CN102041030B - Method for controlling and reforming ultrahigh final boiling point of high-octane gasoline blending component - Google Patents
Method for controlling and reforming ultrahigh final boiling point of high-octane gasoline blending component 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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Abstract
The invention relates to a method for controlling and reforming an ultrahigh final boiling point of a high-octane gasoline blending component. The method comprises the following steps: feeding C8<+> into the middle part of a xylene tower; after xylene fractions (at the top of the tower) as the heat sources of other heat-used devices are cooled, returning the xylene fractions to a reflux accumulator at the top of the xylene tower, pressurizing the xylene fractions, then returning part of the pressurized xylene fractions to the xylene tower to serve as reflux, and cooling the rest part of xylene fractions to serve as products; carrying out fluid-phase side-draw on the side high-octane gasoline blending component at the lower part of the retention section of the xylene tower so as to draw out C9 to C10 components, after carrying out waste heat recovery on the C9 to C10 components by utilizing a heat exchanger, cooling the C9 to C10 components and then sending the C9 to C10 components to a storage tank, wherein the drawing amount of the C9 to C10 components are subject to flow control; taking heavy components at the bottom of the xylene tower as the fuel oil of a heating furnace; and setting temperature measuring points at the upper and lower parts of the xylene tower and a side-draw plate, adjusting the product drawing amount at the top of the tower by a differential temperature controller, and then through the temperature variation of the side-draw plate, controlling the final boiling point of the high-octane gasoline blending component. The method has the advantages that the final boiling point of the side high-octane gasoline blending component is monitored by using a soft measurement method; and the obtained gasoline blending component yield is high, and the energy consumption is low.
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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| 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 |
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| 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
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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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