 description 4
- 230000003111 delayed effect Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000003317 industrial substance Substances 0.000 description 4
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 2
- 239000000084 colloidal system Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910017464 nitrogen compound Inorganic materials 0.000 description 2
- 150000002830 nitrogen compounds Chemical class 0.000 description 2
- 239000010426 asphalt Substances 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 150000004767 nitrides Chemical class 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a solvent refining device and a method of inferior coker gas oil, which takes the inferior coker gas oil as raw oil, in a countercurrent extraction tower, furfural is used as a solvent, the solvent enters an extraction tower from the upper part of the extraction tower, raw oil enters the extraction tower from the lower part of the extraction tower, partial secondary extract oil or secondary extract liquid containing a small amount of solvent through evaporation is mixed with primary extract liquid flowing out from the bottom of the extraction tower, the mixture enters an extract oil solvent refining tank for refining, extract oil raffinate at the top of the refining tank returns to the extraction tower, secondary extract liquid at the bottom of the refining tank is evaporated and stripped to recover the solvent to obtain secondary extract oil, the extract oil has high aromatic hydrocarbon content, is a chemical raw material with wide application, solvent refined oil is obtained after raffinate at the top of an extraction tower is stripped to recover the solvent, the saturated hydrocarbon content is high, and the sulfur and nitrogen content is low, so that the raw material or blending component of catalytic cracking or hydrocracking with excellent cracking performance is obtained.
Description
Technical field
The invention belongs to technical field of petrochemical industry, relate in particular to a kind of solvent refining equipment and method of wax tailings inferior.
Background technology
At present, global crude oil heaviness in poor quality trend is aggravated, and the demand of countries on petroleum is also increasing gradually, and improving heavy oil conversion is that lightweight oil is significant undoubtedly.Delayed coking is the technical way that refinery poor residuum transforms, it is the Main Means of state's residual oil weight-lightenings such as the U.S., China, Venezuela, India, Canada, the whole world has more than 170 and overlaps residual oil delayed coking unit in operation, total working ability more than 400,000,000 tons, China's delayed coking working ability in 2012 has reached 1.13 hundred million tons.Poor residuum produces a large amount of wax tailings in delayed coking process, and this wax tailings is rich in polycyclic aromatic hydrocarbons, colloid and sulphur, nitrogen compound, is difficult to following process process.When as Fcc Unit With Mixing Feed Including raw material, due to containing a large amount of nitride and polycyclic aromatic hydrocarbons, its crackability is too poor, makes light oil yield low, coke and dry gas yield high, oil stability is poor, can only mix less, is not desirable catalytically cracked material; As hydrocracking raw material mix refining component be also like this; Wax tailings inferior carries out hydrotreatment, also because nitrogen and polycyclic aromatic hydrocarbon content cross high reason, difficult, does not reach desirable refining effect.How Appropriate application wax tailings inferior is an important technical barrier.
Wax tailings inferior adopts solvent-refined method can effectively by most polycyclic aromatic hydrocarbons, and colloid and sulphur, nitrogen compound are extracted out, and raffinating oil is catalytic cracking or the hydrocracking raw material of high-quality; The aromaticity content extracting oil out is high, is useful industrial chemicals.Publication number is the technology that the application for a patent for invention of CN1042730A proposes to produce by technical combinations such as single solvent extraction and hydrogenation high-value product, the patent No. be 87107146.0 Chinese invention patent be then utilize solvent pairs extraction technique, compared with single solvent technology, it can make the rate of recovery of the good stable hydrocarbon of cracking performance in raffinating oil in faulty wax oil higher, can obtain more catalytic cracking or hydrocracking raw material.Make the saturated hydrocarbon content of extraction oil lower simultaneously, be conducive to its utilization.The second solvent of solvent pairs extracting is called back suction agent in the above documents, be be the solvent oil of 90-120 DEG C by boiling range, but after introducing back suction agent, add equipment and the operational load of recovery system, plant investment, material consumption, the corresponding increase of energy consumption, therefore this technology does not have industrialization so far.Publication number is the back suction agent of the Chinese invention patent of the CN1061366C oil product being rich in stable hydrocarbon of selecting boiling range higher, wider as extractive process, the method is compared with the Chinese invention patent that the patent No. is 87107146.0 not to be needed to reclaim back suction agent specially, reduce the load of solvent recuperation, but this technique do not have industrialization so far.Therefore being badly in need of can the method for refining solvent of industrialized wax tailings inferior, makes wax tailings inferior obtain Appropriate application.
Summary of the invention
For overcoming the shortcoming of prior art, the object of the present invention is to provide a kind of method for refining solvent of wax tailings inferior, make wax tailings inferior after solvent extraction, the high quality raw material of raffinating oil as catalytic cracking or hydrocracking, extract oil out as the industrial chemicals being rich in aromatic hydrocarbons.
For achieving the above object, the invention provides a kind of solvent refining equipment of wax tailings inferior, comprise extraction tower, extract oil refining tank, raffinate stripping tower and refining oil tank out, described extraction tower comprises the stock oil entrance being arranged at its underpart, the colvent inlet being arranged at its top, the raffinate outlet that is arranged at an Extract outlet bottom it, is arranged at its top; Described extraction oil refining tank comprises an Extract entrance in portion disposed therein, and described Extract outlet is connected with a described Extract entrance; Described raffinate stripping tower comprises the raffinate entrance being arranged at its underpart and the treated oil outlet be arranged at bottom it, and described raffinate outlet is connected with described raffinate entrance; Described refining oil tank exports with described extraction tower treated oil and is connected, and wherein, has an extraction oil raffinate pipeline between described extraction oil refining tank and described extraction tower.
The solvent refining equipment of above-mentioned wax tailings inferior, wherein, described extraction oily raffinate pipeline comprises to be extracted the outlet of oily raffinate out and extracts oily raffinate entrance out, the outlet of described extraction oily raffinate is arranged at the top of described extraction oil refining tank, and described extraction oil raffinate entrance to be arranged on described extraction tower and to be positioned at the position of below the position at place, described colvent inlet or described colvent inlet.
The solvent refining equipment of above-mentioned wax tailings inferior, wherein, described extraction oily raffinate pipeline comprises to be extracted the outlet of oily raffinate out and extracts oily raffinate entrance out, the outlet of described extraction oily raffinate is arranged at the top of described extraction oil refining tank, described extraction oily raffinate entrance is arranged at the position between described colvent inlet and described stock oil entrance, comprises the position at described colvent inlet or described stock oil entrance place.
The solvent refining equipment of above-mentioned wax tailings inferior, wherein, also comprise solvent seasoning tower, wet solvent entrance and solvent outlet after being arranged at bottom it drying after described solvent seasoning tower comprises the stripping being arranged at its top, described raffinate stripping tower also comprises the first wet solvent outlet being arranged at its top, described first wet solvent outlet is connected with wet solvent entrance after described stripping, and after described drying, solvent outlet is connected with described colvent inlet.
The solvent refining equipment of above-mentioned wax tailings inferior, wherein, also comprise secondary Extract evaporator tower, described secondary Extract evaporator tower comprises the secondary Extract entrance being arranged at its underpart, solvent outlet and secondary Extract outlet after being arranged at bottom it evaporation after being arranged at the evaporation at its top, described solvent seasoning tower comprises colvent inlet after the evaporation in portion disposed therein, described extraction oil refining tank also comprises the secondary Extract outlet be arranged at bottom it, described secondary Extract outlet is connected with described secondary Extract entrance, after described evaporation, the outlet of secondary Extract is connected with a described Extract entrance, after described evaporation, solvent outlet is connected with colvent inlet after described evaporation.
The solvent refining equipment of above-mentioned wax tailings inferior, wherein, also comprise secondary extract stripper and secondary extraction oil tank, after described secondary extract stripper comprises the evaporation being arranged at its underpart, secondary Extract entrance and the secondary be arranged at bottom it extract oil export out, after described evaporation, the outlet of secondary Extract is connected with secondary Extract entrance after described evaporation, and described secondary extraction oil export is extracted oil tank out with described secondary and is connected.
The solvent refining equipment of above-mentioned wax tailings inferior, wherein, described secondary extract stripper also comprises the second wet solvent outlet being arranged at its top, and described second wet solvent outlet is connected with wet solvent entrance after described stripping.
The solvent refining equipment of above-mentioned wax tailings inferior, wherein, described secondary is extracted oil export out and is connected with a described Extract entrance.
The present invention also provides a kind of method for refining solvent of wax tailings inferior, wherein, adopts the solvent refining equipment of above-mentioned wax tailings inferior to refine, comprises the steps:
Solvent enters described extraction tower from the top of described extraction tower, stock oil enters described extraction tower from the bottom of described extraction tower and carries out extracting, the Extract that extracting obtains enters described extraction oil refining tank and refines, the refining extraction oil raffinate obtained is back to described extraction tower by described extraction oily raffinate pipeline, the raffinate that in described extraction tower, extracting obtains enters described raffinate stripping tower, and the treated oil that raffinate obtains after carrying out stripping desolvation enters described refining oil tank.
The method for refining solvent of above-mentioned wax tailings inferior, wherein, the wet solvent that described raffinate stripping tower stripping goes out enters described solvent seasoning tower through condensation and carries out drying, and the dried described solvent of described solvent seasoning tower bottom enters described extraction tower and recycles.
The method for refining solvent of above-mentioned wax tailings inferior, wherein, in described extraction oil refining tank, the refining secondary Extract obtained obtains the secondary Extract containing a small amount of solvent after pervaporation, and the secondary Extract containing a small amount of solvent obtains secondary and extracts oil out after stripping.
The method for refining solvent of above-mentioned wax tailings inferior, wherein, part secondary extracts oil out or part mixes with the Extract that described extraction tower extracting obtains through the secondary Extract of evaporation containing a small amount of solvent, enters described extraction oil refining tank and refines.
The method for refining solvent of above-mentioned wax tailings inferior, wherein, the solvent removed during the evaporation of secondary Extract and the wet solvent removed when evaporation contains the secondary Extract stripping of a small amount of solvent enter described solvent seasoning tower respectively and carry out drying.
The method for refining solvent of above-mentioned wax tailings inferior, wherein, the operational condition of described extraction oil refining tank is: secondary extracts oil out or the mass ratio of the amount that mixes with Extract through the secondary Extract of evaporation containing a small amount of solvent and stock oil is 0.2-1.0:1, the temperature of extracting oil refining tank out is 40 DEG C-50 DEG C, and the residence time that Extract stays in described extraction oil refining tank is 50-120 minutes; The residence time that the mixed solution that part secondary extraction oil or part obtain after the secondary Extract of evaporation containing a small amount of solvent mixes with an Extract stays in described extraction oil refining tank is 50-120 minutes.
The method for refining solvent of above-mentioned wax tailings inferior, wherein, described stock oil is wax tailings inferior, and described solvent is furfural.
The method for refining solvent of above-mentioned wax tailings inferior, wherein, the initial boiling point of described wax tailings inferior is greater than 300 DEG C.
The method for refining solvent of above-mentioned wax tailings inferior, wherein, described furfural extraction condition is, described extraction tower tower top temperature 60 DEG C-80 DEG C, described extraction tower column bottom temperature is 40 DEG C-50 DEG C, and the mass ratio of described furfural and described wax tailings inferior is 0.5-1.0:1.
This invention takes and secondary refining is carried out to extraction oil, the extraction obtained oil raffinate is returned the way of extraction tower, solvent extraction with routine is compared, the stable hydrocarbon extracted out in oil is equivalent to reclaim, the yield of raffinating oil can be improved further under the same conditions, secondary extracts the yield reduction of oil out simultaneously, and the saturated hydrocarbon content in secondary extraction oil is lower, aromaticity content is higher; Namely adopt the efficiency the method increasing solvent extraction, be equivalent to the selectivity that improve solvent.
Describe the present invention below in conjunction with the drawings and specific embodiments, but not as a limitation of the invention.
Accompanying drawing explanation
Fig. 1 is the structure diagram of the solvent refining equipment of wax tailings inferior of the present invention;
Fig. 2 is the process flow sheet of the method for refining solvent of wax tailings inferior of the present invention.
Wherein, Reference numeral
100 extraction towers
110 stock oil entrances
120 colvent inlets
130 Extract outlets
140 raffinate outlets
200 extract oil refining tank out
210 Extract entrances
220 2 Extract outlets
300 raffinate stripping towers
310 raffinate entrances
320 treated oil outlets
330 first wet solvent outlets
400 refining oil tanks
500 extract oily raffinate pipeline out
510 extract the outlet of oily raffinate out
520 extract oily raffinate entrance out
600 solvent seasoning towers
Wet solvent entrance after 610 strippings
620 dry rear solvent outlet
Colvent inlet after 630 evaporations
700 2 Extract evaporator towers
710 2 Extract entrances
Solvent outlet after 720 evaporations
Secondary Extract outlet after 730 evaporations
800 2 extract strippers
Secondary Extract entrance after 810 evaporations
Extract oil export out 820 2 times
830 second wet solvent outlets
Extract oil tank out 900 2 times
4 raffinates
5 Extracts
7 extract oily raffinate out
8 two Extracts
10 solvents removed
11,12,13 containing the secondary Extract of a small amount of solvent
14, oil is extracted out 16,17 2 times
15, the wet solvent that goes out of 18 strippings
19 treated oils
Embodiment
Below in conjunction with the drawings and specific embodiments, technical solution of the present invention is described in detail, further to understand object of the present invention, scheme and effect, but not as the restriction of claims protection domain of the present invention.
Principle of the present invention is: on the basis of common single solvent extraction, reclaims the stable hydrocarbon once extracted out in oil and is concentrated in by aromatic hydrocarbons further in secondary extraction oil simultaneously.
The method applied in the present invention is: with wax tailings inferior for stock oil, in counter-current extraction tower, take furfural as solvent, solvent enters extraction tower from the top of extraction tower, stock oil enters extraction tower from the bottom of extraction tower, bottom extraction tower, flow out an Extract, an Extract enters extracts oil refining tank out.Extract oil refining tank top out to flow out and extract oily raffinate out, extracting the position that oily raffinate returns extraction tower out is: between the colvent inlet of extraction tower to stock oil entrance, comprise colvent inlet and stock oil entrance.
The raffinate that extraction tower top is flowed out enters raffinate stripping tower, obtains treated oil after desolvation, can be used as the raw material of catalytic cracking or hydrocracking or it mixes refining component.
Extract oil refining pot bottom out and flow out secondary Extract, secondary Extract enters secondary Extract evaporator tower, flows out the secondary Extract containing a small amount of solvent bottom secondary Extract evaporator tower.
Secondary is extracted oil or secondary Extract out and can be mixed into an Extract through the secondary Extract of evaporation containing a small amount of solvent and extract oil refining tank out and refine.When adopting the secondary Extract containing a small amount of solvent to mix with an Extract, this secondary Extract is divided into two portions, the Extract that a part and extraction tower underflow go out is mixed into extracts oil refining tank out, another part enters secondary extract stripper, obtains secondary and extract oil out after desolvation; When adopting secondary extraction oil to mix with an Extract, a part and an Extract are mixed into extracts oil refining tank out, and remainder enters secondary as byproduct and extracts oil tank out.
Particularly, consult Fig. 1, the solvent refining equipment of wax tailings inferior of the present invention comprises extraction tower 100, extraction oil refining tank 200, raffinate stripping tower 300, refining oil tank 400 and extracts oily raffinate pipeline 500 out.Extraction tower 100 comprises: be arranged at the stock oil entrance 110 of the bottom of extraction tower 100, be arranged at the colvent inlet 120 on extraction tower 100 top, be arranged at an Extract outlet 130 bottom extraction tower 100 and be arranged at the raffinate outlet 140 at extraction tower 100 top.Extract oil refining tank 200 out to comprise: be arranged at the Extract entrance 210 extracted out in the middle part of oil refining tank 200, wherein, an Extract outlet 130 on extraction tower 100 is connected with the Extract entrance 210 extracted out on oil refining tank 200.Raffinate stripping tower 300 comprises: the raffinate entrance 310 being arranged at raffinate stripping tower 300 bottom and the treated oil outlet 320 be arranged at bottom raffinate stripping tower 300, wherein, the raffinate outlet 140 on extraction tower 100 is connected with the raffinate entrance 310 on raffinate stripping tower 300; Refining oil tank 400 exports 320 with the treated oil on raffinate stripping tower 300 and is connected.Extract oily raffinate pipeline 500 out to be arranged between extraction oil refining tank 200 and extraction tower 100, the setting of extracting oily raffinate pipeline 500 out can improve the rate of recovery of stock oil stable hydrocarbon, improves the yield of product.
Extract oily raffinate pipeline 500 out comprise the oily raffinate outlet 510 of extraction and extract oily raffinate entrance 520 out, extract oily raffinate outlet 510 out and be arranged at the top of extracting oil refining tank 200 out, extract oily raffinate entrance 520 out to be arranged on extraction tower 100 and the position being positioned at colvent inlet less than 120, comprise the position at place, colvent inlet 120.
Extract oily raffinate entrance 520 out and be arranged at position on extraction tower 100 between colvent inlet 120 and stock oil entrance 110, comprise the position at colvent inlet 120 and stock oil entrance 110 place.
As shown in Figure 1, the solvent refining equipment of wax tailings inferior of the present invention also comprises solvent seasoning tower 600, secondary Extract evaporator tower 700, secondary extract stripper 800 and secondary extraction oil tank 900.
Solvent seasoning tower 600 comprises: wet solvent entrance 610 and solvent outlet 620 after being arranged at bottom solvent seasoning tower 600 drying after being arranged at the stripping on solvent seasoning tower 600 top.Raffinate stripping tower 300 also comprises: the first wet solvent outlet 330 being arranged at raffinate stripping tower 300 top, the first wet solvent outlet 330 on raffinate stripping tower 300 is connected with wet solvent entrance 610 after the stripping on solvent seasoning tower 600, and after the drying on solvent seasoning tower 600, solvent outlet 620 is connected with the colvent inlet 120 on extraction tower 100.
Secondary Extract evaporator tower 700 comprises: the secondary Extract entrance 710 being arranged at secondary Extract evaporator tower 700 bottom, be arranged at secondary Extract evaporator tower 700 top evaporation after solvent outlet 720 and secondary Extract outlet 730 after being arranged at bottom secondary Extract evaporator tower 700 evaporation.Solvent seasoning tower 600 also comprises: be arranged at colvent inlet 630 after the evaporation in the middle part of solvent seasoning tower 600.Extract oil refining tank 200 out also to comprise: be arranged at the secondary Extract outlet 220 of extracting out bottom oil refining tank 200, the secondary Extract outlet 220 of extracting out bottom oil refining tank 200 is connected with the secondary Extract entrance 710 of secondary Extract evaporator tower 700 bottom, after evaporation bottom secondary Extract evaporator tower 700, secondary Extract outlet 730 is connected with the Extract entrance 210 extracted out in the middle part of oil refining tank 200, and after the evaporation at secondary Extract evaporator tower 700 top, solvent outlet 720 is connected with colvent inlet 630 after the evaporation in the middle part of solvent seasoning tower 600.
Secondary extract stripper 800 comprises: after being arranged at the evaporation of secondary extract stripper 800 bottom, secondary Extract entrance 810 and the secondary be arranged at bottom secondary extract stripper 800 extract oil export 820 out, after evaporation bottom secondary Extract evaporator tower 700, secondary Extract outlet 730 is connected with secondary Extract entrance 810 after the evaporation on secondary extract stripper 800, and the secondary extraction oil export 820 bottom extract stripper 800 is extracted oil tank 900 out with secondary and is connected.
Secondary extract stripper 800 also comprises: the second wet solvent outlet 830 being arranged at secondary extract stripper 800 top, and the second wet solvent outlet 830 on secondary extract stripper 800 is connected with wet solvent entrance 610 after the stripping on solvent seasoning tower 600.
Secondary on secondary extract stripper 800 is extracted oil export 820 out and is connected with the Extract entrance 210 extracted out on oil refining tank 200.
The method for refining solvent of wax tailings inferior of the present invention is specifically implemented as shown in Figure 2: stock oil adopts wax tailings inferior and enters extraction tower 100 from the stock oil entrance 110 of extraction tower 100 bottom, solvent adopts furfural and enters extraction tower 100 from the colvent inlet 120 on extraction tower 100 top, stock oil in extraction tower 100 after solvent treatment, the Extract 5 flowed out bottom extraction tower 100, extract the secondary Extract 8 flowed out bottom oil refining tank 200 out and remove most of solvent through secondary Extract evaporator tower 700, the solvent 10 removed enters the middle part of solvent seasoning tower 600, the secondary Extract 11 containing a small amount of solvent flowed out bottom secondary Extract evaporator tower 700 is divided into two portions 12 and 13, the Extract 5 flowed out bottom the secondary Extract 12 of a part containing a small amount of solvent and extraction tower 100 is mixed into extracts oil refining tank 200 out, the extraction oil raffinate 7 that the top of extracting oil refining tank 200 out is flowed out returns extraction tower 100 by extracting oily raffinate pipeline 500 out, the secondary Extract 13 containing a small amount of solvent flowed out bottom secondary Extract evaporator tower 700 enters secondary extract stripper 800, the wet solvent 15 that stripping goes out enters solvent seasoning tower 600 top through condensation removes moisture as top backflow, dry solvent bottom solvent seasoning tower 600 enters extraction tower 100 to recycle.The raffinate 4 at extraction tower 100 top enters raffinate stripping tower 300, the wet solvent 18 that stripping goes out enters solvent seasoning tower 600 top through condensation removes moisture as top backflow, dry solvent bottom solvent seasoning tower 600 recycles, and flows out treated oil 19 bottom raffinate stripping tower 300.Bottom secondary extract stripper 800, secondary is extracted oil out and 14 is divided into two portions 16 and 17, and a part of secondary is extracted oil 16 out and entered secondary as byproduct and extract oil tank 900 out, and a part of secondary is extracted oil 17 out and once extracted oily 5 and be mixed into and extract oil refining tank 200 out.
This invention takes and secondary refining is carried out to extraction oil, the extraction obtained oil raffinate is returned the way of extraction tower, solvent extraction with routine is compared, the stable hydrocarbon extracted out in oil is equivalent to reclaim, simultaneously owing to extracting the special composition of oily raffinate out, it returns in extraction tower and makes the extracting of extraction tower inside create useful effect, the yield of raffinating oil can be improved further under the same conditions, secondary extracts the yield reduction of oil out simultaneously, and the saturated hydrocarbon content in secondary extraction oil is lower, aromaticity content is higher; Namely adopt the efficiency the method increasing solvent extraction, be equivalent to the selectivity that improve solvent.
The present invention mainly meets treated oil and compares saturated hydrocarbon content with stock oil and increase, and the foreign matter content such as sulphur, nitrogen reduces, and extracts aromatic hydrocarbons in oil out, and the foreign matter content such as sulphur, nitrogen is high, and when more than meeting when requirement, the yield of treated oil is more high better.According to practical situation, the present invention extracts the position range that oily raffinate returns extraction tower out, the position of namely extracting the extraction oil raffinate entrance 520 of oily raffinate pipeline 500 out is: region between stock oil entrance 110 to the colvent inlet 120 of extraction tower 100, comprises the position at feed(raw material)inlet and place, colvent inlet 120.
In the present invention, the opening for feed extracting oil refining tank 200 out can establish feed distributor, extracting out in oil refining tank 200 can be that component is not established in slack tank and inside, or inside increases by one to three layers of sieve plate for preventing back-mixing, extract oil refining tank 200 preferably sleeping tank out, it is 50-120 minutes that the volume extracting oil refining tank 200 out meets the mixed solution residence time wherein that an Extract and secondary extract oil out, time extracted oily raffinate out lower than 50 minutes and is separated not exclusively with Extract, time more than 120 minutes under identical purification condition, the yield of raffinate no longer increases, illustrate that extracting oily raffinate out is fully separated with Extract.
About the operational condition of furfural treating tower, when extraction tower 100 pushes up temperature lower than 60 DEG C, the operation easier of extraction tower 100 increases, and higher than 80 DEG C, the selectivity of solvent declines, and can affect the yield of product; When solvent ratio is less than 0.5, the character of product declines, and solvent recovering system operation easier strengthens simultaneously; Solvent ratio can reduce the yield of treated oil higher than 1.0.Preferred furfural extraction condition is, extracting tower top temperature 60 C-80 DEG C, and extracting column bottom temperature is 40 DEG C-50 DEG C, and the mass ratio of solvent and stock oil is 0.5-1.0:1;
About the operational condition of extracting oil refining tank 200 out, secondary extract out oil or secondary Extract through amount that the secondary Extract of evaporation containing a small amount of solvent mixes with Extract and stock oil mass ratio lower than 0.2 and higher than 1.0 time, not obvious to the raising of the yield of treated oil, so the operational condition of extracting oil refining tank 200 out is: the mass ratio that secondary extracts amount that oil or secondary Extract mix with Extract through the secondary Extract of evaporation containing a small amount of solvent and stock oil out is 0.2-1.0:1; About extraction oil refining tank 200 temperature, temperature, lower than 40 DEG C, is extracted oil out and is raffinated oil excessively slow with the velocity of separation of solvent, higher than 50 DEG C, can affect the yield extracted oil out and raffinate oil, so extracting oil refining tank 200 temperature out is 40 DEG C-50 DEG C.
Embodiment 1
With certain wax tailings for stock oil, character sees attached list 1, purification condition is: extraction tower 100 tower top temperature is 60 DEG C, column bottom temperature is 40 DEG C, the mass ratio of solvent furfural and stock oil is 0.5, the operational condition of extracting oil refining tank 200 out is: temperature is 40 DEG C, being mixed into what extract oil refining tank 200 out with Extract is 0.2 through evaporating containing the secondary Extract of a small amount of solvent and the mass ratio of stock oil, the residence time is 50 minutes, the extraction oil raffinate that the top of extracting oil refining tank 200 out is flowed out enters extraction tower 100 from the colvent inlet 120 of extraction tower 100, treated oil 14 is obtained after the raffinate 4 that extraction tower 100 top is flowed out enters refined liquid stripping tower 300 desolvation, character sees attached list 1.
Comparative example 1
Adopt stock oil, extraction process condition and the extraction tower identical with embodiment 1, namely tower top temperature is 60 DEG C, column bottom temperature is 40 DEG C, the mass ratio of solvent furfural and stock oil is 0.5, obtain after an Extract recycling design extracting oil out, obtain treated oil after raffinate recycling design, character sees attached list 1.
Embodiment 2
With certain wax tailings for stock oil, character sees attached list 2, purification condition is: extraction tower 100 tower top temperature is 70 DEG C, column bottom temperature is 40 DEG C, the mass ratio of solvent furfural and stock oil is 0.8, the operational condition of extracting oil refining tank 200 out is: temperature is 40 DEG C, being mixed into what extract oil refining tank 200 out with Extract is 1.0 through evaporating containing the secondary Extract of a small amount of solvent and the mass ratio of stock oil, the residence time is 120 minutes, the extraction oil refining liquid that the top of extracting oil refining tank 200 out is flowed out enters extraction tower 100 from the stock oil entrance 110 of extraction tower 100, treated oil is obtained after the raffinate 4 that extraction tower 100 top is flowed out enters raffinate stripping tower 300 desolvation, character is in table 2.
Comparative example 2
Adopt stock oil, extraction process condition and the extraction tower identical with embodiment 1, namely tower top temperature is 70 DEG C, column bottom temperature is 40 DEG C, the mass ratio of solvent furfural and stock oil is 0.8, obtain after an Extract recycling design extracting oil out, obtain treated oil after raffinate recycling design, character sees attached list 2.
Embodiment 3
With certain wax tailings for stock oil, character sees attached list 3, purification condition is: extraction tower 100 tower top temperature is 60 DEG C, column bottom temperature is 40 DEG C, the mass ratio of solvent furfural and stock oil is 0.5, the operational condition of extracting oil refining tank 200 out is: temperature is 40 DEG C, being mixed into what extract oil refining tank 200 out with Extract is 0.5 through evaporating containing the secondary Extract of a small amount of solvent and the mass ratio of stock oil, the residence time is 100 minutes, the extraction oil raffinate that the top of extracting oil refining tank 200 out is flowed out enters extraction tower 100 between the stock oil entrance 110 and colvent inlet 120 of extraction tower 100, treated oil is obtained after the raffinate 4 that extraction tower 100 top is flowed out enters raffinate stripping tower 300 desolvation, character sees attached list 3.
Comparative example 3
Adopt stock oil, extraction process condition and the extraction tower identical with embodiment 3, namely tower top temperature is 60 DEG C, column bottom temperature is 40 DEG C, the mass ratio of solvent furfural and stock oil is 0.5, obtain after an Extract recycling design extracting oil out, obtain treated oil after raffinate recycling design, character sees attached list 3.
Embodiment 4
With certain wax tailings for stock oil, character sees attached list 4, purification condition is: extraction tower 100 tower top temperature is 80 DEG C, column bottom temperature is 50 DEG C, the mass ratio of solvent furfural and stock oil is 1.0, the operational condition of extracting oil refining tank 200 out is: temperature is 50 DEG C, being mixed into Extract the secondary extracting oil refining tank 200 out, to extract oil out with the mass ratio of stock oil be 1.0, the residence time is 110 minutes, the extraction oil refining liquid that the top of extracting oil refining tank 200 out is flowed out enters extraction tower 100 from the stock oil entrance 110 of extraction tower 100, treated oil is obtained after the raffinate 4 that extraction tower 100 top is flowed out enters raffinate stripping tower 300 desolvation, character is in table 4.
Comparative example 4
Adopt stock oil, extraction process condition and the extraction tower identical with embodiment 1, namely tower top temperature is 80 DEG C, column bottom temperature is 50 DEG C, the mass ratio of solvent furfural and stock oil is 1.0, obtain after an Extract recycling design extracting oil out, obtain treated oil after raffinate recycling design, character sees attached list 4.
Table 1 embodiment 1
Table 2 embodiment 2
Table 3 embodiment 3
Table 4 embodiment 4
As can be seen from table 1-4 embodiment, this invention takes and carry out secondary refining to extraction oil, the raffinate of the extraction oil obtained is returned the way of extraction tower, the solvent extraction with routine is compared, and can improve the yield of product under the same conditions further.
As can be seen from embodiment 1 and comparative example 1: adopt the method to compare with usual vehicle extracting, yield of raffinating oil improves 6.7%, the saturated point of content extracted out in oil is reduced to 10.4% from 20.16% simultaneously, aromatic hydrocarbons, resin and asphalt content increase, and are rich in aromatic hydrocarbons and are conducive to developing industrial chemicals.Other embodiment is also similar results, adopt this inventive method, compare with common furfural extraction, at identical conditions, be raw material with wax tailings, the yield of the solvent-refined oil obtained is maximum can reach more than 10 quality %, compared with raw material, the saturated hydrocarbon content of raffinating oil obviously increases, and sulphur, nitrogen content obviously decline, and is the excellent catalytic cracking of cracking performance or hydrocracking raw material.The aromaticity content extracting oil out is high, is to apply wide industrial chemicals.
Certainly; the present invention also can have other various embodiments; when not deviating from the present invention's spirit and essence thereof; those of ordinary skill in the art are when making various corresponding change and distortion according to the present invention, but these change accordingly and are out of shape the protection domain that all should belong to the claim appended by the present invention.
Claims (17)
1. the solvent refining equipment of a wax tailings inferior, comprise extraction tower, extract oil refining tank, raffinate stripping tower and refining oil tank out, described extraction tower comprises the stock oil entrance being arranged at its underpart, the colvent inlet being arranged at its top, the raffinate outlet that is arranged at an Extract outlet bottom it, is arranged at its top; Described extraction oil refining tank comprises an Extract entrance in portion disposed therein, and described Extract outlet is connected with a described Extract entrance; Described raffinate stripping tower comprises the raffinate entrance being arranged at its underpart and the treated oil outlet be arranged at bottom it, and described raffinate outlet is connected with described raffinate entrance; Described refining oil tank exports with described extraction tower treated oil and is connected, and it is characterized in that, has an extraction oil raffinate pipeline between described extraction oil refining tank and described extraction tower.
2. the solvent refining equipment of wax tailings inferior according to claim 1, it is characterized in that, described extraction oily raffinate pipeline comprises to be extracted the outlet of oily raffinate out and extracts oily raffinate entrance out, the outlet of described extraction oily raffinate is arranged at the top of described extraction oil refining tank, and described extraction oil raffinate entrance to be arranged on described extraction tower and to be positioned at the position of below the position at place, described colvent inlet or described colvent inlet.
3. the solvent refining equipment of wax tailings inferior according to claim 1, it is characterized in that, described extraction oily raffinate pipeline comprises to be extracted the outlet of oily raffinate out and extracts oily raffinate entrance out, the outlet of described extraction oily raffinate is arranged at the top of described extraction oil refining tank, described extraction oily raffinate entrance is arranged at the position between described colvent inlet and described stock oil entrance, comprises the position at described colvent inlet or described stock oil entrance place.
4. the solvent refining equipment of wax tailings inferior according to claim 1, it is characterized in that, also comprise solvent seasoning tower, wet solvent entrance and solvent outlet after being arranged at bottom it drying after described solvent seasoning tower comprises the stripping being arranged at its top, described raffinate stripping tower also comprises the first wet solvent outlet being arranged at its top, described first wet solvent outlet is connected with wet solvent entrance after described stripping, and after described drying, solvent outlet is connected with described colvent inlet.
5. the solvent refining equipment of wax tailings inferior according to claim 4, it is characterized in that, also comprise secondary Extract evaporator tower, described secondary Extract evaporator tower comprises the secondary Extract entrance being arranged at its underpart, solvent outlet and secondary Extract outlet after being arranged at bottom it evaporation after being arranged at the evaporation at its top, described solvent seasoning tower comprises colvent inlet after the evaporation in portion disposed therein, described extraction oil refining tank also comprises the secondary Extract outlet be arranged at bottom it, described secondary Extract outlet is connected with described secondary Extract entrance, after described evaporation, the outlet of secondary Extract is connected with a described Extract entrance, after described evaporation, solvent outlet is connected with colvent inlet after described evaporation.
6. the solvent refining equipment of wax tailings inferior according to claim 5, it is characterized in that, also comprise secondary extract stripper and secondary extraction oil tank, after described secondary extract stripper comprises the evaporation being arranged at its underpart, secondary Extract entrance and the secondary be arranged at bottom it extract oil export out, after described evaporation, the outlet of secondary Extract is connected with secondary Extract entrance after described evaporation, and described secondary extraction oil export is extracted oil tank out with described secondary and is connected.
7. the solvent refining equipment of wax tailings inferior according to claim 6, it is characterized in that, described secondary extract stripper also comprises the second wet solvent outlet being arranged at its top, and described second wet solvent outlet is connected with wet solvent entrance after described stripping.
8. the solvent refining equipment of wax tailings inferior according to claim 6, is characterized in that, described secondary is extracted oil export out and is connected with a described Extract entrance.
9. a method for refining solvent for wax tailings inferior, is characterized in that, adopts the solvent refining equipment of wax tailings inferior according to claim 1 to refine, comprises the steps:
Solvent enters described extraction tower from the top of described extraction tower, stock oil enters described extraction tower from the bottom of described extraction tower and carries out extracting, the Extract that extracting obtains enters described extraction oil refining tank and refines, the refining extraction oil raffinate obtained is back to described extraction tower by described extraction oily raffinate pipeline, the raffinate that in described extraction tower, extracting obtains enters described raffinate stripping tower, and the treated oil that raffinate obtains after carrying out stripping desolvation enters described refining oil tank.
10. the method for refining solvent of wax tailings inferior according to claim 9, it is characterized in that, the wet solvent that described raffinate stripping tower stripping goes out enters described solvent seasoning tower through condensation and carries out drying, and the dried described solvent of described solvent seasoning tower bottom enters described extraction tower and recycles.
The method for refining solvent of 11. wax tailings inferior according to claim 10, it is characterized in that, in described extraction oil refining tank, the refining secondary Extract obtained obtains the secondary Extract containing a small amount of solvent after pervaporation, and the secondary Extract containing a small amount of solvent obtains secondary and extracts oil out after stripping.
The method for refining solvent of 12. wax tailings inferior according to claim 11, it is characterized in that, part secondary extracts oil out or part mixes with the Extract that described extraction tower extracting obtains through the secondary Extract of evaporation containing a small amount of solvent, enters described extraction oil refining tank and refines.
The method for refining solvent of 13. wax tailings inferior according to claim 11, it is characterized in that, the solvent removed during the evaporation of secondary Extract and the wet solvent removed when evaporation contains the secondary Extract stripping of a small amount of solvent enter described solvent seasoning tower respectively and carry out drying.
The method for refining solvent of 14. wax tailings inferior according to claim 12, it is characterized in that, the operational condition of described extraction oil refining tank is: secondary extracts oil out or the mass ratio of the amount that mixes with Extract through the secondary Extract of evaporation containing a small amount of solvent and stock oil is 0.2-1.0:1, the temperature of extracting oil refining tank out is 40 DEG C-50 DEG C, and the residence time that Extract stays in described extraction oil refining tank is 50-120 minutes; The residence time that the mixed solution that part secondary extraction oil or part obtain after the secondary Extract of evaporation containing a small amount of solvent mixes with an Extract stays in described extraction oil refining tank is 50-120 minutes.
The method for refining solvent of 15. wax tailings inferior according to claim 9, it is characterized in that, described stock oil is wax tailings inferior, described solvent is furfural.
The method for refining solvent of 16. wax tailings inferior according to claim 15, is characterized in that, the initial boiling point of described wax tailings inferior is greater than 300 DEG C.
The method for refining solvent of 17. wax tailings inferior according to claim 15, it is characterized in that, described furfural extraction condition is, described extraction tower tower top temperature 60 DEG C-80 DEG C, described extraction tower column bottom temperature is 40 DEG C-50 DEG C, and the mass ratio of described furfural and described wax tailings inferior is 0.5-1.0:1.
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| CN1184842A (en) * | 1997-12-08 | 1998-06-17 | 中国石油化工总公司 | Extraction method for faulty wax oil solvent |
| CN1258666A (en) * | 1999-04-27 | 2000-07-05 | 中国石油化工集团公司 | Saturated hydrocarbon recovering and utilizing technology |
| CN101684185A (en) * | 2008-09-27 | 2010-03-31 | 中国石油天然气股份有限公司 | Production method of high-aromatic-hydrocarbon environment-friendly rubber oil |
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|---|---|---|---|---|
| CN1176295A (en) * | 1996-09-06 | 1998-03-18 | 中国石油化工总公司 | Double-solvant extraction for inferior paraffin base oil |
| CN1184842A (en) * | 1997-12-08 | 1998-06-17 | 中国石油化工总公司 | Extraction method for faulty wax oil solvent |
| CN1258666A (en) * | 1999-04-27 | 2000-07-05 | 中国石油化工集团公司 | Saturated hydrocarbon recovering and utilizing technology |
| CN101684185A (en) * | 2008-09-27 | 2010-03-31 | 中国石油天然气股份有限公司 | Production method of high-aromatic-hydrocarbon environment-friendly rubber oil |
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