CN109257937A - 用于含甲烷和空气气体的进料流的低温分离的方法、用于通过实施该方法纯化源自非危险废物贮存设备(nhwsf)的生物气以生产生物甲烷的设备 - Google Patents
用于含甲烷和空气气体的进料流的低温分离的方法、用于通过实施该方法纯化源自非危险废物贮存设备(nhwsf)的生物气以生产生物甲烷的设备 Download PDFInfo
- Publication number
- CN109257937A CN109257937A CN201780032072.6A CN201780032072A CN109257937A CN 109257937 A CN109257937 A CN 109257937A CN 201780032072 A CN201780032072 A CN 201780032072A CN 109257937 A CN109257937 A CN 109257937A
- Authority
- CN
- China
- Prior art keywords
- methane
- logistics
- feeding flow
- tower
- cooling
- 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.)
- Granted
Links
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/38—Processes or apparatus using separation by rectification using pre-separation or distributed distillation before a main column system, e.g. in a at least a double column system
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
- F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/04—Mixing or blending of fluids with the feed stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—Nitrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/50—Oxygen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/60—Natural gas or synthetic natural gas [SNG]
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/66—Landfill or fermentation off-gas, e.g. "Bio-gas"
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/60—Methane
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/40—Separating high boiling, i.e. less volatile components from air, e.g. CO2, hydrocarbons
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2280/00—Control of the process or apparatus
- F25J2280/02—Control in general, load changes, different modes ("runs"), measurements
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/90—Details about safety operation of the installation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
含有甲烷和空气气体的进料流的低温分离方法,其中:‑将进料流冷却以产生冷却的物流;‑将冷却的物流的至少一部分送至蒸馏塔的一级;‑从蒸馏塔中采出底部物流,其中底部物流与进料流相比富含甲烷;‑从蒸馏塔中采出与进料流相比富含氧气和氮气的物流;‑将至少一种不可燃且比氧气更易挥发的稀释物流添加低于在比引入冷却的物流的级低至少一级处引入蒸馏塔中,其特征在于从进料流中提取稀释物流。通过实施该方法纯化来自非危险废物贮存设备(NHWSF)的生物气以生产生物甲烷的设备。
Description
本发明涉及一种用于含有甲烷、二氧化碳、氮气和/或氧气以及更通常的空气气体的物流的低温分离的方法和装置,以用于生产富甲烷的物流。
本发明的方法具有与通过纯化来自非危险废物贮存设备(NHWSF)的生物气来生产生物甲烷相关的特别有利的应用。
生物气是由厌氧环境中有机物分解的生物过程产生的气体,其主要由不同量的甲烷、二氧化碳、水蒸气和杂质组成,所述量取决于产生生物气的有机材料。主要发现的杂质是硫化氢,并且当有机材料来自家庭或工业废物时,主要发现的杂质是挥发性有机化合物(VOCs)。
可以在专用反应器(也称为“消化器”)中生产生物气,其中生物反应在完全厌氧环境中且受控的温度下运行。也可以在非危险废物储存设备(NHWSF) 中大量地自然生产生物气,其中将家庭废物储存在地窖中并且当它们充满时用膜覆盖。地窖关闭后,可以开始有机物质产生甲烷的过程。然后通过插入地窖中的收集管将如此产生的生物气吸到增压器中进行收集,从而在所述地窖中产生略微减小的压力。由于这些地窖不是完全密封的,因此其吸入空气,并在生物气中发现不同比例的空气。因此,对于该气体源,空气气体加到前面所述的杂质中,必须将其除去以回收生物气。
也有其他含甲烷、二氧化碳、杂质和不同浓度空气气体的气体源,如来自矿井的气体,其通过废弃矿井中煤层的脱气产生,并与存在于采矿空间中存在的空气混合。出于回收该气体以用于上述应用的目的,必须消除其中含有的杂质。
更具体地,为了生产富甲烷的物流,必须将二氧化碳、氮气和氧气杂质去除至一定水平,使得由此产生的富甲烷的物流可用作天然气、液化天然气或车辆燃料。根据所指示的用途,所需的杂质水平可以不同。同样,富甲烷的物流中这些杂质的典型指标是:低于2摩尔%的二氧化碳,低于1%的氧气和低于1%的氮气。当富甲烷的物流不再含有二氧化碳时,所需的杂质水平为:低于2.5 摩尔%的氮气和低于1%的氧气。
本申请其余部分中的组成以摩尔百分比表示。
在由NHWSF生产的生物气的情况下,需要进行第一处理以除去大部分二氧化碳和杂质。对此存在许多方法,如使用气体渗透膜并结合吸附来处理杂质 (US-2004-0103782),使用压力调制吸附方法,使用水或胺洗涤塔以及使用低温吸附法。用这些方法可以分开生物气杂质和大部分二氧化碳,但是不能将空气气体从富甲烷的气流中分离出来。因此需要附加的处理步骤。
该附加的处理步骤可以包括使用对氮气和氧气有选择性的特定吸附剂进行压力调制吸附(US 8,221,524)。然而,非常低的氧气和氮气浓度是在亏损该方法的甲烷回收率的情况下实现的,这使得它在经济上没有意义。
将空气气体从甲烷中除去的另一种解决方案是低温蒸馏,其可以实现一方面在塔底回收的甲烷与另一方面在塔顶回收的氮气和氧气之间的良好分离能力,这是因为这些组分之间的挥发性差异。
然而,挥发性在甲烷和氮气之间的氧气的存在,导致该化合物倾向于在蒸馏区中浓缩,即使对于塔装载量中的小氧气浓度也是如此。气相甲烷浓度的降低加之气相氧气浓度的增加,可导致由于其组成而可爆炸的气体混合物。
甲烷和空气气体混合物的蒸馏原理已知是在低温温度下,潜在爆炸性气体混合物出现在塔内。因此,文献DE 981,875提出用这样的方式控制蒸馏:使得离开塔顶的气体在爆炸上限(UEL)之外。然而,没有提及蒸馏塔中的天然氧气浓度,因此用该方法不能避免形成爆炸性气体混合物。
文献FR 1,410,494确定了形成这种爆炸性混合物的风险,并提出了一种避免混合物着火的手段,即在蒸馏塔的层级之间放置金属泡沫以消散甲烷氧气化反应热,从而避免爆炸。然而,所提出的手段未避免将产生二氧化碳和水的甲烷氧化反应,这些是不希望的化合物,因为在低温下它们可能阻塞塔。
文献US 3,989,478提出调节蒸馏使得离开塔顶的气体含有至少20%的甲烷,使得蒸馏区中的气相组成不是爆炸性的。这种调节的缺点是,如果塔顶气体含有20%的甲烷,其余是空气,则它极其接近爆炸性。此外,顶部气体中甲烷的损失显著。最后,没有提及蒸馏塔中的天然氧气浓度,因此用该方法不能避免形成爆炸性气体混合物。
另一种解决方案是稀释来自蒸馏塔的气体和/或液体混合物,使得该浓度返回到使得混合物在具有氧气浓度富集的区域中为非爆炸性的值。
因此,文献FR 2,971,331提出了通过将液态甲烷泵入蒸馏塔底来进行稀释并将其再注入塔顶。尽管所提出的手段避免在塔中形成爆炸性混合物,但是它导致增加塔中液态甲烷的存量,并因此增加储存的能量,这从工艺安全性角度是不希望的。还必须安装液体甲烷泵,这是潜在危险泄漏的来源。
文献FR 2,971,332提出通过用取自外源的氮气进行稀释来避免在塔内形成爆炸性混合物。因此,需要使用流体氮用于稀释。流体具有成本,因此增加了该过程的操作成本。应该注意的是,在该文献中,注入塔底的气态甲烷是来自冷凝器-再沸器的可燃物流。它专门用作关系到进料流的蒸馏的上升气相。没有这样的物流,蒸馏是不可能的。
文献US 2,519,955记载了甲烷和氧气混合物的生产方法。与本发明不同,其思想不是将甲烷与氧气分离以降低爆炸风险,反而是将它们结合。基本上,该方法包括将富甲烷但贫氧气的生物气流进行减压,然后在放置于蒸馏塔中的交换器内回收产生的热量。在交换器内,将由液态甲烷组成的进料流的一部分再注入塔底,而将由氮气组成的另一部分在高于进料流的层级处再注入塔顶。因此,氮气流不用作稀释物流,而是用以通过占据塔顶体积来限制甲烷的损失。
本发明提出要解决的问题是改善用于混合物的低温分离的方法,其浓度总是在爆炸区之外并且没有上述缺点。
此外,为了能够通过低温蒸馏进行O2和N2相对于CH4的分离,需要具有 CO2浓度特别低的物流。普遍接受的值是50ppmv-百万分之体积份-的二氧化碳最大值,以避免会堵塞低温交换器的晶体形成。类似地,必须消除水以避免结冰。
为解决该问题,文献FR 2,917,489提出通过在蒸馏塔底部以液态收集并随后汽化的富甲烷的气体,将温度或压力调制吸附器中使用的吸附剂进行再生。使用这种用于再生的流体的缺点在于,需要通过将吸附床出口流与富甲烷的物流混合,来将二氧化碳的量控制到在吸附床的出口处为恒定值。该控制是必要的,因为含有少量来自再生的二氧化碳的富甲烷的物流旨在以生物甲烷形式使用。然而,为了注入天然气网络,必须严格满足网络运营商的质量要求。
因此,本发明提出要解决的第二个问题是从来自低温分离的物流中再生温度或压力调制吸附器中使用的吸附剂而不会导致上述缺陷。
为了解决所有这些问题,本申请人开发了一种低温分离方法,其中O2稀释物流基本上由氮气组成并且来自进料流而不是外源。这导致显著的成本减少。
更确切地,本发明的目的是用于含有甲烷和空气气体的进料流的低温分离方法,其中:
-将进料流冷却以产生冷却的物流;
-将冷却的物流的至少一部分送至蒸馏塔的一级;
-从蒸馏塔中采出底部物流,其中底部物流与进料流相比富含甲烷;
-从蒸馏塔中采出与进料流相比富含氧气和氮气的物流;
-将至少一种不可燃且比氧气更易挥发的稀释物流(意指基本上含有氮气的物流)在比添加冷却的物流的级低至少一级处添加至蒸馏塔。
该方法的特征在于从进料流中提取稀释物流。
在一个优选的实施方案中:
-将冷却的物流至少部分地冷凝;
-然后将至少部分地冷凝的冷却的物流减压;
-通过分离在减压出口处产生的气体馏分来产生稀释物流。
在实践中,进料流含有60至97%的甲烷、3至50%之间的氮气和氧气以及 3%或更少的二氧化碳。
申请人表明,在圆底分离器中将蒸馏塔的进料流先减压,然后在蒸馏塔的填料的下部中注入由此产生的基本上包括氮气的气相(意味着气流的上游),将导致气态氧气的充分稀释,由于这种吹扫流,气态氧气的浓度足够低,使得与甲烷的混合物不可燃。接下来将包含基本上液态甲烷的进料流的液体馏分注入待蒸馏的塔的顶部。
由于进料流的气相与液相的分离以及全部或部分气相的再注入,因此不必使用来自外源的气态氮气作为吹扫流体,从而使氮气消耗降低。
同样地,使用待处理的来自进料流的气体本身作为稀释物流,无论其来自冷却的物流的减压还是在其另一个处理步骤结束时,都不排除将其与来自外源的稀释物流结合。这两种稀释物流可以以单一混合物的形式或分别添加至蒸馏塔。
在实践中,需要冷却塔顶以冷凝所述塔顶中的上升的富氮气体以及必要时来自分离器的进料流的一部分气体。
在第一实施方案中,通过将来自减压的进料流与制冷流体混合以进行冷却来冷却塔顶。换言之,制冷流体流用作塔顶气体冷凝的冷源,并且通过提供仅一部分来自进料流减压的气体的冷凝(另一部分构成稀释物流),来参与蒸馏塔中的氧气稀释作用。
根据本发明,在分离器之前通过将进料流与制冷流体混合,或在分离器中通过将制冷流体直接加入分离器,来冷却进料流。
在第二实施方案中,通过直接添加至塔顶的制冷流体来冷却塔顶。
在实践中,制冷流体是液氮。
在一个具体实施方案中,塔含有多个蒸馏段,且在两个段之间引入稀释进料;
在实践中,蒸馏段为填料或蒸馏平台的形式。在所有情形中,将蒸馏段布置成使得液相将其最易挥发的化合物释放至气相,并且气相将其最小挥发性的化合物释放至液相。
如已经陈述过的,本发明的方法具有与通过纯化来自NHWS的生物气来生产生物甲烷相关的特别有利的应用。
为了能够通过低温蒸馏进行O2和N2相对于CH4的分离,需要具有CO2浓度特别低的物流。普遍接受的值是50ppmv-百万分之体积份-的二氧化碳最大值,以避免会堵塞低温交换器的晶体形成。类似地,出于同样的原因,必须消除水。
换言之,根据本发明,在低温分离之前提供进料流,该进料流富甲烷,含有氮气和氧气,并且具有事先降低的CO2浓度。
为此,通过将富CO2的进料流加入至少一个纯化单元中来降低CO2浓度,优选通过吸附,例如负载能够可逆地吸附大部分CO2的吸附剂的压力调制(PSA) 或温度调制(PTSA)吸附。
这种类型的纯化器是本领域技术人员已知的。在实践中,对于连续操作,至少两个PSA或PTSA并行使用,其中一个用于吸附以消除二氧化碳,而另一个用于再生。通过降低压力,并通过用事先加热的气体吹扫以提供解吸所需的能量,来完成再生。
在第一实施方案中,用于吸附器中的吸附剂通过从塔顶采出的富氧气和氮气的气流进行再生。在实践中,从塔顶采出的贫甲烷的物流含有60%至100%之间的氮气和氧气。
实际上发现,注入塔中的贫甲烷的且还含有氮气的塔顶气体,由于氮气注入,具有足够的流速,以执行吸附剂筛的加热和冷却循环,这对于在再生期间完成二氧化碳解吸是必需的。在这种情况下,不再需要使用从塔底采出的甲烷流来再生吸附剂从而在床出口流中保持恒定的二氧化碳浓度。因此,采出液体形式的富甲烷的物流并将其用作液化天然气是可能的。
在实践中,塔底处的富甲烷的物流含有95%至100%之间的甲烷。
然后,可以以两种不同的方式使用来自再生的负载CO2的气体:或者将负载气体送至氧气破坏系统,或者,若甲烷浓度足够,则将负载气体送至燃烧系统进行电力生产(热电联产微型涡轮机或发动机)。
在第二实施方案中,用于吸附器中的吸附剂通过从塔底抽出的富甲烷的气体而再生。
本发明的另一主题是通过实施上述方法纯化来自非危险废物贮存设备 (NHWSF)的生物气以生产生物甲烷的设备,并且其依次包括:
-用于通过吸附进行二氧化碳纯化的单元,所述吸附能够贫化进料流中的二氧化碳;
-能够冷却贫CO2的物流的热交换器;
-能够通过与从塔底采出的液体进行热交换来冷凝贫CO2的物流的冷凝器- 再沸器;
-用于冷凝流的减压的装置;
-用于从冷凝流中分离液相和气相的圆底分离器;
-蒸馏塔;
-能够将液相从圆底分离器输送至蒸馏塔的一级的导管;
-能够将气相(稀释物流)从圆底分离器在比添加液相的级低至少一级处输入塔中的导管;
-连接至制冷流体源以用于将液氮流送至与进料流混合的位点或者直接送入圆底分离器的装置。
根据本发明的设备还包括:
-用于从塔底采出富甲烷的液体流以将其送入冷凝器-再沸器并产生富甲烷的气流的装置;
-用于将富甲烷的气流返回至塔底的装置;
-用于从塔顶收集贫甲烷的气流并将其送至热交换器的装置;
-用于从塔底收集富甲烷的气流并将其送至热交换器的装置;
-用于将在交换器中再加热的贫甲烷的物流或在交换器中再加热的富甲烷的物流收集至纯化单元的装置。
从由附图支持的以下实施例,本发明及产生的益处将变得清楚。
图1示出甲烷、氧气和氮气混合物的爆炸性图。
图2至4是集成入用于通过纯化来自无危险废物贮存(NHWS)的生物气以生产生物甲烷的设备(部分显示)的低温分离单元的图。这些附图的不同在于低温分离后物流的最终用途。
甲烷、氧气和氮气混合物的爆炸性图如图1所示。在该图中,爆炸性区域是灰的。对于没有安装圆底分离器的情形,在塔的整个高度上的气相的组成用虚线表示;然后蒸气相穿入爆炸区。在安装圆底相分离器,并且用产生的气相吹扫填料的情况下,则塔中上升的气相不是爆炸性的。
对于图2至4中的每一个,将在5至15bar绝对压力下包含60%至97%的甲烷、3%至50%的氮气和氧气以及3%或更少的二氧化碳的进料气流(1)加入用于通过吸附进行纯化的单元(2),有利地是PTSA,以便将水和二氧化碳浓度降低至小于或等于50ppmv的值。
然后通过与富甲烷的液体物流(20)和贫甲烷的物流(23)进行热交换,在热交换器(4)中冷却由此产生的物流(3)。将冷却的物流(5)送入再沸器冷凝器(6),在其中通过与底部液体的热交换再次冷却,使底部液体可以沸腾并产生将用于蒸馏的富甲烷的气体,也可用以冷凝进料流。
然后将冷凝物流(7)在减压构件(8)中减压至塔(18)的操作压力,该操作压力为1至5bar绝对压力。
根据图2和3,将来自液氮储存器(12)的液氮流(13)在减压构件(14) 中减压,并将减压流(15)与进料流(9)在位点16处混合,用以接下来引入用于分离液相和气相的圆底容器(11)中。在未示出的一个实施方案中,将液氮直接注入圆底分离器中。
该实施方案与图4所示的实施方案的不同之处在于,液氮通过例如注射喷嘴(16)直接注入蒸馏塔的上部。
对于所有实施方案,接下来将来自圆底分离器(11)的富液氮的液相(19) 加入蒸馏塔(18)的上部。将气相(17)加入蒸馏塔(18)的填料的下部以构成吹扫气体并参与蒸馏。
由此,蒸馏产生两种物流:蒸馏塔的底部的富甲烷的物流(20),和在蒸馏塔顶部的富O2和N2的贫甲烷的物流(23)。
将富甲烷的液体物流(20)的一部分送至交换器(4)以蒸发并形成气态物流(22)。可以以两种方式使用该气态物流。
如图2所示,气态物流(22)按原样使用。将其输送以用于通过注射站注入天然气网络中,或送至压缩站以产生压缩天然气,例如用于车辆天然气。
如图3所示,该气态物流(22)用于再生纯化单元(2)并形成含有来自纯化单元的再生的二氧化碳的富甲烷物流(26)。接下来将物流(26)送至压缩站以产生压缩天然气,例如用于天然气车辆。
在未示出的实施方案中,将富甲烷的物流(20)以液体形式采出并用作液化天然气。
对于所有实施方案,将塔底中的富甲烷的液体物流的另一部分送至再沸器冷凝器(6)以进行蒸发。将由此产生的气流(21)送至蒸馏塔以产生参与蒸馏的上升蒸气。
然后将包含氧气、氮气和甲烷馏分的气流(23)送至交换器(4)进行再加热。
在图2所示的实施方案中,离开交换器的物流(24)用于再生纯化单元(2) 并产生物流(25),然后处理物流(25)以在氧化器中燃烧残留的甲烷。
若甲烷浓度超过25%,则物流(25)可用于热电联产发动机或微型涡轮机中以产生电力。
在图3所示的实施方案中,将物流(25)直接送至甲烷氧化或上述利用系统。
Claims (11)
1.一种用于含有甲烷和空气气体的进料流的低温分离方法,其中:
-将进料流冷却以产生冷却的物流;
-将所述冷却的物流的至少一部分送至蒸馏塔的一级;
-从所述蒸馏塔中采出底部物流,其中所述底部物流与所述进料流相比富含甲烷;
-从所述蒸馏塔中采出与所述进料流相比富含氧气和氮气的物流;
-将至少一种不可燃且比氧气更易挥发的稀释物流在比添加所述冷却的物流的级低至少一级处添加至所述蒸馏塔,其特征在于从所述进料流中提取所述稀释物流。
2.根据权利要求1所述的方法,其特征在于:
-将所述冷却的物流至少部分地冷凝;
-然后将至少部分冷凝的冷却的物流进行减压;
-通过分离在减压的出口处产生的气体馏分来产生所述稀释物流。
3.根据权利要求2所述的方法,其特征在于,通过将来自所述减压的进料流与制冷流体混合以冷却来自所述减压的进料流来冷却塔顶。
4.根据权利要求1或2之一所述的方法,其特征在于通过直接添加至塔顶的制冷流体来冷却所述塔顶。
5.根据权利要求3至4之一所述的方法,其特征在于所述制冷流体是液氮。
6.根据权利要求2所述的方法,其特征在于所述塔含有多个蒸馏段,并且将来自分离器的蒸气相添加在两个段之间。
7.根据前述权利要求之一所述的方法,其特征在于提供富甲烷、含有氮气和氧气并且具有事先降低的CO2浓度的进料流。
8.根据权利要求7所述的方法,其特征在于通过将富CO2的进料流加入至少一个纯化单元中来降低所述CO2浓度,优选通过负载能够可逆地吸附大部分所述CO2的吸附剂的吸附进行。
9.根据权利要求8所述的方法,其特征在于所述纯化单元是用于通过PSA或PTSA型的吸附进行纯化的单元,且所述PSA或PTSA通过从所述塔顶采出的富氧气和氮气的气流进行再生。
10.根据权利要求8所述的方法,其特征在于所述纯化单元是用于通过PSA或PTSA型的吸附进行纯化的单元,且所述PSA或PTSA通过从所述塔底采出的富甲烷的气流进行再生。
11.通过实施根据权利要求1至10的方法纯化来自非危险废物贮存设备(NHWSF)的生物气以生产生物甲烷的设备,其依次包括:
-用于通过吸附进行二氧化碳纯化的单元,所述吸附能够贫化进料流中的二氧化碳;
-能够冷却贫CO2的物流的热交换器;
-能够通过与从塔底采出的液体进行热交换来冷凝贫CO2的物流的冷凝器-再沸器;
-用于对冷凝物流减压的装置;
-用于从冷凝物流中分离液相和气相的圆底分离器;
-蒸馏塔;
-能够将所述液相从所述圆底分离器输送至蒸馏塔的一级的导管;
-能够将所述气相从所述圆底分离器在比添加所述液相的级低至少一级处输送至所述塔中的导管;
-连接至制冷流体源以用于将液氮流送至与所述进料流混合的位点或者直接送入所述圆底分离器的装置。
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR1654798A FR3051892B1 (fr) | 2016-05-27 | 2016-05-27 | Procede de separation cryogenique d'un debit d'alimentation contenant du methane et des gaz de l'air, installation pour la production de bio methane par epuration de biogaz issus d'installations de stockage de dechets non-dangereux (isdnd) mettant en œuvre le procede |
FR1654798 | 2016-05-27 | ||
PCT/FR2017/050651 WO2017203112A1 (fr) | 2016-05-27 | 2017-03-20 | Procede de separation cryogenique d'un debit d'alimentation contenant du methane et des gaz de l'air, installation pour la production de bio methane par epuration de biogaz issus d'installations de stockage de dechets non-dangereux (isdnd) mettant en œuvre le procede |
Publications (2)
Publication Number | Publication Date |
---|---|
CN109257937A true CN109257937A (zh) | 2019-01-22 |
CN109257937B CN109257937B (zh) | 2020-04-10 |
Family
ID=56511766
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN201780032072.6A Active CN109257937B (zh) | 2016-05-27 | 2017-03-20 | 含甲烷和空气气体的进料流的低温分离方法及其实施设备 |
Country Status (15)
Country | Link |
---|---|
US (2) | US11713920B2 (zh) |
EP (1) | EP3465035B1 (zh) |
CN (1) | CN109257937B (zh) |
AU (1) | AU2017270649B2 (zh) |
BR (1) | BR112018074225B1 (zh) |
CA (1) | CA3024382C (zh) |
ES (1) | ES2791491T3 (zh) |
FR (1) | FR3051892B1 (zh) |
HU (1) | HUE050463T2 (zh) |
MX (1) | MX369339B (zh) |
PL (1) | PL3465035T3 (zh) |
PT (1) | PT3465035T (zh) |
RS (1) | RS60676B1 (zh) |
RU (1) | RU2715636C1 (zh) |
WO (1) | WO2017203112A1 (zh) |
Families Citing this family (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR3075658B1 (fr) * | 2017-12-21 | 2022-01-28 | Air Liquide | Procede de limitation de la concentration d'oxygene contenu dans un courant de biomethane |
FR3075660B1 (fr) * | 2017-12-21 | 2019-11-15 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede de distillation d'un courant gazeux contenant de l'oxygene |
WO2020010430A1 (en) | 2018-07-10 | 2020-01-16 | Iogen Corporation | Method and system for producing a fuel from biogas |
CN109405413B (zh) * | 2018-11-17 | 2024-01-30 | 杭州宏盛中弘新能源有限公司 | 一种避开爆炸极限的含氧煤层气低温精馏系统及方法 |
WO2021003564A1 (en) | 2019-07-09 | 2021-01-14 | Iogen Corporation | Method and system for producing a fuel from biogas |
US20210060486A1 (en) | 2020-11-11 | 2021-03-04 | Waga Energy | Facility For Producing Gaseous Biomethane By Purifying Biogas From Landfill Combining Membranes, Cryodistillation And Deoxo |
US20210055046A1 (en) | 2020-11-11 | 2021-02-25 | Waga Energy | Facility For Producing Gaseous Methane By Purifying Biogas From Landfill, Combining Membranes And Cryogenic Distillation For Landfill Biogas Upgrading |
FR3116445B1 (fr) | 2020-11-23 | 2023-11-17 | Waga Energy | Procédé de séparation cryogénique d'un débit d'alimentation à base de biométhane, procédé de production de biométhane intégrant ladite séparation cryogénique et installation associée. |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2519955A (en) * | 1946-09-03 | 1950-08-22 | Shell Dev | Production of hydrocarbon-oxygen mixtures |
DE951875C (de) * | 1955-02-16 | 1956-11-08 | Linde Eismasch Ag | Verfahren zum Abscheiden von Methan aus methanreichen Gemischen mit Luft |
GB1482196A (en) * | 1973-09-27 | 1977-08-10 | Petrocarbon Dev Ltd | Upgrading air-contaminated methane gas compositions |
FR2917489A1 (fr) * | 2007-06-14 | 2008-12-19 | Air Liquide | Procede et appareil de separation cryogenique d'un debit riche en methane |
FR2971332A1 (fr) * | 2011-02-09 | 2012-08-10 | Air Liquide | Procede et appareil de separation cryogenique d'un debit riche en methane |
FR2971331A1 (fr) * | 2011-02-09 | 2012-08-10 | Air Liquide | Procede et appareil de separation cryogenique d'un debit riche en methane |
Family Cites Families (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE481875C (de) | 1929-09-02 | E H Heinrich Koppers Dr Ing | Kammerofen zur Destillation von Kohle u. dgl. | |
BE652537A (zh) | 1963-09-06 | 1964-12-31 | ||
DE3486017T3 (de) * | 1983-03-08 | 1999-03-04 | Daidousanso Co. Ltd., Osaka | Sehr reiner Stickstoffgaserzeugungsapparat. |
US4889545A (en) * | 1988-11-21 | 1989-12-26 | Elcor Corporation | Hydrocarbon gas processing |
US5051120A (en) * | 1990-06-12 | 1991-09-24 | Union Carbide Industrial Gases Technology Corporation | Feed processing for nitrogen rejection unit |
GB0116960D0 (en) * | 2001-07-11 | 2001-09-05 | Boc Group Plc | Nitrogen rejection method and apparatus |
US6425266B1 (en) * | 2001-09-24 | 2002-07-30 | Air Products And Chemicals, Inc. | Low temperature hydrocarbon gas separation process |
US7025803B2 (en) | 2002-12-02 | 2006-04-11 | L'Air Liquide Societe Anonyme A Directoire et Counsel de Surveillance Pour L'Etude et L'Exploration des Procedes Georges Claude | Methane recovery process |
US8221524B2 (en) | 2009-10-23 | 2012-07-17 | Guild Associates, Inc. | Oxygen removal from contaminated gases |
DE102010020282A1 (de) * | 2010-05-12 | 2011-11-17 | Linde Aktiengesellschaft | Stickstoff-Abtrennung aus Erdgas |
EP3390941A1 (en) * | 2015-12-14 | 2018-10-24 | Exxonmobil Upstream Research Company | Method and system for separating nitrogen from liquefied natural gas using liquefied nitrogen |
FR3046086B1 (fr) * | 2015-12-24 | 2018-01-05 | Waga Energy | Procede de production de biomethane par epuration de biogaz issu d'installations de stockage de dechets non-dangereux (isdnd) et installation pour la mise en œuvre du procede |
-
2016
- 2016-05-27 FR FR1654798A patent/FR3051892B1/fr active Active
-
2017
- 2017-03-20 CN CN201780032072.6A patent/CN109257937B/zh active Active
- 2017-03-20 PT PT177169570T patent/PT3465035T/pt unknown
- 2017-03-20 AU AU2017270649A patent/AU2017270649B2/en active Active
- 2017-03-20 US US16/303,551 patent/US11713920B2/en active Active
- 2017-03-20 RU RU2018140911A patent/RU2715636C1/ru active
- 2017-03-20 BR BR112018074225-2A patent/BR112018074225B1/pt active IP Right Grant
- 2017-03-20 ES ES17716957T patent/ES2791491T3/es active Active
- 2017-03-20 MX MX2018014400A patent/MX369339B/es active IP Right Grant
- 2017-03-20 HU HUE17716957A patent/HUE050463T2/hu unknown
- 2017-03-20 PL PL17716957T patent/PL3465035T3/pl unknown
- 2017-03-20 RS RS20200601A patent/RS60676B1/sr unknown
- 2017-03-20 EP EP17716957.0A patent/EP3465035B1/fr active Active
- 2017-03-20 CA CA3024382A patent/CA3024382C/fr active Active
- 2017-03-20 WO PCT/FR2017/050651 patent/WO2017203112A1/fr unknown
-
2023
- 2023-06-15 US US18/210,413 patent/US20230384027A1/en active Pending
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2519955A (en) * | 1946-09-03 | 1950-08-22 | Shell Dev | Production of hydrocarbon-oxygen mixtures |
DE951875C (de) * | 1955-02-16 | 1956-11-08 | Linde Eismasch Ag | Verfahren zum Abscheiden von Methan aus methanreichen Gemischen mit Luft |
GB1482196A (en) * | 1973-09-27 | 1977-08-10 | Petrocarbon Dev Ltd | Upgrading air-contaminated methane gas compositions |
FR2917489A1 (fr) * | 2007-06-14 | 2008-12-19 | Air Liquide | Procede et appareil de separation cryogenique d'un debit riche en methane |
FR2971332A1 (fr) * | 2011-02-09 | 2012-08-10 | Air Liquide | Procede et appareil de separation cryogenique d'un debit riche en methane |
FR2971331A1 (fr) * | 2011-02-09 | 2012-08-10 | Air Liquide | Procede et appareil de separation cryogenique d'un debit riche en methane |
Also Published As
Publication number | Publication date |
---|---|
US20200318896A1 (en) | 2020-10-08 |
MX2018014400A (es) | 2019-02-14 |
AU2017270649A1 (en) | 2018-12-06 |
CN109257937B (zh) | 2020-04-10 |
ES2791491T3 (es) | 2020-11-04 |
US11713920B2 (en) | 2023-08-01 |
CA3024382A1 (fr) | 2017-11-30 |
FR3051892A1 (fr) | 2017-12-01 |
PT3465035T (pt) | 2020-06-17 |
US20230384027A1 (en) | 2023-11-30 |
RU2715636C1 (ru) | 2020-03-02 |
FR3051892B1 (fr) | 2018-05-25 |
AU2017270649B2 (en) | 2023-03-23 |
HUE050463T2 (hu) | 2020-12-28 |
BR112018074225B1 (pt) | 2023-04-04 |
MX369339B (es) | 2019-11-05 |
BR112018074225A2 (pt) | 2019-03-06 |
PL3465035T3 (pl) | 2020-08-10 |
EP3465035B1 (fr) | 2020-05-13 |
RS60676B1 (sr) | 2020-09-30 |
EP3465035A1 (fr) | 2019-04-10 |
WO2017203112A1 (fr) | 2017-11-30 |
CA3024382C (fr) | 2022-06-14 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CN109257937A (zh) | 用于含甲烷和空气气体的进料流的低温分离的方法、用于通过实施该方法纯化源自非危险废物贮存设备(nhwsf)的生物气以生产生物甲烷的设备 | |
US11708313B2 (en) | System and process for recovering methane and carbon dioxide from biogas and reducing greenhouse gas emissions | |
US10905995B2 (en) | Method for producing biomethane by purifying biogas from non-hazardous waste storage facilities and facility for implementing the method | |
US7731779B2 (en) | Method for processing landfill and other stranded gas containing commercial quantities of methane and contaminated by carbon dioxide, nitrogen and oxygen into a pipeline or vehicle quality natural gas product | |
US3989478A (en) | Producing gaseous fuels of high calorific value | |
US20240019205A1 (en) | Facility for producing gaseous methane by purifying biogas from landfill, combining membranes and cryogenic distillation for landfill biogas upgrading | |
US6071326A (en) | Process for the production of naphtha gas from landfill gas | |
MX2012001425A (es) | Metodo para producir hierro de reduccion directa con emisiones limitadas de co2. | |
WO2006106253A2 (fr) | Procede et installation integres d'adsorption et de separation cryogenique pour la production de co2 | |
CN105293436A (zh) | 一种利用焦炉煤气制取冶金还原气联产液化天然气的工艺 | |
CN104293402B (zh) | 一种含氢气、一氧化碳的甲烷气分离提纯制液化天然气的方法 | |
RU2675581C2 (ru) | Способы и системы получения железа прямого восстановления и газообразного топлива для сталелитейного завода | |
US10132562B2 (en) | Process and device for the cryogenic separation of a methane-rich stream | |
CN1198405A (zh) | 使用低纯度氧生产氨并且分离氩的方法 | |
CA3085236A1 (fr) | Method for distilling a gas stream containing oxygen | |
CN115523718A (zh) | 其中在中间级处提取并且在外部固化二氧化碳的生物气低温纯化 | |
FR2971331A1 (fr) | Procede et appareil de separation cryogenique d'un debit riche en methane | |
US8978413B2 (en) | Rare gases recovery process for triple column oxygen plant | |
CN116045608A (zh) | 用于生产氪氙混合物的设备和方法 | |
CA3085239A1 (en) | Method for limiting the concentration of oxygen contained in a biomethane stream |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PB01 | Publication | ||
PB01 | Publication | ||
SE01 | Entry into force of request for substantive examination | ||
SE01 | Entry into force of request for substantive examination | ||
REG | Reference to a national code |
Ref country code: HK Ref legal event code: DE Ref document number: 1262985 Country of ref document: HK |
|
GR01 | Patent grant | ||
GR01 | Patent grant |