CN117928175A - Cryogenic separation system and method thereof - Google Patents
Cryogenic separation system and method thereof Download PDFInfo
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- CN117928175A CN117928175A CN202211312479.3A CN202211312479A CN117928175A CN 117928175 A CN117928175 A CN 117928175A CN 202211312479 A CN202211312479 A CN 202211312479A CN 117928175 A CN117928175 A CN 117928175A
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- Prior art keywords
- demethanizer
- methane
- feed
- separation tank
- discharge port
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- 238000000926 separation method Methods 0.000 title claims abstract description 150
- 238000000034 method Methods 0.000 title abstract description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 190
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 118
- 239000001257 hydrogen Substances 0.000 claims abstract description 118
- 238000005406 washing Methods 0.000 claims abstract description 53
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 41
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 33
- 239000005977 Ethylene Substances 0.000 claims abstract description 33
- 238000007323 disproportionation reaction Methods 0.000 claims abstract description 23
- 239000003507 refrigerant Substances 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 64
- 239000012071 phase Substances 0.000 claims description 57
- 239000007791 liquid phase Substances 0.000 claims description 45
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 31
- 238000010992 reflux Methods 0.000 claims description 27
- 238000000197 pyrolysis Methods 0.000 claims description 15
- 238000001816 cooling Methods 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 230000008016 vaporization Effects 0.000 claims description 3
- -1 methane hydrogen Chemical class 0.000 claims 6
- 230000008878 coupling Effects 0.000 abstract description 3
- 238000010168 coupling process Methods 0.000 abstract description 3
- 238000005859 coupling reaction Methods 0.000 abstract description 3
- 238000005457 optimization Methods 0.000 abstract description 3
- 239000002994 raw material Substances 0.000 description 5
- 239000000047 product Substances 0.000 description 4
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 3
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 3
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
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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
-
- 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
- F25J3/0228—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
-
- 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
- F25J2200/70—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
- F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
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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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
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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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) 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
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention relates to a cryogenic separation system and a method thereof; there is provided a cryogenic separation system comprising: a feed cooler, an ethylene column intermediate reboiler, a pre-demethanizer reboiler, a first cooler, a demethanizer reboiler, a second cooler, a disproportionation heat exchanger, a scrubber condenser, a first feed separator tank, a demethanizer, a pre-demethanizer, and a scrubber; wherein, the feed cooler, the ethylene tower intermediate reboiler, the pre-demethanizer reboiler, the first cooler, the demethanizer reboiler, the second cooler and the first feed separation tank are connected in sequence through pipelines; the first feeding separation tank is connected with a disproportionation heat exchanger pipeline, and the disproportionation heat exchanger is respectively connected with a demethanizer and a pre-demethanizer pipeline; according to the invention, by adopting feed pre-separation and combining low-temperature washing and heat exchange network coupling optimization, ethylene loss in methane and hydrogen is reduced, low-temperature refrigerant consumption is saved, and economic benefit is improved.
Description
Technical Field
The invention relates to the technical field of ethylene separation, in particular to a cryogenic separation system and a cryogenic separation method.
Background
Ethylene and propylene are important petrochemical basic raw materials, an ethylene steam thermal cracking device is a main source for producing ethylene and propylene, and a series of chemical raw materials such as methane, hydrogen, mixed carbon four, pyrolysis gasoline and the like are also byproducts; thus, ethylene units are often the most upstream, most critical units in chemical plants; the main technical routes of the prior ethylene device comprise front depropanization, front deethanization, sequential separation and the like, and no matter which technical route is, methane hydrogen and hydrogen-rich gas in pyrolysis gas are separated from carbon two and more heavy components through cryogenic separation so as to produce polymerization-grade ethylene and propylene products subsequently, and methane hydrogen and hydrogen-rich gas products are obtained simultaneously; the energy consumption of a cold area of a traditional ethylene device is large, the system flow is long, the heat exchange network is complex, a certain amount of ethylene is inevitably entrained in methane and hydrogen which are separated products in the process, the ethylene is mainly the ethylene entrained by top gas of a demethanizer and top gas of a cryogenic separation tank, the ethylene can cause ethylene loss of the device products, and the ethylene is considerable in daily accumulation and moon.
Therefore, there is a need for a cryogenic separation system that is more energy efficient and reduces ethylene losses.
Disclosure of Invention
The invention aims at overcoming the defects in the prior art and provides a cryogenic separation system and a cryogenic separation method.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
A first aspect of the present invention provides a cryogenic separation system comprising: a feed cooler, an ethylene column intermediate reboiler, a pre-demethanizer reboiler, a first cooler, a demethanizer reboiler, a second cooler, a disproportionation heat exchanger, a scrubber condenser, a first feed separator tank, a demethanizer, a pre-demethanizer, and a scrubber;
Wherein the feed cooler, the ethylene column intermediate reboiler, the pre-demethanizer reboiler, the first cooler, the demethanizer reboiler, the second cooler, and the first feed separation tank are connected in sequence by pipeline; the first feeding separation tank is connected with a disproportionation heat exchanger pipeline, and the disproportionation heat exchanger is respectively connected with the demethanizer and the pre-demethanizer pipeline; the first feeding separation tank is connected with a washing tower pipeline; the washing tower is connected with the condenser of the washing tower and the pipeline of the demethanizer respectively.
Preferably, the feed inlet of the feed cooler is connected with the discharge outlet pipeline of the pyrolysis gas treatment section.
Preferably, the first discharge port of the first feed separation tank is connected with the first feed port of the disproportionation heat exchanger, and the second discharge port of the first feed separation tank is connected with the first feed port of the washing tower;
The first discharge port of the disproportionation heat exchanger is connected with the first feed port of the demethanizer, and the second discharge port of the disproportionation heat exchanger is connected with the first feed port of the pre-demethanizer;
The first discharge port of the washing tower is connected with the second feed port of the demethanizer, and the second discharge port of the washing tower is connected with the first feed port of the condenser of the washing tower;
the first discharge port of the washing tower condenser is connected with the second feed port of the washing tower, and the second discharge port of the washing tower condenser is connected with the feed port of the second feed separation tank;
The first discharge port of the second feed separation tank is connected with the third feed port of the demethanizer, and the second discharge port of the second feed separation tank is connected with the feed port of the first methane-hydrogen separation tank;
the first discharge port of the first methane-hydrogen separation tank is connected with the feed port of the high-pressure methane-hydrogen treatment working section, and the second discharge port of the first methane-hydrogen separation tank is connected with the feed port of the second methane-hydrogen separation tank;
The first discharge port of the second methane-hydrogen separation tank is connected with the feed port of the low-pressure methane-hydrogen treatment working section, and the second discharge port of the second methane-hydrogen separation tank is connected with the feed port of the hydrogen-rich treatment working section;
the first discharge port of the pre-demethanizer is connected with the feed port of the first deethanizer feed section, and the second discharge port of the pre-demethanizer is connected with the fourth feed port of the demethanizer;
the first discharge port of the demethanizer is connected with the feed port of the feed section of the second deethanizer, and the second discharge port of the demethanizer is respectively connected with the feed port of the high-pressure methane hydrogen treatment section and the first feed port of the methane machine inlet-outlet heat exchanger;
The first discharge port of the methane machine inlet-outlet heat exchanger is connected with the first feed port of the methane machine, the first discharge port of the methane machine is connected with the second feed port of the methane machine inlet-outlet heat exchanger, and the second discharge port of the methane machine inlet-outlet heat exchanger is connected with the feed port of the reflux tank;
The first discharge port of the reflux tank is respectively connected with the feed port of the high-pressure methane hydrogen treatment working section and the fifth feed port of the demethanizer; the second discharge port of the reflux tank is connected with the feed port of the high-pressure methane hydrogen treatment working section;
the connection is pipeline connection.
More preferably, a pre-demethanizer bottom pump and a cold box are connected between the first discharge port of the pre-demethanizer and the feed port of the first deethanizer feed section in sequence through pipelines; and a pipeline between a first discharge port of the pre-demethanizer and a second feed port of the pre-demethanizer is connected with a reboiler of the pre-demethanizer.
More preferably, the first discharge port of the demethanizer is connected with the feed port of the second deethanizer feed section through a pipeline in sequence, and the demethanizer bottom pump, the cold box and the feed cooler are connected with each other through pipelines in sequence; and a pipeline between the first discharge port of the demethanizer and the sixth feed port of the demethanizer is connected with the demethanizer reboiler.
More preferably, a methane machine interstage cooler is connected between the first discharge port of the methane machine and the second feed port of the methane machine through a pipeline; and a methane machine outlet cooler and a methane machine inlet-outlet heat exchanger are sequentially connected between the second discharge port of the methane machine and the feed port of the reflux tank through pipelines.
Preferably, the discharge port of the liquid-phase circulating ethane treatment section is connected with a first feed port pipeline of the first cooler, and the first discharge port of the first cooler is connected with the feed port pipeline of the gas-phase circulating ethane treatment section.
More preferably, the cold box is connected between the first discharge port of the first cooler and the feed port of the gas-phase circulating ethane treatment section through a pipeline.
Preferably, the cold box is connected between the second discharge port of the first feed separation tank and the first feed port of the washing tower, between the second discharge port of the washing tower condenser and the feed port of the second feed separation tank, between the second discharge port of the second feed separation tank and the feed port of the first methane-hydrogen separation tank, between the first discharge port of the first methane-hydrogen separation tank and the feed port of the high-pressure methane-hydrogen treatment section, between the second discharge port of the first methane-hydrogen separation tank and the feed port of the second methane-hydrogen separation tank, between the first discharge port of the second methane-hydrogen separation tank and the feed port of the low-pressure methane-hydrogen treatment section, and between the second discharge port of the second methane-hydrogen separation tank and the feed port of the hydrogen-rich treatment section through pipelines.
The second aspect of the present invention provides a cryogenic separation method, using the above-mentioned cryogenic separation system, comprising the steps of:
step one, pyrolysis gas is input into the first feed separation tank from a discharge port of the pyrolysis gas treatment working section through the feed cooler, the ethylene tower intermediate reboiler, the pre-demethanizer reboiler, the first cooler, the demethanizer reboiler and the second cooler;
Step two, cooling the gas phase in the first feeding separation tank through the cold box, and then entering the washing tower, wherein the liquid phase in the first separation tank enters the demethanizer and the pre-demethanizer respectively after passing through the disproportionation heat exchanger;
step three, enabling gas phase in the washing tower to enter a condenser of the washing tower for condensation, and enabling liquid phase in the washing tower to enter a demethanizer; the gas phase in the washing tower condenser enters the second feeding separation tank after being condensed by the cold box, and the liquid phase in the washing tower condenser returns to the washing tower;
Step four, enabling a gas phase at the top end of the second feeding separation tank to enter the first methane-hydrogen separation tank after passing through the cold box, and enabling a liquid phase at the bottom end of the second feeding separation tank to enter the demethanizer;
step five, enabling a gas phase at the top end of the first methane-hydrogen separation tank to enter the second methane-hydrogen separation tank after passing through the cold box, enabling a liquid phase at the bottom end of the first methane-hydrogen separation tank to enter the high-pressure methane-hydrogen treatment working section after being vaporized into a gas phase through heat exchange of the cold box;
Step six, the hydrogen-rich gas at the top end of the second methane-hydrogen separation tank enters the hydrogen-rich gas treatment working section, and the liquid phase at the bottom end of the second methane-hydrogen separation tank is vaporized into a gas phase through heat exchange of the cold box and then enters the low-pressure methane-hydrogen treatment working section;
Step seven, pumping out a liquid phase part at the bottom end of the pre-demethanizer by a bottom pump of the pre-demethanizer, exchanging heat by the cold box, and then sending the liquid phase part into a feeding section of the first deethanizer; reboiling part of the hydrocarbon oil through the pre-demethanizer reboiler; the gas phase at the top end of the pre-demethanizer enters the demethanizer;
Step eight, pumping out a liquid phase part at the bottom end of the demethanizer by a bottom pump of the demethanizer, exchanging heat by the cold box, and then entering the feed cooler and sending into a feed working section of the second deethanizer; part of the water is reboiled through the demethanizer reboiler; the gas phase part at the top end of the demethanizer directly enters the high-pressure methane hydrogen treatment working section through the cold box, and part of the gas phase part enters the methane machine inlet-outlet heat exchanger, returns to the methane machine inlet-outlet heat exchanger after passing through the methane machine, the methane machine interstage cooler, the methane machine and the methane machine outlet cooler, and is then sent into the reflux tank; the gas phase at the top end of the reflux tank is converged with the gas phase at the top end of the demethanizer, the gas phase enters the high-pressure methane hydrogen treatment working section after passing through the cold box, the liquid phase at the bottom end of the reflux tank returns to the demethanizer, and the liquid phase at the bottom end of the reflux tank is converged with the gas phase at the top end of the demethanizer, and enters the high-pressure methane hydrogen treatment working section after passing through the cold box;
and step nine, outputting the liquid-phase ethane from the liquid-phase circulating ethane treatment working section, and vaporizing the liquid-phase ethane into gas-phase ethane after heat exchange by the first cooler and the cold box and outputting the gas-phase ethane to the gas-phase circulating ethane treatment working section.
Compared with the prior art, the invention has the following technical effects:
According to the invention, by adopting the combination of feed pre-separation, reflux washing and heat exchange network coupling optimization, the ethylene loss entrained in methane and hydrogen is reduced, the consumption of low-temperature refrigerant is saved, and the economic benefit is improved.
Drawings
FIG. 1 is a flow chart of the cryogenic separation system of the present invention;
Reference numerals in the drawings include:
A feed cooler E1; a cold box E2; an ethylene tower intermediate reboiler E5; a pre-demethanizer reboiler E6; a first cooler E7; a demethanizer reboiler E9; a second cooler E10; a disproportionation heat exchanger E12; a scrubber condenser E13; a methane machine inlet-outlet heat exchanger E14; a methane machine outlet cooler E16; methane interstage cooler E17; a first feed separator tank D1; a reflux drum D2; a second feed separation tank D3; a first methane-hydrogen separation tank D4; a second methane-hydrogen separation tank D5; a demethanizer T1; a pre-demethanizer T2; a washing tower T3; methane machine C1; a demethanizer bottom pump P1; a pre-demethanizer bottom pump P2; a low pressure methane hydro-treatment section S1; a high pressure methane hydro-treatment section S2; a hydrogen-rich gas treatment section S3; a gas-phase recycle ethane treatment section S4; a first deethanizer feed section S5; a second deethanizer feed section S6; a pyrolysis gas treatment section S7; and a liquid-phase circulating ethane treatment section S8.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
It should be noted that, without conflict, the embodiments of the present invention and features of the embodiments may be combined with each other.
The invention is further described below with reference to the drawings and specific examples, which are not intended to be limiting.
Example 1
The present embodiment provides a cryogenic separation system comprising: a feed cooler E1, a cold box E2, an ethylene column intermediate reboiler E5, a pre-demethanizer reboiler E6, a first cooler E7, a demethanizer reboiler E9, a second cooler E10, a disproportionation heat exchanger E12, a scrubber condenser E13, a methane machine inlet-outlet heat exchanger E14, a methane machine outlet cooler E16, a methane machine inter-stage cooler E17, a first feed separation tank D1, a reflux drum D2, a second feed separation tank D3, a first methane-hydrogen separation tank D4, a second methane-hydrogen separation tank D5, a demethanizer T1, a pre-demethanizer T2, a scrubber T3, a methane machine C1, a demethanizer bottom pump P1, a pre-demethanizer bottom pump P2, a low pressure methane-hydrogen treatment section S1, a high pressure methane-hydrogen treatment section S2, a hydrogen-rich treatment section S3, a gas-phase circulation ethane treatment section S4, a first deethanizer feed section S5, a second deethanizer feed S6, a pyrolysis treatment section S7, and a liquid-phase circulation ethane section S8;
Wherein the discharge port of the pyrolysis gas treatment section S7 is connected with the feed port of the first feed separation tank D1; and a feed cooling box E1, an ethylene tower intermediate reboiler E5, a pre-demethanizer reboiler E6, a first cooler E7, a demethanizer reboiler E9 and a second cooler E10 are sequentially connected between a discharge port of the pyrolysis gas treatment section S7 and a feed port of the first feed separation tank D1.
The first discharge port of the first feed separation tank D1 is connected with the first feed port of the disproportionation heat exchanger E12, and the second discharge port of the first feed separation tank D1 is connected with the first feed port of the washing tower T3;
the first discharge port of the disproportionation heat exchanger E12 is connected with the first feed port of the pre-demethanizer T2, and the second discharge port of the disproportionation heat exchanger E12 is connected with the first feed port of the demethanizer T1;
the first discharge port of the washing tower T3 is connected with the second feed port of the demethanizer T1; the second discharge port of the washing tower T3 is connected with the first feed port of the washing tower condenser E13;
the first discharge port of the washing tower condenser E13 is connected with the second feed port of the washing tower T3, and the second discharge port of the washing tower condenser E13 is connected with the feed port of the second feed separation tank D3;
the first discharge port of the second feed separation tank D3 is connected with the third feed port of the demethanizer T1, and the second discharge port of the second feed separation tank D3 is connected with the feed port of the first methane-hydrogen separation tank D4;
The first discharge port of the first methane-hydrogen separation tank D4 is connected with the feed port of the high-pressure methane-hydrogen treatment working section S2, and the second discharge port of the first methane-hydrogen separation tank D4 is connected with the feed port of the second methane-hydrogen separation tank D5;
the first discharge port of the second methane-hydrogen separation tank D5 is connected with the feed port of the low-pressure methane-hydrogen treatment working section S1, and the second discharge port of the second methane-hydrogen separation tank D5 is connected with the feed port of the hydrogen-rich treatment working section S3;
The first discharge port of the pre-demethanizer T2 is connected with the feed port of the first deethanizer feed section S5, and the pre-demethanizer bottom pump P2 and the cold box E2 are sequentially connected between the first discharge port of the pre-demethanizer T2 and the feed port of the first deethanizer feed section S5; the second discharge port of the pre-demethanizer T2 is connected with the fourth feed port of the demethanizer T1; the pre-demethanizer reboiler E6 is connected between the first discharge port of the pre-demethanizer T2 and the second feed port of the pre-demethanizer T2;
The first discharge port of the demethanizer T1 is connected with the feed port of the second deethanizer feed section S6, and the demethanizer bottom pump P1, the cold box E2 and the feed cooler E1 are sequentially connected between the first discharge port of the demethanizer T1 and the feed port of the second deethanizer feed section S6; the demethanizer reboiler E9 is connected between the first discharge port of the demethanizer T1 and the sixth feed port of the demethanizer T1; the second discharge port of the demethanizer T1 is respectively connected with the feed port of the high-pressure methane hydrogen treatment working section S2 and the first feed port of the methane machine inlet-outlet heat exchanger E14;
The first discharge port of the methane machine inlet-outlet heat exchanger E14 is connected with the first feed port of the methane machine C1, the first discharge port of the methane machine C1 is connected with the second feed port of the methane machine inlet-outlet heat exchanger E14, and the second discharge port of the methane machine inlet-outlet heat exchanger E14 is connected with the feed port of the reflux tank D2; the methane machine interstage cooler E17 is connected between the first discharge port of the methane machine C1 and the second feed port of the methane machine C1; the second discharge port of the methane machine C1 and the feed port of the reflux tank D2 are sequentially connected with the methane machine outlet cooler E16 and the methane machine inlet-outlet heat exchanger E14;
The first discharge port of the reflux tank D2 is respectively connected with the feed port of the high-pressure methane hydro-treatment working section S2 and the fifth feed port of the demethanizer T1; the second discharge port of the reflux tank D2 is connected with the feed port of the high-pressure methane hydrogen treatment working section S2;
The discharge port of the liquid-phase circulating ethane treatment working section S8 is connected with the first feed port of the first cooler E7, and the first discharge port of the first cooler E7 is connected with the feed port of the gas-phase circulating ethane treatment working section S4;
The cold box E2 is connected between the first discharge port of the first cooler E7 and the feed port of the gas-phase circulating ethane treatment section S4, between the second discharge port of the first feed separation tank D1 and the first feed port of the scrubber T3, between the second discharge port of the scrubber condenser E13 and the feed port of the second feed separation tank D3, between the second discharge port of the second feed separation tank D3 and the feed port of the first methane-hydrogen separation tank D4, between the first discharge port of the first methane-hydrogen separation tank D4 and the feed port of the high-pressure methane-hydrogen treatment section S2, between the second discharge port of the first methane-hydrogen separation tank D4 and the feed port of the second methane-hydrogen separation tank D5, between the first discharge port of the second methane-hydrogen separation tank D5 and the feed port of the low-pressure methane-hydrogen treatment section S1, and between the second discharge port of the second methane-hydrogen separation tank D5 and the hydrogen-rich section S3;
the connection is pipeline connection.
Example 2
The embodiment provides a cryogenic separation method, which adopts the cryogenic separation system described in the embodiment 1; the method comprises the following steps:
Step one, after passing through a feed cooler E1, an ethylene tower intermediate reboiler E5, a pre-demethanizer reboiler E6, a first cooler E7, a demethanizer reboiler E9 and a second cooler E10 from a discharge port of a pyrolysis gas treatment section S7, inputting the pyrolysis gas into a first feed separation tank D1;
Step two, cooling a gas phase in the first feeding separation tank D1 through a cold box E2, then entering a washing tower T3, and respectively entering a demethanizer T1 and a pre-demethanizer T2 after a liquid phase in the first separation tank D1 passes through a disproportionation heat exchanger E12;
Step three, enabling gas phase in the washing tower T3 to enter a washing tower condenser E13 for condensation, and enabling liquid phase in the washing tower T3 to enter a demethanizer T1; the gas phase in the washing tower condenser E13 enters a second feeding separation tank D3 after being condensed by a cold box E2, and the liquid phase in the washing tower condenser E13 returns to the washing tower T3;
Step four, enabling a gas phase at the top end of the second feeding separation tank D3 to enter a first methane-hydrogen separation tank D4 after passing through a cold box E2, and enabling a liquid phase at the bottom end of the second feeding separation tank D3 to enter a demethanizer T1;
Step five, enabling a gas phase at the top end of the first methane-hydrogen separation tank D4 to enter a second methane-hydrogen separation tank D5 after passing through a cold box E2, and enabling a liquid phase at the bottom end of the first methane-hydrogen separation tank D4 to enter a high-pressure methane-hydrogen treatment working section S2 after passing through the cold box E2;
step six, the hydrogen rich gas at the top end of the second methane-hydrogen separation tank D5 enters a hydrogen rich gas treatment section S3, and the low-pressure methane hydrogen at the bottom end of the second methane-hydrogen separation tank D5 enters a low-pressure methane-hydrogen treatment section S1;
Step seven, the liquid phase part at the bottom end of the pre-demethanizer T2 is pumped out by a pre-demethanizer bottom pump P2, and is sent to a first deethanizer feeding section S5 after heat exchange by a cold box E2; part of the water is reboiled through a pre-demethanizer reboiler E6; the gas phase at the top end of the pre-demethanizer T2 enters a demethanizer T1;
Step eight, pumping out a liquid phase part at the bottom end of the demethanizer T1 by a demethanizer bottom pump P1, exchanging heat by a cold box E2, and then entering a feed cooler E1 and feeding the liquid phase part into a second deethanizer feed section S6; part of the water is reboiled through a demethanizer reboiler E9; the gas phase part at the top end of the demethanizer T1 directly enters the high-pressure methane hydrogen treatment section S2 through the cold box E2, and part of the gas phase part enters the methane machine inlet-outlet heat exchanger E14, returns to the methane machine inlet-outlet heat exchanger E14 after passing through the methane machine C1, the methane machine interstage cooler E17, the methane machine C1 and the methane machine outlet cooler E16, and then enters the reflux tank D2; the gas phase at the top end of the reflux tank D2 is converged with the gas phase at the top end of the demethanizer T1, enters the high-pressure methane hydrogen treatment working section S2 after passing through the cold box E2, and the liquid phase at the bottom end of the reflux tank D2 returns to the demethanizer T1, and partially converged with the gas phase at the top end of the demethanizer T1, and enters the high-pressure methane hydrogen treatment working section S2 after passing through the cold box E2;
step nine, outputting the liquid-phase ethane from the liquid-phase circulating ethane treatment section S8, and vaporizing the liquid-phase ethane into gas-phase ethane after heat exchange by the first cooler E7 and the cold box E2, and outputting the gas-phase ethane to the gas-phase circulating ethane treatment section S4.
Application examples
The pyrolysis gas is treated by a conventional low-pressure demethanizer sequential separation system and the cryogenic separation system described in example 1;
1. Scheme one
The flow composition of the raw materials and the feeding conditions are shown in Table 1:
TABLE 1
| Project | Numerical value |
| Temperature (. Degree. C.) | 15.5 |
| Pressure (MPaG) | 3.6 |
| Flow rate (kg/hr) | 226800 |
| Composition of the composition | Mass fraction |
| C1- | 1.8％ |
| C1 | 20.5％ |
| C2 | 49.1％ |
| C3 | 20.0％ |
| C3+ | 8.6％ |
The specific parameters of the discharge, ethylene loss and cold consumption are shown in Table 2:
TABLE 2
2. Scheme II
The flow composition of the raw materials and the feeding conditions are shown in Table 3:
TABLE 3 Table 3
| Project | Numerical value |
| Temperature (. Degree. C.) | 15.5 |
| Pressure (MPaG) | 3.56 |
| Flow rate (kg/hr) | 283500 |
| Composition of the composition | Mass fraction |
| C1- | 1.9％ |
| C1 | 20.7％ |
| C2 | 49.4％ |
| C3 | 19.6％ |
| C3+ | 8.4％ |
The specific parameters of the discharge, ethylene loss and cold consumption are shown in Table 4:
TABLE 4 Table 4
3. Scheme III
The flow composition of the raw materials and the feeding conditions are shown in Table 5:
TABLE 5
The specific parameters of the discharge, ethylene loss and cold consumption are shown in Table 6:
TABLE 6
In summary, the invention reduces ethylene loss carried in methane and hydrogen by adopting the combination of feed pre-separation, reflux washing and heat exchange network coupling optimization, saves low-temperature refrigerant consumption and improves economic benefit.
The foregoing description is only illustrative of the preferred embodiments of the present invention and is not to be construed as limiting the scope of the invention, and it will be appreciated by those skilled in the art that equivalent substitutions and obvious variations may be made using the description and illustrations of the present invention, and are intended to be included within the scope of the present invention.
Claims (10)
1. A cryogenic separation system comprising: a feed cooler (E1), an ethylene column intermediate reboiler (E5), a pre-demethanizer reboiler (E6), a first cooler (E7), a demethanizer reboiler (E9), a second cooler (E10), a disproportionation heat exchanger (E12), a scrubber condenser (E13), a first feed separation tank (D1), a demethanizer (T1), a pre-demethanizer (T2), and a scrubber (T3);
Wherein the feed cooler (E1), the ethylene column intermediate reboiler (E5), the pre-demethanizer reboiler (E6), the first cooler (E7), the demethanizer reboiler (E9), the second cooler (E10) and the first feed separation tank (D1) are connected in sequence by pipeline; the first feeding separation tank (D1) is connected with the disproportionation heat exchanger (E12) through a pipeline, and the disproportionation heat exchanger (E12) is connected with the demethanizer (T1) and the pre-demethanizer (T2) through pipelines respectively; the first feeding separation tank (D1) is connected with the washing tower (T3) through a pipeline; the washing tower (T3) is respectively connected with the washing tower condenser (E13) and the demethanizer (T1) through pipelines.
2. Cryogenic separation system according to claim 1, characterized in that the feed inlet of the feed cooler (E1) is connected with the discharge outlet of the pyrolysis gas treatment section (S7) by piping.
3. Cryogenic separation system according to claim 1, characterized in that the first outlet of the first feed separation tank (D1) is connected with the first inlet of the disproportionation heat exchanger (E12), and the second outlet of the first feed separation tank (D1) is connected with the first inlet of the scrubber (T3);
The first discharge port of the disproportionation heat exchanger (E12) is connected with the first feed port of the demethanizer (T1), and the second discharge port of the disproportionation heat exchanger (E12) is connected with the first feed port of the pre-demethanizer (T2);
the first discharge port of the washing tower (T3) is connected with the second feed port of the demethanizer (T1), and the second discharge port of the washing tower (T3) is connected with the first feed port of the washing tower condenser (E13);
The first discharge port of the washing tower condenser (E13) is connected with the second feed port of the washing tower (T3), and the second discharge port of the washing tower condenser (E13) is connected with the feed port of the second feed separation tank (D3);
the first discharge port of the second feed separation tank (D3) is connected with the third feed port of the demethanizer (T1), and the second discharge port of the second feed separation tank (D3) is connected with the feed port of the first methane-hydrogen separation tank (D4);
the first discharge port of the first methane-hydrogen separation tank (D4) is connected with the feed port of the high-pressure methane-hydrogen treatment working section (S2), and the second discharge port of the first methane-hydrogen separation tank (D4) is connected with the feed port of the second methane-hydrogen separation tank (D5);
The first discharge port of the second methane-hydrogen separation tank (D5) is connected with the feed port of the low-pressure methane-hydrogen treatment working section (S1), and the second discharge port of the second methane-hydrogen separation tank (D5) is connected with the feed port of the hydrogen-rich treatment working section (S3);
The first discharge port of the pre-demethanizer (T2) is connected with the feed port of the first deethanizer feed section (S5), and the second discharge port of the pre-demethanizer (T2) is connected with the fourth feed port of the demethanizer (T1);
The first discharge port of the demethanizer (T1) is connected with the feed port of the second deethanizer feed section (S6), and the second discharge port of the demethanizer (T1) is respectively connected with the feed port of the high-pressure methane hydrogen treatment section (S2) and the first feed port of the methane machine inlet-outlet heat exchanger (E14);
The first discharge port of the methane machine inlet-outlet heat exchanger (E14) is connected with the first feed port of the methane machine (C1), the first discharge port of the methane machine (C1) is connected with the second feed port of the methane machine inlet-outlet heat exchanger (E14), and the second discharge port of the methane machine inlet-outlet heat exchanger (E14) is connected with the feed port of the reflux tank (D2);
The first discharge port of the reflux tank (D2) is respectively connected with the feed port of the high-pressure methane hydrogen treatment working section (S2) and the fifth feed port of the demethanizer (T1); the second discharge port of the reflux tank (D2) is connected with the feed port of the high-pressure methane hydrogen treatment working section (S2);
the connection is pipeline connection.
4. A cryogenic separation system according to claim 3, characterized in that a pre-demethanizer bottom pump (P2) and a cold box (E2) are connected in sequence in pipeline between the first outlet of the pre-demethanizer (T2) and the inlet of the first deethanizer feed section (S5); the pipeline connection between the first discharge port of the pre-demethanizer (T2) and the second feed port of the pre-demethanizer (T2) is provided with a pre-demethanizer reboiler (E6).
5. A cryogenic separation system according to claim 3, characterized in that the demethanizer bottom pump (P1), the cold box (E2) and the feed cooler (E1) are connected in series in line between the first outlet of the demethanizer (T1) and the inlet of the second deethanizer feed section (S6); and a pipeline between a first discharge port of the demethanizer (T1) and a sixth feed port of the demethanizer (T1) is connected with the demethanizer reboiler (E9).
6. A cryogenic separation system according to claim 3, characterized in that a methane machine inter-stage cooler (E17) is connected in line between the first discharge port of the methane machine (C1) and the second feed port of the methane machine (C1); and a methane machine outlet cooler (E16) and a methane machine inlet-outlet heat exchanger (E14) are sequentially connected between the second discharge port of the methane machine (C1) and the feed port of the reflux tank (D2) through pipelines.
7. Cryogenic separation system according to claim 1, characterized in that the discharge port of the liquid-phase circulating ethane treatment section (S8) is connected with a first feed port line of the first cooler (E7), the first discharge port of the first cooler (E7) being connected with a feed port line of the gas-phase circulating ethane treatment section (S4).
8. Cryogenic separation system according to claim 7, characterized in that the cold box (E2) is connected in line between the first outlet of the first cooler (E7) and the inlet of the gas-phase recycle ethane treatment section (S4).
9. A cryogenic separation system according to claim 3, characterized in that between the second discharge port of the first feed separation tank (D1) and the first feed port of the scrubber (T3), between the second discharge port of the scrubber condenser (E13) and the feed port of the second feed separation tank (D3), between the second discharge port of the second feed separation tank (D3) and the feed port of the first methane hydrogen separation tank (D4), between the first discharge port of the first methane hydrogen separation tank (D4) and the feed port of the high pressure methane hydrogen treatment section (S2), between the second discharge port of the first methane hydrogen separation tank (D4) and the feed port of the second methane hydrogen separation tank (D5), between the first discharge port of the second methane hydrogen separation tank (D5) and the feed port of the low pressure methane hydrogen treatment section (S1), and between the second methane hydrogen separation tank (D5) and the feed port of the cold tank (E2) are connected.
10. A cryogenic separation process employing a cryogenic separation system according to any one of claims 1-9, comprising the steps of:
step one, after passing through a discharge port of the pyrolysis gas treatment working section (S7) through the feed cooler (E1), the ethylene tower intermediate reboiler (E5), the pre-demethanizer reboiler (E6), the first cooler (E7), the demethanizer reboiler (E9) and the second cooler (E10), the pyrolysis gas is input into the first feed separation tank (D1);
Step two, cooling the gas phase in the first feeding separation tank (D1) through the cold box (E2) and then entering the washing tower (T3), and respectively entering the demethanizer (T1) and the pre-demethanizer (T2) after the liquid phase in the first separation tank (D1) passes through the disproportionation heat exchanger (E12);
Step three, enabling gas phase in the washing tower (T3) to enter a washing tower condenser (E13) for condensation, and enabling liquid phase in the washing tower (T3) to enter a demethanizer (T1); the gas phase in the washing tower condenser (E13) enters the second feeding separation tank (D3) after being condensed by the cold box (E2), and the liquid phase in the washing tower condenser (E13) returns to the washing tower (T3);
Step four, enabling a gas phase at the top end of the second feeding separation tank (D3) to enter the first methane-hydrogen separation tank (D4) after passing through the cold box (E2), and enabling a liquid phase at the bottom end of the second feeding separation tank (D3) to enter the demethanizer (T1);
Step five, enabling a gas phase at the top end of the first methane-hydrogen separation tank (D4) to enter the second methane-hydrogen separation tank (D5) after passing through the cold box (E2), enabling a liquid phase at the bottom end of the first methane-hydrogen separation tank (D4) to enter the high-pressure methane-hydrogen treatment working section (S2) after being vaporized into a gas phase through heat exchange of the cold box (E2);
step six, the hydrogen-rich gas at the top end of the second methane-hydrogen separation tank (D5) enters the hydrogen-rich gas treatment working section (S3), and the liquid phase at the bottom end of the second methane-hydrogen separation tank (D5) is vaporized into a gas phase through heat exchange of the cold box (E2) and then enters the low-pressure methane-hydrogen treatment working section (S1);
Step seven, a liquid phase part at the bottom end of the pre-demethanizer (T2) is pumped out by a pre-demethanizer bottom pump (P2), and is sent into the first deethanizer feeding working section (S5) after heat exchange by the cold box (E2); reboiling a portion through the pre-demethanizer reboiler (E6); the gas phase at the top end of the pre-demethanizer (T2) enters the demethanizer (T1);
Step eight, extracting a liquid phase part at the bottom end of the demethanizer (T1) by a demethanizer bottom pump (P1), exchanging heat by the cold box (E2), and then entering the feed cooler (E1) and delivering the liquid phase part into the second deethanizer feed section (S6); reboiling part of the refrigerant through the demethanizer reboiler (E9); the gas phase part at the top end of the demethanizer (T1) directly enters the high-pressure methane hydrogen treatment working section (S2) through the cold box (E2), and part of the gas phase part enters the methane machine inlet-outlet heat exchanger (E14), returns to the methane machine inlet-outlet heat exchanger (E14) after passing through the methane machine (C1), the methane machine interstage cooler (E17), the methane machine (C1) and the methane machine outlet cooler (E16), and is then sent to the reflux tank (D2); the gas phase at the top end of the reflux tank (D2) is converged with the gas phase at the top end of the demethanizer (T1), the gas phase enters the high-pressure methane hydrogen treatment working section (S2) after passing through the cold box (E2), the liquid phase at the bottom end of the reflux tank (D2) returns to the demethanizer (T1), and the liquid phase at the bottom end of the reflux tank (D2) is partially converged with the gas phase at the top end of the demethanizer (T1), and the gas phase enters the high-pressure methane hydrogen treatment working section (S2) after passing through the cold box (E2);
Step nine, outputting liquid-phase ethane from the liquid-phase circulating ethane treatment working section (S8), and vaporizing the liquid-phase ethane into gas-phase ethane after heat exchange through the first cooler (E7) and the cold box (E2) and outputting the gas-phase ethane to the gas-phase circulating ethane treatment working section (S4).
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