CN104109070B - The product separation method of preparing propylene from methanol - Google Patents
The product separation method of preparing propylene from methanol Download PDFInfo
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- CN104109070B CN104109070B CN201310129830.XA CN201310129830A CN104109070B CN 104109070 B CN104109070 B CN 104109070B CN 201310129830 A CN201310129830 A CN 201310129830A CN 104109070 B CN104109070 B CN 104109070B
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Abstract
The present invention relates to the product separation method of a kind of preparing propylene from methanol, mainly solve the technical problem that in prior art, propylene loss is big, technological process is complicated, energy consumption is high；The present invention is by using the product separation method of a kind of preparing propylene from methanol, including following step: provide olefin stream (11)；Olefin stream (11) is divided into gaseous stream I and liquid phase stream I in compressional zone A；Gaseous stream I removes oxygenates and CO in scrubbing section B2, the liquid phase stream I of gas phase hydrocarbon logistics (16) and compressional zone A sends into knockout drum C in the lump；The gaseous stream II degassing phase exsiccator D that knockout drum C flows out, dried for being dried logistics I；It is dried logistics I and knockout tower is sent in dry logistics II in the lump；Knockout tower H overhead stream II, as reactant, is back to the technical scheme of preparing propylene from methanol reactor, preferably solves these problems, can be applicable in the commercial production of preparing propylene from methanol.
Description
Technical field
The present invention relates to the product separation method of a kind of preparing propylene from methanol.
Background technology
Propylene is a kind of demand king-sized basic organic chemical industry raw material, mostlys come from petroleum refining process.Along with
The plaque day by day of petroleum resources is weary, develops and is increasingly caused both at home and abroad by the technology of the non-oil resource such as coal or natural gas production propylene
Attention.By methanol be waste propylene be the novel process being hopeful most to replace petroleum path, be also realize Coal Chemical Industry or
Gas chemical industry is to the effective way of petrochemical industry infiltration and development.Coal or producing synthesis gas from natural gas, then produced methanol by synthesis gas
It is ripe Technology with dimethyl ether.Therefore, prepare, from methanol, the key technology that propylene is olefin hydrocarbon making by coal route.
Methanol-to-olefins complete set technology is made up of reaction technology and isolation technics.Reaction technology is with the development of catalyst and anti-
Device exploitation is answered to be designed as core, with methanol for olefin production mixture；Isolation technics is then with product as raw material, warp
Impurity removal, compress, the process such as separation produces polymer grade ethylene and propylene product, the exploitation of its core separation process and design.
Such as, patent CN202379908U discloses a kind of olefin separation system, and the product gas prepared by methanol is by pre-
Processing means is compressed, and domethanizing column is connected with pretreatment unit, for isolating the hydrocarbon containing C2 and C3 component at the bottom of tower
Class material, the middle part of dethanizer is connected with at the bottom of the tower of domethanizing column, and dethanizer is for by the hydro carbons containing C2 and C3 component
Material is fractionated into the material containing C2 and the material containing C3, and is flowed out from the tower top of dethanizer by the material containing C2, contains
Have at the bottom of the tower from dethanizer of C3 material and flow out；Propylene tower is connected with at the bottom of the tower of dethanizer, and propylene tower is in tower underflow
Going out by the isolated propane of the material containing C3, wherein, propane is back to domethanizing column after cooling as propane washing material
Tower top also circulates, for reducing the temperature of demethanizer column overhead between domethanizing column and propylene tower.This technique needs demethanation
Cryogenic separation, and separating pressure selects higher, causes tower reactor temperature higher so that energy consumption is higher, and this technological process is more multiple
Miscellaneous, propylene recovery rate is less than 99.7%.
Summary of the invention
The technical problem to be solved is the problem that propylene loss is big, technological process is complicated, energy consumption is high, it is provided that one
Planting the product separation method of preparing propylene from methanol, the method has the advantages that propylene recovery rate is high, flow process is simple, energy consumption is low.
For solving above-mentioned technical problem, the technical solution of the present invention is as follows: the product of a kind of preparing propylene from methanol separates
Method, including following step:
A) provide containing H2、CO2、H2O, methane, methanol, ethylene, ethane, propylene, propane, C4 +Alkene thing with dimethyl ether
Stream 11；
B) olefin stream 11 is divided into gaseous stream I 12 and liquid phase stream I 13 in compressional zone A；
C) gaseous stream I 12 removes oxygenates and CO in scrubbing section B2, and it is divided into gas phase hydrocarbon logistics 16
With liquid phase oxygenatedchemicals logistics 15, the liquid phase stream I 13 of gas phase hydrocarbon logistics 16 and compressional zone A sends into knockout drum in the lump
C；
D) the gaseous stream II 18 degassing phase exsiccator D that knockout drum C flows out, dried for being dried logistics I 19；Knockout drum C
The liquid phase stream II 17 flowed out removes liquid phase exsiccator E, dried for being dried logistics II 20, is dried logistics I 19 and dry logistics II
20 send into knockout tower F in the lump；
E) knockout tower F overhead stream I 21 sends into compressor G, for compression logistics 22 after compression, and compression logistics 22 feeding point
From tower H, knockout tower H overhead stream II 24, as reactant, is back to preparing propylene from methanol reactor, knockout tower H tower reactor logistics II
25 deliver to knockout tower J, and knockout tower J overhead stream III 27 is propylene product, and tower reactor logistics III 28 is by-product；
F) knockout tower I is delivered in knockout tower F tower reactor logistics I 23, and knockout tower I overhead stream IV 26 is back to as reactant
Preparing propylene from methanol reactor, knockout tower I tower reactor logistics IV 29 is by-product.
In technique scheme, preferred technical scheme is, in terms of olefin stream 11 percentage by weight, in olefin stream 11
Containing ethylene and the propylene of at least 25%, and propylene content is at least 2 times of ethylene contents.Preferably technical scheme is, with gas phase
Logistics I 12 percentage by weight meter, the oxygen-bearing organic matter of at least 30% contained in gaseous stream I 12 enters liquid phase oxygenatedchemicals
In logistics 15.Preferably technical scheme is, in terms of gaseous stream I 12 percentage by weight, and the CO of at most 1% in gaseous stream I 122
Enter gas phase hydrocarbon logistics 16.Preferably technical scheme is, by weight percentage, is dried logistics I 19 or dry logistics II 20
In the H that contains2O is at most 100ppm.Preferably technical scheme is, by weight percentage, is dried logistics I 19 and dry logistics
The C3 of at least 98% contained in II 20 and following hydro carbons enter in overhead stream I 21；It is dried logistics I 19 and dry logistics II 20
In contain at least 98% C4 and above hydro carbons enter in tower reactor logistics I 23.
Preferably technical scheme is, by weight percentage, containing containing in compression logistics 22 in overhead stream II 24
The C2 of at least 98% and following hydro carbons, contain the C3 hydro carbons of contain in overhead stream II 24 at least 98% in tower reactor logistics II 25.
By weight percentage, overhead stream III 27 contains the propylene product of contain in tower reactor logistics II 25 at least 99.9%, tower reactor
Logistics III 28 contains the propane of contain in overhead stream II 24 at least 99%.Preferably technical scheme is, with percentage by weight
Meter, contains one or more in C4～the C6 hydro carbons of contain in tower reactor logistics I (23) at least 98% in overhead stream IV 26.
In technique scheme, preferred technical scheme is, the operating condition of distillation column F is: tower top pressure is 1.0 ~
1.4MPag, tower top temperature is-5 ~ 15 DEG C, and bottom temperature is 95 ~ 125 DEG C；The operating condition of distillation column H: tower top pressure is 2.0 ~
2.5MPag, tower top temperature is-45 ~-25 DEG C, and bottom temperature is 45 ~ 65 DEG C；The operating condition of distillation column J: tower top pressure is 1.3
~ 1.8MPag, tower top temperature is 25 ~ 40 DEG C, and bottom temperature is 40 ~ 60 DEG C.
Containing H in the olefin stream provided in such scheme2、CO2、H2O, methane, methanol, ethylene, ethane, propylene, third
Alkane, C4 +Any Common sources is can come from the olefin stream of dimethyl ether, generally this olefin stream.
Such scheme under low pressure carries out C to logistics 19 and 203/C4Between cut so that logistics 21 is containing logistics 19 and 20
Middle C3Following components is close to 100%, and energy consumption is low.The lock out operation of distillation column F, propylene is almost without loss.Such scheme is to only
Being compressed C3 and following logistics 21, energy consumption is low；After compression, logistics 22 carries out C2/C3Between cut so that logistics 25 contains
In logistics 22 close to 100% propylene, propylene is almost without loss.Such scheme carries out distillation operation to logistics 25, separates propylene
And propane so that containing the propylene close to 100% in logistics 25 in logistics 27, in logistics 27, purified propylene is more than 99%, dimethyl ether
Content is less than 1 ppm.The separating technology of the preparing propylene from methanol that this programme is provided, the total loss of propylene is about 0.2%, obtains
Preferable technique effect.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of the present invention program.
In Fig. 1,11～29 is olefin stream, and A is compressional zone, and B is scrubbing section, and C is knockout drum, D and E is respectively gas phase and does
Dry device and liquid phase exsiccator, F～J is knockout tower.
In Fig. 1, logistics 11 is divided into gaseous stream 12 and liquid phase stream 13 in compressional zone A, and gaseous stream 12 sends into washing
It is divided into gas phase hydrocarbon logistics 16 and liquid phase containing oxygenatedchemicals logistics 15, gas phase hydrocarbon logistics 16 and compressional zone liquid phase thing after district B
Stream 13 sends into knockout drum C in the lump；
The gaseous stream 18 degassing phase exsiccator D that knockout drum C flows out, dried for logistics 19；The liquid phase that knockout drum C flows out
Liquid phase exsiccator E is removed in logistics 17, and dried is logistics 20, and knockout tower F is sent in logistics 19 and logistics 20 in the lump；
Knockout tower F overhead stream 21 sends into compressor G, for logistics 22 after compression, sends into knockout tower H, knockout tower H overhead materials
Stream 24 is returned to preparing propylene from methanol reactor as reactant, and knockout tower J, knockout tower J tower top are delivered in knockout tower H tower reactor logistics 25
Logistics 27 is propylene product, and tower reactor logistics 28 is by-product.
Knockout tower I is delivered in knockout tower F tower reactor logistics, and knockout tower I overhead stream 26 is returned to methanol system third as reactant
Alkene reaction device, knockout tower I tower reactor logistics 29 is by-product.
Knockout tower I is delivered in knockout tower F tower reactor logistics 23, and knockout tower I overhead stream 26 is returned to methanol system as reactant
Propylene reactor, knockout tower I tower reactor logistics 29 is by-product.
Below by specific embodiment, this programme is further elaborated.
Detailed description of the invention
[embodiment 1]
Using present invention process flow process, the pressure processing olefin stream (logistics 11) is 0.1MPag, and temperature is 40 DEG C, stream
Amount 334kg/hr.The operating condition of distillation column A, D and G and the composition of logistics I are as shown in table 1, and gained propylene product (i.e. flows stock
27) purified propylene is more than 99.8%, and dimethyl ether content is less than 1PPM, reaches to be polymerized requirement.
Table 1
[embodiment 2]
Changing ethylene and the content of propylene in logistics 11, the operating condition of distillation column F, H and J is constant, acquired results such as table 2
Shown in.As can be seen from the table, when the content of ethylene and propylene changes, gained propylene product (stream stock 27) purified propylene is more than
99.8%, and dimethyl ether content is less than 1PPM, reaches to be polymerized requirement.
Table 2
[embodiment 3]
Keeping logistics I feed composition in embodiment 1 constant, change the operating condition of distillation column F, H and J, gained is tied
Fruit is as shown in table 3.As can be seen from the table, when the operating condition of distillation column F, H and J changes, gained propylene product (stream stock 27)
Middle dimethyl ether content is still less than 1PPM, and purified propylene is more than 99.8%, meets the requirement of polymerization-grade propylene.
Table 3
Claims (9)
1. a product separation method for preparing propylene from methanol, including following step:
A) provide containing H2、CO2、H2O, methane, methanol, ethylene, ethane, propylene, propane, C4 +Olefin stream with dimethyl ether
(11)；
B) olefin stream (11) is divided into gaseous stream I (12) and liquid phase stream I (13) in compressional zone A；
C) gaseous stream I (12) removes oxygenates and CO in scrubbing section B2, and be divided into gas phase hydrocarbon logistics (16) and
Liquid phase oxygenatedchemicals logistics (15), the liquid phase stream I (13) of gas phase hydrocarbon logistics (16) and compressional zone A is sent into gas-liquid in the lump and is divided
From tank C；
D) gaseous stream II (18) the degassing phase exsiccator D that knockout drum C flows out, dried for being dried logistics I (19)；Knockout drum C
The liquid phase stream II (17) flowed out removes liquid phase exsiccator E, dried for being dried logistics II (20), is dried logistics I (19) and is dried
Knockout tower F is sent in logistics II (20) in the lump；
E) knockout tower F overhead stream I (21) sends into compressor G, for compression logistics (22) after compression, and compression logistics (22) feeding point
From tower H, knockout tower H overhead stream II (24), as reactant, is back to preparing propylene from methanol reactor, knockout tower H tower reactor logistics
II (25) delivers to knockout tower J, and knockout tower J overhead stream III (27) is propylene product, and tower reactor logistics III (28) is by-product；
F) knockout tower I is delivered in knockout tower F tower reactor logistics I (23), and knockout tower I overhead stream IV (26) is back to first as reactant
Alcohol propylene reactor, knockout tower I tower reactor logistics IV (29) is by-product；
The operating condition of knockout tower F is: tower top pressure is 1.0～1.4MPag, and tower top temperature is-5～15 DEG C, and bottom temperature is
95～125 DEG C；The operating condition of knockout tower H: tower top pressure is 2.0～2.5MPag, tower top temperature is-45～-25 DEG C, tower reactor
Temperature is 45～65 DEG C；The operating condition of knockout tower J: tower top pressure is 1.3～1.8MPag, tower top temperature is 25～40 DEG C, tower
Still temperature is 40～60 DEG C.
Preparing propylene from methanol the most according to claim 1 product separation method, it is characterised in that with olefin stream (11)
Percentage by weight meter, contains ethylene and the propylene of at least 25% in olefin stream (11), and propylene content is at least ethylene contents
2 times.
The product separation method of preparing propylene from methanol the most according to claim 1, it is characterised in that with gaseous stream I (12)
Percentage by weight meter, the oxygen-bearing organic matter of at least 30% contained in gaseous stream I (12) enters liquid phase oxygenatedchemicals logistics
(15) in.
The product separation method of preparing propylene from methanol the most according to claim 1, it is characterised in that with gaseous stream I (12)
Percentage by weight meter, the CO of at most 1% in gaseous stream I (12)2Enter gas phase hydrocarbon logistics (16).
The product separation method of preparing propylene from methanol the most according to claim 1, it is characterised in that by weight percentage,
It is dried in logistics I (19) or dry logistics II (20) H contained2O is at most 100ppm.
The product separation method of preparing propylene from methanol the most according to claim 1, it is characterised in that by weight percentage, dry
The C3 of at least 98% contained in dry logistics I (19) and dry logistics II (20) and following hydro carbons enter in overhead stream I (21)；
The C4 and the above hydro carbons that are dried in logistics I (19) and dry logistics II (20) contain at least 98% enter tower reactor logistics I (23)
In.
The product separation method of preparing propylene from methanol the most according to claim 1, it is characterised in that by weight percentage, tower
C2 containing at least 98% contained in compression logistics (22) and following hydro carbons in the logistics II (24) of top, in tower reactor logistics II (25)
C3 hydro carbons containing at least 98% contained in overhead stream II (24).
The product separation method of preparing propylene from methanol the most according to claim 1, it is characterised in that by weight percentage, tower
Top logistics III (27) contains the propylene product of contain in tower reactor logistics II (25) at least 99.9%, in tower reactor logistics III (28)
Propane containing at least 99% contained in overhead stream II (24).
The product separation method of preparing propylene from methanol the most according to claim 1, it is characterised in that by weight percentage, tower
Top logistics IV (26) contains one or more in C4～the C6 hydro carbons of contain in tower reactor logistics I (23) at least 98%.
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| CN114671731B (en) * | 2022-04-02 | 2024-04-16 | 国家能源集团宁夏煤业有限责任公司 | Method for improving yield of low-carbon olefin in MTP (methanol to propylene) reaction |
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| CN102040439A (en) * | 2009-10-13 | 2011-05-04 | 中国石油化工股份有限公司 | Method for removing O2, N2 and dimethyl ether from olefin streams |
| CN101973831A (en) * | 2010-10-14 | 2011-02-16 | 东华工程科技股份有限公司 | Separation method for producing light olefins from oxygenated chemicals |
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