CN204058408U - A kind of device of High-efficiency Gas denitrogenation - Google Patents
A kind of device of High-efficiency Gas denitrogenation Download PDFInfo
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- CN204058408U CN204058408U CN201420523021.7U CN201420523021U CN204058408U CN 204058408 U CN204058408 U CN 204058408U CN 201420523021 U CN201420523021 U CN 201420523021U CN 204058408 U CN204058408 U CN 204058408U
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Abstract
The utility model discloses a kind of device of High-efficiency Gas denitrogenation, it comprises interchanger (1), LNG storage tank (2) and washing tower (3), the rich nitrogen pipeline (4) be parallel to each other is provided with in interchanger (1), gas-liquid mixed phase cryogen pipeline (7), gas phase cryogen pipeline I(8), gas phase cryogen pipeline II(9), liquid phase cryogen pipeline I(10) and liquid phase cryogen pipeline II(11), the exit end of LNG storage tank (2) is to pipeline I(5) inlet end to be linked in sequence BOG well heater (12), BOG compressor (13), BOG surge tank (14) and tail-gas compressor (15), fuel gas surge tank (16) is connected with between the exit end of BOG surge tank (14) and the inlet end of rich nitrogen pipeline (4).The beneficial effects of the utility model are: production cost is low, energy consumption is low, simple to operate, the LNG that good environmental benefit and economic benefit, nitrogen content be less than 1.5% can be obtained.
Description
Technical field
The utility model relates to the technical field of natural gas in low temperature denitrogenation, the device of particularly a kind of High-efficiency Gas denitrogenation.
Background technology
Unstripped gas at present for natural gas liquefaction device mainly contains conventional gas (hydrocarbon-bearing pool) and Unconventional forage (coal-seam gas, shale gas etc.), at least containing one or more not liquescent light constituent, such as nitrogen, oxygen, argon, hydrogen and helium etc. in various Sweet natural gas.In gas deliquescence process, if these components are not removed, will cause liquefaction energy consumption increase, LNG calorific value reduce, and give LNG storage, transport and bring potential safety hazard.
Therefore, in Sweet natural gas, removing of light constituent industrially more and more comes into one's own, simultaneously cryogenic rectification method remove above light constituent have remove thoroughly, the advantage such as dependable performance.
US Patent No. 6758060B2 describes a kind of method of producing separation of nitrogen in LNG process.The method adopts high-pressure rectification tower and low-pressure distillation tower, and each rectifying tower all arranges side and to boil device, and lower pressure column tower top arranges decompressor for condenser simultaneously provides condensation.At the bottom of the tower of high and low pressure tower, obtain LNG, obtain at the tower top of lower pressure column the rich nitrogen that methane content is less than 1%.
Similar with it, Chinese utility model patent CN201010561795 describes the method for a kind of nitrogenous methane gas denitrogenation to Sweet natural gas/natural gas liquids.The method comprises the precooling of unstripped gas, high-pressure tower (lower tower) rectifying, lower pressure column (upper tower) carry heat up in a steamer, the step such as gas product re-heat/mixed-refrigerant cycle.Obtain rich nitrogen at the top of lower pressure column (upper tower), the bottom of condenser/evaporator obtains LNG.
Chinese utility model patent CN201320809869 describes a kind of natural gas liquefaction co-producing high-purity nitrogen equipment, and the method comprises compressor, interchanger, denitrogenation rectifying tower, refrigeration agent separating tank, LNG tank and denitrogenation rectifying tower reboiler, condenser and phegma separating tank etc.Obtain LNG in the bottom of reboiler, obtain High Purity Nitrogen at the top of condenser.
Method described above all needs to arrange vaporizer at the bottom of overhead condenser and tower, substantially increases energy consumption and the complicacy of natural gas liquefaction device, and reduces benefit and the competitive power of liquefaction plant.
Utility model content
The purpose of this utility model is the shortcoming overcoming prior art, provide that a kind of production cost is low, energy consumption is low, simple to operate, the device that good environmental benefit and economic benefit, nitrogen content be less than the High-efficiency Gas denitrogenation of the LNG of 1.5% can be obtained.
The purpose of this utility model is achieved through the following technical solutions: a kind of device of High-efficiency Gas denitrogenation, it comprises interchanger, LNG storage tank and washing tower, the rich nitrogen pipeline be parallel to each other is provided with in described interchanger, pipeline I, pipeline II, gas-liquid mixed phase cryogen pipeline, gas phase cryogen pipeline I, gas phase cryogen pipeline II, liquid phase cryogen pipeline I and liquid phase cryogen pipeline II, the described exit end of rich nitrogen pipeline is communicated with the top of washing tower, the bottom of washing tower is communicated with LNG storage tank, and be connected with variable valve m between the inlet end of the bottom of washing tower and LNG storage tank, the exit end of LNG storage tank to be linked in sequence BOG well heater to the inlet end of pipeline I, BOG compressor, BOG surge tank and tail-gas compressor, fuel gas surge tank is connected with between the exit end of BOG surge tank and the inlet end of rich nitrogen pipeline,
The exit end of described pipeline I is connected with the upper end entrance A of washing tower, the lower inlet B of washing tower exports with the C place be arranged on gas-liquid mixed phase cryogen pipeline and the exit end of gas-liquid mixed phase cryogen pipeline is connected, and be connected to variable valve a and variable valve b between the outlet of C place and gas-liquid mixed phase cryogen pipeline
The inlet end of described gas-liquid mixed phase cryogen pipeline to be linked in sequence MR entrance separator, MR compressor, MR aftercooler and MR final stage separator to the inlet end of gas phase cryogen pipeline I, the exit end F of MR final stage separator is connected with the inlet end of liquid phase cryogen pipeline I
It also comprises MR Upper separator and MR Lower separator, the exit end of gas phase cryogen pipeline I is connected with the inlet end K of MR Upper separator, the exit end H of MR Upper separator is connected with the inlet end of gas phase cryogen pipeline II, the exit end of gas phase cryogen pipeline II is connected with the inlet end K of MR Lower separator, the exit end H of MR Lower separator is all connected with the exit end of gas-liquid mixed phase cryogen pipeline with exit end J, the exit end J of described MR Upper separator is connected with the inlet end of liquid phase cryogen pipeline II, the exit end of liquid phase cryogen pipeline II is connected with one end of variable valve c, the other end and the gas-liquid mixed phase cryogen pipeline communication of variable valve c, the exit end of described liquid phase cryogen pipeline I is connected with one end of variable valve d, the other end and the gas-liquid mixed phase cryogen pipeline communication of variable valve d.
Variable valve e is connected with between the exit end of described LNG storage tank and the inlet end of BOG well heater.
Variable valve f is connected with between the exit end of described BOG surge tank and the inlet end of fuel gas surge tank.
Variable valve h is connected with between the upper end entrance A of described washing tower and the exit end of pipeline I.
Variable valve k is connected with between the top of described washing tower and the exit end of rich nitrogen pipeline.
The utility model has the following advantages: the nitrogen that (1) is contained by Sweet natural gas itself washs in washing tower, the LNG that nitrogen content is less than 1.5% is obtained at the bottom of tower, substitute vaporizer and condenser owing to arranging rich solution nitrogen washing tower and BOG heat exchanger channels is set separately to reduce compressor row pressure, liquefaction plant total energy consumption reduces by 5% ~ 10% compared with conventional rectification denitrification system, reduces cost of investment.(2) the utility model can using produce BOG tail gas and rich nitrogen recycling to fuel gas surge tank in as fuel treatment, make waste gas obtain recycling, not only economy and also protect environment.(3) the utility model has that energy consumption is low, simple to operate, applied range, has good environmental benefit and the feature of economic benefit.
Accompanying drawing explanation
Fig. 1 is the structural representation of embodiment one of the present utility model;
Fig. 2 is the structural representation of embodiment two of the present utility model;
Fig. 3 is the structural representation of embodiment three of the present utility model;
Fig. 4 is the structural representation of embodiment four of the present utility model;
In figure, 1-interchanger, 2-LNG storage tank, 3-washing tower, the rich nitrogen pipeline of 4-, 5-pipeline I, 6-pipeline II, 7-gas-liquid mixed phase cryogen pipeline, 8-gas phase cryogen pipeline I, 9-gas phase cryogen pipeline II, 10-liquid phase cryogen pipeline I, 11-liquid phase cryogen pipeline II, 12-BOG well heater, 13-BOG compressor, 14-BOG surge tank, 15-tail-gas compressor, 16-fuel gas surge tank, 17-MR entrance separator, 18-MR compressor, 19-MR aftercooler, 20-MR final stage separator, 21-MR Upper separator, 22-MR Lower separator, 23-variable valve m, 24-variable valve a, 25-variable valve b, 26-variable valve c, 27-variable valve d, 28-variable valve e, 29-variable valve f, 30-variable valve h, 31-variable valve k, 32-LNG technique pump.
Embodiment
Be further described the utility model below in conjunction with accompanying drawing, protection domain of the present utility model is not limited to the following stated:
Embodiment one: as shown in Figure 1, a kind of device of High-efficiency Gas denitrogenation, it comprises interchanger 1, LNG storage tank 2 and washing tower 3, the rich nitrogen pipeline 4 be parallel to each other is provided with in described interchanger 1, pipeline I5, pipeline II6, gas-liquid mixed phase cryogen pipeline 7, gas phase cryogen pipeline I8, gas phase cryogen pipeline II9, liquid phase cryogen pipeline I10 and liquid phase cryogen pipeline II11, the exit end of described rich nitrogen pipeline 4 is communicated with the top of washing tower 3, the bottom of washing tower 3 is communicated with LNG storage tank, and be connected with variable valve m23 between the inlet end of the bottom of washing tower 3 and LNG storage tank 2.As shown in Figure 1; the exit end of LNG storage tank 2 to be linked in sequence BOG well heater 12, BOG compressor 13, BOG surge tank 14 and tail-gas compressor 15 to the inlet end of pipeline I5; fuel gas surge tank 16 is connected with between the exit end of BOG surge tank 14 and the inlet end of rich nitrogen pipeline 4; fuel gas surge tank 16 is for collecting rich nitrogen and part BOG tail gas; use for fuel gas; therefore, save production cost, improve the economic benefit of enterprise, protect ecotope.
As shown in Figure 1, the exit end of pipeline I5 is connected with the upper end entrance A of washing tower 3, the lower inlet B of washing tower 3 exports with the C place be arranged on gas-liquid mixed phase cryogen pipeline 7 and the exit end of gas-liquid mixed phase cryogen pipeline 7 is connected, and is connected to variable valve a24 and variable valve b25 between the outlet of C place and gas-liquid mixed phase cryogen pipeline 7.
As shown in Figure 1, the inlet end of gas-liquid mixed phase cryogen pipeline 7 is connected to the be linked in sequence exit end F of MR entrance separator 17, MR compressor 18, MR aftercooler 19 and MR final stage separator 20, MR final stage separator 20 of the inlet end of gas phase cryogen pipeline I8 with the inlet end of liquid phase cryogen pipeline I10.
As shown in Figure 1, it also comprises MR Upper separator 21 and MR Lower separator 22, the exit end of gas phase cryogen pipeline I8 is connected with the inlet end K of MR Upper separator 21, the exit end H of MR Upper separator 21 is connected with the inlet end of gas phase cryogen pipeline II9, the exit end of gas phase cryogen pipeline II9 is connected with the inlet end K of MR Lower separator 22, the exit end H of MR Lower separator 22 is all connected with the exit end of gas-liquid mixed phase cryogen pipeline 7 with exit end J, the exit end J of described MR Upper separator 21 is connected with the inlet end of liquid phase cryogen pipeline II11, the exit end of liquid phase cryogen pipeline II11 is connected with one end of variable valve c26, the other end of variable valve c26 is communicated with gas-liquid mixed phase cryogen pipeline 7, the exit end of described liquid phase cryogen pipeline I10 is connected with one end of variable valve d27, the other end of variable valve d27 is communicated with gas-liquid mixed phase cryogen pipeline 7, gas phase cryogen is separated for twice with MR Lower separator 22 by MR Upper separator 21 successively, liquid phase cryogen after separation and the temperature of gas phase cryogen very low, these gas phase cryogens and liquid phase cryogen are recycled again after entering gas-liquid mixed phase cryogen pipeline 7, thus provide cold for interchanger 1, for the denitrogenation of Sweet natural gas provides environment.
As shown in Figure 1, variable valve e28 is connected with between the exit end of LNG storage tank 2 and the inlet end of BOG well heater 12; Variable valve f29 is connected with between the exit end of BOG surge tank 14 and the inlet end of fuel gas surge tank 16; Variable valve h30 is connected with between the upper end entrance A of washing tower 3 and the exit end of pipeline I5; Variable valve k31 is connected with between the top of washing tower 3 and the exit end of rich nitrogen pipeline 4.
Nitrogen removal step under the present embodiment is as follows:
Step one: the preparation of gas phase cryogen and liquid phase cryogen, inlet end F to MR entrance separator 17 passes into Hydrocarbon Organic, Hydrocarbon Organic is separated into gaseous state and liquid hydrocarbon and enters after MR compressor 18 compresses in MR aftercooler 19 by MR entrance separator 17, hydrocarbon gas and liquid hydrocarbon be obtained gas phase cryogen and liquid phase cryogen after MR aftercooler 19 condensation, thus achieves the preparation of gas phase cryogen and liquid phase cryogen;
Step 2: liquid phase cryogen enters MR final stage separator 20 and is separated, the liquid phase cryogen after separation enters liquid phase cryogen pipeline I10, and obtained temperature is the liquid phase cryogen of-50 DEG C ~-60 DEG C and enters gas-liquid mixed phase cryogen pipeline 7 after variable valve d27 throttling;
Step 3: gas phase cryogen enters MR final stage separator 20 and is separated, the gas phase cryogen after separation enters gas phase cryogen pipeline I8, and enters MR Upper separator 21, and gas phase cryogen is separated into gas phase cryogen A and liquid phase cryogen B by MR Upper separator 21;
Step 4: the liquid phase cryogen B after separation enters liquid phase cryogen pipeline II11 through the exit end J of MR Upper separator 21, it is the liquid phase cryogen B of-100 DEG C ~-120 DEG C that liquid phase cryogen pipeline II11 flows out obtained temperature after variable valve c26 throttling from interchanger 1, and enters gas-liquid mixed phase cryogen pipeline 7;
Step 5: the gas phase cryogen A after separation enters gas phase cryogen pipeline II9 through the exit end H of MR Upper separator 21, gas phase cryogen A flows out and enters MR Lower separator 22 from interchanger 1, and gas phase cryogen A is separated into gas phase cryogen C and liquid phase cryogen D by MR Lower separator 22;
Step 6: the gas phase cryogen C after separation and liquid phase cryogen D enters in gas-liquid mixed phase cryogen pipeline 7 through the exit end H of MR Lower separator 22 and exit end J respectively, in gas-liquid mixed phase cryogen pipeline 7, gas-liquid mixed phase cryogen is extracted out from interchanger 1, gas-liquid mixed phase cryogen enters in interchanger 1 through MR entrance separator 17, MR compressor 18, MR aftercooler 19 and MR final stage separator 20 successively, thus achieves and provide cold to interchanger 1;
The preparation of step 7: LNG, Sweet natural gas is passed in pipeline II6, Sweet natural gas is backflowed cold flow precooling in interchanger 1, liquefaction is also excessively cold, temperature is that the Sweet natural gas of Sweet natural gas and-150 ~-160 DEG C of-100 ~-120 DEG C flows out from the outlet C of pipeline II6 and outlet B respectively, and enter in washing tower 3 after variable valve a24 and variable valve b25 throttling respectively, in washing tower 3, Sweet natural gas and nitrogen heat exchange, at the bottom of tower, the LNG that nitrogen content is less than 1.5% is obtained after obversion, obtained LNG enters in LNG storage tank 2 after variable valve m23 throttling, thus achieve the LNG that nitrogen content is less than 1.5%,
Step 8: the process of rich nitrogen, the rich nitrogen produced in washing tower 3 turns back in rich nitrogen pipeline 4 through variable valve k31, rich nitrogen is entered in fuel gas surge tank 16 as fuel gas by after Sweet natural gas and the re-heat to normal temperature of gas-liquid mixed phase cryogen, rich nitrogen is collected in fuel gas surge tank 16, not only save production cost, and need not be discharged in air, protect ecotope;
Step 9: the process of BOG tail gas, the BOG tail gas produced in LNG storage tank 2 is successively through BOG well heater 12, divide into two strands of BOG tail gas after BOG compressor 13 and BOG surge tank 14, wherein a part of BOG tail gas enters in fuel gas surge tank 16 as fuel gas, another part BOG tail gas enters in pipeline I5 after tail-gas compressor 15 compresses, BOG tail gas is backflowed cold flow precooling, liquefy and cross cold after enter washing tower 3, thus achieve the process of BOG tail gas, like this BOG exhaust collection is risen and be used as fuel use, not only save production cost, and need not be discharged in air, protect ecotope.
Embodiment 2: as shown in Figure 2, the difference of the present embodiment and embodiment 1 is: when the storage pressure of LNG storage tank 2 is greater than 0.08MPa (G), BOG compressor 13 can be cancelled, simultaneously in order to ensure that finished product LNG can enter LNG storage tank 2, to need by the pressure of governor valve control washing tower, at more than 0.18MPa (G), the LNG that nitrogen content is less than 1.5% can be obtained equally.
Embodiment 3: as shown in Figure 3, the difference of the present embodiment and embodiment 1 is: when the storage pressure of LNG storage tank 2 is greater than 0.08MPa (G), BOG compressor 13 can be cancelled, be with the difference of embodiment 2: in order to ensure that finished product LNG can enter LNG storage tank 2, control the pressure of washing tower 3 at 0.1MPa (G) to guarantee higher detersive efficiency simultaneously, increase LNG technique pump 32, the LNG that nitrogen content is less than 1.5% can be obtained equally.
Embodiment 4: as shown in Figure 4, the difference of the present embodiment and embodiment 1 is: when adopting low temperature BOG compressor 13, cancel BOG well heater 12, improve the row pressure of BOG compressor 13 after 0.2 ~ 2.0MPa (G) simultaneously, cancel tail-gas compressor 15, the LNG that nitrogen content is less than 1.5% can be obtained equally.
Claims (5)
1. the device of a High-efficiency Gas denitrogenation, it is characterized in that: it comprises interchanger (1), LNG storage tank (2) and washing tower (3), the rich nitrogen pipeline (4) be parallel to each other is provided with in described interchanger (1), pipeline I(5), pipeline II(6), gas-liquid mixed phase cryogen pipeline (7), gas phase cryogen pipeline I(8), gas phase cryogen pipeline II(9), liquid phase cryogen pipeline I(10) and liquid phase cryogen pipeline II(11), the exit end of described rich nitrogen pipeline (4) is communicated with the top of washing tower (3), the bottom of washing tower (3) is communicated with LNG storage tank, and be connected with variable valve m(23 between the inlet end of the bottom of washing tower (3) and LNG storage tank (2)), the exit end of LNG storage tank (2) is to pipeline I(5) inlet end to be linked in sequence BOG well heater (12), BOG compressor (13), BOG surge tank (14) and tail-gas compressor (15), fuel gas surge tank (16) is connected with between the exit end of BOG surge tank (14) and the inlet end of rich nitrogen pipeline (4),
Described pipeline I(5) exit end be connected with the upper end entrance A of washing tower (3), the lower inlet B of washing tower (3) exports with the C place be arranged on gas-liquid mixed phase cryogen pipeline (7) and the exit end of gas-liquid mixed phase cryogen pipeline (7) is connected, and be connected to variable valve a(24 between the outlet of C place and gas-liquid mixed phase cryogen pipeline (7)) and variable valve b(25)
The inlet end of described gas-liquid mixed phase cryogen pipeline (7) is to gas phase cryogen pipeline I(8) inlet end to be linked in sequence MR entrance separator (17), MR compressor (18), MR aftercooler (19) and MR final stage separator (20), exit end F and the liquid phase cryogen pipeline I(10 of MR final stage separator (20)) inlet end be connected
It also comprises MR Upper separator (21) and MR Lower separator (22), gas phase cryogen pipeline I(8) exit end be connected with the inlet end K of MR Upper separator (21), exit end H and the gas phase cryogen pipeline II(9 of MR Upper separator (21)) inlet end be connected, gas phase cryogen pipeline II(9) exit end be connected with the inlet end K of MR Lower separator (22), the exit end H of MR Lower separator (22) is all connected with the exit end of gas-liquid mixed phase cryogen pipeline (7) with exit end J, exit end J and the liquid phase cryogen pipeline II(11 of described MR Upper separator (21)) inlet end be connected, liquid phase cryogen pipeline II(11) exit end and variable valve c(26) one end be connected, variable valve c(26) the other end be communicated with gas-liquid mixed phase cryogen pipeline (7), described liquid phase cryogen pipeline I(10) exit end and variable valve d(27) one end be connected, variable valve d(27) the other end be communicated with gas-liquid mixed phase cryogen pipeline (7).
2. the device of a kind of High-efficiency Gas denitrogenation according to claim 1, is characterized in that: be connected with variable valve e(28 between the exit end of described LNG storage tank (2) and the inlet end of BOG well heater (12)).
3. the device of a kind of High-efficiency Gas denitrogenation according to claim 1, is characterized in that: be connected with variable valve f(29 between the exit end of described BOG surge tank (14) and the inlet end of fuel gas surge tank (16)).
4. the device of a kind of High-efficiency Gas denitrogenation according to claim 1, is characterized in that: the upper end entrance A of described washing tower (3) and pipeline I(5) exit end between be connected with variable valve h(30).
5. the device of a kind of High-efficiency Gas denitrogenation according to claim 1, is characterized in that: be connected with variable valve k(31 between the top of described washing tower (3) and the exit end of rich nitrogen pipeline (4)).
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| CN201420523021.7U CN204058408U (en) | 2014-09-12 | 2014-09-12 | A kind of device of High-efficiency Gas denitrogenation |
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| CN201420523021.7U CN204058408U (en) | 2014-09-12 | 2014-09-12 | A kind of device of High-efficiency Gas denitrogenation |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104293404A (en) * | 2014-09-12 | 2015-01-21 | 成都深冷液化设备股份有限公司 | Device and method for efficiently denitrifying natural gas |
| CN107473223A (en) * | 2017-08-15 | 2017-12-15 | 成都深冷液化设备股份有限公司 | A kind of CO cryogenic separation system and method using nitrogen cycle |
| CN107543369A (en) * | 2017-08-15 | 2018-01-05 | 成都深冷液化设备股份有限公司 | Cryogenic separation of CO and H2Double-circulation methane washing system and method |
-
2014
- 2014-09-12 CN CN201420523021.7U patent/CN204058408U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104293404A (en) * | 2014-09-12 | 2015-01-21 | 成都深冷液化设备股份有限公司 | Device and method for efficiently denitrifying natural gas |
| CN107473223A (en) * | 2017-08-15 | 2017-12-15 | 成都深冷液化设备股份有限公司 | A kind of CO cryogenic separation system and method using nitrogen cycle |
| CN107543369A (en) * | 2017-08-15 | 2018-01-05 | 成都深冷液化设备股份有限公司 | Cryogenic separation of CO and H2Double-circulation methane washing system and method |
| CN107473223B (en) * | 2017-08-15 | 2020-04-03 | 成都深冷液化设备股份有限公司 | CO cryogenic separation system adopting nitrogen circulation and method thereof |
| CN107543369B (en) * | 2017-08-15 | 2020-06-16 | 成都深冷液化设备股份有限公司 | Cryogenic separation of CO and H2Double-circulation methane washing system and method |
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Address after: 611700 north area of Chengdu modern industrial port, Pixian County, Chengdu City, Sichuan Province Patentee after: Sichuan Shudao Equipment Technology Co.,Ltd. Address before: 611700 north area of Chengdu modern industrial port, Pixian County, Chengdu City, Sichuan Province Patentee before: CHENGDU SHENLENG LIQUEFACTION PLANT Co.,Ltd. |
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