CN201377961Y - Multi-operating mode air separation equipment - Google Patents
Multi-operating mode air separation equipment Download PDFInfo
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- CN201377961Y CN201377961Y CN200820185786U CN200820185786U CN201377961Y CN 201377961 Y CN201377961 Y CN 201377961Y CN 200820185786 U CN200820185786 U CN 200820185786U CN 200820185786 U CN200820185786 U CN 200820185786U CN 201377961 Y CN201377961 Y CN 201377961Y
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- air
- nitrogen
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Abstract
The utility model provides multi-operating mode air separation equipment. Air passes by air compressors, a precooling unit, a molecular sieve adsorber and a main heat exchanger and then enters a rectifying tower; the rectifying tower comprises an upper tower, a lower tower and a condensing evaporator; the upper tower is communicated with the lower tower; and the upper tower comprises an oxygen outlet, a nitrogen outlet and a polluted nitrogen outlet. The utility model has the advantages that four piston-type air compressors are arranged, and air compressors with different numbers can be adopted to be combined together under different operating modes, so the purpose of saving energy is achieved; because a pressurizing air cooler is additionally provided with backflow polluted nitrogen, the air can be cooled and pressurized simultaneously by backflow oxygen, nitrogen and polluted nitrogen when the air separation equipment is started, the pressurized air can be at normal temperature when entering the main heat exchanger, and the starting time of the air separation equipment can be shortened by one third. The utility model can meet the requirement of different operating modes of 350 Nm<3>/h, 550 Nm<3>/h and 750 Nm<3>/h.
Description
Technical field
The utility model relates to a kind of air separation equipment.
Background technology
Air separation plant is widely used in fields such as oil, chemical industry, metallurgy and environmental protection, and its basic principle is to utilize cryogenic rectification method, and air setting is become liquid, isolates oxygen, nitrogen or other inert gases according to the difference of each component gasification temperature from air.In recent years, large air separation plant is by introducing technology and product, and technological progress is fast, and production cost is declined to a great extent.Though packaged air separation plant also improves to some extent technically, progressive little, increasing with the technological gap of large air separation plant, be faced with severe tests, add that liquid fills the impact to air separation unit, many enterprises are arranged stop production because of loss of capital.Packaged air separation plant demand on the market is big especially, and 350Nm
3/ h, 550Nm
3/ h, 750Nm
3/ h is again the main force on the small-sized empty branch market, more than three types packaged air separation plant and be stored on the market.
The adaptability of general packaged air separation plant load change is poor.Air compressor machine, precooler, purifier all are difficult to satisfy for changing bigger operation operating mode.The operating flexibility load of fractionating column is ± 20%, load surpasses+during the big operating mode of 20%[] and gas flow rate is excessive, liquid can not dirtyly cause liquid flooding, and minimizing load [during unskilled labourer's condition] sieve plate endure, but, have a strong impact on the rectifying quality owing to leak of liquid on the minimizing of rising steam, the sieve plate on the sieve plate can cause efficiency of sieve plate to descend.
The utility model content
The purpose of this utility model is to solve above-mentioned technical problem, and the air separation plant of a kind of efficient energy-saving and the operation of energy multi-state is provided.
The purpose of this utility model is achieved through the following technical solutions:
A kind of multi-state air separation plant comprises by the interconnective air compressor of pipeline, precooling unit, molecular sieve purifier, fractionating column, booster expansion turbine.After air passes through air compressor, precooling unit, molecular sieve purifier successively, the sub-fraction air is introduced the supercharger supercharging, all the other major parts enter fractionating column, and described fractionating column comprises charger-air cooler, main heat exchanger, subcooler, the Xia Ta that is interconnected, last tower and condenser/evaporator.Air enters rectifying column after passing through main heat exchanger, and described rectifying column comprises the Xia Ta that is interconnected, last tower and condenser/evaporator.Described tower down is provided with the compressed-air actuated import behind the purifying, and its bottom is the outlet of oxygen-enriched liquid air, and the top is the import of liquid nitrogen; Described bottom of going up tower is the outlet of oxygen, and its middle part is the import of oxygen-enriched liquid air, is connected by subcooler with the outlet of the oxygen-enriched liquid air of following tower, and the top of last tower is the outlet of nitrogen, and the top of last tower also is provided with the outlet of dirty nitrogen; Described condenser/evaporator is connected with the top of following tower, is used for the part nitrogen of following tower is condensed into liquid nitrogen, the vaporization of liquid oxygen in the last tower; The pipeline of described connection oxygen outlet, nitrogen outlet, dirty nitrogen outlet outputs to oxygen, nitrogen, dirty nitrogen outside the multi-state air separation plant after all passing main heat exchanger respectively again.
Further, the pipeline of described connection nitrogen outlet, dirty nitrogen outlet passes subcooler earlier, nitrogen, dirty nitrogen is outputed to outside the multi-state air separation plant after passing main heat exchanger more again.
Again further, after the pipeline of described dirty nitrogen outlet passes subcooler and main heat exchanger earlier, after passing charger-air cooler more dirty nitrogen is outputed to outside the multi-state air separation plant, increase one returning polluted nitrogen in the described charger-air cooler, when device start, utilized oxygen, nitrogen, three strands of gas charge air coolings simultaneously that backflow of dirty nitrogen.
Again further, the pipeline between the import of the oxygen-enriched liquid air of the outlet of the described oxygen-enriched liquid air of tower down and last tower passes subcooler.
Further, also include two booster expansion turbines, the air after this booster expansion turbine expands is transported to the expanded air import department of tower by pipeline.
Further, described air compressor has separate four.Described precooler only produces a refrigerating circuit, a compressor job.
Further, the pipeline of the dirty nitrogen of described conveying is through behind the main heat exchanger, and a part is passed charger-air cooler, and a part is connected on the electric heater.
The beneficial effects of the utility model are mainly reflected in: be provided with four piston type air compressors, make the compressor combination of selecting varying number under the different operating modes, thereby reached purpose of energy saving; Precooler is according to the variation of compressed air air outlet temperature, and the capacity of compressor output changes, and hot gas bypass valve is assisted a ruler in governing a country adjusting, and the refrigerating capacity that finally reaches system is regulated; Upper and lower tower adopts the efficient convection current sieve plate of all-aluminium construction, fully guarantees the levelness of column plate, and the plate efficiency height makes product recovery rate height, and the new structure rectifying column guarantees multiple variable parameter operation; Increased one returning polluted nitrogen gas in the charger-air cooler, when device start, utilized oxygen, nitrogen, three strands of gas charge air coolings simultaneously that backflow of dirty nitrogen, made pressurized air when entering main heat exchanger, can reach normal temperature, shortened for 1/3rd start-up time; Decompressor utilizes the partial pressure air swell refrigeration of motion device, and the air after the expansion is sent into tower and participated in rectifying, has improved rectification efficiency, has reduced the pressure at expulsion of air compressor machine, from having accomplished low pressure process in essence, has played energy-conservation effect.
Description of drawings
Below in conjunction with accompanying drawing technical solutions of the utility model are described further:
Fig. 1: the schematic diagram of the utility model multi-state air separation plant.
Wherein:
1 air compressor, 2 precooling units, 3 mufflers
4 molecular sieve adsorbers, 5 electric heaters, 6 booster expansion turbines
9 times towers of 7 charger-air coolers, 8 main heat exchangers
Tower 12 subcoolers on 10 condenser/evaporators 11
13 oxygen outlets, 14 expanded airs advance 15 nitrogen outlets
16 dirty nitrogen outlet 17 oxygen-enriched liquid airs advance 18 air intlets
19 oxygen-enriched liquid airs export 20 liquid nitrogen imports
The specific embodiment
Principle of the present utility model is to utilize the difference of oxygen nitrogen boiling point in the air, adopts the method for cryogenic rectification to isolate oxygen and nitrogen from air.
As shown in Figure 1, multi-state air separation plant of the present utility model, comprise that by the interconnective air compressor 1 of pipeline, precooling unit 2, molecular sieve adsorber 3 and fractionating column described fractionating column is made up of charger-air cooler 7, main heat exchanger 8, time tower 9, condenser/evaporator 10, last tower 11, subcooler 12.Air is successively through entering fractionating column behind air compressor 1, precooling unit 2, the molecular sieve adsorber 3.Described air compressor 1 has separate four, selects the compressor combination of varying number under the different operating modes, thereby has reached purpose of energy saving.
Described rectifying column comprises the following tower 9 that is interconnected, last tower 11 and condenser/evaporator 10.Described tower 9 down is provided with the compressed-air actuated import 18 behind the purifying, and its bottom is the outlet 19 of oxygen-enriched liquid air, and the top is the import 20 of liquid nitrogen.
Described bottom of going up tower 11 is the outlet 13 of oxygen, and its middle part is the import 17 of oxygen-enriched liquid air, is connected with the outlet 19 of the oxygen-enriched liquid air of following tower 9, and the top of last tower 11 is the outlet 15 of nitrogen, and the top of last tower 11 also is provided with the outlet 16 of dirty nitrogen.
Described condenser/evaporator 10 is connected with the top of following tower, is used for the part nitrogen of following tower 9 is condensed into liquid nitrogen, the vaporization of liquid oxygen in the last tower.
The pipeline of above-mentioned connection oxygen outlet 13 outputs to oxygen outside the multi-state air separation plant after passing main heat exchanger 8 again.After above-mentioned connection nitrogen outlet 15, the pipeline of dirty nitrogen outlet 16 all pass subcooler 12 earlier, again nitrogen, dirty nitrogen are outputed to outside the multi-state air separation plant after passing main heat exchanger 8 more respectively.Pipeline between the import 17 of the outlet 19 of the described oxygen-enriched liquid air of tower 9 down and the oxygen-enriched liquid air of last tower 11 passes subcooler 12.
The utility model also includes two booster expansion turbines 6, and the air after this booster expansion turbine 6 expands is transported to expanded air import 14 places of tower 11 by pipeline.Decompressor utilizes the partial pressure air swell refrigeration of motion device, and the air after the expansion is sent into tower and participated in rectifying, has improved rectification efficiency, has reduced the pressure at expulsion of air compressor machine, from having accomplished low pressure process in essence, has played energy-conservation effect.
The flow process of the utility model separation of air below underdraws.
Air is after air cleaner removes dust and other mechanical admixtures, in air compressor 1, be compressed into required pressure, cool off and remove profit through aftercooler, enter precooling unit 2 cooling then, enter purifier after separating free water, removed moisture content, carbon dioxide by activated alumina and molecular sieve.
Behind the purifying, wherein most of air enters ice chest, is cooled near condensing temperature with product oxygen, nitrogen, the dirty nitrogen heat exchange of backflowing in main heat exchanger 8, and the following tower 9 that enters rectifying column then carries out initial gross separation.
Obtain pure nitrogen gas at following top of tower, following tower bottom obtains oxygen-enriched liquid air; Pure nitrogen gas carries out heat exchange with the liquid oxygen of opposite side in condenser/evaporator 10, because nitrogen is different with the pressure of liquid oxygen, make the vaporization of liquid oxygen pure nitrogen gas of tower then be condensed into liquid nitrogen.Part in the liquid nitrogen is as the phegma of tower down, another part liquid nitrogen then in subcooler 12 by pure nitrogen gas and dirty nitrogen cross cold after, sent into top of tower by throttling.
The oxygen-enriched liquid air of following tower bottom is crossed cold back throttling by pure nitrogen gas and dirty nitrogen and is sent into the tower middle part in subcooler 12.From the dirty nitrogen that draw at last tower middle part, after subcooler 12 and main heat exchanger 8 re-heats, send ice chest, a part is also as sieve purification system regeneration usefulness.
In order to provide cold to air separation plant, the sub-fraction air behind the purifying is introduced booster expansion turbine 6 superchargings, the air after being pressurized is through charger-air cooler 7 coolings.After in main heat exchanger 8, being cooled to-145 ℃, delivering in the decompressor air behind the swell refrigeration and send into the participation rectifying of tower middle part with backflow product oxygen, low-pressure nitrogen, dirty nitrogen heat exchange.
Booster expansion turbine has two, the using and the reserved.The air separation plant start-up period, two booster expansion turbines put into operation together, to increase refrigerating capacity, shorten start-up time.During normal the operation, as long as a booster expansion turbine input.The work done of decompressor is reclaimed by the supercharger with the coaxial heterodoxy coupling of turbo-expander, in order to improve the inlet pressure of turbo-expander, increases enthalpy drop, reduces the expanded air amount, has also improved a whole set of empty recovery rate that divides simultaneously.The utility model has increased one returning polluted nitrogen in charger-air cooler 7, when device start, utilize oxygen, nitrogen, three strands of gas charge air coolings simultaneously that backflow of dirty nitrogen, make pressurized air main can reach normal temperature when changing entering, improved entry condition greatly, probably can shorten for 1/3rd start-up time by the actual motion proof.
The utility model is provided with four air compressors.During 350 operating modes, open two air compressor machines; During 550 operating modes, open three air compressor machines; During 750 operating modes, with opening four air compressor machines.Saved the air compressor machine energy consumption greatly.And, in case there is an air compressor machine to break down, can't influence normal operation, Off-design operation gets final product, and has improved production efficiency.
The utility model by changing decompressor inlet and outlet pressure and temperature, makes booster expansion turbine 6 can satisfy the requirement of different operating modes by the analog computation of advanced flow process software.During 350 operating modes, expander inlet pressure 0.37MPa is set, inlet temperature 130.5K, gas flow are 480Nm
3/ h; During 550 operating modes, expander inlet pressure 0.55MPa is set, inlet temperature 141.9K, gas flow are 620Nm3/h; During 750 operating modes, expander inlet pressure 0.783MPa is set, inlet temperature 143.1K, gas flow are 850Nm
3/ h.The utility model air separation plant has been realized good the combination with the concrete parameter of decompressor in process organization.
Product oxygen is drawn from last tower bottom, with the raw air heat exchange, reclaims the cold re-heat and send ice chest behind normal temperature in main heat exchanger 8, charger-air cooler 7.
Product nitrogen is drawn from last top of tower, and is cold excessively through subcooler, therein with liquid air, liquid nitrogen heat exchange, sends ice chest through main heat exchanger 8, charger-air cooler 7 after reclaiming cold again.
The extraction sub-fraction charges into ice chest as the blanket gas of air separation plant in the dirty nitrogen after the re-heat of backflowing, makes to keep certain malleation in the ice chest, in order to avoid ambient atmosphere is invaded cold insulated cabinet and the cold insulated cabinet heat-insulating material is made moist, reduces heat insulation effect.
After 8 re-heats of described dirty nitrogen process main heat exchanger, a part enters into electric heater 5, as the regeneration gas of molecular sieve adsorber 4.Waste gas after the regeneration enters atmosphere after muffler 3 is handled.
The utility model has not only satisfied the elastic demand of user to product oxygen, and has saved user's one-time investment, has significantly reduced the oxygen production cost, for the user has created many incomes, has guided the value orientation in market.This air separation plant can satisfy 350Nm
3/ h, 550Nm
3/ h, 750Nm
3The demand of/h different operating operating mode makes each corollary equipment select the air compressor machine capacity according to the size of operating mode, thereby makes corollary equipment can adapt to 350Nm
3/ h to 750Nm
3The operating flexibility load of/h has been saved cost of investment and equipment energy consumption greatly.
The utility model still has multiple concrete embodiment, and all employings are equal to replacement or equivalent transformation and all technical schemes of forming, all drop within the claimed scope of the utility model.
Claims (7)
1. multi-state air separation plant, comprise by the interconnective air compressor of pipeline (1), precooling unit (2), molecular sieve adsorber (3) and fractionating column, described fractionating column is by charger-air cooler (7), main heat exchanger (8), following tower (9), condenser/evaporator (10), last tower (11), subcooler (12) is formed, air passes through air compressor (1) successively, precooling unit (2), molecular sieve adsorber (3), main heat exchanger enters rectifying column after (8), it is characterized in that: described rectifying column comprises the following tower (9) that is interconnected, last tower (11) and condenser/evaporator (10); Described tower (9) down is provided with the compressed-air actuated import (18) behind the purifying, and its bottom is the outlet (19) of oxygen-enriched liquid air, and the top is the import (20) of liquid nitrogen; Described bottom of going up tower (11) is the outlet (13) of oxygen, its middle part is the import (17) of oxygen-enriched liquid air, be connected with the outlet (19) of the oxygen-enriched liquid air of following tower (9), the top of last tower (11) is the outlet (15) of nitrogen, and the top of last tower (11) also is provided with the outlet (16) of dirty nitrogen; Described condenser/evaporator (10) is connected with the top of following tower, and the part nitrogen that is used for Jiang Xiata (9) is condensed into liquid nitrogen, the vaporization of liquid oxygen in the last tower; The pipeline of described connection oxygen outlet (13), nitrogen outlet (15), dirty nitrogen outlet (16) outputs to oxygen, nitrogen, dirty nitrogen outside the multi-state air separation plant after all passing main heat exchanger (8) respectively again.
2. multi-state air separation plant according to claim 1, it is characterized in that: after the pipeline of described connection nitrogen outlet (15), dirty nitrogen outlet (16) passes subcooler (12) earlier, again nitrogen, dirty nitrogen are outputed to outside the multi-state air separation plant after passing main heat exchanger (8) again.
3. multi-state air separation plant according to claim 2, it is characterized in that: after the pipeline of described dirty nitrogen outlet (16) passes subcooler (12) and main heat exchanger (8) earlier, passing charger-air cooler (7) back again outputs to dirty nitrogen outside the multi-state air separation plant, described charger-air cooler has increased one returning polluted nitrogen in (7), utilizes oxygen, nitrogen, three strands of gas charge air coolings simultaneously that backflow of dirty nitrogen when device start.
4. multi-state air separation plant according to claim 1 is characterized in that: the pipeline between the import (17) of the outlet (19) of the described oxygen-enriched liquid air of tower (9) down and the oxygen-enriched liquid air of last tower (11) passes subcooler (12).
5. multi-state air separation plant according to claim 1 is characterized in that: also include two booster expansion turbines (6), the air after this booster expansion turbine (6) expands is located by the expanded air import (14) that pipeline is transported to tower (11).
6. multi-state air separation plant according to claim 1 is characterized in that: described air compressor (1) has separate four.
7. multi-state air separation plant according to claim 1 is characterized in that: behind the pipeline process main heat exchanger (8) of the dirty nitrogen of described conveying, a part is connected on the electric heater (5).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200820185786U CN201377961Y (en) | 2008-09-09 | 2008-09-09 | Multi-operating mode air separation equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200820185786U CN201377961Y (en) | 2008-09-09 | 2008-09-09 | Multi-operating mode air separation equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201377961Y true CN201377961Y (en) | 2010-01-06 |
Family
ID=41518076
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200820185786U Expired - Lifetime CN201377961Y (en) | 2008-09-09 | 2008-09-09 | Multi-operating mode air separation equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201377961Y (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101806529A (en) * | 2010-03-12 | 2010-08-18 | 杭州杭氧股份有限公司 | Integrated main heat exchanger and subcooler |
| CN101929790A (en) * | 2010-08-19 | 2010-12-29 | 苏州制氧机有限责任公司 | High-purity nitrogen equipment |
| CN101929791A (en) * | 2010-08-19 | 2010-12-29 | 苏州制氧机有限责任公司 | Large-tonnage high-purity nitrogen equipment |
| CN102788476A (en) * | 2012-05-23 | 2012-11-21 | 苏州制氧机有限责任公司 | Air separation technology for mainly producing high-purity nitrogen and accessorily producing liquid oxygen by using cryogenic air separation device |
| CN106744697A (en) * | 2017-01-17 | 2017-05-31 | 孔祥旭 | A kind of super energy-conservation making oxygen by air separation device |
| CN107270655A (en) * | 2017-08-04 | 2017-10-20 | 杭州特盈能源技术发展有限公司 | A kind of single column nitrogen halfload operating mode volume increase liquid nitrogen device for making and method |
| CN108072235A (en) * | 2016-11-17 | 2018-05-25 | 北大方正集团有限公司 | Space division system |
| CN108240734A (en) * | 2018-03-08 | 2018-07-03 | 李佳晨 | Booster expansion machine air supply system and air separation plant |
| CN111773878A (en) * | 2020-06-29 | 2020-10-16 | 开封迪尔空分实业有限公司 | Air separation energy-saving control device and method |
| CN113606867A (en) * | 2021-08-14 | 2021-11-05 | 张家港市东南气体灌装有限公司 | Air separation device and method capable of realizing interchange of internal and external oxygen compression processes |
-
2008
- 2008-09-09 CN CN200820185786U patent/CN201377961Y/en not_active Expired - Lifetime
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101806529A (en) * | 2010-03-12 | 2010-08-18 | 杭州杭氧股份有限公司 | Integrated main heat exchanger and subcooler |
| CN101929790A (en) * | 2010-08-19 | 2010-12-29 | 苏州制氧机有限责任公司 | High-purity nitrogen equipment |
| CN101929791A (en) * | 2010-08-19 | 2010-12-29 | 苏州制氧机有限责任公司 | Large-tonnage high-purity nitrogen equipment |
| CN101929791B (en) * | 2010-08-19 | 2012-06-13 | 苏州制氧机有限责任公司 | Large-tonnage high-purity nitrogen equipment |
| CN102788476A (en) * | 2012-05-23 | 2012-11-21 | 苏州制氧机有限责任公司 | Air separation technology for mainly producing high-purity nitrogen and accessorily producing liquid oxygen by using cryogenic air separation device |
| CN102788476B (en) * | 2012-05-23 | 2014-08-06 | 苏州制氧机有限责任公司 | Air separation technology for mainly producing high-purity nitrogen and accessorily producing liquid oxygen by using cryogenic air separation device |
| CN108072235A (en) * | 2016-11-17 | 2018-05-25 | 北大方正集团有限公司 | Space division system |
| CN106744697A (en) * | 2017-01-17 | 2017-05-31 | 孔祥旭 | A kind of super energy-conservation making oxygen by air separation device |
| CN107270655A (en) * | 2017-08-04 | 2017-10-20 | 杭州特盈能源技术发展有限公司 | A kind of single column nitrogen halfload operating mode volume increase liquid nitrogen device for making and method |
| CN107270655B (en) * | 2017-08-04 | 2022-07-15 | 杭州特盈能源技术发展有限公司 | Single-tower nitrogen-making half-load working condition yield-increasing liquid nitrogen making device and method |
| CN108240734A (en) * | 2018-03-08 | 2018-07-03 | 李佳晨 | Booster expansion machine air supply system and air separation plant |
| CN108240734B (en) * | 2018-03-08 | 2024-03-26 | 李佳晨 | Air supply system of booster expander and air separation equipment |
| CN111773878A (en) * | 2020-06-29 | 2020-10-16 | 开封迪尔空分实业有限公司 | Air separation energy-saving control device and method |
| CN113606867A (en) * | 2021-08-14 | 2021-11-05 | 张家港市东南气体灌装有限公司 | Air separation device and method capable of realizing interchange of internal and external oxygen compression processes |
| CN113606867B (en) * | 2021-08-14 | 2022-12-02 | 张家港市东南气体灌装有限公司 | Air separation device and method capable of realizing interchange of internal and external oxygen compression processes |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| DD01 | Delivery of document by public notice |
Addressee: Suzhou oxygen generator, Limited by Share Ltd patent Manager Document name: Notification that Application Deemed not to be Proposed |
|
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: Wuzhong District Mudu town Suzhou city Jiangsu province 215101 Spring Road No. 31 Patentee after: SUZHOU OXYGEN PLANT CO., LTD. Address before: Wuzhong District Mudu town Suzhou city Jiangsu province 215101 Spring Road No. 31 Patentee before: Suzhou Oxygen Plant Co., Ltd. |
|
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20100106 |