CN110183301A - Preparing propylene from methanol system and the method that feeds intake of driving is carried out using it - Google Patents
Preparing propylene from methanol system and the method that feeds intake of driving is carried out using it Download PDFInfo
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- CN110183301A CN110183301A CN201910468188.5A CN201910468188A CN110183301A CN 110183301 A CN110183301 A CN 110183301A CN 201910468188 A CN201910468188 A CN 201910468188A CN 110183301 A CN110183301 A CN 110183301A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
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- C—CHEMISTRY; METALLURGY
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- 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
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- 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
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Abstract
The present invention provides a kind of preparing propylene from methanol system and carries out the method for driving to feed intake using it, and preparing propylene from methanol system includes first reactor, reacts to obtain the first product stream for carrying out methanol-fueled CLC dimethyl ether；Second reactor reacts to obtain the second product stream for carrying out the first product stream propylene；First water vapour pipeline, for providing vapor to first reactor；Heating device, for carrying out heat temperature raising to the first product stream of part and circulation hydrocarbon product stream；First and second side line pipeline, for respectively sending the first product stream of part and process water to second to most end catalyst bed respectively；Refined unit, for being separated to the second product stream, to obtain the circulation hydrocarbon product stream comprising C2, C4, C5 and C6 component；Recycle hydrocarbons storage tank, for providing circulation hydrocarbon product stream to heating device.The preparing propylene from methanol system and method can control the temperature runaway situation in even prevention first reactor and second reactor, so as to shorten driving charging time.
Description
Technical field
The invention belongs to preparing propylene from methanol field, especially preparing propylene from methanol system and the sides for carrying out driving to feed intake using it
Method.
Background technique
Propylene is one of most important industrial chemicals, is mainly derived from the stones such as FCC (catalytic cracking), naphtha pyrolysis at present
Oil circuit line.In recent years, state's inner propene demand sharp increase, but China's oil yield has been far from satisfying the market demand, import
Rate is more than 50%, and in view of this situation, the diversification of production of propylene raw material becomes relationship national energy structural adjustment
Key subjects.It is synthesized that gas-phase methanol transformation technology is mature by natural gas, coal, is established for the development of MTO technology
Good basis, process for preparing propylene from methanol will become another important stable source, methanol-to-olefins after petrochemical industry and urge
Agent is the core of this technology.
It is consolidating of successfully developing in late 1990s of German Lurgi company that preparing propylene from methanol technology is most representative
DME (preparing dimethyl ether from methanol) and MTP (preparing propylene from methanol) is arranged in fixed bed MTP (preparing propylene from methanol) technique, the technological reaction unit
Two reactors, methanol feedstock enter DME reactor from top by preheating, and methanol steam is in alumina base catalyst (DME-
1) effect is lower generates DME (dimethyl ether).It is sent into MTP reactor bed from side after a part of DME product is preheated, in addition DME
Product recycles anti-into MTP after heating stove heating after water vapour mixes with the C2-C6 recycle hydrocarbons from refined unit and partially
Answer device.
Often there is reactor overtemperature situation during preparing propylene from methanol device commissioning run test, overtemperature situation can also when serious
Occur temperature runaway situation, increase the reaction bed temperature in reactor rapidly, substantial deviation design value, to reaction and equipment all
It will cause very big harm.In order to reduce the influence of overtemperature and temperature runaway to catalyst and reactor component, need to spend longer
Time, relatively mitigate manipulation under the conditions of carry out dosing operation, the driving charging time of reaction system at least needs 10-12 small
When, and this during generate material need to set fire torch processing, substantially increase the supplies consumption and energy consumption of MTP device,
Cause huge economic loss.
Summary of the invention
The first purpose of this invention is to provide a kind of preparing propylene from methanol system, preparing propylene from methanol system flow letter
It is single, and can prevent from occurring reactor overtemperature situation during rapid Start-Up feeds intake and influencing the duration that feeds intake, so as to shorten opening
Vehicle feed intake the period, reduce drive feed intake during supplies consumption and energy consumption.
Second object of the present invention, which is to provide, a kind of using preparing propylene from methanol system above-mentioned to be carried out driving to feed intake
Method, this method is simple, can prevent from occurring reactor overtemperature situation during rapid Start-Up feeds intake and influencing the duration that feeds intake,
So as to shorten drive feed intake the period, reduce drive feed intake during supplies consumption and energy consumption.
First purpose to realize the present invention, the following technical solution is employed:
A kind of preparing propylene from methanol system, comprising:
First reactor, for carrying out methanol-fueled CLC dimethyl ether reaction, to obtain the first product stream；First product stream
Including dimethyl ether, water and unreacted methanol；First product flows through the output of the first product stream pipeline；First product
Flow tube line includes flare line, the first pipeline and the second pipeline, for will be from the first product flow point of the first reactor
It does not export, and the flare line from the first product stream of the part of the first reactor for will export to flare system；
Second reactor, for carrying out the first product stream propylene reaction, to obtain the second product stream；And institute
It states and is equipped with multiple catalyst beds in second reactor along longitudinal direction；
First water vapour pipeline, for providing vapor to the first reactor；
Heating device, for the first product stream from first pipeline and following from circulation hydrocarbon product stream pipeline
Cyclic hydrocarbon product stream carries out heat temperature raising, so that it send as the top feed of the second reactor to the first catalyst bed；
First side line pipeline is distinguished for receiving the first product stream from second pipeline, and by received material
It send to second to most end catalyst bed；
Second lateral line canal road, for sending water respectively to second to most end catalyst bed；
Refined unit, for being separated to second product stream, to obtain following comprising C2, C4, C5 and C6 component
The circulation hydrocarbon product stream is sent into the heating device at least partially by the circulation hydrocarbon product stream pipeline by cyclic hydrocarbon product stream
In；
Recycle hydrocarbons storage tank 18, for providing circulation hydrocarbon product stream to the heating device.
Preferably, the preparing propylene from methanol system further includes the second water vapour pipeline, for anti-from top to described second
Device is answered to provide vapor；The heating device is used for the first product stream from first pipeline and comes from second water
The vapor of steam pipe line and from it is described circulation hydrocarbon product stream pipeline circulation hydrocarbon product stream carry out heat temperature raising so that its
Top feed as the second reactor is sent to the first catalyst bed.
Preferably, the preparing propylene from methanol system further includes First Heat Exchanger, for from the first water vapour pipeline
Vapor heats up, so that it is with the methanol from methanol line together as the top feed of the first reactor；
Preferably, the first product stream pipeline further includes third pipeline, for will be from the portion of the first reactor
Divide the output of the first product stream；The preparing propylene from methanol system further includes the second heat exchanger, for from the third pipeline
First product stream is sent into the first side line pipeline after being cooled down.
Preferably, the preparing propylene from methanol system further includes third water vapour pipeline, for vapor to be sent into described
One lateral line canal road.
Second purpose to realize the present invention, the present invention provides a kind of to be driven using aforementioned methanol propylene system
The method to feed intake, described method includes following steps:
(1) 180-220 DEG C is successively purged and is warming up to the preparing propylene from methanol system with nitrogen, then with described
First water vapour pipeline provides vapor to the first reactor the catalyst bed in the first reactor to heat up
To 255-260 DEG C, preparing dimethyl ether from methanol reaction then occurs in the first reactor using the methanol of input and obtains first
Product stream, and exported the first product stream from the first reactor to flare system using flare line；
(2) it is no more than ± 5 DEG C to the out temperature difference of the first reactor, and its reaction bed temperature reaches
At 265-320 DEG C, the flare line is closed, and the Feed space velocities of the methanol are promoted to 0.65-0.75h-1(at this point, institute
The pressure stated in first reactor reaches 1.0-1.45Mpa) after, the first product from the first reactor is flowed through described
First pipeline is exported carry out being warming up to 420-460 DEG C into the heating device after, as the second reactor top into
Material is sent to the first catalyst bed, and methanol to propylene reaction occurs in second reactor (2) and obtains the second product stream；Then will
Second product stream is delivered to the refined unit；
(3) when the outlet temperature of the first reactor reaches 325-345 DEG C, the circulation of self-loopa in future hydrocarbon storage tank 18
Hydrocarbon product stream inputs in the heating device and carries out being warming up to 420- together with the first product stream exported through first pipeline
After 460 DEG C, the top feed as the second reactor is sent to the first catalyst bed, continues to occur in second reactor
Methanol to propylene reaction obtains the second product stream；It then proceedes to second product stream being delivered to the refined unit and be divided
From obtaining the circulation hydrocarbon product stream comprising C2, C4, C5 and C6 component；
Then the circulation hydrocarbon product stream from the refined unit is also inputted in the heating device and through described first
First product stream of pipeline output and the circulation hydrocarbon product stream from the recycle hydrocarbons storage tank 18 carry out being warming up to 420-460 together
After DEG C, continue to send as the top feed of the second reactor to the first catalyst bed anti-to continue generation preparing propylene from methanol
The second product stream should be obtained；The second reactor can persistently be met to the circulation hydrocarbon product stream from the refined unit
Fuel requirements stop supplying the circulation hydrocarbon product stream from recycle hydrocarbons storage tank 18 to the heating device；
(4) when the outlet temperature of the first reactor reaches 360-375 DEG C, the first side line conduit acceptor is utilized
Through second pipeline export the first product stream, using the second lateral line canal road receive water, and respectively using received material as
The side entry feed of the second reactor is sent respectively to second to most end catalyst bed to continue that methanol to propylene reaction occurs
The second product stream is obtained, adjust the reaction bed temperature of the second reactor to 480-490 DEG C and is kept, completes to drive to throw
Material process.
It is appreciated that input first reactor methanol be it is preheated treated, temperature be 250-280 DEG C.
Preferably, the Feed space velocities of the methanol are 0.5-0.6h-1。
Preferably, in the step (1), the vapor utilizes described before being supplied to the first reactor
One heat exchanger is warming up to 200-220 DEG C.
Preferably, in the step (3), the top feed of the second reactor further includes vapor, and is to pass through institute
It states the second water vapour pipeline to be delivered in the heating device, with the first product stream exported through first pipeline and from following
After the circulation hydrocarbon product stream of cyclic hydrocarbon product stream pipeline is heated to 420-460 DEG C together, as second reactor top into
Material is sent to the first catalyst bed.
Preferably, in the step (3), the flow of the vapor from the second water vapour pipeline is Q1, comes from institute
The flow for stating the circulation hydrocarbon product stream of circulation hydrocarbon product stream pipeline is Q2, the flow of methanol from the methanol line is Q3,
Then reached in the step (3) since the reaction bed temperature of top feed to the second reactor the second reactor
To 480-490 DEG C, the ratio of (Q1+Q2)/Q3 is improved from 1:1 to 1.2:1.
Preferably, it in the step (4), when the outlet temperature of the first reactor reaches 360-375 DEG C, also utilizes
Second heat exchanger carries out being cooled to 220-235 DEG C to the first product stream from the third pipeline, then using described
Material after the cooling of first side line conduit acceptor makes itself and the first product stream from second pipeline together as described the
The side entry feed of two reactors send respectively to second to most end catalyst bed with adjust second to most end catalyst bed into
Material temperature degree.
Preferably, it in the step (4), when the outlet temperature of the first reactor reaches 360-375 DEG C, also utilizes
The third water vapour pipeline provides vapor from side line to the second reactor；And in the future using the first side line pipeline
From the vapor of the third water vapour pipeline and the material from second heat exchanger and from second pipeline
The mixed material of first product stream is sent respectively to second to most end catalyst bed to adjust second to most end catalyst bed
Feeding temperature.
The beneficial effects of the present invention are:
Preparing propylene from methanol system of the invention and the method for driving to feed intake is carried out using it,
Vapor is provided to the first reactor by the first water vapour pipeline of setting, on the one hand react first
Catalyst bed in device 1 carries out heat temperature raising, so that the catalyst bed in first reactor 1 reaches methanol vapor phase as early as possible and takes off
The reaction temperature of water dimethyl ether synthesizing reaction shortens charging time, on the other hand can make vapor in catalyst duct
The reaction heat of heat of adsorption and methanol gas phase dehydration dimethyl ether synthesizing reaction by successively sequentially successively discharging respectively, to prevent two kinds
Heat is superimposed and causes temperature runaway；
Vapor, one side vapor energy are provided from top to the second reactor by the way that the second water vapour pipeline is arranged
Enough play the role of carrier gas as carrier, to reduce material benzenemethanol/DME partial pressure, improves the production of reaction selectivity and propylene product
Rate；On the other hand material benzenemethanol can be diluted, contacts less material benzenemethanol with the catalyst in second reactor, to delay
The generation of catalyst surface carbon distribution；
By the way that the second heat exchanger is arranged, so that the side entry feed of the second reactor includes at least two parts: directly coming
From the first product stream of the part of the first reactor and through the second heat exchanger cooling after the first product stream, thus by this two
The respective inlet amount of partial material further regulates and controls the reaction bed temperature of the second reactor, to prevent temperature runaway；
Vapor is provided from side line to the second reactor by the way that third water vapour pipeline is arranged, so that described second is anti-
It answers the side entry feed of device to include at least three parts: being changed directly from the first product stream of part of the first reactor, through second
The first product stream after hot device cooling and the vapor from third water vapour pipeline, thus respective by this three parts material
Inlet amount further regulates and controls the reaction bed temperature of the second reactor, to prevent temperature runaway；
It is contracted significantly by the above-mentioned control of temperature runaway situation during feeding intake to driving to realize the raising of rate of feeding
Short driving charging time foreshortens to it 2 hours by original 10-12 hour, to reduce material waste and energy dissipation；
On the one hand the shortening of driving charging time reduces the methanol feedstock consumption for putting flare system, on the other hand improves product
The yield of (including propylene, LPG and BTX aromatics), two aspects add up, the primary achievable upgrading synergy total 117 that feeds intake of driving
Ten thousand yuan=151.81 ten thousand yuan of Wan Yuan+34.81.
Detailed description of the invention
Fig. 1 is the flow chart of preparing propylene from methanol system of the invention in one embodiment.
Specific embodiment
Technical solution of the present invention and its effect are described further below by way of specific embodiment.Following embodiment party
Formula is merely to illustrate the contents of the present invention, and invention is not limited in following embodiments or embodiment.Using design of the invention
All within the scope of the claimed invention to the simple change of the invention carried out.
As shown in Figure 1, preparing propylene from methanol system of the invention includes:
First reactor 1, for carrying out methanol-fueled CLC dimethyl ether reaction, to obtain the first product stream；First product
Stream includes dimethyl ether, water and unreacted methanol；First product flows through the output of the first product stream pipeline；Described first produces
Logistic pipeline includes flare line 6, the first pipeline 15 and the second pipeline 16, for will from the first reactor 1 first
Product stream exports respectively, and the flare line 6 be used for by the first product stream of part from the first reactor 1 export to
Flare system；
Second reactor 2, for carrying out the first product stream propylene reaction, to obtain the second product stream；And
Multiple catalyst beds are equipped in the second reactor 2 along longitudinal direction；
First water vapour pipeline 3, for providing vapor to the first reactor 1；
Heating device 7, for the first product stream from first pipeline 15 and from circulation hydrocarbon product stream pipeline
Circulation hydrocarbon product stream carry out heat temperature raising so that it send as the top feed of the second reactor 2 to the first catalyst
Bed；
First side line pipeline 9 divides for receiving the first product stream from second pipeline 16, and by received material
It does not send to second to most end catalyst bed；
Second lateral line canal road 10, for sending water respectively to second to most end catalyst bed；
Refined unit 11, for being separated to second product stream, to obtain comprising C2, C4, C5 and C6 component
Hydrocarbon product stream is recycled, the circulation hydrocarbon product stream is sent into the heating at least partially by the circulation hydrocarbon product stream pipeline 8
In device 7；
Recycle hydrocarbons storage tank 18, for providing circulation hydrocarbon product stream to the heating device 7.
It will be understood by those skilled in the art that first reactor 1 is DME reactor (i.e. preparing dimethyl ether from methanol reactor),
Second reactor 2 is MTP reactor (i.e. methanol to propylene reaction device).
It will be understood by those skilled in the art that in the present invention, water can be process water, and the source of process water includes first
Alcohol reaction generates the water generated when dimethyl ether, methanol/dimethyl ether reaction generates the water generated when alkene and preparing propylene from methanol system
The water that generates after the vapor condensation being passed through in system, the summation of this three parts water are known as process water, process water primarily to
The recirculated water of factory distinguishes.Process steam is exactly to be added using process water as raw material by process steam tower tower bottom reboiler
Heat, the vapor of generation.Process steam with steam such as low pressure, high pressure, middle pressures primarily to distinguish.Water in the application
What steam referred to is process steam above-mentioned.
It is tank field that the source for recycling hydrocarbon product stream, which includes two: one sources, i.e., to coming from when being fed intake by preceding primary driving
Second product stream of second reactor carries out isolated；Second source is the of second reactor when feeding intake to this driving
Two product streams are isolated；Tank field is initially come from primarily to whole flow process is enable to operate, can be stablized to whole system
When operating, the second product stream that second reactor 2 generates, which can meet, stablizes supply to recycle hydrocarbons, does not need at this time again from tank
Area introduces the steady running that circulation hydrocarbon product stream ensures that whole system.
When refined unit 11 separates second product stream, the second product flows through gas-liquid separation after cooling, compression；
The liquid hydrocarbon (C4 and the above component) isolated, which enters, isolates remaining low boiling component C4, DME and a small amount of in debutanizing tower
C3 component, and enter dehexanizer from the tower bottom of debutanizing tower, C5 and C6 component obtained at the top of dehexanizer；It isolates
Gas hydrocarbon (C3 and following components) and overhead product C3 and the DME component of debutanizing tower enter depropanizing tower together and separated,
C2, C3 component are isolated from tower top, obtains C4 component from tower bottom；And C2, C3 component of depropanizing tower tower top enter dethanizer
In further separate, obtain C2 component from tower top, isolate C3 component from tower bottom；To obtain comprising C2, C4, C5 and C6 component
Circulation hydrocarbon product stream.
Preparing propylene from methanol system of the invention is provided with the first water vapour pipeline 3 to provide water to the first reactor 1
Steam, so that on the one hand heat temperature raising is carried out to the catalyst bed in first reactor 1, so that urging in first reactor 1
Agent bed reaches the reaction temperature of methanol gas phase dehydration dimethyl ether synthesizing reaction as early as possible, shortens charging time；Another aspect energy
Enough make the reaction heat of heat of adsorption and methanol gas phase dehydration dimethyl ether synthesizing reaction of the vapor in catalyst duct by successively suitable
It is secondary successively to discharge respectively, cause first reactor 1 that temperature runaway situation occurs so that two kinds of heat be prevented to be superimposed in first reactor 1.
Since temperature runaway all has larger impact to catalyst and reactor component, if not set first water vapour pipeline 3, needs to spend
Take longer time, dosing operation is carried out under the conditions of the manipulation relatively mitigated, to reduce temperature runaway in catalyst and reactor
The influence of component；And the temperature runaway situation, very of first reactor 1 can effectively be controlled by the way that the first water vapour pipeline 3 is arranged by inventing
To the occurrence of preventing temperature runaway in first reactor 1, so as to control during driving to feed intake in first reactor 1
Temperature runaway situation, so as to shorten driving charging time, reduces material waste and energy dissipation to realize the raising of rate of feeding.
In one embodiment, the preparing propylene from methanol system further includes the second water vapour pipeline 12, is used for from top
Vapor is provided to the second reactor 2；The heating device 7 is used for the first product from first pipeline 15
Stream, the vapor from the second water vapour pipeline 12 and the circulation hydrocarbon products from the circulation hydrocarbon product stream pipeline 8
Stream carries out heat temperature raising, so that it send as the top feed of the second reactor 2 to the first catalyst bed.
Vapor is provided from top to the second reactor 2 by the way that the second water vapour pipeline 12 is arranged, one side water steams
Gas can play the role of carrier gas as carrier, to reduce material benzenemethanol/DME partial pressure, improve reaction selectivity and propylene product
Yield；On the other hand material benzenemethanol can be diluted, contacts less material benzenemethanol with the catalyst in second reactor 2,
To delay the generation of catalyst surface carbon distribution.
In one embodiment, the preparing propylene from methanol system further includes First Heat Exchanger 4, for from the first water
The vapor of steam pipe line 3 heats up, so that it is with the methanol from methanol line 5 together as the first reactor 1
Top feed, thus make the bed temperature of first reactor 1 reach as early as possible reaction needed for temperature, to shorten charging time.
In one embodiment, the first product stream pipeline further includes third pipeline 17, for will be from described the
The first product stream of part of one reactor 1 exports；The preparing propylene from methanol system further includes the second heat exchanger 13, for coming from
First product stream of the third pipeline 17 is sent into the first side line pipeline 9 after being cooled down.
The setting of second heat exchanger 13, so that the side entry feed of the second reactor 2 includes at least two parts: directly coming
The first product stream of part from the first reactor 1 and the first product stream after the cooling of the second heat exchanger 13, to pass through
This respective inlet amount of two parts material further regulates and controls the reaction bed temperature of the second reactor 2, to prevent
It states and temperature runaway situation occurs in second reactor 2.Since temperature runaway all has larger impact to catalyst and reactor component, if not
Second heat exchanger 13 is set, then needs to spend longer time, dosing operation is carried out under the conditions of the manipulation relatively mitigated, to drop
Influence of the low flight temperature to catalyst and reactor component；And the can easily be controlled by the way that the second heat exchanger 13 is arranged by inventing
Temperature runaway situation in two reactors 2 even prevents the occurrence of temperature runaway in second reactor 2, is driving so as to control
Temperature runaway situation during feeding intake in second reactor 2 realizes further increasing for rate of feeding, drives to further shorten
Charging time reduces material waste and energy dissipation.
In one embodiment, the preparing propylene from methanol system further includes third water vapour pipeline 14, for steaming water
Pneumatic transmission enters the first side line pipeline 9.
The setting of third water vapour pipeline 14, so that the side entry feed of the second reactor 2 includes at least three parts: straight
It fetches the first product stream of part from the first reactor 1, the first product stream after the cooling of the second heat exchanger 13 and comes from
The vapor of third water vapour pipeline 14, to further regulate and control described second by this respective inlet amount of three parts material
The reaction bed temperature of reactor 2, to prevent that temperature runaway situation occurs in the second reactor 2.Since temperature runaway is to catalyst
And reactor component all has larger impact, if not set second heat exchanger 13, needs to spend longer time, relatively slow
Dosing operation is carried out under the conditions of the manipulation of sum, to reduce influence of the temperature runaway to catalyst and reactor component；And it is of the invention
The temperature runaway situation in second reactor 2 can be more effectively controlled by setting third water vapour pipeline 14, even prevent second
In reactor 2 the occurrence of temperature runaway, so as to further control temperature runaway during driving to feed intake in second reactor 2
Situation realizes further increasing for rate of feeding, to further shorten driving charging time, few material waste and energy wave
Take.
It will be understood by those skilled in the art that switch valve and/or flow valve are provided on each pipeline and pipeline, with respectively
Whether the material stream in control respective lines or pipeline conveys, even by the aperture of switch valve or flow valve control respective lines
Or the ratio of the material stream on pipeline, so that the temperature of charge into catalyst bed each in reactor is adjusted, with prophylactic response
Temperature runaway situation occurs in device.For example, adjusting the three parts side of the second reactor 2 respectively by switch valve and/or flow valve
Line charging (the first product stream of part directly from the first reactor 1, the first product after the cooling of the second heat exchanger 13
Stream and the vapor from third water vapour pipeline 14) inlet amount, be finally sent into the second reactor 2 through side line to adjust
Second to most end catalyst bed temperature of charge, to adjust the second of the second reactor 2 to most end catalyst bed
The temperature of layer, to prevent that temperature runaway situation occurs in the second reactor 2.
The present invention also provides a kind of method for carrying out driving to feed intake using preparing propylene from methanol system above-mentioned, the method packets
Include following steps:
(1) 180-220 DEG C of (preferably 190- is successively purged and is warming up to the preparing propylene from methanol system with nitrogen
210 DEG C, such as 195 DEG C, 200 DEG C and 205 DEG C), then provided with the first water vapour pipeline 3 to the first reactor 1
Vapor is to be warming up to 255-260 DEG C (such as 256 DEG C, 257 DEG C and 258 for the catalyst bed in the first reactor 1
DEG C), preparing dimethyl ether from methanol reaction occurs in the first reactor 1 using the methanol of input and obtains the first product stream, and benefit
The pipeline 6 that applies a torch exports the first product stream from the first reactor 1 to flare system；
(2) it is no more than ± 5 DEG C to the out temperature difference of the first reactor 1, and its reaction bed temperature reaches
When to 265-320 DEG C (preferably 275-305 DEG C, such as 282 DEG C, 290 DEG C and 300 DEG C), the flare line 6 is closed, and by institute
The Feed space velocities for stating methanol are promoted to 0.65-0.75h-1(preferably 0.68-0.72h-1, such as 0.7h-1) (at this point, described first is anti-
The pressure in device 1 is answered to reach 1.0-1.45Mpa) after, the first product from the first reactor 1 is flowed through into first pipe
The output of line 15 is carried out into the heating device 7 after being warming up to 420-460 DEG C (preferably 430-450 DEG C, such as 440 DEG C), as
The top feed of the second reactor 2 is sent to the first catalyst bed, and methanol to propylene reaction occurs in second reactor 2
Obtain the second product stream；Then by second product stream be delivered to the refined unit 11 (close the flare line 6 it
Afterwards and the outlet temperature of the first reactor 1 is not up to before 325-345 DEG C (preferably 330-340 DEG C, such as 335 DEG C)
This stage, the heated device 7 of the first product stream from the first reactor 1 are inputted in second reactor 2 after heating and are produced
The second product stream is given birth to, is accumulated in the rectifying column in this second product stream of part input refined unit 11 to separate, still, until
When the outlet temperature of the first reactor 1 reaches 325-345 DEG C (preferably 330-340 DEG C, such as 335 DEG C), cumulant is also
Refined unit 11 cannot be made to separate it, will not more generate the circulation hydrocarbon product stream comprising C2, C4, C5 and C6 component)；
(3) outlet temperature to the first reactor 1 reaches 325-345 DEG C (preferably 330-340 DEG C, such as 335 DEG C)
When, the circulation hydrocarbon product stream of self-loopa in future hydrocarbon storage tank 18 inputs in the heating device 7 to be exported with through first pipeline 15
The first product stream carried out after being warming up to 420-460 DEG C (preferably 430-450 DEG C, such as 440 DEG C) together, it is anti-as described second
It answers the top feed of device 2 to send to the first catalyst bed, continues interior generation methanol to propylene reaction in second reactor 2 and obtain the
Two product streams；Then proceed to second product stream being delivered to the refined unit 11 and separate, obtain comprising C2, C4,
The circulation hydrocarbon product stream of C5 and C6 component；
Then the circulation hydrocarbon product stream from the refined unit 11 is also inputted in the heating device 7 and through described
First product stream of one pipeline 15 output and the circulation hydrocarbon product stream from the recycle hydrocarbons storage tank 18 are warming up to together
After 420-460 DEG C (preferably 430-450 DEG C, such as 440 DEG C), continue to be sent as the top feed of the second reactor 2 to
One catalyst bed obtains the second product stream to continue to occur methanol to propylene reaction；To the circulation from the refined unit 11
Hydrocarbon product stream can persistently meet the fuel requirements of the second reactor 2 (that is, the recycle hydrocarbons from the refined unit 11 produce
Logistics can be stablized is supplied to the second reactor 2 enough, or in addition to this there are also extra circulation hydrocarbon product stream, that
The circulation hydrocarbon product stream of redundance can be sent into tank field storage, use when driving feeds intake so as to next time, or be used as other
Purposes), stop supplying the circulation hydrocarbon product stream from recycle hydrocarbons storage tank 18 to the heating device 7；
(4) outlet temperature to the first reactor 1 reaches 360-375 DEG C (preferably 365-370 DEG C, such as 368 DEG C)
When, the first product stream exported through second pipeline 16 is received using the first side line pipeline 9, utilizes the second lateral line canal road
10 receive water, and send received material respectively as the side entry feed of the second reactor 2 urge to second to most end respectively
Agent bed obtains the second product stream to continue to occur methanol to propylene reaction, adjusts the catalyst bed of the second reactor 2
Layer temperature to 480-490 DEG C (preferably 483-488 DEG C, such as 485 DEG C) and is kept, and completes the process that feeds intake of driving.
When the reaction bed temperature of first reactor 1 reaches 255-260 DEG C, catalyst activity with higher,
Top feed is started to first reactor 1 at this time and helps to improve the methanol conversion and DME that preparing dimethyl ether from methanol reacts in it
Selectivity.
When first reactor 1 is fed, reaction raw materials penetrate catalyst from top to bottom, since reaction is exothermic reaction, with
The hot(test)-spot temperature (i.e. thermal self-restraint stress) of the extension of feed time, catalyst constantly moves down, the out temperature of first reactor 1
Following trend: first stage is presented, inlet temperature is higher than outlet temperature；Second stage, inlet temperature are suitable with outlet temperature；The
Three stages, inlet temperature are lower than outlet temperature.
The out temperature difference of first reactor 1 is no more than ± 5 DEG C, and its reaction bed temperature reaches 265-320
After DEG C, the reaction that dehydration generates dimethyl ether, the catalyst bed temperature difference (top feed mouth temperature and reaction takes place in material benzenemethanol
The temperature difference of device outlet temperature) increase, most of methanol converts, and reaction heat cumulative amount is reduced, and fuel factor reduces.Therefore the
The out temperature difference of one reactor 1 is no more than ± 5 DEG C, and when its reaction bed temperature reaches 265-320 DEG C, closing is put
Flare line promotes feed loading, and the first product from the first reactor 1 is flowed through the output of the first pipeline 15 extremely
It is carried out after being warming up to 420-460 DEG C in the heating device 7, second reactor 2 is fed.
Before the reaction bed temperature in the first reactor 1 is stablized, from the first product of the generation of first reactor 1
Stream should be exported to flare system burning and be handled, to prevent organic materials therein from threatening the safe operation of device.Not set
When one water vapour pipeline 3, the temperature of charge in first reactor 1 can not be adjusted, to be unable to control or prevent temperature runaway situation, is
It avoids affecting greatly catalyst and reactor component, the behaviour that feeds intake can only be carried out under the conditions of the manipulation relatively mitigated
Make, to spend longer time.And after the first water vapour pipeline 3 is set, on the one hand to the catalyst bed in first reactor 1
Layer carries out heat temperature raising, so as to reach methanol gas phase dehydration dimethyl ether synthesis as early as possible anti-for the catalyst bed in first reactor 1
The reaction temperature answered shortens charging time；On the other hand it can make heat of adsorption and methanol gas of the vapor in catalyst duct
The reaction heat of phase dehydration dimethyl ether synthesizing reaction by successively sequentially successively discharging respectively, to prevent two kinds of heat in first reactor
Superposition causes first reactor 1 that temperature runaway situation occurs in 1.By drive feed intake during to the temperature runaway in first reactor 1
The raising of rate of feeding is realized in the control of situation, so as to shorten driving charging time, reduces the material of output to flare system
Amount reduces material waste and energy dissipation.
When the outlet temperature of first reactor 1 reaches 325-345 DEG C, first reactor 1 reaches the steady state that feeds intake.Because
Feed intake middle first reactor 1, second reactor 2 of driving can regard two concatenated units as, if first unit is not achieved steadily
State, then the basis that second unit does not just adjust, even if controlling it has reached balance, first unit is slightly fluctuated, and second
Unit will be involved.Therefore start to carry out heating device 7 when the outlet temperature of first reactor 1 reaches 325-345 DEG C
It recycles the charging of hydrocarbon product stream and (charging herein refers to circulation hydrocarbon product stream and through first pipeline 15 output to charging
First product stream) be heated to 420-460 DEG C to supply second reactor 2, thus to second reactor 2 provide one for
The basis of adjustment.
When reaction bed temperature in second reactor 2 is 420-460 DEG C, catalyst activity with higher is low
In this temperature range, the conversion ratio and Propylene Selectivity of catalyst are lower；Higher than this temperature range, it is anti-that heat release can occur for catalyst
It answers, causes lower catalyst agent that overheating problem can occur, therefore, the outlet mass temperatures of the heating device 7 are 420-460 DEG C.
In one embodiment, in the step (1), the Feed space velocities of the methanol are 0.5-0.6h-1, preferably
0.53-0.57h-1, such as 0.55h-1。
In one embodiment, in the step (1), the vapor before being supplied to the first reactor 1,
200-220 DEG C, preferably 205-215 DEG C, such as 210 DEG C are warming up to using the First Heat Exchanger 4.
In one embodiment, in the step (3), the top feed of the second reactor 2 further includes vapor,
And be to be delivered in the heating device 7 by the second water vapour pipeline 12, with exported through first pipeline 15
One product stream and from circulation hydrocarbon product stream pipeline 8 circulation hydrocarbon product stream be heated to 420-460 DEG C of (preferably 430- together
450 DEG C, such as 440 DEG C) after, the top feed as second reactor 2 is sent to the first catalyst bed.
Vapor, one side vapor energy are provided from top to the second reactor 2 by the second water vapour pipeline 12
Enough play the role of carrier gas as carrier, to reduce material benzenemethanol/DME partial pressure, improves the production of reaction selectivity and propylene product
Rate；On the other hand material benzenemethanol can be diluted, contacts less material benzenemethanol with the catalyst in second reactor 2, to prolong
The generation of slow catalyst surface carbon distribution.
In one embodiment, in the step (3), the flow of the vapor from the second water vapour pipeline 12
For Q1, from it is described circulation hydrocarbon product stream pipeline 8 circulation hydrocarbon product stream flow be Q2, the first from the methanol line 5
The flow of alcohol is Q3, then since top feed the second reactor 2 to the second reactor 2 in the step (3)
Reaction bed temperature reaches 480-490 DEG C, and the ratio of (Q1+Q2)/Q3 is improved from 1:1 to 1.2:1.
Flow refers to the Fluid Volume that closed conduct or open channel effective cross-section are flowed through in the unit time, also known as instantaneous flow.When
Referred to as volume flow when Fluid Volume is indicated with volume；The referred to as mass flow when Fluid Volume is with quality representation.Stream in unit time
The volume of the fluid of a certain segment pipe, the referred to as volume flow of the cross section, referred to as flow are crossed, is indicated with Q.In the present invention
Flow refer to volume flow.
In one embodiment, in the step (4), the outlet temperature to the first reactor 1 reaches 360-375
When DEG C (preferably 365-370 DEG C, such as 368 DEG C), also using second heat exchanger 13 to the from the third pipeline 17
One product stream carries out being cooled to 220-235 DEG C (preferably 224-230 DEG C, such as 225 DEG C), then utilizes the first side line pipeline
9 receive the material after cooling, make itself and the first product stream from second pipeline 16 together as the second reactor 2
Side entry feed send respectively to second to most end catalyst bed with adjust second to most end catalyst bed feeding temperature.
By adjusting the material from second heat exchanger 13 and the first product from second pipeline 16 respectively
The inlet amount or charge proportion of stream control the temperature of the side entry feed of second heat exchanger 13, prevent second heat exchanger
Temperature runaway situation occurs in 13, so as to shorten driving charging time, reduces material waste and energy dissipation.
In one embodiment, in the step (4), the outlet temperature to the first reactor 1 reaches 360-375
When DEG C (preferably 365-370 DEG C, such as 368 DEG C), also using the third water vapour pipeline 14 from side line to second reaction
Device 2 provides vapor；And using the first side line pipeline 9 by from the third water vapour pipeline 14 vapor and come
The mixed material of material from second heat exchanger 13 and the first product stream from second pipeline 16 is sent respectively to
Two to most end catalyst bed with adjust second to most end catalyst bed feeding temperature.
By adjusting the vapor from the third water vapour pipeline 14, the object from second heat exchanger 13 respectively
The inlet amount or charge proportion of material and the first product stream from second pipeline 16, further control second heat exchanger
The temperature of 13 side entry feed prevents that temperature runaway situation occurs in second heat exchanger 13, drives to feed intake to further shorten
Time reduces material waste and energy dissipation.
The process of feeding intake of driving can adjust the inlet amount of different material by the feed rate of different pipelines, and then adjust first
The reaction bed temperature of reactor 1 and second reactor 2, thus prevent in fill process occur temperature runaway situation and to catalyst
And reactor component causes to damage, and improves rate of feeding, shortens charging time.
Startup procedure is further described with reference to embodiments
Embodiment 1
It carries out driving to feed intake using present invention preparing propylene from methanol system as shown in Figure 1, the process that feeds intake is as follows:
(1) about 200 DEG C are successively purged and are warming up to the preparing propylene from methanol system with nitrogen, then with described
One water vapour pipeline 3 provides vapor to the first reactor 1 the catalyst bed in the first reactor 1 to heat up
To about 257 DEG C, the methanol system two that carries out then is sent into first reactor 1 from top together with the methanol inputted through methanol line 5
Methyl ether reaction is obtained the first product stream, and will be exported from the first product stream of the first reactor 1 using flare line 6
To flare system；
(2) it is no more than ± 5 DEG C to the out temperature difference of the first reactor 1, and its reaction bed temperature reaches
When to about 290 DEG C, the flare line 6, and the 0.55h by the Feed space velocities of the methanol by are closed-1It is promoted to 0.7h-1Afterwards, by the first product from the first reactor 1 flow through first pipeline 15 output into the heating device 7 into
After row is warming up to about 440 DEG C, the top feed as the second reactor 2 is sent to the first catalyst bed, in the second reaction
Methanol to propylene reaction occurs in device 2 and obtains the second product stream；Then second product stream is delivered to the refined unit
11；
(3) when the outlet temperature of the first reactor 1 reaches about 335 DEG C, the circulation of self-loopa in future hydrocarbon storage tank 18
Hydrocarbon product stream and vapor from the second water vapour pipeline 12 input in the heating device 7 with it is defeated through first pipeline 15
After the first product stream out is warming up to about 440 DEG C together, the top feed as the second reactor 2 is sent to described
First catalyst bed of two reactors 2 continues that methanol to propylene reaction the second product of acquisition occurs in second reactor 2
Stream；It then proceedes to second product stream being delivered to the refined unit 11 and separate, obtain comprising C2, C4, C5 and C6
The circulation hydrocarbon product stream of component；
Then the circulation hydrocarbon product stream from the refined unit 11 is also inputted in the heating device 7 and through described
One pipeline 15 output the first product stream, the circulation hydrocarbon product stream from the recycle hydrocarbons storage tank 18 and come from the second steam pipe
After the vapor of line 12 is warming up to about 440 DEG C together, continue to send as the top feed of the second reactor 2 to first
Catalyst bed obtains the second product stream to continue to occur methanol to propylene reaction；To the recycle hydrocarbons from the refined unit 11
Product stream can persistently meet the fuel requirements of the second reactor 2, stop supplying to the heating device 7 from recycle hydrocarbons
The circulation hydrocarbon product stream of storage tank 18；
(4) when the outlet temperature of the first reactor 1 reaches about 365 DEG C, using second heat exchanger 13 to next
About 225 DEG C are cooled to from the first product stream of the third pipeline 17, then will come from the third water vapour pipeline 14
Vapor, the material from second heat exchanger 13 and the first product stream from second pipeline 16 mixed material
It send respectively through the first side line pipeline 9 to second to most end catalyst bed, and will be from second lateral line canal road 10
Water is also sent to second to most end catalyst bed, so that temperature of the adjusting second to most end catalyst bed, anti-to described second
It answers the reaction bed temperature of device 2 to stablize at about 485 DEG C, that is, completes driving and feed intake process, driving charging time is only 2 small
When.
Comparative example 1
Compared with Example 1, it during driving feeds intake preparing propylene from methanol system used, is not provided for first reactor 1
First water vapour pipeline 3 of offer vapor, first for heating up to the vapor from the first water vapour pipeline 3 are changed
Hot device 4, the second water vapour pipeline 12 for providing vapor from top to second reactor 2 are reacted for that will come from first
Device 1 the first product stream of part output with second reactor 3 feed from side line third pipeline 17, for come from third pipe
First product stream of line 17 is sent into the second heat exchanger 13 of the first side line pipeline 9, for vapor to be sent into the after being cooled down
The third water vapour pipeline 14 in one lateral line canal road 9；
Compared with Example 1, during feeding intake, only to the top feed methanol of first reactor 1, feed water is not steamed
Gas；Only feed cycle hydrocarbon product stream and the first product stream into the heating device 7, do not feed vapor；Only through the first side line
Side entry feed from pipeline 9 to second reactor 2 from the first product stream of the second pipeline 16, do not feed vapor and from third
Pipeline 17 and the first product stream to cool down through the second heat exchanger 13；Driving charging time is 11 hours.
As a result compare
In embodiment 1, it is 100% charging according to first reactor and second reactor that driving charging time, which is 2 hours,
The methanol consumption of load is 110t/h calculating, and the methanol feedstock consumption for putting flare system is 128 tons；Propene yield is
22.53%, LPG yield are 7.79%, and BTX aromatics yield is 9.7%, total recovery 40.08%；
Methanol feedstock enters the quantity of methyl alcohol that reaction is participated in second reactor 2 according to 220 tons of calculating, and according to market price first
2000 yuan/ton of alcohol, 8000 yuan/ton of propylene, 5000 yuan/ton of LPG, 6000 yuan/ton of BTX aromatics calculating, then it is primary to drive to feed intake
In,
The consumption of methanol are as follows: X1=2000 yuan/ton × (128+220) ton；
The income of product are as follows: Y1=8000 yuan/ton × 220 tons × 22.53% (propylene)+5000 yuan/ton × 220 tons ×
7.79%+6000 yuan/ton of (LPG) × 220 tons × 9.7% (BTX aromatics).
In comparative example 1, the methanol consumption for being 100% feed loading also according to first reactor and second reactor is
110t/h is calculated, and the methanol feedstock consumption for putting flare system is 713 tons；Propene yield is 8.27%, LPG yield is
6.92%, BTX aromatics yield be 3.0%, total recovery 18.19%；
Methanol feedstock enters the quantity of methyl alcohol that reaction is participated in second reactor 2 according to 220 tons of calculating, and according to market price first
2000 yuan/ton of alcohol, 8000 yuan/ton of propylene, 5000 yuan/ton of LPG, 6000 yuan/ton of BTX aromatics calculating, then it is primary to drive to feed intake
In, the consumption of methanol are as follows: X2=2000 yuan/ton × (713+220) ton；
The income of product are as follows: Y2=8000 yuan/ton × 220 tons × 8.27% (propylene)+5000 yuan/ton × 220 tons ×
6.92%+6000 yuan/ton of (LPG) × 220 tons × 3.0% (BTX aromatics).
It is 11 hours accordingly, with respect to driving charging time in comparative example 1, in the embodiment of the present application 1, driving charging time
Only 2 hours, 9 hours are shortened, just not saying cost of labor and energy consumption in this 9 hours, only consider it in methanol
The saving of raw material and the raising of product yield, economic well-being of workers and staff during primary driving feeds intake are as follows:
X2-X1=2000 yuan/ton × (713-128) ton (methanol)=1,170,000 yuan；
Y2-Y1=8000 yuan/ton × 220 tons × (22.53%-8.27%)+5000 yuan/ton × 220 tons × (7.79%-
6.92%)+6000 yuan/ton × 220 tons × (9.7%-3.0%)=34.81 ten thousand yuan；
It is 151.81 ten thousand yuan total.
It follows that carrying out driving to feed intake using the system and method for the application, when greatly can shorten driving and feeding intake
Between, while a large amount of methanol feedstock is saved, product yield is improved, huge economic benefit is thus brought.
Claims (10)
1. a kind of preparing propylene from methanol system characterized by comprising
First reactor (1), for carrying out methanol-fueled CLC dimethyl ether reaction, to obtain the first product stream；First product stream
Including dimethyl ether, water and unreacted methanol；First product flows through the output of the first product stream pipeline；First product
Flow tube line includes flare line (6), the first pipeline (15) and the second pipeline (16), for that will come from the first reactor (1)
The first product stream export respectively, and the flare line (6) for will from the first reactor (1) part first produce
Logistics is exported to flare system；
Second reactor (2), for carrying out the first product stream propylene reaction, to obtain the second product stream；And institute
It states and is equipped with multiple catalyst beds in second reactor (2) along longitudinal direction；
First water vapour pipeline (3), for providing vapor to the first reactor (1)；
Heating device (7), for the first product stream from first pipeline (15) and from circulation hydrocarbon product stream pipeline
(8) circulation hydrocarbon product stream carries out heat temperature raising, urges so that it send as the top feed of the second reactor (2) to first
Agent bed；
First side line pipeline (9) divides for receiving the first product stream from second pipeline (16), and by received material
It does not send to second to most end catalyst bed；
Second lateral line canal road (10), for sending water respectively to second to most end catalyst bed；
Refined unit (11), for being separated to second product stream, to obtain following comprising C2, C4, C5 and C6 component
The circulation hydrocarbon product stream is sent into the heating at least partially by the circulation hydrocarbon product stream pipeline (8) by cyclic hydrocarbon product stream
In device (7)；
Recycle hydrocarbons storage tank (18), for providing circulation hydrocarbon product stream to the heating device (7).
2. preparing propylene from methanol system according to claim 1, which is characterized in that the preparing propylene from methanol system further includes
Two water vapour pipelines (12), for providing vapor from top to the second reactor (2)；The heating device (7) is used for
To the first product stream from first pipeline (15) and the vapor from the second water vapour pipeline (12) and come
Heat temperature raising is carried out from the circulation hydrocarbon product stream of circulation hydrocarbon product stream pipeline (8), so that it is as the second reactor
(2) top feed is sent to the first catalyst bed；
Preferably, the preparing propylene from methanol system further includes First Heat Exchanger (4), for from the first water vapour pipeline (3)
Vapor heat up so that itself and from methanol line (5) methanol together as the first reactor (1) top
Charging.
3. preparing propylene from methanol system according to claim 2, which is characterized in that the first product stream pipeline further includes
Three pipelines (17), for that will be exported from first product stream of part of the first reactor (1)；The preparing propylene from methanol system
It further include the second heat exchanger (13), described in being sent into after cooling down to the first product stream from the third pipeline (17)
First side line pipeline (9).
4. preparing propylene from methanol system according to any one of claim 1-3, which is characterized in that the preparing propylene from methanol system
System further includes third water vapour pipeline (14), for vapor to be sent into the first side line pipeline (9).
5. a kind of method for carrying out driving to feed intake using preparing propylene from methanol system such as of any of claims 1-4,
It is characterized in that, described method includes following steps:
(1) 180-220 DEG C is successively purged and is warming up to the preparing propylene from methanol system with nitrogen, then with described first
Water vapour pipeline (3) Xiang Suoshu first reactor (1) provides vapor with by the catalyst bed in the first reactor (1)
It is warming up to 255-260 DEG C, preparing dimethyl ether from methanol reaction then occurs in the first reactor (1) using the methanol of input and obtains
The first product stream is obtained, and be exported the first product stream from the first reactor (1) to torch system using flare line (6)
System；
(2) it is no more than ± 5 DEG C to the out temperature difference of the first reactor (1), and its reaction bed temperature reaches
At 265-320 DEG C, close the flare line (6), and the Feed space velocities of the methanol are promoted to 0.65-0.75h-1, in the future
The first pipeline (15) output is flowed through from the first product of the first reactor (1) to carry out into the heating device (7)
After being warming up to 420-460 DEG C, the top feed as the second reactor (2) is sent to the first catalyst bed, anti-second
It answers and methanol to propylene reaction the second product stream of acquisition occurs in device (2)；Then second product stream is delivered to the purification
Unit (11)；
(3) when the outlet temperature of the first reactor (1) reaches 325-345 DEG C, self-loopa in future hydrocarbon storage tank (18) are followed
Cyclic hydrocarbon product stream is inputted in the heating device (7) and is risen together with the first product stream exported through first pipeline (15)
Temperature to after 420-460 DEG C, send to the first catalyst bed by the top feed as the second reactor (2), in the second reaction
Continue that methanol to propylene reaction the second product stream of acquisition occurs in device (2)；It then proceedes to second product stream being delivered to institute
It states refined unit (11) to be separated, obtains the circulation hydrocarbon product stream comprising C2, C4, C5 and C6 component；
Then the circulation hydrocarbon product stream from the refined unit (11) is also inputted in the heating device (7) and through described the
First product stream of one pipeline (15) output and the circulation hydrocarbon product stream from the recycle hydrocarbons storage tank (18) heat up together
To after 420-460 DEG C, continue to send to the first catalyst bed as the top feed of the second reactor (2) to continue in institute
It states and methanol to propylene reaction the second product stream of acquisition occurs in second reactor (2)；To following from the refined unit (11)
Cyclic hydrocarbon product stream can persistently meet the fuel requirements of the second reactor (2), stop supplying to come to the heating device (7)
The circulation hydrocarbon product stream of self-loopa hydrocarbon storage tank (18)；
(4) it when the outlet temperature of the first reactor (1) reaches 360-375 DEG C, is connect using the first side line pipeline (9)
The first product stream exported through second pipeline (16) is received, receives water using the second lateral line canal road (10), and will be received respectively
Material as the side entry feed of the second reactor (2) send respectively to second to most end catalyst bed with continue occur first
The reaction of alcohol propylene obtains the second product stream, adjusts the reaction bed temperature of the second reactor (2) to 480-490 DEG C simultaneously
It keeps, completes the process that feeds intake of driving.
6. according to the method described in claim 5, it is characterized in that,
In the step (1), the Feed space velocities of the methanol are 0.5-0.6h-1；
Preferably, in the step (1), the vapor utilizes described first before being supplied to the first reactor (1)
Heat exchanger (4) is warming up to 200-220 DEG C.
7. method according to claim 5 or 6, which is characterized in that
In the step (3), the top feed of the second reactor (2) further includes vapor, and is by second water
Steam pipe line (12) is delivered in the heating device (7), with the first product stream exported through first pipeline (15) and come
After the circulation hydrocarbon product stream of self-loopa hydrocarbon product stream pipeline (8) is heated to 420-460 DEG C together, as second reactor
(2) top feed is sent to the first catalyst bed.
8. the method according to the description of claim 7 is characterized in that coming from the second water vapour pipeline in the step (3)
(12) flow of vapor is Q1, the flow from the circulation hydrocarbon product stream for recycling hydrocarbon product stream pipeline (8) is Q2, comes
Be Q3 from the flow of the methanol of the methanol line (5), then in the step (3) since the second reactor (2) top
The reaction bed temperature for being fed into the second reactor (2) reaches 480-490 DEG C, and the ratio of (Q1+Q2)/Q3 is mentioned from 1:1
Up to 1.2:1.
9. the method according to any one of claim 5,6 and 8, which is characterized in that in the step (4), to described
When the outlet temperature of one reactor (1) reaches 360-375 DEG C, also using second heat exchanger (13) to from the third pipe
First product stream of line (17) carries out being cooled to 220-235 DEG C, after then receiving cooling using the first side line pipeline (9)
Material, make itself and from second pipeline (16) the first product stream together as the second reactor (2) side line into
Material send respectively to second to most end catalyst bed with adjust second to most end catalyst bed feeding temperature.
10. according to the method described in claim 9, it is characterized in that, in the step (4), to the first reactor (1)
When outlet temperature reaches 360-375 DEG C, also using the third water vapour pipeline (14) from side line to the second reactor (2)
Vapor is provided；And using the first side line pipeline (9) by from the third water vapour pipeline (14) vapor and
The mixed material of material from second heat exchanger (13) and the first product stream from second pipeline (16) difference
Send to second to most end catalyst bed with adjust second to most end catalyst bed feeding temperature.
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| CN114210082A (en) * | 2021-12-29 | 2022-03-22 | 中煤陕西榆林能源化工有限公司 | System and method capable of accelerating start of propylene rectifying tower |
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