CN206056115U - A kind of LNG heat pump distillations produce the device of superelevation pure methane - Google Patents
A kind of LNG heat pump distillations produce the device of superelevation pure methane Download PDFInfo
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- CN206056115U CN206056115U CN201621060005.4U CN201621060005U CN206056115U CN 206056115 U CN206056115 U CN 206056115U CN 201621060005 U CN201621060005 U CN 201621060005U CN 206056115 U CN206056115 U CN 206056115U
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Abstract
This utility model belongs to the device that a kind of LNG heat pump distillations produce superelevation pure methane；Including raw material liquid storage tank, raw material liquid storage tank passes through first throttle valve and vaporizer is connected with the first raw material gas inlet of first rectifying column, first raw material gas inlet of the gaseous phase outlet of first rectifying column by the second heat exchanger, the first unstripped gas outlet of the second heat exchanger, heat pump, second raw material gas inlet of the second heat exchanger, the second unstripped gas outlet of the second heat exchanger and threeway are connected with the raw material gas inlet of the second reboiler, the unstripped gas outlet of the second reboiler is connected with the first raw material gas inlet of Second distillation column by the 4th choke valve, First Heat Exchanger is provided with vaporizer, the second unstripped gas outlet of second raw material gas inlet and First Heat Exchanger of the Second distillation column liquid-phase outlet by First Heat Exchanger is connected with storage tank；It is simple, easy to operate with technological process, stable, low energy consumption and prepare liquid phase methane purity be not less than 99.9995% advantage.
Description
Technical field
This utility model belongs to production superelevation pure methane technical field, and in particular to a kind of LNG heat pump distillations produce superelevation
The device of pure methane.
Background technology
At present, methane is produced mainly using two-stage rectification method, absorption-expansion desorption method and absorption-batch fractionating method；Two grades
Rectification method adopt for external refrigeration technology, two-stage rectification legal system takes high-purity methane, product purity up to 99.99%, due to work
Using carrying the remaining cold of helium device during skill, methane is side-product, low cost, but needs support Large Air Separation Devices system.
Absorption-expansion desorption method, by the High Pressure Absorption of multitower, low pressure desorption, realizes the purpose of purification methane, and this method equipment is simple,
Operation, easy maintenance, but yield is low, long flow path, needs corollary equipment many, and floor space is big.And the method needs periodic replacement
Adsorbent, thus it is relatively costly；Absorption-batch fractionating method, this kind of method are to first pass through absorption method to slough H2O, CO2, C2 etc. miscellaneous
Matter, then by batch fractionating, is obtained liquid phase methane product.This method product purity is up to 99.995%, or even can bring up to
99.999%；But its complex operation, technological process are long, adsorbent need to be regularly replaced.
Utility model content
The purpose of this utility model is to overcome of the prior art not enough and provide a kind of using heat pump distillation, double tower coupling
Conjunction rectification, technological process are simple, easy to operate, and stable, low energy consumption and preparation liquid phase methane purity are not less than 99.9995%
A kind of LNG heat pump distillations produce the device of superelevation pure methane.
What the purpose of this utility model was realized in：Including raw material liquid storage tank, raw material liquid storage tank passes through first throttle valve
It is connected with vaporizer with the first raw material gas inlet of first rectifying column, the gaseous phase outlet at the top of first rectifying column is by the second heat exchange
First raw material gas inlet of device, the first unstripped gas outlet of the second heat exchanger, heat pump, the second unstripped gas of the second heat exchanger enter
Mouth, the second unstripped gas outlet of the second heat exchanger and threeway are connected with the raw material gas inlet of the second reboiler, the second reboiler
Unstripped gas outlet is connected with the first raw material gas inlet of Second distillation column by the 4th choke valve, is provided with first and changes inside vaporizer
Hot device, the second of second raw material gas inlet and First Heat Exchanger of the outlet of Second distillation column bottom liquid phases by First Heat Exchanger are former
Material gas outlet is connected with storage tank；First rectifying column bottom liquid phases outlet by second throttle, the inlet exhaust gas of the second heat exchanger,
The offgas outlet of the second heat exchanger is connected with torch；3rd end of threeway passes through the first reboiler and the 3rd choke valve is smart with first
The second raw material gas inlet for evaporating tower top is connected；The top gas phase outlet of Second distillation column by pipeline and First Heat Exchanger the
One raw material gas inlet is connected, and the first unstripped gas outlet of First Heat Exchanger is connected with gas-liquid separator, the gas-liquid separator
Top gas phase outlet is connected with torch by the 5th choke valve, and the bottom liquid phases of the gas-liquid separator are exported and pass through pipeline and the
Second raw material gas inlet of two rectifying columns is connected.
This utility model by the way of heat pump distillation, using first rectifying column top section gas phase by heat pump pressurize as
Two rectifying tower bottom low-temperature heat sources, after liquefaction, and as tower top low-temperature receiver, by flow and the pressure change rectification of adjusting heat pump
Load.This utility model overcomes traditional view, the conventional refrigerants such as the liquid nitrogen of abandoning tradition, methane, with part material as system
Cryogen, participates in kind of refrigeration cycle, while refrigeration cost is greatly lowered, improves the safety coefficient in system operation.It is domestic
The same device for having put into operation at present only has four, five, and scale of the project size gap is larger, for convenience of contrast, this utility model
The Wuhan company for selecting design scale relatively similar with this utility model is contrasted.Following table is can be found in specifically.
This utility model adopts heat pump distillation and double tower coupling rectification, simple, easy to operate with technological process, and operation is steady
Fixed, low energy consumption and preparation liquid phase methane purity are not less than 99.9995% advantage.
Description of the drawings
Fig. 1 is structural representation of the present utility model.
Specific embodiment
In order to be more clearly understood to technical characteristic of the present utility model, purpose and effect, now control is illustrated
Specific embodiment of the present utility model, in the various figures identical label represent identical part.To make simplified form, in each figure
The part related to utility model is schematically show only, they do not represent which as the practical structures of product.
As shown in figure 1, this utility model includes raw material liquid storage tank 48, raw material liquid storage tank 48 passes through first throttle valve 1 and steams
Send out device 2 to enter 33 with the first unstripped gas of first rectifying column 4 and be connected, the gaseous phase outlet 30 at the top of first rectifying column 4 is changed by second
First raw material gas inlet 36 of hot device, the first unstripped gas outlet 41, heat pump 6 of the second heat exchanger, the second heat exchanger it is second former
Expect 28 phase of raw material gas inlet of gas import 38, the second unstripped gas outlet 40 of the second heat exchanger and threeway 17 and the second reboiler 10
Even, the unstripped gas outlet 48 of the second reboiler 10 is by the 4th choke valve 11 and the first raw material gas inlet 44 of Second distillation column 13
It is connected, inside vaporizer 2, is provided with First Heat Exchanger 3,13 bottom liquid phases of Second distillation column outlet 29 by First Heat Exchanger 3 the
The second unstripped gas outlet 19 of two raw material gas inlets 21 and First Heat Exchanger 3 is connected with storage tank 16；4 bottom liquid phases of first rectifying column
Outlet 35 is by second throttle 12, the inlet exhaust gas 39 of the second heat exchanger 5, the offgas outlet 37 of the second heat exchanger 5 and torch 7
It is connected；3rd end of threeway 17 passes through the second unstripped gas of the first reboiler 8 and the 3rd choke valve 9 and 4 top of first rectifying column
Import 31 is connected；The top gas phase outlet 26 of Second distillation column 13 is by pipeline and the first raw material gas inlet of First Heat Exchanger 3
18 are connected, and the first unstripped gas outlet 22 of First Heat Exchanger 3 is connected with gas-liquid separator 14, the top of the gas-liquid separator 14
Gaseous phase outlet 23 is connected with torch 7 by the 5th choke valve 15, and the bottom liquid phases outlet 25 of the gas-liquid separator 14 is by pipe
Road is connected with the second raw material gas inlet 27 of Second distillation column 13.
A kind of production method of the device of LNG heat pump distillations production superelevation pure methane, comprises the steps：
Step one：LNG material liquids in raw material liquid storage tank 48 by the raw material gas inlet 20 of first throttle valve 1, vaporizer,
Enter in first rectifying column 4 after the unstripped gas outlet 17 of vaporizer and the first raw material gas inlet 33 of first rectifying column 4；It is described
The composition of LNG material liquids is：Methane, hydrogen, argon, nitrogen；The temperature of LNG material liquids is：- 160～-155 DEG C, gas phase
Rate is divided to be 0, methane molar fraction：96.4%；After first throttle valve 1, raw material liquid temp is：-156℃；The unstripped gas of vaporizer goes out
Mouthfuls 17 unstripped gas temperature is：- 151～-147 DEG C, gas phase fraction is 1；
Step 2：First rectifying column 4 carries out rectification and purification to unstripped gas, and the gas phase after rectification and purification passes through first rectifying column
4 top gas phase exports the first unstripped gas outlet of first raw material gas inlet 36 and the second heat exchanger 5 of the 30, second heat exchanger 5
41 enter in heat pump 6；The top gas phase of the first rectifying column 4 exports 30 unstripped gas temperature：- 150～-155 DEG C, methane
Molar fraction：98.8%；The unstripped gas temperature of the first unstripped gas outlet 41 of the second heat exchanger 5：0～10 DEG C；
Step 3：The unstripped gas in entrance heat pump 6 described in step 2 is entered by the second unstripped gas of the second heat exchanger
The second unstripped gas outlet 40, threeway 17 of the 38, second heat exchanger of mouth and the raw material gas inlet 28 of the second reboiler 10 enter second
In reboiler 10；The heat pump 6 outlet unstripped gas temperature be：35～40 DEG C, the second unstripped gas outlet 40 of the second heat exchanger 5
Unstripped gas temperature be：- 138～-135 DEG C, gas phase fraction is：0.75；
Step 4：Raw material of the unstripped gas in the second reboiler of entrance 10 described in step 3 by the second reboiler 10
First raw material gas inlet 44 of gas the 48, the 4th choke valve 11 of outlet and Second distillation column 13 enters the inside of Second distillation column 13；
The unstripped gas of the second reboiler exports 48 unstripped gas temperature：- 139 DEG C, gas phase fraction is：0；
Step 5：The unstripped gas entered in Second distillation column 13 described in above-mentioned steps four is made to carry out rectification and purification, rectification
Bottom liquid phases outlet 29, second raw material gas inlet 21 and of First Heat Exchanger 3 of the liquid phase after purification by Second distillation column 13
The second unstripped gas outlet 19 of First Heat Exchanger 3 is entered inside storage tank 16；The bottom liquid phases outlet liquid phase first of Second distillation column 13
The temperature of alkane is：-142℃；Second unstripped gas 19 of First Heat Exchanger 3 exports the temperature of liquid phase methane：- 151 DEG C, gas phase point
Rate 0；The purity of the liquid phase methane inside described storage tank 16 is not less than 99.9995%；
Step 6：First rectifying column 4 described in step 2 carries out the liquid phase after rectification and purification by first to unstripped gas
The tail of the bottom liquid phases outlet 35, second throttle 12, the inlet exhaust gas 39 of the second heat exchanger 5 and the second heat exchanger 5 of rectifying column 4
Gas outlet 37 is entered inside torch 7；The bottom liquid phases of the first rectifying column 4 export 35 waste liquid temperature：- 149 DEG C～-
145℃；37 waste liquid temperature of offgas outlet of the second heat exchanger 5 is：20 DEG C～25 DEG C；
Step 7：Entered in the first reboiler 8 by the 3rd end of threeway 17 by the unstripped gas of threeway 17 in the step 3,
The unstripped gas entered in the first reboiler 8 passes through the 3rd choke valve 9 and the second raw material gas inlet 31 of first rectifying column 4 is entered
Entering in first rectifying column 4 carries out rectification and purification；First reboiler 8 unstripped gas outlet in unstripped gas temperature be：-142
DEG C, gas phase fraction is：0；
Step 8：Gas phase described in step 5 after rectification and purification by the top gas phase of Second distillation column 13 outlet 26,
The first unstripped gas outlet 22 of first raw material gas inlet 18 and First Heat Exchanger 3 of First Heat Exchanger 3 enters gas-liquid separator 14
It is interior, top gas phase outlet 23 and fiveth of the tail gas after gas-liquid separator 14 carries out gas-liquid separation by gas-liquid separator 14
Choke valve 15 is entered in torch 7, bottom of the liquid phase after gas-liquid separator 14 carries out gas-liquid separation by gas-liquid separator 14
Second raw material gas inlet 27 of portion's liquid-phase outlet 25 and Second distillation column 13 carries out rectification and purification into inside Second distillation column 13；
The top gas phase of Second distillation column 13 exports 26 unstripped gas temperature：-144℃；The first unstripped gas outlet 22 of First Heat Exchanger 3
Unstripped gas temperature be：-151℃；The top gas phase of gas-liquid separator 14 exports 23 exhaust temperatures：- 151 DEG C, methane mole point
Number 50%～58%；The bottom liquid phases outlet temperature of gas-liquid separator 14：-151℃.
This utility model be the device that a kind of LNG heat pump distillations produce superelevation pure methane, wherein superelevation pure methane at home
Without related definition, but illustrate in international higher standard, the methane product of methane content >=99.9995% is defined as surpassing
High-purity grade of product, i.e. superelevation pure methane, the superelevation pure methane title in this utility model derive from this, its with specific reference to document
For：《Chinese industrial gas is complete works of》Table II .1.2-20 in page 1704, Messer Griesheim GmbH.High Purity
Gases(Catalog).1992.28。
Those listed above is a series of to describe the tool for being only for feasibility embodiment of the present utility model in detail
Body illustrates that they are simultaneously not used to limit protection domain of the present utility model, all to be made without departing from this utility model skill spirit
Equivalent implementations or change are should be included within protection domain of the present utility model.
Claims (1)
1. a kind of LNG heat pump distillations produce the device of superelevation pure methane, it is characterised in that：Including raw material liquid storage tank (20), raw material
First raw material gas inlet (33) phase of the liquid storage tank (20) by first throttle valve (1) and vaporizer (2) and first rectifying column (4)
Even, the gaseous phase outlet (30) at the top of first rectifying column (4) is by first raw material gas inlet (36) of the second heat exchanger, the second heat exchange
First unstripped gas outlet (34) of device, heat pump (6), second raw material gas inlet (38) of the second heat exchanger, the of the second heat exchanger
Two unstripped gas export (40) and threeway (17) is connected with the raw material gas inlet (28) of the second reboiler (10), the second reboiler (10)
Unstripped gas outlet (24) be connected with first raw material gas inlet (32) of Second distillation column (13) by the 4th choke valve (11), steaming
Send out, Second distillation column (13) bottom liquid phases export (29) by First Heat Exchanger (3)
The second raw material gas inlet (21) and First Heat Exchanger (3) the second unstripped gas outlet (19) be connected with storage tank (16)；First is smart
Evaporate tower (4) bottom liquid phases outlet (35) to change by second throttle (12), the inlet exhaust gas (39) of the second heat exchanger (5), second
The offgas outlet (37) of hot device (5) is connected with torch (7)；3rd end of threeway (17) passes through the first reboiler (8) and Section three
Stream valve (9) is connected with second raw material gas inlet (31) on first rectifying column (4) top；The top gas phase of Second distillation column (13) goes out
Mouth (26) is connected with first raw material gas inlet (18) of First Heat Exchanger (3) by pipeline, the first raw material of First Heat Exchanger (3)
Gas outlet (22) is connected with gas-liquid separator (14), and top gas phase outlet (23) of the gas-liquid separator (14) is by Section five
Stream valve (15) is connected with torch (7), and bottom liquid phases outlet (25) of the gas-liquid separator (14) are by pipeline and the second rectification
Second raw material gas inlet (27) of tower (13) is connected.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621060005.4U CN206056115U (en) | 2016-08-29 | 2016-08-29 | A kind of LNG heat pump distillations produce the device of superelevation pure methane |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621060005.4U CN206056115U (en) | 2016-08-29 | 2016-08-29 | A kind of LNG heat pump distillations produce the device of superelevation pure methane |
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| Publication Number | Publication Date |
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| CN206056115U true CN206056115U (en) | 2017-03-29 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201621060005.4U Withdrawn - After Issue CN206056115U (en) | 2016-08-29 | 2016-08-29 | A kind of LNG heat pump distillations produce the device of superelevation pure methane |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106288652A (en) * | 2016-08-29 | 2017-01-04 | 河南心连心深冷能源股份有限公司 | A kind of LNG heat pump distillation produces device and the production method of ultra-pure methane |
| CN107144092A (en) * | 2017-05-27 | 2017-09-08 | 河南心连心深冷能源股份有限公司 | A kind of device and its production technology that high-purity ethylene is produced with ethene heat pump distillation |
-
2016
- 2016-08-29 CN CN201621060005.4U patent/CN206056115U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106288652A (en) * | 2016-08-29 | 2017-01-04 | 河南心连心深冷能源股份有限公司 | A kind of LNG heat pump distillation produces device and the production method of ultra-pure methane |
| CN106288652B (en) * | 2016-08-29 | 2019-05-10 | 河南心连心深冷能源股份有限公司 | A kind of device and production method of LNG heat pump distillation production superelevation pure methane |
| CN107144092A (en) * | 2017-05-27 | 2017-09-08 | 河南心连心深冷能源股份有限公司 | A kind of device and its production technology that high-purity ethylene is produced with ethene heat pump distillation |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20170329 Effective date of abandoning: 20190510 |
|
| AV01 | Patent right actively abandoned |