CN102660315B - Device for controlling endpoint of gasoline blending component extracted from tower sideline vapor phase and method thereof - Google Patents
Device for controlling endpoint of gasoline blending component extracted from tower sideline vapor phase and method thereof Download PDFInfo
- Publication number
- CN102660315B CN102660315B CN201210107363.6A CN201210107363A CN102660315B CN 102660315 B CN102660315 B CN 102660315B CN 201210107363 A CN201210107363 A CN 201210107363A CN 102660315 B CN102660315 B CN 102660315B
- Authority
- CN
- China
- Prior art keywords
- removing column
- weight
- interchanger
- heat exchanger
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a device for controlling the endpoint of a gasoline blending component extracted from a tower sideline vapor phase and a method thereof. In the device, a first heat exchanger is connected with a weight-removing column phase and stabilized gasoline passes through the first heat exchanger and enters into the weight-removing column; A pipeline at the top of the weight-removing column is connected with a second heat exchanger, which is connected with a reflux drum phase through the pipeline; a light component at the top of the tower passes through the pipeline at the top of the tower, undergoes heat exchange in the second heat exchanger and enters into the reflux drum after cooling; one part of the light component returns to the top of the weight-removing column by the use of a first discharging pump and the other part is outputted as a product; rectifying section sideline of the weight-removing column and/or stripping section sideline are respectively connected with a third heat exchanger and the first heat exchanger; the flow rate of the gasoline blending component extracted from a liquid phase of the rectifying section and/or a vapor phase of the stripping section is controlled according to the temperature change of a temperature measuring point; the extracted gasoline blending component undergoes heat exchange in the third heat exchanger and the first heat exchanger and then is outputted after cooling; a second discharging pump is arranged at the bottom of the weight-removing column, and a removed heavier component is outputted by the second discharging pump.
Description
Technical field
The present invention relates to oil refining and petrochemical industry, extract the device and method controlling gasoline blending component and do in particular to a kind of tower side line vapour phase out.
Background technology
Gasoline endpoint is Con trolling index important in motor spirit national standard, and current standard GB/T 17930-2006 middle finger is designated as and is not more than 205 DEG C.What existing production equipment generally adopted is the method that multitower cuts step by step, Fig. 1 is the schematic flow sheet adopting double tower control gasoline blending component to do in prior art, in FIG, 101 is lightness-removing column, 102 is weight-removing column, 103,104 is cold exchange device, 105,106 is return tank, 107,108 is heating installation, 109,110,111,112 is pump, and arrow A 1 is stable gasoline, and arrow A 2 is light constituent (comprising petroleum naphtha or other products), arrow A 3 is gasoline blending component, and arrow A 4 is heavy constituent.As shown in Figure 1, light constituent is removed in a tower to the gasoline after stable and completes requirement to vapour pressure of gasoline (if produce C8 aromatic hydrocarbons, then separate C8 aromatic hydrocarbons from tower top), then remove heavy constituent with another tower, weight-removing column top gasoline blending component meets does requirement.
But prior art adopts multitower to carry out removing problems such as causing that energy consumption is higher, floor space is comparatively large, investment is higher.
Summary of the invention
The invention provides a kind of tower side line vapour phase and extract the device and method controlling gasoline blending component and do out, adopt multitower to carry out removing and cause the problems such as energy consumption is higher, floor space is comparatively large, investment is higher in order to overcome prior art.
For achieving the above object, the invention provides a kind of tower side line vapour phase and extracting the device controlling gasoline blending component and do out, comprising: weight-removing column, First Heat Exchanger, the second interchanger, the 3rd interchanger and return tank, wherein
First Heat Exchanger is connected with weight-removing column, and stable gasoline enters weight-removing column after First Heat Exchanger heating;
The overhead line of weight-removing column is connected with the second interchanger, second interchanger is connected with return tank by pipeline, return tank is connected with the first discharging pump, the light constituent of tower top enters return tank after overhead line also heat exchange cooling occurs in the second heat exchanger, cooled a part of light constituent is back to weight-removing column tower top through the first discharging pump, and rest part is as output of products;
Weight-removing column rectifying section side line and/or stripping section side line are connected with the 3rd interchanger, First Heat Exchanger successively, rectifying section sidedraw plate and/or stripping section sidedraw plate are provided with point for measuring temperature, control according to the temperature variation of point for measuring temperature the flow extracting gasoline blending component from rectifying section liquid phase and/or stripping section vapour phase, extract gasoline blending component out and export after the 3rd interchanger, First Heat Exchanger heat exchange cooling;
Be provided with the second discharging pump at the bottom of the tower of weight-removing column, the heavy constituent removed exports through the second discharging pump.
Further, overhead line is connected with one or more pipeline, one or more pipeline is connected with the overhead line before return tank after heating equipment.
Further, the second interchanger and the 3rd interchanger pass into coolant media respectively.
Further, the tower top pressure of weight-removing column is 0.05 ~ 15.0MPaG, and tower top temperature is 150 ~ 280 DEG C.
Further, said apparatus also comprises:
Other heating equipment, between being connected at the bottom of the export pipeline of the second discharging pump and the tower of weight-removing column, is delivered to weight-removing column using after a part of heavy constituent heating as thermal source.
For achieving the above object, present invention also offers a kind of tower side line vapour phase and extract the method controlling gasoline blending component and do out, the method comprises the following steps:
Stable gasoline is sent into weight-removing column after First Heat Exchanger heating, and wherein First Heat Exchanger is connected with weight-removing column;
The light constituent of tower top is sent into return tank after overhead line also heat exchange cooling occurs in the second heat exchanger, cooled a part of light constituent is back to weight-removing column tower top through the first discharging pump, rest part is as output of products, wherein the overhead line of weight-removing column is connected with the second interchanger, second interchanger is connected with return tank, and return tank is connected with the first discharging pump;
The flow extracting gasoline blending component from rectifying section liquid phase and/or stripping section vapour phase is controlled according to the temperature variation of point for measuring temperature on rectifying section sidedraw plate and/or stripping section sidedraw plate, extract gasoline blending component out to export after the 3rd interchanger, First Heat Exchanger heat exchange cooling, wherein weight-removing column rectifying section side line and/or stripping section side line are connected with the 3rd interchanger, First Heat Exchanger successively;
The heavy constituent removed is exported through the second discharging pump be arranged at the bottom of weight-removing column tower.
Further, overhead line is connected with one or more pipeline, one or more pipeline is connected with the overhead line before return tank after heating equipment.
Further, the second interchanger and the 3rd interchanger pass into coolant media respectively.
Further, the tower top pressure of weight-removing column is 0.05 ~ 15.0MPaG, and tower top temperature is 150 ~ 280 DEG C.
Further, aforesaid method is further comprising the steps of:
Weight-removing column is delivered to as thermal source after the heating equipment between at the bottom of the tower of the export pipeline and weight-removing column of a part of heavy constituent through being connected to the second discharging pump heats.
In the above-described embodiments, control gasoline blending component by single tower to do, equipment institute floor space is less, it is less to invest, simultaneously by making full use of the heat energy that each component is carried, reduce the energy consumption of device, and control to extract gasoline blending component out according to the extraction plate temperature change that the point for measuring temperature that sidedraw plate is arranged detects to do, gasoline blending component yield is higher.
Accompanying drawing explanation
In order to be illustrated more clearly in the embodiment of the present invention or technical scheme of the prior art, be briefly described to the accompanying drawing used required in embodiment or description of the prior art below, apparently, accompanying drawing in the following describes is only some embodiments of the present invention, for those of ordinary skill in the art, under the prerequisite not paying creative work, other accompanying drawing can also be obtained according to these accompanying drawings.
Fig. 1 is the schematic flow sheet adopting double tower control gasoline blending component to do in prior art;
Fig. 2 is that the tower side line vapour phase of one embodiment of the invention extracts the schematic flow sheet controlling gasoline blending component and do out.
Embodiment
Below in conjunction with the accompanying drawing in the embodiment of the present invention, be clearly and completely described the technical scheme in the embodiment of the present invention, obviously, described embodiment is only the present invention's part embodiment, instead of whole embodiments.Based on the embodiment in the present invention, those of ordinary skill in the art, not paying the every other embodiment obtained under creative work prerequisite, belong to the scope of protection of the invention.
Fig. 2 is that the tower side line vapour phase of one embodiment of the invention extracts the schematic flow sheet controlling gasoline blending component and do out.As shown in Figure 2, this device comprises: weight-removing column 201, First Heat Exchanger 202, second interchanger 203, the 3rd interchanger 205 and return tank 204, wherein
First Heat Exchanger 202 is connected with weight-removing column 201, and stable gasoline enters weight-removing column 201 after First Heat Exchanger 202 heats;
The overhead line of weight-removing column 201 is connected with the second interchanger 203, second interchanger 203 is connected with return tank 204, return tank 204 is connected with the first discharging pump 208, the light constituent of tower top through overhead line and occur in the second interchanger 203 heat exchange cooling after enter return tank 204, cooled a part of light constituent is back to weight-removing column 201 tower top after the first discharging pump 208, and rest part is as output of products;
Weight-removing column rectifying section side line (selecting whether to arrange according to the distribution situation of gasoline blending component in weight-removing column) and/or stripping section side line are connected with the 3rd interchanger 205, First Heat Exchanger 202 successively, rectifying section sidedraw plate and/or stripping section sidedraw plate are provided with point for measuring temperature, control according to the temperature variation of point for measuring temperature the flow extracting gasoline blending component from rectifying section liquid phase and/or stripping section vapour phase, extract gasoline blending component out and export after the 3rd interchanger 205, First Heat Exchanger 202 heat exchange cooling;
Be provided with the second discharging pump 207 at the bottom of the tower of weight-removing column 201, the heavy constituent removed exports through the second discharging pump 207.
In fig. 2, arrow B 1 is stable gasoline, and arrow B 2 is that the 3rd interchanger changes thermogenetic steam, arrow B 3 is de-oxygenised water, and arrow B 6 is that the second interchanger changes thermogenetic steam, and arrow B 7 is de-oxygenised water, arrow B 10 is light constituent, and arrow B 11 is heavy constituent, and arrow B 12 is gasoline blending component.
In the above-described embodiments, control gasoline blending component by single tower to do, equipment institute floor space is less, it is less to invest, simultaneously by making full use of the heat energy that each component is carried, reduce the energy consumption of device, and control to extract gasoline blending component out according to the extraction plate temperature change that the point for measuring temperature that sidedraw plate is arranged detects to do, gasoline blending component yield is higher.
Such as, the heat energy that the light constituent flowed out for making full use of tower top carries, overhead line is connected with one or more pipeline, one or more pipeline is connected with the overhead line before return tank after heating equipment, the heat energy that light constituent is carried as miscellaneous equipment thermal source and produce low-pressure steam, reach energy-conservation object.As heating equipment 1 is gone in arrow B in Fig. 24 instruction, heating equipment 2 is gone in arrow B 5 instruction, and arrow B 8, B9 instruction returns overhead line by heating equipment 1,2.
Such as, the second interchanger and the 3rd interchanger pass into coolant media (as deaerated water), respectively there is steam.
For ensureing the quality requirements of overhead stream, according to different cut split requirements or overhead product requirement, can select different temperature, pressure control strategy, such as, the tower top pressure of weight-removing column can be 0.05 ~ 15.0MPaG, and tower top temperature is 150 ~ 280 DEG C.
The gasoline component of C8 aromatic hydrocarbons and heavy aromatics component is rich in continuous catalytic reforming, does and does not meet Standard, can apply the present invention and produce qualified gasoline blending component.Illustrative example is given technology provided by the present invention and being further illustrated below, but not thereby limiting the invention.
Continuous catalytic reforming device is rich in the gasoline component of C8 aromatic hydrocarbons and heavy aromatics component, need to produce the gasoline blending component meeting national standard and require, tower top produces C8 aromatic hydrocarbons, and stripping section side line vapour phase extracts gasoline blending component out, is the heavy aromatics component affecting gasoline endpoint removed at the bottom of tower.When being rich in C8 aromatic hydrocarbons and heavy aromatics component streams for the treatment of continuous catalytic reforming device, weight-removing column operational condition can design within the scope of tower top pressure 0.05 ~ 15.0MPaG and tower top temperature 150 ~ 280 DEG C.Now illustrate with example, weight-removing column feed stream composition is as table 1.
Table 1
| Feed composition | Composition (wt%) |
| Toluene | 0.18 |
| C8 alkane | 0.01 |
| C8 aromatic hydrocarbons | 49.87 |
| C9 alkane | 0.05 |
| C9 aromatic hydrocarbons | 37.11 |
| C9 cycloalkanes | 0.15 |
| C10 aromatic hydrocarbons | 12.09 |
| C11 aromatic hydrocarbons | 0.34 |
| C12+ | 0.20 |
| Add up to | 100.00 |
It is as shown in table 2 that the material balance needed is separated task, produces qualified C8 aromatic hydrocarbons and gasoline blending component.
Table 2
| Charging | Flow (kg/hr) | Product | Flow (kg/hr) |
| Reformation C8+ component | 121104.20 | C8 aromatic hydrocarbons | 59625.00 |
| Gasoline blending component | 60995.50 | ||
| Heavy aromatics | 483.70 | ||
| Add up to | 121104.20 | Add up to | 121104.20 |
Adopt the inventive method processing list 1 constitutive material, complete table 2 when requiring, the processing condition of weight-removing column are: inlet amount 121104.2kg/hr, tower top working pressure 0.526MPaG, tower top temperature 224.10 DEG C, tower top C8 aromatic hydrocarbons flow 59625kg/hr, gasoline blending component is from the 91st laminate (totally 101 layers of tower tray, from up to down number) top vapour phase extraction, extract gasoline blending composition flow rate 60995.5kg/hr out, do 199.64 DEG C.
And adopt traditional process processing list 1 constitutive material, complete table 2 when requiring, need two towers, C8 aromatic hydrocarbons tower (i.e. lightness-removing column amounts to 94 layers of column plate) and weight-removing column (altogether 38 layers of column plate).First raw material enters C8 aromatic hydrocarbons tower, and tower top obtains C8 aromatic hydrocarbons, and tower base stream is done 206.3 DEG C and exceeded Standard, as weight-removing column charging; Weight-removing column top obtains qualified gasoline blending component, is the heavy aromatics component affecting gasoline endpoint at the bottom of tower.C8 aromatic hydrocarbons tower inlet amount 121104.2kg/hr, tower top working pressure 0.526MPaG, tower top temperature 224.10 DEG C, tower top C8 aromatic hydrocarbons flow 59625kg/hr; Weight-removing column top working pressure 0.13MPaG, tower top temperature 217.40 DEG C, top gasoline blending composition flow rate 60995.5kg/hr, does 199.32 DEG C.
Above-mentioned two kinds of flow processs contrast situation is as shown in table 3:
Table 3
Such as, said apparatus also comprises: process furnace 206, between being connected at the bottom of the export pipeline of the second discharging pump 207 and the tower of weight-removing column 201, is delivered to weight-removing column using after a part of heavy aromatics component heating as thermal source.
Below for tower side line vapour phase extracts the method controlling gasoline blending component and do out, comprise the following steps:
Stable gasoline is sent into weight-removing column after First Heat Exchanger heating, and wherein First Heat Exchanger is connected with weight-removing column;
The light constituent of tower top is sent into return tank after overhead line also heat exchange cooling occurs in the second heat exchanger, cooled a part of light constituent is back to weight-removing column tower top through the first discharging pump, rest part is as output of products, wherein the overhead line of weight-removing column is connected with the second interchanger, second interchanger is connected with return tank, and return tank is connected with the first discharging pump;
Control (to select according to the distribution situation of gasoline blending component weight-removing column from rectifying section liquid phase according to the temperature variation of point for measuring temperature on rectifying section sidedraw plate and/or stripping section sidedraw plate, if need to extract a part from rectifying section liquid phase) and/or stripping section vapour phase extract the flow of gasoline blending component, extract gasoline blending component out through the 3rd interchanger, export after First Heat Exchanger heat exchange cooling, wherein weight-removing column rectifying section side line (selecting whether to arrange according to the distribution situation of gasoline blending component in weight-removing column) and/or stripping section side line successively with the 3rd interchanger, First Heat Exchanger is connected,
The heavy constituent removed is exported through the second discharging pump be arranged at the bottom of weight-removing column tower.
Such as, the heat energy that the light constituent flowed out for making full use of tower top carries, overhead line is connected with one or more pipeline, one or more pipeline is connected with the overhead line before return tank after heating equipment, the heat energy that light constituent is carried as miscellaneous equipment thermal source and produce low-pressure steam, reach energy-conservation object.As heating equipment 1 is gone in arrow B in Fig. 24 instruction, heating equipment 2 is gone in arrow B 5 instruction, and arrow B 8, B9 instruction returns overhead line by heating equipment 1,2.
Such as, the second interchanger and the 3rd interchanger pass into coolant media (as deaerated water), respectively there is steam.
For ensureing the quality requirements of overhead stream, according to different cut split requirements or overhead product requirement, can select different temperature, pressure control strategy, such as, the tower top pressure of weight-removing column can be 0.05 ~ 15.0MPaG, and tower top temperature is 150 ~ 280 DEG C.
Such as, aforesaid method is further comprising the steps of:
Weight-removing column is delivered to as thermal source after the heating equipment between at the bottom of the tower of the export pipeline and weight-removing column of a part of heavy constituent through being connected to the second discharging pump heats.
As can be seen from above-described embodiment, present invention achieves following beneficial effect:
(1) traditional double tower scheme general facilities consume and equipment number of units more than single tower scheme, cause energy consumption about increase by 8% and production cost about increase by 10%;
(2) traditional double tower planning device number of units is more than single tower scheme, and floor space approximately increases by 30%;
(3) each specialized material such as traditional double tower planning device number of units, occupation of land, pipeline, instrument, framework, cable is more than single tower scheme, and causing investing approximately increases by 24%;
Visible, above-described embodiment controls gasoline blending component by single tower and does, equipment institute floor space is less, it is less to invest, simultaneously by making full use of the heat energy that each component is carried, reduce the energy consumption of device, and control to extract gasoline blending component out according to the extraction plate temperature change that the point for measuring temperature that sidedraw plate is arranged detects to do, gasoline blending component yield is higher.
One of ordinary skill in the art will appreciate that: accompanying drawing is the schematic diagram of an embodiment, the module in accompanying drawing or flow process might not be that enforcement the present invention is necessary.
One of ordinary skill in the art will appreciate that: the module in the device in embodiment can describe according to embodiment and be distributed in the device of embodiment, also can carry out respective change and be arranged in the one or more devices being different from the present embodiment.The module of above-described embodiment can merge into a module, also can split into multiple submodule further.
Last it is noted that above embodiment is only in order to illustrate technical scheme of the present invention, be not intended to limit; Although with reference to previous embodiment to invention has been detailed description, those of ordinary skill in the art is to be understood that: it still can be modified to the technical scheme described in previous embodiment, or carries out equivalent replacement to wherein portion of techniques feature; And these amendments or replacement, do not make the essence of appropriate technical solution depart from the spirit and scope of embodiment of the present invention technical scheme.
Claims (8)
1. tower side line vapour phase extracts the device controlling gasoline blending component and do out, it is characterized in that, comprising: weight-removing column, First Heat Exchanger, the second interchanger, the 3rd interchanger and return tank, wherein
Described First Heat Exchanger is connected with described weight-removing column, and stable gasoline enters described weight-removing column after described First Heat Exchanger heating;
The overhead line of described weight-removing column is connected with described second interchanger, described second interchanger is connected with described return tank by pipeline, described return tank is connected with the first discharging pump, the light constituent of tower top through described overhead line and occur in described second interchanger heat exchange cooling after enter described return tank, cooled a part of light constituent is back to described weight-removing column tower top through described first discharging pump, and rest part is as output of products;
Described weight-removing column rectifying section side line and/or stripping section side line are connected with described 3rd interchanger, described First Heat Exchanger successively, described rectifying section sidedraw plate and/or stripping section sidedraw plate are provided with point for measuring temperature, control according to the temperature variation of described point for measuring temperature the flow extracting gasoline blending component from rectifying section liquid phase and/or stripping section vapour phase, extract gasoline blending component out and export after described 3rd interchanger, described First Heat Exchanger heat exchange cooling;
Be provided with the second discharging pump at the bottom of the tower of described weight-removing column, the heavy constituent removed exports through described second discharging pump;
Described overhead line is connected with one or more pipeline, described one or more pipeline is connected with the described overhead line before described return tank after heating equipment.
2. device according to claim 1, is characterized in that, described second interchanger and described 3rd interchanger pass into coolant media respectively.
3. device according to claim 1, is characterized in that, the tower top pressure of described weight-removing column is 0.05 ~ 15.0MPaG, and tower top temperature is 150 ~ 280 DEG C.
4. device according to claim 1, is characterized in that, also comprises:
Heating equipment, between being connected at the bottom of the export pipeline of described second discharging pump and the tower of described weight-removing column, is delivered to described weight-removing column using after a part of heavy constituent heating as thermal source.
5. tower side line vapour phase extracts the method controlling gasoline blending component and do out, it is characterized in that, comprises the following steps:
Stable gasoline is heated laggard feeding weight-removing column through First Heat Exchanger, and wherein said First Heat Exchanger is connected with described weight-removing column;
The light constituent of tower top is sent into return tank after overhead line also heat exchange cooling occurs in the second heat exchanger, cooled a part of light constituent is back to described weight-removing column tower top after the first discharging pump, rest part is as output of products, the overhead line of wherein said weight-removing column is connected with described second interchanger, described second interchanger is connected with described return tank by pipeline, and described return tank is connected with the first discharging pump;
The flow extracting gasoline blending component from rectifying section liquid phase and/or stripping section vapour phase is controlled according to the temperature variation of point for measuring temperature on rectifying section sidedraw plate and/or stripping section sidedraw plate, extract gasoline blending component out to export after the 3rd interchanger, described First Heat Exchanger heat exchange cooling, wherein said weight-removing column rectifying section side line and/or stripping section side line are connected with described 3rd interchanger, described First Heat Exchanger successively;
The heavy constituent removed is exported through the second discharging pump be arranged at the bottom of described weight-removing column tower;
Wherein, described overhead line is connected with one or more pipeline, described one or more pipeline is connected with the described overhead line before described return tank after heating equipment.
6. method according to claim 5, is characterized in that, described second interchanger and described 3rd interchanger pass into coolant media respectively.
7. method according to claim 5, is characterized in that, the tower top pressure of described weight-removing column is 0.05 ~ 15.0MPaG, and tower top temperature is 150 ~ 280 DEG C.
8. method according to claim 5, is characterized in that, further comprising the steps of:
Described weight-removing column is delivered to as thermal source after the heating equipment between at the bottom of the tower of the export pipeline and described weight-removing column of a part of heavy constituent through being connected to described second discharging pump heats.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210107363.6A CN102660315B (en) | 2012-04-12 | 2012-04-12 | Device for controlling endpoint of gasoline blending component extracted from tower sideline vapor phase and method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210107363.6A CN102660315B (en) | 2012-04-12 | 2012-04-12 | Device for controlling endpoint of gasoline blending component extracted from tower sideline vapor phase and method thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102660315A CN102660315A (en) | 2012-09-12 |
| CN102660315B true CN102660315B (en) | 2015-04-01 |
Family
ID=46769899
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210107363.6A Active CN102660315B (en) | 2012-04-12 | 2012-04-12 | Device for controlling endpoint of gasoline blending component extracted from tower sideline vapor phase and method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102660315B (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101717657A (en) * | 2009-11-24 | 2010-06-02 | 江苏工业学院 | Device and method for separating light-colored C9 fraction of cracking |
| CN102041030A (en) * | 2011-01-13 | 2011-05-04 | 中国石油天然气华东勘察设计研究院 | Method for controlling and reforming ultrahigh final boiling point of high-octane gasoline blending component |
| WO2012012153A2 (en) * | 2010-06-30 | 2012-01-26 | Uop Llc | Improved heat pump distillation for <50% light component in feed |
| CN202671500U (en) * | 2012-04-12 | 2013-01-16 | 中国寰球工程公司 | Device for controlling gasoline blending component dry point through tower side line vapor phase extraction |
-
2012
- 2012-04-12 CN CN201210107363.6A patent/CN102660315B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101717657A (en) * | 2009-11-24 | 2010-06-02 | 江苏工业学院 | Device and method for separating light-colored C9 fraction of cracking |
| WO2012012153A2 (en) * | 2010-06-30 | 2012-01-26 | Uop Llc | Improved heat pump distillation for <50% light component in feed |
| CN102041030A (en) * | 2011-01-13 | 2011-05-04 | 中国石油天然气华东勘察设计研究院 | Method for controlling and reforming ultrahigh final boiling point of high-octane gasoline blending component |
| CN202671500U (en) * | 2012-04-12 | 2013-01-16 | 中国寰球工程公司 | Device for controlling gasoline blending component dry point through tower side line vapor phase extraction |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102660315A (en) | 2012-09-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US9568256B2 (en) | Energy-efficient and environmentally advanced configurations for naphtha hydrotreating process | |
| CN102351627A (en) | Process method for extracting normal hexane and isohexane from crude hexane | |
| CN102234541B (en) | Energy-saving pyrolysis gasoline full-cut hydrogenation method and device | |
| CN105647575A (en) | Natural gasoline upgrading and utilizing technology | |
| CN207347520U (en) | A kind of system of diesel hydrotreating unit naphtha direct-furnish reformer | |
| CN112410068A (en) | Wax oil hydrocracking device and method for producing 5# industrial white oil by using same | |
| CN101081993B (en) | Method for recovering aromatic hydrocarbons from hydrocarbons mixture with high content of aromatic hydrocarbons | |
| CN105670689A (en) | Kerosene-hydrogenation production process and system | |
| CN214088414U (en) | Wax oil hydrocracking unit | |
| CN202671500U (en) | Device for controlling gasoline blending component dry point through tower side line vapor phase extraction | |
| CN101091835B (en) | Extractive distillation method with heat exchange through parallel connection | |
| CN105062559A (en) | Novel process for reducing energy consumption of catalytic gasoline hydrogenation refining process | |
| CN102660315B (en) | Device for controlling endpoint of gasoline blending component extracted from tower sideline vapor phase and method thereof | |
| CN202246472U (en) | Device for extracting normal hexane and isohexane from crude hexane | |
| CN201686667U (en) | Cracking gasoline full-fraction hydrogenation device | |
| CN106016794B (en) | A kind of aromatic device waste heat recycling system and method | |
| CN105377393A (en) | Process for heating the column for distillation of the C3 fraction from an FCC unit by means of a circuit of water heated by streams belonging to units placed upstream and/or downstream of the fcc unit | |
| CN102041030B (en) | Method for controlling ultrahigh final boiling point of blending component of reformed high-octane gasoline | |
| CN111534327B (en) | Reforming pretreatment system, reforming pretreatment method and application | |
| CN105087065B (en) | Pyrolysis gasoline central fraction hydrogenation device and method thereof | |
| CN210560267U (en) | Device for recycling heat at top of reforming oil fractionating tower | |
| CN210595940U (en) | Heat conduction oil processing device | |
| CN106147826B (en) | A kind of bifilar feed process of tower of pyrolysis gasoline hydrogenation device decarburization five | |
| CN210065672U (en) | Wax oil hydrocracking system | |
| CN209161967U (en) | Alkylate oil fractionating device and Aviation Fuel production system comprising the device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP03 | Change of name, title or address |
Address after: Two road 100012 Beijing city Chaoyang District high tech Industrial Park, No. 1. Patentee after: China Global Engineering Co. Ltd. Address before: 100029 Beijing city Chaoyang District cherry Garden Street No. 7 Patentee before: China Huanqiu Engineering Co. |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20201120 Address after: 100120 Beijing Xicheng District six laying Kang Patentee after: CHINA NATIONAL PETROLEUM Corp. Patentee after: CHINA HUANQIU CONTRACTING & ENGINEERING Co.,Ltd. Address before: Two road 100012 Beijing city Chaoyang District high tech Industrial Park, No. 1. Patentee before: CHINA HUANQIU CONTRACTING & ENGINEERING Co.,Ltd. |
|
| TR01 | Transfer of patent right |