CN105085146B - The process for purification and refining system of polymerization-grade propylene are made up of refinery's crude propylene - Google Patents
The process for purification and refining system of polymerization-grade propylene are made up of refinery's crude propylene Download PDFInfo
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Abstract
The present invention discloses a kind of process for purification that polymerization-grade propylene is made up of refinery's crude propylene, and refinery's crude propylene is sequentially passed through the treatment of following steps：1) it is dehydrated with solid caustic soda tower, is taken off H2S, de- CO2；2) then be re-fed into desulfurization mechanism removing COS and H2S；3) being removed with lightness-removing column includes CO, O2In interior light component；4) propylene after light component will be removed again send into molecular sieve dehydration；5) and then with the separating methanol bed for being provided with top bed and bottom bed processed：Propylene is entered by the bottom of separating methanol bed, through the Selexsorb CD catalyst removals water and methyl alcohol of bottom bed；Propylene after methanol removal is qualified continues through the Selexsorb COS catalyst removals CO of top bed2It is extremely qualified；6) propylene feeding dearsenification tank is carried out into dearsenification.Process for purification of the invention, flow scheme design is unique, and energy consumption is low, refinery's crude propylene can be carried out into complete refining spearation, obtains high purity extractive propylene, is entirely capable of meeting the demand of continuity method polymarization method for prodcing polyacrylates.
Description
Technical field
The present invention relates to the process for purification technical field of refinery's crude propylene, more particularly to one kind be made up of refinery's crude propylene it is poly-
Close the process for purification and refining system of level propylene.
Background technology
At present, Chinese oil refining enterprise is large number of, and up to 4.6 hundred million tons/year, refinery exhaust contains largely national refinery's total capacity
Propylene, according to statistics, crude propylene total amount is up to 10,000,000 tons/year.A large amount of crude propylenes can only be used as cheap fuel gas, and fuel
Gas can discharge a large amount of CO2Gas, so this way one of prior art influences the performance of enterprises, two ask also bringing environmental protection
Topic, thus crude propylene is used to being polymerized produce the huge market demand, added value polypropylene (abbreviation PP) product high will be into
It is a kind of trend.
But crude propylene contains a large amount of exceeded water, oxygen, alcohols, sulfide, nitrogen oxides, phosphide and micro arsenic
The impurity such as compound, especially the in poor quality trend of current processing crude oil so that the impurity content in crude propylene increases in species,
The increased trend of concentration.The propylene gas major part that current oil refining enterprise produces in process is used to add without refining spearation
The fuel gas of hot stove, part propylene gas utilizes added value by being used for batch tank method polymarization method for prodcing polyacrylates, propylene after simple qi leel
It is low.Requirement of Ziegler-Natta (Z-N) catalyst of propylene polymerization to above-mentioned impurity is very harsh, it is desirable to which impurity content is low
In 1ppmv, so wanting for producing polypropylene, it is necessary to be refined to crude propylene.There is oil refining to look forward to successively in recent years
Propylene is obtained polymer grade purity by industry after essence is separated, for continuity method PP Production Technology.
The refined mode of crude propylene has gas phase high temperature to refine at present, two kinds of techniques of normal temperature liquid-phase refining.Wherein, gas phase is high
Because high energy consumption, catalyst typically uses copper catalyst to warm process for refining, and absorption property is not high, catalyst needs regular regeneration etc. to lack
Fall into and be restricted.Another mode --- normal temperature liquid-phase refining method is increasingly subject to the development of various catalyst for refining
The attention of each manufacturer with use, but constituent parts use normal temperature liquid-phase refining method flow it is different, be not quite similar.Because flow
Arrange and catalyst choice difference, refined effect, the size of energy consumption be different from, and the influence to catalyst activity is larger.
As can be seen here, there is provided a kind of that refinery's crude propylene is removed into corresponding impurity, the refined side of polymerization-grade propylene is finally given
Method, refining effect is good, less energy consumption, and this is the current technical issues that need to address in this area.
The content of the invention
In view of this, refinery's crude propylene is taken off successively by specifically refined program it is an object of the invention to provide one kind
Except corresponding impurity, the process for purification of polymerization-grade propylene is finally given, refining effect is good, less energy consumption, can to greatest extent remove refining
Impurity component in factory's propylene, the need for meeting polymerization technique.Based on this, the present invention also provides one kind and is made up of refinery's crude propylene
The refining system of polymerization-grade propylene.
To solve above technical problem, the technical scheme is that：
A kind of process for purification that polymerization-grade propylene is made up of refinery's crude propylene, following steps are sequentially passed through by refinery's crude propylene
Treatment：
1) with the dehydration of solid caustic soda tower, H2S、CO2；
2) it is re-fed into desulfurization mechanism and removes COS and H2S；
3) being removed with lightness-removing column includes CO, O2In interior light component；
4) propylene after light component will be removed again send into molecular sieve dehydration；
5) and then with the separating methanol bed for being provided with top bed and bottom bed processed：Propylene by separating methanol bed bottom
Into through Selexsorb CD catalyst removals water and methyl alcohol that the bottom bed is set；Propylene after methanol removal is qualified
Continue on through the Selexsorb COS catalyst removals CO that the top bed is set2It is extremely qualified；
6) by propylene feeding dearsenification tank removing arsenic.
Preferably, step 1) it is specially：Refinery's crude propylene is removed into free water by propylene coalescer, then removing is free
The propylene of water flows through the dehydration of solid caustic soda tower, H2S、CO2。
Preferably, step 2) in desulfurization mechanism include COS processors and H2S processors, step 2) it is specially：Will be from admittedly
Washing tower (for removing CO2) propylene feeding COS processor removing COS out, the propylene for removing COS flows through H2S processors remove H2S。
Preferably, step 3) in, the propylene after desulfurization is preheated through propylene feed heat exchanger again after flowing through protection filter, and
Processed into lightness-removing column afterwards.
Preferably, the preheating temperature is 45 DEG C~75 DEG C.
Preferably, step 4) in, the molecular sieve is 3A molecular sieves.
It is of the invention it is a kind of the refining system of polymerization-grade propylene is made up of refinery's crude propylene, including the following dress being sequentially connected
Put：
For to refinery's crude propylene removing water, H2S、CO2Solid caustic soda tower；
For removing COS and H to the propylene from after solid caustic soda tower outflow2The desulfurization mechanism of S；
Include CO, O for the propylene removing to being flowed out from the desulfurization mechanism2In the lightness-removing column of interior light component；
For the molecular sieve of the propylene dehydration to being flowed out from the lightness-removing column；
For propylene removing water, methyl alcohol, CO to being flowed out from the molecular sieve2Separating methanol bed, the separating methanol bed
It is provided with top bed and bottom bed：The bottom bed is provided with the Selexsorb CD catalyst for removing water and methyl alcohol；
The top bed is provided with for removing CO2Selexsorb COS catalyst；
For the dearsenification tank to the propylene dearsenification from separating methanol bed outflow.
Preferably, the solid caustic soda tower, desulfurization mechanism, molecular sieve, separating methanol bed, dearsenification tank are fixed bed.
Preferably, the molecular sieve is 3A molecular sieves.
Preferably, the desulfurization mechanism includes de- COS tanks and de- H2S tanks
Compared with prior art, process for purification of the invention has the following advantages that：
1st, carried out from suitable step and with specific precedence, design is unique：Process for purification of the invention is first used
Solid caustic soda adsorbs substantial amounts of free water, then carries out physical absorption dehydration with 3A molecular sieves, is finally entered with Selexsorb CD catalyst
Row chemical dehydration, requirement is reached by the water content in raw material propylene after three-level dehydration；Separating methanol, CO2Separating methanol bed be placed in
After desulfurization mechanism, lightness-removing column, the CO of sweetening process generation on the one hand can be removed2Accessory substance, another aspect lightness-removing column is removed
CO, O2De- CO can be effectively protected Deng impurity2The Selexsorb COS catalyst of bed.
2nd, in process for purification of the invention, other use fixed bed in addition to lightness-removing column, and energy consumption is low.
3rd, the removable dopant species of process for purification of the invention are more, polishing capability is strong, can be by contained by current crude propylene
All kinds of impurity H2O、O2、CO、CO2、CH3OH、H2S、COS、PH3、NH3, the impurity such as arsenide and chloride impurity effectively remove,
Fully meet the need of the various production technologies of polyolefin, the various preparing process of polyolefin catalyst and prepolymerization technology safety in production
Will.
4th, further, bed catalyst of the present invention, 3A molecular sieves and water/renewable repetition of methyl alcohol process device
Use, other beds are not required to regeneration.Each bed long service life, up to 5~8 years, average annual low cost.
In sum, process for purification of the invention, flow scheme design is unique, and energy consumption is low, can carry out refinery's crude propylene
Full refining spearation, obtains high purity extractive propylene, is entirely capable of meeting the demand of continuity method polymarization method for prodcing polyacrylates.
Brief description of the drawings
Fig. 1 is the structural representation of the refining system that the present invention is made up polymerization-grade propylene of refinery's crude propylene.
Specific embodiment
In order that those skilled in the art more fully understands technical scheme, below by specific embodiment pair
The present invention is described in further detail.
Substantial amounts of small molecule gaseous material can be produced in petroleum refining process, wherein containing H2、CH4、C2H4、C2H6、C3H6、
C3H8Etc. component, separated by simple gas, crude propylene can be obtained, a working ability is ten million ton/year of oil refining of crude oil
Enterprise, produces about 20~250,000 tons of propylene per year.Usually, the crude propylene material composition that oil refining gas separation unit is obtained after separating is as follows：
| Project | Unit | Battery limit (BL) is supplied |
| Propylene | Vol%Min. | 99.5 |
| Methane+ethane+propane | Vol%Max | 0.5 |
| Butylene+butane | ppmv Max | 10 |
| Ethene | ppmv Max | 100 |
| Acetylene+allylene+the butadiene of allene+1,3 (unsaturation hydrocarbon) | wt ppm Max | 10 |
| Acetylene | ppmv Max | 5 |
| Hydrogen | ppmv Max | 5 |
| CO | ppmv Max | 10 |
| ppmv Max | 15 | |
| Oxygen | ppmv Max | 10 |
| Water | ppmv Max | 300 |
| Methyl alcohol | ppmv Max | 5 |
| ppmv Max | 5 | |
| COS | ppmv Max | 5 |
| Total sulfur | ppm wt Max | 15 |
| Arsenic hydride | ppmv Max | 0.03 |
| ppmv Max | 0.03 | |
| ppmv Max | 5 | |
| Chloride | ppmv Max | 1 |
Impurity content requirement of the polymerisation Ziegler-Natta System Catalysts to propylene feedstocks is very strict, refines
Each impurity content is as follows before entering reactor afterwards：
| Project | Unit | After refined |
| Propylene | Vol%Min. | 99.5 |
| Methane+ethane+propane | Vol%Max | 0.5 |
| Butylene+butane | ppmv Max | 10 |
| Ethene | ppmv Max | 100 |
| Acetylene+allylene+the butadiene of allene+1,3 (unsaturation hydrocarbon) | wt ppm Max | 10 |
| Acetylene | ppmv Max | 5 |
| Hydrogen | ppmv Max | 5 |
| CO | ppmv Max | 0.15 |
| ppmv Max | 0.48 | |
| Oxygen | ppmv Max | 0.66 |
| Water | ppmv Max | 1.2 |
| Methyl alcohol | ppmv Max | 0.5 |
| ppmv Max | 0.25 | |
| COS | ppmv Max | 0.07 |
| Total sulfur | ppm wt Max | 0.3 |
| Arsenic hydride | ppmv Max | 0.03 |
| ppmv Max | 0.03 | |
| ppmv Max | 0.5 | |
| Chloride | ppmv Max | 1 |
It is an object of the present invention to provide one kind is by H in refinery's crude propylene2O、O2、CO、CO2、CH3OH、H2S、COS、PH3、
NH3, the impurity removal such as arsenide and chloride and obtain the process for purification of polymerization-grade propylene raw material, by process for purification of the present invention
The propylene feedstocks obtained after treatment, disclosure satisfy that the various polymerization techniques of Ziegler-Natta catalyst system are (vapor phase method, molten
Liquid method, slurry process) polymerization requirement.
The technical scheme is that by a series of order rectification flows：Refinery's crude propylene is passed sequentially through into solid caustic soda removing
Free water, de- cos (COS) processor removing sulphur, lightness-removing column removing CO/O2It is micro etc. what light component, molecular sieve removing were adsorbed
Water/methyl alcohol, separating methanol bed methanol removal, CO2, it is last micro amount of arsenic is removed by dearsenification tank again, the propylene after refining reaches
Polymer grade chemical purity, eventually enters into qualified tank field or is sent directly into reactor, does not interfere with catalyst activity or causes reaction
The inactivation of catalyst.
Process for purification of the invention is described as follows：
1st, solid caustic soda dehydration
Battery limit (BL) carrys out propylene and removes free water by propylene coalescer, and the propylene overflow for removing free water goes out coalescer, collects
Free water arrange to alkali liquid tank (normal temperature, normal pressure).The propylene for removing free water flows through solid caustic soda tower, reduce propylene component reclaimed water,
CO2、H2The content of S, wherein water content are reduced to below 100ppm, CO by 200ppm~400ppm2By 15ppm~20ppm reductions
To below 5ppm, H2S is reduced to below 1.5ppm by 5ppm~10ppm, and solid caustic soda is dissolved due to water suction, through the cone of solid caustic soda tower bottom
Shape tank is discharged into alkali liquid tank (normal temperature, normal pressure).
2nd, desulfurization
Propylene from after the treatment of solid caustic soda tower out enters COS processors and removes COS, and desulfurization bed two can series, parallel behaviour
Make.There is following reaction in COS and water：
COS+H2O-CO2+H2S
COS processors conversion ratio is 99%, and by processor, COS drops to below 0.05ppm, water by 5ppm~6ppm
Content slightly declines, H2S increases to 6.5ppm by 1.5ppm.
The propylene for removing COS flows through H2S processors remove H2S, H2S is qualified.
3rd, CO, O are taken off2Etc. light component
Propylene after desulfurization flows through tower protection filter, and after being preheated through propylene feed heat exchanger, into lightness-removing column, propylene takes off
Light tower bottom is provided with reboiler, and in evaporator overhead condenser partial condensation, propylene enters propylene to lightness-removing column overhead vapor after condensation
Return tank, through propylene backflow pumped back lightness-removing column, inert gas such as hydrogen, CO, O without condensation2Etc. being emitted into device torch
The condenser of the washer of system or device liquid propylene recovery unit, bottom of towe propylene exchanges heat through bottom of towe propylene pump, propylene feed
Device and PPU bottom coohng devices, are sent to 3A molecular sieves to be further dehydrated.After lightness-removing column, hydrogen in propylene, methane, ethane,
CO、O2Qualified etc. component, water content drops to below 20ppm by 90ppm~150ppm.
4th, 3A molecular sieve dehydrations
Further it is dehydrated into 3A molecular sieves from lightness-removing column propylene out, mol sieve beds two, can series and parallel behaviour
Make, by after molecular sieve dehydration, water content is reduced to below 10ppm by 20ppm or so in propylene.
5th, dehydration/methyl alcohol/de- CO2
Separating methanol bed is filled with 2 layers of catalyst：Selexsorb COS catalyst, Selexsorb CD catalyst, difference position
In top bed, bottom bed.
Pending propylene is entered by separating methanol bed bottom, by the Selexsorb CD catalyst of bottom bed, removes first
Alcohol, also can further remove chemical absorbed water.By after the bed of eparating methanol tower bottom, water/methyl alcohol is qualified, water be down to 1.0ppm with
Under；
Then propylene continues through the Selexsorb COS catalyst of top bed, removes CO2It is extremely qualified.
6th, dearsenification
After propylene finally enters dearsenification tank removing arsenic, propylene refining is qualified, can meet the demand of polyplant.
Six steps of propylene refining have succession in the present invention, can not arbitrarily replacing is sequentially.The refined bed in part is renewable
Recycling.3A molecular sieve beds, water/renewable reuse of methyl alcohol process device.Regeneration is purged using hot nitrogen, makes to be adsorbed in bed
Material desorption, bed catalyst renewable reuse in service life periodic regime；COS、H2The suction of S, arsenic processor
Attached dose can not regenerate.All bed catalysts carry out replacing treatment after more than usage cycles.
Process for purification embodiment
The present embodiment is applied to certain 200,000 tons/year of propylene refinings of gas-phase polymerization polypropylene device, the essence in the present embodiment
Method processed comprises the following steps：
1st, solid caustic soda dehydration
Refinery's crude propylene that battery limit (BL) comes removes free water by propylene coalescer, and the propylene overflow for removing free water goes out propylene
Coalescer, the free water of collection is arranged to alkali liquid tank (normal temperature, normal pressure).The propylene for removing free water flows through solid caustic soda tower.Water suction dissolving
Solid caustic soda afterwards, alkali liquid tank (normal temperature, normal pressure) is discharged into through the tapered shaped can of solid caustic soda tower bottom.
2nd, desulfurization
Enter COS processors from solid caustic soda tower propylene out and remove COS, COS processors can series, parallel.In COS treatment
In device, COS reacts to remove COS with water.The propylene for removing COS flows through H2S processors remove H2S, H2S is qualified.
In the present embodiment, de- COS tanks used and de- H2The material of S tanks is low temperature carbon steel.De- COS tanks and de- H2The chi of S tanks
It is very little to be designed according to actual conditions.
3rd, CO, O are taken off2Etc. light component
Propylene after desulfurization flows through tower protection filter, and after being preheated through propylene feed heat exchanger, into lightness-removing column, propylene takes off
Light tower is provided with reboiler, and in evaporator overhead condenser partial condensation, propylene flows back lightness-removing column overhead vapor into propylene after condensation
Tank, through propylene backflow pumped back lightness-removing column, inert gas such as hydrogen, CO, O without condensation2Etc. being emitted into device liquid propylene
The condenser of the washer of recovery unit, bottom of towe propylene through bottom of towe propylene pump, through propylene feed heat exchanger and bottom coohng device (40
DEG C), after lightness-removing column, hydrogen, methane, ethane, CO, O in propylene2Qualified etc. component, water content declines.It is then delivered to molecular sieve
Adsorbent bed is further dehydrated.
In the present embodiment, lightness-removing column uses valve plate, and material is carbon steel, and the size of lightness-removing column can be entered according to actual conditions
Row design.
4th, 3A molecular sieve dehydrations
Further it is dehydrated into 3A molecular sieves from lightness-removing column propylene out, D-609A/B can connect, can be in parallel.
In the present embodiment, 3A molecular sieve tanks material used is low temperature carbon steel, and the size of 3A mol sieve beds can be according to reality
Border situation is designed.
5th, dehydration/methyl alcohol/de- CO2
Propylene dehydration/methyl alcohol/de- CO2Realized by separating methanol bed, separating methanol bed filling two-layer catalyst, respectively positioned at upper
Portion's bed, bottom bed, propylene are entered by bottom bed, by the Selexsorb CD catalyst of bottom bed, remove water/first
Alcohol, water/methyl alcohol is qualified.Propylene after methyl alcohol is qualified continues through the Selexsorb COS catalyst of separating methanol bed top bed,
Removing CO2It is extremely qualified.
In the present embodiment, the material of separating methanol bed used is low temperature carbon steel, and bed size can be designed according to actual conditions.
6th, dearsenification
Propylene finally enters dearsenification tank removing arsenic, by after dearsenification tank, propylene refining is qualified.
In the present embodiment, dearsenification tank material low temperature carbon steel used, the size of dearsenification tank can be designed according to actual conditions.
In the present embodiment, molecular sieve used and water/methyl alcohol process device are renewable, and nitrogen is heated through regenerating hot-air heater
Afterwards, into processor, discharge gas is first emitted into flare system, treats the qualified heel row air of combustible gas.And COS, H2S, arsenic processor
Adsorbent can not regenerate, but processor is equipped with propylene removing when drying and unload bed when hot nitrogen pipeline is loaded for the initial stage, urges
Agent is to being changed after the replacement cycle.
By after above-mentioned PROCESS FOR TREATMENT, battery limit (BL) propylene obtains refined purification, purified propylene such as following table meets propylene polymerization and wants
Ask.
Refining system embodiment
Referring to Fig. 1, the refining system of the present embodiment is applied to the propylene essence of certain 200,000 tons/year of gas-phase polymerization polypropylene device
System, it includes the solid caustic soda tower 1, desulfurization mechanism 2, lightness-removing column 3, molecular sieve 4, the separating methanol bed 5, dearsenification tank 6 that are sequentially connected, refined
During, refinery's crude propylene sequentially passes through solid caustic soda tower 1, desulfurization mechanism 2, lightness-removing column 3, molecular sieve 4, separating methanol bed 5, dearsenification tank 6
After treatment, refined propylene is finally given, detailed process can be found in the embodiment of process for purification, and here is omitted.
Wherein, solid caustic soda tower 1, desulfurization mechanism 2, lightness-removing column 3, molecular sieve 4, the structure of dearsenification tank 6 can select prior art
In conventional equipment.
Wherein, the structure of separating methanol bed 5 is divided into top bed and bottom bed, and top bed and bottom bed are filled out set respectively
Different catalyst.
In the present embodiment, molecular sieve 4 preferably uses 3A molecular sieves, in other embodiments, however it is not limited to such molecule
Sieve.
The above is only the preferred embodiment of the present invention, it is noted that it is right that above-mentioned preferred embodiment is not construed as
Limitation of the invention, protection scope of the present invention should be defined by claim limited range.For the art
For those of ordinary skill, without departing from the spirit and scope of the present invention, some improvements and modifications can also be made, these change
Enter and retouch and also should be regarded as protection scope of the present invention.
Claims (9)
1. a kind of process for purification that polymerization-grade propylene is made up of refinery's crude propylene, it is characterised in that pass through refinery's crude propylene successively
Cross the treatment of following steps：
1) refinery's crude propylene is removed into free water by propylene coalescer, then the propylene for removing free water is flowed through into solid caustic soda tower and taken off
Water, H2S、CO2；The dehydration, H2S、CO2The water content of propylene stream is reduced to below 100ppm, CO by 200ppm~400ppm afterwards2
Below 5ppm, H are reduced to by 15ppm~20ppm2S is reduced to below 1.5mmp by 5ppm~10ppm；
2) it is re-fed into desulfurization mechanism and removes COS and H2S；The removing COS and H2The COS contents of propylene stream are by 5ppm~6ppm after S
It is reduced to below 0.05ppm, H2S increases to 6.5ppm by 1.5ppm；
3) being removed with lightness-removing column includes CO, O2In interior light component；
4) propylene after light component will be removed again send into molecular sieve dehydration；The water content of propylene stream is left by 20ppm after the dehydration
The right side is reduced to below 10ppm；
5) and then with the separating methanol bed for being provided with top bed and bottom bed processed：Propylene is entered by the bottom of separating methanol bed
Enter, through Selexsorb CD catalyst removals water and methyl alcohol that the bottom bed is set；The water of propylene stream after the removing water
Content is reduced to below 1.0ppm；Propylene after methanol removal is qualified continues on through the Selexsorb that the top bed is set
COS catalyst removals CO2It is extremely qualified；
6) by propylene feeding dearsenification tank removing arsenic.
2. the process for purification of polymerization-grade propylene is made up of refinery's crude propylene as claimed in claim 1, it is characterised in that step 2)
In desulfurization mechanism include COS processors and H2S processors, step 2) it is specially：Propylene from solid caustic soda tower out is sent into COS
Processor removes COS, and the propylene for removing COS flows through H2S processors remove H2S。
3. the process for purification of polymerization-grade propylene is made up of refinery's crude propylene as claimed in claim 1, it is characterised in that step 3)
In, the propylene after desulfurization is preheated through propylene feed heat exchanger again after flowing through protection filter, is then processed into lightness-removing column.
4. the process for purification of polymerization-grade propylene is made up of refinery's crude propylene as claimed in claim 3, it is characterised in that described pre-
Hot temperature is 45 DEG C~75 DEG C.
5. the process for purification of polymerization-grade propylene is made up of refinery's crude propylene as claimed in claim 1, it is characterised in that step 4)
In, the molecular sieve is 3A molecular sieves.
6. a kind of refining system that polymerization-grade propylene is made up of refinery's crude propylene, it is characterised in that as follows including what is be sequentially connected
Device：
For to refinery's crude propylene removing water, H2S、CO2Solid caustic soda tower；
For removing COS and H to the propylene from after solid caustic soda tower outflow2The desulfurization mechanism of S；
Include CO, O for the propylene removing to being flowed out from the desulfurization mechanism2In the lightness-removing column of interior light component；
For the zeolite fixed-bed reactor of the propylene dehydration to being flowed out from the lightness-removing column；
For propylene removing water, methyl alcohol, CO to being flowed out from the zeolite fixed-bed reactor2Separating methanol bed, the separating methanol bed
It is provided with top bed and bottom bed：The bottom bed is provided with the Selexsorb CD catalyst for removing water and methyl alcohol；
The top bed is provided with for removing CO2Selexsorb COS catalyst；
For the dearsenification tank to the propylene dearsenification from separating methanol bed outflow.
7. the refining system of polymerization-grade propylene is made up of refinery's crude propylene as claimed in claim 6, it is characterised in that described solid
Washing tower (for removing CO2), desulfurization mechanism, separating methanol bed, dearsenification tank are fixed bed.
8. the refining system of polymerization-grade propylene is made up of refinery's crude propylene as claimed in claim 6, it is characterised in that described point
Son sieve fixed bed is 3A zeolite fixed-bed reactors.
9. the refining system of polymerization-grade propylene is made up of refinery's crude propylene as claimed in claim 6, it is characterised in that described de-
Sulphur mechanism includes de- COS tanks and de- H2S tanks.
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| CN107188776B (en) * | 2017-06-09 | 2020-02-21 | 中石化上海工程有限公司 | Method for removing acid impurities in cracking gas of ethylene device |
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| CN113583167A (en) * | 2021-08-27 | 2021-11-02 | 云南云天化石化有限公司 | Device and method for producing propylene-butylene random copolymerization polypropylene by gas phase process |
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| CN101255089A (en) * | 2008-04-03 | 2008-09-03 | 中国石油大学(北京) | Purification technique for producing propylene by refinery plant |
| CN102653505A (en) * | 2011-03-04 | 2012-09-05 | 中国石油化工股份有限公司 | Propylene refining method |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101255089A (en) * | 2008-04-03 | 2008-09-03 | 中国石油大学(北京) | Purification technique for producing propylene by refinery plant |
| CN102653505A (en) * | 2011-03-04 | 2012-09-05 | 中国石油化工股份有限公司 | Propylene refining method |
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| 炼厂丙烯的精制处理;宋龄新;《当代化工》;20091231;第38卷(第6期);596-598 * |
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