CN110388790A - A kind of ethane cracking deep cooling process for separating method - Google Patents
A kind of ethane cracking deep cooling process for separating method Download PDFInfo
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- CN110388790A CN110388790A CN201910699445.6A CN201910699445A CN110388790A CN 110388790 A CN110388790 A CN 110388790A CN 201910699445 A CN201910699445 A CN 201910699445A CN 110388790 A CN110388790 A CN 110388790A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/04—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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
Abstract
The invention discloses a kind of ethane cracking deep cooling process for separating methods, and for the cracking gas of existing ethane cracking technique, the cracking gas purified treatment that ethane cracking generates is obtained the products such as polymer grade ethylene by the process freezed using multistage rectification and azeotrope.The cryogenic separation system replaces the deep cooling process for separating of ethylene, propylene cascade refrigeration, reduces the investment of refrigeration relevant device, investment cost is greatly saved, simple flow reduces the operation energy consumption of operation difficulty and package unit.
Description
Technical field
The invention belongs to the ethane cracking alkene fields of petrochemical industry, are related to a kind of ethane cracking cryogenic separation work
The cracking gas purified treatment that ethane cracking generates is obtained the products such as polymer grade ethylene by process.
Background technique
Ethylene is most basic, most important petrochemical materials, and the production capacity of ethylene represents a national oil chemical industry
Development level；In China or even the whole world, oil product steam cracking is the main source of ethylene product, although the country was in recent years
Methanol-to-olefins have developed rapidly, but its ethylene production capacity can not be compared with steam cracking.
In the raw material raw material of all preparing ethylene by steam cracking, ethane is the highest pressure of yield of ethene, be can achieve
80.5%；The most important raw material of steam cracking is naphtha, and the yield of ethene of naphtha only has 35% or so, therefore, ethane
It is the raw material of best preparing ethylene by steam cracking.
Ethane cracking ethylene have many advantages, such as at low cost, high income, small investment, pollution it is small, however, China also
It puts into production completely by the cracker of raw material of ethane without one, although there is one or more lighter hydrocarbons in every manufacturing enterprise
Furnace, but the raw material that these lighter hydrocarbons furnaces are cracked mostly is cycle ethane and recycled propane, and really fresh ethane charging is few
It is again few；The main reason for causing this situation has ethane low and storage transport difficult.
In recent years, just with the large scale mining in the U.S., Canada and Middle East natural gas, especially shale gas exploitation
Be is ripe day by day, and the supply of ethane feed greatly improves, and price is also constantly declining；And low-temperature material stores and transport skill
Art is gradually improved, and storage and transport increase substantially, and storage and transport cost is also declining, and the advantage of ethane cracking ethylene is
It highlights.
Currently, domestic You Duojia big companies and the U.S. sign ethane procurement contract, also several ethane crackings are filled
It sets to enter and establishes the stage.
In China, ethane cracking ethylene is a kind of new process, and the purification of matched downstream ethylene, separation,
Purification is even more a kind of new process, there is very big optimization innovative space.
Summary of the invention
The present invention be directed to the cracking gas deep cooling process for separating energy consumptions of existing ethane cracking technique compared with high, equipment is more, technique
Complicated disadvantage proposes a kind of deep cooling process for separating that ethylene, propylene cascade refrigeration are replaced with azeotrope.
The purpose of the present invention is be achieved by following technical proposals: the invention discloses a kind of ethane cracking deep coolings point
Separating process method, comprises the steps of
(1) (40 DEG C of temperature or so, pressure 40-90KPa) of cracking gas from chilling column overhead enter charge gas compressor
One section of suction tank, boosts to 1-3MPa through compressor；
(2) cracking gas uses multi-stage compression, cooling, lime set return chilling top of tower between compressor section between machine, compressor end
End check vent one's spleen (pressure 1-3MPa) cool to 40 DEG C or so, gaseous phase materials, which heat up, enters caustic wash tower after 3-5 DEG C；
(3) cracking gas for removing sour gas leaves caustic wash tower after the washing of caustic wash tower top washing section, changes into cryogen
Hot device, temperature are down to 10-15 DEG C；
(4) cracking gas after cooling down enters knockout drum, and lime set returns to tank between chilling top of tower or compressor section, gas phase
Into drier；
(5) cracking gas for removing moisture enters two Cutting Tap of carbon through cooling, and C2 or more component is condensed into liquid and flows to tower reactor,
C1 and some light-component gas are discharged from cutting column overhead；
(6) two Cutting Tap kettle material of carbon enters dethanizer, and deethanizer overhead condenser is fractional distilling tube, reflux
Tank material is divided into 3 strands, and first burst of reflux as dethanizer, second burst of two Cutting Tap of feeding carbon top is as reflux, reflux
Tank tank deck gaseous phase materials remove back end hydrogenation reactor through re-heat；
(7) dethanizer kettle material enters depropanizing tower, and C4 or more group liquid flows to tower reactor and produced by tower reactor, C3 group
Divide and be discharged from tower top, enter return tank after overhead condenser is cooling and separate, return tank C3 liquid returns stream, surplus liquid work
For the extraction of C3 product；
(8) depropanizing tower kettle material is sent into debutanizing tower, return tank of top of the tower extraction mixing four product of carbon, and tower reactor produces carbon
Five and heavy constituent；
(9) two Cutting Tap top gaseous phase of carbon enters ethylene front-end hydrogenation reactor after re-heat, removes the acetylene group in material
Point；
(10) ethylene front-end hydrogenation reactor outlet material enters the second drier removing micro-moisture after cooling down；
(11) second driers enter deep-cooling heat exchanger, the liquid phase object of the different temperatures condensed out after flowing out material cooling
Material respectively enters the different location of domethanizing column；
(12) the thick hydrogen of low temperature of 95% or more purity is isolated in deep-cooling heat exchanger end, and the thick hydrogen of low temperature flows through ice chest heat exchanger
Rewarming is to room temperature；
(13) the thick hydrogen of room temperature can enter the hydrogen product of methanation and 95% or more hydrogen dryer output purity；
(14) the thick hydrogen of room temperature obtains high purity hydrogen product after can entering PSA device pressure-variable adsorption；
(15) enter after the cooling of acetylene back end hydrogenation reactor outlet material and wash green oil tank, two material of carbon for removing green oil enters
Third drier；
(16) third dryer export material enters domethanizing column after cooling down；
(17) material is divided into gas-liquid two-phase in domethanizing column, and gas phase enters overhead condenser from demethanizer column overhead, warp
Condensation material enters demethanizer reflux tank, and return tank of top of the tower liquid phase material is pumped into demethanizer column overhead as reflux, return tank
Top produces gas phase low temperature methane, charging of the domethanizing column tower bottoms phase materials as ethylene rectifying column；
(18) it is distillated from the material that domethanizing column tower reactor is sent into ethylene rectifying column and is separated into two kinds of products, tower top is polymerization
Grade ethylene product, tower reactor is cycle ethane；
(19) cycle ethane vaporizes recycling cooling capacity at a lower temperature, and low-temperature gaseous phase ethane is answered after recycling cooling capacity in ice chest
Temperature to room temperature is sent to cracking unit, is then preheated as raw material into pyrolysis furnace.
As a kind of perferred technical scheme: using azeotrope refrigeration skill in the ethane cracking deep cooling process for separating
Art, for cryogenic separation cooling capacity is provided be three kinds or more the cryogen that mixes according to a certain percentage such as hydro carbons and nitrogen,
The proportion of the azeotrope is C1 10~20%, C2 15~20%, C3 20~30%, N220~30%.
As a kind of perferred technical scheme: the liquid phase ethane as raw material, into the vaporization process before pyrolysis furnace
It is all carried out in cryogenic separation unit, recycling vaporization potential reduces the energy consumption of refrigerant compressor.
As a kind of perferred technical scheme: the liquid phase of step (1) (4) condensation finally returns that the chilling of quenching unit
Water tower.
As a kind of perferred technical scheme: the charging of two Cutting Tap of carbon can be cooled to bubble point temperature into tower；Carbon
Two Cutting Taps flow back mainly from the low temperature liquid phase material of the return tank of dethanizer, and another part is from downstream deep cooling ice chest
Cryogenic liquid；When two Cutting Tap operating pressure of carbon is higher than dethanizer, two Cutting Tap tower reactor liquid phase material of carbon can be sent directly into
Dethanizer when two Cutting Tap operating pressure of carbon is lower than dethanizer, can guarantee tower reactor liquid phase object with dethanizer is pumped into
Material can smoothly enter into dethanizer.
As a kind of perferred technical scheme: the two Cutting Tap operating pressure of carbon is lower than dethanizer, dethanizer tower
The gas phase that the gaseous phase materials of top or return tank can cut at the top of column overhead or return tank with carbon two adds before entering acetylene after preheating
Hydrogen reactor.When overhead condenser, return tank and reflux pump, reflux the returning by oneself of two Cutting Tap of carbon is arranged in two Cutting Tap of carbon
Stream pump provides a part；When two Cutting Tap of carbon is not provided with overhead condenser, return tank and reflux pump, the reflux of two Cutting Tap of carbon is complete
It is provided entirely by the cryogenic liquid that deethanizer reflux tank cryogenic liquid and downstream ice chest generate.
As a kind of perferred technical scheme: described when dethanizer operating pressure cuts tower height than carbon two, deethanization
Column overhead condenser is partial condensation, and material point three parts after condensing in overhead condenser, liquid phase material is respectively that carbon two is cut
It cuts tower and dethanizer provides reflux, gas phase enters acetylene back end hydrogenation reactor through rewarming.When dethanizer operating pressure compares carbon
Two Cutting Taps are low, and complete condenser also can be set in deethanizer overhead, the extra liquid phase material of return tank by being pumped into low-temperature vaporization device,
Low-temperature gaseous phase material after vaporization merges with the low-temperature gaseous phase material of two Cutting Tap of carbon；Acetylene back end hydrogenation system is no longer arranged in downstream
It unites, wash green oil and third drying system.
As a kind of perferred technical scheme: described when light group of acetylene back end hydrogenation reactor outlet material methane, hydrogen etc.
Divide content higher, material removing green oil and moisture enter domethanizing column.When acetylene back end hydrogenation reactor outlet material methane, hydrogen
Etc. light components content it is lower when, material removing green oil and moisture ethylene distillation can be sent directly into according to the technique of ethylene rectifying column
Tower.
As a kind of perferred technical scheme: two Cutting Tap of carbon can be (pure with qualified low temperature ethane when driving
Degree >=99%) as reflux, the cryogenic liquid of deep cooling ice chest can also be used as supplement reflux and driven with reflux.
As a kind of perferred technical scheme: the demethanizer column overhead return tank low-temperature gaseous phase methane enters turbine expansion
Cooling capacity is provided for deep cooling ice chest after machine expansion cooling, can be used as regeneration gas use after rewarming.
Compared with prior art, the beneficial effects of the present invention are: present invention process method acetylene removal system is innovated
Optimization, the technique can reduce investment cost and operating cost.
Detailed description of the invention
Fig. 1 is a kind of system flow schematic diagram of ethane cracking deep cooling process for separating method of an embodiment of the present invention.
Specific embodiment
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments, is based on
Embodiment in the present invention, it is obtained by those of ordinary skill in the art without making creative efforts every other
Embodiment shall fall within the protection scope of the present invention.
Invention is described in further detail with reference to the accompanying drawing.
Fig. 1 schematically shows a kind of ethane cracking deep cooling process for separating method according to the present invention.
The invention discloses a kind of ethane cracking deep cooling process for separating methods, comprise the steps of
(1) (40 DEG C of temperature or so, pressure 40-90KPa) of cracking gas from chilling column overhead enter charge gas compressor
One section of suction tank, boosts to 1-3MPa through compressor；
(2) cracking gas uses multi-stage compression, cooling, lime set return chilling top of tower between compressor section between machine, compressor end
End check vent one's spleen (pressure 1-3MPa) cool to 40 DEG C or so, gaseous phase materials, which heat up, enters caustic wash tower after 3-5 DEG C；
(3) cracking gas for removing sour gas leaves caustic wash tower after the washing of caustic wash tower top washing section, changes into cryogen
Hot device, temperature are down to 10-15 DEG C；
(4) cracking gas after cooling down enters knockout drum, and lime set returns to tank between chilling top of tower or compressor section, gas phase
Into drier；
(5) cracking gas for removing moisture enters two Cutting Tap of carbon through cooling, and C2 or more component is condensed into liquid and flows to tower reactor,
C1 and some light-component gas are discharged from cutting column overhead；
(6) two Cutting Tap kettle material of carbon enters dethanizer, and deethanizer overhead condenser is fractional distilling tube, reflux
Tank material is divided into 3 strands, and first burst of reflux as dethanizer, second burst of two Cutting Tap of feeding carbon top is as reflux, reflux
Tank tank deck gaseous phase materials remove back end hydrogenation reactor through re-heat；
(7) dethanizer kettle material enters depropanizing tower, and C4 or more group liquid flows to tower reactor and produced by tower reactor, C3 group
Divide and be discharged from tower top, enter return tank after overhead condenser is cooling and separate, return tank C3 liquid returns stream, surplus liquid work
For the extraction of C3 product；
(8) depropanizing tower kettle material is sent into debutanizing tower, return tank of top of the tower extraction mixing four product of carbon, and tower reactor produces carbon
Five and heavy constituent；
(9) two Cutting Tap top gaseous phase of carbon enters ethylene front-end hydrogenation reactor after re-heat, removes the acetylene group in material
Point；
(10) ethylene front-end hydrogenation reactor outlet material enters the second drier removing micro-moisture after cooling down；
(11) second driers enter deep-cooling heat exchanger, the liquid phase object of the different temperatures condensed out after flowing out material cooling
Material respectively enters the different location of domethanizing column；
(12) the thick hydrogen of low temperature of 95% or more purity is isolated in deep-cooling heat exchanger end, and the thick hydrogen of low temperature flows through ice chest heat exchanger
Rewarming is to room temperature；
(13) the thick hydrogen of room temperature can enter the hydrogen product of methanation and 95% or more hydrogen dryer output purity；
(14) the thick hydrogen of room temperature obtains high purity hydrogen product after can entering PSA device pressure-variable adsorption；
(15) enter after the cooling of acetylene back end hydrogenation reactor outlet material and wash green oil tank, two material of carbon for removing green oil enters
Third drier；
(16) third dryer export material enters domethanizing column after cooling down；
(17) material is divided into gas-liquid two-phase in domethanizing column, and gas phase enters overhead condenser from demethanizer column overhead, warp
Condensation material enters demethanizer reflux tank, and return tank of top of the tower liquid phase material is pumped into demethanizer column overhead as reflux, return tank
Top produces gas phase low temperature methane, charging of the domethanizing column tower bottoms phase materials as ethylene rectifying column；
(18) it is distillated from the material that domethanizing column tower reactor is sent into ethylene rectifying column and is separated into two kinds of products, tower top is polymerization
Grade ethylene product, tower reactor is cycle ethane；
(19) cycle ethane vaporizes recycling cooling capacity at a lower temperature, and low-temperature gaseous phase ethane is answered after recycling cooling capacity in ice chest
Temperature to room temperature is sent to cracking unit, is then preheated as raw material into pyrolysis furnace.
In the present embodiment, azeotrope Refrigeration Technique is used in the ethane cracking deep cooling process for separating, for deep cooling point
From cooling capacity is provided be three kinds or more the cryogen that mixes according to a certain percentage such as hydro carbons and nitrogen, the azeotrope
Proportion be C1 10~20%, C2 15~20%, C3 20~30%, N2 20~30%.
In the present embodiment, the liquid phase ethane as raw material is all dividing in deep cooling into the vaporization process before pyrolysis furnace
It is carried out from unit, recycling vaporization potential reduces the energy consumption of refrigerant compressor.
In the present embodiment, the liquid phase of step (1) (4) condensation finally returns that the quenching water column of quenching unit.
In the present embodiment, the charging of two Cutting Tap of carbon can be cooled to bubble point temperature into tower；Two Cutting Tap of carbon returns
Flow the low temperature liquid phase material of the return tank mainly from dethanizer, cryogenic liquid of the another part from downstream deep cooling ice chest；
When two Cutting Tap operating pressure of carbon is higher than dethanizer, two Cutting Tap tower reactor liquid phase material of carbon can be sent directly into dethanizer,
When two Cutting Tap operating pressure of carbon is lower than dethanizer, can with dethanizer is pumped into, guarantee tower reactor liquid phase material smoothly into
Enter dethanizer.
In the present embodiment, the two Cutting Tap operating pressure of carbon is lower than dethanizer, deethanizer overhead or return tank
Gaseous phase materials the gas phase preheating at the top of column overhead or return tank can be cut with carbon two after enter ethylene front-end hydrogenation reactor.When
Overhead condenser, return tank and reflux pump is arranged in two Cutting Tap of carbon, and the reflux of two Cutting Tap of carbon provides one by the reflux pump of oneself
Part；When two Cutting Tap of carbon is not provided with overhead condenser, return tank and reflux pump, the reflux of two Cutting Tap of carbon is completely by deethanization
The cryogenic liquid that tower return tank cryogenic liquid and downstream ice chest generate provides.
In the present embodiment, described when dethanizer operating pressure cuts tower height than carbon two, deethanizer overhead condensation
Device is partial condensation, and material point three parts after condensing in overhead condenser, liquid phase material is respectively two Cutting Tap of carbon and de- second
Alkane tower provides reflux, and gas phase enters acetylene back end hydrogenation reactor through rewarming；When dethanizer operating pressure is lower than two Cutting Tap of carbon,
Complete condenser also can be set in deethanizer overhead, and the extra liquid phase material of return tank is low after vaporization by being pumped into low-temperature vaporization device
Wet phase materials merge with the low-temperature gaseous phase material of two Cutting Tap of carbon；Acetylene back end hydrogenation system is no longer arranged in downstream, wash green oil and
Third drying system.
In the present embodiment, the light components contents such as acetylene back end hydrogenation reactor outlet material methane, hydrogen of working as are higher,
Material removing green oil and moisture enter domethanizing column.When the light components such as acetylene back end hydrogenation reactor outlet material methane, hydrogen contain
When measuring lower, material removing green oil and moisture can be sent directly into ethylene rectifying column according to the technique of ethylene rectifying column.
In the present embodiment, two Cutting Tap of carbon can be made when driving with qualified low temperature ethane (purity >=99%)
For reflux, the cryogenic liquid of deep cooling ice chest can also be used as supplement reflux and driven with reflux.
In the present embodiment, the demethanizer column overhead return tank low-temperature gaseous phase methane enters turbo-expander expansion cooling
Cooling capacity is provided for deep cooling ice chest afterwards, can be used as regeneration gas use after rewarming.
(40 DEG C of temperature or so, pressure 30-90KPa) of cracking gas from chilling column overhead enter one section of charge gas compressor
Suction tank boosts to 1-3MPa through compressor, is sent after being cooled to 40 DEG C or so to caustic wash tower and removes acidic materials.Remove sour gas
The cracking gas of body through caustic wash tower top washing section washing after leave caustic wash tower, into cryogen heat exchanger, temperature be down to 10-15 DEG C into
Enter gas-liquid separator to separate completely the liquid to cool down, gas enters drying unit removing moisture, then enters carbon through cooling
Two Cutting Taps, at -60~-20 DEG C, C2 or more component is condensed into liquid and flows to tower reactor, C2 and light component gas overhead condensation temperature
Body is discharged from cutting column overhead；Two Cutting Tap kettle material of carbon enters dethanizer and continues rectifying, and overhead condensation temperature is -60
~-20 DEG C, return tank of top of the tower is entered after deethanizer overhead gas partial condensation, return tank material is divided into 3 strands, first burst of conduct
The reflux of dethanizer, as reflux, return tank tank deck gaseous phase materials go second through re-heat at second burst of two Cutting Tap of feeding carbon top
Alkynes back end hydrogenation reactor；
Described, pressure is 1~3MPa, and the dethanizer kettle material that temperature is 30~80 DEG C or so enters depropanizing tower essence
It evaporates, C4 or more component is condensed into liquid and flows to tower reactor, and C3 component is discharged from tower top, is cooled to 0~50 DEG C by overhead condenser
Enter return tank afterwards, return tank liquid material returns stream, and surplus liquid material is produced as three product of carbon；The dethanizer behaviour
Make two Cutting Tap of pressure ratio carbon it is low when, complete condenser also can be set in deethanizer overhead, and the extra liquid phase material of return tank is by pumping
Enter low-temperature vaporization device, the low-temperature gaseous phase material after vaporization merges with the low-temperature gaseous phase material of two Cutting Tap of carbon；Downstream is no longer arranged
Acetylene back end hydrogenation system washes green oil and third drying system.
Described, pressure is 0.6~1.5MPa, and temperature is that 50~110 DEG C of depropanizing tower kettle materials are sent into debutanizing tower, tower
Return tank extraction mixing four product of carbon is pushed up, tower reactor produces light dydrocarbon and heavy constituent；
Described, two Cutting Tap top gaseous phase of carbon enters ethylene front-end hydrogenation reactor after re-heat, removes the acetylene in material
Then component enters the second drier after cooling down and removes micro-moisture；Second drier outflow material is cooled to -90~-40
DEG C enter deep-cooling heat exchanger, the different temperatures liquid phase material condensed out respectively enters the different pelverized coal feeder positions of domethanizing column；It is deep
The thick hydrogen of low temperature of 95% or more purity is isolated in cold heat exchanger end, and the thick hydrogen of low temperature flows through ice chest heat exchanger rewarming to room temperature.
Described, when two Cutting Tap operating pressure of carbon is higher than dethanizer carbon, two Cutting Tap tower reactor liquid phase materials can be straight
It picks into dethanizer, guarantees that tower reactor liquid phase material can smoothly enter into dethanizer.When two Cutting Tap operating pressure of carbon is lower than de- second
When alkane tower, two Cutting Tap tower reactor liquid phase material of carbon can be with being pumped into dethanizer.Described, two Cutting Tap operating pressure of carbon is lower than
The gaseous phase materials of dethanizer, deethanizer overhead or return tank can cut the gas phase at the top of column overhead or return tank with carbon two
Enter ethylene front-end hydrogenation reactor after preheating.
Described, when two Cutting Tap of carbon is not provided with overhead condenser, return tank and reflux pump, the reflux of two Cutting Tap of carbon is complete
It is provided by the cryogenic liquid that deethanizer reflux tank cryogenic liquid and downstream ice chest generate.
Need the thick hydrogen of room temperature can be into methanation and the hydrogen of 95% or more hydrogen dryer output purity according to user
Product；High purity hydrogen product is obtained after PSA device pressure-variable adsorption can also being entered；
It is described, enter after the cooling of acetylene back end hydrogenation reactor outlet material and wash green oil tank, remove two material of carbon of green oil into
Enter third drier removing moisture, is then cooled to -90~-30 DEG C and enters domethanizing column；Material is divided into gas in domethanizing column
Liquid two-phase, gas phase enter overhead condenser from demethanizer column overhead, are condensed material and enter demethanizer reflux tank, overhead reflux
Tank liquid phase material is pumped into demethanizer column overhead as reflux, and return tank top produces gas phase low temperature methane, domethanizing column tower bottoms
Charging of the phase materials as ethylene rectifying column.Demethanizer column overhead return tank low-temperature gaseous phase methane enters turbo-expander expansion drop
Wen Houwei deep cooling ice chest provides cooling capacity, can be used as regeneration gas use after rewarming.
Described, pressure is 0.5~3.0MPa, and temperature is that -70~45 DEG C of domethanizing column tower reactor materials are sent into ethylene rectifying column,
The material for being sent into ethylene rectifying column, which is distillated, is separated into two kinds of products, tower top output polymer grade ethylene product, tower reactor extraction circulation
Ethane；
Described, cycle ethane vaporizes recycling cooling capacity at a lower temperature, after low-temperature gaseous phase ethane recycles cooling capacity in ice chest
Rewarming to room temperature is sent to cracking unit, is then preheated as raw material into pyrolysis furnace.
Described, the cooling capacity needed for the rectifying of cracking gas component gas and separation process is mentioned by azeotrope refrigeration system
For.
The present invention by with azeotrope replace ethylene, propylene cascade refrigeration deep cooling process for separating, meanwhile, acetylene removal
System and deethanization system have done innovation optimization, which can reduce investment cost and operating cost.
It is obvious to a person skilled in the art that invention is not limited to the details of the above exemplary embodiments, Er Qie
In the case where without departing substantially from spirit or essential attributes of the invention, the present invention can be realized in other specific forms.Therefore, no matter
From the point of view of which point, the present embodiments are to be considered as illustrative and not restrictive, and the scope of the present invention is by appended power
Benefit requires rather than above description limits, it is intended that all by what is fallen within the meaning and scope of the equivalent elements of the claims
Variation is included within the present invention.Any reference signs in the claims should not be construed as limiting the involved claims.
In addition, it should be understood that although this specification is described in terms of embodiments, but not each embodiment is only wrapped
Containing an independent technical solution, this description of the specification is merely for the sake of clarity, and those skilled in the art should
It considers the specification as a whole, the technical solutions in the various embodiments may also be suitably combined, forms those skilled in the art
The other embodiments being understood that.
Claims (10)
1. the invention discloses a kind of ethane cracking deep cooling process for separating methods, it is characterised in that successively comprise the steps of
(1) (40 DEG C of temperature or so, pressure 40-90KPa) of cracking gas from chilling column overhead enter one section of charge gas compressor
Suction tank boosts to 1-3MPa through compressor；
(2) cracking gas uses multi-stage compression, cools down between machine, lime set returns to chilling top of tower between compressor section, and compressor end is split
Vent one's spleen (pressure 1-3MPa) cool to 40 DEG C or so, gaseous phase materials, which heat up, enters caustic wash tower after 3-5 DEG C；
(3) cracking gas for removing sour gas leaves caustic wash tower after the washing of caustic wash tower top washing section, into cryogen heat exchanger,
Temperature is down to 10-15 DEG C；
(4) cracking gas after cooling down enters knockout drum, and lime set returns to tank between chilling top of tower or compressor section, and gas phase enters
Drier；
(5) cracking gas for removing moisture enters two Cutting Tap of carbon through cooling, and C2 or more component is condensed into liquid and flows to tower reactor, C1 and
Some light-component gas are discharged from cutting column overhead；
(6) two Cutting Tap kettle material of carbon enters dethanizer, and deethanizer overhead condenser is fractional distilling tube, return tank object
Material is divided into 3 strands, and first burst of reflux as dethanizer, second burst of two Cutting Tap of feeding carbon top is as reflux, return tank tank
Top gas phase materials remove back end hydrogenation reactor through re-heat；
(7) dethanizer kettle material enters depropanizing tower, and C4 or more group liquid flows to tower reactor and produced by tower reactor, C3 component from
Tower top discharge enters return tank after overhead condenser is cooling and separates, and return tank C3 liquid returns stream, and surplus liquid is as C3
Product extraction；
(8) depropanizing tower kettle material be sent into debutanizing tower, return tank of top of the tower extraction mixing four product of carbon, tower reactor produce light dydrocarbon and
Heavy constituent；
(9) two Cutting Tap top gaseous phase of carbon enters ethylene front-end hydrogenation reactor after re-heat, removes the acetylene component in material；
(10) ethylene front-end hydrogenation reactor outlet material enters the second drier removing micro-moisture after cooling down；
(11) second driers enter deep-cooling heat exchanger, the liquid phase material point of the different temperatures condensed out after flowing out material cooling
Not Jin Ru domethanizing column different location；
(12) the thick hydrogen of low temperature of 95% or more purity is isolated in deep-cooling heat exchanger end, and the thick hydrogen of low temperature flows through ice chest heat exchanger rewarming
To room temperature；
(13) the thick hydrogen of room temperature can enter the hydrogen product of methanation and 95% or more hydrogen dryer output purity；
(14) the thick hydrogen of room temperature obtains high purity hydrogen product after can entering PSA device pressure-variable adsorption；
(15) enter after the cooling of acetylene back end hydrogenation reactor outlet material and wash green oil tank, two material of carbon for removing green oil enters third
Drier；
(16) third dryer export material enters domethanizing column after cooling down；
(17) material is divided into gas-liquid two-phase in domethanizing column, and gas phase enters overhead condenser from demethanizer column overhead, through condensing
Material enters demethanizer reflux tank, and return tank of top of the tower liquid phase material is pumped into demethanizer column overhead as reflux, return tank top
Produce gas phase low temperature methane, charging of the domethanizing column tower bottoms phase materials as ethylene rectifying column；
(18) it is distillated from the material that domethanizing column tower reactor is sent into ethylene rectifying column and is separated into two kinds of products, tower top is polymer grade second
Alkene product, tower reactor are cycle ethane；
(19) cycle ethane vaporizes recycling cooling capacity at a lower temperature, and rewarming is extremely after low-temperature gaseous phase ethane recycles cooling capacity in ice chest
Room temperature is sent to cracking unit, is then preheated as raw material into pyrolysis furnace.
2. a kind of ethane cracking deep cooling process for separating method as described in claim 1, which is characterized in that the ethane cracking is deep
In cold separating technology use azeotrope Refrigeration Technique, for cryogenic separation cooling capacity is provided be three kinds or more hydro carbons and
The cryogen that nitrogen etc. mixes according to a certain percentage, the proportion of the azeotrope are C1 10~20%, C2 15~20%, C3
20~30%, N2 20~30%.
3. a kind of ethane cracking deep cooling process for separating method as described in claim 1, which is characterized in that described as raw material
Liquid phase ethane is all being carried out in cryogenic separation unit into the vaporization process before pyrolysis furnace, and recycling vaporization potential reduces cryogen compression
The energy consumption of machine.
4. a kind of ethane cracking deep cooling process for separating method as described in claim 1, which is characterized in that the step (1) (4)
The liquid phase of condensation finally returns that the quenching water column of quenching unit.
5. a kind of ethane cracking deep cooling process for separating method as described in claim 1, which is characterized in that two Cutting Tap of carbon
Charging can be cooled to bubble point temperature into tower；Two Cutting Tap of carbon flows back mainly from the low temperature liquid phase of the return tank of dethanizer
Material, cryogenic liquid of the another part from downstream deep cooling ice chest；When two Cutting Tap operating pressure of carbon is higher than dethanizer, carbon two
Cutting Tap tower reactor liquid phase material can be sent directly into dethanizer, can be with when two Cutting Tap operating pressure of carbon is lower than dethanizer
With dethanizer is pumped into, guarantee that tower reactor liquid phase material can smoothly enter into dethanizer.
6. a kind of ethane cracking deep cooling process for separating method as described in claim 1, which is characterized in that two Cutting Tap of carbon
Operating pressure is lower than dethanizer, and the gaseous phase materials of deethanizer overhead or return tank can cut column overhead or reflux with carbon two
Enter ethylene front-end hydrogenation reactor after the gas phase preheating of tank top.When overhead condenser, return tank is arranged in two Cutting Tap of carbon and returns
The reflux of stream pump, two Cutting Tap of carbon provides a part by the reflux pump of oneself；When two Cutting Tap of carbon be not provided with overhead condenser, return
Flow tank and reflux pump, the low temperature that the reflux of two Cutting Tap of carbon is generated by deethanizer reflux tank cryogenic liquid and downstream ice chest completely
Liquid provides.
7. a kind of ethane cracking deep cooling process for separating method as described in claim 1, which is characterized in that described to work as dethanizer
When operating pressure cuts tower height than carbon two, deethanizer overhead condenser is partial condensation, and material is through condensing in overhead condenser
After divide three parts, liquid phase material is respectively two Cutting Tap of carbon and dethanizer provides reflux, gas phase after rewarming enters acetylene plus
Hydrogen reactor；When dethanizer operating pressure is lower than two Cutting Tap of carbon, complete condenser, return tank is also can be set in deethanizer overhead
Extra liquid phase material is by being pumped into low-temperature vaporization device, the low-temperature gaseous phase material of low-temperature gaseous phase material and two Cutting Tap of carbon after vaporization
Merge；Downstream is no longer arranged acetylene back end hydrogenation system, washes green oil and third drying system.
8. a kind of ethane cracking deep cooling process for separating method as described in claim 1, which is characterized in that described to add after acetylene
The light components contents such as hydrogen reactor outlet material methane, hydrogen are higher, and material removing green oil and moisture enter domethanizing column.Work as second
When the light components contents such as alkynes back end hydrogenation reactor outlet material methane, hydrogen are lower, material removes green oil and moisture can basis
The technique of ethylene rectifying column is sent directly into ethylene rectifying column.
9. a kind of ethane cracking deep cooling process for separating method as described in claim 1, which is characterized in that two Cutting Tap of carbon
It can use qualified low temperature ethane (purity >=99%) as reflux when driving, can also be made with the cryogenic liquid of deep cooling ice chest
For supplement reflux and drive with reflux.
10. a kind of ethane cracking deep cooling process for separating method as described in claim 1, which is characterized in that the domethanizing column
Return tank of top of the tower low-temperature gaseous phase methane, which enters after turbo-expander expansion cooling, provides cooling capacity for deep cooling ice chest, can make after rewarming
For regeneration gas use.
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