KR20140120329A - Method for providing a purified crude gaseous c4 fraction as an input stream for an extractive distillation using a selective solvent - Google Patents
Method for providing a purified crude gaseous c4 fraction as an input stream for an extractive distillation using a selective solvent Download PDFInfo
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- KR20140120329A KR20140120329A KR1020147021970A KR20147021970A KR20140120329A KR 20140120329 A KR20140120329 A KR 20140120329A KR 1020147021970 A KR1020147021970 A KR 1020147021970A KR 20147021970 A KR20147021970 A KR 20147021970A KR 20140120329 A KR20140120329 A KR 20140120329A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/28—Recovery of used solvent
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
- C10G21/12—Organic compounds only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/12—Liquefied petroleum gas
Abstract
The present invention relates to a process for the production of C 3 hydrocarbons, C 4 oligomers, C 4 A selective solvent is used to obtain crude 1,3-butadiene based on liquid C 4 -fraction (1) as a feed stream containing the polymer and C 5 + hydrocarbons together with butane, butene and 1,3-butadiene (2) as crude stream C 4 fraction (2) as an input stream for extractive distillation. The method comprises the steps of 1) purifying the crude phase C 4 The C 4 oligomer, C 4 oligomer, Separating the polymer and the C 5 + hydrocarbons, and 2) has a step of evaporation of the liquid crude C 4 fraction in an evaporator tank (VK). The invention is characterized in that the evaporation tank (VK) is associated with a stripping column (K) having one or more separation stages and the liquid C 4 fraction (1) is fed to the top of the stripping column. The stripping column directly exchanges the gas and liquid from the bottom of the column with the vaporizer tank (VK), and the purified crude vapor phase C 4 fraction (2) is withdrawn from the top of the stripping column. The stripping column (K) runs on the column head without a condenser.
Description
The present invention relates to a process for providing a gas phase purified crude C 4 cut as a feed stream for extractive distillation using a selective solvent.
The term "C 4 fraction" refers to a mixture of hydrocarbons predominantly having four carbon atoms per molecule. The C 4 fraction can be recovered, for example, from ethylene oxide and / or propylene by thermal decomposition in petroleum oils, such as liquefied petroleum gas, light gasoline or gas oils, typically steam crackers, in particular naphtha crackers or FCC (fluid catalyzed cracking) ≪ / RTI > The C 4 fraction is also obtained in catalytic dehydrogenation of n-butane and / or n-butene. The C 4 fraction generally comprises butane, butene, 1,3-butadiene, minor amounts of C 3 - and C 4 -acetylene, 1,2-butadiene and C 5 + hydrocarbons.
The separation of the C 4 fraction is a complicated distillation problem because the relative volatilities of the components have small differences. Therefore, the separation is carried out by distillation, referred to as extractive distillation, that is to say by addition of a selective solvent (also referred to as an extractant), which has a higher boiling point than the mixture to be separated and the relative volatility of the components to be separated Increase the difference.
Many methods of separating the C 4 fraction by extractive distillation using selective solvents are known. They flow countercurrently to the liquid selective solvent in the form of vapor in the C 4 fraction which is to be separated under suitable thermodynamic conditions, usually at low temperatures, usually in the range of 20 to 80 ° C and at mild pressure, often standard pressure to 6 bar, As a result, while the components from the C 4 fraction with higher affinity are loaded into the selective solvent, the components with lower affinity for the selective solvent remain in the vapor phase and have a common characteristic that they are taken off as the overhead stream. Subsequently, in one or more further processing steps, the components in the selective solvent are removed from the solvent stream loaded by suitable thermodynamic conditions, i.e., by fractional distillation at higher temperatures and / or lower pressures as compared to the first processing step.
The crude C 4 fraction contains impurities which cause problems in extractive distillation, more specifically solvent droplet formation and device fouling, and therefore to ensure reliable operation of the extractive distillation, they are particularly advantageous in that the crude C 4 fraction is subjected to extraction distillation Must be removed before being supplied.
Among these, C 5 + hydrocarbons (hydrocarbons, isoprene, C 4 oligomers and C 4 polymers having predominantly 5 or more carbon atoms per molecule), especially those having a higher boiling point than 1,3-butadiene, , Oligomers of butadiene having the formula (C 4 H 6 ) n where n is greater than or equal to 2, and optionally a polymer). The ratio of C 5 + hydrocarbons in the C 4 fraction in particular columns is dependent on the operating conditions of degradation based on the total weight of the crude C 4 fraction, 1000 ppmw or less, or even more than 5000 ppmw, a particular case, not more than 1% by weight . C 4 oligomer and C 4 The polymer is formed in particular as a result of storage and transport; The ratio thus depends predominantly on the storage and transport conditions and, in particular, on the temperature, duration and degree of inactivation of the environment in which the storage and / or transport takes place.
C 3 hydrocarbons of the extractive distillation, that is, hydrocarbons having three carbon atoms per molecule, can also cause problems. This is in particular methyl acetylene, which has an affinity similar to that of a typical optional solvent, for example 1,3-butadiene. Thus, the proportion of C 3 hydrocarbons in the feed stream for extractive distillation should be limited to less than 50 ppmw based on the total weight of the feed stream.
The above problem in the preliminary purification of the feed stream for the crude distillation of the crude C 4 fraction has now been solved in several ways: in one known mode of operation, in the distillation column connected upstream of the extractive distillation, the C 3 hydrocarbons And the remaining components are taken out through the bottom of the column. Subsequently, the bottoms stream is fed to an apparatus having an evaporator vessel, i. E. A single plate, for the removal of high boiling point components which have a boiling point relative to 1,3-butadiene. In the evaporator vessel, the high boiling point component of the residual liquid component with a high boiling point relative to 1,3-butadiene is present in an amount of 5% by weight, in particular 1% by weight, or even 1% by weight, based on the total weight of the crude C 4 fraction fed to the evaporator vessel The crude C 4 stream depleted of the C 3 component is substantially completely evaporated under flow control so as not to exceed 0.1% by weight. The liquid stream remaining in the evaporator vessel is discharged as a purge stream. However, the disadvantage here is that the purge stream also releases C 4 hydrocarbons, which are high-value valuable materials with high boiling point materials.
In this connection, it is an object of the present invention to remove the secondary components of the crude C 4 fraction, which interfere with the extractive distillation, in a technically simple manner with low capital and energy costs and as a result the effective life of the extractive distillation column life is increased.
This object is achieved through a process for providing a gas phase purified crude C 4 fraction as a feed stream for extractive distillation using an optional solvent,
Butane, and 1,3-butadiene as well as C 3 hydrocarbons, C 4 oligomers, C 4 Proceeds from the polymer and the C 5 + liquid fraction as a crude C 4 feed stream comprising a hydrocarbon,
A crude C 4 fraction is the purified gas
- less than two-thirds of the C 5 + hydrocarbons present in the feed stream and
- C 4 oligomers present in the feed stream and less than 5% by weight of the C 4 polymer
/ RTI >
1) a process step of removing C 4 oligomers, C 4 polymers and C 5 + hydrocarbons in each case with the residual content specified above for the gas phase purified crude C 4 fraction, and
2) process steps for evaporating the liquid C 4 fraction from the evaporator vessel
Lt; / RTI >
here
The evaporator vessel is assigned to a stripping column having one or more plates, a liquid C 4 fraction is fed to the top of the stripping column, a direct exchange of gas and liquid with the evaporator vessel takes place at the bottom of the stripping column, The purified crude C 4 fraction is withdrawn from its upper region and the stripping column is run without a condenser on the top of the column.
By associating the stripping column with an evaporator vessel, we have found that by increasing the removal of high boiling point material in the evaporator vessel and simultaneously reducing the C 4 hydrocarbons lost from the evaporator vessel through the purge stream, in a technically simple and not very energy- I realized that it was possible.
In this context, and more particularly in the construction of a new plant, it is possible to place the stripping column on top of the evaporator vessel, i.e. to integrate the evaporator vessel and the stripping column into a single apparatus.
In another embodiment, especially in an existing plant, it is also possible to associate the evaporator vessel with the stripping column, i.e. to provide the evaporator vessel and the stripping column as separate devices.
Evaporator vessels are simple devices known in the art of process technology. This generally comprises a vessel capable of separating the gas phase from the liquid phase and a heat exchanger arranged inside or outside the vessel.
According to the invention, a stripping column is assigned to the evaporator vessel.
Since the stripping columns and evaporator vessels are only provided for the depletion of high boiling point materials, it is possible to operate the stripping columns in a simple manner, without the condenser on the top of the column.
A typical crude C 4 fraction from a naphtha cracker has the following weight percent composition.
The crude C 4 fraction from the naphtha cracker thus predominantly contains butane, butene and 1,3-butadiene. There is also a small amount of other hydrocarbons. C 4 -acetylene is often present in proportions of up to 5% by weight or up to 2% by weight.
In the above-described extractive distillation, useful optional solvents are generally substances or mixtures having higher boiling points than the mixture to be separated and having a conjugate double bond and a triple bond rather than a simple double bond and a single bond, Is a dipole, more preferably a dipole aprotic solvent. For device reasons, less corrosive or noncorrosive materials are desirable.
Suitable optional solvents for the process according to the invention include, for example, butyrolactone, nitriles, such as acetonitrile, propionitrile, methoxypropionitrile, ketones such as acetone, furfural, N-alkyl- Aliphatic acid amides such as dimethylformamide, diethylformamide, dimethylacetamide, diethylacetamide, N-formylmorpholine, N-alkyl-substituted cyclic acid amides (lactams), such as N-alkylpyrrolidines Money, especially N-methyl pyrrolidone. Generally, N-alkyl-substituted lower aliphatic acid amides or N-alkyl-substituted cyclic acid amides are used. Particularly preferred are dimethylformamide, acetonitrile, furfural and especially N-methylpyrrolidone.
However, a mixture of the above solvents, for example a mixture of N-methylpyrrolidone and acetonitrile, a solvent and a co-solvent such as water and / or tert-butyl ether, for example methyl tert-butyl ether, Butyl ether, ethyl tert-butyl ether, propyl tert-butyl ether, n- or isobutyl tert-butyl ether may be used.
N-methylpyrrolidone, preferably N-methylpyrrolidone as an aqueous solution, especially N-methylpyrrolidone as an aqueous solution having 8 to 10% by weight of water, more preferably 8.3% by weight of water is particularly suitable Do.
In order to avoid the problems of the extractive distillation, use of which has to be supplied with an optional solvent stream, based on the total weight of the purified gaseous crude C 4 fraction containing the C 3 hydrocarbons of less than 50 ppmw, and C present in the feed stream 5 + is less than two-thirds of the C 4 hydrocarbons and oligomers, and a gas phase purification the crude C 4 fraction containing less than 5% by weight of the polymer present in the C 4 feed stream.
The inventors have found that it is possible to improve the removal of high boiling point materials in a simple manner by associating an evaporator vessel with a stripping column.
It is also possible in the process according to the invention to remove much of the valuable product C 4 hydrocarbons while removing much less boiling point components from the C 4 fraction than 1,3-butadiene.
Preferably, in the distillation column connected upstream of the evaporator vessel, the C 3 hydrocarbons in the gas phase purification the crude C 4 fraction, based on the total weight of the gaseous purification the crude C 4 fraction, preferably to less than 10 ppmw, or more Lt; RTI ID = 0.0 > ppmw. ≪ / RTI >
Further preferably, the C 5 + hydrocarbons in the gas phase purified C 4 fraction are depleted to less than half of the C 5 + hydrocarbons present in the feed stream.
The stripping column is operated preferably at an overhead pressure of 3 to 7 bar absolute pressure, further preferably at an overhead pressure of 4.5 to 5.5 bar absolute pressure.
The stripping column has in particular 1 to 15 theoretical plates.
BRIEF DESCRIPTION OF THE DRAWINGS The invention is illustrated in detail in the following figures and examples.
In the drawings,
1 and 2, which are schematic diagrams of an evaporator vessel in which a stripping column is located,
Figure 2 is a schematic diagram of the evaporator vessel with which the stripping column is associated.
The schematic diagram of Figure 1 shows an evaporator vessel (VK) in which a stripping column (K) is connected to the top of an evaporator vessel in such a way that the evaporator vessel (VK) and the stripping column (K) form a single unit. At the lower end of the evaporator vessel (VK), reboiler is provided.
The stripping column K is fed with the liquid C 4 fraction as
2 schematically shows a further preferred embodiment in which the evaporator vessel VK and the stripping column K are constructed as separate units and in which the direct gas and liquid exchange with the stripping column K is provided at the top of the evaporator vessel VK In diagram is shown.
The evaporator vessel (VK) is provided with a reboiler (S).
The stripping column K is fed with a liquid C 4 fraction as
<Examples>
The starting material is in each case, based on the total weight of the feed stream, 200 ppm of propane, 400 ppm of propene, 300 ppm of propadiene, 400 ppm of propyne, 2.0% of n-butane, 6.0% of iso Butane, 19.0% n-butene, 28.3% isobutene, 5.5% trans-2-butene, 4.4% cis-2-butene, 39.0% 1,3-butadiene, 0.2% 1,2- , A liquid as a 100 kt / one-year plant feed stream comprising 1200 ppm of 1-butyne, 4500 ppm of vinylacetylene and 1000 ppm of isopentane, 3-methyl-1-butene and 2-methyl- Crude C 4 fraction. C 4 oligomers and C 4 polymers may be present in the% range depending on storage and transport conditions. The C 3 hydrocarbons were removed via the top and the remaining components were removed through the bottom and subsequently the bottom stream was fed to an evaporator vessel, a device with a single plate, for the removal of the high boiling point component, which is boiling point relative to 1,3-butadiene For comparison with a plant with a distillation column, the crude C 4 fraction was pre-purified so that it could be used as a feed stream of extractive distillation. In the evaporator vessel, the crude C 4 stream depleted of the C 3 component was substantially completely evaporated and the boiling point of the residual liquid component having a boiling point higher than 1,3-butadiene in order to minimize the loss of the C 4 component in the liquid residue The point C 5 component was discharged under flow control such that it did not exceed 5% by weight based on the total weight of the crude C 4 fraction fed to the evaporator vessel. The proportion of oligomer and polymer present in the liquid residue was much greater due to the low vapor pressure. The liquid stream remaining in the evaporator vessel was discharged as a purge stream.
In accordance with an embodiment of the present invention, the same crude C 4 fraction was fed as a feed stream to an evaporator vessel (VK), a stripping column (K) with a theoretical number of stages 5 was located at the top of the evaporator vessel (VK) 4 fraction (1) was fed to the top of the stripping column (K) and the gas phase purified C fraction 4 was taken out from the top of the stripping column (K), and the stripping column (K) . The plant is schematically shown in Fig.
According to the prior art, less than 5% of the C 5 component present in the C 4 fraction is removed through the residual stream (= purge stream), whereas in the process according to the present invention, the amount of C 5 + hydrocarbons present in the feed stream Min and more than 95% by weight of the C 4 oligomer and polymer present in the feed stream were discharged from the residual stream through the bottom of the column.
According to the prior art, the residue flow rate (exiting the evaporator vessel) was 160 kg / h with a 1,3-butadiene ratio of 38.6% by weight.
By comparison, in the process according to the invention, the flow rate of the residue (distillation flow) from the distillation column was also 160 kg / h, but only 23% by weight of 1,3-butadiene. 1,3-butadiene yield (crude C 4 fraction of 1,3-butadiene in the purified C 4 fraction on the basis of 1,3-butadiene in) in the preliminary distillation is, in the embodiment of the present invention compared to the prior inde 99.49% And 99.29% depending on the technique. This means that a higher yield of valuable 1,3-butadiene product is achieved in the process according to the invention.
As a further advantage, in the process according to the invention the purified crude C 4 fraction was removed at a higher purity compared to the prior art process. In total 3000% ppmw 32 t / h crude C 4 feed in which the C 5 components of (where there may be an additional proportion of the C 6 component, and oligomers and polymers are added for not considered), of 94.16 kg / h The C 5 component was sent to extractive distillation according to prior art. By contrast, in the case of the present invention, only 55.1 kg / h of the C 5 component was sent to the extractive distillation. The loss of 1,3-butadiene in extractive distillation or subsequent refinery distillation was also correspondingly reduced since the C 5 component from the pre-distillation was fed to the extractive distillation to a lower level. Based on the pure product (pure 1,3-butadiene) resulting from total extractive distillation, including pre-distillation, the yield of 1,3-butadiene (calculated as 100% 1,3-butadiene) according to the prior art was 96.47% , And 96.66% in the case of the present invention.
In the above-mentioned large-scale plant of 1000 kt / a, the loss of valuable 1,3-butadiene product was therefore approximately 192 t / year greater in the process according to the prior art than the process according to the invention.
Thanks to the fact that the solvent forms a closed loop, the solvent was kept clean by the pre-removal of the problematic components and impurities, which minimized the regeneration complexity. At the same time, the contamination of the extractive distillation plant (contamination of the layer of the column) and droplet formation were minimized. As a result, less defoamer was required at a corresponding low cost. Reduced contamination reduces cleaning expense during shutdown. All shutdowns mean a production shutdown of about 2 weeks; Additional cleaning expense is required. This results in a cost in the 7-digit range.
Claims (9)
Butane, butene and butadiene as well as the proceeds from the C 3 hydrocarbons, C 4 oligomer, polymer C 4 and C 5 + liquid crude C 4 fraction (1) as the feed stream comprising a hydrocarbon,
A crude C 4 fraction is the purified gas
- less than two-thirds of the C 5 + hydrocarbons present in the feed stream and
- C 4 oligomers present in the feed stream and less than 5% by weight of the C 4 polymer
/ RTI >
1) C 4 oligomer, C 4 A processing step for removing the residual content to the specified for the polymer and the C 5 + hydrocarbons in the gas phase purification the crude C 4 fraction in each case, and
2) process step of evaporating the liquid C 4 fraction in the evaporator vessel (VK)
Lt; / RTI >
here
The evaporator vessel VK is assigned to a stripping column K having one or more plates and the liquid C 4 fraction 1 is fed to the top of the stripping column K and the bottom of the stripping column K is fed to the evaporator vessel K VK), and the crude C 4 fraction (2) gas phase purified from the stripping column (K) is taken out of its upper region, and the stripping column (K) is placed on the column top without a condenser Running
Way.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP12150824.6 | 2012-01-11 | ||
| EP12150824 | 2012-01-11 | ||
| PCT/EP2013/050366 WO2013104692A1 (en) | 2012-01-11 | 2013-01-10 | Method for providing a purified crude gaseous c4 fraction as an input stream for an extractive distillation using a selective solvent |
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| KR20140120329A true KR20140120329A (en) | 2014-10-13 |
| KR102049312B1 KR102049312B1 (en) | 2019-11-28 |
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| EP (1) | EP2802637B1 (en) |
| JP (1) | JP6067748B2 (en) |
| KR (1) | KR102049312B1 (en) |
| CN (1) | CN104053752B (en) |
| WO (1) | WO2013104692A1 (en) |
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| EP3793969A1 (en) * | 2018-05-18 | 2021-03-24 | SABIC Global Technologies B.V. | Method of producing a fuel additive with a hydration unit |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2877173A (en) * | 1955-03-23 | 1959-03-10 | Standard Oil Co | Hydroforming process |
| US4419188A (en) * | 1980-06-02 | 1983-12-06 | Mccall Thomas F | Thermally coupled extractive distillation process |
| US20080168797A1 (en) * | 2004-07-06 | 2008-07-17 | Fluor Technologies Corporation | Configurations and Methods for Gas Condensate Separation from High-Pressure Hydrocarbon Mixtures |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58167683A (en) * | 1982-03-29 | 1983-10-03 | Nippon Zeon Co Ltd | Extractive distillation |
| DE10022465A1 (en) * | 2000-05-09 | 2001-11-15 | Basf Ag | Processing a four carbon cut from the fractionation of crude oil, useful for the recovery of 1,4-butadiene, comprises extractive distillation, selective hydrogenation and distillation |
| DE10333756A1 (en) * | 2003-07-24 | 2005-02-17 | Basf Ag | Process for the separation of a crude C4 cut |
| DE102004005930A1 (en) * | 2004-02-06 | 2005-08-25 | Basf Ag | Process for the recovery of crude 1,3-butadiene |
| KR101440637B1 (en) * | 2006-07-12 | 2014-09-19 | 바스프 에스이 | Method for separating a c4 fraction by means of extractive distillation using a selective solvent |
| CN101492335B (en) * | 2008-01-23 | 2013-07-31 | 中国石油化工股份有限公司 | Combination method for comprehensive utilization of mix C4 |
-
2013
- 2013-01-10 EP EP13700159.0A patent/EP2802637B1/en active Active
- 2013-01-10 JP JP2014551607A patent/JP6067748B2/en active Active
- 2013-01-10 CN CN201380005242.3A patent/CN104053752B/en active Active
- 2013-01-10 KR KR1020147021970A patent/KR102049312B1/en active IP Right Grant
- 2013-01-10 WO PCT/EP2013/050366 patent/WO2013104692A1/en active Application Filing
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2877173A (en) * | 1955-03-23 | 1959-03-10 | Standard Oil Co | Hydroforming process |
| US4419188A (en) * | 1980-06-02 | 1983-12-06 | Mccall Thomas F | Thermally coupled extractive distillation process |
| US20080168797A1 (en) * | 2004-07-06 | 2008-07-17 | Fluor Technologies Corporation | Configurations and Methods for Gas Condensate Separation from High-Pressure Hydrocarbon Mixtures |
Also Published As
| Publication number | Publication date |
|---|---|
| EP2802637A1 (en) | 2014-11-19 |
| JP6067748B2 (en) | 2017-01-25 |
| EP2802637B1 (en) | 2017-03-22 |
| JP2015508409A (en) | 2015-03-19 |
| WO2013104692A1 (en) | 2013-07-18 |
| KR102049312B1 (en) | 2019-11-28 |
| CN104053752A (en) | 2014-09-17 |
| CN104053752B (en) | 2016-08-31 |
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