CN107602324A - The method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique - Google Patents
The method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique Download PDFInfo
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Abstract
The present invention relates to a kind of method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique, mainly solve the problems, such as to exist in the prior art that utilization rate of equipment and installations is low, engineering investment cost is high, occupation area of equipment is big, light olefins output is low.A kind of method that the present invention couples by using dehydrogenating propane technique with naphtha pyrolysis predepropanization technique, the equipment of ethylene unit separative element is subjected to local capacity expansion revamping, the method that pyrolysis furnace and PDH reactors " two " and separative element " one " and 2 propylene towers " two tails " in parallel are set, in 80~1,200,000 tons/year of ethylene units and 600,000 tons/year of PDH devices, under the conditions of P/E=0.47~0.60, increasing output of ethylene 1.6%~2.4%, propylene enhancing 78%~119%, reduce investment 8.8%~9.0%, the technical scheme for reducing 1.8 hectares of floor space preferably solves above mentioned problem, in being coupled available for dehydrogenating propane technique with naphtha pyrolysis predepropanization technique.
Description
Technical field
The present invention relates to a kind of dehydrogenating propane PDH devices and naphtha steam thermal cracking predepropanization separating ethene device coupling
The method of conjunction；The existing equipment of ethylene unit predepropanization separation process is being leveraged fully on, and is keeping cracking stock combined feed not
On the premise of change, realize that PDH devices couple with ethylene unit, equipment investment is reduced with this, reduces construction land, raising low-carbon alkene
Hydrocarbon yield, it can be applied in the industrial production of production low-carbon alkene.
Background technology
Ethene and propylene are important basic petrochemical raw materials.Ethylene unit is main to prepare ethene, propylene at present
Deng low-carbon alkene product, the leading industrial installation of ethylene product, compared with ethylene unit, PDH device energy are especially prepared
Enough produce more propylene products.
Ethylene unit and PDH devices require and ethene are filled to produce qualified ethene, propylene, mixing carbon fourth class product
Put cracking gas and PDH device reactions gas carries out separation and purification.Therefore, the ethylene unit of predepropanization technique and PDH devices are existed
Separation process part carries out integrated coupling, and keeping, ethylene unit cracking stock is constant, takes off third before leveraging fully on ethylene unit
The existing equipment of alkane separation process and on the premise of carrying out local capacity expansion revamping, can effectively increase propylene yield, be one
Feasible prepares low-carbon alkene production line.
At present, preparing propylene by dehydrogenating propane patented technology has in the world：The Catofin techniques of ABB Lummus companies, UOP are public
The Oleflex techniques of department, the Star techniques of Uhde companies, the FBD-4 techniques of Snamprogetti/Yarsintz companies and woods
The PDH techniques of moral/BASF AG.These techniques are generally using deep cooling process for separating come refined purification preparing propylene by dehydrogenating propane
Reaction product.Meanwhile deep cooling process for separating is also the main method of naphtha steam cracking product separation and purification.Therefore, deep cooling
Separating technology have the advantages that technology maturation, be widely used, material recovery rate it is high.But the process operation temperatures of cryogenic separation compared with
It is low, higher is required to equipment material, thus engineering construction investment is also big.Predepropanization technique and PDH separating technologies are carried out
Coupling, the existing equipment of ethylene unit predepropanization separation process is leveraged fully on, only the equipment of existing separative element is carried out
Local capacity expansion revamping, engineering construction investment can be substantially reduced.
PDH application is more and more in recent years, such as a kind of preparation methods of propylene of patent publication No. CN103664455A, specially
The separation method of sharp publication number CN106316761A preparing propylene by dehydrogenating propane reaction products, patent publication No. CN105152840A mono-
The process for refining of kind C_4 hydrocarbon logistics, all discloses the method that PDH techniques prepare propylene.
In the prior art, patent publication No. CN103664455A and patent publication No. CN106316761A and patent disclose
Although number CN105152840A discloses the method that PDH techniques prepare propylene, but there is not yet before PDH techniques and naphtha pyrolysis
The report of depropanization technique coupling.Equipment be present using the conventional process techniques route of setting ethylene unit and PDH devices respectively
The problems such as construction investment is high, floor space is big, light olefins output is low.
The content of the invention
The technical problems to be solved by the invention be exist in the prior art utilization rate of equipment and installations is low, engineering investment cost is high,
The problem of occupation area of equipment is big, light olefins output is low, there is provided a kind of new dehydrogenating propane technique before naphtha pyrolysis with taking off
The method of propane technique coupling, there is utilization rate of equipment and installations height, engineering investment cost is low, occupation area of equipment is small, low-carbon alkene production
Measure the advantages of high.
To solve the above problems, the technical solution adopted by the present invention is as follows：A kind of dehydrogenating propane technique and naphtha pyrolysis
The method of predepropanization technique coupling, on the premise of keeping ethylene unit cracking stock constant, wherein, (1) dehydrogenating propane PDH
Device：Fresh propane feeds mixed with the tower top lime set charging from the charging of propylene rectification tower bottom of towe recycled propane and de-oiling tower
Close, gasified into propane gasification tank, dehydrogenation reactor system is delivered to after phase propane is heated and carries out dehydrogenation reaction, generation is anti-
Product propylene is answered, reaction product delivers to ethylene cracking gas suction port of compressor after cooling, and the liquid of propane gasification tank is delivered to
De-oiling tower, de-oiling column overhead lime set remove propane gasification tank, and dehydrogenation reactor system reaction is sent into de-oiling tower tower reactor logistics after cooling
Device charging heating furnace is used as supplement fuel；(2) ethylene unit：Naphtha pyrolysis raw material enters ethylene unit cracking unit and split
Solution reaction generation cracking gas, after over-quenching with PDH come reactor product gas together with compressed, alkali cleaning, dry after enter ethene
Device predepropanization separative element, the C4 isolated by high pressure depropanizer and low pressure depropanizer and more than C4 restructuring dispensings
Enter ethylene unit debutanizing tower, finally give mixing C4 products；The C3 and below C3 light components of high and low pressure depropanizer unit outflow
Ethene, propylene product are finally given through ethylene unit demethanation, deethanization, ethylene distillation, propylene rectification cell.
In above-mentioned technical proposal, it is preferable that dehydrogenating propane PDH devices set PDH reaction members and propylene rectification cell.
In above-mentioned technical proposal, it is preferable that the ethane isolated is back to ethylene unit cracking unit, and propane is back to
PDH device propane gasification tanks.
In above-mentioned technical proposal, it is preferable that PDH device reactions product gas and ethylene cracking gas difference are reacted, anxious
After cold, two strands of materials merge be compressed together, alkali cleaning, drying, ethylene cracking gas shares with PDH device reaction product gas
A set of high and low pressure depropanizer, demethanation, deethanization, debutanization, ethylene distillation, ethene freezing, propylene refrigeration system.
In above-mentioned technical proposal, it is preferable that ethylene unit nominal capacity is 80~1,200,000 tons/year, and cracking selectivity is：
Propylene/ethylene=0.47~0.60.
In above-mentioned technical proposal, it is preferable that PDH devices nominal capacity is 600,000 tons/year.
In above-mentioned technical proposal, it is preferable that PDH device reaction products are sent to meeting behind ethylene cracking gas suction port of compressor
Cause ethylene unit compression, alkali cleaning, drying and separative element excess load, load designs meet 140%~180% to be former, second
The equipment of alkene device separative element needs to carry out local capacity expansion revamping.
The present invention relates to a kind of method that PDH techniques couple with naphtha pyrolysis predepropanization technique.Keeping cracking former
On the premise of expecting that combined feed is constant, rely on ethylene unit existing equipment simultaneously to carry out local capacity expansion revamping, set ethane cracking furnace and
PDH reactors " two " and the separative element " one " and the simultaneously method of di- platform propylene rectification tower " two tails " of technique coupling,
It thereby simplify PDH device technique flows.For 80~1,200,000 tons/year of ethylene units and 600,000 tons/year of PDH devices,
Under the conditions of cracking selective P/E=0.47~0.60, compared with ethylene unit, increasing output of ethylene 1.6%~2.4%, propylene enhancing
78%~119%；Compared with ethylene unit and PDH devices are set respectively, investment 8.8%~9.0% can be reduced, reduces occupation of land face
1.8 hectares or so of product；Achieve preferable technique effect.
Brief description of the drawings
Fig. 1 is the flow signal after the PDH devices of the present invention couple with the ethylene unit technique of predepropanization separation process
Figure.In Fig. 1,100 be naphtha, and 101 be pyrolysis furnace, and 102 be quenching unit, and 103 be compression and caustic wash unit, and 104 be high pressure
Depropanizing tower, 105 be demethanation system, and 106 be dethanizer, and 107 be ethylene rectifying column, and 201 be low pressure depropanizer, 202
It is that propylene rectification tower 1,204 is propylene rectification tower 2 for debutanizing tower, 203；300 be fresh propane, and 301 be propane gasification tank,
302 be heating furnace and reactor, and 303 be de-oiling tower.
Wherein：(1) ethylene unit：Cracking stock naphtha 100 enters pyrolysis furnace 101, and naphtha 100 is in pyrolysis furnace 101
Middle generation cracking reaction generation hydrocarbon cracking gas logistics 1 is simultaneously sent to quenching unit 102.Cracking gas is isolated after chilling, washing
Heavy hydrocarbon, remaining cracking gas logistics 2 are sent to compression caustic wash unit 103.(2) PDH devices：Fresh propane 300 and propylene rectification tower tower
The recycled propane logistics 23 that the recycled propane logistics 19 and PDH de-oilings column overhead that kettle comes out come out is combined into propane gasification tank
301 are gasified, and the propylene oxide stream 20 after gasification enters PDH unit furnaces and the progress dehydrogenating propane of reactor unit 302 is anti-
Should, reacted reactor product gas logistics 21 enters jointly after converging with the cracking gas logistics 2 after ethylene unit chilling for logistics 3
The compression of ethylene unit and caustic wash unit 103.(3) ethene and PDH coupling devices：Before ethylene unit separative element of the present invention uses
The logistics 3 that depropanization technological process, ethylene cracking gas 2 and PDH device products gas 21 converge is entered in compression caustic wash unit 103
It is logistics 4 after capable compression, alkali cleaning, drying, is sent to depropanization unit 104 first.Logistics 4 enters high pressure depropanizer 104, at this
The tower top of tower 104 isolates H2, C1, C2, C3 logistics 5, is sent to domethanizing column 105 and further separates.The tower of high pressure depropanizer 104
Kettle isolates C3, C4 and more heavy constituent logistics 6, is sent to the separation that low pressure depropanizer 201 carries out next step.Logistics 6 enters low
C3 logistics 13 is isolated in tower top be sent to propylene rectification tower 203 and 204 after pressure depropanizing tower 201.The tower reactor of low pressure depropanizer 201
Isolate C4 and C4 more heavy constituent logistics 15 and be sent to debutanizing tower 202.After the rectifying of debutanization system 202 separation logistics 15, tower top
Logistics 16 is that final products mix C4, and tower reactor logistics 17 more reassembles into for C5 and C5 is incorporated to the submitting of drippolene product.Demethanation
System and cryogenic system 105 separate logistics 5, isolate methane hydrogen logistics 7 and include all C1 and more light component, remaining logistics is C2
And C3 logistics 7, it is sent to deethanization unit 106.Dethanizer 106 separates logistics 8, the tower top of dethanizer 106 outflow C2 component things
Stream 9 is sent to ethylene rectifying column 107.The tower reactor of dethanizer 106 outflow C3 components 12 are sent to third after merging into logistics 14 with logistics 13
Alkene rectifying column 203 and 204.Ethylene distillation system 107 separates logistics 9, and tower top obtains ethene production after the separation of ethylene rectifying column 107
Product logistics 10, tower reactor obtain ethane product logistics 11.(4) ethylene unit and PDH device propylene distillation systems：Due to ethylene unit
After being coupled with PDH devices, C3 Load liftings are larger, it is necessary to set up 1 set of new propylene rectification tower, and logistics 14 is further separated into propylene essence
Tower 203 and propylene rectification tower 204 are evaporated, propylene is respectively obtained on 2 propylene rectification tower tops and is converged for the propylene product of logistics 18,2
Individual propylene rectification tower kettle is obtained converging after propane as logistics 19, and PDH device propane gasification tank 301 is recycled back into as propane feed
Entrance.
Below by embodiment, the invention will be further elaborated, but is not limited only to the present embodiment.
Embodiment
【Comparative example 1】
Ethylene unit of the prior art uses predepropanization separating technology flow, 800,000 tons/year of nominal capacity, cracking choosing
Selecting property P/E=0.59, produce polymer grade ethylene >=99.95wt%, 80.00 ten thousand tons/year of ethylene yield；Production polymerization-grade propylene >=
99.6wt%, 47.20 ten thousand tons/year of propylene yield.Under conditions of ethylene unit and PDH devices are set respectively, engineering construction is thrown
Provide 66.03 hundred million yuans.
【Embodiment 1】
It is to be solved to be the present invention relates to a kind of method that PDH techniques couple with naphtha pyrolysis predepropanization technique
The technical problems such as utilization rate of equipment and installations is poor, engineering investment cost is high, floor space is big, light olefins output is low be present in prior art,
A kind of brand-new PDH devices and ethylene unit separation of olefins integral process flow are provided.Separated in ethylene unit predepropanization
On the basis of flow, 1 PDH device reactions system and the piece-rate system of carbon three are only increased newly, you can with predepropanization separation process
Ethylene unit carry out the height coupling of integration, be combined as the new coupling process of " the two first tails of body two ", this method has
Technological process is simple, equipment investment is few, floor space is small, can increasing output of ethylene propylene the advantages that.
The technical solution adopted by the present invention is as follows：
PDH devices：Fresh propane charging fills with the recycled propane charging from propylene rectification tower tower reactor and from PDH first
Put the top pronane product mix of de-oiling tower；Then the mixed material enters reactor feed gasification tank, passes through thermal siphon reboiling
Device is gasified using propylene refrigerant to the reactor feed in reactor feed gasification tank；Total reactor charging after gasification
Reactor is sent into after being heated to reaction temperature into heating furnace.Propane is converted by fixed catalyst bed in PDH reactors
For propylene.Reactor product gas delivers to ethylene device compressor entrance after cooling.The liquid of feed vaporization tank is delivered to de-oiling tower and entered
The rectifying of row material separates.In de-oiling tower, propane is separated from tower top and is sent into reactor feed gasification tank, by propane
Butane and more heavy constituent remove from tower reactor, are sent into reactor feed heating furnace after cooling and are used as supplement fuel.
Ethylene unit：Using predepropanization separation process, the constant condition of ethylene unit cracking stock combined feed is being kept
Under, after PDH device reaction product gas is sent to ethylene unit, now the compression unit of ethylene unit, separative element all excess loads are grasped
Make.According to the different production scale of ethylene unit, the substantially original ethylene unit of these unit loads 170.91%, it is necessary to will
The equipment of separative element carries out local capacity expansion revamping.Naphtha pyrolysis raw material enters ethylene unit cracking unit and cracking reaction occurs
Cracking gas is generated, after quenching unit cooling down, compressed, alkali cleaning, drying are laggard together with the reactor product gas next with PDH
Enter ethylene unit predepropanization separative element.C4 and more than the C4 weight isolated by high pressure depropanizer and low pressure depropanizer
Component is sent into ethylene unit debutanizing tower, finally gives mixing C4 products；The C3 and below C3 of high and low pressure depropanizer unit outflow
Light component finally gives methane hydrogen, ethene, third through units such as ethylene unit demethanation, deethanization, ethylene distillation, propylene rectifying
The products such as alkene, ethane, propane, propane return to PDH devices as reaction raw materials.
In the above-mentioned technical solutions, after PDH device reactions product gas and ethylene cracking gas distinguish reacted, chilling, 2
Stock material merge be compressed together, alkali cleaning, drying, ethylene cracking gas shares a set of high with PDH device reaction product gas
Low pressure depropanization, demethanation, deethanization, debutanization, ethylene distillation, ethene freezing, propylene refrigeration system.Whole integrated process
Cracking stock combined feed with merge before existing ethylene unit cracking stock combined feed it is suitable, but these unit loads are substantially
For the 170.91% of original ethylene unit.PDH devices are cancelled compared with single PDH devices before merging in whole integrated process
The systems such as the compressions of PDH devices, alkali cleaning, drying, depropanization, demethanation, deethanization, ethene freezing, propylene freezing, Jin Jinshe
PDH reaction members and propylene rectification cell are put, the equipment investment of PDH devices is thus greatlyd save, decreases construction land.
Table 1 is coupling technique flow PDH appliance arrangement lists.
Table 1 uses coupling process PDH device capital equipment lists
Ethylene unit involved in the present invention uses predepropanization separating technology flow, 800,000 tons/year of nominal capacity, cracking
Selective P/E=0.59；600,000 tons/year of PDH devices nominal capacity.Using before PDH techniques of the present invention and naphtha pyrolysis de- third
The method of alkane technique coupling：(1) ethylene unit：Cracking stock naphtha enters pyrolysis furnace, and naphtha splits in pyrolysis furnace
Solution reaction generation hydrocarbon cracking gas logistics 1 is simultaneously sent to quenching unit.Cracking gas isolates heavy hydrocarbon, remaining splits after chilling, washing
Cracked gas stream 2 is sent to compression caustic wash unit.(2) PDH devices：The recycled propane thing that fresh propane comes out with propylene rectification tower tower reactor
The recycled propane logistics 23 that 19 and PDH de-oilings column overhead comes out is flowed, three bursts of logistics are gasified into propane gasification tank jointly,
Propylene oxide stream 20 after gasification enters PDH unit furnaces and reactor unit carries out dehydrogenating propane reaction, reacted reaction
Product gas logistics 21 enters the compression of ethylene unit jointly for logistics 3 after converging with the cracking gas logistics 2 after ethylene unit chilling
And caustic wash unit.(3) ethene and PDH coupling devices：Ethylene unit separative element of the present invention uses the technological process of predepropanization,
The logistics 3 that ethylene cracking gas and PDH device product gas converge compression caustic wash unit be compressed, alkali cleaning, dry after be
Logistics 4, depropanization unit is sent to first.Logistics 4 enters high pressure depropanizer, and H2, C1, C2, C3 thing are isolated in the column overhead
Stream 5, is sent to domethanizing column and further separates.High pressure depropanizer kettle isolates C3, C4 and more heavy constituent logistics 6, is sent to low
Depropanizing tower is pressed to carry out the separation of next step.C3 logistics 13 is isolated in tower top be sent to third after the entrance low pressure depropanizer of logistics 6
Alkene rectifying column.Low pressure depropanizer tower reactor isolates C4 and C4 more heavy constituent logistics 15 and is sent to debutanizing tower.Debutanization system essence
After cut is from logistics 15, overhead stream 16 is that final products mix C4, and tower reactor logistics 17 more reassembles into for C5 and C5 and is incorporated to cracking
Gasoline products are sent out.Demethanation system and cryogenic system separation logistics 5, isolate methane hydrogen logistics 7 and include all C1 and lighter
Component, remaining logistics are C2 and C3 logistics 7, are sent to deethanization unit.Dethanizer separates logistics 8, and deethanizer overhead stream goes out
C2 component streams 9 are sent to ethylene rectifying column.Dethanizer tower reactor flows out C3 components, and third is sent to after merging into logistics 14 with logistics 13
Alkene rectifying column.Ethylene distillation system separates logistics 9, and tower top obtains ethylene product stream 10, tower reactor after ethylene rectifying column separates
Obtain ethane product logistics 11.(4) ethylene unit and PDH device propylene distillation systems：Because ethylene unit and PDH devices couple
Afterwards, C3 Load liftings are larger, it is necessary to set up 1 set of new propylene rectification tower, and logistics 14 is further separated into propylene rectification tower 203 and propylene
Rectifying column 204, propylene is respectively obtained on 2 propylene rectification tower tops and is converged for the propylene product of logistics 18, in two propylene rectification towers
Kettle is obtained converging after propane as logistics 19, and PDH device propane gasification tank entrances are recycled back into as propane feed.Using the present invention
Technique coupling process, existing ethylene unit equipment lifting load, see the table below 2.
The existing ethylene unit equipment lifting Load lifting list of table 2
Thus, using the present invention technique coupling process, with【Comparative example 1】Existing ethylene unit is compared, ethylene unit and
After the coupling of PDH device techniques, polymer grade ethylene >=99.95wt%, 81.97 ten thousand tons/year of ethylene yield, increment are produced
2.462%；Produce polymerization-grade propylene >=99.6wt%, 103.47 ten thousand tons/year of propylene yield, increment 119.216%；With【Compare
Example 1】Ethylene unit sets and compared respectively with PDH devices, after ethylene unit and the coupling of PDH device techniques, engineering construction investment
60.08 hundred million yuans, 5.96 hundred million yuans of investment reduction, equivalent to 9.019% investment is saved, reduce floor space 1.8
Hectare.
【Comparative example 2】
Ethylene unit of the prior art uses predepropanization separating technology flow, 1,000,000 tons/year of nominal capacity, cracking
Selective P/E=0.59, produce polymer grade ethylene >=99.95wt%, 100.00 ten thousand tons/year of ethylene yield；Produce polymer grade third
Alkene >=99.6wt%, 59.00 ten thousand tons/year of propylene yield.Under conditions of ethylene unit and PDH devices are set respectively, engineering is built
If 72.79 hundred million yuans of investment.
【Embodiment 2】
Together【Embodiment 1】, ethylene unit involved in the present invention uses predepropanization separating technology flow, nominal capacity
1000000 tons/year, crack selective P/E=0.59；600,000 tons/year of PDH devices nominal capacity.Coupled using the technique of the present invention
Method, existing ethylene unit equipment lifting load, see the table below 3.
The existing ethylene unit equipment lifting Load lifting list of table 3
Thus, using the present invention technique coupling process, with【Comparative example 2】Existing ethylene unit is compared, ethylene unit and
After the coupling of PDH device techniques, polymer grade ethylene >=99.95wt%, 101.97 ten thousand tons/year of ethylene yield, increment are produced
1.970%；Produce polymerization-grade propylene >=99.6wt%, 115.27 ten thousand tons/year of propylene yield, increment 95.373%；With【Comparative example
2】Ethylene unit sets and compared respectively with PDH devices, after ethylene unit and the coupling of PDH device techniques, engineering construction investment
66.36 hundred million yuans, 6.44 hundred million yuans of investment reduction, equivalent to 8.841% investment is saved, reduce floor space 1.8
Hectare.
【Comparative example 3】
Ethylene unit of the prior art uses predepropanization separating technology flow, 1,100,000 tons/year of nominal capacity, cracking
Selective P/E=0.59, produce polymer grade ethylene >=99.95wt%, 110.00 ten thousand tons/year of ethylene yield；Produce polymer grade third
Alkene >=99.6wt%, 64.90 ten thousand tons/year of propylene yield.Under conditions of ethylene unit and PDH devices are set respectively, engineering is built
If 75.63 hundred million yuans of investment.
【Embodiment 3】
Together【Embodiment 1】, ethylene unit involved in the present invention uses predepropanization separating technology flow, nominal capacity
1100000 tons/year, crack selective P/E=0.59；600,000 tons/year of PDH devices nominal capacity.Coupled using the technique of the present invention
Method, existing ethylene unit equipment lifting load, see the table below 4.
The existing ethylene unit equipment lifting Load lifting list of table 4
Thus, using the present invention technique coupling process, with【Comparative example 3】Existing ethylene unit is compared, ethylene unit and
After the coupling of PDH device techniques, polymer grade ethylene >=99.95wt%, 111.97 ten thousand tons/year of ethylene yield, increment are produced
1.791%；Produce polymerization-grade propylene >=99.6wt%, 121.17 ten thousand tons/year of propylene yield, increment 86.703%；With【Comparative example
3】Ethylene unit sets and compared respectively with PDH devices, after ethylene unit and the coupling of PDH device techniques, engineering construction investment
68.91 hundred million yuans, 6.72 hundred million yuans of investment reduction, equivalent to 8.889% investment is saved, reduce floor space 1.8
Hectare.
【Comparative example 4】
Ethylene unit of the prior art uses predepropanization separating technology flow, 1,200,000 tons/year of nominal capacity, cracking
Selective P/E=0.59, produce polymer grade ethylene >=99.95wt%, 120.00 ten thousand tons/year of ethylene yield；Produce polymer grade third
Alkene >=99.6wt%, 70.80 ten thousand tons/year of propylene yield.Under conditions of ethylene unit and PDH devices are set respectively, engineering is built
If 78.10 hundred million yuans of investment.
【Embodiment 4】
Together【Embodiment 1】, ethylene unit involved in the present invention uses predepropanization separating technology flow, nominal capacity
1200000 tons/year, crack selective P/E=0.59；600,000 tons/year of PDH devices nominal capacity.Coupled using the technique of the present invention
Method, existing ethylene unit equipment lifting load, see the table below 5.
The existing ethylene unit equipment lifting Load lifting list of table 5
Thus, using the present invention technique coupling process, with【Comparative example 4】Existing ethylene unit is compared, ethylene unit and
After the coupling of PDH device techniques, polymer grade ethylene >=99.95wt%, 121.97 ten thousand tons/year of ethylene yield, increment are produced
1.642%；Produce polymerization-grade propylene >=99.6wt%, 127.07 ten thousand tons/year of propylene yield, increment 79.477%；With【Comparative example
4】Ethylene unit sets and compared respectively with PDH devices, after ethylene unit and the coupling of PDH device techniques, engineering construction investment
71.08 hundred million yuans, 7.03 hundred million yuans of investment reduction, equivalent to 8.999% investment is saved, reduce floor space 1.8
Hectare.
【Embodiment 5】
Together【Embodiment 4】, ethylene unit involved in the present invention uses predepropanization separating technology flow, nominal capacity
1200000 tons/year, crack selective P/E=0.47；600,000 tons/year of PDH devices nominal capacity.Thus, using the technique of the present invention
Coupling process, with【Comparative example 4】Existing ethylene unit is compared, and after ethylene unit and the coupling of PDH device techniques, produces polymer grade
Ethene >=99.95wt%, 121.97 ten thousand tons/year of ethylene yield, increment 1.642%；Produce polymerization-grade propylene >=99.6wt%, third
112.67 ten thousand tons/year of alkene yield, increment 99.770%.
【Embodiment 6】
Together【Embodiment 4】, ethylene unit involved in the present invention uses predepropanization separating technology flow, nominal capacity
1200000 tons/year, crack selective P/E=0.60；600,000 tons/year of PDH devices nominal capacity.Thus, using the technique of the present invention
Coupling process, with【Comparative example 4】Existing ethylene unit is compared, and after ethylene unit and the coupling of PDH device techniques, produces polymer grade
Ethene >=99.95wt%, 121.97 ten thousand tons/year of ethylene yield, increment 1.642%；Produce polymerization-grade propylene >=99.6wt%, third
128.27 ten thousand tons/year of alkene yield, increment 78.153%.
Obviously, using the method for the present invention, for 80~1,200,000 tons/year of ethylene units and 600,000 tons/year of PDH devices, P/
Under the conditions of E=0.47~0.60, increasing output of ethylene 1.6%~2.4%, propylene enhancing 78%~119%, reduction investment 8.8%~
9.0%, 1.8 hectares of floor space is reduced, achieves preferable technology and economic effect.
Claims (7)
1. a kind of method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique, keeping, ethylene unit cracking is former
Expect it is constant on the premise of, wherein, (1) dehydrogenating propane PDH devices：Fresh propane is fed with circulating third from propylene rectification tower bottom of towe
Alkane is fed and the charging mixing of the tower top lime set of de-oiling tower, is gasified into propane gasification tank, is sent after phase propane is heated
Dehydrogenation reaction, reaction of formation product propylene are carried out to dehydrogenation reactor system, reaction product delivers to ethylene unit cracking after cooling
Air compressor entrance, the liquid of propane gasification tank deliver to de-oiling tower, and de-oiling column overhead lime set goes propane gasification tank, de-oiling tower tower reactor
Logistics is sent into dehydrogenation reactor system reactor feed heating furnace and is used as supplement fuel after cooling；(2) ethylene unit：Naphtha splits
Solve raw material and enter ethylene unit cracking unit generation cracking reaction generation cracking gas, the reactor product come after over-quenching with PDH
Gas is compressed together, alkali cleaning, dry after enter ethylene unit predepropanization separative element, taken off by high pressure depropanizer and low pressure
C4 and more than the C4 restructuring that propane tower is isolated are distributed into ethylene unit debutanizing tower, finally give mixing C4 products；High-low pressure
The C3 and below C3 light components of depropanization unit outflow are through ethylene unit demethanation, deethanization, ethylene distillation, propylene rectification cell
Finally give ethene, propylene product.
2. the method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique according to claim 1, its feature
It is that dehydrogenating propane PDH devices set PDH reaction members and propylene rectification cell.
3. the method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique according to claim 1, its feature
The ethane for being to isolate is back to ethylene unit cracking unit, and propane is back to PDH device propane gasification tanks.
4. the method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique according to claim 1, its feature
After being PDH device reactions product gas and the reacted, chilling of ethylene cracking gas difference, two strands of materials merge is pressed together
Contracting, alkali cleaning, drying, ethylene cracking gas share a set of high and low pressure depropanizer, demethanation with PDH device reaction product gas, taken off
Ethane, debutanization, ethylene distillation, ethene freezing, propylene refrigeration system.
5. the method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique according to claim 1, its feature
It is 80~1,200,000 tons/year to be ethylene unit nominal capacity, and cracking selectivity is：Propylene/ethylene=0.47~0.60.
6. the method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique according to claim 1, its feature
It is 600,000 tons/year to be PDH devices nominal capacity.
7. the method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique according to claim 1, its feature
It is that PDH device reaction products can cause ethylene unit compression, alkali cleaning, drying after being sent to ethylene cracking gas suction port of compressor
With separative element excess load, load meet for former design 140%~180%, the equipment of ethylene unit separative element need into
The local capacity expansion revamping of row.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109503309A (en) * | 2018-12-10 | 2019-03-22 | 中石化上海工程有限公司 | The method that light hydrocarbon cracking predepropanization technique is coupled with MTO technique |
| CN109651038A (en) * | 2018-12-10 | 2019-04-19 | 中石化上海工程有限公司 | The method that MTO technique is coupled with dehydrogenating propane technique |
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| CN109851460A (en) * | 2019-01-21 | 2019-06-07 | 中石化上海工程有限公司 | Naphtha pyrolysis sequentially separates the method coupled with PDH technique |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102795956A (en) * | 2012-08-30 | 2012-11-28 | 惠生工程（中国）有限公司 | Method for separating reaction products produced during preparation of propylene by dehydrogenating propane |
| CN104151121A (en) * | 2014-08-13 | 2014-11-19 | 中石化上海工程有限公司 | Method for coupling MTO (Methanol to Olefins) process with naphtha cracking front-end depropanization process |
| WO2016093558A1 (en) * | 2014-12-11 | 2016-06-16 | 에스케이가스 주식회사 | Method for separating propylene from dehydrogenation reaction products of propane-containing feedstock |
| CN107056568A (en) * | 2017-05-10 | 2017-08-18 | 中石化上海工程有限公司 | The method that MTO techniques are coupled with naphtha and Deposition During Propane Pyrolysis predepropanization technique |
| CN107056575A (en) * | 2017-05-10 | 2017-08-18 | 中石化上海工程有限公司 | The method that MTO techniques are coupled with naphtha and Deposition During Propane Pyrolysis front-end deethanization technique |
-
2017
- 2017-10-11 CN CN201710939558.XA patent/CN107602324A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102795956A (en) * | 2012-08-30 | 2012-11-28 | 惠生工程（中国）有限公司 | Method for separating reaction products produced during preparation of propylene by dehydrogenating propane |
| CN104151121A (en) * | 2014-08-13 | 2014-11-19 | 中石化上海工程有限公司 | Method for coupling MTO (Methanol to Olefins) process with naphtha cracking front-end depropanization process |
| WO2016093558A1 (en) * | 2014-12-11 | 2016-06-16 | 에스케이가스 주식회사 | Method for separating propylene from dehydrogenation reaction products of propane-containing feedstock |
| CN107056568A (en) * | 2017-05-10 | 2017-08-18 | 中石化上海工程有限公司 | The method that MTO techniques are coupled with naphtha and Deposition During Propane Pyrolysis predepropanization technique |
| CN107056575A (en) * | 2017-05-10 | 2017-08-18 | 中石化上海工程有限公司 | The method that MTO techniques are coupled with naphtha and Deposition During Propane Pyrolysis front-end deethanization technique |
Non-Patent Citations (1)
| Title |
|---|
| 许晨等: "丙烷脱氢装置经济性分析", 《当代石油化工》 * |
Cited By (14)
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| CN109851461A (en) * | 2019-01-21 | 2019-06-07 | 中石化上海工程有限公司 | The method that naphtha and Deposition During Propane Pyrolysis front-end deethanization are coupled with PDH |
| CN109851460A (en) * | 2019-01-21 | 2019-06-07 | 中石化上海工程有限公司 | Naphtha pyrolysis sequentially separates the method coupled with PDH technique |
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| CN111875466B (en) * | 2020-07-08 | 2022-10-14 | 中国石油化工股份有限公司 | Coupling method of depropanization process before hydrocarbon steam cracking and propane dehydrogenation process |
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