CN103438733A - Primary heat-regeneration multi-flow heat exchange device for low-temperature liquid nitrogen - Google Patents
Primary heat-regeneration multi-flow heat exchange device for low-temperature liquid nitrogen Download PDFInfo
- Publication number
- CN103438733A CN103438733A CN2013103875759A CN201310387575A CN103438733A CN 103438733 A CN103438733 A CN 103438733A CN 2013103875759 A CN2013103875759 A CN 2013103875759A CN 201310387575 A CN201310387575 A CN 201310387575A CN 103438733 A CN103438733 A CN 103438733A
- Authority
- CN
- China
- Prior art keywords
- level
- outlet
- dirty nitrogen
- bobbin carriage
- synthesis gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Abstract
The invention belongs to the technical field of synthesis ammonia low-temperature liquid nitrogen processing equipment, and relates to the technology of a primary heat-regeneration multi-flow heat exchange device for low-temperature liquid nitrogen. Secondary refrigerating plant outlet -66.3 DEG C, 1.77MPaH2, -66.3 DEG C, 5.10MPaN2-H mixed gas and -66.3 DEG C, 0.13 MPaN2-Ar-CO-CH4 waste nitrogen cooling from 42 DEG C, 5.9MPaN2 to -63.3 DEG C, 5.8MPa in the low-temperature liquid nitrogen process are used, namely, secondary refrigerating plant outlet N2-H2 mixed gas, high-pressure H2, and waste nitrogen cooling capacity regenerative cooling incoming flow high pressure N2 are used for providing -63.3 DEG C nitrogen temperature conditions for a secondary refrigerating plant. Based on the multi-flow tube nest low-temperature heat exchange technology, spacer sleeves are used for controlling the distance between tube nests, and the side tube plate technology is used for achieving free contraction of tube bundles. The primary heat-regeneration multi-flow heat exchange device for the low-temperature liquid nitrogen is compact in structure, high in heat exchange efficiency and capable of being used in the field of 42 DEG C to -66.3 DEG C gas low-temperature multi-flow heat exchange, solves the technical problem of the primary refrigeration technology of the low-temperature liquid nitrogen, and improves the low-temperature heat-regeneration heat exchange efficiency of a low-temperature liquid nitrogen process system.
Description
Technical field
The present invention is mainly used in synthetic ammonia low-temperature liquid nitrogen process equipment technical field, relates to one-level backheat multiple flow heat exchange equipment technology for low temperature liquid nitrogen, two-stage system device for cooling outlet-66.3 ℃, 1.77MPa H in application of cold temperature liquid nitrogen technique
2,-66.3 ℃, 5.10MPa N
2-H
2mist and-66.3 ℃, 0.13MPa N
2-A
r-CO-CH
4cooling 42 ℃ of dirty nitrogen, 5.9MPa N
2to-63.3 ℃, 5.8MPa, apply the N of two-stage system device for cooling outlet
2-H
2synthesis gas, high pressure H
2and the cooling incoming flow high pressure of the cold backheat N of dirty nitrogen
2, temperature conditions is provided to the two-stage system device for cooling; It adopts thimble control tubulation spacing and side tube sheet technology to realize the multiple flow shell and tube low-temperature heat exchange technology of low temperature free shrink, compact conformation, heat exchange efficiency is high, can be used for 42 ℃～-66.3 ℃ gas band phase transformation low temperature multiple flow heat exchange fields, solve a low temperature liquid nitrogen one-level Refrigeration Technique difficult problem, improve the low temperature backheat heat exchange efficiency of low temperature liquid nitrogen process system.
Background technology
Main heat exchange equipment in synthetic ammonia low-temperature liquid nitrogen technique bag is Heat Exchangers, the main heat exchange technological process mainly comprises three phases, mainly the heat exchanger by three various heat exchange warm areas forms, wherein, first stage is that the high pressure nitrogen after compression is carried out to precooling, is about to 42 ℃ of high pressure nitrogens and is chilled in advance-63.3 ℃; Second stage is that high pressure nitrogen is cooled to-127.2 ℃ from-63.3 ℃, is that three sections refrigeration are prepared; Three phases is cooled to-188 ℃ by-127.2 ℃ of high pressure nitrogens and also liquefies and come-127.2 ℃ of purified gas to be cooled to-188.2 ℃ low-temp methanol technique.Three processes can adopt various heat exchange equipment.At first, low temperature liquid nitrogen is washed process system and is adopted the overall heat exchange mode mostly at present, three sections process of refrigerastions are connected to an integral body, the heat exchanger height can reach 60～80 meters, heat exchange efficiency is improved significantly, but it is too complicated that the problem existed is the heat-exchanging process flow process, the heat transmission equipment volume is too huge, bring serious inconvenience to processing and manufacturing, on-the-spot installation and transportation, and once the problem such as pipe leakage appears, and be difficult to detect, easily cause whole heat exchanger to scrap, the set technique equipment stops production, and the present invention solves LN from the three-segment type heat exchange equipment
2the precooling Liquefaction is started with, and emphasis solves the low-temperature heat exchange problem of one section refrigerating plant.Secondly, because adopting the whole tube sheet in two ends, common tubular heat exchanger connects the bundle of parallel tubes mode, vertical pipe self-constriction ability under worst cold case is poor, easily introducing pipe joint and tube sheet throws off, and because two ends adopt whole tube sheet, number of tubes is many, the general sub-thread that adopts flows heat exchange, be difficult for carrying out the multiple flow heat exchange, heat exchange efficiency is lower, volume is larger, the temperature difference is less, be difficult to carry out large temperature difference low-temperature heat exchange, the present invention adopts side multitube plate three tube bank type multiple flow shell and tube heat exchange equipments to carry out the intensive heat transfer process of multiple flow low temperature, by three femoral canal beam tube plate sides in the cylindrical shell side, adopt bending two ends, the pipe arrangement mode of intermediate vertical, can solve worst cold case next stage refrigeration multiple flow low-temperature heat exchange problem, reduce heat exchanger quantity, improve heat exchange efficiency.Finally, due to the heat exchanger structure that does not adopt upper and lower horizontal large tubesheet and Intermediate Gray deflection plate, between vertical pipe, distance can not be determined by tube sheet and deflection plate, and the form that adopts thimble is determined the vertical range of pipe interior, thimble plays the effect of pipeline spacing on the one hand, and one side plays baffling and increases the effect of turbulent-flow heat-exchanging.The present invention washes technology features and N according to low temperature liquid nitrogen
2one-level cryogenic refrigeration characteristics, adopt three grades separately independently Heat Exchangers as main heat transmission equipment, the segmentation independent cooling, emphasis is for the first order three tube bank type multiple flow heat-exchanging process flow processs, first order refrigeration process technology and the pipe type heat transfer equipment of research and development warm area between 42 ℃～-66.3 ℃, solve one-level high pressure N
2low temperature backheat precooling Key technique problem, the i.e. three heat exchange equipment technological process of tube bank multiple flow shell and tube and structure problems.
Summary of the invention
The present invention is mainly for one section 42 ℃～-63.3 ℃ low-temperature heat exchange problem of high pressure nitrogen, employing has four plumes three that volume is little, heat exchange efficiency is high, heat transfer temperature difference is large, have self-tightening contraction adjustment function and restrains tubular heat exchangers as main heat exchange equipment, applies-66.3 ℃, 1.77MPa H
2,-66.3 ℃, 5.10MPa N
2-H
2mist and-66.3 ℃, 0.13MPa N
2-A
r-CO-CH
4the technological process of dirty nitrogen backheat refrigeration, control high pressure nitrogen precooling temperature and pressure, improves heat exchange efficiency, solves high pressure nitrogen one grade low-temp backheat precooling problem, for synthetic ammonia low-temperature liquid nitrogen two-stage system device for cooling provides pre-cool condition.
Technical solution of the present invention:
One-level backheat multiple flow heat exchange equipment for low temperature liquid nitrogen, comprise one-level high pressure N
2suction flange (1), one-level N
2-H
2syngas outlet flange (2), one-level N
2-H
2syngas outlet is taken over (3), one-level N
2-H
2syngas outlet bobbin carriage (4), one-level N
2-H
2syngas outlet tube sheet (5), the dirty nitrogen outlet(discharge) flange (6) of one-level, the dirty nitrogen discharge connection (7) of one-level, the dirty nitrogen outlet of one-level bobbin carriage (8), the dirty nitrogen outlet of one-level tube sheet (9), the dirty nitrogen tube bank of one-level (10), one-level cylindrical shell (11), one-level lower support circle (12), the dirty nitrogen inlet bobbin carriage (13) of one-level, the dirty nitrogen inlet flange (14) of one-level, the dirty nitrogen inlet of one-level is taken over (15), the dirty nitrogen inlet tube sheet (16) of one-level, one-level low head (17), one-level skirt (18), one-level high pressure N
2outlet(discharge) flange (19), one-level high pressure N
2discharge connection (20), one-level N
2-H
2synthesis gas suction flange (21), one-level N
2-H
2synthesis gas entrance sleeve (22), one-level N
2-H
2synthesis gas import bobbin carriage (23), one-level N
2-H
2synthesis gas import tube sheet (24), one-level H
2suction flange (25), one-level H
2entrance sleeve (26), one-level H
2import bobbin carriage (27), one-level H
2import tube sheet (28), one-level pipeline (29), one-level cylinder spool (30), one-level upper support circle (31), one-level N
2-H
2synthesis gas tube bank (32), one-level H
2tube bank (33), one-level H
2outlet bobbin carriage (34), one-level H
2outlet(discharge) flange (35), one-level H
2discharge connection (36), one-level H
2outlet tube sheet (37), one-level upper cover (38), one-level high pressure N
2entrance sleeve (39) is characterized in that: the dirty nitrogen tube bank of one-level (10), one-level N
2-H
2synthesis gas tube bank (32), one-level H
2on all one-level pipelines (29) that tube bank (33) comprises, a plurality of hollow cylinder barrel shape one-level cylinder spools (30) are installed respectively at a certain distance, one-level cylinder spool (30) inner surface on same one-level pipeline (29) contacts with one-level pipeline (29) outer surface, one-level cylinder spool (30) outer surface one-level pipeline adjacent with other (29) outer surface contacts, and with upper other one-level cylinder spool (30) of adjacent one-level pipeline (29), keeps certain vertical range and is not in contact with one another, all one-level pipelines (29) are arranged according to equilateral triangle, and between one-level pipeline (29), vertical range is determined by one-level cylinder spool (30), and is the wall thickness of one-level cylinder spool (30), the dirty nitrogen tube bank of one-level (10), one-level N
2-H
2synthesis gas tube bank (32), one-level H
2export tube sheet (9), one-level N with the dirty nitrogen of corresponding one-level after all one-level pipelines (29) upper end bending that tube bank (33) comprises
2-H
2syngas outlet tube sheet (5), one-level H
2outlet tube sheet (37) connects, after the bending of lower end with the dirty nitrogen inlet tube sheet (16) of corresponding one-level, one-level N
2-H
2synthesis gas import tube sheet (24), one-level H
2import tube sheet (28) connects, one-level upper support circle (31) is fixed in one-level cylindrical shell (11) top, and one-level lower support circle (12) is fixed in one-level cylindrical shell (11) bottom, the dirty nitrogen tube bank of one-level (10), one-level N
2-H
2synthesis gas tube bank (32), one-level H
2in tube bank (33), the vertical component of band one-level cylinder spool (30) is installed between one-level upper support circle (31) and one-level lower support circle (12), one-level cylindrical shell (11) top is connected with one-level upper cover (38), and one-level high pressure N is installed at one-level upper cover (38) top
2entrance sleeve (39) and one-level high pressure N
2suction flange (1), one-level cylindrical shell (11) bottom is connected with one-level low head (17), and one-level high pressure N is installed at one-level low head (17) top
2discharge connection (20) and one-level high pressure N
2outlet(discharge) flange (19), one-level skirt (18) is installed in bottom, one-level cylindrical shell (11) upper left-hand is installed the dirty nitrogen outlet of one-level tube sheet (9), the dirty nitrogen outlet tube sheet of one-level (9) left side connects the dirty nitrogen outlet of one-level bobbin carriage (8), and the dirty nitrogen outlet of one-level bobbin carriage (8) top connects the dirty nitrogen discharge connection (7) of one-level and the dirty nitrogen outlet(discharge) flange (6) of one-level, one-level N is installed in the middle of one-level cylindrical shell (11) top
2-H
2syngas outlet tube sheet (5), one-level N
2-H
2syngas outlet tube sheet (5) front connects one-level N
2-H
2syngas outlet bobbin carriage (4), one-level N
2-H
2syngas outlet bobbin carriage (4) top connects one-level N
2-H
2syngas outlet is taken over (3) and one-level N
2-H
2syngas outlet flange (2), one-level cylindrical shell (11) upper right is installed one-level H
2outlet tube sheet (37), one-level H
2outlet tube sheet (37) right side connects one-level H
2outlet bobbin carriage (34), one-level H
2outlet bobbin carriage (34) top connects one-level H
2discharge connection (36) and one-level H
2outlet(discharge) flange (35), one-level cylindrical shell (11) lower left side is installed the dirty nitrogen inlet tube sheet (16) of one-level, the dirty nitrogen inlet tube sheet of one-level (16) left side connects the dirty nitrogen inlet bobbin carriage (13) of one-level, and the dirty nitrogen inlet bobbin carriage (13) of one-level top connects the dirty nitrogen inlet of one-level and takes over (15) and the dirty nitrogen inlet flange (14) of one-level, one-level N is installed in the middle of one-level cylindrical shell (11) bottom
2-H
2synthesis gas import tube sheet (24), one-level N
2-H
2synthesis gas import tube sheet (24) front connects one-level N
2-H
2synthesis gas import bobbin carriage (23), one-level N
2-H
2synthesis gas import bobbin carriage (23) top connects one-level N
2-H
2synthesis gas entrance sleeve (22) and one-level N
2-H
2synthesis gas suction flange (21), one-level H is installed on one-level cylindrical shell (11) right side, bottom
2import tube sheet (28), one-level H
2import tube sheet (28) right side connects one-level H
2import bobbin carriage (27), one-level H
2import bobbin carriage (27) top connects one-level H
2entrance sleeve (26) and one-level H
2suction flange (25).
H
2-66.3 ℃, enter one-level H during 1.77MPa
2import bobbin carriage (27), at one-level H
2the import bobbin carriage is allocated in one-level H in (27)
2tube bank (33) each arm, one-level H
2tube bank (33) is through one-level cylindrical shell (11), with in one-level cylindrical shell (11) by from one-level high pressure N
2the shell side high pressure N of entrance sleeve (39)
2heating, temperature is increased to 39 ℃, pressure decreased to 1.75MPa, then flow to one-level H
2outlet bobbin carriage (34), then through one-level H
2discharge connection (36) flows out the one-level refrigerating plant.
N
2-H
2synthesis gas-66.3 ℃, enter one-level N during 5.10MPa
2-H
2synthesis gas import bobbin carriage (23), at one-level N
2-H
2be allocated in one-level N in synthesis gas import bobbin carriage (23)
2-H
2synthesis gas tube bank (32) each arm, one-level N
2-H
2synthesis gas tube bank (32) is through one-level cylindrical shell (11), with in one-level cylindrical shell (11) by from one-level high pressure N
2the shell side high pressure N of entrance sleeve (39)
2heating, temperature is increased to 39 ℃, pressure decreased to 5.04MPa, then flow to one-level N
2-H
2syngas outlet bobbin carriage (4), then through one-level N
2-H
2syngas outlet is taken over (3) and is flowed out the one-level refrigerating plant.
N
2-A
r-CO-CH
4dirty nitrogen-66.3 ℃, enter the dirty nitrogen inlet bobbin carriage (13) of one-level during 0.13MPa, be allocated in the dirty nitrogen tube bank of one-level (10) each arm in the dirty nitrogen inlet bobbin carriage of one-level (13), the dirty nitrogen tube bank of one-level (10) is through one-level cylindrical shell (11), with in one-level cylindrical shell (11) by from one-level high pressure N
2the shell side high pressure N of entrance sleeve (39)
2heating, temperature is increased to 39 ℃, pressure decreased to 0.11MPa, then flow to the dirty nitrogen outlet of one-level bobbin carriage (8), then flows out the one-level refrigerating plant through the dirty nitrogen discharge connection of one-level (7).
High pressure N
242 ℃, during 5.9MPa through one-level high pressure N
2entrance sleeve (39) enters housing, by dirty nitrogen, one-level N in the dirty nitrogen tube bank of one-level (10)
2-H
2synthesis gas tube bank (32) interior synthesis gas, one-level H
2tube bank (33) interior hydrogen_cooling is to-63.3 ℃, 5.8MPa, through one-level high pressure N
2discharge connection (20) flows out into the two-stage system device for cooling.
The Principle Problems that scheme is related:
At first, traditional low temperature nitrogen liquefaction system adopts plate-fin overall heat exchange mode more, heat exchange efficiency is significantly improved than tandem type nitrogen liquefaction system, heat exchanger quantity is reduced, whole LNG Lquified Process Flow is simplified, and the refrigeration system of independent operating reduces, convenient management, but the problem existed makes LN after being the LNG Lquified Process Flow simplification
2main heat exchanger is bulky, the heat-exchanging process complexity, and processing and manufacturing, on-the-spot install and transport difficulty increases, once and the problem such as leakages occurs, be difficult to detect, easily cause whole heat exchanger to scrap, the stopping production of set technique equipment.For addressing this problem, the present invention is divided into 42 ℃～-63.3 ℃ ,-63.3 ℃～-127.2 ℃ by main heat exchanger inner high voltage nitrogen temperature change procedure,-127.2 ℃～-188.2 ℃ three ranks, adopt three independently heat exchangers, complete three temperature ranges heat transfer process from high to low, primary study exploitation 42 ℃～-63.3 ℃ nitrogen low-temperature heat exchange flow processs of the first order and first order heat exchanger general structure and heat-exchanging process parameter, and adopt multiple flow backheat refrigeration process, solve first order refrigeration heat transmission equipment problem.Research process is relatively independent, can be connected to become integral body with rear two-stage, consistent with integrated main heat exchanger heat exchange principle after connecting, and is convenient to transport and install after the main heat exchanger partition.Secondly, because adopting the whole tube sheet in two ends, common tubular heat exchanger connects the bundle of parallel tubes mode, vertical pipe self-constriction ability under worst cold case is poor, easily introducing pipe joint and tube sheet throws off, and because two ends adopt whole tube sheet, number of tubes is many, the general sub-thread that adopts flows heat exchange, be difficult for carrying out the multiple flow heat exchange, heat exchange efficiency is lower, volume is larger, the temperature difference is less, be difficult to carry out large temperature difference heat exchange, the present invention adopts side multitube plate four plume three tube bank type multiple flow shell and tube heat exchange equipments to carry out the intensive heat transfer process of multiple flow low temperature, by three femoral canal beam tube plate sides in the cylindrical shell side, adopt bending two ends, the pipe arrangement mode of intermediate vertical, can solve worst cold case next stage refrigeration multiple flow low-temperature heat exchange problem, reduce heat exchanger quantity, improve heat exchange efficiency.Finally, due to the heat exchanger structure that does not adopt upper and lower horizontal large tubesheet and Intermediate Gray deflection plate, between vertical pipe, distance can not be determined by tube sheet and deflection plate, and the form that adopts thimble is determined the vertical range of pipe interior, thimble plays the effect of pipeline spacing on the one hand, and one side plays baffling and increases the effect of turbulent-flow heat-exchanging.The wall thickness of thimble can be required according to heat exchange pipeline vertical range determine, and the dirty nitrogen tube bank of one-level (10), one-level N
2-H
2synthesis gas tube bank (32), one-level H
2on all one-level pipelines (29) that tube bank (33) comprises, a plurality of hollow cylinder barrel shape one-level cylinder spools (30) are installed respectively at a certain distance, one-level cylinder spool (30) inner surface on same one-level pipeline (29) contacts with one-level pipeline (29) outer surface, one-level cylinder spool (30) outer surface one-level pipeline adjacent with other (29) outer surface contacts, keep certain vertical range and be not in contact with one another with upper other one-level cylinder spool (30) of adjacent one-level pipeline (29), to reach, air-flow passes through and the purpose of baffling heat exchange.All one-level pipelines (29) are arranged according to equilateral triangle, and to be suitable for the equidistant spread configuration of circular pipe, between one-level pipeline (29), vertical range is determined by one-level cylinder spool (30), and is the wall thickness of one-level cylinder spool (30).The dirty nitrogen tube bank of one-level (10), one-level N
2-H
2synthesis gas tube bank (32), one-level H
2export tube sheet (9), one-level N with the dirty nitrogen of corresponding one-level after all one-level pipelines (29) upper end bending that tube bank (33) comprises
2-H
2syngas outlet tube sheet (5), one-level H
2outlet tube sheet (37) connects, after the bending of lower end with the dirty nitrogen inlet tube sheet (16) of corresponding one-level, one-level N
2-H
2synthesis gas import tube sheet (24), one-level H
2import tube sheet (28) connects, and adopts bending two ends to connect tube sheet, can make pipeline free shrink under worst cold case, and can not pull with tube sheet.The dirty nitrogen tube bank of one-level (10), one-level N
2-H
2synthesis gas tube bank (32), one-level H
2in tube bank (33), vertical component of band one-level cylinder spools (30) is installed between one-level upper support circle (31) and one-level lower support circle (12), mainly plays and controls and bundle the vertical component pipeline and be difficult for scattering, and prevents from that pipeline from becoming flexible to act on.Apply three tube bank multitube plate the side mount type tubular heat exchangers of three strands of cooling one incoming flows of backheat cold flow, can complete multiple flow heat transfer process under the high pressure low temperature operating mode.
Technical characterstic of the present invention:
The present invention is mainly for one-level backheat multiple flow heat exchange equipment for low temperature liquid nitrogen, employing has that volume is little, heat exchange efficiency is high, heat transfer temperature difference is large, have self-tightening shrinks the four plumes three tube bank shell and tube heat exchange equipments of adjusting function, the application-66.3 of two-stage system device for cooling outlet ℃ in application of cold temperature liquid nitrogen technique, 1.77MPa H
2,-66.3 ℃, 5.10MPa N
2-H
2mist and-66.3 ℃, 0.13MPa N
2-A
r-CO-CH
4cooling 42 ℃ of dirty nitrogen, 5.9MPa N
2to-63.3 ℃, 5.8MPa, apply the N of two-stage system device for cooling outlet
2-H
2synthesis gas, high pressure H
2and the cooling incoming flow high pressure of the cold backheat N of dirty nitrogen
2, temperature conditions is provided to the two-stage system device for cooling.The present invention adopts side multitube plate three tube bank type multiple flow shell and tube heat exchange equipments to carry out the intensive heat transfer process of multiple flow low temperature, by three femoral canal beam tube plate sides in the cylindrical shell side, adopt bending two ends, the pipe arrangement mode of intermediate vertical, can solve low temperature nitrogen one-level refrigeration multiple flow low temperature backheat heat transfer problem, reduce heat exchanger quantity, improve heat exchange efficiency, but guarantee heat exchanger tube free shrink under worst cold case, can not pull tube sheet.The present invention adopts the form of thimble to determine the vertical range of pipe interior, can be according to shell side heat exchanging fluid parameter, adjust flexibly the vertical tube spacing by adjusting the thimble wall thickness, and play baffling simultaneously and increase the effect of turbulent-flow heat-exchanging.The present invention adopts the mode of bending two ends connecting pipe and sleeve pipe spacing, can make pipeline free shrink under worst cold case, and can not pull tube sheet, has the advantages that to bear large temperature difference low-temperature heat exchange.
The accompanying drawing explanation
Figure 1 shows that critical piece structure and the position relationship of low temperature liquid nitrogen with one-level backheat multiple flow heat exchange equipment.
Figure 2 shows that vertical pipe and the sleeve arrangement top view of low temperature liquid nitrogen with one-level backheat multiple flow heat exchange equipment.
Figure 3 shows that vertical pipe and the sleeve arrangement front view of low temperature liquid nitrogen with one-level backheat multiple flow heat exchange equipment.
The specific embodiment
One-level backheat multiple flow heat exchange equipment for the processing and manufacturing low temperature liquid nitrogen, comprise one-level high pressure N
2suction flange (1), one-level N
2-H
2syngas outlet flange (2), one-level N
2-H
2syngas outlet is taken over (3), one-level N
2-H
2syngas outlet bobbin carriage (4), one-level N
2-H
2syngas outlet tube sheet (5), the dirty nitrogen outlet(discharge) flange (6) of one-level, the dirty nitrogen discharge connection (7) of one-level, the dirty nitrogen outlet of one-level bobbin carriage (8), the dirty nitrogen outlet of one-level tube sheet (9), the dirty nitrogen tube bank of one-level (10), one-level cylindrical shell (11), one-level lower support circle (12), the dirty nitrogen inlet bobbin carriage (13) of one-level, the dirty nitrogen inlet flange (14) of one-level, the dirty nitrogen inlet of one-level is taken over (15), the dirty nitrogen inlet tube sheet (16) of one-level, one-level low head (17), one-level skirt (18), one-level high pressure N
2outlet(discharge) flange (19), one-level high pressure N
2discharge connection (20), one-level N
2-H
2synthesis gas suction flange (21), one-level N
2-H
2synthesis gas entrance sleeve (22), one-level N
2-H
2synthesis gas import bobbin carriage (23), one-level N
2-H
2synthesis gas import tube sheet (24), one-level H
2suction flange (25), one-level H
2entrance sleeve (26), one-level H
2import bobbin carriage (27), one-level H
2import tube sheet (28), one-level pipeline (29), one-level cylinder spool (30), one-level upper support circle (31), one-level N
2-H
2synthesis gas tube bank (32), one-level H
2tube bank (33), one-level H
2outlet bobbin carriage (34), one-level H
2outlet(discharge) flange (35), one-level H
2discharge connection (36), one-level H
2outlet tube sheet (37), one-level upper cover (38), one-level high pressure N
2entrance sleeve (39), and make each parts keep following annexation: the dirty nitrogen tube bank of one-level (10), one-level N
2-H
2synthesis gas tube bank (32), one-level H
2on all one-level pipelines (29) that tube bank (33) comprises, a plurality of hollow cylinder barrel shape one-level cylinder spools (30) are installed respectively at a certain distance, one-level cylinder spool (30) inner surface on same one-level pipeline (29) contacts with one-level pipeline (29) outer surface, one-level cylinder spool (30) outer surface one-level pipeline adjacent with other (29) outer surface contacts, and with upper other one-level cylinder spool (30) of adjacent one-level pipeline (29), keeps certain vertical range and is not in contact with one another, all one-level pipelines (29) are arranged according to equilateral triangle, and between one-level pipeline (29), vertical range is determined by one-level cylinder spool (30), and is the wall thickness of one-level cylinder spool (30), the dirty nitrogen tube bank of one-level (10), one-level N
2-H
2synthesis gas tube bank (32), one-level H
2export tube sheet (9), one-level N with the dirty nitrogen of corresponding one-level after all one-level pipelines (29) upper end bending that tube bank (33) comprises
2-H
2syngas outlet tube sheet (5), one-level H
2outlet tube sheet (37) connects, after the bending of lower end with the dirty nitrogen inlet tube sheet (16) of corresponding one-level, one-level N
2-H
2synthesis gas import tube sheet (24), one-level H
2import tube sheet (28) connects, one-level upper support circle (31) is fixed in one-level cylindrical shell (11) top, and one-level lower support circle (12) is fixed in one-level cylindrical shell (11) bottom, the dirty nitrogen tube bank of one-level (10), one-level N
2-H
2synthesis gas tube bank (32), one-level H
2in tube bank (33), the vertical component of band one-level cylinder spool (30) is installed between one-level upper support circle (31) and one-level lower support circle (12), one-level cylindrical shell (11) top is connected with one-level upper cover (38), and one-level high pressure N is installed at one-level upper cover (38) top
2entrance sleeve (39) and one-level high pressure N
2suction flange (1), one-level cylindrical shell (11) bottom is connected with one-level low head (17), and one-level high pressure N is installed at one-level low head (17) top
2discharge connection (20) and one-level high pressure N
2outlet(discharge) flange (19), one-level skirt (18) is installed in bottom, one-level cylindrical shell (11) upper left-hand is installed the dirty nitrogen outlet of one-level tube sheet (9), the dirty nitrogen outlet tube sheet of one-level (9) left side connects the dirty nitrogen outlet of one-level bobbin carriage (8), and the dirty nitrogen outlet of one-level bobbin carriage (8) top connects the dirty nitrogen discharge connection (7) of one-level and the dirty nitrogen outlet(discharge) flange (6) of one-level, one-level N is installed in the middle of one-level cylindrical shell (11) top
2-H
2syngas outlet tube sheet (5), one-level N
2-H
2syngas outlet tube sheet (5) front connects one-level N
2-H
2syngas outlet bobbin carriage (4), one-level N
2-H
2syngas outlet bobbin carriage (4) top connects one-level N
2-H
2syngas outlet is taken over (3) and one-level N
2-H
2syngas outlet flange (2), one-level cylindrical shell (11) upper right is installed one-level H
2outlet tube sheet (37), one-level H
2outlet tube sheet (37) right side connects one-level H
2outlet bobbin carriage (34), one-level H
2outlet bobbin carriage (34) top connects one-level H
2discharge connection (36) and one-level H
2outlet(discharge) flange (35), one-level cylindrical shell (11) lower left side is installed the dirty nitrogen inlet tube sheet (16) of one-level, the dirty nitrogen inlet tube sheet of one-level (16) left side connects the dirty nitrogen inlet bobbin carriage (13) of one-level, and the dirty nitrogen inlet bobbin carriage (13) of one-level top connects the dirty nitrogen inlet of one-level and takes over (15) and the dirty nitrogen inlet flange (14) of one-level, one-level N is installed in the middle of one-level cylindrical shell (11) bottom
2-H
2synthesis gas import tube sheet (24), one-level N
2-H
2synthesis gas import tube sheet (24) front connects one-level N
2-H
2synthesis gas import bobbin carriage (23), one-level N
2-H
2synthesis gas import bobbin carriage (23) top connects one-level N
2-H
2synthesis gas entrance sleeve (22) and one-level N
2-H
2synthesis gas suction flange (21), one-level H is installed on one-level cylindrical shell (11) right side, bottom
2import tube sheet (28), one-level H
2import tube sheet (28) right side connects one-level H
2import bobbin carriage (27), one-level H
2import bobbin carriage (27) top connects one-level H
2entrance sleeve (26) and one-level H
2suction flange (25).
By H
2-66.3 ℃, squeeze into one-level H during 1.77MPa
2import bobbin carriage (27), at one-level H
2the import bobbin carriage is allocated in one-level H in (27)
2tube bank (33) each arm, one-level H
2tube bank (33) is through one-level cylindrical shell (11), with in one-level cylindrical shell (11) by from one-level high pressure N
2the shell side high pressure N of entrance sleeve (39)
2heating, temperature is increased to 39 ℃, pressure decreased to 1.75MPa, then flow to one-level H
2outlet bobbin carriage (34), then through one-level H
2discharge connection (36) flows out the one-level refrigerating plant.
By N
2-H
2synthesis gas-66.3 ℃, squeeze into one-level N during 5.10MPa
2-H
2synthesis gas import bobbin carriage (23), at one-level N
2-H
2be allocated in one-level N in synthesis gas import bobbin carriage (23)
2-H
2synthesis gas tube bank (32) each arm, one-level N
2-H
2synthesis gas tube bank (32) is through one-level cylindrical shell (11), with in one-level cylindrical shell (11) by from one-level high pressure N
2the shell side high pressure N of entrance sleeve (39)
2heating, temperature is increased to 39 ℃, pressure decreased to 5.04MPa, then flow to one-level N
2-H
2syngas outlet bobbin carriage (4), then through one-level N
2-H
2syngas outlet is taken over (3) and is flowed out the one-level refrigerating plant.
By N
2-A
r-CO-CH
4dirty nitrogen-66.3 ℃, squeeze into the dirty nitrogen inlet bobbin carriage (13) of one-level during 0.13MPa, be allocated in the dirty nitrogen tube bank of one-level (10) each arm in the dirty nitrogen inlet bobbin carriage of one-level (13), the dirty nitrogen tube bank of one-level (10) is through one-level cylindrical shell (11), with in one-level cylindrical shell (11) by from one-level high pressure N
2the shell side high pressure N of entrance sleeve (39)
2heating, temperature is increased to 39 ℃, pressure decreased to 0.11MPa, then flow to the dirty nitrogen outlet of one-level bobbin carriage (8), then flows out the one-level refrigerating plant through the dirty nitrogen discharge connection of one-level (7).
By high pressure N
242 ℃, during 5.9MPa through one-level high pressure N
2entrance sleeve (39) is squeezed into housing, and by dirty nitrogen, one-level N in the dirty nitrogen tube bank of one-level (10)
2-H
2synthesis gas tube bank (32) interior synthesis gas, one-level H
2tube bank (33) interior hydrogen_cooling is to-63.3 ℃, 5.8MPa, through one-level high pressure N
2discharge connection (20) flows out into the two-stage system device for cooling.
Claims (5)
1. one-level backheat multiple flow heat exchange equipment for low temperature liquid nitrogen, comprise one-level high pressure N
2suction flange (1), one-level N
2-H
2syngas outlet flange (2), one-level N
2-H
2syngas outlet is taken over (3), one-level N
2-H
2syngas outlet bobbin carriage (4), one-level N
2-H
2syngas outlet tube sheet (5), the dirty nitrogen outlet(discharge) flange (6) of one-level, the dirty nitrogen discharge connection (7) of one-level, the dirty nitrogen outlet of one-level bobbin carriage (8), the dirty nitrogen outlet of one-level tube sheet (9), the dirty nitrogen tube bank of one-level (10), one-level cylindrical shell (11), one-level lower support circle (12), the dirty nitrogen inlet bobbin carriage (13) of one-level, the dirty nitrogen inlet flange (14) of one-level, the dirty nitrogen inlet of one-level is taken over (15), the dirty nitrogen inlet tube sheet (16) of one-level, one-level low head (17), one-level skirt (18), one-level high pressure N
2outlet(discharge) flange (19), one-level high pressure N
2discharge connection (20), one-level N
2-H
2synthesis gas suction flange (21), one-level N
2-H
2synthesis gas entrance sleeve (22), one-level N
2-H
2synthesis gas import bobbin carriage (23), one-level N
2-H
2synthesis gas import tube sheet (24), one-level H
2suction flange (25), one-level H
2entrance sleeve (26), one-level H
2import bobbin carriage (27), one-level H
2import tube sheet (28), one-level pipeline (29), one-level cylinder spool (30), one-level upper support circle (31), one-level N
2-H
2synthesis gas tube bank (32), one-level H
2tube bank (33), one-level H
2outlet bobbin carriage (34), one-level H
2outlet(discharge) flange (35), one-level H
2discharge connection (36), one-level H
2outlet tube sheet (37), one-level upper cover (38), one-level high pressure N
2entrance sleeve (39) is characterized in that: the dirty nitrogen tube bank of one-level (10), one-level N
2-H
2synthesis gas tube bank (32), one-level H
2on all one-level pipelines (29) that tube bank (33) comprises, a plurality of hollow cylinder barrel shape one-level cylinder spools (30) are installed respectively at a certain distance, one-level cylinder spool (30) inner surface on same one-level pipeline (29) contacts with one-level pipeline (29) outer surface, one-level cylinder spool (30) outer surface one-level pipeline adjacent with other (29) outer surface contacts, and with upper other one-level cylinder spool (30) of adjacent one-level pipeline (29), keeps certain vertical range and is not in contact with one another, all one-level pipelines (29) are arranged according to equilateral triangle, and between one-level pipeline (29), vertical range is determined by one-level cylinder spool (30), and is the wall thickness of one-level cylinder spool (30), the dirty nitrogen tube bank of one-level (10), one-level N
2-H
2synthesis gas tube bank (32), one-level H
2export tube sheet (9), one-level N with the dirty nitrogen of corresponding one-level after all one-level pipelines (29) upper end bending that tube bank (33) comprises
2-H
2syngas outlet tube sheet (5), one-level H
2outlet tube sheet (37) connects, after the bending of lower end with the dirty nitrogen inlet tube sheet (16) of corresponding one-level, one-level N
2-H
2synthesis gas import tube sheet (24), one-level H
2import tube sheet (28) connects, one-level upper support circle (31) is fixed in one-level cylindrical shell (11) top, and one-level lower support circle (12) is fixed in one-level cylindrical shell (11) bottom, the dirty nitrogen tube bank of one-level (10), one-level N
2-H
2synthesis gas tube bank (32), one-level H
2in tube bank (33), the vertical component of band one-level cylinder spool (30) is installed between one-level upper support circle (31) and one-level lower support circle (12), one-level cylindrical shell (11) top is connected with one-level upper cover (38), and one-level high pressure N is installed at one-level upper cover (38) top
2entrance sleeve (39) and one-level high pressure N
2suction flange (1), one-level cylindrical shell (11) bottom is connected with one-level low head (17), and one-level high pressure N is installed at one-level low head (17) top
2discharge connection (20) and one-level high pressure N
2outlet(discharge) flange (19), one-level skirt (18) is installed in bottom, one-level cylindrical shell (11) upper left-hand is installed the dirty nitrogen outlet of one-level tube sheet (9), the dirty nitrogen outlet tube sheet of one-level (9) left side connects the dirty nitrogen outlet of one-level bobbin carriage (8), and the dirty nitrogen outlet of one-level bobbin carriage (8) top connects the dirty nitrogen discharge connection (7) of one-level and the dirty nitrogen outlet(discharge) flange (6) of one-level, one-level N is installed in the middle of one-level cylindrical shell (11) top
2-H
2syngas outlet tube sheet (5), one-level N
2-H
2syngas outlet tube sheet (5) front connects one-level N
2-H
2syngas outlet bobbin carriage (4), one-level N
2-H
2syngas outlet bobbin carriage (4) top connects one-level N
2-H
2syngas outlet is taken over (3) and one-level N
2-H
2syngas outlet flange (2), one-level cylindrical shell (11) upper right is installed one-level H
2outlet tube sheet (37), one-level H
2outlet tube sheet (37) right side connects one-level H
2outlet bobbin carriage (34), one-level H
2outlet bobbin carriage (34) top connects one-level H
2discharge connection (36) and one-level H
2outlet(discharge) flange (35), one-level cylindrical shell (11) lower left side is installed the dirty nitrogen inlet tube sheet (16) of one-level, the dirty nitrogen inlet tube sheet of one-level (16) left side connects the dirty nitrogen inlet bobbin carriage (13) of one-level, and the dirty nitrogen inlet bobbin carriage (13) of one-level top connects the dirty nitrogen inlet of one-level and takes over (15) and the dirty nitrogen inlet flange (14) of one-level, one-level N is installed in the middle of one-level cylindrical shell (11) bottom
2-H
2synthesis gas import tube sheet (24), one-level N
2-H
2synthesis gas import tube sheet (24) front connects one-level N
2-H
2synthesis gas import bobbin carriage (23), one-level N
2-H
2synthesis gas import bobbin carriage (23) top connects one-level N
2-H
2synthesis gas entrance sleeve (22) and one-level N
2-H
2synthesis gas suction flange (21), one-level H is installed on one-level cylindrical shell (11) right side, bottom
2import tube sheet (28), one-level H
2import tube sheet (28) right side connects one-level H
2import bobbin carriage (27), one-level H
2import bobbin carriage (27) top connects one-level H
2entrance sleeve (26) and one-level H
2suction flange (25).
2. according to claim
1one-level backheat multiple flow heat exchange equipment for described low temperature liquid nitrogen, is characterized in that: H
2-66.3 ℃, enter one-level H during 1.77MPa
2import bobbin carriage (27), at one-level H
2the import bobbin carriage is allocated in one-level H in (27)
2tube bank (33) each arm, one-level H
2tube bank (33) is through one-level cylindrical shell (11), with in one-level cylindrical shell (11) by from one-level high pressure N
2the shell side high pressure N of entrance sleeve (39)
2heating, temperature is increased to 39 ℃, pressure decreased to 1.75MPa, then flow to one-level H
2outlet bobbin carriage (34), then through one-level H
2discharge connection (36) flows out the one-level refrigerating plant.
3. according to claim
1one-level backheat multiple flow heat exchange equipment for described low temperature liquid nitrogen, is characterized in that: N
2-H
2synthesis gas-66.3 ℃, enter one-level N during 5.10MPa
2-H
2synthesis gas import bobbin carriage (23), at one-level N
2-H
2be allocated in one-level N in synthesis gas import bobbin carriage (23)
2-H
2synthesis gas tube bank (32) each arm, one-level N
2-H
2synthesis gas tube bank (32) is through one-level cylindrical shell (11), with in one-level cylindrical shell (11) by from one-level high pressure N
2the shell side high pressure N of entrance sleeve (39)
2heating, temperature is increased to 39 ℃, pressure decreased to 5.04MPa, then flow to one-level N
2-H
2syngas outlet bobbin carriage (4), then through one-level N
2-H
2syngas outlet is taken over (3) and is flowed out the one-level refrigerating plant.
4. according to claim
1one-level backheat multiple flow heat exchange equipment for described low temperature liquid nitrogen, is characterized in that: N
2-A
r-CO-CH
4dirty nitrogen-66.3 ℃, enter the dirty nitrogen inlet bobbin carriage (13) of one-level during 0.13MPa, be allocated in the dirty nitrogen tube bank of one-level (10) each arm in the dirty nitrogen inlet bobbin carriage of one-level (13), the dirty nitrogen tube bank of one-level (10) is through one-level cylindrical shell (11), with in one-level cylindrical shell (11) by from one-level high pressure N
2the shell side high pressure N of entrance sleeve (39)
2heating, temperature is increased to 39 ℃, pressure decreased to 0.11MPa, then flow to the dirty nitrogen outlet of one-level bobbin carriage (8), then flows out the one-level refrigerating plant through the dirty nitrogen discharge connection of one-level (7).
5. according to claim
1one-level backheat multiple flow heat exchange equipment for described low temperature liquid nitrogen, is characterized in that: high pressure N
242 ℃, during 5.9MPa through one-level high pressure N
2entrance sleeve (39) enters housing, by dirty nitrogen, one-level N in the dirty nitrogen tube bank of one-level (10)
2-H
2synthesis gas tube bank (32) interior synthesis gas, one-level H
2tube bank (33) interior hydrogen_cooling is to-63.3 ℃, 5.8MPa, through one-level high pressure N
2discharge connection (20) flows out into the two-stage system device for cooling.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310387575.9A CN103438733B (en) | 2013-08-31 | 2013-08-31 | Primary heat-regeneration multi-flow heat exchange device for low-temperature liquid nitrogen |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310387575.9A CN103438733B (en) | 2013-08-31 | 2013-08-31 | Primary heat-regeneration multi-flow heat exchange device for low-temperature liquid nitrogen |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103438733A true CN103438733A (en) | 2013-12-11 |
| CN103438733B CN103438733B (en) | 2015-07-01 |
Family
ID=49692430
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310387575.9A Expired - Fee Related CN103438733B (en) | 2013-08-31 | 2013-08-31 | Primary heat-regeneration multi-flow heat exchange device for low-temperature liquid nitrogen |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103438733B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107055570A (en) * | 2017-03-21 | 2017-08-18 | 武汉金中石化工程有限公司 | Low-pressure synthetic ammonia equipment and low-pressure synthetic ammonia method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6076597A (en) * | 1997-12-31 | 2000-06-20 | Flowserve Management Company | Helical coil heat exchanger with removable end plates |
| US20030217565A1 (en) * | 2000-06-28 | 2003-11-27 | Kevin Flynn | Liquid chiller evaporator |
| CN102455113A (en) * | 2011-11-25 | 2012-05-16 | 张周卫 | Liquefied natural gas (LNG) low-temperature liquefied primary refrigerating four-stream spiral twined pipe type heat exchange equipment |
| CN102455139A (en) * | 2011-10-18 | 2012-05-16 | 张周卫 | Double-strand-flow low-temperature spiral winding pipe type heat exchanger with vacuum heat insulation function |
| CN102538388A (en) * | 2011-11-24 | 2012-07-04 | 张周卫 | Three-stream spiral wound type heat exchange equipment for secondary refrigeration and low-temperature liquefaction of LNG (liquefied natural gas) |
-
2013
- 2013-08-31 CN CN201310387575.9A patent/CN103438733B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6076597A (en) * | 1997-12-31 | 2000-06-20 | Flowserve Management Company | Helical coil heat exchanger with removable end plates |
| US20030217565A1 (en) * | 2000-06-28 | 2003-11-27 | Kevin Flynn | Liquid chiller evaporator |
| CN102455139A (en) * | 2011-10-18 | 2012-05-16 | 张周卫 | Double-strand-flow low-temperature spiral winding pipe type heat exchanger with vacuum heat insulation function |
| CN102538388A (en) * | 2011-11-24 | 2012-07-04 | 张周卫 | Three-stream spiral wound type heat exchange equipment for secondary refrigeration and low-temperature liquefaction of LNG (liquefied natural gas) |
| CN102455113A (en) * | 2011-11-25 | 2012-05-16 | 张周卫 | Liquefied natural gas (LNG) low-temperature liquefied primary refrigerating four-stream spiral twined pipe type heat exchange equipment |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107055570A (en) * | 2017-03-21 | 2017-08-18 | 武汉金中石化工程有限公司 | Low-pressure synthetic ammonia equipment and low-pressure synthetic ammonia method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103438733B (en) | 2015-07-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102538387A (en) | Liquefied natural gas (LNG) low temperature liquefied three-level refrigeration spiral wound tube type heat exchanger | |
| CN102538388B (en) | Three-stream spiral wound type heat exchange equipment for secondary refrigeration and low-temperature liquefaction of LNG (liquefied natural gas) | |
| CN104896971B (en) | Spiral tubular heat exchanger for reducing tube winding | |
| WO2013071789A1 (en) | Device and method for liquefying natural gas using single mixed working medium as refrigeration medium | |
| CN103017573B (en) | Low-temperature spiral wound heat exchanger for non-converted gas cooler | |
| CN103245226A (en) | Small liquefied natural gas vaporizer | |
| CN113983760A (en) | Helium ultra-low temperature purification and liquefaction system | |
| CN102564056B (en) | Multi-flow spiral winding tube type main heat exchange equipment with mixed refrigerant for low-temperature liquefaction of LNG (liquefied natural gas) | |
| CN103063057B (en) | Feed gas chiller three plume low temperature wrap-round tubular heat exchangers | |
| CN103033074B (en) | Low-temperature wound-tube heat exchanger used for converted gas cooler | |
| CN103438667B (en) | Low temperature liquid nitrogen three grades of backheat multiple flows are wound around pipe type heat transfer equipment | |
| CN103438733B (en) | Primary heat-regeneration multi-flow heat exchange device for low-temperature liquid nitrogen | |
| CN102455113B (en) | Liquefied natural gas (LNG) low-temperature liquefied primary refrigerating four-stream spiral twined pipe type heat exchange equipment | |
| CN103438666B (en) | Multi-strand winding pipe type main back heating and heat exchange device for low-temperature liquid nitrogen | |
| CN106123484A (en) | Cold three stream plate-fin heat exchanger of LNG low-temperature liquefaction three tier structure | |
| CN103438736B (en) | Two-stage back heating multi-strand winding pipe type heat exchange device for low-temperature liquid nitrogen | |
| CN210425762U (en) | Synthetic ammonia compression system | |
| CN211977383U (en) | Helium liquefying and helium cold source supply device with different temperature grades | |
| CN104215098A (en) | Heat exchanger for polypropylene chemical process | |
| CN115854651B (en) | Hydrogen liquefaction method and device for precooling by utilizing refrigerator | |
| CN115371355B (en) | Natural gas liquefaction system and method suitable for standard modularization | |
| CN215672383U (en) | Liquid air energy storage power generation system | |
| CN114719559B (en) | Cold box separation system and method for preparing isobutene by isobutane dehydrogenation of Olefex process | |
| CN216868943U (en) | Hydrogen liquefaction device | |
| CN216205595U (en) | Cryogenic treatment equipment for cold energy recovery |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150701 Termination date: 20160831 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |