CN205603542U - System for flue gas system of utilization liquefied natural gas - Google Patents
System for flue gas system of utilization liquefied natural gas Download PDFInfo
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- CN205603542U CN205603542U CN201620350536.0U CN201620350536U CN205603542U CN 205603542 U CN205603542 U CN 205603542U CN 201620350536 U CN201620350536 U CN 201620350536U CN 205603542 U CN205603542 U CN 205603542U
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- flue gas
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Abstract
The utility model discloses a system for flue gas system of utilization liquefied natural gas, include: carbon dioxide recovery unit, gas holder, carbon dioxide recovery unit, compressor, methane synthesis reactor, liquefaction separator, liquefaction separator passes through the tube coupling with methane synthesis reactor. The technical scheme of the utility model the advantage be: be transformed into CH4 with the CO2 in the flue gas, reduced CO2's the emission while, increased liquefied natural gas's output, it is energy -concerving and environment -protective, the hydrogen rich gas that will liquefy among the separator returns to the gas holder, has increased the utilization ratio of hydrogen.
Description
Technical field
This utility model relates to waste gas recovery and utilizes field, particularly relates to one and utilizes flue gas system liquefaction sky
So system of gas.
Background technology
China is the first big coke production state in the world, and current coke aggregated capacity is about 500,000,000 tons, 2015
Coke output is 4.48 hundred million tons, and the oven gas of by-product enormous amount.These gas except personal, civilian and
Outside business-purpose fuel, the oven gas diffused every year is more than 20,000,000,000 m3。
Coke-oven gas methanation preparing natural gas has the function turned waste into wealth,
At present methanation process mainly has: the methanation technology of rope company of Top, wear dimension methanation technology and
The strange methanation technology in Shandong.Its dominant response is hydrogen and CO and CO2Reaction generates CH4And H2O is also put
Going out heat, reactive chemistry formula is:
CO+3H2→CH4+H2O △ H298K=-206.2KJ/mol
CO2+4H2→CH4+2H2O △ H298K=-165.0KJ/mol
The methane generated can make CNG can also be separated into liquefied natural gas by direct liquefaction, and reaction is released
Heat generation high temperature and high pressure steam.Owing to liquefied natural gas is under normal temperature and pressure the 1/625 of natural gas volume,
Therefore natural gas direct liquefaction can be greatly saved storage and transportation space and cost, means of transportation is the most flexible, and
And improve combustibility, successively along with the development of cryogenic separation technology, by gas liquefaction preparing liquefied natural gas
Application also get more and more.
Owing to the hydrogen in coke-stove gas is rich, and carbon is not enough, typical oven gas composition such as table
Shown in 1.
Table 1
| Composition | CH4 | N2 | CO2 | CO | H2 | C2H6 |
| Content, mol% | 24.7 | 4.5 | 2.8 | 7.4 | 57.8 | 2 |
For chemical plant, the source of carbon is the abundantest, and the most utilizable have flue gas, flue gas
Middle CO2Content is about 13%, and the typical composition of flue gas is as shown in table 2, CO2Directly discharge can increase temperature
Room effect, pollutes environment, brings significant wastage.
Table 2
| Composition | N2 | CO2 | CO | O2 | H2O |
| Content, mol% | 64.4 | 12.9 | 5.5 | 9.2 | 8 |
Utility model content
The technical problems to be solved in the utility model is to provide and a kind of can utilize cigarette with what flue gas made full use of
The system of road gas preparing liquefied natural gas.
The system utilizing flue gas preparing liquefied natural gas of the present utility model, including:
For reclaiming the carbon dioxide recovering apparatus of the carbon dioxide in flue gas, with flue gas source of the gas by pipe
Road connects；
For oven gas, carbon dioxide, hydrogen rich gas being mixed to get the gas holder of gaseous mixture, the air inlet of gas holder
It is connected by the first pipeline with oven gas source of the gas；The carbon dioxide vent of carbon dioxide recovering apparatus and gas holder
Air inlet by second pipeline connect；
For compressing the compressor of gaseous mixture, the air inlet of compressor is with the gas outlet of gas holder by pipeline even
Connect；
For making the methane synthesis reactor of the hydrogen in gaseous mixture and carbon dioxide reaction generation methane, with pressure
Contracting machine is connected by pipeline；
For separating treatment that the gaseous mixture of methanation is liquefied, the mixed gas separation of methanation is made to go out to liquefy natural
Gas, hydrogen rich gas and the liquefaction segregation apparatus of rich nitrogen, be connected by pipeline with methane synthesis reactor, liquefaction
The hydrogen rich gas outlet of segregation apparatus is connected by the 3rd pipeline with the air inlet of gas holder.
The system utilizing flue gas preparing liquefied natural gas of the present utility model, wherein, also includes: for mixed
Close gas purified treatment, make mixing QI prostration naphthalene, detar, the purifier of desulfurization, the air inlet of purifier
It is connected by pipeline with the gas outlet of compressor, the gas outlet of purifier and the air inlet of methane synthesis reactor
Mouth is connected by pipeline.
The system utilizing flue gas preparing liquefied natural gas of the present utility model, wherein, methane synthesis reactor with
It is provided with between liquefaction segregation apparatus for the gaseous mixture of methanation being dried pure before liquefaction separating treatment
Change processes, and makes the molecular sieve of the gaseous mixture dehydration decarburization of methanation, and molecular sieve is 4A molecular sieve or 13X divides
Son sieve.
The system utilizing flue gas preparing liquefied natural gas of the present utility model, wherein, compressor can be reciprocal
Compressor or helical-lobe compressor or centrifugal compressor.
The system utilizing flue gas preparing liquefied natural gas of the present utility model, wherein, carbon dioxide recovering apparatus
For amine absorption tower or pressure-swing absorber.
The advantage of the technical solution of the utility model is: by the CO in flue gas2It is transformed into CH4, reduce
CO2Discharge simultaneously, add the yield of liquefied natural gas, energy-conserving and environment-protective；To be liquefied segregation apparatus
In hydrogen rich gas be back to gas holder, add the utilization rate of hydrogen.
Accompanying drawing explanation
Fig. 1 is the structural representation of the system utilizing flue gas preparing liquefied natural gas of the present utility model.
Detailed description of the invention
As it is shown in figure 1, the system utilizing flue gas preparing liquefied natural gas of the present utility model, including:
For reclaiming the carbon dioxide recovering apparatus 1 of the carbon dioxide in flue gas, pass through with flue gas source of the gas
Pipeline connects；
For oven gas, carbon dioxide, hydrogen rich gas being mixed to get the gas holder 2 of gaseous mixture, the air inlet of gas holder
Mouth is connected by the first pipeline 11 with oven gas source of the gas；The carbon dioxide vent of carbon dioxide recovering apparatus
It is connected by the second pipeline 12 with the air inlet of gas holder；
For compressing the compressor 3 of gaseous mixture, the air inlet of compressor 3 passes through pipe with the gas outlet of gas holder 2
Road connects；
For making the methane synthesis reactor 4 of the hydrogen in gaseous mixture and carbon dioxide reaction generation methane, with
Compressor is connected by pipeline；
For separating treatment that the gaseous mixture of methanation is liquefied, the mixed gas separation of methanation is made to go out to liquefy natural
Gas, hydrogen rich gas and the liquefaction segregation apparatus 5 of rich nitrogen, be connected by pipeline with methane synthesis reactor, liquid
The hydrogen rich gas outlet changing segregation apparatus 5 is connected by the 3rd pipeline 13 with the air inlet of gas holder 2.
The system utilizing flue gas preparing liquefied natural gas of the present utility model, wherein, also includes: for mixed
Close gas purified treatment, make the purifier 6 of mixing QI prostration naphthalene, detar, desulfurization, entering of purifier 6
QI KOU is connected by pipeline with the gas outlet of compressor, the gas outlet of purifier 6 and methane synthesis reactor
Air inlet connected by pipeline.
The system utilizing flue gas preparing liquefied natural gas of the present utility model, wherein, methane synthesis reactor with
It is provided with between liquefaction segregation apparatus for the gaseous mixture of methanation being dried pure before liquefaction separating treatment
Change processes, and makes the molecular sieve 7 of the gaseous mixture dehydration decarburization of methanation, and molecular sieve 7 is 4A molecular sieve or 13X
Molecular sieve.
The system utilizing flue gas preparing liquefied natural gas of the present utility model, wherein, compressor 3 can be past
Compound compression machine or helical-lobe compressor or centrifugal compressor.
The system utilizing flue gas preparing liquefied natural gas of the present utility model, wherein, carbon dioxide recovering apparatus
1 is amine absorption tower or pressure-swing absorber.
The system utilizing flue gas preparing liquefied natural gas of the present utility model, wherein, liquefy segregation apparatus 5
For ice chest, the equipment inside ice chest is dehydrogenation tower and methane rectifier column.
The system utilizing flue gas preparing liquefied natural gas of the present utility model, wherein, purifier 6 includes living
Property charcoal adsorption tower and zinc oxide desulfurization tower, activated carbon adsorber can remove benzene naphthalene simultaneously, zinc oxide desulfurization
Tower is used for desulfurization.
When the technical solution of the utility model is implemented, from flue gas, extract CO2After, it is mixed into oven gas
In, mixed mixed air, after purifying compression, carries out methanation operation, in methanation operation, mixed
Close CO, the CO in gas2With hydrogen exothermic reaction, generate CH4, during due to gaseous mixture methanation, hydrogen
It is rich, therefore to provide the yield of methane, supplements CO from the external world2Seem the most necessary, and
The gas after methanation hydrogen after cryogenic separation, separation adds to methanation device again, improves first
The transformation efficiency of alkanisation, increases liquefied natural gas product output capacity, it is thus achieved that maximum economic benefit.
The workflow utilizing the system utilizing flue gas preparing liquefied natural gas of the present utility model is as follows: coke oven
Gas and the CO from carbon dioxide recovering apparatus 12Gas and the hydrogen rich gas from liquefaction segregation apparatus 5
After mixing, enter gas holder 2, be compressed to high pressure then in turn through compression section, then carry out cleaning procedure
De-naphthalene, detar, desulfurization, prevent these foreign gas from entering the methane synthetic reaction implementing methanation operation
Device, makes catalyst poisoning, and purified gas carries out methanation operation, hydrogen and one in methanation operation
Carbonoxide and the chemical reaction of carbon dioxide generation very exothermic, generate methane and water and release substantial amounts of heat
Amount, subsequently into molecular sieve, is dried purification procedures, the CO contained in removing gas2And H2O,
Make the dew point ＜-65 DEG C of oven gas, CO2Content ＜ 2ppm, finally carries out the separation circuit that liquefies, isolates
Liquefied natural gas product, hydrogen rich gas and rich nitrogen, liquefied natural gas product exports, and hydrogen rich gas is back to gas
Cabinet entrance.
The advantage of technical solutions of the utility model is:
(1) by the CO in flue gas2It is transformed into CH4, decrease CO2Discharge simultaneously, add liquid
Change the yield of natural gas, energy-conserving and environment-protective；
(2) hydrogen rich gas in liquefaction segregation apparatus is back to gas holder, adds the utilization rate of hydrogen.
Detailed description of the invention of the present utility model is:
Flue gas pressure is 1.03bar, flow is 10000Nm3/ h, component are as shown in table 2, purified after,
1290Nm3The CO of/h2Gas holder is entered with oven gas and hydrogen rich gas after mixing；The pressure of oven gas is
1.03bar, flow are 30000Nm3/ h, component are as shown in table 1；The pressure of hydrogen rich gas is 1.03bar, stream
Amount is 7295Nm3/ h, component are as shown in table 3.
Table 3 hydrogen rich gas component
| Composition | CH4 | H2 | N2 |
| Content, mol% | 0.5 | 78.8 | 20.7 |
Compressed operation is compressed to 25bar, then removes benzene, naphthalene and sulfur through cleaning procedure, by benzene, naphthalene,
The content of sulfur controls at 20ppm, 1ppm, below 0.1ppm, subsequently into methanation operation, methanation
Reaction, primary response equation is:
CO+3H2→CH4+H2O △ H298K=-206.2KJ/mol
CO2+4H2→CH4+2H2O △ H298K=-165.0KJ/mol
In methanation operation, it is possible to CO, CO2 are substantially converted to methane, the component after methanation
As shown in table 4, subsequently into dry purification procedures, the remaining CO after removing methanation2And H2O, really
Protect dew point ＜-65 DEG C, CO2Content ＜ 2ppm, finally enters liquefaction separation circuit, at liquefaction separation circuit
In, the mixed gas separation of methanation is gone out liquefied natural gas product, hydrogen rich gas and rich nitrogen.
Gas component after table 4 methanation
| Component | CH4 | N2 | CO | CO2 | H2 | C2H6 | C3H8 | H2O |
| Content, mol% | 28.4 | 8.6 | 0.0048 | 0.0052 | 15.1 | 1.63 | 0.03 | 46.23 |
In practice, oven gas does not supplement CO2If, liquefied natural gas (LNG)-throughput is about 11150Nm3/h,
Supplement 10000Nm3After the flue gas of/h, liquefied natural gas (LNG)-throughput is 12910Nm3/ h, output increased
15.8%.
Below it is only preferred implementation of the present utility model, it is noted that common for the art
For technical staff, on the premise of without departing from this utility model principle, it is also possible to make some improvement and profit
Decorations, these improvements and modifications also should be regarded as protection domain of the present utility model.
Claims (5)
1. the system utilizing flue gas preparing liquefied natural gas, it is characterised in that including:
For reclaiming the carbon dioxide recovering apparatus of the carbon dioxide in flue gas, with flue gas source of the gas by pipe
Road connects；
For oven gas, carbon dioxide, hydrogen rich gas being mixed to get the gas holder of gaseous mixture, the air inlet of gas holder
It is connected by the first pipeline with oven gas source of the gas；The carbon dioxide vent of carbon dioxide recovering apparatus and gas holder
Air inlet by second pipeline connect；
For compressing the compressor of gaseous mixture, the air inlet of compressor is with the gas outlet of gas holder by pipeline even
Connect；
For making the methane synthesis reactor of the hydrogen in gaseous mixture and carbon dioxide reaction generation methane, with pressure
Contracting machine is connected by pipeline；
For separating treatment that the gaseous mixture of methanation is liquefied, the mixed gas separation of methanation is made to go out to liquefy natural
Gas, hydrogen rich gas and the liquefaction segregation apparatus of rich nitrogen, be connected by pipeline with methane synthesis reactor, liquefaction
The hydrogen rich gas outlet of segregation apparatus is connected by the 3rd pipeline with the air inlet of gas holder.
Utilize the system of flue gas preparing liquefied natural gas the most as claimed in claim 1, it is characterised in that
Also include: for gaseous mixture purified treatment, make mixing QI prostration naphthalene, detar, the purifier of desulfurization,
The air inlet of purifier is connected by pipeline with the gas outlet of compressor, the gas outlet of purifier and methane
The air inlet of synthesis reactor is connected by pipeline.
Utilize the system of flue gas preparing liquefied natural gas the most as claimed in claim 2, it is characterised in that
Methane synthesis reactor and liquefaction segregation apparatus between be provided with for liquefaction separating treatment before to methane
The gaseous mixture changed is dried purification process, makes the molecular sieve of the gaseous mixture dehydration decarburization of methanation, and molecular sieve is
4A molecular sieve or 13X molecular sieve.
Utilize the system of flue gas preparing liquefied natural gas the most as claimed in claim 3, it is characterised in that
Compressor can be reciprocating compressor or helical-lobe compressor or centrifugal compressor.
Utilize the system of flue gas preparing liquefied natural gas the most as claimed in claim 4, it is characterised in that
Carbon dioxide recovering apparatus is amine absorption tower or pressure-swing absorber.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620350536.0U CN205603542U (en) | 2016-04-22 | 2016-04-22 | System for flue gas system of utilization liquefied natural gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620350536.0U CN205603542U (en) | 2016-04-22 | 2016-04-22 | System for flue gas system of utilization liquefied natural gas |
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| CN205603542U true CN205603542U (en) | 2016-09-28 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109609220A (en) * | 2018-11-29 | 2019-04-12 | 山西易高煤层气有限公司 | A kind of method of coal bed gas LNG natural gas |
-
2016
- 2016-04-22 CN CN201620350536.0U patent/CN205603542U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109609220A (en) * | 2018-11-29 | 2019-04-12 | 山西易高煤层气有限公司 | A kind of method of coal bed gas LNG natural gas |
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|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |