CN102041030B - Method for controlling ultrahigh final boiling point of blending component of reformed high-octane gasoline - Google Patents
Method for controlling ultrahigh final boiling point of blending component of reformed high-octane gasoline Download PDFInfo
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- CN102041030B CN102041030B CN 201110006649 CN201110006649A CN102041030B CN 102041030 B CN102041030 B CN 102041030B CN 201110006649 CN201110006649 CN 201110006649 CN 201110006649 A CN201110006649 A CN 201110006649A CN 102041030 B CN102041030 B CN 102041030B
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- 238000002156 mixing Methods 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 27
- 238000009835 boiling Methods 0.000 title claims abstract description 22
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims abstract description 34
- 238000000605 extraction Methods 0.000 claims abstract description 14
- 239000007791 liquid phase Substances 0.000 claims abstract description 6
- 238000001816 cooling Methods 0.000 claims abstract description 5
- 239000002918 waste heat Substances 0.000 claims abstract description 4
- 239000000295 fuel oil Substances 0.000 claims abstract 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 54
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 claims description 27
- 239000000470 constituent Substances 0.000 claims description 13
- 230000008569 process Effects 0.000 claims description 10
- 239000000284 extract Substances 0.000 claims description 7
- 241000282326 Felis catus Species 0.000 claims description 6
- 239000000446 fuel Substances 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 4
- 238000005259 measurement Methods 0.000 claims description 4
- 238000011084 recovery Methods 0.000 claims description 3
- 238000002309 gasification Methods 0.000 claims description 2
- 238000000926 separation method Methods 0.000 claims description 2
- 238000009834 vaporization Methods 0.000 claims description 2
- 230000008016 vaporization Effects 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000012544 monitoring process Methods 0.000 abstract description 4
- 239000008096 xylene Substances 0.000 abstract 4
- 238000004821 distillation Methods 0.000 abstract 2
- 238000010992 reflux Methods 0.000 abstract 2
- 238000010438 heat treatment Methods 0.000 abstract 1
- 238000000691 measurement method Methods 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 5
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical compound CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- UHOVQNZJYSORNB-UHFFFAOYSA-N benzene Substances C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- IVSZLXZYQVIEFR-UHFFFAOYSA-N m-xylene Chemical group CC1=CC=CC(C)=C1 IVSZLXZYQVIEFR-UHFFFAOYSA-N 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a method for controlling the ultrahigh final boiling point of a blending component of reformed high-octane gasoline; c8 +Entering the middle part of a xylene tower; overhead xylene fractionCooling as heat source of other heat-using equipment, returning to the reflux tank at the top of the dimethylbenzene tower, pressurizing, returning a part of the pressurized dimethylbenzene tower as reflux, and cooling the rest of the pressurized dimethylbenzene tower as product; performing liquid phase side extraction on the side-line high-octane gasoline blending component at the lower part of a xylene column extraction section to obtain C9-C10 components, recovering waste heat of a heat exchanger, cooling and conveying the components to a storage tank, wherein the extraction amount is controlled by adopting flow; the heavy component at the bottom of the dimethylbenzene tower is used as heating furnace fuel oil; temperature measuring points are arranged at the upper part and the lower part of the xylene column and at the side draw-out column plate, the drawn-out amount of the product at the top of the column is adjusted by using a temperature difference controller, and the final distillation point of the high-octane gasoline blending component is controlled by the temperature change of the draw-out plate; monitoring the final distillation point of the side-stream high-octane gasoline blending component by adopting a soft measurement method; the gasoline blending component has high yield and low energy consumption.
Description
Technical field
The present invention relates to a kind of method of controlling reformation high octane value gasoline blending component final boiling point superelevation, more particularly, be a kind of method that adopts the benzenol hydrorefining side line to extract out, realize that by the content of heavy constituent in the control gasoline blending component gasoline final boiling point meets the demands.
Background technology
Along with the increasingly stringent that requires of world's environmental regulation, production environment close friend's clean fuel becomes the theme of 21 century petroleum refining industry's development.Catalytic reforming gasoline does not contain alkene substantially, and its sulphur, nitrogen content are extremely low, and vapour pressure is little, and octane value is higher, is a kind of clean gasoline component of high-quality, and reformer can also provide cheap hydrogen source for hydrogenation unit simultaneously.Therefore, greatly develop the reformation technology especially the CONTINUOUS REFORMER technology be the main path that solves this difficult problem.
Reformed oil can be directly as the blending component of gasoline, also can produce aromatic hydrocarbon product through aromatic hydrocarbons extracting or other conversions and separating technology---benzene, toluene and dimethylbenzene.But reformed oil excision C
6, C
7And C
8High octane value gasoline blending component final boiling point after the component is more than 250 ℃, can not satisfy the requirement of China's motor spirit quality standard (GB17930-2006), illustrate and contain too much heavy component in the high octane value gasoline blending component, be difficult to guarantee gasoline evaporation and perfect combustion fully under working conditions, finally cause the interior carbon deposit of petrol engine cylinder to increase, oil consumption increases; Evaporate incomplete gasoline heavy component simultaneously and also can flow into crankcase along cylinder wall, make lubricating oil dilution and add galling, so must take measures its heavy constituent excision is guaranteed that the final boiling point of high octane value gasoline blending component is less than 205 ℃.
Traditional method is to take off heavies column one of benzenol hydrorefining downstream tandem, and cat head is produced the stop bracket gasoline blend component, the oil that acts as a fuel of the heavy constituent at the bottom of the tower.This flow and method has the shortcoming that investment is high, floor space is big, energy consumption is high.And the method that adopts the benzenol hydrorefining side line to extract out can realize deviating from the heavy constituent in the reformed oil in a tower, can guarantee that again the high octane value gasoline blending component final boiling point satisfies national gasoline standard requirement simultaneously.This method is compared with traditional heavies column flow process of taking off, the advantage that have reduced investment, take up an area of less, energy consumption is low, yield is high.
Summary of the invention
The purpose of this invention is to provide a kind of benzenol hydrorefining side line that adopts and extract the method for controlling reformation high octane value gasoline blending component final boiling point superelevation out, in a tower, realized deviating from the heavy constituent in the reformed oil.
The present invention is with excision C
6, C
7After C
8 +Send into the benzenol hydrorefining middle part, by pressurized operation, overhead gas can be other and provides thermal source with hot equipment, carries out UTILIZATION OF VESIDUAL HEAT IN, cuts down the consumption of energy, and cooling back overhead product is xylol.Benzenol hydrorefining bottom profit reduction and reserving section arranges side line, extracts liquid phase C out
9～C
10The low-pressure steam recovery waste heat after taking place, by pumping out as high octane value gasoline blending component in component.The heavy constituent oil that acts as a fuel at the bottom of the tower.
The present invention arranges temperature difference recording controller and the temperature monitoring point is adjusted the sideline product quality at benzenol hydrorefining.Temperature difference recording controller is the extraction amount of adjusting overhead product by the temperature that compares the sensitive column plate in the upper and lower, stablize the given setting temperature difference in this way, guarantee the quality product of dimethylbenzene, utilize the temperature of the point for measuring temperature of side-draw plate simultaneously, adjust sideline product produced quantity control sideline product quality.
Sideline product produced quantity of the present invention adopts flow control.
The present invention carries out the final boiling point monitoring by the method that adopts soft measurement to the side line high octane gasoline component.Soft basic principle of measurement is: the vapour-liquid load has very big relation in the fractionation separates effect of logistics and the tower, and the vapour-liquid load then can be obtained by enthalpy balance and material balance; Temperature EFV for equilibrium flash vaporization gasification (EFV)
t, then there is funtcional relationship:
EFV
t＝f(t，p，x
ml，K)
In the formula:
T-extracts the temperature of plate place's logistics out;
P-extracts the pressure of plate place's logistics out;
x
MlThe liquid phase mole fraction of-extraction stream components;
The K-material characteristic factor.
The numerical applications formula of corresponding A STMD86
ASTMD86＝f(EFV
t，SG)
In the formula:
SG-proportion.
Utilize the API chart, find the value of 90% in gasoline and final boiling point (100% point).
Superiority of the present invention:
(1) gasoline blending component yield height
If adopt two traditional tower serial flows, in order to guarantee to take off the normal running of heavies column, heavy constituent have certain flow at the bottom of must guaranteeing tower, certainly will cause in the heavy constituent at the bottom of the tower and have certain light constituent, thereby influenced the yield of high octane value gasoline blending component, the method that adopts the benzenol hydrorefining side line to extract out can remedy this deficiency, and the high octane gasoline component yield can increase by 0.5～1%.Be example with 2,000,000 tons of/year continuous reformers, only increase stop bracket gasoline blend component yield and can be enterprise an every year and increase by 5,000 ten thousand yuan of benefits.
(2) less energy-consumption
The potential temperature of benzenol hydrorefining side line extractum can take full advantage of thermal source than higher, realizes heat integration, has reduced the general facilities consumption of full device, has reduced the energy consumption of device.Compare with establishing the two tower flow processs of taking off the heavies column system, need still less boiling hot amount and condensation number again, can save energy about 15%.
(3) reduced investment
Adopt benzenol hydrorefining to take out the side line flow process, only adopt a tower, compare with the two tower serial flows that take off the heavies column system are arranged, only need the equipment of half, so can significantly reduce cost of investment.
(4) floor space is few
The side line flow process of taking out the employing benzenol hydrorefining has reduced takes off the heavies column system, has simplified technical process, has reduced floor space, and floor space reduces can reach 25%.
Two kinds of schemes relatively see Table 1.
Table 1 traditional scheme and benzenol hydrorefining side line are extracted the scheme comparison sheet out
| Project | Set up and take off the heavies column scheme | The benzenol hydrorefining side line is extracted scheme out |
| Floor space | Radix+25% | Radix |
| Investment cost | Radix+12% | Radix |
| General facilities consumes | Radix+15% | Radix |
| The high octane gasoline component yield | Radix-0.5～1.0% | Radix |
Description of drawings
Fig. 1 is that the benzenol hydrorefining side line is extracted schematic flow sheet out.
Embodiment
Now by reference to the accompanying drawings 1, technology contents of the present invention is further described.
Method provided by the invention is so concrete enforcement:
The stable gasoline that comes from continuous reformer removes C through the reformate separation column
6, C
7C after the component
8 +Enter benzenol hydrorefining 7 middle parts, be divided into dimethylbenzene cut (cat head), high octane value gasoline blending component (side line) and heavy constituent (at the bottom of the tower).Cat head dimethylbenzene cut returns dimethylbenzene cat head return tank 5 after lowering the temperature as other thermals source with hot equipment 6, and jar end liquid part after pump 4 pressurizations is returned benzenol hydrorefining as backflow, and storage tank is delivered to as product in all the other cooling backs.Gasoline blending component carries out the liquid phase side line at benzenol hydrorefining profit reduction and reserving pars infrasegmentalis to be extracted out, and Extract is delivered to storage tank as high octane value gasoline blending component through overcooling by pump 2 again after interchanger 1 generation low-pressure steam is carried out waste heat recovery, and the extraction amount adopts flow control.Heavy constituent are as process furnace 3 oil fuel at the bottom of the benzenol hydrorefining.Be the monitoring product quality, on benzenol hydrorefining top, bottom and side-draw plate place arrange point for measuring temperature, utilize temperature difference recording controller to adjust overhead product extraction amount and control the dimethylbenzene quality product, utilize sidedraw plate temperature adjustment extraction amount simultaneously, guarantee that the high octane value gasoline blending component final boiling point is qualified.
Following example will give further instruction to technology provided by the present invention, but not thereby limiting the invention.
Embodiment 1
Adopt the benzenol hydrorefining side line to extract flow process out and produce high octane value gasoline blending component: processing condition are: inlet amount is 129000t/h, raw material is formed as shown in table 2, the benzenol hydrorefining working pressure is 0.53MPa (g), stage number is 101 layers, side line is extracted the position out 90 layers (counting from top to down), and processing parameter is as shown in table 3.The result shows that the gasoline blending component final boiling point is 198.6 ℃, and the extraction amount is 66188kg/h.Compare with two tower flow processs, the gasoline blending component yield improves 0.98%, reboiler thermal load energy-conservation 15.4%.
Table 2 raw material is formed
| Form | Shared mark |
| C 8Alkane | 0.0113 |
| Ethylbenzene | 0.0887 |
| O-Xylol | 0.1981 |
| M-xylene | 0.0934 |
| P-Xylol | 0.1232 |
| C 9Alkane | 0.0062 |
| C 9Aromatic hydrocarbons | 0.3887 |
| C 10Aromatic hydrocarbons | 0.0794 |
| C 11Aromatic hydrocarbons | 0.011 |
Comparative Examples 1
Employing is provided with the two tower serial flows that take off the heavies column system and produces high octane value gasoline blending component: processing condition are: inlet amount is 129000kg/h, raw material is formed as shown in table 2, the benzenol hydrorefining working pressure is 0.527MPa (g), and taking off the heavies column working pressure is 0.19MPa (g).The result shows that the gasoline blending component final boiling point is 198.3 ℃, and flow is 65541kg/h, needs 139 blocks of column plates altogether.
Table 3 liang flow process parameter comparison table look-up
Claims (3)
1. method of controlling reformation high octane value gasoline blending component final boiling point superelevation is characterized in that: the stable gasoline that comes from continuous reformer removes C through the reformate separation column
6, C
7C after the component
8 +Enter benzenol hydrorefining middle part, be divided into heavy constituent at the bottom of cat head dimethylbenzene cut, side line high octane value gasoline blending component and the tower; Cat head dimethylbenzene cut returns dimethylbenzene cat head return tank after lowering the temperature as other thermal source with hot equipment, and jar end liquid part after the pump pressurization is returned benzenol hydrorefining as backflow, and storage tank is delivered to as product in all the other cooling backs; The side line high octane value gasoline blending component carries out the liquid phase side line at benzenol hydrorefining profit reduction and reserving pars infrasegmentalis and extracts C out
9-C
10Component, Extract after interchanger generation low-pressure steam is carried out waste heat recovery, again through overcooling by being pumped to storage tank as high octane value gasoline blending component, the extraction amount adopts flow control; Heavy constituent are as process furnace oil fuel at the bottom of the benzenol hydrorefining; On benzenol hydrorefining top, bottom and sidedraw plate place arrange point for measuring temperature, the mode of utilizing temperature difference recording controller to adjust overhead product extraction amount is stablized the given setting temperature difference and is controlled the dimethylbenzene quality product, change control high octane value gasoline blending component final boiling point simultaneously by extracting plate temperature out; The final boiling point of side line high octane value gasoline blending component adopts the method for soft measurement to monitor.
2. the method for control reformation high octane value gasoline blending component final boiling point superelevation according to claim 1, it is characterized in that: temperature difference recording controller is the quality index of adjusting overhead product by the temperature between the sensitive column plate in comparison the upper and lower, change control high octane value gasoline blending component final boiling point simultaneously by extracting plate temperature out.
3. the method for control reformation high octane value gasoline blending component final boiling point superelevation according to claim 1 is characterized in that:
Soft measurement is: (1) obtains the vapour-liquid load by enthalpy balance and the material balance of cat head part,
(2) obtain the temperature EFV of equilibrium flash vaporization gasification EFV
t:
EFV
t=f(t,p,x
ml,K)
In the formula:
The temperature of t-extraction plate place's logistics;
The pressure of p-extraction plate place's logistics;
x
MlThe liquid phase mole fraction of-extraction stream components;
K-material characteristic the factor;
(3) use ASTMD86=f (EFV
t, SG) funtcional relationship
In the formula:
SG-proportion;
Utilize the API chart, find the value of 90% in gasoline and final boiling point.
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| CN 201110006649 CN102041030B (en) | 2011-01-13 | 2011-01-13 | Method for controlling ultrahigh final boiling point of blending component of reformed high-octane gasoline |
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|---|---|---|---|
| CN 201110006649 CN102041030B (en) | 2011-01-13 | 2011-01-13 | Method for controlling ultrahigh final boiling point of blending component of reformed high-octane gasoline |
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| CN102041030B true CN102041030B (en) | 2013-07-03 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102660315B (en) * | 2012-04-12 | 2015-04-01 | 中国寰球工程公司 | Device for controlling endpoint of gasoline blending component extracted from tower sideline vapor phase and method thereof |
| CN107325836A (en) * | 2017-08-10 | 2017-11-07 | 山东汇丰石化集团有限公司 | The equipment for reducing the reformed oil end point of distillation |
| CN114212841A (en) * | 2021-11-15 | 2022-03-22 | 北方华锦化学工业股份有限公司 | Method for quickly and accurately positioning ammonia enrichment area of acid water stripper |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6143166A (en) * | 1998-08-17 | 2000-11-07 | Chevron Chemical Co. Llc | Process for production of aromatics in parallel reformers with an improved catalyst life and reduced complexity |
| CN101028985A (en) * | 2006-12-06 | 2007-09-05 | 湖南长岭石化科技开发有限公司 | Method for producing benzene arenes from coarse benzene |
| CN101824336A (en) * | 2010-04-22 | 2010-09-08 | 中国寰球工程公司辽宁分公司 | Technique for producing terphenyl, indane and aromatics solvent oil by cracking C9 fraction and hydrogenation |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3010779B2 (en) * | 1991-04-24 | 2000-02-21 | 東ソー株式会社 | Benzene distillation method |
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2011
- 2011-01-13 CN CN 201110006649 patent/CN102041030B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6143166A (en) * | 1998-08-17 | 2000-11-07 | Chevron Chemical Co. Llc | Process for production of aromatics in parallel reformers with an improved catalyst life and reduced complexity |
| CN101028985A (en) * | 2006-12-06 | 2007-09-05 | 湖南长岭石化科技开发有限公司 | Method for producing benzene arenes from coarse benzene |
| CN101824336A (en) * | 2010-04-22 | 2010-09-08 | 中国寰球工程公司辽宁分公司 | Technique for producing terphenyl, indane and aromatics solvent oil by cracking C9 fraction and hydrogenation |
Non-Patent Citations (1)
| Title |
|---|
| JP特开平6-166640A 1994.06.14 |
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