CN101424453B - High temperature heat integration system for oil-extraction plant and use thereof - Google Patents
High temperature heat integration system for oil-extraction plant and use thereof Download PDFInfo
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- CN101424453B CN101424453B CN2008102041299A CN200810204129A CN101424453B CN 101424453 B CN101424453 B CN 101424453B CN 2008102041299 A CN2008102041299 A CN 2008102041299A CN 200810204129 A CN200810204129 A CN 200810204129A CN 101424453 B CN101424453 B CN 101424453B
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Abstract
The invention relates to a heat exchange system for high temperature heat of a plant, in particular to an oil refining plant high-temperature heat integration system designed for using high-temperature mass flow heat. The system is characterized in that three independent heat source devices are connected through thermal medium pipes and heat-conducting oil in the thermal medium pipes are used as a heat-transfer medium to form heat integration, so as to collect and use high-temperature heat. Compared with the prior art, the system optimizes a heat exchange network, saves fuel gases and steam in a reboiler at the tower bottom, reduces energy consumption of equipment, lowers oil refining cost and improves economic benefits.
Description
[technical field]
The present invention relates to the heat-exchange system of factory's elevated temperature heat, specifically a kind of a kind of high temperature heat integration system for oil-extraction plant that utilizes high potential temperature logistics heat and design.
[technical background]
At present, the utilization of the elevated temperature heat of known factory is to be utilized as characteristics in each device, as steam etc. takes place, do not consider the comprehensive utilization of heat between each cell arrangement, have that the heat exchange between the logistics has the situation of the low usefulness of high temperature to exist in the cell arrangement of elevated temperature heat, on the other hand, the hot trap logistics of other cell arrangement needs heat temperature raising, some logistics will or utilize the temperature of middle pressure steam heating with the hot trap logistics that raises by the heating furnace consume fuel, in full factory scope, the be unrealized multistage utilization of high potential temperature heat, cause energy dissipation, do not conform to the energy principle with " temperature counterpart, cascade utilization " science, cause fuel and steam consumption bigger, the plant energy consumption height, consumption of natural resource is many.Existing apparatus and workflow are as follows:
Heat power supply device 11: described heat power supply device 11, as catalytic cracking unit, the logistics of about 350-300 ℃ the heat power supply device 11 that the fractionating column 6 in the catalytic cracking unit comes out is through first heat transmission equipment 3 and other device that comes from heat power supply device 11 outsides, as atmospheric and vacuum distillation unit, other rig stream about the 80-150 that devices such as hydrotreatment come out ℃ carries out heat exchange, other device logistics is arrived temperature T a=170-230 ℃ by heat exchange, after the logistics of heat power supply device 11 is arrived temperature T b=350-280 ℃ by heat exchange, the logistics of heat power supply device 11 divides two-way through the tube side of second heat transmission equipment 5 and about 240 ℃ middle pressure steam heat exchange in second heat transmission equipment, 5 shell sides after temperature T c=270-250 ℃, one the tunnel returns fractionating column 6, and one the tunnel is cooled to go out device about 90 ℃ through the 3rd heat transmission equipment 7.Wherein, 240 ℃ of left and right sides middle pressure steams are to be produced by 104-200 ℃ deaerated water in second heat transmission equipment, 5 shell sides, and the logistics of the heat power supply device 11 of about 350-300 ℃ the high temperature that comes out in fractionating column 6 bottoms is big with the heat transfer temperature difference of the deaerated water that produces these 240 ℃ of left and right sides middle pressure steams, high potential temperature heat does not obtain scientific and rational cascade utilization, reduced the quality that energy utilizes, not energy-conservation.
Heat power supply device 22: described heat power supply device 22, as reformer or methyl ethyl ketone plant or special solvent oil device, another fractionating column 10 is returned in about 200-260 ℃ the hot trap logistics of coming out in these devices after heating furnace 9 is heated to temperature T 1r=200-280 ℃, because about the 200-260 ℃ hot trap logistics of extracting out from another 10 ends of fractionating column need be heated to required temperature T 1r through heating furnace, the tower that returns that just can return another fractionating column 10 then enters the mouth, yet this temperature T 1r temperature a little more than about 200-260 ℃ the hot trap logistics of extracting out from another 10 ends of fractionating column, so heat with heating furnace specially, increased energy consumption, not science.
Heat power supply device 33: described heat power supply device 33, as aromatic extraction unit or methyl ethyl ketone plant, about 150-200 ℃ the logistics that extract out another fractionating column 14 bottoms from these devices is returned another fractionating column 14 through the 4th heat transmission equipment 13 and about 250-400 ℃ the pipe network middle pressure steam heat exchange that factory's internal steam pipe net comes out again to temperature T 2r=150-300 ℃.Because about 150-200 ℃ the logistics of extracting out from 14 ends of another fractionating column is heated to required 150-300 ℃ temperature T 2r, and then return another fractionating column 14, it is lower that the tower temperature is returned in this T2r=150-300 ℃ logistics, middle pressure steam heated stream with about 250-400 ℃, heat transfer temperature difference is big, the heat of steam is underused, and has reduced the quality that energy utilizes, and is not energy-conservation.
The utilization of above-mentioned each cell arrangement energy does not have taking all factors into consideration of system, does not optimize coupling in full factory scope, and the mode of utilizing of the heat of high potential temperature logistics is that steam takes place; The steam that produces enters steam pipe system, is delivered to the thermal source of other device as other device; This way power conversion link is more, and the conveying of steam is also lossy, and final result is exactly that the utilization ratio of heat of high potential temperature logistics is low, high-quality low usefulness, and waste is serious, has also increased the consumption of the high-quality fuel of heating furnace.
[summary of the invention]
The objective of the invention is according to the science of " temperature counterpart, cascade utilization " energy principle, in full factory scope, to fully utilize elevated temperature heat, set up the big system of elevated temperature heat, optimize heat-exchange network, energy savings in order to overcome the deficiencies in the prior art.
For achieving the above object, a kind of high temperature heat integration system for oil-extraction plant is provided, comprise three heat power supply devices, heat power supply device 11 is mainly extracted the tube side that mouth connects first heat transmission equipment 3 and second heat transmission equipment 5 successively out by fractionating column 6 bottoms, the tube side outlet of second heat transmission equipment 5 divides two-way again, one the tunnel returns the bottom reflux inlet that connects fractionating column 6, and another road connects the tube side import of the 3rd heat transmission equipment 7 and forms; Another heat power supply device 22 is mainly extracted mouthful connection heating furnace 9 imports out by another fractionating column 10 bottoms, and heating furnace 9 outlets connect the tower inlet that returns of another fractionating column 10 again and form; Another heat power supply device 33 is established two-way for mainly extracting mouth out by another fractionating column 14 bottoms, one the tunnel for going out device, another road connects the shell side import of the 4th heat transmission equipment 13, the shell side outlet of the 4th heat transmission equipment 13 is returned the tower inlet that returns that connects another fractionating column 14 again and is formed, it is characterized in that with three independently heat power supply device adopt the thermal medium pipe to connect and be that the mode that heat catalysis forms heat integration is carried out the collection utilization of heat of high temperature with the conduction oil in the thermal medium pipe, its concrete syndeton is:
Set up the 5th heat transmission equipment 16 between the fractionating column 6 in heat power supply device 11 and first heat transmission equipment 3, fractionating column 6 bottoms are extracted a mouthful tube side import that connects the 5th heat transmission equipment 16 out, and the tube side outlet of the 5th heat transmission equipment 16 connects the tube side import of first heat transmission equipment 3;
Adopt the 6th heat transmission equipment 17 shell sides to connect in another heat power supply device 22 and replace former heating furnace 9 connections, be that another fractionating column 10 bottoms are extracted mouthful connection the 6th heat transmission equipment 17 shell side imports out, the outlet of the 6th heat transmission equipment 17 shell sides connects the tower inlet that returns of another fractionating column 10 again and forms;
The shell side import of the 5th heat transmission equipment 16 in the heat power supply device 11 adopts the thermal medium pipe to connect the tube side outlet of the 4th heat transmission equipment 13 in the another heat power supply device 33, the shell side outlet of the 5th heat transmission equipment 16 connects the tube side import of the 6th heat transmission equipment 17 in another heat power supply device 22, and the tube side outlet of the 6th heat transmission equipment 17 connects the tube side import of the 4th heat transmission equipment 13 in the another heat power supply device 33 again;
Its heat exchange process is: 200-250 ℃ conduction oil enters the shell side of the 5th newly-increased in the heat power supply device 11 heat transmission equipment 16 by the thermal medium pipe, with a logistics heat exchange of extracting the heat power supply device 11 that mouth comes out in the tube side of the 5th heat transmission equipment 16 by fractionating column 6 bottoms out, the temperature of heat power supply device 11 logistics is Td after the heat exchange, the tube side that first heat transmission equipment 3 is advanced in heat power supply device 11 logistics again carries out heat exchange with the logistics of advancing first heat transmission equipment, 3 shell sides, the logistics of advancing first heat transmission equipment, 3 shell sides is arrived Ta by heat exchange, the logistics of heat power supply device 11 is arrived Tb ' by heat exchange, the logistics of heat power supply device 11 tube side that advances second heat transmission equipment 5 again and the logistics heat exchange of advancing second heat transmission equipment, 5 shell sides divides two-way to the Tc logistics of heat power supply device 11 afterwards then, one the tunnel returns fractionating column 6 bottom reflux inlets, go out device after the tube side heat exchange to 90 of another Lu Jindi three heat transmission equipments 7 ℃, make second heat transmission equipment 5 that middle pressure steam not take place or take place less; The temperature that is higher than T1r of coming out from the 5th heat transmission equipment 16 shell sides is the tube side that the conduction oil 15 of T1r ' enters the 6th heat transmission equipment 17 heat power supply device 22, and with the 6th heat transmission equipment 17 shell sides in the hot trap logistics heat exchange of coming out from another fractionating column 10, what another fractionating column 10 was returned in hot trap logistics heat exchange behind the T1r returns the tower inlet, conduction oil heat exchange is again replaced out the primary energy of the high energy matter of former heating furnace 9 consumption to the temperature T 2r ' that is higher than T2r; Temperature is the logistics heat exchange that the conduction oil of T2r ' enters the heat power supply device 33 that is come out by fractionating column 14 bottoms in the tube side of the 4th heat transmission equipment 13 in the heat power supply device 33 and the 4th heat transmission equipment 13 shell sides again, the logistics heat exchange of heat power supply device 33 enters the mouth to the tower that returns that T2r returns fractionating column 14, conduction oil heat exchange again arrives T3, replace out the middle pressure steam that former the 4th heat transmission equipment 13 consumes, temperature is that the conduction oil of T3 enters heat power supply device 11 beginning cycle heat exchanges again.
Described heat power supply device 11 is a catalytic cracking unit; Described heat power supply device 22 is reformer or methyl ethyl ketone plant or special solvent oil device; Described heat power supply device 33 is aromatic extraction unit or methyl ethyl ketone plant.
Described heat transmission equipment is made up of the heat exchanger of 1-6 platform.
Described temperature T d is 290-260 ℃, and Ta is 170-230 ℃, and Tb ' is 280-260 ℃, and Tc is 270-250 ℃, and T1r is 200-280 ℃, and T1r ' is 250-300 ℃, and T2r is 150-300 ℃, and T2r ' is 210-290 ℃, and T3 is 200-250 ℃.
A kind of application of high temperature heat integration system for oil-extraction plant is characterized in that: be applied to potential temperature at the chemical plant installations of 350-260 ℃ thermal source logistics or the chemical plant installations of potential temperature 150-280 ℃ hot trap logistics arranged.
Compared with prior art, the present invention optimizes heat-exchange network, and the middle pressure steam of fuel savings gas and tower bottom reboiler reduces plant energy consumption, reduces the oil refining cost, increases economic efficiency.
[description of drawings]
Fig. 1 is existing chemical unit device heat-exchange system connection diagram.
Fig. 2 is the connection diagram that the big system synthesis of elevated temperature heat of the present invention is utilized
Appointment Fig. 2 is a Figure of abstract.
Referring to Fig. 1 and Fig. 2,3 is first heat transmission equipment; 5 is second heat transmission equipment; 6 is fractionating column; 7 is the 3rd heat transmission equipment; 9 is heating furnace; 10 is another fractionating column; 13 is the 4th heat transmission equipment; 14 is another fractionating column; 16 is the 5th heat transmission equipment; 17 is the 6th heat transmission equipment; 11 is heat power supply device; 22 another heat power supply devices; 33 is another heat power supply device.
[specific embodiment]
Below the invention will be further described.
200-250 ℃ conduction oil enters the shell side of the 5th newly-increased in the heat power supply device 11 heat transmission equipment 16 by the thermal medium pipe, with a logistics heat exchange of extracting the heat power supply device 11 that mouth comes out in the tube side of the 5th heat transmission equipment 16 by fractionating column 6 bottoms out, the temperature of heat power supply device 11 logistics is Td=290-260 ℃ after the heat exchange, the tube side that first heat transmission equipment 3 is advanced in heat power supply device 11 logistics again carries out heat exchange with the logistics of advancing first heat transmission equipment, 3 shell sides, the logistics of advancing first heat transmission equipment, 3 shell sides is arrived Ta=170-230 ℃ by heat exchange, the logistics of heat power supply device 11 is arrived Tb '=280-260 ℃ by heat exchange, the logistics of heat power supply device 11 tube side that advances second heat transmission equipment 5 again and the logistics heat exchange of advancing second heat transmission equipment, 5 shell sides divides two-way to the Tc=270-250 ℃ of logistics of heat power supply device 11 afterwards then, one the tunnel returns fractionating column 6 bottom reflux inlets, go out device after the tube side heat exchange to 90 of another Lu Jindi three heat transmission equipments 7 ℃, make second heat transmission equipment 5 that middle pressure steam not take place or take place less; The temperature of coming out from the 5th heat transmission equipment 16 shell sides is that T1r '=250-300 ℃ conduction oil 15 is higher than temperature T 1r=200-280 ℃, enter the tube side of the 6th heat transmission equipment 17 in the heat power supply device 22, and with the 6th heat transmission equipment 17 shell sides in the hot trap logistics heat exchange of coming out from another fractionating column 10, what another fractionating column 10 was returned in hot trap logistics heat exchange behind the T1r returns the tower inlet, conduction oil heat exchange again arrives temperature T 2r '=210-290 ℃, this T2r ' temperature is higher than T2r=150-300 ℃, replaces out the primary energy of the high energy matter that former heating furnace 9 consumes; Temperature is the logistics heat exchange that the conduction oil of T2r ' enters the heat power supply device 33 that is come out by fractionating column 14 bottoms in the tube side of the 4th heat transmission equipment 13 in the heat power supply device 33 and the 4th heat transmission equipment 13 shell sides again, the logistics heat exchange of heat power supply device 33 enters the mouth to the tower that returns that T2r returns fractionating column 14, conduction oil heat exchange again arrives T3=200-250 ℃, replace out the middle pressure steam that former the 4th heat transmission equipment 13 consumes, temperature is that the conduction oil of T3 enters heat power supply device 11 beginning cycle heat exchanges again.
Extract mouthful logistics of about 350-300 ℃ the heat power supply device 11 that comes out out by fractionating column 6 bottoms of heat power supply device 11 in the above-mentioned heat exchange process middle pressure steam does not take place in the tube side of the 5th heat transmission equipment 16 or takes place less, temperature is T3=200-250 ℃ conduction oil heat exchange in the logistics of heat power supply device 11 and the thermal medium pipe, the conduction oil temperature is T1r '=250-300 ℃ after the heat exchange, the temperature heat exchange of the logistics of heat power supply device 11 is to Td=290-260 ℃, conduction oil again with the hot trap logistics heat exchange of another heat power supply device 22, saved the fuel that heating furnace 9 consumes in original equipment; Afterwards conduction oil again with the hot trap logistics heat exchange of another heat power supply device 33, saved the steam that the 4th heat transmission equipment 13 consumes, finally saved the primary energy fuel of original heating furnace 9 consumption and the middle pressure steam that the 4th heat transmission equipment 13 consumes, energy is fully used.
Claims (4)
1. high temperature heat integration system for oil-extraction plant, comprise three heat power supply devices, heat power supply device (11) is mainly extracted the tube side that mouth connects first heat transmission equipment (3) and second heat transmission equipment (5) successively out by fractionating column (6) bottom, the tube side outlet of second heat transmission equipment (5) divides two-way again, one the tunnel returns the bottom reflux inlet that connects fractionating column (6), and another road connects the tube side import of the 3rd heat transmission equipment (7) and forms; Another heat power supply device (22) is mainly extracted mouth out by another fractionating column (10) bottom and is established two-way, and one the tunnel for going out device, and another road connects heating furnace (9) import, and heating furnace (9) outlet connects the tower inlet that returns of another fractionating column (10) again and forms; Another heat power supply device (33) is established two-way for mainly extracting mouth out by another fractionating column (14) bottom, one the tunnel for going out device, another road connects the shell side import of the 4th heat transmission equipment (13), the shell side outlet of the 4th heat transmission equipment (13) is returned the tower inlet that returns that connects another fractionating column (14) again and is formed, it is characterized in that with three independently heat power supply device adopt the thermal medium pipe to connect and be that the mode that heat catalysis forms heat integration is carried out the collection utilization of heat of high temperature with the conduction oil in the thermal medium pipe, its concrete syndeton is:
Set up the 6th heat transmission equipment (16) between fractionating column (6) in heat power supply device (11) and first heat transmission equipment (3), fractionating column (6) bottom is extracted a mouthful tube side import that connects the 6th heat transmission equipment (16) out, and the tube side outlet of the 6th heat transmission equipment (16) connects the tube side import of first heat transmission equipment (3); Adopt the shell side of the 7th heat transmission equipment (17) to connect the former heating furnace of replacement (9) connection in another heat power supply device (22), the shell side import of the 6th heat transmission equipment (16) in the heat power supply device (11) adopts the thermal medium pipe to connect the tube side outlet of the 4th heat transmission equipment (13) in the another heat power supply device (33), the shell side outlet of the 6th heat transmission equipment (16) connects the tube side import of the 7th heat transmission equipment (17) in another heat power supply device (22), and the tube side outlet of the 7th heat transmission equipment (17) connects the tube side import of the 4th heat transmission equipment (13) in the another heat power supply device (33) again;
Its heat exchange process is: 200-250 ℃ conduction oil enters the shell side of the 6th heat transmission equipment (16) newly-increased in the heat power supply device (11) by the thermal medium pipe, with a logistics heat exchange of extracting the heat power supply device (11) that mouth comes out in the tube side of the 6th heat transmission equipment (16) by fractionating column (6) bottom out, the temperature of heat power supply device after the heat exchange (11) logistics is Td, the tube side that first heat transmission equipment (3) is advanced in heat power supply device (11) logistics again carries out heat exchange with the logistics of advancing first heat transmission equipment (3) shell side, the logistics of advancing first heat transmission equipment (3) shell side is arrived Ta by heat exchange, the logistics of heat power supply device (11) is arrived Tb ' by heat exchange, the logistics of heat power supply device (11) tube side that advances second heat transmission equipment (5) again and the logistics heat exchange of advancing second heat transmission equipment (5) shell side divides two-way to the Tc logistics of heat power supply device (11) afterwards then, one the tunnel returns fractionating column (6) bottom reflux inlet, go out device after the tube side heat exchange to 90 of another Lu Jindi three heat transmission equipments (7) ℃, make second heat transmission equipment (5) that middle pressure steam not take place or take place less; The temperature that is higher than T1r of coming out from the 6th heat transmission equipment (16) shell side is the tube side that the conduction oil (15) of T1r ' enters the 7th heat transmission equipment (17) the heat power supply device (22), and with the 7th heat transmission equipment (17) shell side in the hot trap logistics heat exchange of coming out from another fractionating column (10), what another fractionating column (10) was returned in hot trap logistics heat exchange behind the T1r returns the tower inlet, conduction oil heat exchange is again replaced out the primary energy of the high energy matter of former heating furnace (9) consumption to the temperature T 2r ' that is higher than T2r; Temperature is the conduction oil of T2r ' enters the tube side and the heat power supply device (33) that comes out in the 4th heat transmission equipment (13) shell side of the 4th heat transmission equipment (13) in the heat power supply device (33) again bottom fractionating column (14) logistics heat exchange, the logistics heat exchange of heat power supply device (33) enters the mouth to the tower that returns that T2r returns fractionating column (14), conduction oil heat exchange again arrives T3, replace out the middle pressure steam that former the 4th heat transmission equipment (13) consumes, temperature is that the conduction oil of T3 enters heat power supply device (11) beginning cycle heat exchange again.
2. a kind of high temperature heat integration system for oil-extraction plant as claimed in claim 1 is characterized in that: described heat power supply device (11) is a catalytic cracking unit; Described another heat power supply device (22) is reformer or methyl ethyl ketone plant or special solvent oil device; Described another heat power supply device (33) is aromatic extraction unit or methyl ethyl ketone plant.
3. a kind of high temperature heat integration system for oil-extraction plant as claimed in claim 1 is characterized in that: described heat transmission equipment is made up of the heat exchanger of 1-6 platform.
4. a kind of high temperature heat integration system for oil-extraction plant as claimed in claim 1, it is characterized in that: described temperature T d is 290-260 ℃, Ta is 170-230 ℃, Tb ' is 280-260 ℃, and Tc is 270-250 ℃, and T1r is 200-280 ℃, T1r ' is 250-300 ℃, T2r is 150-300 ℃, and T2r ' is 210-290 ℃, and T3 is 200-250 ℃.
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| CN2008102041299A CN101424453B (en) | 2008-12-05 | 2008-12-05 | High temperature heat integration system for oil-extraction plant and use thereof |
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| CN101424453B true CN101424453B (en) | 2011-01-26 |
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Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102116593B (en) * | 2011-01-30 | 2013-01-02 | 北京三博中自科技有限公司 | Structured heat exchange network system and construction method thereof |
| CN105651067B (en) * | 2014-12-02 | 2018-04-06 | 上海优华系统集成技术有限公司 | A kind of high-temperature flue gas heat integrated system |
| US9803507B2 (en) | 2015-08-24 | 2017-10-31 | Saudi Arabian Oil Company | Power generation using independent dual organic Rankine cycles from waste heat systems in diesel hydrotreating-hydrocracking and continuous-catalytic-cracking-aromatics facilities |
| US9803513B2 (en) | 2015-08-24 | 2017-10-31 | Saudi Arabian Oil Company | Power generation from waste heat in integrated aromatics, crude distillation, and naphtha block facilities |
| US9725652B2 (en) | 2015-08-24 | 2017-08-08 | Saudi Arabian Oil Company | Delayed coking plant combined heating and power generation |
| US9803145B2 (en) | 2015-08-24 | 2017-10-31 | Saudi Arabian Oil Company | Power generation from waste heat in integrated crude oil refining, aromatics, and utilities facilities |
| US9803508B2 (en) | 2015-08-24 | 2017-10-31 | Saudi Arabian Oil Company | Power generation from waste heat in integrated crude oil diesel hydrotreating and aromatics facilities |
| US9803506B2 (en) | 2015-08-24 | 2017-10-31 | Saudi Arabian Oil Company | Power generation from waste heat in integrated crude oil hydrocracking and aromatics facilities |
| US9803511B2 (en) | 2015-08-24 | 2017-10-31 | Saudi Arabian Oil Company | Power generation using independent dual organic rankine cycles from waste heat systems in diesel hydrotreating-hydrocracking and atmospheric distillation-naphtha hydrotreating-aromatics facilities |
| US9803505B2 (en) | 2015-08-24 | 2017-10-31 | Saudi Arabian Oil Company | Power generation from waste heat in integrated aromatics and naphtha block facilities |
| US10227899B2 (en) | 2015-08-24 | 2019-03-12 | Saudi Arabian Oil Company | Organic rankine cycle based conversion of gas processing plant waste heat into power and cooling |
| US9745871B2 (en) | 2015-08-24 | 2017-08-29 | Saudi Arabian Oil Company | Kalina cycle based conversion of gas processing plant waste heat into power |
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Denomination of invention: High temperature heat integration system for oil-extraction plant and use thereof Effective date of registration: 20120326 Granted publication date: 20110126 Pledgee: Pudong Productivity Promotion Center, Shanghai Pledgor: Shanghai Youhua System Integration Technology Co., Ltd. Registration number: 2012990000107 |