CN103497804B - The method of heavy hydrocarbon in Sweet natural gas is deviate from a kind of low temperature capillary condensation - Google Patents
The method of heavy hydrocarbon in Sweet natural gas is deviate from a kind of low temperature capillary condensation Download PDFInfo
- Publication number
- CN103497804B CN103497804B CN201310467386.2A CN201310467386A CN103497804B CN 103497804 B CN103497804 B CN 103497804B CN 201310467386 A CN201310467386 A CN 201310467386A CN 103497804 B CN103497804 B CN 103497804B
- Authority
- CN
- China
- Prior art keywords
- natural gas
- heavy hydrocarbon
- tower
- low temperature
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a kind of method that heavy hydrocarbon in Sweet natural gas is deviate from low temperature capillary condensation, it is characterized in that: comprise the following steps: (1), by raw natural gas through the first heat exchanger precooling, precooling temperature 5.5 ~-15.5 DEG C, at this temperature, there is not the phenomenon of condensing in the heavy hydrocarbon in raw natural gas; (2) the low temperature feedstock gas, after precooling enters the tower group being filled with capillary-porous material, and in described tower, working pressure is 2-8MPa, and heavy hydrocarbon is condensed upon in the endoporus of capillary-porous material, and gas product flows out from tower bottom.The present invention is applicable to deep cooling should not be adopted to remove the Sweet natural gas of heavy hydrocarbon containing higher, the volatile components of condensation point, is also applicable to the unstripped gas of the liquefaction plant of the general Sweet natural gas that heavy hydrocarbons content exceeds standard.Remove the raw natural gas after heavy hydrocarbon and meet natural gas liquefaction for the requirement of raw natural gas to heavy hydrocarbons content.
Description
Technical field
The present invention relates to the imurity-removal method of Sweet natural gas, particularly one pre-treatment before natural gas liquefaction, the method for heavy hydrocarbon in Sweet natural gas is deviate from low temperature capillary condensation.
Background technology
Sweet natural gas is a kind of clean energy, has the features such as calorific value is high, efficiency of combustion is high, post-combustion pollution discharge is few.Along with urban pipe network build day by day perfect, the use of pipe natural gas is day by day extensive.Because natural gas field is general and use gas demand often not in areal, some is even transnational, and the use of Sweet natural gas has period and seasonal, therefore, ageing with solving Sweet natural gas for the purpose of natural gas transport natural gas liquids becomes a kind of important means.Along with the user of natural gas liquids is to the expansion of transportation industry, in natural gas liquids pollutes in reduction, increase the benefit etc., give play to increasing effect.
Sweet natural gas divides conventional gas and Unconventional forage, conventional gas refers generally to the reservoir gas of Sweet natural gas, Unconventional forage then comprises wider, and as coal-seam gas, biogas, associated gas, shale gas and gas hydrate etc., wherein gas hydrate are otherwise known as combustible ice.These sources of the gas all can be used as the raw material producing natural gas liquids, and because gas reservoir geographical position is different, the composition of Sweet natural gas may have very large difference, these unstripped gass CH
4be main ingredient, may H be contained in addition
2, CO
2, H
2s, N
2, C
2h
6, C
3h
8, i-C
4h
10, n-C
4h
10, Neo-C
5h
12(neopentane), i-C
5h
12, n-C
5h
12, C
6h
14, C
7h
16, C
6h
6, toluene, ethylbenzene, dimethylbenzene, naphthenic hydrocarbon, H
2o, Hg etc., what have even contains C
10above component, the complicated production of component to natural gas liquids has a great impact.
Liquefied natural gas (LNG) plant mainly comprises three operations such as storage of the pre-treatment of unstripped gas, condensation liquefaction, Sweet natural gas.Wherein the pre-treatment of unstripped gas all has a great impact liquefied natural gas product quality, device security and factory's long-period stable operation, therefore, in the process of natural gas liquefaction plant design, operation, the strict pre-treatment controlling to enter natural gas liquefaction ice chest unstripped gas is needed.
The pre-treatment of general liquefaction plant comprises depickling gas, dehydration, demercuration etc., and the object of depickling gas is mainly by the H in Sweet natural gas
2s and CO
2physics, chemistry or physicochemical method is utilized to remove, because H
2s has certain corrodibility to steel, can cause the corrosion of container and equipment, and CO
2under pressure, when being cooled to certain temperature, becoming solid phase when not yet forming liquid phase, causing ice chest ice to block up, therefore, before liquefaction plant requires that unstripped gas enters ice chest, need by CO
2and H
2s is removed to 50ppm(V/V respectively) and 4ppm(V/V) below.Due to H
2o can form solid phase hydration thing with hydrocarbon compound, and in addition when lower than 0 DEG C, self also may form solid phase, and therefore, before unstripped gas enters ice chest, water-content requires lower than 10ppb(V/V).
Because the component of the Sweet natural gas of various places is different, when containing other heavy hydrocarbon in Sweet natural gas, as Neo-C
5h
12, C
6h
6or toluene, when ethylbenzene and carbon chain lengths are greater than 6 carbon atoms, the pre-treatment of unstripped gas must take into full account removing of these hydrocarbon components.Table 1 lists the condensation point of common hydro carbons in several Sweet natural gas.
Condensation point under the normal pressure of the several frequently seen hydro carbons of table 1
| Material | Neo-C 5H 12 | n-C 5H 12 | C 6H 14 | Hexanaphthene | C 6H 6 | Toluene | Ethylbenzene |
| Condensation point DEG C | -16.57 | -129.73 | -95.31 | 6,539 | 5.53 | -94.97 | -94.95 |
As can be seen from the table, in raw natural gas containing a certain amount of above-mentioned hydro carbons and the component that also weighs than above-mentioned hydro carbons as heptane, octane etc., dimethylbenzene or other naphthenic hydrocarbon time, these unstripped gass enter the frozen block that ice chest is easy to cause ice chest, thus affect the steady running of factory.
Therefore, when containing comparatively heavy hydrocarbons, especially Neo-C in fuel gas
5h
12, C
6h
6, toluene, hexanaphthene and containing a certain amount of C5+ time, must remove these hydro carbons, be reduced to these hydro carbons allow exist content range.
The technique adopting the mode of solvent absorbing to remove hydro carbons in unstripped gas is described in patent ZL2005100118034.4, the mode that in this technology utilization Sweet natural gas, heavy hydrocarbon autolysis absorbs removes the heavy hydrocarbon in unstripped gas, this separate mode needs to adopt separate absorbent tower, and coordinating the circulation of a large amount of liquid, dynamic equipment is many.Adopt this patent to provide the mode of de-heavy hydrocarbon, removing containing Neo-C
5h
12, benzene, during the heavy hydrocarbon of the contour volatile-type of hexanaphthene, can not meet ice chest for Neo-C
5h
12, benzene, the requirement of the content of hexanaphthene etc.
Utilize cryogenic condensation to remove heavy hydrocarbon and also have certain application, patent ZL200610046233.0 utilizes conventional deep cooling freezing mode, freezingly removes water in oil and gas and heavy hydrocarbon.
Chinese patent application 200910119273.7 utilizes deep cooling freezing, then by gas through absorption tower adsorbs, foreign gas is adsorbed onto the surface of sorbent material to reach the object of purification.But as can be seen from Table 1, when containing C in unstripped gas
6h
6, hexanaphthene, Neo-C5 time, because the zero pour of these materials is higher, natural gas liquids then needs C
6h
6, hexanaphthene, Neo-C5 etc. be reduced to below 5ppm, otherwise, when next step liquefies.Easily there is the phenomenon of Cold box blocking and freezing.And the vapour pressure of these materials is higher, therefore, the method adopting conventional cold method to add common absorption substantially can not reach such and remove concentration.
Summary of the invention
The capillary condensation of a kind of energy low temperature is the object of the present invention is to provide to deviate from the method for heavy hydrocarbon in Sweet natural gas, be applicable to containing condensation point higher and volatile components should not adopt deep cooling to remove the Sweet natural gas of heavy hydrocarbon, be also applicable to the unstripped gas of the liquefaction plant of the general Sweet natural gas that heavy hydrocarbons content exceeds standard.Remove the raw natural gas after heavy hydrocarbon and meet natural gas liquefaction for the requirement of raw natural gas to heavy hydrocarbons content.
For achieving the above object, technical scheme of the present invention is: the method for heavy hydrocarbon in Sweet natural gas is deviate from a kind of low temperature capillary condensation, it is characterized in that: comprise the following steps:
(1), by raw natural gas through the first heat exchanger precooling, precooling temperature 5.5 ~-15.5 DEG C, at this temperature, there is not the phenomenon of condensing in the heavy hydrocarbon in raw natural gas;
(2) the low temperature feedstock gas, after precooling enters the tower group being filled with capillary-porous material, and in described tower, working pressure is 2-8MPa, and heavy hydrocarbon is condensed upon in the endoporus of capillary-porous material, and gas product flows out from tower bottom.
Adopt technique scheme, raw natural gas is chilled to 5.5 ~-15.5 DEG C in advance, at this temperature, the heavy hydrocarbon in raw natural gas do not occur condense phenomenon, there will not be because of heavy hydrocarbon condense cause pipeline to be blocked phenomenon appearance.
Through the raw natural gas of precooling, enter in tower and deviate from heavy hydrocarbon by capillary condensation, (so-called capillary condensation phenomenon refers to, in capillary channel, namely saturated vapor pressure condenses lower than flat subsurface vapour pressure P0, when pore diameter more hour, the vapour pressure needed for cohesion is lower, in other words, when pore diameter more hour, under lower P/P0 pressure, coagulation liquid can be formed in hole, but along with hole dimension increases, only under higher P/P0 pressure, form coagulation liquid.）。That is: at capillary-porous material inner surface, the material be in contact with it can produce enrichment effect, due to the existence of pore, under pressurized conditions, reduce the temperature of the material contacted with capillary material, can capillary condensation be produced, the dissolution characteristics of coagulation liquid, can promote that agglomeration process occurs further, and reduce the content of product wherein volatile components.
The present invention utilizes the feature of capillary-size pore just, by by unstripped gas precooling, then pressurize, make the heavy hydrocarbon component in raw natural gas by capillary condensation in conjunction with coagulation liquid dissolve realize heavy hydrocarbon and easily frozen block component be separated with light constituent, light constituent then flows out system, realize raw natural gas heavy hydrocarbon to remove, meet the requirement of natural gas liquefaction for heavy hydrocarbons content in unstripped gas, avoid frozen block ice chest interchanger.
In technique scheme: the heavy hydrocarbon that exceeds standard described in step (1) is the heavy hydrocarbon that carbonatoms is more than or equal to 5.
In technique scheme: described capillary-porous material is gac or silica gel or aluminum oxide or porous amorphous silicon aluminium hydrochlorate or zeolite or mesoporous molecular sieve.
In technique scheme: in order to reach better capillary condensation effect, in step (2), described working pressure is 4MPa-6.2MPa.
In technique scheme: the process also comprising capillary-porous material bed regeneration in step (3) tower, described regeneration is at least one vacuumizing and heat up in air lift two kinds of modes.Adopt the combination of two kinds of regenerations, regeneration effect is better, and efficiency is higher, and after regeneration, heavy hydrocarbon out can be used for making heavier hydrocarbon products.
In technique scheme: in step (2): described tower group comprises at least two towers, make at least one in running order.Facilitate continuous seepage like this, production efficiency is high.
In technique scheme: described tower is one, adopt the mode of cohesion and regeneration periodical operation.
Beneficial effect: the present invention is according to component LOW TEMPERATURES characteristic each in Sweet natural gas, adopt the method for low temperature capillary condensation, heavy hydrocarbon in Sweet natural gas is removed, meet in liquefied natural gas process the requirement entering heavy hydrocarbons content in ice chest unstripped gas, this operational path is regenerated capillary-porous bed by the mode reducing pressure and vacuumize and (or) improve bed temperature, run by the mode of multitower sequential operation, realize operate continuously.There is dynamic equipment few, stable, feature easy and simple to handle.The present invention contains C in unstripped gas
6h
6, hexanaphthene, Neo-C
5h
12especially applicable etc. Deep Cooling Method should not be adopted to remove the raw natural gas of heavy hydrocarbon, remove the raw natural gas after heavy hydrocarbon and meet the requirement of natural gas liquefaction to heavy hydrocarbons content in unstripped gas.
Accompanying drawing explanation
Fig. 1 is the structural representation that the embodiment of the present invention 1 deviates from heavy hydrocarbon use system in Sweet natural gas;
Fig. 2 is the structural representation that the embodiment of the present invention 2 deviates from heavy hydrocarbon use system in Sweet natural gas.
Embodiment
Below in conjunction with embodiment, the present invention is further illustrated:
Embodiment 1
As shown in Figure 1, this process adopts two tower low temperature capillary condensations to take off heavy hydrocarbon flow process.Tower of the present invention is identical with the structure of the adsorption tower used on the market at present.Described first tower 2 and the second tower 3 arranged in parallel, operate out of phase.The capillary-porous material of filling in the first tower 2 and the second tower 3 adopts cocoanut active charcoal, apparent diameter 3mm, aperture 7.8nm-15000nm, integrated distribution at 108nm, specific surface area 1030m
2/ g, bulk density 0.43g/cm
3, through fully dry before using.
Raw natural gas through the first heat exchanger 1 precooling, precooling temperature 6.5 DEG C.Low temperature feedstock gas after precooling enters in the first tower 2 from the first tower 2 top, and heavy hydrocarbon (hydro carbons that carbonatoms is greater than 5) is condensed upon bed by enrichment, and the gas product after purification flows out from the first tower 2 bottom.Working pressure in first tower 2 is 4MPa.
Now 3, the second tower is in step-down, regeneration, boosting and stand-by state.Bed regeneration adopts the mode vacuumized.During regeneration, control the pressure 70Pa of bed.Gas phase born is again aspirated from the vacuum pump 4 of the second tower 3 top exit and is got rid of, and cools and isolate liquid phase heavy hydrocarbon as heavier hydrocarbon products through the second heat exchanger 5.Vacuum regeneration, the 8h/ cycle.
After the second tower 3 has regenerated, raw natural gas has entered working order by the second tower 3 again, and the first 2, tower is in reproduced state.
Result through the raw natural gas of the present embodiment is as shown in the table:
As can be seen from the table, the Sweet natural gas after purification meets natural gas liquids needs by C
6h
6, hexanaphthene, Neo-C5 etc. be reduced to the requirement of below 5ppm.
Embodiment 2
As shown in accompanying drawing Fig. 2, this process adopts three tower low temperature capillary condensation flow processs.First, second, third 3 towers 2,3,6 arranged in parallel, operate out of phase.The capillary-porous material of filling in first, second, and third 3 towers 2,3,6 is silica gel, the cylindrical particle of this silica gel to be diameter be 2.5mm, aperture 8.5-38nm, integrated distribution at 22nm, specific surface area 350m
2/ g, bulk density 0.75g/cm
3, through fully dry before using.
Raw natural gas through the first heat exchanger 1 precooling, precooling temperature 5.5 DEG C.Low temperature feedstock gas low temperature capillary condensation after precooling takes off heavy hydrocarbon system, at first, to lower the temperature after first tower 2 is in regeneration done state, second tower has then been in the mid-term of low temperature capillary condensation process, 3rd 6, tower is in low temperature capillary condensation latter stage, is first cut out from capillary condensation state by the 3rd tower 6, and all presses to the first tower 2, after all having pressed, the 3rd tower 6 enters ramp regeneration, cold blowing temperature-fall period.First tower 2 then continues to boost to working pressure, then to come into operation use in parallel with the second tower 3, low temperature capillary condensation latter stage is arrived to the second tower 3,3rd tower 6 cold blowing terminates, and is now cut out by the second tower 3, all presses to the 3rd tower 6, after all having pressed, second tower 3 enters ramp regeneration and cold blowing process, and the 3rd tower 6 then continues to boost to working pressure, then comes into operation.When the first tower 2 enters capillary condensation latter stage, second tower 3 completes cold blowing, now the first tower 2 is all pressed to the second tower 3, after all having pressed, first tower 2 enters ramp regeneration and cold blowing process, second tower 3 then continues to boost to working pressure, then comes into operation, and the first tower 2 then enters ramp regeneration and cold blowing process.
So complete a circulation, during cohesion, working pressure 6.2MPa in tower.Regenerative process adopts intensification stripping regime, and regeneration pressure is normal pressure, and air lift adopts the gas product purified, and stripping temperature is 150 DEG C.Gas phase born again, cools through the second heat exchanger 5 and isolates liquid phase heavy hydrocarbon as heavier hydrocarbon products.
Result through the raw natural gas of the present embodiment is as shown in the table:
As can be seen from the table, the Sweet natural gas after purification meets natural gas liquids needs by C
6h
6, hexanaphthene, Neo-C5 etc. be reduced to the requirement of below 5ppm.
Embodiment 3
As shown in Figure 1, this process adopts two tower low temperature capillary condensations to take off heavy hydrocarbon flow process.Described first tower 2 and the second tower 3 arranged in parallel, operate out of phase.First tower 2 and the interior capillary-porous material of filling of the second tower 3 adopt molecular sieve MCM-41, apparent diameter 3mm, aperture 15nm, specific surface area 985m
2/ g, bulk density 0.68g/cm
3, through fully dry before using.
Raw natural gas through the first heat exchanger 1 precooling, precooling temperature 5.8 DEG C.Low temperature feedstock gas after precooling enters in the first tower 2 from the first tower 2 top, and heavy hydrocarbon (hydro carbons that carbonatoms is greater than 5) is condensed upon bed by enrichment, and the gas product after purification flows out from the first tower 2 bottom.First tower 2 working pressure is 2MPa.
Now 3, the second tower is in step-down, regeneration, boosting and stand-by state.Bed regeneration adopts the mode vacuumized.During regeneration, control the pressure 70Pa of bed.Gas phase born is again aspirated from the vacuum pump 4 of the second tower 3 top exit and is got rid of, and cools and isolate liquid phase heavy hydrocarbon as heavier hydrocarbon products through the second heat exchanger 5.Vacuum regeneration, the 8h/ cycle.
After the second tower 3 has regenerated, raw natural gas has carried out purifying by the second tower 3 again, and the first 2, tower is in reproduced state.
Result through the raw natural gas of the present embodiment is as shown in the table:
As can be seen from the table, the Sweet natural gas after purification meets natural gas liquids needs by C
6h
6, hexanaphthene, Neo-C5 etc. be reduced to the requirement of below 5ppm.
Embodiment 4
As shown in Figure 1, this process adopts two tower low temperature capillary condensations to take off heavy hydrocarbon flow process.The capillary-porous material of filling in the first tower 2 and the second tower 3 adopts activated alumina, apparent diameter 3mm, aperture 7.8nm-150nm, integrated distribution at 29nm, specific surface area 878m
2/ g, bulk density 0.63g/cm
3, through fully dry before using.
Raw natural gas through the first heat exchanger 1 precooling, precooling temperature 5.8 DEG C.Low temperature feedstock gas after precooling enters in the first tower 2 from the first tower 2 top, and heavy hydrocarbon (hydro carbons that carbonatoms is greater than 5) is condensed upon bed by enrichment, and the gas product after purification flows out from the first tower 2 bottom.Pressure in first tower 2 is 8MPa.
Now 3, the second tower is in step-down, regeneration, boosting and stand-by state.Bed regeneration adopts the mode vacuumized.During regeneration, control the pressure 70Pa of bed.Gas phase born is again aspirated from the vacuum pump 4 of the second tower 3 top exit and is got rid of, and cools and isolate liquid phase heavy hydrocarbon as heavier hydrocarbon products through the second heat exchanger 5.Vacuum regeneration, the 8h/ cycle.
After the second tower 3 has regenerated, raw natural gas has carried out purifying by the second tower 3 again, and the first 2, tower is in reproduced state.
Result through the raw natural gas of the present embodiment is as shown in the table:
As can be seen from the table, the Sweet natural gas after purification meets natural gas liquids needs by C
6h
6, hexanaphthene, Neo-C5 etc. be reduced to the requirement of below 5ppm.
The present invention is not limited to embodiment, and described capillary-porous material, except the material enumerated in embodiment, can also adopt silica gel, aluminum oxide, porous amorphous silicon aluminium hydrochlorate, zeolite, mesoporous molecular sieve medium.Described tower with single tower work, also can also can connect multiple tower, as long as adopt method of the present invention all to fall within the scope of protection of the present invention.
Claims (6)
1. a method for heavy hydrocarbon in Sweet natural gas is deviate from low temperature capillary condensation, it is characterized in that: comprise the following steps:
(1), by raw natural gas through the first heat exchanger precooling, precooling temperature 5.5 ~-15.5 DEG C, at this temperature, there is not the phenomenon of condensing in the heavy hydrocarbon that exceeds standard in raw natural gas;
(2) the low temperature feedstock gas, after precooling enters the tower group being filled with capillary-porous material, in described tower, working pressure is 2-8MPa, heavy hydrocarbon is condensed upon in the endoporus of capillary-porous material, gas product flows out from tower bottom, and described capillary-porous material is gac or silica gel or aluminum oxide or porous amorphous silicon aluminium hydrochlorate or zeolite or mesoporous molecular sieve.
2. the method for heavy hydrocarbon in Sweet natural gas is deviate from low temperature capillary condensation according to claim 1, it is characterized in that: the heavy hydrocarbon that exceeds standard described in step (1) is the heavy hydrocarbon that carbonatoms is more than or equal to 5.
3. according to any one of claim 1-2, the method for heavy hydrocarbon in Sweet natural gas is deviate from low temperature capillary condensation, it is characterized in that: in step (2), and in described tower, working pressure is 4MPa-6.2MPa.
4. according to any one of claim 1-2, the method for heavy hydrocarbon in Sweet natural gas is deviate from low temperature capillary condensation, it is characterized in that: the process also comprising capillary-porous material bed regeneration in step (3) tower, described regeneration is at least one vacuumizing and heat up in air lift two kinds of modes.
5. the method for heavy hydrocarbon in Sweet natural gas is deviate from low temperature capillary condensation according to claim 4, it is characterized in that: in step (2): described tower group comprises at least two towers, make wherein at least one in running order.
6. the method for heavy hydrocarbon in Sweet natural gas is deviate from low temperature capillary condensation according to claim 4, it is characterized in that: described tower is one, adopts the mode of capillary condensation and regeneration periodical operation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310467386.2A CN103497804B (en) | 2013-10-09 | 2013-10-09 | The method of heavy hydrocarbon in Sweet natural gas is deviate from a kind of low temperature capillary condensation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310467386.2A CN103497804B (en) | 2013-10-09 | 2013-10-09 | The method of heavy hydrocarbon in Sweet natural gas is deviate from a kind of low temperature capillary condensation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103497804A CN103497804A (en) | 2014-01-08 |
| CN103497804B true CN103497804B (en) | 2015-08-26 |
Family
ID=49863065
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310467386.2A Active CN103497804B (en) | 2013-10-09 | 2013-10-09 | The method of heavy hydrocarbon in Sweet natural gas is deviate from a kind of low temperature capillary condensation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103497804B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11988336B2 (en) | 2021-03-16 | 2024-05-21 | Marathon Petroleum Company Lp | Scalable greenhouse gas capture systems and methods |
Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104061758A (en) * | 2014-07-01 | 2014-09-24 | 天津市振津工程设计咨询有限公司 | Device and method for removing heavy hydrocarbon in natural gas through step-by-step condensation |
| US10024768B1 (en) | 2016-06-17 | 2018-07-17 | Markwest Energy Partners, L.P. | System, method, and apparatus for determining air emissions during pig receiver depressurization |
| US10001240B1 (en) | 2016-11-02 | 2018-06-19 | Markwest Energy Partners, L.P. | Pig ramp, system and method |
| US10196243B1 (en) | 2017-02-28 | 2019-02-05 | Markwest Energy Partners, L.P. | Heavy compressor valve lifting tool and associated methods |
| US11607654B2 (en) | 2019-12-30 | 2023-03-21 | Marathon Petroleum Company Lp | Methods and systems for in-line mixing of hydrocarbon liquids |
| CA3103416C (en) | 2019-12-30 | 2022-01-25 | Marathon Petroleum Company Lp | Methods and systems for inline mixing of hydrocarbon liquids |
| CA3104319C (en) | 2019-12-30 | 2023-01-24 | Marathon Petroleum Company Lp | Methods and systems for spillback control of in-line mixing of hydrocarbon liquids |
| US11655940B2 (en) | 2021-03-16 | 2023-05-23 | Marathon Petroleum Company Lp | Systems and methods for transporting fuel and carbon dioxide in a dual fluid vessel |
| US11447877B1 (en) | 2021-08-26 | 2022-09-20 | Marathon Petroleum Company Lp | Assemblies and methods for monitoring cathodic protection of structures |
| CN113877534A (en) * | 2021-11-17 | 2022-01-04 | 重庆耐德工业股份有限公司 | Activated carbon treatment method and heavy hydrocarbon removal method by natural gas liquefaction adsorption method |
| US11686070B1 (en) | 2022-05-04 | 2023-06-27 | Marathon Petroleum Company Lp | Systems, methods, and controllers to enhance heavy equipment warning |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030192343A1 (en) * | 2001-05-04 | 2003-10-16 | Wilding Bruce M. | Apparatus for the liquefaction of natural gas and methods relating to same |
| CN202297537U (en) * | 2011-09-30 | 2012-07-04 | 新地能源工程技术有限公司 | Methane gas-rich purification device adopting hydrogen-rich nitrogen gas for precooling |
| CN202297494U (en) * | 2011-09-30 | 2012-07-04 | 上海森鑫新能源科技有限公司 | Device for recycling mixed hydrocarbon from oil associated gas |
| CN203096015U (en) * | 2012-08-03 | 2013-07-31 | 气体产品与化学公司 | Device for removing heavy hydrocarbons in natural gas feed flow |
-
2013
- 2013-10-09 CN CN201310467386.2A patent/CN103497804B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030192343A1 (en) * | 2001-05-04 | 2003-10-16 | Wilding Bruce M. | Apparatus for the liquefaction of natural gas and methods relating to same |
| CN202297537U (en) * | 2011-09-30 | 2012-07-04 | 新地能源工程技术有限公司 | Methane gas-rich purification device adopting hydrogen-rich nitrogen gas for precooling |
| CN202297494U (en) * | 2011-09-30 | 2012-07-04 | 上海森鑫新能源科技有限公司 | Device for recycling mixed hydrocarbon from oil associated gas |
| CN203096015U (en) * | 2012-08-03 | 2013-07-31 | 气体产品与化学公司 | Device for removing heavy hydrocarbons in natural gas feed flow |
Non-Patent Citations (1)
| Title |
|---|
| 李士伦等.多孔介质中的毛细凝聚现象.《气田及凝析气田开发新理论、新技术》.石油工业出版社,2005, * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11988336B2 (en) | 2021-03-16 | 2024-05-21 | Marathon Petroleum Company Lp | Scalable greenhouse gas capture systems and methods |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103497804A (en) | 2014-01-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103497804B (en) | The method of heavy hydrocarbon in Sweet natural gas is deviate from a kind of low temperature capillary condensation | |
| CN108689381B (en) | Oil gas recovery system and recovery method for oil loading and unloading platform of refinery area | |
| CN101040674B (en) | Method for producing food level liquid carbon dioxide product | |
| CN100595263C (en) | Front end combination purification technique for producing liquefied natural gas from mixture gas rich-containing methane | |
| RU2575846C1 (en) | Methods and devices for obtaining of liquefied natural gas | |
| CN205461098U (en) | Oil -gas recovery processing device | |
| RU2613914C1 (en) | Method for processing natural hydrocarbon gas | |
| EA023224B1 (en) | Method for the purification of carbon dioxide using liquide carbon dioxide | |
| RU2014153653A (en) | The method of complex extraction of valuable impurities from natural helium-containing hydrocarbon gas with a high nitrogen content | |
| CN202295966U (en) | Oil gas recovery device | |
| CN208345747U (en) | A kind of area of refinery oil loading platform gas recovery system for oil | |
| CN104815519A (en) | Recovery technology for volatile oil gas in lightweight aromatic hydrocarbons filling process | |
| CN102764562B (en) | Absorption type oil gas recovery processing system and recovery processing technique thereof | |
| CN204637927U (en) | A kind of device for recovering oil and gas | |
| CN203419745U (en) | Carbon dioxide distillation recycling device with double gas cabinets | |
| US20140230650A1 (en) | Method to retrofit system with enhanced capacity for removing mercury from a produced hydrocarbon fluid. | |
| CN104194852A (en) | High-yield light hydrocarbon recovery method from low-pressure natural gas | |
| CN205011721U (en) | Smart dewatering system of synthesis of LNGLPGNGL product is retrieved to saturation wet oil associated gas | |
| CN100411711C (en) | Method for removing hydrocarbons from a vapour-gas medium formed during petroleum product storage and a tank filling therewith | |
| CN203904299U (en) | Pipeline natural gas heavy hydrocarbon removal unit | |
| KR20050090774A (en) | Apparatus and method for decomposing volatile organic compound of facilities for storing oil | |
| CN209885536U (en) | Multistage adsorption oil gas recovery device | |
| RU2691341C1 (en) | Method of purifying natural gas from impurities | |
| RU2607631C1 (en) | Method for production of liquefied hydrocarbon gases | |
| CN211799844U (en) | Aromatic hydrocarbon tank field oil gas step recovery processing system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |