CN205730772U - System for recovering mixed hydrocarbon from polyolefin discharge flare gas - Google Patents
System for recovering mixed hydrocarbon from polyolefin discharge flare gas Download PDFInfo
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- CN205730772U CN205730772U CN201620049954.6U CN201620049954U CN205730772U CN 205730772 U CN205730772 U CN 205730772U CN 201620049954 U CN201620049954 U CN 201620049954U CN 205730772 U CN205730772 U CN 205730772U
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- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 62
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 61
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 57
- 229920000098 polyolefin Polymers 0.000 title claims abstract description 43
- 239000007788 liquid Substances 0.000 claims abstract description 109
- 239000000203 mixture Substances 0.000 claims abstract description 64
- 239000012530 fluid Substances 0.000 claims description 93
- 239000007789 gas Substances 0.000 claims description 85
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 18
- 238000001816 cooling Methods 0.000 claims description 18
- 230000004044 response Effects 0.000 claims description 13
- 229910052757 nitrogen Inorganic materials 0.000 claims description 9
- 238000000926 separation method Methods 0.000 abstract description 31
- 238000006116 polymerization reaction Methods 0.000 abstract description 11
- 239000000126 substance Substances 0.000 abstract description 5
- 238000007711 solidification Methods 0.000 abstract description 2
- 230000008023 solidification Effects 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 25
- -1 ethylene, propylene Chemical group 0.000 description 14
- 239000012071 phase Substances 0.000 description 12
- 239000007791 liquid phase Substances 0.000 description 10
- 239000000047 product Substances 0.000 description 10
- 238000009833 condensation Methods 0.000 description 9
- 230000005494 condensation Effects 0.000 description 9
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 9
- 238000004519 manufacturing process Methods 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- 239000004698 Polyethylene Substances 0.000 description 6
- 150000001335 aliphatic alkanes Chemical class 0.000 description 6
- 230000006835 compression Effects 0.000 description 6
- 238000007906 compression Methods 0.000 description 6
- 239000000463 material Substances 0.000 description 6
- 229920000573 polyethylene Polymers 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 239000004743 Polypropylene Substances 0.000 description 5
- 229920001155 polypropylene Polymers 0.000 description 5
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 5
- 150000001336 alkenes Chemical class 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 238000009835 boiling Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 3
- 239000005977 Ethylene Substances 0.000 description 3
- 230000008676 import Effects 0.000 description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 3
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 3
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000000178 monomer Substances 0.000 description 2
- 229910052756 noble gas Inorganic materials 0.000 description 2
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- BKOOMYPCSUNDGP-UHFFFAOYSA-N 2-methylbut-2-ene Chemical group CC=C(C)C BKOOMYPCSUNDGP-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000007613 slurry method Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model provides a system for retrieve hydrocarbon mixture in follow polyolefin row torch gas, it includes desicator, one-level plate fin heat exchanger, second grade plate fin heat exchanger, one-level vapour and liquid separator, second grade vapour and liquid separator, tertiary vapour and liquid separator and contain the expansion unit of inflation end and pressure boost end. The system for recovering the mixed hydrocarbon from the polyolefin discharged flare gas utilizes tail gas expansion to obtain the cold quantity required by the system, and the pressure energy of the recovered tail gas is maximized; meanwhile, multi-stage gas-liquid separation is adopted, wherein ingenious design of first-stage gas-liquid separation and third-stage gas-liquid separation is used for recovering heavy hydrocarbon components (mainly C4+ components) serving as an outlet of an inert substance discharged out of a polymerization reaction system, and the problem that a heat exchanger is blocked due to solidification of the C6+ components is avoided.
Description
Technical field
This utility model relates to the environmental technology field of petroleum chemical industry, particularly relates to a kind of from polyolefin row
Torch gas reclaims the system and method for hydrocarbon mixture.
Background technology
Polyolefin is (such as ethylene, propylene, 1-butylene, 1-by many identical or different simple olefins molecules
Amylene etc.) through sudden reaction formed macromolecular compound, wherein mostly important with polyethylene and polypropylene.
Due to abundant raw material, cheap, be easily worked molding, high comprehensive performance, polyolefin is producing and raw
The every field lived all has a wide range of applications.Polyolefinic production method has high pressure polymerisation and low-pressure polymerization (bag
Include solwution method, slurry method, substance law, vapor phase method).
Polyolefinic production is usually present a common problem, has a large amount of discharge gas to produce the most in process of production
Raw, as discharged reaction periodic off-gases in order to control the content of noble gas in polymerization process from reactor.
These discharge gas are essentially from devices such as reactor, flash tank, degassing cabins, containing a large amount of unreacted alkene
Monomer, comonomer, hydrogen, nitrogen, byproduct of reaction, alkane impurity and induced condensing agent.In order to carry
High raw material availability, reduces production cost, and above-mentioned discharge gas needs to take certain technological means, reclaims it
In active component send response system back to, fixed gas be then emitted into torch burning process (this portion gas be referred to as
For row's torch gas).Traditional recovery process typically uses compression condensation method, and its flow process is that first low pressure condensation is the highest
Pressure condensation, i.e. discharge gas first sends into low pressure cold after low-pressure condenser is cooled to uniform temperature (generally-5 DEG C)
Solidifying tank, uncooled gas then by compressor boost, is cooled to uniform temperature (generally through high pressure condenser
-10 DEG C) send into high pressure drainer afterwards, the high pressure condensed fluid of isolated and low pressure cold lime set send response system back to,
Fixed gas is then discharged into torch.
At ambient pressure, the boiling point of ethylene is-103.9 DEG C, and the boiling point of propylene is-47.4 DEG C, and the boiling point of 1-butylene is
-6.3℃.Obviously, compression condensation method can realize the preliminary of discharge gas is reclaimed (C4 and above component), boiling
Relatively low component such as the ethylene, propylene of point is then only capable of reclaiming a part, and major part is all as arranging at torch gas burning
Reason.Wherein, ethylene/propene is the primary raw material of polyethylene/polypropylene, directly burns unfortunately.Then have
Researcher proposes " compression condensation+membrance separation " the integrated method organic efficiency with raising light hydrocarbon component, such as U.S.
State's patent US 5769927 proposes to be used for the method polypropylene effluent gas recovery, but the effect of membrance separation is only
For concentration, Rich propylene also needs to return compression further, condensation, thus circulating load is more than initial ejection amount,
This causes compression and the corresponding equipment investment of condensation phase and energy consumption all to dramatically increase；Chinese patent
CN1228366C proposes the method that " compression condensation+vacuum recovery+membrance separation " is integrated, according in patent
Described, the exit gas that secondary membrane separates also has 10～the propylene of 20%, and processing mode is to send into flare stack
Evacuating pipeline burns.
Understanding from the above mentioned, after compressed condensation and membrance separation two-step pretreatment, row's torch gas still contains alkene
, there is the probability continuing recycling in the useful constituents such as monomer.Then there is researcher (Chinese patent
CN1048417C, CN202485331U, CN103520946B) propose to use deep cooling to divide after membrance separation
From method reclaim lighter hydrocarbons further.Wherein, patent CN202485331U and CN103520946B provide
Cryogenic separation part use turbine expansion technology obtain cold, its advantage is to take full advantage of membrance separation tail gas
The pressure energy of self, it is not necessary to additionally increase power-equipment, saves equipment investment and occupation of land, returns simultaneously
Receive part hydrocarbons in membrance separation tail gas.
In terms of the data of actual production, the raw material used by polyolefin often contains a small amount of alkane, as methane,
Ethane, propane, butane, pentane, hexane, heptane, the most in the course of the polymerization process, there is also production alkane
Side reaction, and alkane is noble gas for olefinic polymerization system, is the most progressively enriched with,
When alkane excessive concentration, the carrying out of polyreaction can be affected.If reclaiming the hydrocarbon mixture obtained all to return instead
Answer system will increase the weight of to be enriched with effect, therefore need to take measures to avoid alkane (especially heavy hydrocarbon) to return reaction
System.
It addition, the fusing point of hexane and above component is higher, as used the mode of cryogenic separation, it is possible to solidification,
Thus block the passage of plate-fin heat exchanger.
After the expanded machine of gas expands, in addition to producing cold, also can produce a part of expansion work, this part
Merit can realize reclaiming by designing the special expansion unit of a set of polyolefin tail.The expansion work reclaimed is permissible
For rich nitrogen tail gas supercharging, it is used as de-storehouse gas or other workshop sections.
In sum, traditional deep cooling separating method there is also the biggest room for improvement.
Utility model content
In view of this, in order to overcome defect and the problem of prior art, this utility model provides a kind of from polyene
Hydrocarbon row's torch gas reclaims the system and method for hydrocarbon mixture.
A kind of system reclaiming hydrocarbon mixture from polyolefin row's torch gas, comprising:
Exsiccator 110), it is for receiving the row's torch gas 1 from polyolefin response system, and exports first
Fluid 2；
One-level plate-fin heat exchanger 121, it is used for cooling down described first fluid 2, and exports the first gas-liquid mixture
3；
One-level gas-liquid separator 131, it is for separating the heavy hydrocarbon component in described first gas-liquid mixture 3, defeated
Go out second fluid 5 and form the second gas-liquid mixture 15 to described one-level plate-fin heat exchanger 121, and export richness
Containing nitrogen and the 3rd fluid 4 of light hydrocarbon component；
Two grades of plate-fin heat exchangers 122, it is used for cooling down described 3rd fluid 4, and exports the 3rd gas-liquid mixture
6；
Two grades of gas-liquid separators 132, it is for separating the light hydrocarbon component in described 3rd gas-liquid mixture 6, and
Exporting the 4th fluid 7 and the 5th fluid 8, described 4th fluid 7 order successively is by described two step wing heat exchange
Device 122 and described one-level plate-fin heat exchanger 121 form the 6th fluid 10；
Comprising the expansion unit of expanding end 141 and pressurized end 142, described expanding end 141 is for described the
Five fluids 8 carry out expanding cooling, and output cryogen 11 order successively is by described two grades of plate-fin heat exchangers 122
Formed with described one-level plate-fin heat exchanger 121 and expand fluid 13, export expansion work, described pressurized end 142 simultaneously
Receive the expansion work of described expanding end 141 output, and be the supercharging of described expansion fluid 13, export the 7th fluid
14；
Three grades of gas-liquid separators 133, it is for separating the light hydrocarbon component in described second gas-liquid mixture 15,
Exporting the 8th fluid 16 and the 9th fluid 17, wherein said 9th fluid 17 converges with described 6th fluid 10
After be back to described polyolefin response system.
In this utility model one better embodiment, the first gas-liquid of described one-level plate-fin heat exchanger 121 output
The temperature range of mixture 3 is-30～-70 DEG C.
In this utility model one better embodiment, the 3rd gas-liquid of described two grades of plate-fin heat exchangers 122 output
The temperature range of mixture 6 is-80～-150 DEG C.
In this utility model one better embodiment, described expansion unit is Turbine expansion unit.
In this utility model one better embodiment, it is 1.1～1.6MPa that described expanding end 141 expands front pressure,
After expansion, pressure is 0.05～0.2MPa.
A kind of method reclaiming hydrocarbon mixture from polyolefin row's torch gas, it comprises the steps:
Row's torch gas 1 drying device 110 of S101, in the future autohemagglutination olefine reaction system delivers to one-level after processing
Plate-fin heat exchanger 121 is lowered the temperature；
Row's torch gas after S102, cooling is delivered to one-level gas-liquid separator 131 and is carried out gas-liquid separation, and output contains
The second fluid 5 of heavy hydrocarbon component, and export the 3rd 4 to two grades of plate-fins of fluid rich in nitrogen and light hydrocarbon component
Heat exchanger 122 forms the 3rd gas-liquid mixture 6；
S103, described 3rd gas-liquid mixture 6 are delivered to two grades of gas-liquid separators 132 and are carried out gas-liquid separation, shape
The 4th fluid 7 become order successively is by described two grades of plate-fin heat exchangers 122 and described one-level plate-fin heat exchanger
121 form the 6th fluid 10, after the expanding end 141 of the 5th expanded unit of fluid 8 of formation expands cooling,
Order is formed by described two grades of plate-fin heat exchangers 122 and described one-level plate-fin heat exchanger 121 and expands stream successively
Body 13, forms the 7th fluid 14 after described expansion fluid 13 intensified end 142 supercharging；
S104, described second fluid 5 export the second gas-liquid after described one-level plate-fin heat exchanger 121 is lowered the temperature
15 to three grades of gas-liquid separators of mixture 133 carry out gas-liquid separation, export the 8th fluid 16, and export described
9th fluid 17 is back to described polyolefin response system after converging with described 6th fluid 10.
Relative to prior art, what what this utility model provided reclaimed hydrocarbon mixture from polyolefin row's torch gas is
System utilizes tail gas to expand acquisition system institute chilling requirement, maximizes the pressure energy reclaiming tail gas；Use multistage simultaneously
Gas-liquid separation, wherein first order gas-liquid separation and the ingehious design of third level gas-liquid separation, be on the one hand used for back
Receive heavy hydrocarbon component (predominantly C4+ component), discharge an outlet of polymerization reaction system as inert substance,
On the other hand the problem that C6+ curing components causes heat exchanger to block also is avoided；In addition a set of polyolefin is devised
The expansion unit that tail gas is special, utilizes the pressure of tail gas can obtain cold, the most also reclaims expansion work.
It is understood that polyethylene and polyacrylic row's torch gas composition approximation, this practicality can be used
The system and method reclaiming hydrocarbon mixture from polyolefin row's torch gas of novel proposition reclaims, and difference only exists
Different in operating condition.
Accompanying drawing explanation
Fig. 1 for this utility model first embodiment provide from polyolefin row torch gas reclaim hydrocarbon mixture be
The composition schematic diagram of system；
The side reclaiming hydrocarbon mixture from polyolefin row's torch gas that Fig. 2 provides for this utility model the second embodiment
The flow chart of method.
Detailed description of the invention
For the ease of understanding this utility model, below with reference to relevant drawings, this utility model is carried out more comprehensively
Description.Accompanying drawing gives better embodiment of the present utility model.These are only of the present utility model excellent
Select embodiment, not thereby limit the scope of the claims of the present utility model, every utilize this utility model description
And the equivalent structure made of accompanying drawing content or equivalence flow process conversion, or it is relevant to be directly or indirectly used in other
Technical field, is the most in like manner included in scope of patent protection of the present utility model.
Unless otherwise defined, all of technology used herein and scientific terminology with belong to of the present utility model
The implication that those skilled in the art are generally understood that is identical.Institute in description of the present utility model herein
The term used is intended merely to describe the purpose of specific embodiment, it is not intended that in limiting this utility model.
Term as used herein " and/or " include the arbitrary and all of one or more relevant Listed Items
Combination.
Referring to Fig. 1, this utility model first embodiment provides a kind of and reclaims mixing from polyolefin row's torch gas
The system 100 of hydrocarbon, it include exsiccator 110,121, two grades of plate-fin heat exchangers 122 of one-level plate-fin heat exchanger,
One-level gas-liquid separator 132, three grades of gas-liquid separators 133 of 131, two grades of gas-liquid separators and comprise expanding end
141 and the expansion unit of pressurized end 142.
Described exsiccator 110 is used for receiving the row's torch gas 1 from polyolefin response system (not shown), and
Output first fluid 2；Specifically, the material from upstream process (i.e. polyolefin response system) (i.e. arranges fire
Torch gas, flows stock 1) through described exsiccator 110, its dew points at normal pressure delivers to the separative element that liquefies after being down to-70 DEG C
(include described one-level gas-liquid separator 131, described two grades of gas-liquid separators 132 and three grades of gas-liquid separators
133) carry out liquefaction to separate.
Described one-level plate-fin heat exchanger 121 is used for cooling down described first fluid 2, and exports the first gas-liquid mixture
3.Specifically, described exsiccator 110 processes described in qualified material (i.e. first fluid flows stock 2) feeding
One-level plate-fin heat exchanger 121, through being cooled to-30～-70 DEG C (depending on actual temp forms according to material) step by step
After, send into described one-level gas-liquid separator 131.
In the present embodiment, the first gas-liquid mixture 3 (stream stock 3) of described one-level plate-fin heat exchanger 121 output
Temperature range be-30～-70 DEG C, it is to be understood that actual temp can be according to concrete group of row's torch gas 1
Depending on one-tenth.
Described one-level gas-liquid separator 131 is used for separating the heavy hydrocarbon component in described first gas-liquid mixture 3,
Output second fluid 5 forms the second gas-liquid mixture 15 to described one-level plate-fin heat exchanger 121, and exports
Rich in nitrogen and the 3rd fluid 4 of light hydrocarbon component.Specifically, divide through described one-level gas-liquid separator 131 gas-liquid
, deliver to after described one-level plate-fin heat exchanger 121 rewarming from the liquid phase (i.e. second fluid flows stock 5) obtained
Described three grades of gas-liquid separators 133.
Described two grades of plate-fin heat exchangers 122 are used for cooling down described 3rd fluid 4, and export the 3rd gas-liquid mixture
6.Specifically, gas phase (the i.e. the 3rd fluid, the stream obtained through the gas-liquid separation of described one-level gas-liquid separator 131
Stock 4) send into described two grades of plate-fin heat exchangers 122, through being cooled to-80～-150 DEG C of (actual temp roots step by step
Depending on forming according to material) after, send into described two grades of gas-liquid separators 132.It is understood that described two grades
Depending on the temperature of the stream stock 6 of the plate-fin heat exchanger 122 output particular make-up according to row's torch gas 1.
In the present embodiment, the temperature model of the 3rd gas-liquid mixture 6 of described two grades of plate-fin heat exchangers 122 output
Enclose for-80～-150 DEG C.It is understood that actual temp can be according to the 3rd gas-liquid mixture 6 (stream stock 6)
Particular make-up depending on.
Described two grades of gas-liquid separators 132 are used for separating the light hydrocarbon component in described 3rd gas-liquid mixture 6,
And exporting the 4th fluid 7 and the 5th fluid 8, described 4th fluid 7 order successively is changed by described two step wings
Hot device 122 and described one-level plate-fin heat exchanger 121 form the 6th fluid 10.Specifically, through described two grades of gas
The gas phase (the i.e. the 5th fluid flows stock 8) that liquid/gas separator 132 gas-liquid separation obtains is special through polyolefin tail
The expanding end 141 of described expansion unit expands cooling, returns described two grades of plate-fin heat exchangers 122 and institute successively
State one-level plate-fin heat exchanger 121, provide for the described system 100 reclaiming hydrocarbon mixture from polyolefin row's torch gas
Cold, then sends battery limit (BL) after pressurized end 142 supercharging of described expansion unit.Divide through described two grades of gas-liquids
The liquid phase (the i.e. the 4th fluid flows stock 7) obtained from device 132 gas-liquid separation returns described two step wings successively and changes
Hot device 122 and described one-level plate-fin heat exchanger 121 rewarming, eventually form the 6th fluid 10 (stream stock 10) with
9th fluid (stream stock 17) converges and sends polymerization reaction system back to.
In the present embodiment, described expansion unit comprises expanding end 141 and pressurized end 142, described expanding end 141
For described 5th fluid 8 carries out expanding cooling, output cryogen 11 order successively is by described two grades
Plate-fin heat exchanger 122 and described one-level plate-fin heat exchanger 121 are formed and expand fluid 13, export expansion work simultaneously,
Described pressurized end 142 receives the expansion work of described expanding end 141 output, and is the supercharging of described expansion fluid 13,
Export the 7th fluid 14.Preferably, described expansion unit is Turbine expansion unit, it is to be understood that institute
State expand unit can Turbine expansion unit that more preferably polyolefin tail is special, comprise described expansion
End 141 and described pressurized end 142；It is 1.1～1.6MPa that described expanding end 141 expands front pressure, after expansion
Pressure is 0.05～0.2MPa, it is to be understood that the expanding end 141 of described expansion unit expands front pressure
With pressure after expansion according to depending on feed pressure.
Described three grades of gas-liquid separators 133 are used for separating the light hydrocarbon component in described second gas-liquid mixture 15,
Exporting the 8th fluid 16 and the 9th fluid 17, wherein said 9th fluid 17 converges with described 6th fluid 10
After be back to described polyolefin response system.Specifically, through the gas-liquid separation of described three grades of gas-liquid separators 133
The liquid phase (the i.e. the 8th fluid flows stock 16, based on the heavier hydrocarbon products of C5+ component) obtained sends battery limit (BL),
The gas phase (the 9th fluid flows stock 17) obtained through the gas-liquid separation of described three grades of gas-liquid separators 133 imports stream
Stock 10, i.e. converges send polymerization reaction system back to the 6th fluid 10 (stream stock 10).
Referring to Fig. 2, this utility model the second embodiment provides a kind of and reclaims mixing from polyolefin row's torch gas
The method of hydrocarbon, it comprises the steps:
Row's torch gas 1 drying device 110 of S101, in the future autohemagglutination olefine reaction system delivers to one-level after processing
Plate-fin heat exchanger 121 is lowered the temperature.
Specifically, from the material (i.e. arranging torch gas, flow stock 1) of upstream process (i.e. polyolefin response system)
Through described exsiccator 110, its dew points at normal pressure is down to-70 DEG C, delivers to thereafter described one-level plate-fin heat exchanger 121
Lower the temperature.
Row's torch gas after S102, cooling is delivered to one-level gas-liquid separator 131 and is carried out gas-liquid separation, and output contains
The second fluid 5 of heavy hydrocarbon component, and export the 3rd 4 to two grades of plate-fins of fluid rich in nitrogen and light hydrocarbon component
Heat exchanger 122 forms the 3rd gas-liquid mixture 6.
Specifically, the liquid that the row's torch gas after cooling obtains through the gas-liquid separation of described one-level gas-liquid separator 131
Phase (i.e. second fluid flows stock 5) and gas phase (the i.e. the 3rd fluid flows stock 4), wherein liquid phase is through described one
After level plate-fin heat exchanger 121 rewarming, deliver to described three grades of gas-liquid separators 133；Gas phase sends into described two steps
Wing heat exchanger 122, after being cooled to-80～-150 DEG C (depending on actual temp forms according to material) step by step,
Send into described two grades of gas-liquid separators 132.
S103, described 3rd gas-liquid mixture 6 are delivered to two grades of gas-liquid separators 132 and are carried out gas-liquid separation, shape
The 4th fluid 7 become order successively is by described two grades of plate-fin heat exchangers 122 and described one-level plate-fin heat exchanger
121 form the 6th fluid 10, after the expanding end 141 of the 5th expanded unit of fluid 8 of formation expands cooling,
Order is formed by described two grades of plate-fin heat exchangers 122 and described one-level plate-fin heat exchanger 121 and expands stream successively
Body 13, forms the 7th fluid 14 after described expansion fluid 13 intensified end 142 supercharging.
Specifically, the gas phase that obtains through the gas-liquid separation of described two grades of gas-liquid separators 132 (the i.e. the 5th fluid,
Stream stock 8) expand cooling through the expanding end 141 of the special described expansion unit of polyolefin tail, return institute successively
State two grades of plate-fin heat exchangers 122 and described one-level plate-fin heat exchanger 121, for described from polyolefin row's torch gas
The system 100 reclaiming hydrocarbon mixture provides cold, then send after pressurized end 142 supercharging of described expansion unit
Go out battery limit (BL).Through the liquid phase (the i.e. the 4th fluid flows stock 7) that the gas-liquid separation of described two grades of gas-liquid separators 132 obtains
Return described two grades of plate-fin heat exchangers 122 and described one-level plate-fin heat exchanger 121 rewarming successively, eventually form
6th fluid 10 (stream stock 10) converges send polymerization reaction system back to the 9th fluid (stream stock 17).
S104, described second fluid 5 export the second gas-liquid after described one-level plate-fin heat exchanger 121 is lowered the temperature
15 to three grades of gas-liquid separators of mixture 133 carry out gas-liquid separation, export the 8th fluid 16, and export described
9th fluid 17 is back to described polyolefin response system after converging with described 6th fluid 10.
Specifically, the liquid phase that obtains through the gas-liquid separation of described three grades of gas-liquid separators 133 (the i.e. the 8th fluid,
Stream stock 16, based on the heavier hydrocarbon products of C5+ component) send battery limit (BL), through described three grades of gas-liquid separators 133
The gas phase (the 9th fluid flows stock 17) that gas-liquid separation obtains imports stream stock 10, i.e. with the 6th fluid 10 (stream
Stock 10) converge and send polymerization reaction system back to.
Embodiment
The measured value of row's torch gas duty parameter of certain petro-chemical corporation's polyethylene production device is as shown in table 1.Its
Pressure limit is 1.3MPa (G), and temperature is 40 DEG C, and flow is 2030Nm3/h.
Table 1 row's torch gas composition measured value (v%)
Row's torch gas (stream stock 1) initially enters exsiccator 110 and processes, and treats that dew point reaches about-70 DEG C, send
To one-level plate-fin heat exchanger 121, temperature drops to-40 DEG C step by step, is then sent to one-level gas-liquid separator 131.
Through the liquid phase (stream stock 5) of one-level gas-liquid separator 131 isolated after one-level plate-fin heat exchanger 121 rewarming,
Deliver to three grades of gas-liquid separators 133.Gas phase (stream stock 17) through three grades of gas-liquid separator 133 isolateds
Import stream stock 10, through the liquid phase (stream stock 16, heavy hydrocarbons product) of three grades of gas-liquid separator 133 isolateds
Send battery limit (BL).Two grades of plate-fin heat exchangers are delivered to through one-level gas-liquid separator 131 isolated gas phase (stream stock 4)
122 continue to be cooled to-125 DEG C, are then sent to two grades of gas-liquid separators 132.Through two grades of gas-liquid separators 132
The liquid phase (stream stock 7) of isolated is successively through two grades of plate-fin heat exchangers 122, one-level plate-fin heat exchanger 121 again
Temperature, returns polymerization reaction system (stream stock 10, light hydrocarbon product), separates through two grades of gas-liquid separators 132
To the expanding end 141 of gas phase (stream stock 8) expanded unit expand and be cooled to-138 DEG C after, sequentially pass through two
Level plate-fin heat exchanger 122, one-level plate-fin heat exchanger 121, provide necessary cold for system, abundant rewarming,
Battery limit (BL) (stream stock 14) is sent after pressurized end 142 supercharging of the most expanded unit.
Row's torch gas 1 carries out deep cooling through the described system 100 reclaiming hydrocarbon mixture from polyolefin row's torch gas and divides
After processing, respectively obtain the tail gas (stream stock 14) based on nitrogen, the heavy hydrocarbons product (stream based on C5+
Stock 16) and light hydrocarbon product based on ethylene (flowing stock 11).Wherein the parameter of stream stock 14 is: pressure
0.29MPa (G), temperature 30 DEG C, flow are 1506Nm3/h, and its composition is as shown in table 2；Wherein stream stock 16
Parameter be pressure 0.085MPa (G), temperature 30 DEG C, flow be 94Nm3/h, its composition is as shown in table 3；
The parameter wherein flowing stock 11 is pressure 0.075MPa (G), temperature 40 DEG C, flow are 430Nm3/h, its group
Become as shown in table 4.
Table 2 tail gas composition (v%)
Table 3 heavy hydrocarbons product composition (v%)
Table 4 light hydrocarbon product composition (v%)
It addition, the hexane content in stream stock 4 is down to 74ppm, greatly reduce two grades of plate-fin heat exchangers 122
There is the probability of frozen block.As can be seen here, the described system 100 reclaiming hydrocarbon mixture from polyolefin row's torch gas
(one-level gas-liquid separator 132, three grades of gas-liquids of 131, two grades of gas-liquid separators are divided to use multiple flash chamber
From device 133) design there is goodish effect really.
The system reclaiming hydrocarbon mixture from polyolefin row's torch gas that the utility model proposes has the advantage that
One, the design of multiple flash chamber have both sides benefit: on the one hand, the 3rd gas-liquid separator obtains
To liquid-phase product based on heavy hydrocarbon, this product transmitting system, alleviate the heavy hydrocarbon enrichment at response system；
On the other hand, utilize the first gas-liquid separator the most first to isolate heavy hydrocarbon, reduce second
The risk of plate-fin heat exchanger generation frozen block.Two, expand unit design ingenious, utilize expanding end to obtain cold,
Pressurized end has reclaimed again expansion work, the maximized pressure energy utilizing tail gas simultaneously；For traditional method,
In order to ensure that tail gas sends battery limit (BL) smoothly, outlet pressure of expansion machine can not too low (be generally not capable of less than 0.2
MPa (G), is mainly used in overcoming the resistance of downstream line and equipment), which limits what decompressor was obtained in that
Cold；And this utility model is additionally arranged decompressor pressurized end, thus the pressure of expanding end outlet can be as little as
0.05～0.2MPa (G), it means that under conditions of equal feed pressure, the utility model proposes from poly-
The system reclaiming hydrocarbon mixture in alkene row's torch gas obtains more cold than traditional method, and recovering effect is more preferable.
Three, the nitrogen content in tail gas is up to 97%, can directly recycle.
It addition, polyethylene is similar with the tail gas of polypropylene production process composition, identical recovery can be used completely
Method, only difference on design parameter.Therefore the utility model proposes from polyolefin row torch gas
The system reclaiming hydrocarbon mixture is simultaneously suitable for polyethylene and polypropylene row's torch gas and has the discharge being approximated to
Gas recycles.
Meanwhile, the step of the method reclaiming hydrocarbon mixture from polyolefin row's torch gas of described proposition is simple,
Easy to utilize.
Embodiment described above only have expressed several embodiments of the present utility model, its describe more concrete and
In detail, but therefore can not be interpreted as the restriction to this utility model the scope of the claims.It should be pointed out that,
For the person of ordinary skill of the art, without departing from the concept of the premise utility, it is also possible to
Making some deformation and improvement, these broadly fall into protection domain of the present utility model.Therefore, this utility model
The protection domain of patent should be as the criterion with claims.
Claims (5)
1. the system reclaiming hydrocarbon mixture from polyolefin row's torch gas, it is characterised in that including:
Exsiccator (110), it is for receiving the row's torch gas (1) from polyolefin response system, and exports first fluid (2)；
One-level plate-fin heat exchanger (121), it is used for cooling down described first fluid (2), and exports the first gas-liquid mixture (3)；
One-level gas-liquid separator (131), it is used for separating the heavy hydrocarbon component in described first gas-liquid mixture (3), output second fluid (5) to described one-level plate-fin heat exchanger (121) forms the second gas-liquid mixture (15), and exports the 3rd fluid (4) rich in nitrogen and light hydrocarbon component；
Two grades of plate-fin heat exchangers (122), it is used for cooling down described 3rd fluid (4), and exports the 3rd gas-liquid mixture (6)；
Two grades of gas-liquid separators (132), it is used for separating the light hydrocarbon component in described 3rd gas-liquid mixture (6), and exporting the 4th fluid (7) and the 5th fluid (8), described 4th fluid (7) order successively forms the 6th fluid (10) by described two grades of plate-fin heat exchangers (122) and described one-level plate-fin heat exchanger (121)；
Comprise expanding end (141) and the expansion unit of pressurized end (142), described expanding end (141) is lowered the temperature for carrying out described 5th fluid (8) expanding, output cryogen (11) order successively is formed by described two grades of plate-fin heat exchangers (122) and described one-level plate-fin heat exchanger (121) and expands fluid (13), export expansion work simultaneously, described pressurized end (142) receives the expansion work that described expanding end (141) exports, and be the supercharging of described expansion fluid (13), export the 7th fluid (14)；
Three grades of gas-liquid separators (133), it is used for separating the light hydrocarbon component in described second gas-liquid mixture (15), exporting the 8th fluid (16) and the 9th fluid (17), wherein said 9th fluid (17) and described 6th fluid (10) are back to described polyolefin response system after converging.
2. from polyolefin row's torch gas, reclaim as claimed in claim 1 the system of hydrocarbon mixture, it is characterised in that the temperature range of the first gas-liquid mixture (3) that described one-level plate-fin heat exchanger (121) exports is-30～-70 DEG C.
3. from polyolefin row's torch gas, reclaim as claimed in claim 1 the system of hydrocarbon mixture, it is characterised in that the temperature range of the 3rd gas-liquid mixture (6) that described two grades of plate-fin heat exchangers (122) export is-80～-150 DEG C.
4. from polyolefin row's torch gas, reclaim the system of hydrocarbon mixture as claimed in claim 1, it is characterised in that described expansion unit is Turbine expansion unit.
5. from polyolefin row's torch gas, reclaim the system of hydrocarbon mixture as claimed in claim 1, it is characterised in that before described expanding end (141) expands, pressure is 1.1～1.6MPa, and after expansion, pressure is 0.05～0.2MPa.
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| CN201620049954.6U CN205730772U (en) | 2016-01-19 | 2016-01-19 | System for recovering mixed hydrocarbon from polyolefin discharge flare gas |
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| CN201620049954.6U CN205730772U (en) | 2016-01-19 | 2016-01-19 | System for recovering mixed hydrocarbon from polyolefin discharge flare gas |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105536425A (en) * | 2016-01-19 | 2016-05-04 | 北京优工科技有限公司 | System and method for recovering mixed hydrocarbon from polyolefin discharged flare gas |
| CN107513005A (en) * | 2017-09-27 | 2017-12-26 | 中科瑞奥能源科技股份有限公司 | The technique and system of ethene, iso-butane and nitrogen are reclaimed from polyethylene engineering tail gas |
| CN109621685A (en) * | 2019-01-31 | 2019-04-16 | 滨化集团股份有限公司 | A kind of technique that deep cooling adds carbon fiber adsorption and catalytic combustion processing chlorohydrination tail gas |
| EP3444019A4 (en) * | 2016-12-13 | 2020-09-09 | Dalian Eurofilm Industrial Ltd. | Method for recycling polyolefin tail gas |
| CN112473331A (en) * | 2020-11-27 | 2021-03-12 | 东明前海化工有限公司 | Continuous method polypropylene device tail gas processing apparatus |
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2016
- 2016-01-19 CN CN201620049954.6U patent/CN205730772U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105536425A (en) * | 2016-01-19 | 2016-05-04 | 北京优工科技有限公司 | System and method for recovering mixed hydrocarbon from polyolefin discharged flare gas |
| EP3444019A4 (en) * | 2016-12-13 | 2020-09-09 | Dalian Eurofilm Industrial Ltd. | Method for recycling polyolefin tail gas |
| CN107513005A (en) * | 2017-09-27 | 2017-12-26 | 中科瑞奥能源科技股份有限公司 | The technique and system of ethene, iso-butane and nitrogen are reclaimed from polyethylene engineering tail gas |
| CN107513005B (en) * | 2017-09-27 | 2022-11-15 | 中科瑞奥能源科技股份有限公司 | Process and system for recovering ethylene, isobutane and nitrogen from polyethylene engineering tail gas |
| CN109621685A (en) * | 2019-01-31 | 2019-04-16 | 滨化集团股份有限公司 | A kind of technique that deep cooling adds carbon fiber adsorption and catalytic combustion processing chlorohydrination tail gas |
| CN112473331A (en) * | 2020-11-27 | 2021-03-12 | 东明前海化工有限公司 | Continuous method polypropylene device tail gas processing apparatus |
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