CN106748610A - Increment utilizes the system and method for preparing propylene from methanol tail oil - Google Patents
Increment utilizes the system and method for preparing propylene from methanol tail oil Download PDFInfo
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- CN106748610A CN106748610A CN201611252839.XA CN201611252839A CN106748610A CN 106748610 A CN106748610 A CN 106748610A CN 201611252839 A CN201611252839 A CN 201611252839A CN 106748610 A CN106748610 A CN 106748610A
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- China
- Prior art keywords
- accessory substance
- freshening
- hydrocarbon
- product stream
- heating furnace
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 189
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 97
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 96
- 238000000034 method Methods 0.000 title claims abstract description 28
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 117
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 117
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 115
- 238000010438 heat treatment Methods 0.000 claims abstract description 67
- 239000000463 material Substances 0.000 claims abstract description 43
- 239000000203 mixture Substances 0.000 claims abstract description 42
- 238000000926 separation method Methods 0.000 claims abstract description 27
- 238000000895 extractive distillation Methods 0.000 claims abstract description 25
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 claims abstract description 24
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 claims abstract description 22
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 claims abstract description 22
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 claims abstract description 20
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 14
- 238000006243 chemical reaction Methods 0.000 claims abstract description 10
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 9
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 9
- 239000000126 substance Substances 0.000 claims description 164
- 238000012544 monitoring process Methods 0.000 claims description 15
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 11
- 229910052799 carbon Inorganic materials 0.000 claims description 11
- 238000002156 mixing Methods 0.000 claims description 4
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical group CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 abstract description 22
- 239000000047 product Substances 0.000 description 84
- 239000001273 butane Substances 0.000 description 18
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 18
- 238000004519 manufacturing process Methods 0.000 description 11
- 239000007789 gas Substances 0.000 description 6
- 150000001336 alkenes Chemical class 0.000 description 5
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- -1 propylene hydrocarbon Chemical class 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000010117 shenhua Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/09—Preparation of ethers by dehydration of compounds containing hydroxy groups
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
- C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
- C07C7/08—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds by extractive distillation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention provides a kind of system and method rised in value using preparing propylene from methanol tail oil, and system includes carrying out the first reactor that preparing dimethyl ether from methanol reaction obtains the first product stream；Since the material of self-heating stove obtain the second reactor of the second product stream for Material synthesis propylene；Receive the second product stream and separate, obtain the product separative element of propylene, C_4 hydrocarbon, the hydrocarbon mixture of C 5/C six and ethene；At least part of C_4 hydrocarbon is separated to obtain the C_4 hydrocarbon separation of extractive distillation device of butene product stream；Receive at least part of first product stream, at least part of butene product stream, the hydrocarbon mixture of at least part of C 5/C six and at least part of ethene and the heating furnace for heating.Butylene therein only can not only be used for freshening by the system and method, and will can be supplemented with the hydrocarbon mixture of C 5/C six due to the butane part for removing, the freshening amount of tail oil is improve, help to increase the yield of propylene, realize and the increment of tail oil is utilized, increase economic efficiency.
Description
Technical field
System and side the invention belongs to process for preparing propylene from methanol field, particularly increment using preparing propylene from methanol tail oil
Method.
Background technology
Propylene is one of important basic chemical industry raw material in chemical industry.Process for preparing propylene from methanol, i.e., with coal or natural gas
For raw material through synthesis gas, methyl alcohol, arrive the process route of propylene hydrocarbon again as a kind of Non oil-based route technology, break away from oil shortage
Constraint, is that the production of propylene opens a new raw material route.
Preparing propylene from methanol technology positioned at the Shenhua Ningxia Coal Industry Group in Ningxia east is provided by German LURGI.To this
For device, the inlet amount of its raw material dimethyl ether/methanol is with ethene, C_4 hydrocarbon, (C 5/C six mixes the hydrocarbon mixture of C 5/C six
Hydrocarbon belongs to the part of tail oil) freshening amount be subject to the design maximum value for allowing to limit.Therefore, produced in preparing propylene from methanol
During, how to go to increase the yield of target product propylene using accessory substance, the purpose of the propylene of volume increase high added value is reached, from
And Business Economic Benefit is improved, it is that technologists face one of problem.
The C_4 hydrocarbon produced in process for preparing propylene from methanol, its component relative volatility is close to 1, it is difficult to use conventional rectification side
Method is separated.And existing many extraction and distillation technologies can be effectively applied to the separation of C_4 hydrocarbon, such as Chinese patent CN at present
103193577 102992933 B etc. of B, CN.These in the prior art, after carrying out extract and separate to C_4 hydrocarbon, only will separate after
Butylene carry out freshening, and produce the bad butane of propylene effect and send out battery limit (BL) as liquefied gas, so as to reduce C_4 hydrocarbon
Freshening amount.And do not mention the influence of freshening amount to the hydrocarbon mixture of C 5/C six, that is, do not increase the utilization of tail oil, can not
Make full use of the accessory substance propylene enhancing in process for preparing propylene from methanol.
The content of the invention
It is an object of the invention to provide a kind of system rised in value using preparing propylene from methanol tail oil, the system can reduce carbon
The freshening amount of four hydrocarbon, increases the freshening amount of accessory substance tail oil.
Another object of the present invention is to provide it is a kind of using above-mentioned system to preparing propylene from methanol tail oil carry out increment profit
Method.
To realize first purpose of the invention, using following technical scheme：
A kind of system rised in value using preparing propylene from methanol tail oil, including first reactor, second reactor, heating furnace, product
Thing separative element and C_4 hydrocarbon separation of extractive distillation device；Wherein,
The first reactor is used to carry out the reaction of preparing dimethyl ether from methanol, to obtain the first product stream；
It is Material synthesis propylene that the second reactor is used for the material from the heating furnace, to obtain the second product
Stream；
The product separative element is used to receive the second product stream from the second reactor and separate it,
To obtain the propylene as purpose product, the C_4 hydrocarbon as the first accessory substance, the mixing of C 5/C six as the second accessory substance
Hydrocarbon, the ethene as the 3rd accessory substance and the carbon seven and hydrocarbon mixed above as the 4th accessory substance；
The C_4 hydrocarbon separation of extractive distillation device is used to separate at least part of first accessory substance, to obtain butylene
Product stream；
The heating furnace is used to receive at least part of first product stream, at least part of butene product stream, at least part of second
Accessory substance and at least part of 3rd accessory substance, and heat temperature raising is carried out to it.
Preferably, the system also includes：
First accessory substance efferent duct, for first accessory substance to be sent into the C_4 hydrocarbon separation of extractive distillation device；
Freshening one is managed, and the first end of the pipe of the freshening one is connected to the C_4 hydrocarbon separation of extractive distillation device, to receive
The butene product stream；
Second accessory substance efferent duct, the first end of the second accessory substance efferent duct is connected to the product separative element,
To receive the second accessory substance；Second end of the second accessory substance efferent duct is respectively connecting to the of the first branch pipe and the second branch pipe
One end, for exporting the second accessory substance；Second end of first branch pipe is connected to the heating furnace；
Freshening two is managed, the first end of the pipe of the freshening two the second end respectively with the pipe of the freshening one and second branch pipe
The second end be connected, the second end of the pipe of the freshening two is connected to the heating furnace；
3rd accessory substance efferent duct, for the 3rd accessory substance to be sent into the heating furnace；
The first current limliting flowmeter is provided with first branch pipe, the heating is input into through first branch pipe for monitoring
The mass flow of stove.
Preferably, the second current limliting flowmeter is provided with the pipe of the freshening two, is input into through the pipe of the freshening two for monitoring
The mass flow of the heating furnace.
Preferably, the second end of the second accessory substance efferent duct is also associated with the 3rd branch pipe, and the 3rd branch pipe is used for
The second accessory substance that will be received is sent out.
Preferably, the system includes gasoline component tank, and the gasoline component tank is used to receive from the 3rd branch pipe
Material.
Preferably, the 3rd current limliting flowmeter is provided with the 3rd accessory substance efferent duct, for monitoring through the described 3rd
Accessory substance efferent duct is input into the mass flow of the heating furnace.
To realize another object of the present invention, using following technical scheme：
A kind of method for utilizing that to preparing propylene from methanol tail oil rise in value using foregoing system, including：
The reaction of preparing dimethyl ether from methanol is carried out using first reactor, to obtain the first product stream；
The material of self-heating stove is Material synthesis propylene since using second reactor, to obtain the second product stream；
The second product stream from the second reactor is received using product separative element and it is separated, with
To the propylene as purpose product, the C_4 hydrocarbon as the first accessory substance, the hydrocarbon mixture of C 5/C six as the second accessory substance,
Ethene as the 3rd accessory substance and the carbon seven and hydrocarbon mixed above as the 4th accessory substance；
At least part of first accessory substance is separated using C_4 hydrocarbon separation of extractive distillation device, to obtain butene product
Stream；
At least part of first product stream, at least part of butene product stream, at least part of second by-product are received using heating furnace
Thing and at least part of 3rd accessory substance, and heat temperature raising is carried out to it.
Preferably, methods described also includes：
Using the first accessory substance efferent duct by first accessory substance feeding C_4 hydrocarbon separation of extractive distillation device；
Part second accessory substance is input into the heating furnace using the second accessory substance efferent duct and the first branch pipe
Row freshening；
Part second accessory substance is delivered to the pipe of the freshening two using the second accessory substance efferent duct and the second branch pipe
In；
The butene product stream is delivered in the pipe of the freshening two using the pipe of freshening one；
Managed by part second accessory substance from second branch pipe and from the freshening one using the pipe of freshening two
Butene product stream be input into the heating furnace and carry out freshening；
The 3rd accessory substance is input into the heating furnace using the 3rd accessory substance efferent duct carry out freshening；
The mass flow of the heating furnace is input into through first branch pipe using the first current limliting flowmeter monitoring.
Preferably, methods described also includes：
The mass flow of the heating furnace is input into through the pipe of the freshening two using the monitoring of the second current limliting flowmeter；
The mass flow of the heating furnace is input into through the 3rd accessory substance efferent duct using the monitoring of the 3rd current limliting flowmeter.
Preferably, methods described also includes：
The accessory substance of part second that will be received using the 3rd branch pipe is sent out；
The material from the 3rd branch pipe is received using gasoline component tank.
The beneficial effects of the present invention are：
It is of the invention increment using preparing propylene from methanol tail oil system and method, by preparing propylene from methanol is obtained first
Accessory substance C_4 hydrocarbon is separated, and butane that can not only be by removes (butane is not conducive to freshening to increase propylene yield), and
The butylene that only will can wherein increase productivity of propylene is used for freshening, helps to reduce energy ezpenditure, improves productivity of propylene；In addition,
In the case where the freshening material total amount being input into heating furnace is constant, the hydrocarbon mixture of C 5/C six (i.e. preparing propylene from methanol tail is increased
The component Parts of oil) freshening amount to replace the butane part that is removed, so as to further increase the yield of propylene, and reduce
The hydrocarbon mixture of C 5/C six (i.e. the part of preparing propylene from methanol tail oil) is used as the amount of gasoline component, realizes to C 5/C
The increment of six hydrocarbon mixtures (i.e. the component Parts of preparing propylene from methanol tail oil) is utilized, and be furthermore achieved that to preparing propylene from methanol tail oil
Increment is utilized, and is favorably improved economic benefit.
Brief description of the drawings
Fig. 1 is system schematic diagram in one embodiment of the increment of the invention using preparing propylene from methanol tail oil；
Fig. 2 is system schematic diagram in another embodiment of the increment of the invention using preparing propylene from methanol tail oil.
Fig. 3 is the schematic diagram of the system of prior art.
Specific embodiment
Technical scheme and its effect are described further below by way of specific embodiment.Following embodiment party
Formula is merely to illustrate present disclosure, the protection domain being not intended to limit the invention.Using design of the invention to this hair
The bright simple change for carrying out is all in the scope of protection of present invention.
As shown in figure 1, system of the increment of the invention using preparing propylene from methanol tail oil, including first reactor 9, second is anti-
Answer device 1, heating furnace 2, product separative element 8 and C_4 hydrocarbon separation of extractive distillation device 3；Wherein,
The first reactor 9 is used to carry out the reaction of preparing dimethyl ether from methanol, to obtain the first product stream；
It is Material synthesis propylene that the second reactor 1 is used for the material from the heating furnace 2, to obtain the second product
Logistics；
The product separative element 8 is used to receive the second product stream from the second reactor 1 and divide it
From to obtain the propylene as purpose product, the C_4 hydrocarbon as the first accessory substance, the C 5/C six as the second accessory substance
Hydrocarbon mixture, the ethene as the 3rd accessory substance and the carbon seven and hydrocarbon mixed above as the 4th accessory substance；Second by-product
Thing is the part of preparing propylene from methanol tail oil with the 4th accessory substance；
The C_4 hydrocarbon separation of extractive distillation device 3 is used to separate at least part of first accessory substance, to obtain fourth
Ene product stream；
The heating furnace 2 is used to receive at least part of first product stream, at least part of butene product stream, at least part of second
Accessory substance and at least part of 3rd accessory substance, and heat temperature raising is carried out to it.
Usually, product separative element 8 include depropanizing tower, debutanizing tower, dethanizer, domethanizing column, C3 knockout towers,
C2 knockout towers and dehexanizer, the debutanizing tower are used to receive the product from the second reactor 1 and divide it
From；The depropanizing tower is used to receive the tower top material of debutanizing tower；The dehexanizer is used to receive the bottom of towe of debutanizing tower
Material；The dethanizer is used to receive the tower top material of depropanizing tower；The domethanizing column is used to receive the tower of dethanizer
Top material；The C3 knockout towers are used to receive the materials at bottom of tower of dethanizer；The C2 knockout towers are used to receive domethanizing column
Materials at bottom of tower；It is the bottom of towe from the depropanizing tower in the product separative element 8 as the C_4 hydrocarbon of first accessory substance
Material；It is from the dehexanizer in the product separative element 8 as the hydrocarbon mixture of C 5/C six of second accessory substance
Tower top material；It is the tower from the dehexanizer in the separative element 8 as the carbon seven and hydrocarbon mixed above of the 4th accessory substance
Substrate material；It is the tower top material from the C2 knockout towers in the product separative element 8 as the ethene of the 3rd accessory substance；As
Tower top material of the propylene of purpose product from the C3 knockout towers in the product separative element 8.
There was only butylene in C_4 hydrocarbon can be used for freshening and can substantially increase the yield of propylene, and propane contribution is smaller, and if fourth
Heated rear input preparing propylene from methanol system carries out freshening to alkene together, then waste the energy, increases the production burden of system.The present invention
Increment using preparing propylene from methanol tail oil system, by the setting to C_4 hydrocarbon separation of extractive distillation device, can be by methyl alcohol
Butane in the C_4 hydrocarbon that propylene processed is obtained removes (butane is not conducive to freshening to increase propylene yield), and can wherein will only increase
Plus the butylene of productivity of propylene is used for freshening, reduces energy waste, reduce the production burden of system, be favorably improved propylene product
Rate；In addition, in the case where the freshening material total amount being input into heating furnace is constant, increased the hydrocarbon mixture of C 5/C six (i.e. methyl alcohol
The component Parts of propylene tail oil processed) freshening amount to replace the butane part that is removed, so as to further increase the product of propylene
Rate, and amount of the hydrocarbon mixture of C 5/C six (i.e. the part of preparing propylene from methanol tail oil) as gasoline component is reduced, realize
Increment to the hydrocarbon mixture of C 5/C six (i.e. the component Parts of preparing propylene from methanol tail oil) is utilized, and be furthermore achieved that to tail oil
Increment is utilized, and is favorably improved economic benefit.
In one embodiment, as shown in Fig. 2 the system also includes：
First accessory substance efferent duct 6, for first accessory substance to be sent into the C_4 hydrocarbon separation of extractive distillation device
3；
The pipe 31 of freshening one, the first end of the pipe 31 of the freshening one is connected to the C_4 hydrocarbon separation of extractive distillation device 3, with
Receive the butene product stream；
Second accessory substance efferent duct 4, the first end of the second accessory substance efferent duct 4 is connected to the product separative element
8, to receive the second accessory substance；Second end of the second accessory substance efferent duct 4 is respectively connecting to the first branch pipe 41 and second
The first end of pipe 42, for exporting the second accessory substance；Second end of first branch pipe 41 is connected to the heating furnace 2；
The pipe 7 of freshening two, the first end of the pipe 7 of the freshening two respectively with second end and described second of the pipe 31 of the freshening one
Second end of branch pipe 42 is connected, and the second end of the pipe 7 of the freshening two is connected to the heating furnace 2；
3rd accessory substance efferent duct 5, for the 3rd accessory substance to be sent into the heating furnace 2；
The first current limliting flowmeter 411 is provided with first branch pipe 41, is input into through first branch pipe 41 for monitoring
The mass flow of the heating furnace 2.
In the accessory substance that second reactor 1 is produced, the amount as the hydrocarbon mixture of C 5/C six of the second accessory substance is larger, because
This sets the first current limliting flowmeter 411 on the first branch pipe 41 is used to monitor freshening amount, and is at by suitable regulation and control
In suitable range of flow, prevent the freshening amount of the hydrocarbon mixture of C 5/C six excessive and exceed the load of the second reactor 1,
Ensure safety in production.
The content of butylene is 20-50wt% in C_4 hydrocarbon, when C_4 hydrocarbon is separated through C_4 hydrocarbon separation of extractive distillation device 3
Afterwards, can be used for the part only butylene of freshening so that the freshening amount of C_4 hydrocarbon is reduced, therefore C 5/C six can be increased mixing
The freshening amount of hydrocarbon is closed, and because the flow of the first branch pipe 41 for conveying the hydrocarbon mixture of C 5/C six has limitation, the first branch pipe
The hydrocarbon mixture of C 5/C six of 41 conveyings can not exceed the flow restriction, therefore can again draw second branch pipe of line 42, by one
Dividing the hydrocarbon mixture of C 5/C six that heating furnace is transmitted back to together with butylene carries out freshening.To can cause not meeting due to removal butane
The part of the mass flow that the second current limliting flowmeter is allowed is supplemented with the hydrocarbon mixture of C 5/C six, is improve C 5/C six and is mixed
The freshening amount of hydrocarbon (i.e. the part of preparing propylene from methanol tail oil) is closed, the hydrocarbon mixture of C 5/C six (i.e. preparing propylene from methanol tail is reduced
The part of oil) it is used as the amount of gasoline component, help to increase the yield of propylene, realize to the hydrocarbon mixture of C 5/C six
Increment is utilized, and furthermore achieved that and the increment of preparing propylene from methanol tail oil is utilized, and helps further to increase economic efficiency.
In one embodiment, the second current limliting flowmeter 71 is provided with the pipe 7 of the freshening two, for monitoring through described
The pipe 7 of freshening two is input into the mass flow of the heating furnace 2.
The setting of the second current limliting flowmeter 71 on the pipe 7 of freshening two, contributes to butylene and portion that control is input into through two pipe of freshening 7
Divide total freshening amount of the second accessory substance (hydrocarbon mixture of C 5/C six), the part second that further monitoring is input into through the second branch pipe 42
The freshening amount of accessory substance, prevents the load beyond system.
After at least part of first accessory substance of 3 pairs, C_4 hydrocarbon separation of extractive distillation device is separated, except obtaining fourth
Ene product stream, also obtains butane product stream.
In one embodiment, the system includes butane export pipeline 32, and the butane export pipeline 32 is used for will
Butane product stream output from the C_4 hydrocarbon separation of extractive distillation device 3.
In one embodiment, the system includes liquid gas storage tank, and the liquid gas storage tank is used to receive from the fourth
The material of alkane export pipeline 32.
In one embodiment, the second end of the second accessory substance efferent duct 4 is also associated with the 3rd branch pipe 43, described
The second accessory substance that 3rd branch pipe 43 is used to receive is sent out.
In one embodiment, the system includes gasoline component tank, and the gasoline component tank is used to receive from institute
State the material of the 3rd branch pipe 43.
In one embodiment, the 3rd current limliting flowmeter 51 is provided with the 3rd accessory substance efferent duct 5, for supervising
Control is input into the mass flow of the heating furnace 2 through the 3rd accessory substance efferent duct 5.
In the accessory substance that second reactor 1 is produced, the amount as the ethene of the 3rd accessory substance is smaller, therefore the settable 3rd
Current limliting flowmeter 51, can also be not provided with.
In one embodiment, the range of flow of the first current limliting flowmeter 411 being arranged on first branch pipe 41
It is 0~180t/h, preferably 60~145t/h.
In one embodiment, control is arranged at the flow model of the second current limliting flowmeter 71 on the pipe 7 of the freshening two
It is 0~100t/h to enclose, preferably 20~56t/h.
In one embodiment, control is arranged at the 3rd current limliting flowmeter 51 on the 3rd accessory substance efferent duct 5
Range of flow be 0~50t/h, preferably 8~14t/h.
The scope of flow can be controlled by pump.
The setting of range of flow, can anti-locking system overload operation, it is ensured that safety in production.
In one embodiment, the system also includes the second surge tank, the entrance point of second surge tank and institute
The second end for stating the second accessory substance efferent duct 4 is connected, for receiving the second accessory substance from the product separative element 8,
The port of export of second surge tank is connected with first branch pipe 41, the first branch pipe 42 and the 3rd branch pipe 43 respectively, is used for
Export as the hydrocarbon mixture of C 5/C six of the second accessory substance.
In one embodiment, the system also includes the first surge tank, and list is separated from the product for receiving
First accessory substance of unit 8, C_4 hydrocarbon separation of extractive distillation device 3 is received as the carbon of the first accessory substance from the 3rd surge tank
Four hydrocarbon.
In one embodiment, the system also includes the 3rd surge tank, and list is separated from the product for receiving
3rd accessory substance of unit 8, heating furnace 2 is received as the ethene of the 3rd accessory substance from the 3rd surge tank.
To realize another object of the present invention, using following technical scheme：
A kind of method for utilizing that to preparing propylene from methanol tail oil rise in value using foregoing system, including：
The reaction of preparing dimethyl ether from methanol is carried out using first reactor 9, to obtain the first product stream；
The material of self-heating stove 2 is Material synthesis propylene since using second reactor 1, to obtain the second product stream；
The second product stream from the second reactor 1 is received using product separative element 8 and it is separated, with
Obtain the propylene as purpose product, the C_4 hydrocarbon as the first accessory substance, the mixing of C 5/C six as the second accessory substance
Hydrocarbon, the ethene as the 3rd accessory substance and the carbon seven and hydrocarbon mixed above as the 4th accessory substance；
Separated using 3 pairs of at least part of first accessory substances of C_4 hydrocarbon separation of extractive distillation device, to obtain butylene product
Logistics；
At least part of first product stream, at least part of butene product stream, at least part of second by-product are received using heating furnace 2
Thing and at least part of 3rd accessory substance, and heat temperature raising is carried out to it.
There was only butylene in C_4 hydrocarbon can be used for freshening and can substantially increase the yield of propylene, and propane contribution is smaller, and if fourth
Heated rear input preparing propylene from methanol system carries out freshening to alkene together, then waste the energy, increases the production burden of system.The present invention
Method, remove that (butane is not conducive to freshening and is produced to increase propylene by the butane in the C_4 hydrocarbon that obtains preparing propylene from methanol
Amount), and the butylene that only will can wherein increase productivity of propylene is used for freshening, reduces energy waste, reduces the production of system
Burden, is favorably improved productivity of propylene；In addition, in the case where the freshening material total amount being input into heating furnace is constant, increased
Butane part of the freshening amount of the hydrocarbon mixture of C 5/C six (i.e. the component Parts of preparing propylene from methanol tail oil) to replace being removed, from
And the yield of propylene is further increased, and reduce the hydrocarbon mixture of C 5/C six (i.e. the part of preparing propylene from methanol tail oil)
Amount as gasoline component, realizes the increment profit to the hydrocarbon mixture of C 5/C six (i.e. the component Parts of preparing propylene from methanol tail oil)
With, furthermore achieved that and the increment of tail oil is utilized, it is favorably improved economic benefit.
In one embodiment, methods described also includes：
First accessory substance is sent into the C_4 hydrocarbon separation of extractive distillation device 3 using the first accessory substance efferent duct 6
In；
Part second accessory substance is input into the heating furnace 2 using the second accessory substance efferent duct 4 and the first branch pipe 41
In carry out freshening；
Part second accessory substance is delivered to the freshening two using the second accessory substance efferent duct 4 and the second branch pipe 42
In pipe 7；
The butene product stream is delivered in the pipe 7 of the freshening two using the pipe 31 of freshening one；
Using the pipe 7 of freshening two by part second accessory substance from second branch pipe 42 and from the freshening one
The butene product stream of pipe 31 is input into the heating furnace 2 and carries out freshening；
The 3rd accessory substance is input into the heating furnace 2 using the 3rd accessory substance efferent duct 5 carry out freshening；
The material stream that the heating furnace 2 is input into through first branch pipe 41 is monitored using the first current limliting flowmeter 411
Amount.
The content of butylene is 20-50wt% in C_4 hydrocarbon, in the inventive method, when C_4 hydrocarbon is through C_4 hydrocarbon extracting rectifying point
After the separation of device 3, can be used for the part only butylene of freshening so that the freshening amount of C_4 hydrocarbon is reduced, therefore will can be increased
The freshening amount of the hydrocarbon mixture of C 5/C six, and there is flow restriction due to conveying the first branch pipe 41 of the hydrocarbon mixture of C 5/C six, the
The hydrocarbon mixture of C 5/C six of the conveying of one branch pipe 41 can not exceed the flow restriction, therefore can be by the second branch pipe 42 by one
Dividing the hydrocarbon mixture of C 5/C six that heating furnace is transmitted back to together with butylene carries out freshening.To can cause not meeting due to removal butane
The part of the mass flow that the second current limliting flowmeter is allowed is supplemented with the hydrocarbon mixture of C 5/C six, is improve C 5/C six and is mixed
The freshening amount of hydrocarbon (i.e. the part of preparing propylene from methanol tail oil) is closed, the hydrocarbon mixture of C 5/C six (i.e. preparing propylene from methanol tail is reduced
The part of oil) it is used as the amount of gasoline component, help to increase the yield of propylene, realize to the hydrocarbon mixture of C 5/C six
Increment is utilized, and furthermore achieved that and the increment of preparing propylene from methanol tail oil is utilized, and helps further to increase economic efficiency.
In one embodiment, methods described also includes：
The mass flow that the heating furnace 2 is input into through the pipe 7 of the freshening two is monitored using the second current limliting flowmeter 71；
The material that the heating furnace 2 is input into through the 3rd accessory substance efferent duct 5 is monitored using the 3rd current limliting flowmeter 51
Flow.
In one embodiment, methods described also includes：
The accessory substance of part second that will be received using the 3rd branch pipe 43 is sent out；
The material from the 3rd branch pipe 43 is received using gasoline component tank.
Increment as shown in Figure 2 is as follows using the system operation of preparing propylene from methanol tail oil：
Preparing dimethyl ether from methanol reaction is carried out in methyl alcohol input first reactor 9 obtain the first product stream (dimethyl ether/methanol),
The heated stove 2 of the first product stream from first reactor 9 is input into second reactor 1 after heating and synthesizes propylene, obtains second
Product stream；Separated in second product stream input product separative element 8, obtained as the propylene of purpose product and as first
The C_4 hydrocarbon of accessory substance, the hydrocarbon mixture of C 5/C six as the second accessory substance, the ethene as the 3rd accessory substance and conduct
The carbon seven and hydrocarbon mixed above of the 4th accessory substance；The C_4 hydrocarbon as the first accessory substance from the product separative element 8 is passed through
The first accessory substance export pipeline 6 is input into the C_4 hydrocarbon separation of extractive distillation device 3 and carries out isolated butene product
Stream and butane product stream, butene product flow through the pipe 31 of freshening one and export, and butane product flows through butane export pipeline 32 and exports；Come from
The hydrocarbon mixture of C 5/C six part as the second accessory substance of the product separative element 8 is exported through the second accessory substance successively
Heated in the input heating furnace 2 of 4 and first branch pipe of pipe 41, another part is successively through the second accessory substance efferent duct 4 and second
Pipe 42 is input into the pipe 7 of freshening two together with the butene product stream from the pipe 31 of freshening one, and is input into heating furnace 2 through two pipe of freshening 7
In heated；The ethene as the 3rd accessory substance from the product separative element 8 is input into through the 3rd accessory substance efferent duct 5
Heated in heating furnace 2；Material input second reactor 1 after heating carries out reaction and prepares propylene；Wherein, from the fourth
It is used as liquefied gas in the material input liquid gas storage tank of alkane export pipeline 32, the material from the 3rd branch pipe 43 is input into the vapour
With carbon seven and hydrocarbon mixed above as the 4th accessory substance from the product separative element 8 together as vapour in oil ingredient tank
Oil ingredient；In above process, the range of flow for controlling the first current limliting flowmeter 411 being arranged on first branch pipe 41 is
60~145t/h, the range of flow for controlling the second current limliting flowmeter 71 being arranged on the pipe 7 of the freshening two is 20~56t/h；
The range of flow for controlling the 3rd current limliting flowmeter 51 being arranged on the 3rd accessory substance efferent duct 5 is 8~14t/h.
Embodiment 1
205t/h methyl alcohol is input into system as shown in Figure 2, is run according to above-mentioned running, wherein, by the first limit
The flow of the first branch pipe 41 of the stream limitation of flowmeter 411 is 145t/h, the stream of the pipe 7 of freshening two of the limitation of the second current limliting flowmeter 71
It is 56t/h to measure, and the flow on the 3rd accessory substance efferent duct 5 controlled by the 3rd current limliting flowmeter 51 is 10t/h, obtains propylene
56.8t/h, the yield of propylene is 27.71wt%.
System in prior art as shown in Figure 3, running is as follows：
Preparing dimethyl ether from methanol reaction is carried out in methyl alcohol input first reactor 9 ' obtain the first product stream (dimethyl ether/first
Alcohol), the heated stove 2 ' of the first product stream from first reactor 9 ' is input into synthesis propylene in second reactor 1 ' after heating, and obtains
To the second product stream；Separated in second product stream input product separative element 8 ', obtain as purpose product propylene and
As the C_4 hydrocarbon of the first accessory substance, the hydrocarbon mixture of C 5/C six and the second as the 3rd accessory substance as the second accessory substance
Alkene；The first accessory substance from the product separative element 8 ' (is not isolated, butylene therein and butane are returned together
Refining) heated through the first accessory substance export pipeline 6 ' and the input heating furnace 2 ' of two pipe of freshening 7 ' successively；From the product point
At least part of second accessory substance from unit 8 is successively through the second accessory substance efferent duct 4 ' and the input heating furnace 2 ' of the first branch pipe 41 '
Heated；At least part of 3rd accessory substance from the product separative element 8 adds through the input of the 3rd accessory substance efferent duct 5 '
Heated in hot stove 2 ', wherein the flow restriction of the first branch pipe 41 ' is as the flow restriction of the first branch pipe 41 in Fig. 2, the
The flow restriction of three accessory substance efferent ducts 5 ' as the flow restriction of the 3rd accessory substance efferent duct 5 in Fig. 2, the pipe 7 ' of freshening two
Flow restriction is as the flow restriction of the pipe 7 of freshening in Fig. 2 two
Comparative example 1
205t/h methyl alcohol is input into system as shown in Figure 3, is run according to above-mentioned running, wherein, the first branch pipe
41 ' flow is 145t/h, and the flow of the first accessory substance export pipeline 6 ' is 56t/h, the stream on the 3rd accessory substance efferent duct 5 '
It is 10t/h to measure, and obtains propylene 50.7t/h, and the yield of propylene is 24.73wt%.
From embodiment 1 and the comparative result of comparative example 1, methyl alcohol inlet amount is identical, freshening material total amount identical
In the case of, the freshening amount of the hydrocarbon mixture of C 5/C six increased 17.92t/h, and yield improves 2.98wt%, daily can fecund third
Alkene 146.4t.It follows that the flow difference identical situation of, each freshening pipeline identical in the material total flow for freshening
Under, it is used in the C_4 hydrocarbon of freshening in comparative example 1, the butylene of propylene product is not only improved including can be used for freshening, also include
The butane almost not acted on so that the yield of propylene improves less；And in embodiment 1, after C_4 hydrocarbon is separated, will only can be used for
Freshening and improve propylene product butylene be used for freshening, and will remove butane part hydrocarbon mixture (the methyl alcohol system third of C 5/C six
The part of alkene tail oil) supplement, not only without departing from the load of system, while also add returning for the hydrocarbon mixture of C 5/C six
Refining amount, improves the yield of propylene, and fully increment make use of the hydrocarbon mixture of C 5/C six, so as to rise in value make use of tail oil.
Claims (10)
1. it is a kind of rise in value using preparing propylene from methanol tail oil system, it is characterised in that the system include first reactor (9),
Second reactor (1), heating furnace (2), product separative element (8) and C_4 hydrocarbon separation of extractive distillation device (3)；Wherein,
The first reactor (9) for carrying out the reaction of preparing dimethyl ether from methanol, to obtain the first product stream；
The second reactor (1) for the material from the heating furnace (2) be Material synthesis propylene, to obtain the second product
Logistics；
The product separative element (8) is for receiving the second product stream from the second reactor (1) and it being divided
From to obtain the propylene as purpose product, the C_4 hydrocarbon as the first accessory substance, the C 5/C six as the second accessory substance
Hydrocarbon mixture, the ethene as the 3rd accessory substance and the carbon seven and hydrocarbon mixed above as the 4th accessory substance；
The C_4 hydrocarbon separation of extractive distillation device (3) for being separated at least part of first accessory substance, to obtain butylene
Product stream；
The heating furnace (2) is for receiving at least part of first product stream, at least part of butene product stream, at least part of second pair
Product and at least part of 3rd accessory substance, and heat temperature raising is carried out to it.
2. system according to claim 1, it is characterised in that the system also includes：
First accessory substance efferent duct (6), for first accessory substance to be sent into the C_4 hydrocarbon separation of extractive distillation device
(3)；
Freshening one is managed (31), and the first end that the freshening one manages (31) is connected to the C_4 hydrocarbon separation of extractive distillation device (3),
To receive the butene product stream；
Second accessory substance efferent duct (4), the first end of the second accessory substance efferent duct (4) is connected to the product separative element
(8), receiving the second accessory substance；Second end of the second accessory substance efferent duct (4) be respectively connecting to the first branch pipe (41) and
The first end of the second branch pipe (42), for exporting the second accessory substance；Second end of first branch pipe (41) is connected to described adding
Hot stove (2)；
Freshening two is managed (7), and the first end that the freshening two manages (7) manages second end and described of (31) with the freshening one respectively
Second end of two branch pipes (42) is connected, and the second end that the freshening two manages (7) is connected to the heating furnace (2)；
3rd accessory substance efferent duct (5), for the 3rd accessory substance to be sent into the heating furnace (2)；
The first current limliting flowmeter (411) is provided with first branch pipe (41), it is defeated through first branch pipe (41) for monitoring
Enter the mass flow of the heating furnace (2).
3. system according to claim 2, it is characterised in that the freshening two is managed and the second current limliting flow is provided with (7)
Meter (71), the mass flow that (7) are input into the heating furnace (2) is managed for monitoring through the freshening two.
4. the system according to Claims 2 or 3, it is characterised in that the second end of the second accessory substance efferent duct (4) is also
The 3rd branch pipe (43) is connected with, the 3rd branch pipe (43) is sent out for the second accessory substance that will be received.
5. system according to claim 4, it is characterised in that the system includes gasoline component tank, the gasoline component
Tank is used to receive the material from the 3rd branch pipe (43).
6. system according to claim 5, it is characterised in that be provided with the 3rd on the 3rd accessory substance efferent duct (5)
Current limliting flowmeter (51), the mass flow of the heating furnace (2) is input into for monitoring through the 3rd accessory substance efferent duct (5).
7. a kind of system according to claim any one of 1-6 to preparing propylene from methanol tail oil rise in value the method for utilizing,
Characterized in that, methods described includes：
The reaction of preparing dimethyl ether from methanol is carried out using first reactor (9), to obtain the first product stream；
The material of self-heating stove (2) is Material synthesis propylene since using second reactor (1), to obtain the second product stream；
The second product stream from the second reactor (1) is received using product separative element (8) and it is separated, with
Obtain the propylene as purpose product, the C_4 hydrocarbon as the first accessory substance, the mixing of C 5/C six as the second accessory substance
Hydrocarbon, the ethene as the 3rd accessory substance and the carbon seven and hydrocarbon mixed above as the 4th accessory substance；
At least part of first accessory substance is separated using C_4 hydrocarbon separation of extractive distillation device (3), to obtain butene product
Stream；
At least part of first product stream, at least part of butene product stream, at least part of second accessory substance are received using heating furnace (2)
With at least part of 3rd accessory substance, and heat temperature raising is carried out to it.
8. method according to claim 7, it is characterised in that methods described also includes：
First accessory substance is sent into the C_4 hydrocarbon separation of extractive distillation device (3) using the first accessory substance efferent duct (6)
In；
Part second accessory substance is input into the heating furnace using the second accessory substance efferent duct (4) and the first branch pipe (41)
(2) freshening is carried out in；
Part second accessory substance is delivered to the freshening two using the second accessory substance efferent duct (4) and the second branch pipe (42)
In pipe (7)；
(31) are managed using freshening one the butene product stream is delivered to during the freshening two manages (7)；
(7) are managed by part second accessory substance from second branch pipe (42) and from the freshening one using freshening two
Freshening is carried out in the butene product stream input heating furnace (2) for managing (31)；
The 3rd accessory substance is input into the heating furnace (2) using the 3rd accessory substance efferent duct (5) carry out freshening；
The material of the heating furnace (2) is input into through first branch pipe (41) using the first current limliting flowmeter (411) monitoring
Flow.
9. method according to claim 8, it is characterised in that methods described also includes：
Using the monitoring of the second current limliting flowmeter (71) mass flow that (7) are input into the heating furnace (2) is managed through the freshening two；
The thing of the heating furnace (2) is input into through the 3rd accessory substance efferent duct (5) using the monitoring of the 3rd current limliting flowmeter (51)
Stream amount.
10. method according to claim 9, it is characterised in that methods described also includes：
The accessory substance of part second that will be received using the 3rd branch pipe (43) is sent out；
The material from the 3rd branch pipe (43) is received using gasoline component tank.
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| CN110041157A (en) * | 2019-05-10 | 2019-07-23 | 国家能源投资集团有限责任公司 | A method of it improving preparing propylene from methanol yield and extends catalyst life |
| CN110054539A (en) * | 2019-05-10 | 2019-07-26 | 国家能源投资集团有限责任公司 | A kind of preparing propylene from methanol device and method |
| CN110078586A (en) * | 2019-05-06 | 2019-08-02 | 聊城氟尔新材料科技有限公司 | The device and technique of a kind of tetrafluoroethene coproduction hexafluoropropene and application |
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| CN103420759A (en) * | 2012-05-16 | 2013-12-04 | 中国石油化工股份有限公司 | Propylene production method |
| CN206359441U (en) * | 2016-12-30 | 2017-07-28 | 神华集团有限责任公司 | The system that increment utilizes preparing propylene from methanol tail oil |
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| CN206359441U (en) * | 2016-12-30 | 2017-07-28 | 神华集团有限责任公司 | The system that increment utilizes preparing propylene from methanol tail oil |
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| CN110054539A (en) * | 2019-05-10 | 2019-07-26 | 国家能源投资集团有限责任公司 | A kind of preparing propylene from methanol device and method |
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