CN103043609B - Liquid nitrogen washing device with function of producing natural gas - Google Patents
Liquid nitrogen washing device with function of producing natural gas Download PDFInfo
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- CN103043609B CN103043609B CN201210564062.6A CN201210564062A CN103043609B CN 103043609 B CN103043609 B CN 103043609B CN 201210564062 A CN201210564062 A CN 201210564062A CN 103043609 B CN103043609 B CN 103043609B
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Abstract
The invention discloses a liquid nitrogen washing device with a function of producing natural gas, which comprises a first feed gas cooler 1, a second feed gas cooler 2, a nitrogen washing tower 3, a purifying synthesis gas pipe and a demethanizer 3, wherein the purifying synthesis gas pipe runs through the first feed gas cooler 1 and the second feed gas cooler 2 in sequence; the demethanizer 3 is provided with an air inlet end, an air outlet end and a fraction output end; the purifying synthesis gas pipe is communicated with the air inlet end after running through the second feed gas cooler; and the air outlet end is communicated with the nitrogen washing tower 3 through a pipe. The liquid nitrogen washing device with the function of producing natural gas is capable of recycling methane generated during the process of coal gasification and manufacturing the methane into natural gas, which not only realizes the goal of obtaining clean natural gas containing about 99% of methane while producing refined ammonia synthesis gas, but also adds a new product variety and increases the business opportunity of a factory.
Description
Technical field
The present invention relates to coal chemical technology, for the synthetic gas process for refining of synthetic ammonia processed, particularly relate to the liquid nitrogen washing device that a kind of double system produces Sweet natural gas.
Background technology
Coal obtains raw gas through gasification workshop section, raw gas enters low temperature washing device for methanol after conversion section, after low temperature washing device for methanol removes sour gas, be purified synthetic gas, decontaminating syngas enters the material synthesis gas obtaining synthetic ammonia after liquid nitrogen washing device removes trace amounts of CO etc.
At present, domestic " liquid nitrogen washing device " refining synthetic gas for coal chemical technology, synthetic ammonia processed is all the CO for removing in decontaminating syngas.But while washing lower CO, CH
4also washed down with Ar, and with excessive liquid N
2mix, the fuel gas of this mixture all as factory after re-heat.Containing higher CO in this fuel gas.
There is following problem in prior art:
1. usual, if methane concentration≤1% in the decontaminating syngas entering liquid nitrogen washing device, liquid nitrogen washing device can safe handling; If methane concentration >=1% or higher time, then very easily under-180 DEG C or lower temperature, there is the ice that CH4 freezes to solidify and block up phenomenon, and cause the parking of device and factory be forced to stop.
At ambient pressure, pure CH
4boiling point-162 DEG C, freezing point (or claim solidification point)-182 DEG C.At low temperature and pressurization under the operational condition namely in liquid nitrogen washing, CH
4then liquefy (working pressure depending primarily on system and CH in the decontaminating syngas entering liquid nitrogen washing device from-127 DEG C (very causing in also having from-92 DEG C)
4concentration), its freezing point temperature also can raise with the increase of working pressure.
But the service temperature that feeding gas is going out the final stage plate-fin heat exchanger of liquid nitrogen washing device (i.e. the present invention second feed gas chiller E04305) is generally about-186 DEG C.It is at that time improper to control at underload or operation especially, and the cold in system there will be surplus, thus just the CH in feeding gas very easily occurs
4, solidify in final stage plate-fin heat exchanger and freezingly block its passage.Thus the parking because of liquid nitrogen washing device forces the parking of factory, its similar accident had generation in certain factory.、
2. if still adopt the way of former liquid nitrogen washing device, CH4 is not removed separately, even if suppose that it there will not be CH
4ice block up, then can be excessive because of fuel quantity, there will be that supply exceed demand; Extract part out and make domestic fuel then containing higher CO (CO content can exceed the safety standards of domestic fuel), and also should not do.Certainly be also not suitable for being carried this its by pipe network, otherwise the effusion that CO can occur causes the security incident of " carbon monoxide poisoning ".
3. large-scale coal gasification plant is refined in the technique of ammonia synthesis gas in liquid nitrogen washing and (especially in raw gas, is contained cut CH
4time higher), if the fuel gas cut that liquid nitrogen washing device is discharged all is delivered to the fuel gas system of factory, a large amount of burning and exhausting of accident flare system in factory can be caused too greatly because of tolerance.Thus, not only can cause the waste of the energy, also add CO
2quantity discharged.
Summary of the invention
Object of the present invention solve exactly when CH4 content >=1% in decontaminating syngas or higher time (as in the raw gas that lurgi pressure gasification, KBR pressurized gasification or other gasification process etc. are made containing about 2% (butt meter) and above methane), methane solidifies frozen block in the ice chest of liquid nitrogen washing device, cause liquid nitrogen washing device cannot the problem of normal running, by-product high-purity methane can be realized simultaneously, high-purity methane is clean fuel---and Sweet natural gas, post liquefaction i.e. " LNG " (natural gas liquids).
The system of holding concurrently produces the liquid nitrogen washing device of Sweet natural gas, comprise the first feed gas chiller 1, second feed cooler 2, nitrogen wash column 3 and decontaminating syngas pipeline, described decontaminating syngas pipeline flows through the first feed gas chiller 1 and the second feed cooler 2 successively, also comprise demethanizing tower 5, described demethanizing tower 5 establishes inlet end, outlet side and cut output terminal, connect described inlet end after described decontaminating syngas pipeline flows through the second feed cooler with described inlet end, middle part that outlet side, cut output terminal lay respectively at described demethanizing tower 5, top and bottom.
Described double system produces the liquid nitrogen washing device of Sweet natural gas, also comprise elevated pressure nitrogen water cooler 4 and tower reactor fraction seperation device 6, described tower reactor fraction seperation device 6 is provided with the first separator input terminus, the first liquid phase output and the first gas phase outlet, described first separator input terminus connects described cut output terminal by pipeline, described first liquid phase output is connected Sweet natural gas delivery conduit with the first gas phase outlet, and described Sweet natural gas delivery conduit flows through the second feed cooler 2, first feed gas chiller 1 and elevated pressure nitrogen water cooler 4 successively.
Described double system produces the liquid nitrogen washing device of Sweet natural gas, also comprise trim the top of column separator 7, described trim the top of column separator 7 establishes the second separator input terminus, second liquid phase output terminal and the second gas phase outlet, described second separator input terminus is by outlet side described in pipeline connection, and described second gas phase outlet is by nitrogen wash column 3 described in pipeline connection; Liquid-phase reflux end established by described demethanizing tower, and described second liquid phase output terminal is by liquid-phase reflux end described in pipeline connection.
Described liquid-phase reflux end is positioned at the top of described demethanizing tower.
The pipeline that described second liquid phase output terminal is communicated with liquid-phase reflux end establishes liquid phase pump 9.
The pipeline that described outlet side is communicated with the second separator input terminus flows through described second feed cooler 2, and the pipeline that described second gas phase outlet is communicated with nitrogen wash column 3 flows through described second feed cooler 2.
Described demethanizing tower 5 tower reactor is provided with reboiler 8.
Still liquid recycle pump 10 established by described reboiler 8.
Described decontaminating syngas pipeline flows through the first feed gas chiller 1, reboiler, the first feed gas chiller 1, second feed gas chiller 2 successively.
The present invention owing to being provided with demethanizing tower in ice chest, utilize the cold in traditional liquid nitrogen washing, before-180 DEG C, the methane in feeding gas (containing methane >=5%) is separated before entering nitrogen wash column, therefore solid-state methane ice would not be had again to block up the situation of device channels there is the low-temperature condition lower than-180 DEG C in rear system under, middle appearance blocks up the situation of device channels lower than there being solid-state methane ice under the low-temperature condition of-180 DEG C again, guarantees safety in production and the long period continuous seepage of factory.
Because the methane fraction separated meets the national standard of Sweet natural gas, therefore directly can send into weather sale pipe network; In addition CH
4after cut is separated separately in time, effectively avoid methane under zero pour, solidify the long period stable operation that ice blocked up, ensure that ice chest.
The present invention holds concurrently and makes the liquid nitrogen washing device of production Sweet natural gas, the methane recovery generated in coal gasification course is made Sweet natural gas, can realize while refining ammonia synthesis gas, also obtain the clean Sweet natural gas containing methane about 99%, Ye Shi factory increases by a new range of product, adds the business opportunity of factory.
Accompanying drawing explanation
Fig. 1 is that the present invention's system of holding concurrently produces the schematic diagram of liquid nitrogen washing device of Sweet natural gas.
Description of reference numerals:
In figure, 1 is the first feed gas chiller, and 2 is the second feed cooler, and 3 is nitrogen wash column, and 4 is elevated pressure nitrogen water cooler, and 5 is demethanizing tower, and 6 is tower reactor fraction seperation device, and 7 is trim the top of column separator, and 8 is reboiler, and 9 is liquid phase pump, and 10 is still liquid recycle pump.
Embodiment
Embodiment 1
Decontaminating syngas is introduced in the molecular sieve adsorber in liquid nitrogen washing device, the CO of its contained trace
2and CH
3oH is adsorbed in adsorber.Afterwards, decontaminating syngas (3-001 flows stock) then enters the first feed gas chiller in " ice chest ", is cooled to about-128 DEG C by several bursts of re-heat logistics; Then enter the second feed gas chiller to continue again to be cooled to about-155 DEG C by several bursts of re-heat logistics and the middle part of extracting, delivering to demethanizing tower from the middle part of the second feed gas chiller out enters tower.Now, tower logistics is entered close to bubble point state and containing a small amount of liquid phase: vapor phase stream is to tower top, and liquid phase then flows to tower reactor.
Enter tower reactor fraction seperation device after tower reactor cut (i.e. Sweet natural gas) decompression, the gas/liquid two-phase of separation and water cooler re-heat are to normal temperature 30 DEG C and the natural gas storage tank delivered to outside battery limit (BL) or gas distributing system.3-011 during its gaseous constituent and quantity see attached list flows stock.
The tower reactor of demethanizing tower is provided with reboiler, and the thermal source system of reboiler is provided by the hot logistics (from the decontaminating syngas of low-temperature rectisol, seeing schema) in the first feed gas chiller, and returns demethanizing tower by still liquid recycle pump pump circulation.The overhead gas of demethanizing tower is sent in the second feed gas chiller, continue to be cooled to about-178 DEG C by several bursts of re-heat logistics from about-158 DEG C after, extract out from the second feed gas chiller again, then deliver to the trim the top of column separator of demethanizing tower.In trim the top of column separator, gas/liquid two-phase laminated flow: liquid phase pump pressure is sent into demethanizing tower and made phegma; Gas phase is (containing CH
4be about: 1%) be the synthetic gas after demethanizing then send back to again second feed gas chiller continue be cooled to about-187 DEG C by several bursts of re-heat logistics after (because of CH
4content only 1%, owing to there being the N of considerable part
2liquefaction, and there will not be condensation ice block up), as nitrogen wash column (C04301) bottom feeding gas.
The structure of demethanizing tower and size: Φ 1600-1100; H (tangent line height) about 30000; Theoretical plate number: 12; Plate efficiency: 0.33; Tray type: 25 × 25 square float valves.
Gas after the demethanizing of the bottom of nitrogen wash column rises along tower, by from CO and Ar etc. under the liquid nitrogen washing of tower top contained by it.
Discharge purified gas from the top of nitrogen wash column, it is containing CO≤3ppm, and temperature about-189 DEG C first through the second feed gas chiller re-heat, then makes its H through joining nitrogen mixing tank (SP04301)
2/ N
2after being about 3/1, be divided into two strands again: one returns cold to low temperature washing device for methanol, another stock then sends ice chest through the re-heat of elevated pressure nitrogen water cooler to 30 DEG C.Two strands of gases converge outside ice chest, then join nitrogen through essence and make its H
2/ N
2than being 3/1, arriving subsequent processing afterwards---ammonia synthesis.
Go out the pressure of the refining synthetic gas of liquid nitrogen washing: 2.85Mpa, temperature: 30 DEG C, and very clean.Its gaseous constituent and quantity as follows: 3-040 in seeing attached list flows number of share of stock certificate.
The liquid phase of discharging from the still portion of nitrogen wash column enters tower reactor separator.At tower reactor separator, be divided into gas/liquid two-phase: gas phase is the H dissolved
2through the second feed gas chiller, the first feed gas chiller and the re-heat of elevated pressure nitrogen water cooler to 30 DEG C, send ice chest and pressurize to the recycle gas compressor of low temperature washing device for methanol; Liquid phase system (the excessive liquid N of CO+Ar+
2) etc. send ice chest and to the fuel gas pipe network of factory through the second feed gas chiller, the first feed gas chiller and the re-heat of elevated pressure nitrogen water cooler to 30 DEG C.
Elevated pressure nitrogen both available pressures of liquid nitrogen washing: 5.0Mpa, temperature: about 40 DEG C, also available pressure: 3.0Mpa, temperature: about 40 DEG C.Unlike: if by pressure: 3.0Mpa, temperature: the nitrogen of about 40 DEG C, than by pressure: 5.0Mpa, temperature: the required cold confessed to ice chest of the nitrogen of about 40 DEG C is more, and the liquid nitrogen that namely will supplement to system is more, and this is high pressure N
2be incorporated to H
2the result of Shi Fasheng J-T effect.
Native system selects the pressure of elevated pressure nitrogen: 5.0Mpa, temperature: about 40 DEG C.
Elevated pressure nitrogen by elevated pressure nitrogen water cooler, the first feed gas chiller and part by the second feed gas chiller be as cold as-186 DEG C become liquid nitrogen after, send the top of nitrogen wash column, as the washings of nitrogen wash column; Do not cooled by the second feed gas chiller, namely extract out from the outlet of the first feed gas chiller, flow through and join nitrogen mixing tank (SP04301), carry out gas with the tower top from nitrogen wash column and mix, and make the H in gas mixture
2/ N
23/1 is about than reaching.
The cold of system is not enough, then provide by liquid nitrogen and maintain balance.
This liquid nitrogen (pressure is: 0.25Mpa) is from air separation facility.
Liquid nitrogen is introduced into tower reactor fraction seperation device, and gas/liquid then enters the second feed gas chiller, the first feed gas chiller and elevated pressure nitrogen water cooler respectively afterwards.Its pressure is: 0.20Mpa gasified, heating, and after surrendering cold, about 0.15Mpa, can deliver to the low pressure N2 gas pipe network of full factory.
When high pressure nitrogen selects the pressure of 5.0Mpa, the amount of liquid nitrogen that native system (comprising the cold damage of system) will supplement: 4740Kg/h, namely needs external system semen donors to be: 550Kw.
Claims (8)
1. system of holding concurrently produces the liquid nitrogen washing device of Sweet natural gas, comprise the first feed gas chiller (1), second feed cooler (2), nitrogen wash column (3) and decontaminating syngas pipeline, described decontaminating syngas pipeline flows through the first feed gas chiller (1) and the second feed cooler (2) successively, characterized by further comprising demethanizing tower (5), inlet end established by described demethanizing tower (5), outlet side and cut output terminal, be communicated with described inlet end after described decontaminating syngas pipeline flows through the second feed cooler, described outlet side and described nitrogen wash column (3) pass through pipeline connection,
Described demethanizing tower (5) tower reactor is provided with reboiler (8), and the thermal source system of described reboiler (8) is provided by the hot logistics in the first feed gas chiller;
Also comprise elevated pressure nitrogen water cooler (4) and tower reactor fraction seperation device (6), described tower reactor fraction seperation device (6) is provided with the first separator input terminus, the first liquid phase output and the first gas phase outlet, described first separator input terminus connects described cut output terminal by pipeline, described first liquid phase output is connected Sweet natural gas delivery conduit with the first gas phase outlet, and described Sweet natural gas delivery conduit flows through the second feed gas chiller (2), the first feed cooler (1) and elevated pressure nitrogen water cooler (4) successively.
2. double system according to claim 1 produces the liquid nitrogen washing device of Sweet natural gas, it is characterized in that described inlet end, middle part that outlet side, cut output terminal lay respectively at described demethanizing tower (5), top and bottom.
3. double system according to claim 2 produces the liquid nitrogen washing device of Sweet natural gas, characterized by further comprising trim the top of column separator (7), described trim the top of column separator (7) establishes the second separator input terminus, second liquid phase output terminal and the second gas phase outlet, described second separator input terminus is by outlet side described in pipeline connection, and described second gas phase outlet is by nitrogen wash column (3) described in pipeline connection; Liquid-phase reflux end established by described demethanizing tower, and described second liquid phase output terminal is by liquid-phase reflux end described in pipeline connection.
4. double system according to claim 3 produces the liquid nitrogen washing device of Sweet natural gas, it is characterized in that described liquid-phase reflux end is positioned at the top of described demethanizing tower.
5. double system according to claim 3 produces the liquid nitrogen washing device of Sweet natural gas, it is characterized in that the pipeline that described second liquid phase output terminal is communicated with liquid-phase reflux end establishes liquid phase pump (9).
6. double system according to claim 3 produces the liquid nitrogen washing device of Sweet natural gas, it is characterized in that the pipeline that described outlet side is communicated with the second separator input terminus flows through described second feed cooler (2), the pipeline that described second gas phase outlet is communicated with nitrogen wash column (3) flows through described second feed cooler (2).
7. double system according to claim 1 produces the liquid nitrogen washing device of Sweet natural gas, it is characterized in that still liquid recycle pump (10) established by described reboiler (8).
8. double system according to claim 1 produces the liquid nitrogen washing device of Sweet natural gas, it is characterized in that described decontaminating syngas pipeline flows through the first feed gas chiller (1), reboiler, the first feed gas chiller (1), the second feed gas chiller (2) successively.
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| CN201210564062.6A CN103043609B (en) | 2012-12-24 | 2012-12-24 | Liquid nitrogen washing device with function of producing natural gas |
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| CN201210564062.6A CN103043609B (en) | 2012-12-24 | 2012-12-24 | Liquid nitrogen washing device with function of producing natural gas |
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| CN103043609B true CN103043609B (en) | 2015-01-21 |
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Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105157348B (en) * | 2015-08-17 | 2017-06-23 | 杭州中泰深冷技术股份有限公司 | The liquid nitrogen washing device and its method of a kind of recovery LNG |
| CN106185801B (en) * | 2016-07-04 | 2018-10-16 | 华陆工程科技有限责任公司 | A kind of scrubbing with liquid nitrogen devices and methods therefor that can recycle methane |
| CN106642988B (en) * | 2016-12-07 | 2022-07-05 | 中科瑞奥能源科技股份有限公司 | System for utilize liquid nitrogen to wash and prepare synthetic ammonia feed gas and LNG |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3801712A1 (en) * | 1988-01-21 | 1989-07-27 | Linde Ag | Process for purifying a gas mixture |
| DE3815866A1 (en) * | 1988-05-09 | 1989-11-23 | Linde Ag | Process for purifying a crude gas for the ammonia synthesis by means of a nitrogen scrub |
| US4917716A (en) * | 1988-01-28 | 1990-04-17 | Linde Aktiengesellschaft | Process for purifying a gaseous mixture |
| KR20060096494A (en) * | 2003-09-30 | 2006-09-11 | 오르트로프 엔지니어스, 리미티드 | Liquified natural gas processing |
| CN201729816U (en) * | 2009-12-02 | 2011-02-02 | 北京新峰泰克工程技术有限公司 | Liquid nitrogen washing device for purifying synthesis gas |
| CN102295960A (en) * | 2011-06-21 | 2011-12-28 | 杭州中泰深冷技术股份有限公司 | Apparatus and method for purifying synthetic gas with liquid nitrogen |
| CN102353233A (en) * | 2011-08-03 | 2012-02-15 | 成都蜀远煤基能源科技有限公司 | Process method and device for cryogenically separating and liquefying gas obtained after coal gas methanation |
-
2012
- 2012-12-24 CN CN201210564062.6A patent/CN103043609B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3801712A1 (en) * | 1988-01-21 | 1989-07-27 | Linde Ag | Process for purifying a gas mixture |
| US4917716A (en) * | 1988-01-28 | 1990-04-17 | Linde Aktiengesellschaft | Process for purifying a gaseous mixture |
| DE3815866A1 (en) * | 1988-05-09 | 1989-11-23 | Linde Ag | Process for purifying a crude gas for the ammonia synthesis by means of a nitrogen scrub |
| KR20060096494A (en) * | 2003-09-30 | 2006-09-11 | 오르트로프 엔지니어스, 리미티드 | Liquified natural gas processing |
| CN201729816U (en) * | 2009-12-02 | 2011-02-02 | 北京新峰泰克工程技术有限公司 | Liquid nitrogen washing device for purifying synthesis gas |
| CN102295960A (en) * | 2011-06-21 | 2011-12-28 | 杭州中泰深冷技术股份有限公司 | Apparatus and method for purifying synthetic gas with liquid nitrogen |
| CN102353233A (en) * | 2011-08-03 | 2012-02-15 | 成都蜀远煤基能源科技有限公司 | Process method and device for cryogenically separating and liquefying gas obtained after coal gas methanation |
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