CN107144092A - A kind of device and its production technology that high-purity ethylene is produced with ethene heat pump distillation - Google Patents
A kind of device and its production technology that high-purity ethylene is produced with ethene heat pump distillation Download PDFInfo
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- CN107144092A CN107144092A CN201710417334.2A CN201710417334A CN107144092A CN 107144092 A CN107144092 A CN 107144092A CN 201710417334 A CN201710417334 A CN 201710417334A CN 107144092 A CN107144092 A CN 107144092A
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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
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
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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
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
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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
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main 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
- F25J2200/40—Features relating to the provision of boil-up in the bottom of a 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/72—Refluxing the column with at least a part of the totally 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
- F25J2200/74—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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
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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
- F25J2270/12—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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Abstract
The invention belongs to a kind of device and its production technology that high-purity ethylene is produced with ethene heat pump distillation；Including raw material liquid storage tank, products pot, raw material liquid storage tank passes sequentially through first rectifying column the first material liquid import, first rectifying column gaseous phase outlet, the raw material gas inlet of First Heat Exchanger first, the unstripped gas of First Heat Exchanger first is exported, first gas-liquid separator import, first gas-liquid separator liquid-phase outlet, first rectifying column the second material liquid import, first rectifying column liquid-phase outlet, Second distillation column the first material liquid import, Second distillation column gaseous phase outlet, the raw material gas inlet of First Heat Exchanger second, the outlet of the unstripped gas of First Heat Exchanger second is connected with the second gas-liquid separator, the the second material liquid import respectively with Second distillation column of second gas-liquid separator liquid-phase outlet and products pot are connected；Have the advantages that simple, stable technological process, low energy consumption, low safe and reliable to operation, unit of the product power consumption, reduction production cost and product purity are high.
Description
Technical field
The invention belongs to produce high-purity ethylene technical field, and in particular to a kind of to produce high-purity ethylene with ethene heat pump distillation
Device and its production technology.
Background technology
1st, ethene is reclaimed from oven gas：Be it is a kind of start from 1940s and be eliminated in the sixties it is industrially prepared
The method of ethene.Contain about 2% ethene in usual oven gas.Sulphate method separating ethene from oven gas is used earliest, i.e.,
Ethene is first converted into ethanol with sulfuric acid, then obtain ethene through catalytic dehydration again.The ethylene impurities produced in this way are more,
Purity is low, and later a company of Britain succeeds in developing oven gas low temperature processing.Then German company has also built up a few set low temperature
Separating and preparing hydrogen device and ethene refining plant, make the purity of ethene reach more than 95%.
2nd, acetylene hydrogenation legal system ethene：Germany has developed the work that ethene is produced with acetylene hydrogenation method in 1930s
Skill, and built up several set commercial scale plants.It is that carrier, palladium are active component that hydrogenation catalyst used, which is subject to silica gel, uses the longevity
Life was up to 8 months, and acetylene need to be purified before hydrogenation, but this method is eliminated in 1960s.
3rd, producing ethylene from dehydration of ethanol：The commercial run of ethylene preparation by ethanol dehydration, dehydration are carried out using aluminium oxide catalyst
Catalyst is loaded with the coke of phosphoric acid in addition to activated alumina, also, and reaction temperature is 300~400 DEG C, and ethylene product purity is
97%-99.5%, the catalyst used at present is Mars aluminum oxide.Possess abundant molasses in India, Pakistan and Brazil etc.
Or the country of other agricultural resources, due to petroleum resources shortage, ethene is produced using this method, used technique is then by fixing
Bed develops into fluid bed, it is said that reaction selectivity brings up to about 99% by the former 94%~96%, investment cost is relatively low.China
Also some enterprises produce ethene using this method.The cost for producing ethene with this method is far above hydrocarbons pyrolysis method.
4th, hydrocarbons pyrolysis method：Modern ethylene industry production method is mainly using petroleum hydrocarbon as raw material, in isolation air
With under hot conditions by macromolecular cleavage be small molecule.Extensively, this is also current most popular side to the method raw material sources
Method, but its can only separation purity 99% or so ethene, it is impossible to reach high-purity.
5th, the high-purity ethylene using ethene as raw material produces flow (cryogenic rectification method), and the technique mainly utilizes unstripped gas each group
Under the difference of point relative volatility, cryogenic conditions, liquefying and rectifying is carried out in rectifying column, Ethylene purity is up to 99.99%, still
Traditional cryogenic rectification method purifying ethylene technology existing defects, the height of product purity and equipment investment etc. are directly proportional, smart in addition
The thermal efficiency of rectifying during evaporating is low, causes the waste of energy, the rise of production cost.
The content of the invention
There is provided a kind of using heat pump distillation and double tower it is an object of the invention to overcome defect present in prior art
The cryogenic rectification mode of rectifying, technological process are simple, easy to operate, and stable, low energy consumption and preparation liquid phase Ethylene purity are not
A kind of device and its production technology that high-purity ethylene is produced with ethene heat pump distillation less than 99.999%.
The present invention is achieved through the following technical solutions above-mentioned purpose：Including raw material liquid storage tank, heat pump, waste gas stove, by-product
Product tank and products pot, raw material liquid storage tank are connected by first throttle valve with the first material liquid import of first rectifying column, the first essence
Evaporate the gaseous phase outlet of top of tower by the first unstripped gas outlet of the first raw material gas inlet of First Heat Exchanger, First Heat Exchanger with
The import of first gas-liquid separator is connected, the liquid-phase outlet of the first gas-liquid separator bottom and the second material liquid of first rectifying column
Import is connected；The outlet of first rectifying column bottom liquid phases passes through the second regulating valve and the first material liquid import phase of Second distillation column
Even, Second distillation column top gas phase outlet passes through the second raw material gas inlet of First Heat Exchanger and the second raw material of First Heat Exchanger
Gas outlet is connected with the second gas-liquid separator, the second gas-liquid separator bottom liquid phases export pass through pipeline respectively with Second distillation column
The second material liquid import be connected with products pot, Second distillation column bottom liquid phases outlet pass through the 3rd regulating valve and byproduct tank phase
Even；Gaseous phase outlet at the top of first gas-liquid separator passes sequentially through the inlet exhaust gas of the second heat exchanger, the tail gas of the second heat exchanger
Outlet and the first regulating valve are connected with waste gas stove；The first circulation gas that the outlet of heat pump cycle gas passes sequentially through the second heat exchanger enters
Mouth, the first circulation gas of the second heat exchanger export, are located at the first reboiler of first rectifying column bottom, are located at Second distillation column bottom
Second reboiler in portion, second throttle, the circulation fluid import of First Heat Exchanger, the circulating air outlet of First Heat Exchanger, second
The second circulation gas outlet of the second circulation gas import of heat exchanger and the second heat exchanger is connected, and the second of described the second heat exchanger
Circulating air outlet is connected by pipeline with heat pump cycle gas import, and the first circulation gas of second heat exchanger exports and be located at the
Between first reboiler of one rectifier bottoms be provided with the first threeway, first reboiler for being located at first rectifying column bottom and
It is located between the second reboiler of Second distillation column bottom and is provided with the second threeway, the of the 3rd end of the first threeway and the second threeway
Shortcut pipeline is provided between three ends.
A kind of production method for the device that superelevation pure ethylene is produced with ethene heat pump distillation, comprises the following steps：
Step one：The first material liquid import that material liquid in raw material liquid storage tank passes through first throttle valve and first rectifying column
Into in first rectifying column；Described material liquid is technical grade ethene, and its composition is：Ethene, ethane, propane, propylene, first
Alkane, water, hydrogen；The temperature of unstripped gas is：- 24 DEG C, pressure be：2.5Mpa, flow are：200Nm3/ h, gas phase fraction are 0, second
Alkene molar fraction：99.9%；
Step 2：Make to enter in step one rectification and purification of material liquid progress, a rectification and purification in first rectifying column
Gas phase afterwards passes through the gaseous phase outlet at the top of first rectifying column, the first raw material gas inlet of First Heat Exchanger and First Heat Exchanger
The outlet of first unstripped gas, which enters, carries out gas-liquid separation in the first gas-liquid separator, the liquid phase after gas-liquid separation passes through the first gas-liquid point
Liquid-phase outlet from device bottom enters in first rectifying column, and the outlet of first rectifying column bottom liquid phases enters the by the second regulating valve
First material liquid import of two rectifying columns；The first rectifying column top gas phase outlet gas phase temperature be：- 85~-87 DEG C,
Ethylene mole fraction：99.97%；The liquid-phase outlet of first gas-liquid separator enter first rectifying column in liquidus temperature be：-
87.6 DEG C, flow is：61Nm3/h；The liquid phase flow that the bottom of towe liquid-phase outlet of first rectifying column enters in Second distillation column：
90Nm3/ h, gas phase fraction：0；
Step 3：The liquid phase entered in step 2 in Second distillation column is set to carry out secondary rectification and purification, secondary rectification and purification
Gaseous products afterwards pass sequentially through the second raw material gas inlet of First Heat Exchanger, the outlet of the second unstripped gas, the second gas-liquid separator
Liquid-phase outlet respectively enter in Second distillation column and products pot, the bottom that Second distillation column liquid phase byproduct passes through Second distillation column
Portion's liquid-phase outlet and the 3rd regulating valve enter in byproduct tank；The liquid-phase product temperature of the entrance products pot is：- 92~-93
DEG C, flow be：30Nm3/ h, purity are not less than 99.999%, and the liquid-phase product of the entrance products pot is superelevation pure ethylene；Enter
The liquid phase byproduct temperature for entering byproduct tank is：- 90~-92 DEG C, flow be：60Nm3/ h, main component：99.8% ethene,
0.13% ethane, can be as technical grade ethene, and the liquid-phase product of the entrance byproduct tank is technical grade ethene；
Step 4：The waste gas after gas-liquid separation is carried out in the gas-liquid separator of entrance first described in step 2 to pass sequentially through
The outlet of first gas-liquid separator top gas phase, the inlet exhaust gas of the second heat exchanger, the offgas outlet of the second heat exchanger and first are adjusted
Valve is saved to enter in waste gas stove；The EGT of first gas-liquid separator top gas phase outlet is：It is -87 DEG C~-88 DEG C, described
Exhaust temperature in waste gas stove is：33~37 DEG C；
Step 5：Circulating air in heat pump passes sequentially through the first circulation gas import of the second heat exchanger, the second heat exchanger
The outlet of first circulation gas, the first reboiler for being located at first rectifying column bottom, the second reboiler for being located at Second distillation column bottom
The circulation fluid for entering First Heat Exchanger with second throttle enters intraoral；The component of the circulating air：Ethene, ethane, methane, ethene
Molar fraction：99%；Second heat exchanger first circulation gas outlet circulating air temperature be：- 51~-52 DEG C, gas phase fraction：1；
First reboiler outlet circulation fluid temperature be：- 84~-82 DEG C of gas phase fractions：0；The circulation fluid temperature of second reboiler outlet
For：- 88~-89 DEG C, gas phase fraction：0；Second throttle outlet circulation fluid temperature be：- 99~-100 DEG C；
Step 6：The circulation fluid for entering First Heat Exchanger by second throttle in above-mentioned steps five is set to enter intraoral circulation
Liquid is exchanged heat, and the circulating air after heat exchange passes sequentially through the circulating air outlet of First Heat Exchanger, the second heat exchanger second circulation gas
The second circulation gas outlet of import and the second heat exchanger enters in heat pump 9, completes ethylene recycle；The first of the First Heat Exchanger
Circulating air outlet circulating air temperature be：- 92~-93 DEG C, gas phase fraction：0.98, the second circulation gas outlet of the second heat exchanger
Circulating air temperature be：13~15 DEG C, gas phase fraction：1.
The present invention produces high-purity ethylene using heat pump distillation, the cryogenic rectification mode of two-tower rectification, and product liquid phase ethylene is pure
Degree is not less than 99.999%, and it has filled up the blank of domestic high-purity ethylene production, and compared with traditional distillation technology, the present invention has
Following advantage：1. reverse Carnot cycle principle and heat-pump rectifying process are used for into the purification and liquefaction of ethene, condensation heat is used as
Reboiler thermal source, improves the capacity usage ratio of distillation system, product energy consumption is greatly reduced；2. using two-tower rectification technology, improve
The diversification of unstripped gas, solves the problem of methane in material liquid, ethane, propane, propylene etc. are difficult to remove, remove high energy consumption；
3. product purity is up to more than 99.999%, domestic high-purity ethylene production blank is filled up, traditional cracking process production ethene is solved
Product purity 99%.Catalysis is solved while the problems such as traditional purifying plant complexity, big investment, thermodynamic efficiency is solved to split
Not the problem of solution product quality does not reach high-purity grade；With technological process is simple, easy to operate, stable, low energy consumption, operation
Safe and reliable, unit of the product power consumption is low, reduces production cost and can improve product purity to the spy of 99.999% high-purity rank
Point；The development of research and semiconductor applications to high-purity ethylene gas provides safeguard, with good economic and social benefit.
Brief description of the drawings
Fig. 1 is structural representation of the invention.
Embodiment
In order to which technical characteristic, purpose and effect to the present invention are more clearly understood from, now control illustrates this hair
Bright embodiment, in the various figures identical label represent identical part.It is only schematic in simplified form, each figure to make
Ground indicates the part related to invention, and they do not represent it as the practical structures of product.
As shown in figure 1, the present invention is a kind of device and its production technology that high-purity ethylene is produced with ethene heat pump distillation；Bag
Raw material liquid storage tank 7, heat pump 9, waste gas stove 6, byproduct tank 19 and products pot 15 are included, raw material liquid storage tank 7 passes through first throttle valve 39
It is connected with the first material liquid import 20 of first rectifying column 10, the gaseous phase outlet 21 at the top of first rectifying column 10 passes through the first heat exchange
First raw material gas inlet 22 of device 12, the first unstripped gas outlet 23 of First Heat Exchanger 12 and the import of the first gas-liquid separator 11
It is connected, the liquid-phase outlet of the bottom of the first gas-liquid separator 11 is connected with the second material liquid import 25 of first rectifying column 10；First
The bottom liquid phases of rectifying column 10 outlet 32 is connected by the second regulating valve 4 with the first material liquid import 26 of Second distillation column 14, the
The top gas phase of two rectifying column 14 outlet 27 pass through the second raw material gas inlet 28 of First Heat Exchanger 12 and First Heat Exchanger 12 the
Two unstripped gas outlet 29 is connected with the second gas-liquid separator 13, and the bottom liquid phases of the second gas-liquid separator 13 outlet 2 passes through pipeline point
The second material liquid import 31 and products pot 15 not with Second distillation column 14 are connected, and the bottom liquid phases of Second distillation column 14 outlet 33 leads to
The 3rd regulating valve 5 is crossed with byproduct tank 19 to be connected；The gaseous phase outlet 35 at the top of the first gas-liquid separator 11 passes sequentially through second and changed
The inlet exhaust gas 36 of hot device 8, the regulating valve 1 of offgas outlet 37 and first of the second heat exchanger 8 are connected with waste gas stove 6；Heat pump 9 is circulated
Gas outlet passes sequentially through the first circulation gas import 41 of the second heat exchanger 8, the first circulation gas outlet 40 of the second heat exchanger 8, set
The first reboiler 16 in the bottom of first rectifying column 10, the second reboiler 17, second throttling for being located at the bottom of Second distillation column 14
Valve 3, the circulation fluid import 34 of First Heat Exchanger 12, the circulating air of First Heat Exchanger 12 export the second of the 30, second heat exchanger 8 and followed
Ring gas import 24 is connected with the second circulation gas outlet 18 of the second heat exchanger 8, and the second circulation gas of the second described heat exchanger 8 goes out
Mouth 18 is connected by pipeline with the circulating air import of heat pump 9, and the first circulation gas of second heat exchanger 8 exports 40 and is located at first
The first threeway 42 is provided between first reboiler 16 of the bottom of rectifying column 10, it is described to be located at the first of the bottom of first rectifying column 10 again
The second threeway 42, the 3rd of the first threeway 43 the are provided between boiling device 16 and the second reboiler 17 for being located at the bottom of Second distillation column 43
Shortcut pipeline is provided between end and the 3rd end of the second threeway 42.
A kind of production method for the device that superelevation pure ethylene is produced with ethene heat pump distillation, comprises the following steps：
Step one：The first raw material that material liquid in raw material liquid storage tank 7 passes through first throttle valve 39 and first rectifying column 10
Liquid import 20 enters in first rectifying column 10；Described material liquid is technical grade ethene, and its composition is：Ethene, ethane, third
Alkane, propylene, methane, water, hydrogen；The temperature of unstripped gas is：- 24 DEG C, pressure be：2.5Mpa, flow are：200Nm3/ h, gas phase
It is 0, ethylene mole fraction to divide rate：99.9%；
Step 2：Make to enter in step one rectification and purification of material liquid progress in first rectifying column 10, a rectifying is carried
Gas phase after pure passes through the gaseous phase outlet 21 at the top of first rectifying column 10, the first raw material gas inlet 22 of First Heat Exchanger 12 and the
The first unstripped gas outlet 23 of one heat exchanger 12, which enters in the first gas-liquid separator 11, carries out gas-liquid separation, the liquid after gas-liquid separation
Entered by the liquid-phase outlet 38 of the bottom of the first gas-liquid separator 11 in first rectifying column 10, the bottom liquid phases of first rectifying column 10
Outlet 32 enters the first material liquid import 26 of Second distillation column 14 by the second regulating valve 4；The top of the first rectifying column 10
The gas phase temperature of portion's gaseous phase outlet 21 is：- 85~-87 DEG C, ethylene mole fraction：99.97%；The liquid of first gas-liquid separator 11
Mutually outlet is into the liquidus temperature in first rectifying column 10：- 87.6 DEG C, flow is：61Nm3/h；The tower of first rectifying column 10
The liquid phase flow that bottom liquid-phase outlet 32 enters in Second distillation column 14：90Nm3/ h, gas phase fraction：0；
Step 3：The liquid phase entered in step 2 in Second distillation column 14 is set to carry out secondary rectification and purification, secondary rectifying is carried
Gaseous products after pure pass sequentially through the second raw material gas inlet 28 of First Heat Exchanger 12, the second unstripped gas and export the 29, second gas
The liquid-phase outlet of liquid/gas separator 13 is respectively enterd in Second distillation column 14 and products pot 15, and the liquid phase byproduct of Second distillation column 14 leads to
The bottom liquid phases outlet 33 and the 3rd regulating valve 5 for crossing Second distillation column 14 enter in byproduct tank 19；The entrance products pot 15
Liquid-phase product temperature be：- 92~-93 DEG C, flow be：30Nm3/ h, purity are not less than 99.999%, the entrance products pot
15 liquid-phase product is superelevation pure ethylene；Liquid phase byproduct temperature into byproduct tank 19 is：- 90~-92 DEG C, flow be：
60Nm3/ h, main component：99.8% ethene, 0.13% ethane, can as technical grade ethene, the entrance byproduct tank 19
Liquid-phase product is technical grade ethene；
Step 4：The waste gas after gas-liquid separation is carried out in the first gas-liquid separator of entrance 11 described in step 2 successively to lead to
Inlet exhaust gas 36, the tail gas of the second heat exchanger 8 for crossing the 35, second heat exchanger 8 of the top gas phase of the first gas-liquid separator 11 outlet go out
The regulating valve 1 of mouth 37 and first enters in waste gas stove 6；The EGT of the top gas phase of first gas-liquid separator 11 outlet 35
For：- 87 DEG C~-88 DEG C, the exhaust temperature in the waste gas stove 6 is：33~37 DEG C；
Step 5：The first circulation gas import 41, second that circulating air in heat pump 9 passes sequentially through the second heat exchanger 8 exchanges heat
The first circulation gas of device 8 exports 40, is located at the first reboiler 16 of the bottom of first rectifying column 10, is located at the bottom of Second distillation column 14
The second reboiler 17 and second throttle 3 enter First Heat Exchanger 12 circulation fluid import 34 in；The component of the circulating air：
Ethene, ethane, methane, ethylene mole fraction：99%；The circulating air temperature of the first circulation gas outlet 40 of second heat exchanger 8
For：- 51~-52 DEG C, gas phase fraction：1；First reboiler 16 outlet circulation fluid temperature be：- 84~-82 DEG C of gas phase fractions：0；
Second reboiler 17 outlet circulation fluid temperature be：- 88~-89 DEG C, gas phase fraction：0；The circulation fluid that second throttle 3 is exported
Temperature is：- 99~-100 DEG C；
Step 6：Make in the circulation fluid import 34 in above-mentioned steps five by the entrance First Heat Exchanger 12 of second throttle 3
Circulation fluid exchanged heat, the circulating air after heat exchange pass sequentially through First Heat Exchanger 12 circulating air export the 30, second heat exchanger 8
The second circulation gas outlet 18 of the import 24 of second circulation gas and the second heat exchanger 8 enters in heat pump 9, completes ethylene recycle；It is described
First Heat Exchanger 12 first circulation gas outlet 30 circulating air temperature be：- 92~-93 DEG C, gas phase fraction：0.98, second changes
Hot device 8 second circulation gas outlet 18 circulating air temperature be：13~15 DEG C, gas phase fraction：1.
The present invention is a kind of device and production method that high-purity ethylene is produced with ethene heat pump distillation, wherein technical grade ethene
There is national standard, but high-purity ethylene product quality does not have national standard, reference《Chinese industrial gas is complete works of》And offshore company
Company standard, ethene is divided into seven ranks：Two grades：>=99.85%, one-level：>=99.9%, top grade：>=99.9%, and U.S.'s mark
Standard 99.95%；Bibliography：《Chinese industrial gas is complete works of》3rd, the 2427th page table II.2.6.41 foreign countries ethylene product matter
Amount standard.The book is write by Chinese industrial gas industry association, and publishing house of Dalian University of Technology publishes.Present invention process method
Advantage is the high-purity ethylene using technical grade ethene as raw material production quality 99.999%, also has to a certain degree in product quality
Breakthrough, fill up domestic high-purity ethylene product blank.Secondly, technique is entered on the basis of combining existing two-tower rectification and heat pump techniques
Row process modification and innovation, so as to drastically increase recycling for energy, the involvement of heat pump techniques solves traditional rectifying
Equipment energy consumption is big, the low problem of thermodynamic efficiency, and heat pump distillation is that rectifying tower top steam is pressurizeed to heat up, and serves as bottom of towe again
Device thermal source is boiled, the condensation latent heat of overhead vapours is reclaimed.Again, using ethene as refrigerant, heat is provided for system by heat pump techniques
Amount and cold, utilize ethylene recycle, ethene pressurizes through heat pump, are provided into rectifying column reboiler after heat, itself liquefaction, warp
After choke valve decompression, go rectifying column evaporator overhead condenser to provide cold, itself gasification is reclaimed after cold, return to heat pump import progress
Subsequent cycle.The utilization ratio for the energy that above-mentioned pattern is greatly improved, reduces the waste of energy.This last process is used
Heat pump techniques, two-tower rectification, with technological process is simple, easy to operate, stable and safe in operation the characteristics of.
For the more detailed explanation present invention, the present invention is further elaborated in conjunction with embodiment.Specific embodiment
It is as follows：
Embodiment one
A kind of device that high-purity ethylene is produced with ethene heat pump distillation, including raw material liquid storage tank 7, heat pump 9, waste gas stove 6, pair
Products pot 19 and products pot 15, the first material liquid import that raw material liquid storage tank 7 passes through first throttle valve 39 and first rectifying column 10
20 are connected, and the gaseous phase outlet 21 at the top of first rectifying column 10 is changed by the first raw material gas inlet 22 of First Heat Exchanger 12, first
The first unstripped gas outlet 23 of hot device 12 is connected with the import of the first gas-liquid separator 11, the liquid of the bottom of the first gas-liquid separator 11
Mutually outlet is connected with the second material liquid import 25 of first rectifying column 10；The bottom liquid phases of first rectifying column 10 outlet 32 passes through second
Regulating valve 4 is connected with the first material liquid import 26 of Second distillation column 14, and the top gas phase of Second distillation column 14 outlet 27 passes through the
The second raw material gas inlet 28 and the second unstripped gas outlet 29 of First Heat Exchanger 12 and the second gas-liquid separator of one heat exchanger 12
13 are connected, and the bottom liquid phases of the second gas-liquid separator 13 export 2 the second material liquid by pipeline respectively with Second distillation column 14 and entered
Mouth 31 is connected with products pot 15, and the bottom liquid phases of Second distillation column 14 outlet 33 is connected by the 3rd regulating valve 5 with byproduct tank 19；
The gaseous phase outlet 35 at the top of the first gas-liquid separator 11 passes sequentially through the inlet exhaust gas 36 of the second heat exchanger 8, the second heat exchanger 8
The regulating valve 1 of offgas outlet 37 and first is connected with waste gas stove 6；The outlet of the circulating air of heat pump 9 passes sequentially through the first of the second heat exchanger 8
Circulating air import 41, the first circulation gas outlet 40 of the second heat exchanger 8, the first reboiler for being located at the bottom of first rectifying column 10
16th, be located at the second reboiler 17 of the bottom of Second distillation column 14, second throttle 3, the circulation fluid import 34 of First Heat Exchanger 12,
The circulating air of First Heat Exchanger 12 exports the second circulation gas import 24 of the 30, second heat exchanger 8 and the second of the second heat exchanger 8 follows
Ring gas outlet 18 is connected, and the second circulation gas outlet 18 of the second described heat exchanger 8 passes through pipeline and the circulating air import phase of heat pump 9
Even, between the first circulation gas outlet 40 of second heat exchanger 8 and the first reboiler 16 for being located at the bottom of first rectifying column 10
Provided with the first threeway 42, first reboiler 16 for being located at the bottom of first rectifying column 10 and the bottom of Second distillation column 43 is located at
The second threeway 42 is provided between second reboiler 17, is provided between the 3rd end of the first threeway 43 and the 3rd end of the second threeway 42
Shortcut pipeline.
A kind of production method for the device that superelevation pure ethylene is produced with ethene heat pump distillation, comprises the following steps：
Step one：The first raw material that material liquid in raw material liquid storage tank 7 passes through first throttle valve 39 and first rectifying column 10
Liquid import 20 enters in first rectifying column 10；Described material liquid is technical grade ethene, and its composition is：Ethene, ethane, third
Alkane, propylene, methane, water, hydrogen；The temperature of unstripped gas is：- 24 DEG C, pressure be：2.5Mpa, flow are：200Nm3/ h, gas phase
It is 0, ethylene mole fraction to divide rate：99.9%；
Step 2：Make to enter in step one rectification and purification of material liquid progress in first rectifying column 10, a rectifying is carried
Gas phase after pure passes through the gaseous phase outlet 21 at the top of first rectifying column 10, the first raw material gas inlet 22 of First Heat Exchanger 12 and the
The first unstripped gas outlet 23 of one heat exchanger 12, which enters in the first gas-liquid separator 11, carries out gas-liquid separation, the liquid after gas-liquid separation
Entered by the liquid-phase outlet 38 of the bottom of the first gas-liquid separator 11 in first rectifying column 10, the bottom liquid phases of first rectifying column 10
Outlet 32 enters the first material liquid import 26 of Second distillation column 14 by the second regulating valve 4；The top of the first rectifying column 10
The gas phase temperature of portion's gaseous phase outlet 21 is：- 85~-87 DEG C, ethylene mole fraction：99.97%；The liquid of first gas-liquid separator 11
Mutually outlet is into the liquidus temperature in first rectifying column 10：- 87.6 DEG C, flow is：61Nm3/h；The tower of first rectifying column 10
The liquid phase flow that bottom liquid-phase outlet 32 enters in Second distillation column 14：90Nm3/ h, gas phase fraction：0；
Step 3：The liquid phase entered in step 2 in Second distillation column 14 is set to carry out secondary rectification and purification, secondary rectifying is carried
Gaseous products after pure pass sequentially through the second raw material gas inlet 28 of First Heat Exchanger 12, the second unstripped gas and export the 29, second gas
The liquid-phase outlet of liquid/gas separator 13 is respectively enterd in Second distillation column 14 and products pot 15, and the liquid phase byproduct of Second distillation column 14 leads to
The bottom liquid phases outlet 33 and the 3rd regulating valve 5 for crossing Second distillation column 14 enter in byproduct tank 19；The entrance products pot 15
Liquid-phase product temperature be：- 92~-93 DEG C, flow be：30Nm3/ h, purity are not less than 99.999%, the entrance products pot
15 liquid-phase product is superelevation pure ethylene；Liquid phase byproduct temperature into byproduct tank 19 is：- 90~-92 DEG C, flow be：
60Nm3/ h, main component：99.8% ethene, 0.13% ethane, can as technical grade ethene, the entrance byproduct tank 19
Liquid-phase product is technical grade ethene；
Step 4：The waste gas after gas-liquid separation is carried out in the first gas-liquid separator of entrance 11 described in step 2 successively to lead to
Inlet exhaust gas 36, the tail gas of the second heat exchanger 8 for crossing the 35, second heat exchanger 8 of the top gas phase of the first gas-liquid separator 11 outlet go out
The regulating valve 1 of mouth 37 and first enters in waste gas stove 6；The EGT of the top gas phase of first gas-liquid separator 11 outlet 35
For：- 87 DEG C~-88 DEG C, the exhaust temperature in the waste gas stove 6 is：33~37 DEG C；
Step 5：The first circulation gas import 41, second that circulating air in heat pump 9 passes sequentially through the second heat exchanger 8 exchanges heat
The first circulation gas of device 8 exports 40, is located at the first reboiler 16 of the bottom of first rectifying column 10, is located at the bottom of Second distillation column 14
The second reboiler 17 and second throttle 3 enter First Heat Exchanger 12 circulation fluid import 34 in；The component of the circulating air：
Ethene, ethane, methane, ethylene mole fraction：99%；The circulating air temperature of the first circulation gas outlet 40 of second heat exchanger 8
For：- 51~-52 DEG C, gas phase fraction：1；First reboiler 16 outlet circulation fluid temperature be：- 84~-82 DEG C of gas phase fractions：0；
Second reboiler 17 outlet circulation fluid temperature be：- 88~-89 DEG C, gas phase fraction：0；The circulation fluid that second throttle 3 is exported
Temperature is：- 99~-100 DEG C；
Step 6：Make in the circulation fluid import 34 in above-mentioned steps five by the entrance First Heat Exchanger 12 of second throttle 3
Circulation fluid exchanged heat, the circulating air after heat exchange pass sequentially through First Heat Exchanger 12 circulating air export the 30, second heat exchanger 8
The second circulation gas outlet 18 of the import 24 of second circulation gas and the second heat exchanger 8 enters in heat pump 9, completes ethylene recycle；It is described
First Heat Exchanger 12 first circulation gas outlet 30 circulating air temperature be：- 92~-93 DEG C, gas phase fraction：0.98, second changes
Hot device 8 second circulation gas outlet 18 circulating air temperature be：13~15 DEG C, gas phase fraction：1.
In the description of the invention, it is to be understood that term " bottom ", " middle part ", " top ", " top " etc. are indicated
Orientation or position relationship be based on orientation shown in the drawings or position relationship, be for only for ease of description the present invention and simplification retouch
State, rather than indicate or imply that the device or element of meaning there must be specific orientation, with specific azimuth configuration and operation,
Therefore it is not considered as limiting the invention.In the description of the invention, it is necessary to which explanation, is provided unless otherwise clear and definite
And restriction, term " setting ", " installation ", " dress ", " connected " etc. should be interpreted broadly, for example, it may be being fixedly connected, integratedly
Connect or be detachably connected；It can also be the connection of two element internals；Can be joined directly together, can also pass through
Intermediary is indirectly connected to, for the ordinary skill in the art, can understand that above-mentioned term exists as the case may be
Concrete meaning in the present invention.It is to be noted that herein, " first ", " second " etc. are only used for mutual differentiation, rather than
Represent their significance level and order etc..Tool of the foregoing detailed description only for the feasibility embodiment of the present invention
Body illustrates that they simultaneously are not used to limit the scope of the invention, all equivalence enforcements made without departing from skill spirit of the present invention
Mode, change and transformation should be included in the scope of the protection.
Experimental example
The technique of the present invention is compared with using the process of hydrocarbons pyrolysis, and it has in energy consumption and product quality
Obvious difference, specifically see the table below：
| Sequence number | Process | Product power consumption (comprehensive consumption) | Product quality |
| 1 | Hydrocarbons pyrolysis | 2500KW/t | >=99% |
| 2 | The present invention | 1500KW/t | >=99.999% |
As seen from the above table, the present invention is applied to industrial-scale production, and it mainly has, and energy consumption is low and product quality is high
Feature, product quality of the invention can be improved to 99.999% electron level rank.
Claims (2)
1. a kind of device that high-purity ethylene is produced with ethene heat pump distillation, including raw material liquid storage tank (7), heat pump (9), waste gas stove
(6), byproduct tank (19) and products pot (15), it is characterised in that：Raw material liquid storage tank (7) passes through first throttle valve (39) and first
First material liquid import (20) of rectifying column (10) is connected, and the gaseous phase outlet (21) at the top of first rectifying column (10) is changed by first
The first raw material gas inlet (22) of hot device (12), the first unstripped gas outlet (23) and the first gas-liquid separation of First Heat Exchanger (12)
The import of device (11) is connected, the liquid-phase outlet of the first gas-liquid separator (11) bottom and the second material liquid of first rectifying column (10)
Import (25) is connected；First rectifying column (10) bottom liquid phases outlet (32) passes through the second regulating valve (4) and Second distillation column (14)
The first material liquid import (26) be connected, Second distillation column (14) top gas phase exports (27) the by First Heat Exchanger (12)
The second unstripped gas outlet (29) of two raw material gas inlets (28) and First Heat Exchanger (12) is connected with the second gas-liquid separator (13),
Second gas-liquid separator (13) bottom liquid phases export the second material liquid import of (2) by pipeline respectively with Second distillation column (14)
(31) it is connected with products pot (15), Second distillation column (14) bottom liquid phases outlet (33) passes through the 3rd regulating valve (5) and byproduct
Tank (19) is connected；
Gaseous phase outlet (35) at the top of first gas-liquid separator (11) pass sequentially through the second heat exchanger (8) inlet exhaust gas (36),
The offgas outlet (37) and the first regulating valve (1) of second heat exchanger (8) are connected with waste gas stove (6)；
Heat pump (9) circulating air exports first circulation gas import (41), the second heat exchanger (8) for passing sequentially through the second heat exchanger (8)
First circulation gas outlet (40), be located at first reboiler (16) of first rectifying column (10) bottom, be located at Second distillation column
(14) the second reboiler (17) of bottom, second throttle (3), the circulation fluid import (34) of First Heat Exchanger (12), first are changed
The circulating air outlet (30) of hot device (12), the of the second circulation gas import (24) of the second heat exchanger (8) and the second heat exchanger (8)
Two circulating air outlet (18) is connected, and the second circulation gas outlet (18) of described the second heat exchanger (8) passes through pipeline and heat pump (9)
Circulating air import is connected, and the first circulation gas of second heat exchanger (8) exports (40) and is located at first rectifying column (10) bottom
The first reboiler (16) between be provided with the first threeway (42), first reboiler for being located at first rectifying column (10) bottom
(16) and it is located between second reboiler (17) of Second distillation column (43) bottom and is provided with the second threeway (42), the first threeway (43)
The 3rd end and the second threeway (42) the 3rd end between be provided with shortcut pipeline.
2. a kind of production method of the device as claimed in claim 1 that superelevation pure ethylene is produced with ethene heat pump distillation, it is special
Levy and be：Comprise the following steps：
Step one：Material liquid in raw material liquid storage tank (7) passes through first throttle valve (39) and the first original of first rectifying column (10)
Liquor inlet (20) enters in first rectifying column (10)；Described material liquid is technical grade ethene, and its composition is：Ethene,
Ethane, propane, propylene, methane, water, hydrogen；The temperature of unstripped gas is：- 24 DEG C, pressure be：2.5Mpa, flow are：200Nm3/
H, gas phase fraction are 0, ethylene mole fraction：99.9%；
Step 2：Make to enter first rectifying column (10) rectification and purification of interior material liquid progress, a rectification and purification in step one
Gas phase afterwards passes through the gaseous phase outlet (21) at the top of first rectifying column (10), the first raw material gas inlet of First Heat Exchanger (12)
(22) gas-liquid separation and in the first unstripped gas outlet (23) the first gas-liquid separator of entrance (11) of First Heat Exchanger (12) is carried out,
Liquid phase after gas-liquid separation is entered in first rectifying column (10) by the liquid-phase outlet (38) of the first gas-liquid separator (11) bottom,
First rectifying column (10) bottom liquid phases export the first material liquid that (32) enter Second distillation column (14) by the second regulating valve (4)
Import (26)；The first rectifying column (10) top gas phase outlet (21) gas phase temperature be：- 85~-87 DEG C, ethylene molar
Fraction：99.97%；The liquid-phase outlet of first gas-liquid separator (11) enter first rectifying column (10) in liquidus temperature be：-
87.6 DEG C, flow is：61Nm3/h；The bottom of towe liquid-phase outlet (32) of first rectifying column (10) enters in Second distillation column (14)
Liquid phase flow：90Nm3/ h, gas phase fraction：0；
Step 3：The liquid phase entered in step 2 in Second distillation column (14) is set to carry out secondary rectification and purification, secondary rectification and purification
Gaseous products afterwards pass sequentially through the second raw material gas inlet (28) of First Heat Exchanger (12), the second unstripped gas outlet (29), the
The liquid-phase outlet of two gas-liquid separators (13) is respectively enterd in Second distillation column (14) and products pot (15), Second distillation column (14)
Liquid phase byproduct exports (33) by the bottom liquid phases of Second distillation column (14) and the 3rd regulating valve (5) enters byproduct tank (19)
It is interior；The liquid-phase product temperature of the entrance products pot (15) is：- 92~-93 DEG C, flow be：30Nm3/ h, purity are not less than
99.999%, the liquid-phase product of the entrance products pot (15) is superelevation pure ethylene；Into the liquid phase by-product of byproduct tank (19)
Product temperature degree is：- 90~-92 DEG C, flow be：60Nm3/ h, main component：99.8% ethene, 0.13% ethane, can be used as industry
Level ethene, the liquid-phase product of the entrance byproduct tank (19) is technical grade ethene；
Step 4：The waste gas after gas-liquid separation is carried out in the gas-liquid separator of entrance first (11) described in step 2 to pass sequentially through
First gas-liquid separator (11) top gas phase outlet (35), the inlet exhaust gas (36) of the second heat exchanger (8), the second heat exchanger (8)
Offgas outlet (37) and the first regulating valve (1) enter in waste gas stove (6)；First gas-liquid separator (11) top gas phase goes out
The EGT of mouthful (35) is：- 87 DEG C~-88 DEG C, the exhaust temperature in the waste gas stove (6) is：33~37 DEG C；
Step 5：Circulating air in heat pump (9) passes sequentially through the first circulation gas import (41) of the second heat exchanger (8), second changed
The first circulation gas of hot device (8) exports (40), is located at first reboiler (16) of first rectifying column (10) bottom, is located at the second essence
The second reboiler (17) and second throttle (3) for evaporating tower (14) bottom enter the circulation fluid import (34) of First Heat Exchanger (12)
It is interior；The component of the circulating air：Ethene, ethane, methane, ethylene mole fraction：99%；The first circulation of second heat exchanger (8)
Gas outlet (40) circulating air temperature be：- 51~-52 DEG C, gas phase fraction：1；The circulation fluid temperature of first reboiler (16) outlet
For：- 84~-82 DEG C of gas phase fractions：0；Second reboiler (17) outlet circulation fluid temperature be：- 88~-89 DEG C, gas phase fraction：
0；Second throttle (3) outlet circulation fluid temperature be：- 99~-100 DEG C；
Step 6：Make the circulation fluid import (34) for entering First Heat Exchanger (12) in above-mentioned steps five by second throttle (3)
Interior circulation fluid is exchanged heat, and the circulating air after heat exchange passes sequentially through the circulating air outlet (30) of First Heat Exchanger (12), second
The second circulation gas outlet (18) of heat exchanger (8) second circulation gas import (24) and the second heat exchanger (8) enters in heat pump (9),
Complete ethylene recycle；The First Heat Exchanger (12) first circulation gas outlet (30) circulating air temperature be：- 92~-93 DEG C,
Gas phase fraction：0.98, the circulating air temperature of the second circulation gas of the second heat exchanger (8) outlet (18) is：13~15 DEG C, gas phase point
Rate：1.
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