CN203048845U - Ethylene tar processing system - Google Patents
Ethylene tar processing system Download PDFInfo
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- CN203048845U CN203048845U CN 201220690904 CN201220690904U CN203048845U CN 203048845 U CN203048845 U CN 203048845U CN 201220690904 CN201220690904 CN 201220690904 CN 201220690904 U CN201220690904 U CN 201220690904U CN 203048845 U CN203048845 U CN 203048845U
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Abstract
The utility model relates to an ethylene tar processing system which comprises a pressure-reduced reaction fractionation tower and a plurality of repolymerization towers, wherein the fractionation tower material outlet of the pressure-reduced reaction fractionation tower is connected with the repolymerization tower material inlet of one repolymerization tower; the repolymerization tower material inlets of the rest repolymerization towers are connected with the repolymerization tower material outlet of one repolymerization tower; a tower kettle and a fractionation segment are arranged on the pressure-reduced reaction fractionation tower from bottom to top; a plurality of fractionation tower disks which are distributed up and down and shaped liked a taper with an upward taper angle are arranged in the tower kettle; the top ends of the fractionation tower disks are opened; fractionation tower air raising pipes, of which the pipe walls extend upwards, are arranged at the top ends of all the fractionation tower disks or at the top ends of the other fractionation tower disks except the fractionation tower disks at the uppermost top; and overflow weirs are arranged at the bottom end of the fractionation tower disks. According to the ethylene tar processing system, the coking in each tower is nearly not generated; and the evaporation intensity is enhanced; so that the softening point of products discharged from the pressure-reduced reaction fractionation tower can reach 85 DEG C. After the products are repeatedly heated, evaporated and cooled in the repolymerization towers, the softening point of the products can reach 125 to 150 DEG C.
Description
Technical field
The utility model relates to a kind of ethylene bottom oil system of processing, belongs to chemical machinery field.
Background technology
At present external pyrolysis fuel oil is mainly as the raw material of producing carbon black.China's pyrolysis fuel oil is mainly for the production of road bitumen, and the use that also acts as a fuel has only the device of seldom part pyrolysis fuel oil utilization introduction to produce carbon black, the application of delayed coking unit at home, and comprehensive utilization ratio is not high on the whole, and added value of product has much room for improvement.
The comprehensive utilization process of present domestic ethylene bottom oil mainly is directly to adopt conventional equipment to carry out air distillation.Because the special property of ethylene bottom oil, the comprehensive utilization device of domestic a lot of ethylene bottom oils has all run into the serious problem of tower bottom coke, the frequent parking, and the petroleum resin products softening temperature of producing is lower, and added value of product is low.
The utility model content
For overcoming the above-mentioned defective of prior art, the purpose of this utility model is to provide a kind of ethylene bottom oil system of processing, can produce the petroleum resin products of high softening-point by this system.
The technical solution adopted in the utility model is: a kind of ethylene bottom oil system of processing, comprise decompression reaction separation column and several repolymerization towers, the separation column material outlet of described decompression reaction separation column connects the polymerization tower material inlet of a described repolymerization tower, the polymerization tower material inlet of remaining described repolymerization tower connects the polymerization tower material outlet of previous repolymerization tower, described decompression reaction separation column is provided with the separation column material inlet, described decompression reaction separation column is divided into tower reactor and distillation stage from bottom to top, comprise in the described tower reactor that several distribute tapered up and down and cone angle separation column tower tray up, the top end opening of described separation column tower tray, the top of whole described separation column tower trays or other separation column tower tray except topmost is provided with the upwardly extending separation column Steam Pipe of tube wall, and the bottom of described separation column tower tray is provided with separation column tower tray overflow weir.
Can be provided with the back taper separation column flow deflector that supplies flow downward between any two adjacent described separation column tower trays, the upper end of described separation column flow deflector and the sidewall of described tower reactor are tightly connected, link position is preferably placed at the below of the overflow weir of top described separation column tower tray, the lower end of described separation column flow deflector and preferably leave the gap between the sidewall of the Steam Pipe of following described separation column tower tray, the lower end of described separation column flow deflector can be provided with separation column flow deflector overflow weir.
Described distillation stage can be provided with packing layer, is filled with the filler for the material fractionation in the described packing layer, and described packing layer can adopt multilayered structure, is divided into some segments from top to bottom, can be provided with sparger between adjacent two segments.
Preferably, described separation column material inlet is arranged on the sidewall of described distillation stage, and described separation column material outlet is arranged on the bottom of described tower reactor, and the top of described distillation stage is provided with the separation column gaseous phase outlet.
Can be provided with the tower reactor refluxing opening on the sidewall of described tower reactor, the position is positioned at the top of uppermost described separation column tower tray, can be provided with separation column middle part refluxing opening on the sidewall at the middle part of described distillation stage, can be provided with separation column top refluxing opening on the sidewall at the top of described distillation stage, the top of described distillation stage can also be provided with the separation column bypass outlet, described separation column bypass outlet can be by each refluxing opening of a pipe connection separation column, perhaps can be respectively by each refluxing opening of different pipe connection separation columns, described tower reactor can be provided with outer well heater.
Described repolymerization tower can comprise several evaporator sections from bottom to top, can comprise in the described evaporator section that several distribute tapered up and down and cone angle polymerization tower tower tray up, the top end opening of described polymerization tower tower tray, the top of whole described polymerization tower tower trays or other polymerization tower tower tray except uppermost polymerization tower tower tray can be provided with the upwardly extending polymerization tower Steam Pipe of tube wall, and the bottom of described polymerization tower tower tray can be provided with polymerization tower tower tray overflow weir.
Can be provided with the back taper polymerization tower flow deflector that supplies flow downward between any two adjacent described polymerization tower tower trays, the upper end of described polymerization tower flow deflector and the sidewall of described evaporator section are tightly connected, link position is preferably placed at the below of the overflow weir of top described polymerization tower tower tray, the lower end of described polymerization tower flow deflector and preferably leave the gap between the sidewall of the Steam Pipe of following described polymerization tower tower tray, the lower end of described polymerization tower flow deflector can be provided with polymerization tower flow deflector overflow weir.
Be positioned at nethermost described evaporator section and can be provided with outer well heater, can be provided with the heating agent chuck on the outer wall of other evaporator section except nethermost described evaporator section, the position of described heating agent chuck is preferably corresponding with adjacent described polymerization tower tower tray overflow weir and the position of polymerization tower flow deflector upper end in the described evaporator section at its place, and described heating agent chuck can be provided with thermal medium import and thermal medium outlet.
Preferably, described polymerization tower material inlet is arranged on the sidewall of described repolymerization tower, the position is positioned at the top of uppermost described polymerization tower tower tray of the described evaporator section at its place, described polymerization tower material outlet is arranged on the bottom of described repolymerization tower, and the top of described repolymerization tower is provided with the polymerization tower gaseous phase outlet.
Can be provided with the polymerization tower refluxing opening on the sidewall of described evaporator section all or part, the position of described polymerization tower refluxing opening is preferably placed at the top of the uppermost polymerization tower tower tray in the described evaporator section at its place, the top of described repolymerization tower can be provided with the polymerization tower bypass outlet, described polymerization tower bypass outlet can connect each polymerization tower refluxing opening respectively by a pipeline, perhaps can pass through different each polymerization tower refluxing openings of pipe connection respectively.
The beneficial effects of the utility model: the utility model combines ethylene bottom oil evaporative fractionation technology and repolymerization technology effectively, by the repolymerization tower heat repeatedly, evaporate and cool off after can produce the petroleum resin products of high softening-point;
The design of the tower tray of the taper in decompression reaction separation column and the repolymerization tower has guaranteed enough evaporation areas, also helps to improve the softening temperature of product;
The design of the refluxing opening in decompression reaction separation column and the repolymerization tower, make the solid circulating rate in the corresponding column strengthen, cooperate the taper tower tray to provide enough sliding forces for material, the flowability of material itself is washed away corresponding tower tray, make homogeneous heating, avoided the coking of material;
The overflow weir of the tower tray in decompression reaction separation column and the repolymerization tower and the overflow weir of flow deflector have guaranteed that effectively material can be evenly distributed in each position of the tower tray of below, avoids the material skewness;
The design of the heating agent chuck of repolymerization tower has been avoided material to assemble generation for a long time in the corresponding position effectively and has been solidified;
Substantially do not produce coking in decompression reaction separation column of the present utility model and the repolymerization tower, adopt a repolymerization tower can produce the petroleum resin products of softening temperature about up to 125 ℃, adopt two repolymerization towers can produce the petroleum resin products of softening temperature about up to 150 ℃.
Description of drawings
Fig. 1 is structural representation of the present utility model;
Fig. 2 is the structural representation of decompression reaction separation column of the present utility model;
Fig. 3 is the structural representation of repolymerization tower of the present utility model.
Embodiment
Referring to Fig. 1, Fig. 2 and Fig. 3, the utility model provides a kind of ethylene bottom oil system of processing, comprise decompression reaction separation column 1 and several repolymerization towers, the separation column material outlet of described decompression reaction separation column connects the polymerization tower material inlet of a described repolymerization tower, the polymerization tower material inlet of remaining described repolymerization tower connects the polymerization tower material outlet of previous repolymerization tower, the quantity of described repolymerization tower can be two, be respectively one-level repolymerization tower 2 and secondary repolymerization tower 3, processing by two described repolymerization towers, the softening temperature of the petroleum resin products of producing can be up to 150 ℃ about, described decompression reaction separation column is provided with the separation column material inlet.Described decompression reaction separation column is divided into tower reactor and distillation stage from bottom to top, described tower reactor is used for material is evaporated, described distillation stage is used for vaporized product is carried out prefractionation, comprise in the described tower reactor that several distribute tapered up and down and cone angle separation column tower tray 4 up, improve the evaporation area of described separation column tower tray effectively, the top end opening of described separation column tower tray, the top of whole described separation column tower trays or other separation column tower tray except topmost is provided with the upwardly extending separation column Steam Pipe of tube wall, the vaporized product that is used for the below is passed, described separation column Steam Pipe can be determined its height according to operational load, the bottom of described separation column tower tray is provided with separation column tower tray overflow weir, is used for the convection cell material and distributes.
Can be provided with the back taper separation column flow deflector 5 that supplies flow downward between any two adjacent described separation column tower trays, the upper end of described separation column flow deflector and the sidewall of described tower reactor are tightly connected, link position is preferably placed at the below of the overflow weir of top described separation column tower tray, the material that assurance flows down from top described separation column tower tray can all drop on the described separation column tower tray below being positioned at by described separation column flow deflector, the lower end of described separation column flow deflector and between the sidewall of the Steam Pipe of following described separation column tower tray, preferably leave the gap, make things convenient for fluid to pass through, for the material that flows down from described separation column flow deflector can be evenly distributed on the described separation column tower tray of described separation column flow deflector below, the lower end of described separation column flow deflector can be provided with separation column flow deflector overflow weir.
The quantity of described separation column tower tray can be two, and the quantity of described separation column flow deflector can be one.
Described distillation stage can be provided with packing layer, be used for vaporized product is carried out fractionation, be filled with the filler 6 for the material fractionation in the described packing layer, described packing layer can adopt multilayered structure, be divided into some segments from top to bottom, such as 3 sections, 4 sections, 5 sections or 6 sections, both can have guaranteed that gaseous substance and liquid phase substance successfully realized countercurrent flow, can improve the contact area of gaseous substance and liquid phase substance again, improve fractionating effect.Can be provided with sparger between adjacent two segments, described sparger can evenly distribute liquid phase substance again, to improve the homogeneity that liquid phase substance distributes at the cross section of next section filler.
Each segment of described packing layer can adopt identical or different filler respectively, the vertical height of each segment can be identical or different, can suitably regulate filler and segment vertical height according to fractionation requirement and fractionating effect, reach requirement to guarantee fractionating effect.
Preferably, described separation column material inlet 7 is arranged on the sidewall of described distillation stage, and described separation column material outlet 8 is arranged on the bottom of described tower reactor, and the top of described distillation stage is provided with separation column gaseous phase outlet 9.
Can be provided with tower reactor refluxing opening 10 on the sidewall of described tower reactor, the position is positioned at the top of uppermost described separation column tower tray, make the tower reactor solid circulating rate strengthen, cooperate the separation column tower tray of taper to provide enough sliding forces for material, avoid the coking of material, can be provided with separation column middle part refluxing opening 11 on the sidewall at the middle part of described distillation stage, can be provided with separation column top refluxing opening 12 on the sidewall at the top of described distillation stage, the top of described distillation stage can also be provided with the separation column bypass outlet, described separation column bypass outlet can be by each refluxing opening of a pipe connection separation column, perhaps can pass through each refluxing opening of different pipe connection separation columns respectively, described tower reactor can be provided with outer well heater, is used for the material in the described tower reactor is heated.
Described repolymerization tower can comprise several evaporator sections from bottom to top, can be three, four, five or more, preferably more than three, help the evaporation of material, can comprise in the described evaporator section that several distribute tapered up and down and cone angle polymerization tower tower tray 13 up, effectively improve the evaporation area of described polymerization tower tower tray, the top end opening of described polymerization tower tower tray, the top of whole described polymerization tower tower trays or other polymerization tower tower tray except uppermost polymerization tower tower tray can be provided with the upwardly extending polymerization tower Steam Pipe of tube wall, the passing of vaporized product that is used for the below, described polymerization tower Steam Pipe can be determined its height according to operational load, the bottom of described polymerization tower tower tray can be provided with polymerization tower tower tray overflow weir, is used for the convection cell material and distributes.
Can be provided with the back taper polymerization tower flow deflector 14 that supplies flow downward between any two adjacent described polymerization tower tower trays in the same described evaporator section, the upper end of described polymerization tower flow deflector and the sidewall of described evaporator section are tightly connected, link position is preferably placed at the below of the overflow weir of top described polymerization tower tower tray, the material that assurance flows down from top described polymerization tower tower tray can all drop on the described polymerization tower tower tray below being positioned at by described polymerization tower flow deflector, the lower end of described polymerization tower flow deflector and between the sidewall of the Steam Pipe of following described polymerization tower tower tray, preferably leave the gap, make things convenient for fluid foods to pass through, for the material that flows down from described polymerization tower flow deflector can be evenly distributed on the described polymerization tower tower tray of described polymerization tower flow deflector below, the lower end of described polymerization tower flow deflector can be provided with polymerization tower flow deflector overflow weir.
The quantity of polymerization tower tower tray can be two described in described evaporator section, and the quantity of described polymerization tower flow deflector can be one.
Be positioned at nethermost described evaporator section and can be provided with outer well heater, be used for the material of its inside is heated, can be provided with heating agent chuck 15 on the outer wall of other evaporator section except nethermost described evaporator section, the position of described heating agent chuck is preferably corresponding with adjacent described polymerization tower tower tray overflow weir and the position of polymerization tower flow deflector upper end (being the position that the upper end of polymerization tower tower tray overflow weir and polymerization tower flow deflector connects) in the described evaporator section at its place, solidify to prevent that the long-time gathering of fluid material from causing, described heating agent chuck can be provided with thermal medium import and thermal medium outlet.
Preferably, described polymerization tower material inlet 16 is arranged on the sidewall of described repolymerization tower, the position is positioned at the top of uppermost described polymerization tower tower tray of the described evaporator section at its place, described polymerization tower material outlet 17 is arranged on the bottom of described repolymerization tower, and the top of described repolymerization tower is provided with polymerization tower gaseous phase outlet 18.
Can be provided with the polymerization tower refluxing opening on the sidewall of described evaporator section all or part, the position of described polymerization tower refluxing opening is preferably placed at the top of the uppermost polymerization tower tower tray in the described evaporator section at its place, make the interior solid circulating rate of tower strengthen, cooperate the polymerization tower tower tray of taper to provide enough sliding forces for material, thereby the flowability of utilizing material itself is washed away described polymerization tower tower tray, make homogeneous heating, effectively prevent the material coking.Preferably, described ethylene bottom oil repolymerization tower is provided with three refluxing openings, be respectively the top refluxing opening 19 of the portion of being located thereon, be positioned at the middle part refluxing opening 20 and the bottom refluxing opening 21 that is positioned at the bottom at middle part, the design of three refluxing openings in upper, middle and lower can improve temperature distribution in the tower effectively, avoids local temperature low excessively.The top of described repolymerization tower can be provided with the polymerization tower bypass outlet, and described polymerization tower bypass outlet can connect each polymerization tower refluxing opening respectively by a pipeline, perhaps can pass through different each polymerization tower refluxing openings of pipe connection respectively.
Principle of work of the present utility model: the raw material ethylene bottom oil enters decompression reaction separation column by the separation column material inlet after preheating, flash distillation takes place in tower, preliminary polymerization and fractionation, comparatively the material of lightweight is overflowed from the separation column gaseous phase outlet, analyze the qualified product of softening temperature and enter one-level repolymerization tower from the discharge of separation column material outlet, in one-level repolymerization tower, carry out multistage evaporation, analyze the qualified product of softening temperature and enter secondary repolymerization tower from the polymerization tower material outlet outflow of one-level repolymerization tower, in secondary repolymerization tower, proceed multistage evaporation, analyze the qualified product of softening temperature and discharge from the polymerization tower material outlet of secondary repolymerization tower, be delivered to subsequent technique equipment.
Basic noncoking in decompression reaction separation column of the present utility model and the repolymerization tower, the softening temperature that reacts the product of separation column discharge from decompression can reach 80～85 ℃, as 80 ℃, 82 ℃, 83 ℃ or 85 ℃, the softening temperature of the product of discharging from one-level repolymerization tower can reach 120～125 ℃, as 120 ℃, 122 ℃, 124 ℃ or 125 ℃, multistage evaporation through secondary repolymerization tower can make the softening temperature of product reach 145～150 ℃ again, as 145 ℃, 147 ℃, 148 ℃ or 150 ℃.
Claims (10)
1. ethylene bottom oil system of processing, it is characterized in that comprising decompression reaction separation column and several repolymerization towers, the separation column material outlet of described decompression reaction separation column connects the polymerization tower material inlet of a described repolymerization tower, the polymerization tower material inlet of remaining described repolymerization tower connects the polymerization tower material outlet of previous repolymerization tower, described decompression reaction separation column is provided with the separation column material inlet, described decompression reaction separation column is divided into tower reactor and distillation stage from bottom to top, comprise in the described tower reactor that several distribute tapered up and down and cone angle separation column tower tray up, the top end opening of described separation column tower tray, the top of whole described separation column tower trays or other separation column tower tray except topmost is provided with the upwardly extending separation column Steam Pipe of tube wall, and the bottom of described separation column tower tray is provided with separation column tower tray overflow weir.
2. ethylene bottom oil system of processing as claimed in claim 1, it is characterized in that being provided with the back taper separation column flow deflector that supplies flow downward between any two adjacent described separation column tower trays, the upper end of described separation column flow deflector and the sidewall of described tower reactor are tightly connected, link position is positioned at the below of the overflow weir of top described separation column tower tray, the lower end of described separation column flow deflector and leave the gap between the sidewall of the Steam Pipe of following described separation column tower tray, the lower end of described separation column flow deflector is provided with separation column flow deflector overflow weir.
3. ethylene bottom oil system of processing as claimed in claim 2, it is characterized in that described distillation stage is provided with packing layer, be filled with the filler for the material fractionation in the described packing layer, described packing layer adopts multilayered structure, be divided into some segments from top to bottom, be provided with sparger between adjacent two segments.
4. ethylene bottom oil system of processing as claimed in claim 3, it is characterized in that described separation column material inlet is arranged on the sidewall of described distillation stage, described separation column material outlet is arranged on the bottom of described tower reactor, and the top of described distillation stage is provided with the separation column gaseous phase outlet.
5. ethylene bottom oil system of processing as claimed in claim 4, the sidewall that it is characterized in that described tower reactor is provided with the tower reactor refluxing opening, the position is positioned at the top of uppermost described separation column tower tray, the sidewall at the middle part of described distillation stage is provided with separation column middle part refluxing opening, the sidewall at the top of described distillation stage is provided with separation column top refluxing opening, the top of described distillation stage also is provided with the separation column bypass outlet, described separation column bypass outlet is by each refluxing opening of a pipe connection separation column, perhaps respectively by each refluxing opening of different pipe connection separation columns, described tower reactor is provided with outer well heater.
6. as claim 1,2,3,4 or 5 described ethylene bottom oil systems of processing, it is characterized in that described repolymerization tower comprises several evaporator sections from bottom to top, comprise in the described evaporator section that several distribute tapered up and down and cone angle polymerization tower tower tray up, the top end opening of described polymerization tower tower tray, the top of whole described polymerization tower tower trays or other polymerization tower tower tray except uppermost polymerization tower tower tray is provided with the upwardly extending polymerization tower Steam Pipe of tube wall, and the bottom of described polymerization tower tower tray is provided with polymerization tower tower tray overflow weir.
7. ethylene bottom oil system of processing as claimed in claim 6, it is characterized in that being provided with the back taper polymerization tower flow deflector that supplies flow downward between any two adjacent described polymerization tower tower trays, the upper end of described polymerization tower flow deflector and the sidewall of described evaporator section are tightly connected, link position is positioned at the below of the overflow weir of top described polymerization tower tower tray, the lower end of described polymerization tower flow deflector and leave the gap between the sidewall of the Steam Pipe of following described polymerization tower tower tray, the lower end of described polymerization tower flow deflector is provided with polymerization tower flow deflector overflow weir.
8. ethylene bottom oil system of processing as claimed in claim 7, it is characterized in that being positioned at nethermost described evaporator section and be provided with outer well heater, the outer wall of other evaporator section except nethermost described evaporator section is provided with the heating agent chuck, the position of the adjacent described polymerization tower tower tray overflow weir in the described evaporator section at the position of described heating agent chuck and its place and polymerization tower flow deflector upper end is corresponding, and described heating agent chuck is provided with thermal medium import and thermal medium outlet.
9. ethylene bottom oil system of processing as claimed in claim 8, it is characterized in that described polymerization tower material inlet is arranged on the sidewall of described repolymerization tower, the position is positioned at the top of uppermost described polymerization tower tower tray of the described evaporator section at its place, described polymerization tower material outlet is arranged on the bottom of described repolymerization tower, and the top of described repolymerization tower is provided with the polymerization tower gaseous phase outlet.
10. ethylene bottom oil system of processing as claimed in claim 9, the sidewall that it is characterized in that described evaporator section whole or part is provided with the polymerization tower refluxing opening, the position of described polymerization tower refluxing opening is positioned at the top of uppermost polymerization tower tower tray of the described evaporator section at its place, the top of described repolymerization tower is provided with the polymerization tower bypass outlet, described polymerization tower bypass outlet connects each polymerization tower refluxing opening respectively by a pipeline, perhaps respectively by different each polymerization tower refluxing openings of pipe connection.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220690904 CN203048845U (en) | 2012-12-14 | 2012-12-14 | Ethylene tar processing system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220690904 CN203048845U (en) | 2012-12-14 | 2012-12-14 | Ethylene tar processing system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203048845U true CN203048845U (en) | 2013-07-10 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220690904 Expired - Lifetime CN203048845U (en) | 2012-12-14 | 2012-12-14 | Ethylene tar processing system |
Country Status (1)
| Country | Link |
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| CN (1) | CN203048845U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110204657A (en) * | 2019-06-18 | 2019-09-06 | 安徽同心新材料科技有限公司 | Light number a kind of, high softening-point C9 hot polymerization petroleum resin products and preparation process |
| CN113599856A (en) * | 2021-08-11 | 2021-11-05 | 安徽晟捷新能源科技有限公司 | Equipment for recycling tar at bottom of NMP (N-methyl pyrrolidone) rectifying tower |
-
2012
- 2012-12-14 CN CN 201220690904 patent/CN203048845U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110204657A (en) * | 2019-06-18 | 2019-09-06 | 安徽同心新材料科技有限公司 | Light number a kind of, high softening-point C9 hot polymerization petroleum resin products and preparation process |
| CN110204657B (en) * | 2019-06-18 | 2022-07-19 | 安徽同心新材料科技有限公司 | Light-color C9 heat-polymerized petroleum resin product with high softening point and preparation process thereof |
| CN113599856A (en) * | 2021-08-11 | 2021-11-05 | 安徽晟捷新能源科技有限公司 | Equipment for recycling tar at bottom of NMP (N-methyl pyrrolidone) rectifying tower |
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Granted publication date: 20130710 |
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