CN1407304A - Improved light hydrocarbon deep cooling separating method - Google Patents
Improved light hydrocarbon deep cooling separating method Download PDFInfo
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- CN1407304A CN1407304A CN 01132960 CN01132960A CN1407304A CN 1407304 A CN1407304 A CN 1407304A CN 01132960 CN01132960 CN 01132960 CN 01132960 A CN01132960 A CN 01132960A CN 1407304 A CN1407304 A CN 1407304A
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- carbon
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- methane
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- 238000000034 method Methods 0.000 title claims abstract description 63
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 26
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 26
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 20
- 238000001816 cooling Methods 0.000 title claims description 23
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 68
- 239000007789 gas Substances 0.000 claims abstract description 52
- 239000007791 liquid phase Substances 0.000 claims abstract description 35
- 239000007788 liquid Substances 0.000 claims abstract description 26
- 230000008569 process Effects 0.000 claims abstract description 22
- 239000012071 phase Substances 0.000 claims abstract description 18
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 16
- 239000001257 hydrogen Substances 0.000 claims abstract description 16
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000000203 mixture Substances 0.000 claims abstract description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 83
- 229910052799 carbon Inorganic materials 0.000 claims description 83
- 238000000926 separation method Methods 0.000 claims description 24
- 238000005201 scrubbing Methods 0.000 claims description 20
- 238000007600 charging Methods 0.000 claims description 15
- 238000004140 cleaning Methods 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 150000002431 hydrogen Chemical class 0.000 claims description 7
- 238000005406 washing Methods 0.000 claims description 6
- 239000007792 gaseous phase Substances 0.000 claims description 5
- 230000008859 change Effects 0.000 claims description 4
- 238000005057 refrigeration Methods 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 3
- 238000005204 segregation Methods 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 230000008901 benefit Effects 0.000 abstract description 2
- 239000003507 refrigerant Substances 0.000 abstract 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 59
- 239000005977 Ethylene Substances 0.000 description 30
- 239000000463 material Substances 0.000 description 14
- 238000005984 hydrogenation reaction Methods 0.000 description 9
- 241000282326 Felis catus Species 0.000 description 8
- 238000011084 recovery Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 4
- 238000004134 energy conservation Methods 0.000 description 4
- 235000019628 coolness Nutrition 0.000 description 3
- 238000005336 cracking Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 2
- 238000007701 flash-distillation Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 101000911390 Homo sapiens Coagulation factor VIII Proteins 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000001345 alkine derivatives Chemical class 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 102000057593 human F8 Human genes 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229940047431 recombinate Drugs 0.000 description 1
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- 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
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- 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
- F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
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- 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
- F25J3/0238—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 2 carbon atoms or more
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- 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
- F25J3/0252—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 hydrogen
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- 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
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- 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
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- 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
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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- 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
- F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
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- 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
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- 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
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- 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
- F25J2210/12—Refinery or petrochemical off-gas
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- 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
- F25J2215/62—Ethane or ethylene
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- 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
- F25J2270/04—Internal refrigeration with work-producing gas expansion loop
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- 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
- F25J2270/12—External refrigeration with liquid vaporising loop
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- 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
- F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
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- 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
- F25J2290/40—Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
An improved deep-cold process for separating light hydrocarbon mixture is disclosed. The compressed and cooled raw hydrocarbons gas is separated into gas and liquid. The gas phase comes in distributor to make all the C3 components, the most of C2 components and less methane come in bottom liquid phase. Its top gas phase is cooled and flash-vaporated, and then comes in hydrogen system. The resultant all the liquid components come in the demethonizing tower to obtain the top gas not containing C3 component and bottom liquid not containing methane. Said top gas comes also in the demethanizing tower. Its advantages are low load to cooler and demethanizing tower and less refrigerant and energy consumption.
Description
The present invention relates to the deep cooling separating method of light hydrocarbon mixture.More particularly, relate to improvement, so that the new method of operating that further cuts down the consumption of energy and improve yield of ethene to be provided to the light component refrigerated separation.
Mainly containing hydrogen, methane, carbon two, carbon three and the light hydrocarbon mixture of carbon four generally separates by cryogenic method.In the order separation process of ethylene unit, common way is at first unstripped gas to be compressed to 3.4MPa～3.9MPa, gas phase is cooled off and flash distillation step by step then, be cooled to-163～-169 ℃ at last, isolate hydrogen and methane hydrogen liquid phase in hydrogen gas tank, the liquid phase of each flash tank enters domethanizing column, and it is low that the operating pressure of this tower has height to have with the difference of technology, generally in 0.59MPa～3.1MPa scope, tower top temperature-135～-98 ℃.In predepropanization front-end hydrogenation flow process, be at first with carbon three and more light component and carbon four and more heavy ends separate, adopt then with the similar method of order separation process lighter hydrocarbons carried out cryogenic separation.The deep cooling separating method energy consumption of this routine is higher and the ethylene recovery rate is lower, reason is: for material being cooled to needed temperature, usually draw one liquid phase methane and carry out throttling from demethanation tower return tank, for system provides cold, increase the load of low temperature ethylene cryogen, also lost some ethene; Because the liquid phase of flash tank all enters domethanizing column, the domethanizing column load is big; Hydrogen gas tank and domethanizing column lose a certain amount of ethene.
Chinese patent CN1023685C has narrated the light hydrocarbon separating method that is used for the ethene sequence flow, and it adopts pre-dethanizer that the unstripped gas from the compressional zone is carried out non-clear cutting apart.The cat head of pre-dethanizer not carbon containing three, tower still does not contain methane, has reduced the load of domethanizing column bottom like this.But because pre-dethanizer increases carbon two amounts that enter ice chest, move after making cold, cause promptly more that the cryogen consumption of low temperature increases, so do not reach purpose of energy saving.Still lose a certain amount of ethene in addition in the tail gas.
Chinese patent CN1048713C has increased methane absorber on the basis of CN1023685C, though the ethylene loss in the tail gas is decreased, do not change the problem of moving behind the cold.
The objective of the invention is to improve existing light hydrocarbon separating method, provide a kind of being used for effectively to separate, the both energy-conservation and high light hydrocarbon separating method of ethylene recovery rate containing hydrogen, methane, carbon two and the third-class lighter hydrocarbons of carbon.
For achieving the above object, the main feature of light hydrocarbon separating method of the present invention is, lighter hydrocarbons after boosting at first enter the component distributor through precooling, whole carbon three components in the gas phase are changed in the liquid phase of component distributor bottom, simultaneously most of carbon two and a small amount of methane are also forwarded in the tower bottoms.The gas phase at component distributor top is through entering the Hydrogen Separation system after the refrigerated separation step by step.Separate the liquid phase that obtains step by step and enter domethanizing column.The liquid phase of component distributor bottom enters pre-domethanizing column, and pre-domethanizing column is separated into the overhead stream of carbon containing three not and the still liquid of carbon containing one not with charging.
The invention provides a kind of deep cooling separating method of light hydrocarbon mixture, this method comprises:
After light hydrocarbon feedstocks gas enters knockout drum and carries out gas-liquid separation, the component distributor is set in the downstream of gaseous phase outlet and pre-domethanizing column is set in the downstream of the liquid phase outlet of the liquid phase outlet of knockout drum and component distributor;
Light hydrocarbon feedstocks gas through overcompression, drying and precooling enters knockout drum;
The gas phase that knockout drum separates is further sent into the bottom of component separator after the cooling, this device in through washing and cooling with whole carbon three and most of carbon two and on a small quantity methane change over to bottom the component distributor, bottom liquid phases enters the top of pre-domethanizing column; Component distributor top gas is carbon containing three not, separates obtaining the multiply liquid phase with flash tank through a series of cooler coolings, enters the middle and upper part diverse location of domethanizing column respectively successively;
Through the liquid phase that knockout drum separates, pre-domethanizing column is sent in carbon containing two, carbon three and more heavy ends and methane on a small quantity;
The liquid phase that pre-domethanizing column separates knockout drum and the bottom liquid phases of component distributor are separated into the tower overhead gas of carbon containing three not and do not contain the tower bottoms of methane, and tower overhead gas is sent into the domethanizing column bottom;
Domethanizing column is separated into tower overhead gas methane and tower bottoms carbon two with the multiply charging.
A preferred implementation of the inventive method also comprises:
In the end one-level flash tank downstream is provided with carbon two scrubbing towers;
The gas phase that flash tank separates enters the bottom of carbon two scrubbing towers after the cooler cooling, introduce one liquid that contains methane and small quantity of hydrogen from the top of tower gas in the tower is washed, and carbon two is washed in the tower bottoms, and tower bottoms is sent into the topmost of domethanizing column; Tower overhead gas enters downstream hydrogen/methane separation system.Wherein, preferably adopt the partial condensation liquid of carbon two scrubbing tower tower overhead gases as cleaning solution.
Described component separator can be any separator that makes carbon two in the light hydrocarbon mixture and methane component change bottom of device by a certain percentage over to, for example, comprises scrubbing tower, fractionating column, fractional condensation separator or segregation fractionating column.As select scrubbing tower for use, and can be any type of tower, comprise plate column and packed tower.The number of plates generally is less than 20, so tower can be very not high, invests also few.Preferable methods is to adopt the condensate liquid of tower overhead gas as cleaning solution.When adopting the cat head gaseous condensate as cleaning solution, condenser and condensate flash jar can place on cat head or the higher platform, and liquid relies on gravity to return cat head, can reduce pipeline consumption and cryogenic pump of cancellation like this.
The gas phase that enters the component distributor can be removed whole carbon three through washing and cooling, surpasses 50% carbon two simultaneously and surpass 10% part methane also to wash the auto levelizer bottom, and the present invention does not require in the liquid phase of bottom of device and do not contain methane.
When domethanizing column is operated under high pressure (about 3.0MPa), in the tower overhead gas outlet downstream of domethanizing column decompressor is set, tower overhead gas methane is carried out swell refrigeration, for cooling system provides cold.
Accompanying drawing and explanation thereof:
Fig. 1 is a process flow diagram of the present invention
Fig. 2 is a preferred version process flow diagram of the present invention
Fig. 3 is the process flow diagram that the present invention is applied to the predepropanization front-end hydrogenation flow process of ethylene unit
Fig. 4 is the process flow diagram that the present invention is applied to the sequence flow of ethylene unit
Describe the characteristics of the inventive method in detail below in conjunction with accompanying drawing.
As shown in Figure 1, unstripped gas is cooled to-15～-21 ℃ through behind the compression drying, and enters knockout drum 1, and the main carbon containing two/three of isolated liquid phase reaches more to recombinate and divides and a small amount of methane, and this burst liquid phase enters pre-domethanizing column 4 and separates; Knockout drum 1 isolated gas phase further enters component distributor 3 (selecting scrubbing tower herein) after the cooling through cooler 2 from the bottom. The hydrocarbon liquid of in device 3, introducing one carbon containing two and light component from the top charging gas phase is washed and, thereby all carbon three and a large amount of carbon two and one washings of part carbon are arrived tower reactor, preferred method is that the gas phase of separating device 3 is cooled off, and utilizes its condensate liquid (tank 6 bottoms) as wash liquid. The still liquid of device 3 is sent into the upper strata column plate of pre-domethanizing column 4, and the cleaning solution temperature can be according to raw material and cryogen grade optimizing generally at-41～-80 ℃. The top gaseous phase of component distributor 3 is through further cooling off (such as cooler 7, plate-fin heat exchanger 20 and cooler 10) and obtaining two bursts of liquid phases at tank 9 and 11 interior flash distillations, and these two bursts of liquid phases enter the diverse location of domethanizing column 13 successively. In the rational situation of the temperature of tank 6, also can cancel heat exchanger 7 and flash tank 9. Enter flash tank 8 from tank 11 gas phase out after the 21 interior coolings of cold box plate fin heat exchanger, the liquid phase of tank 8 enters the top of domethanizing column 13, and gas phase enters the hydrogen gas system (being comprised of plate-fin heat exchanger 23 and tank 16) in downstream. The effect of pre-domethanizing column 4 is for the top gaseous phase of carbon containing three not with do not contain the still liquid of methane with the feed separation of tank 1 and tower 3, they send into respectively the dethanizer 24 in domethanizing column 13 and downstream (such as Fig. 3, shown in 4), pre-domethanizing column can provide backflow by overhead condenser, also can draw one liquid phase as backflow from domethanizing column 13. Demethanation top gaseous phase temperature behind decompressor 15 reduces, and goes out device after system's ( heat exchanger 21,20,19) reclaims cold. Because all chargings of domethanizing column 13 are carbon containing three not all, so its tower reactor product only has carbon two. For the Front-end depropanization and front-end hydrogenation of ethylene unit, this strand material can directly enter ethylene column 27 (as shown in Figure 3). For the sequence flow of ethylene unit, this strand material can enter the upper strata column plate (as shown in Figure 4) of ethylene column behind reactor 26 carbon two hydrogenation.
In order further to reduce the load of domethanizing column 13 and the ethylene loss that minimizing enters hydrogen gas system, the present invention has also set up carbon two scrubbing towers 12, referring to Fig. 2. Material from ice chest heat exchanger 21 enters carbon two scrubbing towers 12 by the bottom, liquid (preferred method is to carry out partial condensation by the material to tower 12 tops to provide cleaning solution) by one carbon containing one and a small amount of hydrogen washs gas phase in the tower, and the gas phase after the washing enters the hydrogen gas system in downstream. Scrubbing tower can reach following effect: the temperature (about 110 ℃) that 1. enters tower 12 enters the temperature of tank 8 (generally being lower than-128 ℃) height, so the light component of condensation reduces, has reduced the liquid measure that enters tower 13; Increase although 2. enter the flow of hydrogen gas system, the content decrease of ethene, ethylene loss reduces; 3. carbon two scrubbing towers 12 is simple in structure, can adopt plate column and packed tower, because this tower is not high, so tank 14 can place the top of tower 12, can economize like this one. Certainly, also the washing liquid pump can be set.
The effect that method of the present invention has following advantage and is achieved as follows:
1. reduction energy consumption
The present invention has reduced energy consumption from four aspects: 1. because component separating device 3 can make very most carbon two and a small amount of carbon one enter pre-domethanizing column in company with still liquid during removing charging in the carbon three, thereby reduced the load of ice chest and the load of cryogenic coolant; 2. the lighter hydrocarbons condensate liquid after the precooling enters pre-domethanizing column from tank 1, and the carbon two and the methane that wherein contain do not enter ice chest, have reduced the load of ice chest yet. By knockout drum 1 and component separating device 3, the ratio that C3, C2 and C1 remove in the charging is respectively 100%, 55～89% and 10～27%; 3. the methane of 15 pairs of demethanation cats head of decompressor carries out swell refrigeration and can be ice chest heat exchanger 22,21 enough colds are provided, and does not provide cold so do not need to extract the liquid phase methane out from domethanizing column 13 for ice chest, has reduced the refrigeration duty of domethanizing column 13 condensers. 4. carbon two scrubbing towers 12 have also reduced the load of domethanizing column 13 when improving Recovery rate of ethylene. Calculating shows that the comparable CN1048713C of the present invention reduces by about 10% ethene cryogen consumption.
2. Recovery rate of ethylene is high
General separation method must be extracted one liquid phase out from domethanizing column and provide cold for ice chest, and the content of ethene is higher in this burst liquid phase, and in 0.6～0.95mol% scope, separation method of the present invention need not extracted this burst liquid phase out usually.
In addition, the ethene that carbon two scrubbing towers 12 will enter in the material of Hydrogen Separation system washs tower reactor, makes substantially not contain ethene in hydrogen and the tail gas. In general flow process, enter the ethene that contains 0.15～0.23mol% in the material of Hydrogen Separation system, and adopt carbon two scrubbing towers 12 can make the content of ethene in this strand material be lower than 0.1mol%.
Therefore, cryogenic system Recovery rate of ethylene of the present invention can be up to 99.5%.
3. to the improvement of down-stream system
The present invention also has suitable improvement to technique and the energy consumption in downstream simultaneously except the energy consumption that reduces ice chest and demethanation part. Because the component distributor is divided into two parts with the carbon two in the charging, the part that wherein enters domethanizing column does not have the restructuring of carbon more than three to divide, so the material of demethanation tower reactor can not enter dethanizer. The charging of dethanizer is only from pre-demethanation tower reactor, and the dethanizer of old process need to be processed whole carbon two, so the present invention makes the dethanizer load reduction. Secondly, the charging of ethylene column becomes two bursts of different chargings of concentration by the sub-thread of routine, and conventional ethylene column is only from one charging of deethanization cat head, adopt method of the present invention after, the charging of ethylene column is respectively from domethanizing column and dethanizer, so also reduced the energy consumption of ethylene column.
Method of the present invention can be used for sequence flow and the predepropanization process of light hydrocarbon mixture cryogenic separation.
Fig. 3 is the situation that the present invention is used for ethylene unit predepropanization front-end hydrogenation separation process. Cracking gas is after over-quenching, compression, alkali cleaning and dry precooling, under 1.1MPa～1.5MPa pressure, carry out predepropanization (tower 1d), the lighter hydrocarbons on depropanizing tower 1d top only contain hydrogen, methane, carbon two, carbon three and other trace impurity, pressure rose to 3.6MPa～3.8MPa after process compressor 1a compressed again, and then carried out front-end hydrogenation and cooler 1c precooling in reactor 1g. Temperature after the precooling can arrive below-15 ℃, and gas-liquid separation in depropanizing tower return tank 1. The liquid phase part of tank 1 is returned depropanizing tower 1d as backflow, and all the other then enter pre-domethanizing column 4; The gas phase of tank 1 is further by entering component distributor 3 after cooler 2 coolings. Then separate by flow process of the present invention. For predepropanization process, because the tower reactor of domethanizing column 13 and the cat head carbon two of dethanizer 24 all do not contain alkynes, can directly enter ethylene column 27, tower 27 is produced product ethene and ethane. Tower 27 can adopt the low pressure heat pump techniques, and when domethanizing column 13 was high-pressure tower, the condenser that can be cooler 5 and pre-domethanizing column 4 after the decompression of carbon two components of tower reactor provided cold, so can reduce the ethene cryogen of a potential temperature.
Fig. 4 is the situation that the present invention is used for ethylene unit order separation process. After cracking gas boosts through compressor 1a, by drier 1b dehydration and cooler 1c cooling, enter afterwards knockout drum 1. Below separate by method of the present invention, but because all contain acetylene in the cat head carbon two of the still liquid of domethanizing column 13 of order separation process and dethanizer 24, so must be through just sending into ethylene column 27 behind two acetylene removal reactors 25,26.
Further specify characteristics of the present invention below by embodiment, but the present invention is not subjected to the restriction of these embodiment.
Embodiment one
For 800,000 tons of/year ethylene units, employing predepropanization front-end hydrogenation flow process does not add the method (option A) of carbon two scrubbing towers to the present invention under identical design basis and the method (option b) of CN1023685C+ decompressor is carried out flowsheeting, the results are shown in Table one
Table one
| Option A | Option b | ?B-A | |
| Remove the material (kgmol/h) of ice chest | ?5645 | ?7163 | ?1518 |
| Remove carbon two/feed carbon two (%) | ?61 | ?40 | ?-21 |
| -62 ℃ of ethene cryogens (MMkcal/hr) | ?2.689 | ?5.0543 | ?2.3653 |
| -76 ℃ of ethene cryogens (MMkcal/hr) | ?3.8564 | ?5.6944 | ?1.838 |
| -101 ℃ of ethene cryogens (MMkcal/hr) | ?3.1544 | ?3.9714 | ?0.817 |
As can be seen, because the present invention adopts the component distributor and is used pre-domethanizing column, the inventory that enters ice chest reduces significantly, and the cryogen load of each temperature grade that ice chest and carbon one system are consumed is also few, so flow process of the present invention compared with the prior art is energy-conservation.
Embodiment two
For 800,000 tons of/year ethylene units, adopt sequence flow under identical design basis: the present invention not to be added the method (option A) of carbon two scrubbing towers and the method (option b) of CN 1023685C+ decompressor is carried out flowsheeting, the results are shown in Table two
Table two
| Option A | Option b | ?B-A | |
| Remove the material (kgmol/h) of ice chest | ?5745 | ?7640 | ?1895 |
| Remove carbon two/feed carbon two (%) | ?62 | ?31 | ?-31 |
| -62 ℃ of ethene cryogens (MMkcal/hr) | ?2.7513 | ?5.7217 | ?2.9704 |
| -76 ℃ of ethene cryogens (MMkcal/hr) | ?3.6802 | ?7.4043 | ?3.7241 |
| -101 ℃ of ethene cryogens (MMkcal/hr) | ?3.2513 | ?3.7181 | ?0.4668 |
As can be seen, because the present invention adopts the component distributor and is used pre-domethanizing column, the inventory that enters ice chest reduces significantly, and the cryogen load of each temperature grade that ice chest and carbon one system are consumed is also few, so flow process of the present invention compared with the prior art is energy-conservation.
Embodiment three
For 800,000 tons of/year ethylene units, adopt predepropanization front-end hydrogenation flow process under identical design basis, the method (option b) of method of the present invention (option A) and CN1048713C+ decompressor is carried out flowsheeting.The temperature grade of ethene cryogen is decided to be respectively and is-62 ℃ ,-76 ℃ ,-101 ℃.Deep cooling part result of calculation sees Table three.Clearly, flow process energy consumption of the present invention compared with the prior art is low.
Table three
| Option A | Option b | ?B-A | |
| Remove the material (kgmol/h) of ice chest | 5645 | ?7161 | ?1516 |
| Remove carbon two/feed carbon two (%) | 61 | ?40 | ?-21 |
| -62 ℃ of ethene cryogens (MMkcal/hr) | 2.689 | ?5.0543 | ?2.3653 |
| -76 ℃ of ethene cryogens (MMkcal/hr) | 3.8564 | ?6.4755 | ?2.6191 |
| -101 ℃ of ethene cryogens (MMkcal/hr) | 2.8705 | ?3.2251 | ?0.3546 |
For 800,000 tons of/year ethylene units, cracking stock is a naphtha in addition, adopts the predepropanization front-end hydrogenation flow process of Fig. 3, and the material balance that flowsheeting calculates sees Table four, and the total losses amount of ethene has only 4.84kgmol/h, and the ethylene recovery rate reaches 99.8%:
Table four
Embodiment four
| Thing stream number flow, the KG-MOL/HR temperature, ℃ pressure, KPA kgmol/h H 2CO CH 4C 2H 2C 2H 4C 2H 6MAPD C 3H 6C 3H 8C4’S | ?100????????110????????120???????130???????140????????150????????160??????170???????180???????190?????200 ?8967.6?????799.3??????5645.2????3322.4????971.2??????2657.8?????1908.0???2050.7????3150.5????485.2???2275.6 ?-17.24?????17.24??????-54???????-37.7?????-44????????-123???????-98.9????-10.6?????13.35?????-113.9??-17.4 ?3544.00????3544???????3487??????3520??????3450???????3261???????3000?????3080??????3490??????3274????2489 ?1640.3?????8.3????????1597.8????42.47?????50.8???????1538.9?????109.7????????????????????????12.26 ?9.8????????0.1????????9.0???????0.642?????0.75???????7.4????????2.36?????????????????????????0.44 ?2827???????76.6???????2361.3????466.2?????542.4??????1109.5?????1793.1???1.23??????0.315?????343.9 ?3291???????346.1??????1495.4????1796.0????334.5??????1.98???????2.86?????1825.0????1807.7????122.83??1807.7 ?598????????90.4???????180.7?????417.4?????42.3???????????????????????????223.0?????465.4?????5.75????465.35 ?5.2????????3.8??????????????????5.2????????????????????????????????????????????????8.96 ?578.5??????262.5??????0.8???????577.6?????0.483??????????????????????????1.35??????839.6?????????????2.26 ?14.4???????7.6??????????????????14.3?????????????????????????????????????0.007?????21.9 ?2.55???????4.0??????????????????2.55???????????????????????????????????????????????6.52 |
For 800,000 tons of/year ethylene units, employing order separation process is with identical design basis, the method (option b) that adopts method of the present invention (option A) and CN1048713C+ decompressor is carried out flowsheeting, and the temperature grade of ethene cryogen is decided to be respectively and is-62 ℃ ,-76 ℃ ,-101 ℃.Result of calculation sees Table five.As can be seen, because the present invention adopts the component distributor and is used pre-domethanizing column, the inventory that enters ice chest reduces significantly, and the cryogen load of each temperature grade that ice chest and carbon one system are consumed is also few, so flow process of the present invention compared with the prior art is energy-conservation.
Table five
| Option A | Option b | ?B-A | |
| Remove the material (kgmol/h) of ice chest | ?5745 | ?7640 | ?1895 |
| Remove carbon two/feed carbon two (%) | ?62 | ?31 | -31 |
| -62 ℃ of ethene cryogens (MMkcal/hr) | ?2.7513 | ?5.7217 | ?2.9704 |
| -76 ℃ of ethene cryogens (MMkcal/hr) | ?3.6802 | ?6.4757 | ?2.7955 |
| -101 ℃ of ethene cryogens (MMkcal/hr) | ?3.0804 | ?3.3615 | ?0.2811 |
Claims (9)
1. deep cooling separating method that contains the light hydrocarbon mixture of hydrogen, methane, carbon two, carbon three and the carbon fourth class, this method comprises:
After light hydrocarbon feedstocks gas enters knockout drum and carries out gas-liquid separation, the component distributor is set in the downstream of gaseous phase outlet and pre-domethanizing column is set in the downstream of the liquid phase outlet of the liquid phase outlet of knockout drum and component distributor;
Light hydrocarbon feedstocks gas through overcompression, drying and precooling enters knockout drum;
After further cooling off, the gas phase that knockout drum separates sends into the bottom of component separator, in this device, change whole carbon three and most of carbon two and a small amount of methane over to the component separation unit bottoms through washing and cooling, bottom liquid phases enters the top of pre-domethanizing column, component separator top gas phase is carbon containing three not, separate to obtain the multiply liquid phase through the cooling of a series of coolers with flash tank, enter the middle and upper part diverse location of domethanizing column respectively successively;
Through the liquid phase that knockout drum separates, pre-domethanizing column is sent in carbon containing two, carbon three and more heavy ends and methane on a small quantity;
The liquid phase that pre-domethanizing column separates knockout drum and the bottom liquid phases of component distributor are separated into the tower overhead gas of carbon containing three not and do not contain the tower bottoms of methane, and tower bottoms is sent into the domethanizing column bottom;
Domethanizing column is separated into tower overhead gas methane and tower bottoms carbon two with the multiply charging.
2. also comprise according to the process of claim 1 wherein:
In the end one-level flash tank downstream is provided with carbon two scrubbing towers,
The liquid that flash tank separates enters the bottom of carbon two scrubbing towers after the cooler cooling, introduce one liquid that contains methane and small quantity of hydrogen from the top of tower gas in the tower is washed, and carbon two is washed in the tower bottoms, and tower bottoms is sent into the topmost of domethanizing column; Tower overhead gas enters downstream hydrogen/methane separation system.
3. according to the method for claim 2, the partial condensation liquid that wherein adopts carbon two scrubbing tower tower overhead gases is as cleaning solution.
4. according to the method for claim 1 or 2, wherein the component distributor comprises scrubbing tower, fractionating column, fractional condensation separator or segregation fractionating column.
5. according to the method for claim 4, the partial condensation liquid that wherein adopts the scrubbing tower tower overhead gas is as cleaning solution.
6. according to the method for claim 1 or 2, what wherein carbon two accounted for charging in the liquid phase of component distributor bottom accounts for charging more than 10% with methane 50% or more.
7. according to the method for claim 1 or 2, wherein also comprise:
Tower overhead gas outlet downstream at domethanizing column is provided with decompressor, tower overhead gas methane is carried out swell refrigeration, for cooling system provides cold.
8. according to the method for claim 1 or 2, be used for the sequence flow of light hydrocarbon mixture cryogenic separation.
9. according to the method for claim 1 or 2, be used for the predepropanization process of light hydrocarbon mixture cryogenic separation.
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Address after: 100029, No. six, Xin Xin Street East, Beijing, Chaoyang District Patentee after: Sinopec Corp. Patentee after: Sinopec Engineering Incorporation Address before: 100029, No. six, Xin Xin Street East, Beijing, Chaoyang District Patentee before: Sinopec Corp. Patentee before: Engrg Construction Co., SINOPEC |
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