CN103183577B - Heat exchange system and heat exchange method for carbon five extractive distillation - Google Patents
Heat exchange system and heat exchange method for carbon five extractive distillation Download PDFInfo
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Abstract
The invention discloses a heat exchange system and a heat exchange method for carbon five extractive distillation. The system comprises a first extraction tower divided into upper and lower sections, wherein the lower section of the first extraction tower is provided a lower section reboiler A; a de-heavy fractionator divided into upper and lower sections, wherein the upper section of the de-heavy fractionator is provided with an upper section reboiler A; and a second extraction tower into divided upper and lower sections provided with an upper section reboiler B and a lower section reboiler B respectively. The heat exchange method comprises the steps that materials at the bottom of a first stripping tower are exchanged heat through the lower section reboiler A and the upper section reboiler A of the de-heavy fractionator and sent to the upper section of the first extraction tower; materials at the bottom of a second stripping tower are exchanged heat through the lower section reboiler B and sent to the upper section of a third stripping tower; and materials at the bottom of the third stripping tower are exchanged heat through the upper section reboiler B, cooled and sent to a solvent feeding port at the upper section of the second extraction tower. The heat exchange system and the heat exchange method realize gradient recovery and utilization of energy, and have the advantages of low investment, low energy consumption, simple process route and the like in industrial applications.
Description
Technical field
The present invention relates to chemical field, say further, relate to a kind of heat-exchange system and heat-exchange method of carbon five extracting rectifying.
Background technology
The C5 fraction of the quite a lot of quantity of by-product in petroleum cracking process of producing ethylene, the dienes such as isoprene, m-pentadiene and cyclopentadiene are rich in C5 fraction.These diolefin chemical property are active, are important industrial chemicals.Due to the difference on the raw material of petroleum hydrocarbon cracking, cracking severity and separation degree, the diolefin content in C5 fraction is different, but total amount is in the middle of 40 ~ 60%.Therefore, extraction and application C5 fraction for improve ethylene unit economic benefit, comprehensive utilization petroleum resources there is profound significance.
Cracked C 5 fraction is close by more than 20 kinds of boiling points, and easily form the component composition of azeotrope to each other, the diolefin difficulty therefrom isolating purity load application requiring is higher, and technique is comparatively complicated, generally adopts extraction fractional distillation in prior art.Conventional selective solvent has dimethyl formamide (DMF) and acetonitrile, the processing method as patent JP63101338, JP74019245, US3510405, US3535260 etc. Suo Gongkai.Because the boiling point of extraction agent is far away higher than carbon five hydrocarbon, its heat enthalpy value is higher, if can, by its Appropriate application, carbon five plant energy consumption will be made to reduce further.Traditional process adopts a set of hot-water system to carry out solvent heat exchange, but temperature influence heat transfer effect is limited, and the hot water of the steam condensate by-product of this device by-product is excessive simultaneously, and therefore, carbon five plant energy consumption of traditional process is higher, directly affects the economic benefit of device.
Summary of the invention
For solving the problem in prior art in energy recovery and UTILIZATION OF VESIDUAL HEAT IN, the invention provides a kind of heat-exchange system and heat-exchange method of carbon five extracting rectifying, the step achieving energy reclaims and utilizes, and has the advantages such as reduced investment, energy consumption is low, operational path is simple and direct in industrial application.
An object of the present invention is to provide a kind of heat-exchange system of carbon five extracting rectifying.
Comprise: the first extraction tower, the first stripping tower, weight-removing column, the second extraction tower, the second stripping tower and the 3rd stripping tower, each tower tower reactor is provided with reboiler, first extraction tower, the second extraction tower and weight-removing column are divided into two sections respectively, first extraction tower hypomere arranges hypomere reboiler A, described hypomere reboiler A is arranged on optional position between hypomere tower reactor the 1 to 10 block of plate reciprocal usually, first extraction tower epimere is provided with solvent feed mouth, and the first extraction tower hypomere is provided with carbon five opening for feed;
Weight-removing column is divided into two sections, and weight-removing column epimere arranges epimere reboiler A, and described epimere reboiler A is arranged on optional position between epimere tower reactor the 1 to 10 block of plate reciprocal;
After described first stripping tower tower reactor outlet connects the first extraction tower hypomere reboiler A, weight-removing column epimere reboiler A successively, connect the first extraction tower epimere solvent feed mouth; Also can first stripping tower tower reactor outlet connect successively the first extraction tower hypomere reboiler A, weight-removing column epimere reboiler A and one extraction solvent cooler A after, connect the first extraction tower epimere solvent feed mouth;
Described second extraction tower epimere and hypomere arrange epimere reboiler B and hypomere reboiler B respectively, and described epimere reboiler B is arranged on optional position between epimere tower reactor the 1 to 10 block of plate reciprocal; Described hypomere reboiler B is arranged on optional position between hypomere tower reactor the 1 to 10 block of plate reciprocal;
Second extraction tower epimere is provided with solvent feed mouth; Second extraction tower hypomere is provided with weight-removing column top material feeding mouth;
After described second stripping tower tower reactor outlet connection second extraction tower hypomere reboiler B, connect the 3rd stripping tower;
3rd stripping tower tower reactor outlet connects the second extraction tower epimere solvent feed mouth after connecting the second extraction tower epimere reboiler B, two extraction solvent cooler B successively.
Above-described first extraction tower, the second extraction tower and weight-removing column are divided into two sections and divide with stage number, and there is no particular limitation, preferably stage number can be divided into two sections.
Two of object of the present invention is to provide a kind of heat-exchange method of carbon five extracting rectifying.
Comprise:
First stripping tower kettle material, after the hypomere reboiler A of the first extraction tower and the epimere reboiler A heat exchange of weight-removing column, after cooling or without cooling, sends into the first extraction tower epimere as solvent;
Second stripping tower kettle material, after the second extraction tower hypomere reboiler B heat exchange, sends into the 3rd stripping tower top;
3rd stripping tower kettle material, after the second extraction tower epimere reboiler B heat exchange, through cooling, sends into the second extraction tower epimere solvent feed mouth.
Wherein, the first extraction tower and the second extraction tower can adopt setting of the prior art and processing condition, can be preferred in the present invention:
The total stage number of described first extraction tower is 100 ~ 200, and working pressure is 0.03 ~ 0.2MPaG, and tower top temperature is 35 ~ 60 DEG C, bottom temperature 100 ~ 140 DEG C, and reflux ratio is 1 ~ 5, and solvent ratio is 1 ~ 10;
The total stage number of described second extraction tower is 100 ~ 200, and working pressure is 0.03 ~ 0.2MPaG, and tower top temperature is 35 ~ 60 DEG C, bottom temperature 100 ~ 140 DEG C, and reflux ratio is 1 ~ 5, and solvent ratio is 1 ~ 10.
Described first extraction tower and the second extraction tower column internals adopt sieve plate, float valve or their composite type.
Setting and the processing condition of the first stripping tower in the present invention, weight-removing column, the second stripping tower, the 3rd stripping tower can adopt setting of the prior art and processing condition.
The present invention can be achieved through the following technical solutions:
First extraction tower is divided into two sections, and the top of epimere 1A arranges the opening for feed of extraction solvent, and hypomere 1B top arranges carbon five feeding line, and hypomere tower bottom arranges hypomere reboiler A, and hypomere tower reactor extraction pipeline is connected with the first stripping tower feeding line; First stripper overhead stream divides two strands after condensation, one sends into the first extraction tower tower reactor reboiler entrance, another stock sends into weight-removing column hypomere, first stripping tower tower reactor extraction lean solvent is after the hypomere reboiler A heat exchange of the first extraction tower, then through the epimere reboiler A heat exchange of weight-removing column, be more directly connected with the first extraction tower epimere 1A as the solvent feed of the first extraction tower after water cooler A cools or without cooling; After cooling, send into the second extraction tower hypomere 4A top by the logistics of weight-removing column epimere 3A overhead extraction, tower reactor extraction logistics then sends into m-pentadiene, dicyclopentadiene processing unit; Second extraction tower is divided into two sections, the top of epimere 4A arranges lean solvent feeding line, second extraction tower epimere 4A tower reactor arranges epimere reboiler B, hypomere 4B top arranges carbon five feeding line, hypomere 4B bottom arranges hypomere reboiler B, and hypomere tower reactor extraction pipeline is connected with the second stripping tower feeding line; Second stripper overhead stream after condensation points two strands, one sends into the second extraction tower tower reactor reboiler entrance, another burst of extraction, the second stripping tower reactor extraction lean solvent after the hypomere reboiler B heat exchange of the second extraction tower as the 3rd stripping tower charging; 3rd stripping tower tower reactor extraction lean solvent is after the second extraction tower epimere reboiler B heat exchange, and the solvent feed as the second extraction tower after water cooler B cools is connected with the second extraction tower epimere 4A.
Heat-exchange method of the present invention is: using the lean solvent of the first stripping tower reactor extraction successively as the thermal source that the hypomere reboiler A of the first extraction tower, weight-removing column are the first extraction tower epimere reboiler A, after water cooler A lowers the temperature, send into the first extraction tower again after heat exchange to recycle as solvent feed, or directly send into the first extraction tower without water cooler and recycle as solvent feed, depending on circulating solvent temperature out after the heat exchange of weight-removing column epimere tower reactor reboiler;
The 3rd stripping tower charging is sent into as after the hypomere reboiler B thermal source heat exchange of the second extraction tower by the lean solvent of the second stripping tower reactor extraction; The lean solvent of the 3rd stripping tower reactor extraction recycles as solvent feed as sending into the second extraction tower after the epimere reboiler B thermal source heat exchange of the second extraction tower after water cooler B lowers the temperature.
Particularly,
Carbon five material sent here by pretreatment unit enters the first extraction tower lower section upper portion, this tower is divided into upper-lower section, total stage number 100 ~ 200, working pressure is 0.03 ~ 0.2MPaG, tower top temperature 35 ~ 60 DEG C, reflux ratio 1 ~ 5, solvent ratio 1 ~ 10, column internals adopts sieve plate, float valve or their composite type; First extraction tower top steams C 5 alkane, monoolefine, tower reactor extraction C 5 diene, alkynes and solvent; First extraction tower hypomere (1B) arranges hypomere reboiler A from tower reactor the 1 to 10 piece of plate optional position reciprocal, and heating medium is the lean solvent of the first stripping tower reactor extraction; First extraction tower reactor production material is sent into the first stripping tower and is separated, after hydrocarbon and separated from solvent, the solvent of the first stripping tower reactor is cooled to through water cooler A and sends into the first extraction tower after assigned temperature and recycle as solvent feed after the hypomere reboiler A of the first extraction tower and the epimere reboiler A of weight-removing column reclaims heat, or directly send into the first extraction tower without water cooler A and recycle as solvent feed, depending on circulating solvent temperature out after the heat exchange of weight-removing column epimere tower reactor reboiler.
Carbon five material sent here by weight-removing column top enters the second extraction tower lower section upper portion, this tower is divided into upper-lower section, total stage number 100 ~ 200, working pressure is 0.03 ~ 0.2MPaG, tower top temperature 35 ~ 60 DEG C, reflux ratio 1 ~ 5, solvent ratio 1 ~ 10, column internals can adopt sieve plate, float valve or their composite type; Second extraction tower top steams the isoprene of more than 99%, sends to lightness-removing column and processes further, tower reactor extraction C 5 diene, alkynes and solvent; Second extraction tower hypomere 4B arranges hypomere reboiler B from tower reactor the 1 to 10 piece of plate optional position reciprocal, and heating medium is the lean solvent of the second stripping tower reactor extraction; Second extraction tower epimere 4A tower reactor arranges epimere reboiler B, and heating medium is the lean solvent of the 3rd stripping tower reactor extraction; Second extraction tower reactor production material is sent into the second stripping tower and is carried out solvent recuperation, after removing alkynes, sends into the 3rd stripping tower charging by the lean solvent of the second stripping tower reactor extraction as after the hypomere reboiler B thermal source heat exchange of the second extraction tower; The lean solvent of the 3rd stripping tower reactor extraction recycles as solvent feed as sending into the second extraction tower after the epimere reboiler B thermal source heat exchange of the second extraction tower after water cooler B lowers the temperature.
Solvent in abstraction distillation system used for the present invention is selected from least one in dimethyl formamide, N,N-DIMETHYLACETAMIDE, the N-Methyl pyrrolidone aqueous solution and acetonitrile solution.
The present invention has the following advantages: 1. hot solvent achieves cascaded utilization of energy, saves steam consumption 5 ~ 10%; 2. due to the energy supplement of intermediate reboiler, reduce the phase load of tower especially hypomere, gas phase load reduces 10 ~ 30%, and liquid phase load reduces 1 ~ 10%, for the tower of taking as the leading factor with gas phase load, reduces tower diameter accordingly, saves investment.
Accompanying drawing explanation
Fig. 1 embodiments of the invention heat-exchange system schematic flow sheet
Fig. 2 comparative example heat-exchange system schematic flow sheet
Description of reference numerals:
1-first extraction tower (A-epimere, B-hypomere), 2-first stripping tower, 3-weight-removing column (A-epimere, B-hypomere), 4-second extraction tower (A-epimere, B-hypomere), 5-second stripping tower, 6-the 3rd stripping tower, 7-first extraction tower tower reactor reboiler, 8-first extraction tower hypomere reboiler A, 9-first extraction tower epimere reboiler A, 10-mono-extracts solvent cooler A, 11-first stripper reboiler, 12-first stripper condenser, 13-weight-removing column reboiler, 14-weight-removing column condenser, 15-second extraction tower tower reactor reboiler, 16-second extraction tower hypomere reboiler B, 17-second extraction tower epimere reboiler B, 18-bis-extracts solvent cooler B, 19-second stripper reboiler, 20-second stripper condenser, 21-the 3rd stripper reboiler, 22-hot water heat exchanger
Embodiment
Below in conjunction with embodiment, further illustrate the present invention.
Embodiment:
As shown in Figure 1, a kind of heat-exchange system of carbon five extracting rectifying.
Comprise: the first extraction tower 1, first stripping tower 2, weight-removing column 3, second extraction tower 4, second stripping tower 5 and the 3rd stripping tower 6, each tower tower reactor is provided with reboiler,
Described first extraction tower 1 is divided into two sections, and the first extraction tower hypomere arranges hypomere reboiler A8, and described hypomere reboiler A8 is arranged on from hypomere tower reactor the 2nd piece of Board position reciprocal; First extraction tower 1 epimere is provided with solvent feed mouth, and the first extraction tower 1 hypomere is provided with carbon five material inlet;
Weight-removing column 3 is divided into two sections, and weight-removing column epimere arranges epimere reboiler A9, and described epimere reboiler A9 is arranged on from epimere tower reactor the 1st piece of Board position reciprocal;
After first stripping tower 2 tower reactor outlet connects hypomere reboiler A8, epimere reboiler A9 and water cooler A10 successively, connect the first extraction tower 1 epimere solvent feed mouth;
Described second extraction tower 4 is divided into two sections, arranges epimere reboiler B17 and hypomere reboiler B16 respectively; Described hypomere reboiler B16 is arranged on from hypomere tower reactor the 2nd piece of Board position reciprocal, and described epimere reboiler B17 is arranged on from epimere tower reactor the 1st piece of Board position reciprocal.
Second extraction tower 4 epimere is provided with solvent feed mouth; Second extraction tower 4 hypomere is provided with weight-removing column top material feeding mouth;
After described second stripping tower 5 tower reactor outlet connects hypomere reboiler B16, connect the 3rd stripping tower 6;
After 3rd stripping tower 6 tower reactor outlet connects epimere reboiler B17, water cooler B18 successively, connect the second extraction tower 4 epimere solvent feed mouth.
When carrying out heat exchange,
First stripping tower kettle material, after the hypomere reboiler A of the first extraction tower and the epimere reboiler A heat exchange of weight-removing column, after cooling, sends into the first extraction tower epimere as solvent;
Second stripping tower kettle material, after the second extraction tower hypomere reboiler B heat exchange, sends into the 3rd stripping tower top;
3rd stripping tower kettle material, after the second extraction tower tower epimere reboiler B heat exchange, through cooling, sends into the second extraction tower epimere solvent feed mouth as solvent.
Wherein, the total stage number of described first extraction tower is 149, wherein epimere 77 blocks of plates, hypomere 72 blocks of plates, epimere tower top working pressure is 0.042MPaG, epimere tower top temperature is 45 DEG C, and reflux ratio is 3.5, and hypomere tower top working pressure is 0.082MPaG, hypomere tower top temperature 72 DEG C, hypomere bottom temperature 110 DEG C, solvent ratio be 5 (solvent ratio is defined as the ratio of solvent feed amount and extraction tower carbon five inlet amount, lower with);
The total stage number of described second extraction tower is 186, wherein epimere 94 pieces, hypomere 92 pieces, epimere tower top working pressure is 0.032MPaG, and epimere tower top temperature is 42 DEG C, and reflux ratio is 2, hypomere tower top working pressure is 0.082MPaG, hypomere tower top temperature 72 DEG C, hypomere bottom temperature 120 DEG C, solvent ratio is 5;
Described first extraction tower and the second extraction tower column internals adopt valve tray.
Comparative example:
As shown in Figure 2, a kind of heat-exchange system of carbon five extracting rectifying.
Comprise: the first extraction tower 1, first stripping tower 2, weight-removing column 3, second extraction tower 4, second stripping tower 5 and the 3rd stripping tower 6, each tower tower reactor is provided with reboiler,
Described first extraction tower 1 is divided into two sections, and the first extraction tower hypomere arranges hypomere reboiler A8, and described hypomere reboiler A8 is arranged on from tower reactor the 2nd piece of Board position reciprocal; First extraction tower 1 epimere is provided with solvent feed mouth, and the first extraction tower 1 hypomere is provided with material inlet;
First stripping tower 2 tower reactor outlet connects the first extraction tower 1 epimere solvent feed mouth after connecting hypomere reboiler A8, an extraction solvent cooler A10 successively;
Described weight-removing column 3 is divided into two sections, and tower reactor only has a reboiler 13;
Described second extraction tower 4 is divided into two sections, wherein only has hypomere tower reactor to have a reboiler 15;
Second extraction tower 4 epimere is provided with solvent feed mouth; Second extraction tower 4 hypomere is provided with weight-removing column top material feeding mouth;
After described second stripping tower 5 tower reactor outlet connects hot water heat exchanger 22, connect the 3rd stripping tower 6;
After 3rd stripping tower 6 tower reactor outlet connection two extracts solvent cooler 18, connect the second extraction tower 4 epimere solvent feed mouth.
When carrying out heat exchange,
First stripping tower kettle material, after the hypomere reboiler A8 heat exchange of the first extraction tower, after an extraction solvent cooler 10 cools, sends into the first extraction tower epimere as solvent;
Second stripping tower kettle material, after hot water heat exchanger 16 heat exchange, sends into the 3rd stripping tower top;
3rd stripping tower kettle material, after cooling through two extraction solvent cooler 18, sends into the second extraction tower epimere solvent feed mouth.
Wherein, the total stage number of described first extraction tower is 149, wherein epimere 77 blocks of plates, hypomere 72 blocks of plates, epimere tower top working pressure is 0.042MPaG, epimere tower top temperature is 45 DEG C, and reflux ratio is 3.5, and hypomere tower top working pressure is 0.082MPaG, hypomere tower top temperature 72 DEG C, hypomere bottom temperature 110 DEG C, solvent ratio be 5 (solvent ratio is defined as the ratio of solvent feed amount and extraction tower carbon five inlet amount, lower with);
The total stage number of described second extraction tower is 186, wherein epimere 94 pieces, hypomere 92 pieces, upper end tower top working pressure is 0.032MPaG, and epimere tower top temperature is 42 DEG C, and reflux ratio is 2, hypomere tower top working pressure is 0.082MPaG, hypomere tower top temperature 72 DEG C, hypomere bottom temperature 120 DEG C, solvent ratio is 5;
Described first extraction tower and the second extraction tower column internals adopt valve tray.
Table 1 is the energy consumption comparison of embodiment and comparative example.
Table 1
| Project | Comparative example | Embodiment | Deviation, % |
| Low-pressure steam consumption, t/hr | 47.67 | 43.84 | -8 |
| Middle pressure steam consumption, t/hr | 9.77 | 9.77 | 0 |
| Consumption of cooling-water, t/hr | 4449 | 4433 | -16 |
Data as can be seen from table 1, adopt heat-exchange system of the present invention and heat-exchange method can obviously reduce steam consumption and cooling water consumption, thus, of the present invention remarkably productive, obviously can reduce energy consumption.
Claims (4)
1. the heat-exchange system of carbon five extracting rectifying, comprise: the first extraction tower, the first stripping tower, weight-removing column, the second extraction tower, the second stripping tower and the 3rd stripping tower, each tower tower reactor is provided with reboiler, first extraction tower, the second extraction tower and weight-removing column are divided into two sections respectively, first extraction tower hypomere arranges hypomere reboiler A, first extraction tower epimere is provided with solvent feed mouth, and the first extraction tower hypomere is provided with carbon five opening for feed; It is characterized in that:
Described weight-removing column epimere arranges epimere reboiler A, and described epimere reboiler A is arranged on optional position between epimere tower reactor the 1 to 10 block of plate reciprocal;
Described first stripping tower tower reactor outlet connects the first extraction tower epimere solvent feed mouth after connecting the first extraction tower hypomere reboiler A, weight-removing column epimere reboiler A and an extraction solvent cooler A successively;
Described second extraction tower epimere and hypomere arrange epimere reboiler B and hypomere reboiler B respectively; Described epimere reboiler B is arranged on optional position between epimere tower reactor the 1 to 10 block of plate reciprocal; Hypomere reboiler B is arranged on optional position between hypomere tower reactor the 1 to 10 block of plate reciprocal;
Second extraction tower epimere is provided with solvent feed mouth; Second extraction tower hypomere is provided with weight-removing column top material feeding mouth;
After described second stripping tower tower reactor outlet connection second extraction tower hypomere reboiler B, connect the 3rd stripping tower;
3rd stripping tower tower reactor outlet connects the second extraction tower epimere solvent feed mouth after connecting the second extraction tower epimere reboiler B, two extraction solvent cooler B successively.
2. adopt a heat-exchange method for the heat-exchange system of carbon five extracting rectifying as claimed in claim 1, comprising:
First stripping tower kettle material after the hypomere reboiler A of the first extraction tower and the epimere reboiler A heat exchange of weight-removing column, then sends into the first extraction tower epimere as solvent after cooling;
Second stripping tower kettle material, after the second extraction tower hypomere reboiler B heat exchange, sends into the 3rd stripping tower top;
3rd stripping tower kettle material, after the second extraction tower tower epimere reboiler B heat exchange, through cooling, sends into the second extraction tower epimere solvent feed mouth.
3. heat-exchange method as claimed in claim 2, is characterized in that:
The total stage number of described first extraction tower is 100 ~ 200, and working pressure is 0.03 ~ 0.2MPaG, and tower top temperature is 35 ~ 60 DEG C, bottom temperature 100 ~ 140 DEG C, and reflux ratio is 1 ~ 5, and solvent ratio is 1 ~ 10.
4. heat-exchange method as claimed in claim 3, is characterized in that:
The total stage number of described second extraction tower is 100 ~ 200, and working pressure is 0.03 ~ 0.2MPaG, and tower top temperature is 35 ~ 60 DEG C, bottom temperature 100 ~ 140 DEG C, and reflux ratio is 1 ~ 5, and solvent ratio is 1 ~ 10.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101244974A (en) * | 2007-02-15 | 2008-08-20 | 中国石油化工股份有限公司 | Method for one-section abstraction distillation separation cracking carbon 5-cut fraction |
| CN101450885A (en) * | 2007-12-07 | 2009-06-10 | 中国石油化工股份有限公司 | Method for separating carbon 5 fraction by one-stage extraction and rectification |
| CN101723788A (en) * | 2008-10-10 | 2010-06-09 | 中国石油化工股份有限公司 | Separation method of cracking C5 fractions |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101244974A (en) * | 2007-02-15 | 2008-08-20 | 中国石油化工股份有限公司 | Method for one-section abstraction distillation separation cracking carbon 5-cut fraction |
| CN101450885A (en) * | 2007-12-07 | 2009-06-10 | 中国石油化工股份有限公司 | Method for separating carbon 5 fraction by one-stage extraction and rectification |
| CN101723788A (en) * | 2008-10-10 | 2010-06-09 | 中国石油化工股份有限公司 | Separation method of cracking C5 fractions |
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Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: China Petrochemical Group Co., Ltd Patentee after: Sinopec Engineering Construction Co., Ltd Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: China Petrochemical Corp Patentee before: Sinopec Engineering Construction Co., Ltd |