CN202898374U - Liquefied natural gas production device - Google Patents
Liquefied natural gas production device Download PDFInfo
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- CN202898374U CN202898374U CN2012205380592U CN201220538059U CN202898374U CN 202898374 U CN202898374 U CN 202898374U CN 2012205380592 U CN2012205380592 U CN 2012205380592U CN 201220538059 U CN201220538059 U CN 201220538059U CN 202898374 U CN202898374 U CN 202898374U
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- natural gas
- hydrogen
- oven
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 39
- 239000003949 liquefied natural gas Substances 0.000 title abstract description 25
- 239000007789 gas Substances 0.000 claims abstract description 79
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 58
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 47
- 239000001257 hydrogen Substances 0.000 claims abstract description 46
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 32
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 30
- 239000000571 coke Substances 0.000 claims abstract description 29
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 16
- 239000000446 fuel Substances 0.000 claims abstract description 12
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 239000002994 raw material Substances 0.000 claims abstract description 9
- 239000006227 byproduct Substances 0.000 claims abstract description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 4
- 238000010438 heat treatment Methods 0.000 claims abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 3
- 239000007788 liquid Substances 0.000 claims description 28
- 239000003345 natural gas Substances 0.000 claims description 28
- 238000009434 installation Methods 0.000 claims description 22
- 235000011089 carbon dioxide Nutrition 0.000 claims description 17
- 238000000746 purification Methods 0.000 claims description 6
- 238000010521 absorption reaction Methods 0.000 claims description 5
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 3
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 3
- 239000004571 lime Substances 0.000 claims description 3
- 239000012528 membrane Substances 0.000 claims description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 7
- 239000001569 carbon dioxide Substances 0.000 abstract description 7
- 238000007670 refining Methods 0.000 abstract description 3
- 239000000047 product Substances 0.000 description 19
- 230000000052 comparative effect Effects 0.000 description 12
- 238000000034 method Methods 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 238000010276 construction Methods 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 239000000470 constituent Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000003245 coal Substances 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000001465 metallisation Methods 0.000 description 1
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Abstract
The utility model provides a liquefied natural gas production device which takes coke-oven gas as a main raw material and sequentially comprises a gas refining unit, a conversion reaction unit and a liquefaction unit, wherein the conversion reaction unit is used for converting water and carbon monoxide into hydrogen and carbon dioxide, and a carbonic acid removal unit for removing carbon dioxide and a hydrogen separation unit for selectively separating hydrogen are arranged between the conversion reaction unit and the liquefaction unit. The liquefied natural gas production device can increase the yield of hydrogen as well as the yield of carbon dioxide which is used as a raw material when the coke-oven gas is used for producing SNG (Synthetic Natural Gas). The liquefied natural gas production device can increase the heating value of byproduct non-condensable gas in the liquefaction unit to a certain degree, and facilitates that the non-condensable gas is conveyed to a coke oven so that the non-condensable gas serves as a fuel of the coke oven to be used, thus the operation efficiency of the liquefied natural gas production device can be further improved.
Description
Technical field
The utility model relates to natural gas liquids (LNG) manufacturing installation take coke(oven)gas (COG) as main raw material, relates in particular to the device of coproduction hydrogen in the manufacturing of the natural gas liquids take coke(oven)gas as main raw material.
Background technology
At present, in China, large-scale coke oven occurred in various places take abundant coal resource as background, SNGization is also being carried out energetically, and the technique of being made LNG by COG reaches its maturity.In addition, also someone studies the hydrogen composition by containing among the separation of C OG, makes simultaneously the technology of hydrogen with LNG.
At present, to separate again the method for remaining hydrogen composition after LNG is made in existing methanation through COG and in order reducing production costs, COG to be made with extra care the rear method of directly making LNG without methanation.These two kinds of methods are according to still being selected use take hydrogen as the major objective product take LNG as the major objective product.
Particularly, for the hydrogen composition by containing among the separation of C OG, thereby make simultaneously the technology of hydrogen with LNG, if having the methanation operation, then construction cost is higher, in addition, in hope hydrogen during as product separation, is difficult to obtain the hydrogen of q.s.Therefore, in order to reduce production costs or when high to the demand of hydrogen, as mentioned above, can to consider to adopt and directly make the method for LNG without methanation after COG is refining.
For example, at patent documentation 1(CN101747131A) in put down in writing and will remove CO by acid gas absorption tower through the coke(oven)gas of gas purification
2After (causing stopping up because it can solidify in the LNG liquefaction unit), after with hydrogen separation membrane the hydrogen in the product gas slightly being carried, the technology of producing LNG through liquefaction unit.
In addition, at patent documentation 2(CN102031159A) in put down in writing from coke(oven)gas except behind the impurity such as desulfuration composition and tar ingredients the technology that directly liquefies.And owing to not containing the unit such as hydrogen separation, so in non-condensable gases, contain a large amount of hydrogen, CO, therefore proposed its fuel as coke oven is utilized.
Yet, in the invention of patent documentation 1, although in order to prevent the obstruction in the LNG liquefaction unit, removed CO
2, but for the CO in the gas, do not consider to convert thereof into CO
2The feasibility of processing, and only be after it is reclaimed as non-condensable gases, utilization acts as a fuel.And CO can reduce the thermal value of non-condensable gases, to being disadvantageous with non-condensable gases as the fuel utilization of coke oven.Therefore, this is in efficient utilization of resource, positive existing problems aspect the recovery.
And in the invention of patent documentation 2, especially the operation of removing about carbonic acid gas does not have any record, so will stop up because of solidifying of carbonic acid gas in the LNG liquefaction operation.And, as patent documentation 1, for the CO in the gas, do not consider to convert thereof into CO
2The feasibility of processing, and only be after it is reclaimed as non-condensable gases, utilization acts as a fuel.And CO can reduce the thermal value of non-condensable gases, to being disadvantageous with non-condensable gases as the fuel utilization of coke oven.Therefore, this is at efficient utilization of resource, actively have problems too aspect the recovery.
The prior art document
Patent documentation 1:CN101747131A
Patent documentation 2:CN102031159A
The utility model content
In view of above-mentioned condition, problem of the present utility model is, during co-producing hydrogen, increases the output of hydrogen and carbon dioxide in the manufacturing of the natural gas liquids take coke(oven)gas as raw material.In addition, make the to a certain extent gain of heat of non-condensable gases in the liquefaction unit, thereby be conducive to effectively utilize as the fuel of coke oven.
In order to solve above-mentioned problem, in the utility model, by utilizing conversion reaction before the decarbonate unit, to make hydrogen and CO the CO gas in the coke(oven)gas
2Thereby, make the hydrogen volume increase, and simultaneously volume increase can be used as the carbonic acid gas of product.So, remove as product after can converting thermal value CO gas lower, that belong to a reason of the thermal value that reduces non-condensable gases to hydrogen and carbonic acid gas, can also expect to improve to a certain extent the effect of the thermal value of non-condensable gases, resulting non-condensable gases can be conducive to effectively utilize as the fuel of coke oven.
That is, the utility model provides a kind of manufacturing installation of natural gas liquids, it is characterized in that, is the manufacturing installation of the natural gas liquids take coke(oven)gas as main raw material, comprises successively such as lower unit: gas purification unit, conversion reaction unit and liquefaction unit, wherein,
Described conversion reaction unit is to make water and carbon monoxide convert the unit of hydrogen and carbonic acid gas to,
And, between described conversion reaction unit and described liquefaction unit, be provided with the decarbonate unit of removing carbonic acid gas and the hydrogen separating unit that hydrogen is carried out selective separation.
According to the utility model, by the gas take coke(oven)gas as main raw material is refining through the gas purification unit, and CO and H that will be wherein in the conversion reaction unit
2O converts CO to
2And H
2, then with the CO that obtains
2And H
2In decarbonate unit, hydrogen separating unit, remove and reclaim respectively, then carry out LNGization in liquefaction unit, thus, can make the hydrogen volume increase, can be used as product and reclaim highly purified hydrogen, and simultaneously volume increase can be used as the carbonic acid gas of product.Simultaneously, the non-condensable gases of by-product in the liquefaction unit, because the major part of the hydrogen that thermal value is lower (also comprising the hydrogen by the CO conversion) is removed, and compare with the non-condensable gases in the conventional art, because the conversion of CO, its content has also significantly obtained minimizing, so can expect to improve to a certain extent the effect of the thermal value of non-condensable gases.
In the manufacturing installation of natural gas liquids of the present utility model, carbonic acid gas is removed so that the concentration of the carbonic acid gas in the gas of the ingress of described liquefaction unit becomes the following mode of 50ppm in preferred described decarbonate unit.
According to the utility model, by described decarbonate unit, preferably with CO
2Removing to its concentration is below the 50ppm, to prevent thus in the liquefaction unit because of CO in the gas of the ingress of liquefaction unit
2Solidify and the problem stopped up.
In the manufacturing installation of natural gas liquids of the present utility model, preferably also be provided with the non-condensable gases transfer lime, be used for and be delivered to coke oven at the non-condensable gases of described liquefaction unit by-product as the fuel of coke oven, sneak in the rich gas of heating coke oven.
According to the utility model, because can expect to make the to a certain extent gain of heat of non-condensable gases of by-product in the liquefaction unit, by the non-condensable gases transfer lime, non-condensable gases is delivered to coke oven as the fuel utilization of coke oven, thereby can further improve the operational efficiency of the manufacturing installation of natural gas liquids.
In the manufacturing installation of natural gas liquids of the present utility model, described hydrogen separating unit is preferably and is selected from least a in pressure-swing absorption apparatus (PSA) and the membrane separation unit.
In the utility model, the high situation of demand of reply hydrogen in the LNG metallization processes take COG as raw material in the technology of coproduction hydrogen, is omitted the methanation unit and has been promoted competitive power.And, by the Combination conversion reaction member, realized the volume increase of hydrogen and carbonic acid gas.In addition, because can expect the to a certain extent gain of heat of non-condensable gases in the liquefaction unit, be conducive to non-condensable gases and effectively utilize as the fuel of coke oven, thereby can further improve operational efficiency.
Description of drawings
Fig. 1 is the schematic diagram of the manufacturing installation of the expression natural gas liquids that uses the utility model embodiment 1.
Fig. 2 is the schematic diagram of comparative example 1 of an example that represents the manufacturing installation of natural gas liquids in the past.
Fig. 3 is the schematic diagram of another routine comparative example 2 that represents the manufacturing installation of natural gas liquids in the past.
Embodiment
The below is described in detail the utility model with specific embodiment, but following embodiment is only used for illustrating concrete implementation method of the present utility model, and those skilled in the art can not break away from fully in the situation of purport of the present utility model and carry out various changes and replacing.And, in order to further specify effect of the present utility model, put down in writing as a comparison 2 prior aries as a comparative example 1 and 2.
Embodiment 1
Fig. 1 is the schematic diagram of manufacturing installation of the natural gas liquids of expression the utility model embodiment 1.
As shown in Figure 1, the manufacturing installation of the natural gas liquids of embodiment 1 comprises successively such as lower unit: gas purification unit, conversion reaction unit, decarbonate unit (acid gas absorption tower), hydrogen separating unit (H
2PSA), compressed element, dewatering unit and liquefaction unit.Wherein, carry out following conversion reaction in the conversion reaction unit.
CO+H
2O→H
2+CO
2
Use the manufacturing installation of the natural gas liquids of embodiment 1, to the coke(oven)gas of the composition of record in the table 1 gas 10000m as principal constituent
3/ hr has made natural gas liquids as unstripped gas.
Particularly, unstripped gas enters in the conversion reaction unit after the gas purification unit is made with extra care, and makes carbon monoxide be converted to H by conversion reaction
2And CO
2, then enter in the acid gas absorption tower, remove CO
2, make CO
2Concentration becomes below the 50ppm, then enters H
2PSA removes most H
2After, compressed unit, dewatering unit supply to liquefaction unit, thereby make LNG.
The thermal value of its product LNG amount, product hydrogen amount, the product carbon dioxide gas scale of construction, non-condensable gases is shown in table 2.
Comparative example 1
Fig. 2 is the schematic diagram of comparative example 1 of an example that represents the manufacturing installation of natural gas liquids in the past.
Utilize the device of comparative example 1, the coke(oven)gas of the composition of record in table 1 is the gas 10000m of principal constituent
3/ hr has made natural gas liquids as unstripped gas.
The thermal value of its product LNG amount, product hydrogen amount, the product carbon dioxide gas scale of construction, non-condensable gases is shown in table 2.
Comparative example 2
Fig. 3 is the schematic diagram of another routine comparative example 2 that represents the manufacturing installation of natural gas liquids in the past.
Use device shown in Figure 3, the coke(oven)gas of the composition of record in table 1 is the gas 10000m of principal constituent
3/ hr has made natural gas liquids as unstripped gas.
The thermal value of its product LNG amount, the product carbon dioxide gas scale of construction, non-condensable gases is shown in table 2.
Table 1
| Composition | mol％ |
| H 2 | 57.72 |
| N 2 | 3.01 |
| O 2 | 0.4 |
| CO | 6.02 |
| CO 2 | 2.51 |
| CH 4 | 27.6 |
| C 2H 6 | 0.5 |
| C 2H 4 | 2.01 |
| C 3 + | 0 |
| H 2S | 0.01 |
| Other | 0.22 |
| Amount to | 100 |
Table 2
| Comparative example 1 | Comparative example 2 | Embodiment 1 | |
| LNG manufacture [ton/day] | 43.8 | 43.8 | 43.8 |
| Product H 2Manufacture [m 3/day] | 4410 | - | 4850 |
| Products C O 2Manufacture [ton/day] | 12.8 | 12.8 | 39 |
| Non-condensable gases thermal value 4.18[kJ/m 3] | 4420 | 3240 | 4700 |
As seen from Table 2, use in the manufacturing of natural gas liquids of manufacturing installation of natural gas liquids of embodiment 1, compare with comparative example 1, can confirm 10% hydrogen effect of increasing production and 300% carbonic acid gas effect of increasing production.In addition, can confirm approximately 6% gain of heat effect about the thermal value of non-condensable gases.
And, compare with the comparative example 2 that makes non-condensable gases carry out recirculation, although can't compare about hydrogen, can confirm 300% volume increase to carbonic acid gas.In addition, can confirm 45% gain of heat effect about the thermal value of non-condensable gases.
Therefore, present technique makes the maximization of hydrogen production amount when making hydrogen, LNG from COG, simultaneously, also can increase production the carbonic acid gas as product, and, the heat of the non-condensable gases of by-product in LNG is increased.
Claims (4)
1. the manufacturing installation of a natural gas liquids is characterized in that, is the manufacturing installation of the natural gas liquids take coke(oven)gas as main raw material, comprises successively such as lower unit: gas purification unit, conversion reaction unit and liquefaction unit, wherein,
Described conversion reaction unit is to make water and carbon monoxide convert the unit of hydrogen and carbonic acid gas to,
And, between described conversion reaction unit and described liquefaction unit, be provided with the decarbonate unit of removing carbonic acid gas and the hydrogen separating unit that hydrogen is carried out selective separation.
2. the manufacturing installation of natural gas liquids according to claim 1, wherein, carbonic acid gas is removed so that the concentration of the carbonic acid gas in the gas of the ingress of described liquefaction unit becomes the following mode of 50ppm in described decarbonate unit.
3. the manufacturing installation of natural gas liquids according to claim 1 wherein, also is provided with the non-condensable gases transfer lime, is used for being delivered to coke oven as the fuel of coke oven at the non-condensable gases of described liquefaction unit by-product, sneaks in the rich gas of heating coke oven.
4. the manufacturing installation of natural gas liquids according to claim 1, wherein, described hydrogen separating unit is to be selected from least a in pressure-swing absorption apparatus and the membrane separation unit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012205380592U CN202898374U (en) | 2012-10-19 | 2012-10-19 | Liquefied natural gas production device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012205380592U CN202898374U (en) | 2012-10-19 | 2012-10-19 | Liquefied natural gas production device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202898374U true CN202898374U (en) | 2013-04-24 |
Family
ID=48119066
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012205380592U Expired - Lifetime CN202898374U (en) | 2012-10-19 | 2012-10-19 | Liquefied natural gas production device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202898374U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103265986A (en) * | 2013-05-30 | 2013-08-28 | 中煤能源黑龙江煤化工有限公司 | Method for extracting coal-based natural gas from methanol blowdown gas and method for producing CNG (compressed natural gas) |
-
2012
- 2012-10-19 CN CN2012205380592U patent/CN202898374U/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103265986A (en) * | 2013-05-30 | 2013-08-28 | 中煤能源黑龙江煤化工有限公司 | Method for extracting coal-based natural gas from methanol blowdown gas and method for producing CNG (compressed natural gas) |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130424 |
|
| CX01 | Expiry of patent term |