CN107602323A - The method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique - Google Patents
The method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique Download PDFInfo
- Publication number
- CN107602323A CN107602323A CN201710939515.1A CN201710939515A CN107602323A CN 107602323 A CN107602323 A CN 107602323A CN 201710939515 A CN201710939515 A CN 201710939515A CN 107602323 A CN107602323 A CN 107602323A
- Authority
- CN
- China
- Prior art keywords
- propane
- ethylene
- technique
- propylene
- light hydrocarbon
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a kind of method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique, mainly solve the problems, such as to exist in the prior art that unreasonable products structure, engineering investment cost are high, occupation area of equipment is big, low-carbon alkene especially propylene yields poorly.A kind of method that the present invention couples by using dehydrogenating propane technique with light hydrocarbon cracking predepropanization technique, on the premise of keeping lighter hydrocarbons inlet amount constant, rely on ethylene unit existing equipment and local capacity expansion revamping, the method that pyrolysis furnace separates " one " and 2 propylene towers " two tails " in parallel with PDH reactors " two " and predepropanization is set, for 80~1,200,000 tons/year of ethylene units and 600,000 tons/year of PDH devices, increasing output of ethylene 2.100%~3.150%, propylene enhancing 212.121%~318.182%, reduce investment 5.908%~6.742%, 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 light hydrocarbon cracking predepropanization technique.
Description
Technical field
The present invention relates to a kind of ethylene unit of lighter hydrocarbons steam thermal cracking predepropanization separation process to couple dehydrogenating propane system
The technology of standby propylene PDH devices；On the premise of keeping ethylene unit cracking stock constant, before leveraging fully on ethylene unit
The existing separation equipment of depropanization technique, the capacity expansion revamping of local devices is only carried out, by the coupling with PDH devices, realized
Propylene enhancing, optimize the method for lighter hydrocarbons steam thermal cracking process product structure.Thus, the present invention reduces consolidating for industrial installation
Fixed investment and operating cost, reduce construction land, optimize product structure, fully to improve the spirit of ethylene unit reply turn of the market
Activity, it can be applied in the industrial production of ethene, propylene and low-carbon alkene.
Background technology
The separation process that existing ethylene producing device uses mainly has：Order separation process, front-end deethanization flow, preceding de- third
Alkane flow, the present invention use predepropanization isolation technics.Predepropanization separation process is cracking gas after three sections of compressions, first will
The C3 and cut C3- lighter than C3 with C4 and than C4 weight cut C4+ separated, make C4+ do not enter back into compressor high pressure section and
Related rectifying piece-rate system, then separates the products such as methane hydrogen, ethene, propylene successively from C3 and C3- light components again.Preceding de- third
The steam crack material of alkane separation process can be gas raw material or liquid charging stock.Gas raw material is primarily referred to as lighter hydrocarbons,
Including C2~C5 alkanes and LPG liquefied petroleum gas etc., liquid charging stock is primarily referred to as naphtha, kerosene, diesel oil, is hydrocracked tail
Oil etc..In general, the yield of ethene of gas raw material steam cracking is higher than liquid charging stock, the ethylene contents in cracking gas are higher,
The fuel that the pyrolysis furnace of identical ethylene production capacity is consumed is less, and the power of compressor is also smaller；So gas cracking stock
It is lower than the production cost of liquid cracking stock.But the propylene/ethylene ratio only 0.2~0.3 or so of lighter hydrocarbons steam cracking, connection
The propylene of production is less, and product structure is single.And China's propylene is mainly for the production of polypropylene, expoxy propane, acrylonitrile, isopropyl
Benzene, phenol, acetone, butanol, octanol, isopropanol etc., in recent years, due to the fast development of propylene downstream product, China's propylene needs
The amount of asking also rapid growth, so the product structure of optimization lighter hydrocarbons steam cracking, especially increases propylene yield, it is that China's development is light
One of key technology of hydrocarbon steam cracking.
Preparing propylene by dehydrogenating propane is the propylene that low value-added dehydrogenating propane is converted into high added value, the patent of the technique
Technology includes：The PDH techniques of Lin De/BASF AG, the Oleflex techniques of Uop Inc., the Catofin of ABB Lummus companies
Technique, the Star techniques of Uhde companies, FBD-4 techniques of Snamprogetti/Yarsintz companies etc..Dehydrogenating propane product
Separation generally use cryogenic rectification separating technology, the technology good separating effect, propene yield are high, but to equipment material
It is required that it is high, therefore plant engineering investment is also big.In addition, the C2 and below C2 lighter hydrocarbons contents in PDH device reaction gas are relatively low, lead to
Often, the ethene in the product gas of PDH reactor outlets no longer carries out rectifying separation, is delivered to out-of-bounds directly as fuel gas, thus,
The non-separation and purification of ethylene product of high added value is simultaneously reclaimed, and economic benefit is poor.
Patent CN104193574B, CN104151121B, CN104193570B take off second before individually disclosing the coupling of MTO devices
Alkane route, predepropanization route, order disjunctive path naphtha steam cracking device optimize technique, patent
CN102286292B, which is disclosed, utilizes method of cracking c_4 raffinate propylene enhancing and ethene etc..
Patent CN104193574B, CN104151121B, CN104193570B and CN102286292B of the prior art
The coupling process of MTO devices and deethanization, predepropanization, the naphtha steam cracking device sequentially separated is disclose only, with
And the method using cracking c_4 raffinate propylene enhancing and ethene, also without the light of PDH devices and predepropanization disjunctive path
The technique coupling technique of hydrocarbon steam cracking device.Therefore, there is unreasonable products structure, low-carbon alkene in prior art, especially
The problem of propylene of coproduction yields poorly, engineering investment cost is high, occupation area of equipment is big.
The content of the invention
The technical problems to be solved by the invention are unreasonable products structure, engineering investment cost in the prior art be present
It is high, occupation area of equipment is big, low-carbon alkene the problem of especially propylene yields poorly, there is provided a kind of new dehydrogenating propane technique with it is light
The hydrocarbon pyrolysis predepropanization technique coupling method, have product structure is reasonable, engineering investment cost is low, occupation area of equipment is small,
Low-carbon alkene the advantages of especially propylene yield is high.
To solve the above problems, the technical solution adopted by the present invention is as follows：Before a kind of dehydrogenating propane technique and light hydrocarbon cracking
The method of depropanization technique coupling, keep ethylene unit cracking stock constant, keep ethylene unit cracking stock constant, wherein,
(1) dehydrogenating propane PDH devices：Fresh propane charging mixes with the recycled propane from de-oiling column overhead and propylene rectification tower bottom of towe
Close, into propane gasification tank, enter dehydrogenating propane reactor after gasification tank top gas phase is heated, propane is through catalyst fixed bed
Dehydrogenation reaction is converted into propylene, and propane gasification pot bottom liquid phase component delivers to propane de-oiling tower recovery propane, propane de-oiling tower tower
Push up lime set and return to propane gasification tank, tower reactor key component is mixing more than C4 components, and it is further to deliver to ethylene unit debutanizing tower
Rectifying separates；(2) ethylene unit：Light hydrocarbon gas raw material containing ethane, propane, butane into steam pyrocrack furnace crack instead
Should, generation includes the product of ethene, propylene, and Pintsch process gas is after chilling, the next PDH reactor outlets with PDH devices
Product gas converge be compressed, alkali cleaning processing, and enter predepropanization separative element, obtain polymer grade ethylene, propylene product
And byproduct.
In above-mentioned technical proposal, it is preferable that predepropanization separative element includes：High pressure depropanizer, low pressure depropanizer,
Pre- domethanizing column, domethanizing column, dethanizer, ethylene rectifying column, propylene rectification tower, debutanizing tower.
In above-mentioned technical proposal, it is preferable that the ethane isolated in coupling device be back to ethylene unit cracking unit, third
Alkane is back to PDH device propane gasification tanks.
In above-mentioned technical proposal, it is preferable that ethylene contents >=99.95mol%, polymerization-grade propylene in polymer grade ethylene product
Product propylene content >=99.6mol%.
In above-mentioned technical proposal, it is preferable that ethylene unit nominal capacity be 80~1,200,000 tons/year, cracking stock by
40wt% ethane, 40wt% propane, the lighter hydrocarbons composition of 20wt% butane, the conversion ratio of light hydrocarbon feedstocks is 60%~97%, is used
Predepropanization separating technology flow.
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 149%~178% to be former, institute
The excess load unit stated needs to carry out local capacity expansion revamping to reach the technical requirements of the present invention.
In above-mentioned technical proposal, it is preferable that byproduct includes methane hydrogen, mixing C4 components and drippolene, cracking fuel
Oil.
The present invention relates to a kind of method that PDH techniques couple with light hydrocarbon cracking predepropanization technique.Keeping cracking stock
On the premise of light hydrocarbon gas inlet amount is constant, relies on ethylene unit existing equipment and carry out local capacity expansion revamping, set ethene to split
Solve the predepropanization separative element " one " of stove and PDH reactors " two " and coupling and 2 propylene rectification towers " two in parallel
The method of tail ", thus greatly simplify PDH device technique flows.For 80~1,200,000 tons/year of ethylene units and 600,000 tons/year
For PDH devices, using 40wt% ethane, 40wt% propane, 20wt% butane light hydrocarbon cracking raw material, its conversion ratio be 60%
Between~97%.Compared with ethylene unit, increasing output of ethylene 2.100%~3.150%, propylene enhancing 212.121%~
318.182%；Compared with ethylene unit and PDH devices are set respectively, investment 5.908%~6.742% can be reduced, and can reduce
1.8 hectares of floor space；Thus, preferable technique effect is achieved.
Brief description of the drawings
Fig. 1 is that PDH techniques couple general flow chart with light hydrocarbon cracking predepropanization technique.
In Fig. 1,01 light hydrocarbon cracking raw material, 11 cracking units, 12 quenching units, 13 compression units, 21 pre- demethanation/piptonychias
Alkane tower, 22 dethanizers, 23 ethylene rectifying columns, 24 high low pressure depropanizing towers, 25 propylene rectification towers, 26 debutanizing towers, 31 methane
Hydrogen, 32 polymer grade ethylene products, 33 polymerization-grade propylene products, 34 mixing C4 components, 35 drippolenes, 36 Pyrolysis fuel oil PFOs, 71
Propane feed, 81PDH reaction members, 82PDH separative elements.
The light hydrocarbon cracking raw material 01 of ethylene unit is sent into cracking unit 11 and carries out cracking reaction generation cracking gas, cracks pneumatic transmission
Enter quenching unit 12 and isolate drippolene 35 and Pyrolysis fuel oil PFO 36, cracking gas enters compression unit 13.The propane of PDH devices
Raw material 71 is sent into PDH reaction members 81, and the reaction gas of generation also enters the compression unit 13 of ethylene unit.In compression unit 13,
Through too high/low pressure depropanizer 24, pre- demethanation/demethanation after ethylene cracking gas and the merging supercharging of PDH device products gas
Tower 21, dethanizer 22, ethylene rectifying column 23, propylene rectification tower 25, the isolated methane hydrogen 31 of rectifying of debutanizing tower 26, gather
Close level ethylene product 32, polymerization-grade propylene product 33, mixing C4 components 34, drippolene 35, Pyrolysis fuel oil PFO 36, ethane and third
Alkane is returned and recycled.
Below by embodiment, the invention will be further elaborated, but is not limited only to the present embodiment.
Embodiment
【Comparative example 1】
Using 800,000 tons/year of the light hydrocarbon cracking ethylene unit nominal capacity of predepropanization separating technology, raw material lighter hydrocarbons by
40% ethane, 40% propane and 20% butane form, and the ethane conversion in lighter hydrocarbons is 60%, conversion of propane 93%, fourth
Alkane conversion ratio is 97%, 80.00 ten thousand tons/year of ethylene yield, 17.60 ten thousand tons/year of propylene yield, propylene product/ethylene product ratio
=0.22,189.41 ten thousand tons/year of light hydrocarbon gas consumption of raw materials amount.
【Embodiment 1】
The present invention relates to a kind of method that PDH techniques couple with light hydrocarbon cracking predepropanization technique, is keeping ethylene unit
Cracking stock is constant, on the premise of ethylene unit predepropanization existing equipment part capacity expansion revamping, increases 1 set of PDH reaction system newly
With 1 set of propylene distillation system, and the predepropanization piece-rate system of remaining piece-rate system of PDH devices and light hydrocarbon cracking ethylene unit
Carry out height coupling, the shared piece-rate system of two sets of process units of PDH devices and ethylene unit.I.e.：Cracking of ethylene is set
The skill of the separative element " one " and 2 propylene rectification towers " two tails " in parallel of stove and PDH reactors " two " and technique coupling
Art method.The concrete technical scheme that the present invention uses is as follows：
Ethylene unit：Light hydrocarbon gas raw material containing ethane, propane, butane enters steam pyrocrack furnace and carries out cracking reaction,
Generate ethene, the product such as propylene, Pintsch process gas after quenching, converge with PDH device reaction gas be compressed, alkali cleaning
Processing, and enter predepropanization separative element.Due to converging for PDH device reaction device exported product gas, the compression of ethylene unit,
Alkali cleaning and drying unit all excess loads operate, and load increases to the 177.95% of original ethylene unit.Predepropanization separative element bag
Include：High pressure depropanizer, low pressure depropanizer, pre- domethanizing column, domethanizing column, dethanizer, ethylene rectifying column, propylene rectifying
Also excess load operates for tower, debutanizing tower, and relevant device load increases to some extent, and thus existing ethylene unit equipment needs office
Portion's capacity expansion revamping.The PDH device products gas and ethylene cracking gas merged obtains by predepropanization separative element
Content >=99.95mol% polymer grade ethylenes product, content >=99.6mol% polymerization-grade propylenes product, methane hydrogen, mixing C4 groups
Point and the byproduct such as drippolene, Pyrolysis fuel oil PFO, and ethane and propane are returned and recycled.
PDH devices：Fresh propane charging mixes with the recycled propane from de-oiling column overhead and propylene rectification tower bottom of towe, enters
Enter PDH reactor feeds gasification tank.It is anti-into dehydrogenating propane that the reacted heating furnace of gasification tank top gas phase is heated to reaction temperature
Device is answered, propane is converted into propylene through catalyst fixed bed dehydrogenation reaction.Gasification tank bottom liquid phases component is delivered to propane de-oiling tower and returned
Receive propane.Propane de-oiling column overhead lime set returns to propane gasification tank, and tower reactor key component is mixing C4 and C4 more heavy constituents, is delivered to
Ethylene unit debutanizing tower is further subject to rectifying separation.Because PDH devices compressibility, piece-rate system rely on ethene to fill completely
Corresponding compressibility, piece-rate system are put, only increases 1 propylene rectification tower newly, cancels product air compressor, the alkali of PDH devices
Tower, drier, product gas ice chest, dethanizer, depropanizing tower, debutanizing tower, ethylene refrigeration machine, propylene refrigeration machine are washed, therefore
Complicated tediously long compression separation process is greatly simplified, and is shown in Table 1.
The capital equipment list of the present invention of table 1
| Sequence number | Device name | Remarks | Sequence number | Device name | Remarks |
| 1 | Pyrolysis furnace | It is constant | 18 | Propane feed gasification tank | Newly added equipment |
| 2 | Quenching oil column | It is constant | 19 | Propane de-oiling tower | Newly added equipment |
| 3 | Quenching water column | It is constant | 20 | Dehydrogenation feed heating furnace | Newly added equipment |
| 4 | Charge gas compressor | Load increase | 21 | Dehydrogenation reactor | Newly added equipment |
| 5 | Caustic wash tower | Load increase | 22 | Regeneration air heating furnace | Newly added equipment |
| 6 | Drier | Load increase | 23 | Waste Heat System | Newly added equipment |
| 7 | High pressure depropanizer | Load increase | 24 | Regeneration air compressor | Newly added equipment |
| 8 | Low pressure depropanizer | Load increase | 25 | 2# propylene rectification towers | Newly added equipment |
| 9 | Cold box system | Load increase | 26 | Product air compressor | Cancel |
| 10 | Pre- domethanizing column | Load increase | 27 | Product gas caustic wash tower | Cancel |
| 11 | Domethanizing column | Load increase | 28 | Product gas dryer | Cancel |
| 12 | Dethanizer | Load increase | 29 | Product gas ice chest | Cancel |
| 13 | Ethylene rectifying column | Load increase | 30 | Product gas dethanizer | Cancel |
| 14 | 1# propylene rectification towers | It is constant | 31 | Product gas depropanizing tower | Cancel |
| 15 | Debutanizing tower | Load increase | 32 | Product gas debutanizing tower | Cancel |
| 16 | Propylene refrigeration machine | Load increase | 33 | Product gas ethylene refrigeration machine | Cancel |
| 17 | Ethylene refrigeration machine | Load increase | 34 | Product gas propylene refrigeration machine | Cancel |
The method coupled using a kind of PDH techniques of the present invention with light hydrocarbon cracking predepropanization technique, containing in ethylene unit
Ethane, propane, the light hydrocarbon gas raw material of butane enter steam pyrocrack furnace and carry out the product such as cracking reaction, generation ethene, propylene,
Pintsch process gas after quenching, converge with PDH device product gas be compressed, alkali cleaning processing, and enter predepropanization
Separative element.Due to converging for PDH device product gas, compression, alkali cleaning and drying unit all excess loads of ethylene unit operate, and bear
Lotus increases to 177.95% or so of original ethylene unit.Predepropanization separative element includes：High pressure depropanizer, low pressure depropanization
Also excess load operates for tower, pre- domethanizing column, domethanizing column, dethanizer, ethylene rectifying column, propylene rectification tower, debutanizing tower, phase
Machine utilization is answered to increase to some extent, thus existing ethylene unit equipment needs local capacity expansion revamping.The PDH merged
Device product gas and ethylene cracking gas obtain content >=99.95mol% polymer grade ethylenes by predepropanization separative element
Product, content >=99.6mol% polymerization-grade propylenes product, methane hydrogen, the mixing pair such as C4 components and drippolene, Pyrolysis fuel oil PFO
Product, and ethane, propane return, and recycle.Fresh propane charging in PDH devices is with coming from de-oiling column overhead and propylene
The recycled propane mixing at rectifying tower bottom, into PDH reactor feeds gasification tank.The reacted heating furnace of gasification tank top gas phase adds
Heat enters dehydrogenating propane reactor to reaction temperature, and propane is converted into propylene through catalyst fixed bed dehydrogenation reaction.Gasification tank bottom
Portion's liquid phase component delivers to propane de-oiling tower recovery propane.Propane de-oiling column overhead lime set returns to propane gasification tank, the main group of tower reactor
It is divided into mixing C4 and C4 more heavy constituents, delivers to ethylene unit debutanizing tower and be further subject to rectifying separation.PDH devices compression system
System, piece-rate system rely on the corresponding compressibility of ethylene unit, piece-rate system completely, only increase 1 propylene rectification tower newly.
Using 80 tons/year of the light hydrocarbon cracking ethylene unit nominal capacity of predepropanization separating technology, raw material lighter hydrocarbons are by 40%
Ethane, 40% propane and 20% butane form, and the ethane conversion in lighter hydrocarbons is 60%, conversion of propane 93%, butane turn
Rate is 97%, 80.00 ten thousand tons/year of ethylene yield, 17.60 ten thousand tons/year of propylene yield, light hydrocarbon gas consumption of raw materials amount 189.41
Ten thousand tons/year.60 tons/year of PDH devices nominal capacity, 2.52 ten thousand tons/year of ethylene yield, 56.00 ten thousand tons/year of propylene yield.Coupling
Device adds up to 82.52 ten thousand tons/year of ethylene yield, 73.60 ten thousand tons/year of propylene yield, ethylene unit and the coupling of PDH device techniques
59.32 hundred million yuans of engineering construction investment.With【Comparative example 1】Compare, 56.00 ten thousand tons/year of propylene enhancing, propylene product/second
Alkene product ratio=0.89, ethylene yield increase by 3.15%, propylene yield increase by 318.18%, save engineering construction investment 3.75 hundred million
Yuan, equivalent to investment reduction 5.947%, reduce 1.8 hectares of floor space.
【Comparative example 2】
Using 1,000,000 tons/year of the light hydrocarbon cracking ethylene unit nominal capacity of predepropanization separating technology, raw material lighter hydrocarbons by
40% ethane, 40% propane and 20% butane form, and the ethane conversion in lighter hydrocarbons is 60%, conversion of propane 93%, fourth
Alkane conversion ratio is 97%, 100.00 ten thousand tons/year of ethylene yield, 22.00 ten thousand tons/year of propylene yield, propylene product/ethylene product ratio
=0.22,235.32 ten thousand tons/year of light hydrocarbon gas consumption of raw materials amount.
【Embodiment 2】
Using 100 tons/year of the light hydrocarbon cracking ethylene unit nominal capacity of predepropanization separating technology, raw material lighter hydrocarbons are by 40%
Ethane, 40% propane and 20% butane form, and the ethane conversion in lighter hydrocarbons is 60%, conversion of propane 93%, butane turn
Rate is 97%, 100.00 ten thousand tons/year of ethylene yield, 22.00 ten thousand tons/year of propylene yield, light hydrocarbon gas consumption of raw materials amount
235.32 ten thousand tons/year.60 tons/year of PDH devices nominal capacity, 2.52 ten thousand tons/year of ethylene yield, 56.00 ten thousand tons of propylene yield/
Year.Coupling device adds up to 102.52 ten thousand tons/year of ethylene yield, 78.00 ten thousand tons/year of propylene yield, ethylene unit and PDH device works
65.26 hundred million yuans of the engineering construction investment of skill coupling.With【Comparative example 2】Compare, 56.00 ten thousand tons/year of propylene enhancing, propylene
Product/ethylene product ratio=0.76, ethylene yield increase by 2.52%, propylene yield increase by 254.55%, save engineering construction and throw
4.10 hundred million yuans are provided, equivalent to investment reduction 5.908%, reduces 1.8 hectares of floor space.
【Comparative example 3】
Using 1,100,000 tons/year of the light hydrocarbon cracking ethylene unit nominal capacity of predepropanization separating technology, raw material lighter hydrocarbons by
40% ethane, 40% propane and 20% butane form, and the ethane conversion in lighter hydrocarbons is 60%, conversion of propane 93%, fourth
Alkane conversion ratio is 97%, 110.00 ten thousand tons/year of ethylene yield, 24.20 ten thousand tons/year of propylene yield, propylene product/ethylene product ratio
=0.22,258.27 ten thousand tons/year of light hydrocarbon gas consumption of raw materials amount.
【Embodiment 3】
Using 110 tons/year of the light hydrocarbon cracking ethylene unit nominal capacity of predepropanization separating technology, raw material lighter hydrocarbons are by 40%
Ethane, 40% propane and 20% butane form, and the ethane conversion in lighter hydrocarbons is 60%, conversion of propane 93%, butane turn
Rate is 97%, 110.00 ten thousand tons/year of ethylene yield, 24.20 ten thousand tons/year of propylene yield, light hydrocarbon gas consumption of raw materials amount
258.27 ten thousand tons/year.60 tons/year of PDH devices nominal capacity, 2.52 ten thousand tons/year of ethylene yield, 56.00 ten thousand tons of propylene yield/
Year.Coupling device adds up to 112.52 ten thousand tons/year of ethylene yield, 80.20 ten thousand tons/year of propylene yield, ethylene unit and PDH device works
67.66 hundred million yuans of the engineering construction investment of skill coupling.With【Comparative example 3】Compare, 56.00 ten thousand tons/year of propylene enhancing, propylene
Product/ethylene product ratio=0.71, ethylene yield increase by 2.29%, propylene yield increase by 231.41%, save engineering construction and throw
4.33 hundred million yuans are provided, equivalent to investment reduction 6.011%, reduces 1.8 hectares of floor space.
【Comparative example 4】
Using 1,200,000 tons/year of the light hydrocarbon cracking ethylene unit nominal capacity of predepropanization separating technology, raw material lighter hydrocarbons by
40% ethane, 40% propane and 20% butane form, and the ethane conversion in lighter hydrocarbons is 60%, conversion of propane 93%, fourth
Alkane conversion ratio is 97%, 120.00 ten thousand tons/year of ethylene yield, 26.40 ten thousand tons/year of propylene yield, propylene product/ethylene product ratio
=0.22,281.22 ten thousand tons/year of light hydrocarbon gas consumption of raw materials amount.
【Embodiment 4】
Using 120 tons/year of the light hydrocarbon cracking ethylene unit nominal capacity of predepropanization separating technology, raw material lighter hydrocarbons are by 40%
Ethane, 40% propane and 20% butane form, and the ethane conversion in lighter hydrocarbons is 60%, conversion of propane 93%, butane turn
Rate is 97%, 120.00 ten thousand tons/year of ethylene yield, 26.40 ten thousand tons/year of propylene yield, light hydrocarbon gas consumption of raw materials amount
281.22 ten thousand tons/year.60 tons/year of PDH devices nominal capacity, 2.52 ten thousand tons/year of ethylene yield, 56.00 ten thousand tons of propylene yield/
Year.Coupling device adds up to 122.52 ten thousand tons/year of ethylene yield, 82.40 ten thousand tons/year of propylene yield, ethylene unit and PDH device works
69.28 hundred million yuans of the engineering construction investment of skill coupling.With【Comparative example 4】Compare, 56.00 ten thousand tons/year of propylene enhancing, propylene
Product/ethylene product ratio=0.67, ethylene yield increase by 2.10%, propylene yield increase by 212.12%, save engineering construction and throw
5.01 hundred million yuans are provided, equivalent to investment reduction 6.742%, reduces 1.8 hectares of floor space.
The coupling technique ethylene unit machine utilization of table 2 lifts list
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | |
| Pyrolysis furnace | It is constant | It is constant | It is constant | It is constant |
| Chilling tower | It is constant | It is constant | It is constant | It is constant |
| Charge gas compressor | 77.95% | 61.96% | 56.19% | 49.05% |
| Caustic wash tower | 77.95% | 61.96% | 56.19% | 49.05% |
| Crack gas dryer | 77.95% | 61.96% | 56.19% | 49.05% |
| High pressure depropanizer | 77.95% | 61.96% | 56.19% | 49.05% |
| Low pressure depropanizer | 203.70% | 161.90% | 146.84% | 134.34% |
| C2 hydrogenation reactors | 3.59% | 2.86% | 2.59% | 2.37% |
| Cold box system | 18.41% | 14.63% | 13.27% | 12.14% |
| Expanding machine | 18.41% | 14.63% | 13.27% | 12.14% |
| Pre- domethanizing column | 42.26% | 32.98% | 29.64% | 31.07% |
| Domethanizing column | 18.41% | 14.63% | 13.27% | 12.14% |
| Dethanizer | 42.14% | 31.79% | 28.06% | 24.97% |
| Ethylene rectifying column | 3.59% | 2.86% | 2.59% | 2.37% |
| Propylene rectification tower | 458.23% | 343.70% | 302.42% | 268.16% |
| Debutanizing tower | 13.51% | 10.74% | 9.74% | 8.91% |
The technological parameter of table 3 and techno economic parameter summary sheet
Obviously, using the method for the present invention, come for 80~1,200,000 tons/year of ethylene units and 600,000 tons/year of PDH devices
Say, using 40wt% ethane, 40wt% propane, 20wt% butane light hydrocarbon cracking raw material, its conversion ratio be 60%~97% it
Between., can be with increasing output of ethylene 2.100%~3.150%, propylene enhancing 212.121%~318.182% compared with ethylene unit；
Compared with ethylene unit and PDH devices are set respectively, investment 5.908%~6.742% can be reduced, and floor space can be reduced
1.8 hectare；Thus, preferable technique effect is achieved.
Claims (8)
1. a kind of method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique, keep ethylene unit cracking stock not
Become, wherein, (1) dehydrogenating propane PDH devices：Fresh propane is fed and the circulation from de-oiling column overhead and propylene rectification tower bottom of towe
Propane mixes, and into propane gasification tank, enters dehydrogenating propane reactor after gasification tank top gas phase is heated, propane is through catalyst
Fixed-bed dehydrogenation reaction is converted into propylene, and propane gasification pot bottom liquid phase component delivers to propane de-oiling tower recovery propane, and propane takes off
Oily column overhead lime set returns to propane gasification tank, and tower reactor key component is mixing more than C4 components, delivers to ethylene unit debutanizing tower
Further rectifying separation；(2) ethylene unit：Light hydrocarbon gas raw material containing ethane, propane, butane is carried out into steam pyrocrack furnace
Cracking reaction, generation include the product of ethene, propylene, and after chilling, the PDH come with PDH devices reacts Pintsch process gas
Device outlet product gas converge be compressed, alkali cleaning processing, and enter predepropanization separative element, obtain polymer grade ethylene, third
Alkene product and byproduct.
2. the method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique according to claim 1, its feature exist
Include in predepropanization separative element：High pressure depropanizer, low pressure depropanizer, pre- domethanizing column, domethanizing column, deethanization
Tower, ethylene rectifying column, propylene rectification tower, debutanizing tower.
3. the method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique according to claim 1, its feature exist
The ethane isolated in coupling device 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 light hydrocarbon cracking predepropanization technique according to claim 1, its feature exist
Ethylene contents >=99.95mol%, polymerization-grade propylene product propylene content >=99.6mol% in polymer grade ethylene product.
5. the method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique according to claim 1, its feature exist
It it is 80~1,200,000 tons/year in ethylene unit nominal capacity, cracking stock is by 40wt% ethane, 40wt% propane, 20wt% butane
Lighter hydrocarbons composition, the conversion ratios of light hydrocarbon feedstocks is 60%~97%, using predepropanization separating technology flow.
6. the method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique according to claim 1, its feature exist
In PDH devices nominal capacity be 600,000 tons/year.
7. the method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique according to claim 1, its feature exist
Can cause after PDH device reaction products are sent to ethylene cracking gas suction port of compressor ethylene unit compression, alkali cleaning, drying and
Separative element excess load, load design meet 149%~178% to be former, and described excess load unit needs to carry out local expansion
It can transform to reach requirement.
8. the method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique according to claim 1, its feature exist
Include methane hydrogen, mixing C4 components and drippolene, Pyrolysis fuel oil PFO in byproduct.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710939515.1A CN107602323A (en) | 2017-10-11 | 2017-10-11 | The method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710939515.1A CN107602323A (en) | 2017-10-11 | 2017-10-11 | The method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107602323A true CN107602323A (en) | 2018-01-19 |
Family
ID=61068464
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710939515.1A Pending CN107602323A (en) | 2017-10-11 | 2017-10-11 | The method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107602323A (en) |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109438163A (en) * | 2018-11-23 | 2019-03-08 | 内蒙古中煤蒙大新能源化工有限公司 | A kind of method of tail gas recycle propane in polypropylene plant |
| 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 |
| CN109761735A (en) * | 2019-01-21 | 2019-05-17 | 中石化上海工程有限公司 | The method that naphtha and Deposition During Propane Pyrolysis predepropanization are coupled with PDH |
| CN109809957A (en) * | 2019-01-21 | 2019-05-28 | 中石化上海工程有限公司 | The method that light hydrocarbon cracking front-end deethanization technique is coupled with PDH technique |
| CN109809958A (en) * | 2019-01-21 | 2019-05-28 | 中石化上海工程有限公司 | The method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique |
| 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 |
| CN111848327A (en) * | 2020-07-08 | 2020-10-30 | 中国石油化工股份有限公司 | Method for coupling depropanization process and propane dehydrogenation process before hydrocarbon steam cracking |
| CN111875466A (en) * | 2020-07-08 | 2020-11-03 | 中国石油化工股份有限公司 | Coupling method of depropanization process and propane dehydrogenation process before hydrocarbon steam cracking |
| CN111892475A (en) * | 2020-06-30 | 2020-11-06 | 中石化宁波工程有限公司 | Method for increasing propylene and ethylene yield of propane dehydrogenation device |
| CN111943800A (en) * | 2020-06-30 | 2020-11-17 | 中石化宁波工程有限公司 | Method for producing propylene and ethylene by thermal cracking of light hydrocarbon |
| CN112209794A (en) * | 2020-11-13 | 2021-01-12 | 洛阳智达石化工程有限公司 | System and method for producing propylene by combining light hydrocarbon modification and propane dehydrogenation |
| CN113461474A (en) * | 2021-06-30 | 2021-10-01 | 中国石油化工股份有限公司 | System and method for industrially and continuously preparing propylene oxide from propane |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102320912A (en) * | 2011-06-03 | 2012-01-18 | 神华集团有限责任公司 | Method for maximizing total ethylene and propylene yield in process of preparing low-carbon olefin by oxygen compound conversion |
| CN102603457A (en) * | 2012-01-17 | 2012-07-25 | 马俊杰 | Production device and process for generating propylene by utilizing C3 and C4 in liquid gas deep processing |
| 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 |
| CN104193574A (en) * | 2014-08-13 | 2014-12-10 | 中石化上海工程有限公司 | Method for coupling MTO (methanol to olefin) process with process of preparing ethylene by cracking naphtha steam |
-
2017
- 2017-10-11 CN CN201710939515.1A patent/CN107602323A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102320912A (en) * | 2011-06-03 | 2012-01-18 | 神华集团有限责任公司 | Method for maximizing total ethylene and propylene yield in process of preparing low-carbon olefin by oxygen compound conversion |
| CN102603457A (en) * | 2012-01-17 | 2012-07-25 | 马俊杰 | Production device and process for generating propylene by utilizing C3 and C4 in liquid gas deep processing |
| 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 |
| CN104193574A (en) * | 2014-08-13 | 2014-12-10 | 中石化上海工程有限公司 | Method for coupling MTO (methanol to olefin) process with process of preparing ethylene by cracking naphtha steam |
Cited By (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109438163A (en) * | 2018-11-23 | 2019-03-08 | 内蒙古中煤蒙大新能源化工有限公司 | A kind of method of tail gas recycle propane in polypropylene plant |
| CN109438163B (en) * | 2018-11-23 | 2021-07-02 | 内蒙古中煤蒙大新能源化工有限公司 | Method for recovering propane from tail gas in polypropylene device |
| 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 |
| CN109809958A (en) * | 2019-01-21 | 2019-05-28 | 中石化上海工程有限公司 | The method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique |
| CN109761735A (en) * | 2019-01-21 | 2019-05-17 | 中石化上海工程有限公司 | The method that naphtha and Deposition During Propane Pyrolysis predepropanization are coupled with PDH |
| 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 |
| CN109809957A (en) * | 2019-01-21 | 2019-05-28 | 中石化上海工程有限公司 | The method that light hydrocarbon cracking front-end deethanization technique is coupled with PDH technique |
| CN111892475B (en) * | 2020-06-30 | 2023-04-07 | 中石化宁波工程有限公司 | Method for increasing propylene and ethylene yield of propane dehydrogenation device |
| CN111892475A (en) * | 2020-06-30 | 2020-11-06 | 中石化宁波工程有限公司 | Method for increasing propylene and ethylene yield of propane dehydrogenation device |
| CN111943800A (en) * | 2020-06-30 | 2020-11-17 | 中石化宁波工程有限公司 | Method for producing propylene and ethylene by thermal cracking of light hydrocarbon |
| CN111943800B (en) * | 2020-06-30 | 2023-04-07 | 中石化宁波工程有限公司 | Method for producing propylene and ethylene by thermal cracking of light hydrocarbon |
| CN111848327A (en) * | 2020-07-08 | 2020-10-30 | 中国石油化工股份有限公司 | Method for coupling depropanization process and propane dehydrogenation process before hydrocarbon steam cracking |
| 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 |
| CN111875466A (en) * | 2020-07-08 | 2020-11-03 | 中国石油化工股份有限公司 | Coupling method of depropanization process and propane dehydrogenation process before hydrocarbon steam cracking |
| CN111848327B (en) * | 2020-07-08 | 2023-07-11 | 中国石油化工股份有限公司 | Method for coupling depropanization process and propane dehydrogenation process before hydrocarbon steam cracking |
| CN112209794A (en) * | 2020-11-13 | 2021-01-12 | 洛阳智达石化工程有限公司 | System and method for producing propylene by combining light hydrocarbon modification and propane dehydrogenation |
| CN113461474A (en) * | 2021-06-30 | 2021-10-01 | 中国石油化工股份有限公司 | System and method for industrially and continuously preparing propylene oxide from propane |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107602323A (en) | The method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique | |
| CN107673947A (en) | The method that dehydrogenating propane technique couples with naphtha pyrolysis front-end deethanization technique | |
| CN107602324A (en) | The method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique | |
| CN109809958A (en) | The method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique | |
| CN104230617B (en) | The method that MTO technique couples with Petroleum and Deposition During Propane Pyrolysis order separating technology | |
| CN104151121B (en) | The method that MTO technique is coupled with naphtha cracking predepropanization technique | |
| CN101323798B (en) | Catalytic conversion method and special apparatus therefor | |
| CN109761734A (en) | The method that naphtha and ethane cracking front-end deethanization are coupled with PDH | |
| CN109809957A (en) | The method that light hydrocarbon cracking front-end deethanization technique is coupled with PDH technique | |
| CN102942435B (en) | Reaction technology using moving bed technique to convert methanol into propylene | |
| CN109336726A (en) | A kind of technique of carbon four, light oil and coupling between methanol preparing propylene by catalytic cracking ethylene | |
| CN104177214B (en) | A kind of catalytic cracking rich gas and methanol to olefins reaction product composite liberation method | |
| CN109761736A (en) | Naphtha and ethane cracking sequentially separate the method coupled with PDH | |
| CN109851461A (en) | The method that naphtha and Deposition During Propane Pyrolysis front-end deethanization are coupled with PDH | |
| CN101092325B (en) | Method for preparing propylene by catalytic cracking olefin of containing carbon | |
| CN109761733A (en) | The method that naphtha and ethane cracking predepropanization are coupled with PDH | |
| CN109761735A (en) | The method that naphtha and Deposition During Propane Pyrolysis predepropanization are coupled with PDH | |
| CN103333040B (en) | Low energy consumption propylene production technology | |
| CN103382145A (en) | Preparation process for propylene from methanol or dimethyl ether | |
| CN104557368B (en) | Polymorphic type material coupled conversion ethene processed, propylene and the system and method for aromatic hydrocarbons | |
| CN109734549A (en) | Naphtha and Deposition During Propane Pyrolysis sequentially separate the method coupled with PDH | |
| CN109957421A (en) | A kind of combined method of catalytic cracking and lighter hydrocarbons deep processing | |
| CN102285851B (en) | Method for increasing yields of ethylene and propylene | |
| CN102070390B (en) | The method of refinery's mixed c 4 propylene | |
| CN104926584A (en) | System and method for preparing isobutane |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20180119 |
|
| RJ01 | Rejection of invention patent application after publication |