CN103925771A - Process for manufacturing methane - Google Patents
Process for manufacturing methane Download PDFInfo
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- CN103925771A CN103925771A CN201310428523.1A CN201310428523A CN103925771A CN 103925771 A CN103925771 A CN 103925771A CN 201310428523 A CN201310428523 A CN 201310428523A CN 103925771 A CN103925771 A CN 103925771A
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Abstract
The invention discloses a process for manufacturing methane. The process includes virgin gas purification operation, refrigerating compression operation, liquefaction operation and LNG (liquefied natural gas) storage operation. The virgin gas purification operation is used for carrying out purification operation on virgin gas, and purified gas is delivered to a liquefaction unit to be subjected to liquefaction operation; the refrigerating compression operation is used for carrying out pressurization and cooling operation on nitrogen, and expanded and refrigerated low-temperature gas is delivered to the liquefaction unit; the liquefaction operation is used for receiving the virgin gas from the purification operation and the low-temperature gas from the compression operation; the virgin gas is cooled by the low-temperature gas under the control and then is subjected to separation operation, and separated LNG is delivered to be subjected to the storage operation. The process has the advantages that by the aid of a method for recycling and manufacturing the liquefied natural gas in tail gas, energy conservation measures of enterprises can be effectively upgraded, resource consumption of the enterprises can be reduced, and an effect of comprehensively utilizing energy of the enterprises can be enhanced.
Description
Technical field
The present invention relates to the recovery technology field of liquefied natural gas and methane, especially a kind of preparation technology of methane.
Background technology
At present, along with improving constantly of people's living standard, for the utilization of the energy also age different from the past, so, the energy-saving and cost-reducing of the energy all advocated in a lot of areas energetically now, reduces the loss of the energy, increases the utilization ratio of the energy, the descendants that not only can better bring benefit to the mankind, has responded the guiding theory of country about sustainable development especially energetically.Investigation demonstration, the methane concentration in atmosphere has increased more than one times for many years, mainly by mankind's activity, is caused.The energy force rate carbon dioxide that methane stops heat to distribute from atmosphere is high 23 times, and therefore reducing discharge of methane and reclaiming in time methane is to solve the good approach that global warming issue can take effect in a short time.
Wherein, recycle methane as clean energy resource, can not only reduce global discharge of methane, also promote the production safety coefficients such as colliery, improve local air quality.The methane marketization is the new period mankind's a wise selection, for consolidating economic growth, promote energy security, improving environment and reduce greenhouse gas emission, is all a thing being highly profitable.In prior art, for film, carry in hydrogen tail gas and do not carry out a well recycling, the methane recovery operation of especially carrying in hydrogen tail gas for film does not have an effective way.
Summary of the invention
The technical problem that the present invention solves is to provide a kind of preparation technology of methane, can in tail gas, reclaim and prepare the method for methane, can effectively improve the conservation measures of enterprise, reduces the resource consumption of enterprise, improves the comprehensive utilization of energy of enterprise.
For solving the problems of the technologies described above, the invention provides a kind of preparation technology of methane, it is characterized in that; Comprise unstripped gas purification process, refrigerant compression operation, Operation for liquefaction, LNG store operation, diffuse operation; Wherein,
Unstripped gas purification process, for unstripped gas is carried out to purification run, and flows to liquefaction unit by purified gas and carries out Operation for liquefaction; Wherein, described unstripped gas purification process adopts drying tower and filter to realize; After described unstripped gas drying tower, remove H
2o enters Operation for liquefaction after filter carries out dust pretreatment;
Refrigerant compression operation, for nitrogen is carried out to supercharging cooling down operation, and is delivered to liquefaction unit by the cryogenic gas after swell refrigeration; Wherein, described refrigerant compression operation adopts compressor, cooler and surge tank to realize; Described nitrogen, after nitrogen buffer tank carries out buffer operation, enters compressor and carries out boost operations, enters cooler and carry out cooling down operation after boost operations completes, and coldly goes the cryogenic gas after operation to be delivered to Operation for liquefaction and to use as cold-producing medium
Operation for liquefaction, for receiving from the unstripped gas of purification run with from the cryogenic gas of squeeze operation; Control unstripped gas and after cryogenic gas is cooling, carry out lock out operation, and the LNG of separation place is flowed to store operation; Wherein, described Operation for liquefaction adopts heat exchanger, knockout drum and rectifying column to realize; Described unstripped gas carries out cooling down operation under the effect of described cryogenic gas, and entering knockout drum after cooling carries out lock out operation, and the gas of sub-department enters after rectifying column from tower top output hydrogen and nitrogen, from output LNG product at the bottom of tower and flow to store operation;
LNG store operation, for storing the LNG of Operation for liquefaction output to reclaim;
Wherein, described unstripped gas purification process, refrigerant compression operation, Operation for liquefaction, LNG store operation and diffuse control mode that operation adopts for controlling on the spot the control mode combining with Central Control Room Long-distance Control, Central Control Room is controlled employing DCS control system; Wherein, measurement and control operation, the operation of stopping in emergency are all carried out in described Central Control Room; Device parameter and running state parameter show in Central Control Room DCS display unit, go forward side by side line item and corresponding alarm operation; The operation of device start that described operation relates to is carried out with control mode on the spot.
Technique scheme of the present invention has following beneficial features:
The present invention can reclaim and prepare the method for liquefied natural gas by technique scheme in tail gas, can effectively improve the conservation measures of enterprise, reduces the resource consumption of enterprise, improves the comprehensive utilization of energy of enterprise; By CH in the final LNG obtaining of technique scheme
4purity:>=98% (V/V).
The application's further feature and advantage will be set forth in the following description, and, partly from description, become apparent, or understand by implementing the application.The application's object and other advantages can be realized and be obtained by specifically noted structure in description, claims and accompanying drawing.
Accompanying drawing explanation
Fig. 1 is the operation chart of the embodiment of the present invention.
The specific embodiment
For making the object, technical solutions and advantages of the present invention clearer, hereinafter will be elaborated to embodiments of the invention.It should be noted that, in the situation that not conflicting, embodiment and the feature in embodiment in the application can be combined mutually.
The invention provides a kind of preparation technology of methane, comprise unstripped gas purification process, refrigerant compression operation, Operation for liquefaction, LNG store operation, diffuse operation; Wherein,
Unstripped gas purification process, for unstripped gas is carried out to purification run, and flows to liquefaction unit by purified gas and carries out Operation for liquefaction;
Refrigerant compression operation, for nitrogen is carried out to supercharging cooling down operation, and is delivered to liquefaction unit by the cryogenic gas after swell refrigeration;
Operation for liquefaction, for receiving from the unstripped gas of purification run with from the cryogenic gas of squeeze operation; Control unstripped gas and after cryogenic gas is cooling, carry out lock out operation, and the LNG of separation place is flowed to store operation;
LNG store operation, for storing the LNG of Operation for liquefaction output to reclaim;
Diffuse operation, for the exhaust gas centralized high and medium discharge that Operation for liquefaction is produced;
Wherein, the control mode that said method provided by the invention adopts in practical operation is for controlling on the spot the control mode combining with Central Control Room Long-distance Control, and Central Control Room is controlled and adopted DCS control system.
Measurement and control operation in above-mentioned each operation provided by the invention are all carried out in Central Control Room, and the operation of stopping in emergency is also carried out in Central Control Room; The device parameter that each operating unit relates to and running state parameter show in Central Control Room DCS display unit, go forward side by side line item and corresponding alarm operation.Wherein, the device start of unit carries out with control mode on the spot, carries out at the scene start-up operation.
Accordingly, the invention provides a kind of preparation system of methane, as shown in Figure 1, comprise unstripped gas purification unit, refrigerant compression unit, liquefaction unit, LNG storage element, diffuse unit; Wherein,
Unstripped gas purification unit, for unstripped gas is carried out to purification run, and flows to liquefaction unit by purified gas and carries out liquefaction unit;
Refrigerant compression unit, for nitrogen is carried out to supercharging cooling down operation, and is delivered to liquefaction unit by the cryogenic gas after swell refrigeration;
Liquefaction unit, for receiving from the unstripped gas of clean unit with from the cryogenic gas of compression unit; Control unstripped gas and after cryogenic gas is cooling, carry out lock out operation, and the LNG of separation place is flowed to storage element;
LNG storage element, for storing the LNG of liquefaction unit output to reclaim;
Diffuse unit, for the exhaust gas centralized high and medium discharge that liquefaction unit is produced;
Wherein, the control mode that said method provided by the invention adopts in actual cell is for controlling on the spot the control mode combining with Central Control Room Long-distance Control, and Central Control Room is controlled and adopted DCS control system.
Measurement and control operation in above-mentioned unit provided by the invention are all carried out in Central Control Room, and the operation of stopping in emergency is also carried out in Central Control Room; The device parameter that unit relates to and running state parameter show in Central Control Room DCS display unit, go forward side by side line item and corresponding alarm operation.Wherein, the device start of unit carries out with control mode on the spot, carries out at the scene device start operation.
In concrete operations, technique scheme technological process provided by the invention specifically describes as follows:
This project adopts proposes to being rich in the film of CH4 the technological process that hydrogen tail gas is purified and developed, and adopts nitrogen expanding refrigeration liquefaction technology, low-temperature fractionating tower isolation technics to produce highly purified LNG product.
Refrigeration system adopts single cycle refrigeration technique.Kind of refrigeration cycle technological process adopts nitrogen expansion refrigeration.Nitrogen, when compressor supercharging is cooled to 0.8MPaG, temperature to be 40 ℃, then enters ice chest and is cooled to-140 ℃, then enters after decompressor swell refrigeration obtains-185 ℃ of cryogenic gases and returns to liquefaction ice chest, precooling unstripped gas, liquefied methane.
In concrete operations, the process equipment and the corresponding operating that relate to are described below:
1, unstripped gas purification unit and unstripped gas purification process; First unstripped gas enters in molecular sieve dehydration drying device and meets after decontamination index requires and enter liquefaction unit; It is as follows that unstripped gas purification unit relates to equipment:
1) drying tower; Drying tower is mainly used to adsorb the micro-H2O in unstripped gas, prevents that H2O from stopping up plate-fin heat exchanger in low temperature process process.
Drying tower technical parameter is as follows:
Quantity: 2
Pattern: vertical
Working media: unstripped gas
Operating pressure: 3.8MPaG
Operating temperature: 35 ℃
Adsorbent pattern: 4A molecular sieve
Work period: 8h
Material: Q345R
Size: φ 1000 * 3000
2) regeneration gas heater; Regeneration gas heater is used for the gas that thermal regeneration molecular sieve is used.
Regeneration gas heater technical parameter is as follows:
Quantity: 1
Tube side medium: the warm steam of office
Tube side inlet temperature: press saturated vapor in 2.5MPaG
Tube side outlet temperature: condensed steam
Shell side medium: regeneration gas (rich nitrogen)
Operating pressure: 0.07MPaG
Shell side inlet temperature: 40 ℃
Outlet temperature: 240 ℃
Material: Q345R
3) piping filter; Filter is mainly used to filter the molecular sieve dust in preprocessing process; Prevent from entering aluminum plate-fin heat exchanger, stop up Cryo Equipment.
Filter technology parameter is as follows:
Quantity: 2
Pattern: vertical
Working media: unstripped gas
Operating pressure: 3.8MPaG
Operating temperature: 40 ℃
Filtering accuracy: 0.125mm
2, refrigerant compression unit and refrigerant compression operation; For nitrogen is carried out to supercharging cooling down operation, and be delivered to Operation for liquefaction by the cryogenic gas after swell refrigeration; Squeeze operation can comprise compressor, cooler and surge tank; Nitrogen, after nitrogen buffer tank carries out buffer operation, enters compressor and carries out boost operations, enters cooler and carry out cooling down operation after boost operations completes, and coldly goes the cryogenic gas after operation to be delivered to Operation for liquefaction and to use as cold-producing medium.
Preferably, in concrete operations, refrigerant compression operation is comprised of single cycle nitrogen compressor, water cooler and nitrogen buffer tank.Low-pressure nitrogen from ice chest heat exchanger enters nitrogen buffer tank, then enters nitrogen compressor and boosts to 0.8MPaG, then enters water cooler cooling, goes out that water cooler is laggard enters ice chest precooling, then enters expander refrigeration end.Mix refrigerant enters cold-producing medium surge tank, then enters cold-producing medium and presses
Wherein, refrigerant compression unit key equipment is that nitrogen compressor, its technical parameter are as follows:
Quantity: 1
Air inflow: 18000Nm3/h
Admission pressure (gauge pressure): 0.2MPaG
Intake air temperature: 36.4 ℃
Medium: nitrogen
Outlet pressure (gauge pressure): 0.8MpaG
Outlet temperature :≤40 ℃
Shaft power: 1750kW
3, liquefaction unit and Operation for liquefaction; For receiving from the unstripped gas of purification run unit with from the cryogenic gas of squeeze operation; Control unstripped gas and after cryogenic gas is cooling, carry out lock out operation, and the LNG of separation place is flowed to LNG store operation.
Liquefaction unit can adopt liquefaction ice chest, and wherein, liquefaction ice chest is comprised of equipment such as plate-fin heat exchanger, rectifying column, knockout drums.Unstripped gas is cooled to-160 ℃ in ice chest, and throttling flash separation goes out the laggard low-temperature fractionating tower T1301 of entering of gas.Tower top is isolated all hydrogen and nitrogen, from the LNG product of producing at the bottom of tower.
The technical parameter of liquefaction ice chest is as follows:
Quantity: 1
Appearance and size: 4 * 4 * 20m*m*m
Insulation pattern: pearlife
Heat-preserving range: wing heat exchanger, flash tank, rectifying column etc.
4, LNG storage element and LNG store operation; For the LNG of Operation for liquefaction output is stored and is reclaimed.Wherein, this project adopts LNG primary and secondary tank stores with pressure, and tank volume is 300m3, can meet the storage needs of 4 days full load LNG products.
LNG storage tank technical parameter is as follows:
Quantity: 1
Pattern: vertical
Working media: LNG
Operating pressure: 0.3MPaG
Operating temperature :-160 ℃
Design pressure: 0.5MPaG
Design temperature :-196 ℃
5, diffuse unit and diffuse operation; Waste gas cloud diffusing tower from the safety valve discharge in liquefaction unit is concentrated high altitude discharge; Diffuse unit and can comprise diffusing tower.
Diffusing tower technical parameter is as follows:
Diffuse medium: normal-temperature natural-gas
Designing and arranging is high-volume: 6000m3/h
Exhaust stack inlet pressure: 6-12kPa
Steam pressure: 0.2-0.4MPa
Caliber interface: DN50
Power Level: AC220/50Hz
Diffuse height :～40m
Earthquake intensity: 7 degree
6, control module and control operation; Preferably, the above-mentioned unit in the present invention adopts and controls on the spot the control mode combining with Central Control Room Long-distance Control; Wherein, Central Control Room is controlled and is adopted DCS control system.
Measurement and control operation in above-mentioned unit provided by the invention are all carried out in Central Control Room, and the operation of stopping in emergency is also carried out in Central Control Room; The device parameter of unit and running state parameter show in Central Control Room DCS display unit, go forward side by side line item and corresponding alarm operation.Wherein, the device start of unit carries out with control mode on the spot, carries out at the scene start-up operation.
As follows by the final LNG technical parameter obtaining of technique scheme provided by the invention:
CH in LNG
4purity:>=98% (V/V) volume ratio;
LNG flow: 1313.9Nm3/h;
LNG temperature :-160 ℃;
LNG pressure: 0.2MpaA.
CH in the LNG liquefied natural gas finally obtaining by technique scheme provided by the invention
4purity higher than the CH of preparation of the prior art
4purity; Easy to spread and implement.
Although the disclosed embodiment of the present invention as above, the embodiment that described content just adopts for the ease of understanding the present invention, not in order to limit the present invention.Technical staff in any the technical field of the invention; do not departing under the prerequisite of the disclosed spirit and scope of the present invention; can do any modification and variation what implement in form and in details; but scope of patent protection of the present invention, still must be as the criterion with the scope that appending claims was defined.
Claims (1)
1. a preparation technology for methane, is characterized in that; Comprise unstripped gas purification process, refrigerant compression operation, Operation for liquefaction, LNG store operation; Wherein,
Unstripped gas purification process, for unstripped gas is carried out to purification run, and flows to liquefaction unit by purified gas and carries out Operation for liquefaction;
Wherein, described unstripped gas purification process adopts drying tower and filter to realize; After described unstripped gas drying tower, remove H2O, after filter carries out dust pretreatment, enter Operation for liquefaction;
Refrigerant compression operation, for nitrogen is carried out to supercharging cooling down operation, and is delivered to liquefaction unit by the cryogenic gas after swell refrigeration;
Wherein, described refrigerant compression operation adopts compressor, cooler and surge tank to realize; Described nitrogen, after nitrogen buffer tank carries out buffer operation, enters compressor and carries out boost operations, enters cooler and carry out cooling down operation after boost operations completes, and coldly goes the cryogenic gas after operation to be delivered to Operation for liquefaction and to use as cold-producing medium
Operation for liquefaction, for receiving from the unstripped gas of purification run with from the cryogenic gas of squeeze operation; Control unstripped gas and after cryogenic gas is cooling, carry out lock out operation, and the LNG of separation place is flowed to store operation;
Wherein, described Operation for liquefaction adopts heat exchanger, knockout drum and rectifying column to realize; Described unstripped gas carries out cooling down operation under the effect of described cryogenic gas, and entering knockout drum after cooling carries out lock out operation, and the gas of sub-department enters after rectifying column from tower top output hydrogen and nitrogen, from output LNG product at the bottom of tower and flow to store operation;
LNG store operation, for storing the LNG of Operation for liquefaction output to reclaim;
Wherein, the control mode that described unstripped gas purification process, refrigerant compression operation, Operation for liquefaction, LNG store operation adopt is for controlling on the spot the control mode combining with Central Control Room Long-distance Control, and Central Control Room is controlled and adopted DCS control system; Wherein, measurement and control operation, the operation of stopping in emergency are all carried out in described Central Control Room; Device parameter and running state parameter show in Central Control Room DCS display unit, go forward side by side line item and corresponding alarm operation; The operation of device start that described operation relates to is carried out with control mode on the spot.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310428523.1A CN103925771A (en) | 2013-09-21 | 2013-09-21 | Process for manufacturing methane |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310428523.1A CN103925771A (en) | 2013-09-21 | 2013-09-21 | Process for manufacturing methane |
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| CN103925771A true CN103925771A (en) | 2014-07-16 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104961097A (en) * | 2015-07-16 | 2015-10-07 | 浙江海天气体有限公司 | DCS (distributed control system) automatic control hydrogen purification system |
| CN106123486A (en) * | 2016-08-05 | 2016-11-16 | 成都赛普瑞兴科技有限公司 | The natural gas liquefaction being combined with distributed energy and system |
| CN108266963A (en) * | 2018-01-16 | 2018-07-10 | 中科睿凌江苏低温设备有限公司 | A kind of tail gas recycle prepares the device of liquefied natural gas |
| CN106091574B (en) * | 2016-06-02 | 2018-10-30 | 成都深冷液化设备股份有限公司 | Gas liquefaction device with compression heat recovery function and liquefaction method thereof |
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| CN103215093A (en) * | 2013-03-14 | 2013-07-24 | 上海交通大学 | Miniature skid type nitrogen expansion natural gas liquefaction system and method thereof |
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| CN102453570A (en) * | 2010-10-18 | 2012-05-16 | 袁俊海 | Nitrogen expanding refrigeration liquefaction process |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104961097A (en) * | 2015-07-16 | 2015-10-07 | 浙江海天气体有限公司 | DCS (distributed control system) automatic control hydrogen purification system |
| CN104961097B (en) * | 2015-07-16 | 2017-03-08 | 浙江海天气体有限公司 | DCS automatically controls hydrogen purification system |
| CN106091574B (en) * | 2016-06-02 | 2018-10-30 | 成都深冷液化设备股份有限公司 | Gas liquefaction device with compression heat recovery function and liquefaction method thereof |
| CN106123486A (en) * | 2016-08-05 | 2016-11-16 | 成都赛普瑞兴科技有限公司 | The natural gas liquefaction being combined with distributed energy and system |
| CN106123486B (en) * | 2016-08-05 | 2019-06-07 | 成都赛普瑞兴科技有限公司 | Natural gas liquefaction and system in conjunction with distributed energy |
| CN108266963A (en) * | 2018-01-16 | 2018-07-10 | 中科睿凌江苏低温设备有限公司 | A kind of tail gas recycle prepares the device of liquefied natural gas |
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Application publication date: 20140716 |