CN105906470A - Reaction system for preparing ethylene by inputting gas at different heights and method - Google Patents
Reaction system for preparing ethylene by inputting gas at different heights and method Download PDFInfo
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- CN105906470A CN105906470A CN201610417508.0A CN201610417508A CN105906470A CN 105906470 A CN105906470 A CN 105906470A CN 201610417508 A CN201610417508 A CN 201610417508A CN 105906470 A CN105906470 A CN 105906470A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/08—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds
- C07C5/09—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds to carbon-to-carbon double bonds
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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
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/04—Ethylene
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
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- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention relates to a reaction system for preparing ethylene by inputting gas at different heights and a method. The system comprises a slurry state bed reactor, a condenser, a condensation separator, a condensate storage tank, a solvent pump, a tower bottom solvent storage tank, a filtering device, a green oil removing system, a high-temperature heating device and a catalyst reduction device. The slurry state bed reactor comprises a shell, a heater and a screen plate. The lower portion of the side face of the shell and the middle portion of the side face of the shell are provided with reaction gas inlets, and the lower portion of the shell is provided with a liquid solvent inlet and a liquid outlet. The upper portion of the shell is provided with a gas outlet and a liquid inlet. The invention further provides the method for preparing ethylene through the system. The method includes the steps of sending mixed gas of acetylene and hydrogen into the slurry state bed reactor for reaction, conducting condensation separation on reaction gas to obtain ethylene, and conducting filtering to obtain a catalyst which can be recycled. The problems that in the prior art, when ethylene is prepared, inner heat is not transmitted out easily, and the catalyst is low in utilization rate are solved.
Description
Technical field
Present invention relates generally to the preparation field of ethylene, be specifically related to a kind of differing heights input gas
The response system preparing ethylene and method.
Background technology
Ethylene is a kind of important basic material in modern industry, is also the chemistry of world wide production maximum
One of product, its product is widely used in the fields such as national economy, people's lives, national defence, is " to have
The mother of machine synthesis ".In the face of the shortage of petroleum resources and riseing of international oil price, raw material sources become
The bottleneck of development ethylene industry, is also to put the problem that must solve in face of people.Therefore, research
Develop a kind of new Technology to prepare ethylene, to be allowed to petroleum replacing as industrial raw materials,
The modern industry dependency to oil can be alleviated.
In coal chemical technology, with coal for raw material by carbide technique, or lead to natural gas for raw material
Cross non-catalytic partial oxidation technique and produce acetylene, it has also become maturation process.Again with acetylene as raw material,
Under the effect of selective hydrocatalyst, obtain ethylene product by hydrogenation process, can be further
Expand Coal Chemical Industry Route.Therefore, the novel technique of exploitation producing ethylene with acetylene hydrogenation, have wide
Application prospect.
Low concentration acetylene gas solid catalysis hydrogen addition technology is the most highly developed, mainly uses
Removing acetylene impurities in ethylene, the reactor of use is fixed bed reactors, fills in the reactor
Fill out solid-phase catalyst and carry out gas-solid phase reaction.But owing to ethyne reactive is high, hydrogenation reaction thermal discharge is big,
Even there is a small amount of acetylene in cracking gas, traditional gas-solid fixes bed hydroprocessing reactor and still suffers from
The serious problems such as green oil generating amount is big, catalyst cycle period is short, reactor easily " temperature runaway ".
Prior art one is fluidized-bed process and the device of a kind of producing ethylene with acetylene hydrogenation.This technique bag
Include following steps: in fluidized-bed reactor, add catalyst and diluent；Catalyst is risen
Temperature reduction；Acetylene and hydrogen mixture are passed through fluidized-bed reactor；Selective hydrogenation of acetylene generates
Ethylene；Cooling medium is passed through reactor heat exchange component to remove reaction heat；Isolated ethylene produces
Product.This Technology has the disadvantage in that
Preparing ethylene by selective hydrogenation of acetylene is strong exothermal reaction, although cooling medium is used in the process
The substantial amounts of heat released during to remove reaction, but still it is difficult to be completely eliminated local when reacting
The hidden danger that gas temperature is too high；
The fluid bed used because of this technique, is just difficult to avoid that the mutual sharp impacts of catalyst particles intergranular,
This can bring the loss of catalyst, increase the difficulty of dedusting, increase heat exchange component and the mill of reactor
The problems such as damage.
Prior art two is continuously separated production line, including oxygen hydrogenation reactor, cracking for a kind of ethylene
Gas the second exsiccator, removal of mercaptans/cos reactor, dearsenization reactor, acetylene hydrogenation reactor.
The reactor that its acetylene hydrogenation reactor used is used is fixed bed reactors.It is merely able to process
The acetylene of low concentration, and treating capacity is smaller；If acetylene content increase, can generate a large amount of green oil,
Cause the problem that catalyst cycle period shortens, even there will be reactor " temperature runaway ".
Therefore, so that reactor adapts to larger amount of reaction acetylene gas, do not result in and urge
Agent utilization rate is low, the problem of reactor " temperature runaway ", fundamentally improves gas-liquid flow field distribution,
Improve the quality of fluidisation in reactor, it is necessary to propose a kind of new response system preparing ethylene and
Method.
Summary of the invention
It is an object of the invention to provide the reaction system preparing ethylene of a kind of differing heights input gas
System and method, with solve prior art prepare ethylene make internal heat be difficult to spread out of, catalyst profit
By the low problem of rate.
The present invention provides the response system preparing ethylene of a kind of differing heights input gas, comprising:
Paste state bed reactor, condenser, condensation separator, condensate tank, solvent pump, tower base solvent store up
Tank, filter plant, green oil removing system, high-temperature heating equipment and catalyst reduction device；Wherein institute
State paste state bed reactor and include housing, heater and sieve plate；The bottom of described housing side and housing side
The middle part in face is provided with reaction gas inlet；The bottom of described housing is provided with liquid flux entrance and liquid discharge
Mouthful；The top of described housing is provided with gas outlet and liquid inlet；Described heater is arranged on described shell
Internal bottom；Described sieve plate is positioned at described housing, is fixed in described inner walls, is positioned at institute
State under liquid inlet, on described reaction gas inlet, described liquid flux entrance；Described green oil
Removing system is connected with described paste state bed reactor by described liquid flux entrance, described tower base solvent
Storage tank is connected with described paste state bed reactor by described liquid outlet, and described condenser passes through described gas
Body outlet connects with described paste state bed reactor, and described solvent pump is by described liquid inlet and described slurry
State bed reactor connects；Described condenser, described condensation separator, described condensate tank and described
Solvent pump is sequentially communicated；Described tower base solvent storage tank, described filter plant, described high-temperature heating equipment,
Described catalyst reduction device and described condensate tank are sequentially communicated；Described filter plant is green with described
Oil removing system connectivity.
Above-mentioned system, is provided with agitating device in described condensate tank.
Above-mentioned system, described condensation separator connection ethylene collection device.
Above-mentioned system, is dispersed with the sieve plate that multilamellar is parallel to each other, phase inside described paste state bed reactor
Between the sieve plate of adjacent bed spaced, the interval of each layer sieve plate is equal.
Above-mentioned system, every layer of described sieve plate includes seal pot, bubbling area, downflow weir and downspout；
Wherein, the part edge of described sieve plate is fixed with described inner walls；Described fixing part edge with
The part that described downflow weir fences up is seal pot；For holding the liquid flowed down from downspout described in upper strata
Body；The centre of described seal pot is distributed sieve aperture, forms bubbling area, and described bubbling area is gas-liquid
The main region of reaction；Described downflow weir is located at revocable edge of described sieve plate, described downflow weir
Higher than the seal pot of place layer, for keeping the height of liquid on every layer of described sieve plate；Described downspout
For making liquid flow to the seal pot of sieve plate described in lower floor from the downflow weir of sieve plate described in upper strata, it is positioned at institute
State the side of downflow weir.
Above-mentioned system, described sieve aperture is equally distributed circular aperture, and the centre-to-centre spacing of described aperture is
1-5 times of aperture, a diameter of 5-20mm of described aperture.
Above-mentioned system, the sieve aperture of described sieve plate is provided with float valve or bubble-cap.
Above-mentioned system, the bottom of the downspout of sieve plate described in upper strata is not higher than sieve plate overflow described in lower floor
The height on weir.
The present invention provides a kind of method utilizing said system to prepare ethylene, and described method includes:
The gaseous mixture of acetylene and hydrogen is sent in described paste state bed reactor；Described solvent pump is utilized to incite somebody to action
Liquid flux and catalyst in described condensate tank are sent in described paste state bed reactor；Make described
Liquid flux and catalyst flow to described slurry reactor through described sieve plate in described paste state bed reactor
The bottom of device；Utilize the described heater bottom described paste state bed reactor that described liquid flux is evaporated
For solvent vapo(u)r；The gaseous mixture making described acetylene and hydrogen is reacted by catalyst；Make described second
Alkynes and the reacted gas of hydrogen circulate into described condenser from described paste state bed reactor, then pass through institute
State condensation separator, the solvent in described reacted gas is condensed out；Make to condense out is molten
Agent enters into described condensate tank, by the most cooled for condensed gas isolated ethylene；Make institute
State the partially liq solvent bottom paste state bed reactor and catalyst enters described tower base solvent storage tank, then
By described filter plant；The described partially liq solvent being filtrated to get is sent into the removing of described green oil is
The bottom of described paste state bed reactor is returned again to after system；By the described partial catalyst that is filtrated to get successively
Send into described high-temperature heating equipment, catalyst reduction device and condensate tank.
Above-mentioned method, by the agitating device in described condensate tank by described catalyst and described
After liquid flux mix homogeneously, then by described solvent pump by described mixed described catalyst and institute
State liquid flux to send in described paste state bed reactor.
The beneficial effects of the present invention is, the present invention proposes a kind of new differing heights input gas
Preparing response system and the method for ethylene, this response system and method are simple to operation, course of reaction
It is easily achieved shifting heat, catalyst reusable edible, it is possible to remove green oil in time so that utilize slurry
Bed reactor carries out high concentration selective hydrogenation of acetylene and becomes the production way of a kind of important alkene processed
Footpath.
Accompanying drawing explanation
Fig. 1 is the structural representation that technical solution of the present invention prepares the paste state bed reactor of ethylene；
Fig. 2 is the plan structure schematic diagram of sieve plate in technical solution of the present invention；And
Fig. 3 is the system structure schematic flow sheet that technical solution of the present invention embodiment prepares ethylene.
Detailed description of the invention
Below in conjunction with drawings and Examples, the detailed description of the invention of the present invention is carried out more detailed
Explanation, so as to the advantage being more fully understood that the solution of the present invention and its various aspects.But,
Specific embodiments described below and embodiment are only descriptive purposes rather than to the present invention
Limit.
If Fig. 1 is the structure chart of the paste state bed reactor in the present invention.Wherein: 1, reacting gas
Entrance；2, liquid outlet；3, gas outlet；4, liquid inlet；5, sieve plate；6, descending liquid
Pipe；7, heater；8, solvent liquid entrance.
The principle of paste state bed reactor is that gas (is starched by being suspended with the liquid of solid fine grain with bubbling form
Liquid) layer, to realize the reactor of gas-liquid-solid phase reaction process.This kind is used for selective hydrogenation of acetylene system
The paste state bed reactor of ethylene, described paste state bed reactor includes reactor shell, heater 7 and
Sieve plate 5.
The bottom of reactor enclosure body side surface and the middle part of housing side are provided with reaction gas inlet 1；
Reactor shell bottom is provided with solvent liquid entrance 8 and liquid outlet 2, and reactor shell top has
Gas outlet 3.
At the bottom having heaters 7 of reactor, it penetrates in reactor enclosure body.Wherein, heater
7 can make solvent evaporate, it is provided that the steam air-flow risen continuously, provide for whole reactor simultaneously
Thermal source.
Described sieve plate 5 is positioned at described housing, is fixed in described inner walls, is positioned at described liquid
Under entrance 4, on described reaction gas inlet 1, described liquid flux entrance 8.
Middle part in reactor enclosure body, is evenly distributed sieve plate 5.Every layer of sieve plate 5 has
Seal pot, downflow weir, downspout 6 and bubbling area.The part edge of sieve plate is fixed with inner walls,
Revocable edge is provided with downflow weir.The part that fixing part edge and described downflow weir fence up is
Seal pot, for holding the liquid flowed down from upper strata downspout.
The top view of sieve plate 5 is as shown in Figure 2.Effect at the downflow weir of one end of sieve plate 5 is to protect
Hold the liquid having certain altitude on every layer of sieve plate.It is next to downspout 6 at downflow weir.Specifically,
Downspout can be formed by the gap of the downflow weir of described sieve plate Yu described reactor wall.Certainly downspout 6
May also be other structure is such as pipeline configuration.The effect of downspout 6 is to allow liquid from upper strata sieve plate
Downflow weir at flow to the seal pot of lower floor's sieve plate.The bottom of the downspout 6 of upper strata sieve plate 5 is the highest
Height in lower floor's sieve plate 5 downflow weir.So design be to realize fluid-tight, i.e. prevent gas from
Rising at downspout 6 causes each layer gas to connect and short-circuit.Central region on sieve plate 5 is bubbling
District, it is uniform-distribution with circular aperture.Aperture is the main thoroughfare that gas rises, it is possible to make
Gas and liquid uniform contact.
Described downspout 6 being projected on the direction being perpendicular to described seal pot of reactor adjacent layer
It is staggeredly arranged on circumferential angle.The most conveniently realize the liquid that upper strata sieve plate 5 flows down be stored in adjacent under
Layer sieve plate 5 upper certain time, until liquid exceeds the downflow weir of this lower floor and flows out to the sieve of lower floor again
Plate 5.
Aperture can keep pitching row's state with the flow direction of liquid, and the arrangement mode of aperture can be positive triangle
Formula.Small hole center is away from for 1-5 times of aperture, and the centre-to-centre spacing between preferred hole is 1.5 times；Hole
A diameter of 5-20mm, a diameter of 10mm in preferred hole.
The position of the reaction gas inlet 1 at the middle part of reactor enclosure body side surface between two-layer sieve plate 5,
And higher than the height of lower floor's sieve plate downflow weir.Reacting gas is after by which floor sieve plate, owing to adding
The generation of hydrogen reaction, the flow of gas has a certain degree of minimizing, little in order to make full use of every layer
Paste state bed reactor, is passed through reacting gas from reactor differing heights and can make full use of reactor,
Increase the utilization ratio of reactor.
The sieve aperture of sieve plate also can be provided with float valve or bubble-cap.Float valve can float on sieve plate, with
The change of gas flow and change its open degree.Riser is had, at bubble-cap and riser in bubble-cap
Between formed rotary space.Riser is fixed on sieve plate, and gas phase enters revolution sky by riser
Between, sprayed by slot with certain spouting velocity, form bubbling with the liquid on sieve plate and contact.
Being illustrated in figure 3 the response system preparing ethylene of differing heights input gas, it includes above-mentioned
The paste state bed reactor 10 mentioned in explanation, condenser 30, condensation separator 40, condensate tank
50, solvent pump 60, tower base solvent storage tank 70, filter plant 80, green oil removing system 90, high temperature
Heater 100 and catalyst reduction device 110.Green oil removing system 90 is by described liquid flux
Entrance connects with described paste state bed reactor 10, and described tower base solvent storage tank 70 is by described liquid discharge
Mouth connects with described paste state bed reactor 10, and described condenser 30 passes through described gas outlet with described
Paste state bed reactor 10 connects, and described solvent pump 60 is anti-with described slurry bed system by described liquid inlet
Device 10 is answered to connect；Described condenser 30, described condensation separator 40, described condensate tank 50 and
Described solvent pump 60 is sequentially communicated；Described tower base solvent storage tank 70, described filter plant 80, described
High-temperature heating equipment 100, described catalyst reduction device 110 and described condensate tank 50 connect successively
Logical, catalyst passes sequentially through the said equipment；Described paste state bed reactor 10, described tower base solvent storage tank
70, described filter plant 80 connects with described green oil removing system 90, and solvent passes sequentially through above-mentioned setting
Standby.
Above-mentioned system, is provided with agitating device in described condensate tank 50, for condensate tank 50
Middle solvent and the stirring of catalyst.
When preparing ethylene, the gaseous mixture of acetylene and hydrogen passes through paste state bed reactor 10 housing side
Bottom and the reaction gas inlet 1 at middle part of housing side enter in reactor；Reacting gas
Along with solvent vapo(u)r is entered among liquid phase by the aperture on the sieve plate of inside reactor together.Its
Middle solvent vapo(u)r is generated by 7 liquid flux heating evaporations of heater of reactor lower part.Catalysis
The liquid inlet 4 on agent and carrier solvent autoreactor top flows into.Because aperture is on sieve plate 5
It is equally distributed, so reacting gas evenly spreads in the middle of liquid the most therewith.In a liquid, instead
Answer and react under the catalytic action of gas catalyst in being suspended in liquid.Reacted gas
Depart from this layer of sieve plate 5, then entered in the middle of supernatant liquid by the aperture of upper strata sieve plate 5.So
Repeatedly until by reactor sieve plate 5 topmost, going out from the gas outlet 3 of reactor top.
In the reactor, gas be to lower and on the flow direction, liquid is the flow direction from top to down, gas
Present the direction of adverse current mutually with liquid phase entirety, increase the effect of mass transfer and heat transfer.Due to reaction
Device has multiple sieve plate, namely means reactor also exists multiple little slurry reactor
Device, increases the area that gas-liquid-solid three-phase is fully contacted, and improves gas-liquid flow field distribution, it is to avoid short
Road, but also turbulence and gas-liquid mass transfer can be strengthened, the quality fluidized in improving reactor.
From reactor top reaction gas out, then by the cooling of condenser 30 by gas temperature
Cool down.Subsequently, then by condensation separator 40 solvent in gas is condensed out.Cold
Coagulate the solvent got off and enter into condensate tank 50.Condensation separator 40 can connect ethylene further
Collection device, such as cryogenic separation device, gas i.e. can get product through degree of depth refrigerated separation again
Ethylene.
Solvent at reactor bottom enters into tower base solvent storage tank 70 by liquid outlet, then leads to
Cross filter plant 80, the catalyst after filtration again after the calcining of high-temperature heating equipment 100,
Can the effective impurity such as the green oil of Removal of catalyst surface attachment and solvent, it is achieved catalyst is again
Raw；But the catalyst after calcination is oxidation state, therefore will be through catalyst reduction device 110 with reality
The reduction of existing catalyst.Catalyst after reducing/regenerating adds to condensate tank 50 again.Cross
Solvent caught on a filter then enters in green oil removing system 90.By green oil removing system 90 by green
Oil separates with solvent, and solvent is returned to reactor by the liquid inlet of reactor bottom, green
Oil then enters green oil storage tank and preserves.
In condensate tank 50, by agitating device by after catalysts and solvents mix homogeneously,
By solvent pump 60, mixed liquid is sent in reactor again.This process can realize catalysis
Recycling of agent.
In the present embodiment, the solvent of use is distilled water (electrical conductivity ＜ 5 μm/cm).From instead
Answering the steam of rising bottom device is the thermal source of whole reactor, keeps the most stable of system temperature.
When starting selective hydrogenation of acetylene reaction, the substantial amounts of heat of releasing can be come by the evaporation of solvent
Transfer, it is to avoid in reactor the phenomenon that local temperature is too high occurs.
Heater in the present invention can use electrical heating, steam heating, flue gas or conduction oil
The mode of heating realizes.
High-temperature heating equipment in the present invention can use the heating such as electrical heating, revolving bed, fluid bed
Device realizes.
Compared with the technology of acetylene hydrogenation a small amount of with current ethylene, this technology can realize by high concentration
Preparing ethylene by selective hydrogenation of acetylene, has expanded the technology path of Coal Chemical Industry further.
Further, in the inventive solutions, gas be to lower and on the flow direction, liquid
The flow direction from top to down, gas phase and liquid phase entirety present adverse current direction, increase mass transfer and
The effect of heat transfer.
Further, the present invention can be passed through the reaction gas of different proportion at the differing heights at reactor
Body, takes full advantage of the reaction capacity of different layers sieve plate on reactor, adds the utilization of reactor
Efficiency, and hydrogenation reaction is uniformly distributed, in reactor, liquidus temperature distribution is more uniform.
Further, the reactor of technical scheme there is multiple sieve plate, namely mean anti-
Answering and there is multiple little paste state bed reactor in device, increase that gas-liquid-solid three-phase is fully contacted connects
Contacting surface is amassed, and improves gas-liquid flow field distribution, can avoid short circuit, but also can strengthen turbulence and gas
Liquid mass transfer, the quality fluidized in improving reactor.
Further, system is provided with green oil removing system and catalyst regeneration system, greatly
Reduce green oil and catalyst activity reduces the impact on reaction, it is achieved that the long-term smooth fortune of device
OK；The system and method for the present invention makes catalyst to recycle simultaneously, improves catalyst
Utilization ratio.
Technical scheme utilize liquid phase solvent sensible heat (sensible heat refer to when this heat add or
After removing, the change of mass temperature can be caused, and do not undergo phase transition), heat-sinking capability significantly improves,
The heat produced because selective hydrogenation of acetylene generates ethylene can be quickly moved out, reduce reaction bed
Temperature, improves conversion ratio and the selectivity of ethylene of acetylene.
It addition, the heating system of the technical program is simple, just only rely on the heater of reactor bottom
It is capable of heat supply.
In a word, the response system of present invention offer and method, when carrying out selective hydrogenation of acetylene reaction,
Can be effectively prevented from " temperature runaway " phenomenon, can preferably suppress preparation of ethylene through selective hydrogenation of acetylene mistake
The appearance of focus in the beds caused because of exothermic reaction in journey, it is possible to removing is green in time
Oil, it is to avoid catalysqt deactivation, improves the stability of catalyst.The equipment that the present invention proposes uses and urges
The mode that agent recycles solves the problem that catalyst use efficiency is low well.
Embodiment 1
Use the system for preparing ethylene by selective hydrogenation of acetylene in embodiment as shown in Figure 3.
System structure form as described in above-mentioned embodiment.The operation pressure of this system is
0.25MPa, temperature is 130 DEG C.
Can first use nitrogen as the solvent containing catalyst in source of the gas, with paste state bed reactor 10
Set up gas-liquid to flow to；Subsequently, more gradually open bottom heater, set up steam ascending air.
When steam rises to reactor head cooling for reflux, and after temperature stabilization, can by nitrogen by
The gaseous mixture being gradually converted to hydrogen and acetylene gas is passed in the middle of reactor.
In the reactor, acetylene and hydrogen generate ethylene under the catalytic action of catalyst；After reaction
Gas again by condenser 30 and condensation separator 40, after the solvent in gas is condensed out,
Send response system battery limit (BL) again.Condensation separator 40 can connect ethylene collection device further, than
Such as cryogenic separation device, obtain ethylene product.
It flow to the catalyst of reactor bottom from reactor head with solvent, then pass through filter plant
80 filter out.When finding that catalyst activity reduces when, catalyst is passed sequentially through high temperature
Heater 100 and the catalyst regeneration system of catalyst reduction device 110 composition, it is achieved catalysis
The regeneration of agent, is transferred to the catalyst after regeneration in the middle of condensate tank 50 the most again.Catalysis
Agent after mix homogeneously, uses solvent pump 60 to be transported to reactor top in condensate tank 50
Portion.When the green oil amount found in solvent increases, when making reactivity reduce, can will set from filtration
Standby 80 solvents filtered out are passed in green oil removing system 90, remove green oil therein.Green oil
Removing system 90 and catalyst regeneration system significantly reduce green oil and catalyst activity reduction is right
The impact of reaction, it is achieved that the smooth long term running of device.
In the present embodiment, the solvent of use is distilled water (electrical conductivity ＜ 5 μm/cm), from reaction
The steam risen bottom device is the thermal source of whole reactor, keeps the most stable of system temperature.When
When starting selective hydrogenation of acetylene reaction, the substantial amounts of heat of releasing, can be come by the evaporation of solvent
Transfer, it is to avoid local temperature is too high.The particle diameter of the catalyst used is 40-150 μm, uses
The filtering accuracy of filter plant be 1 μm.
Last it is noted that obvious, above-described embodiment is only for clearly demonstrating institute of the present invention
The citing made, and not restriction to embodiment.Those of ordinary skill in the field are come
Say, can also make other changes in different forms on the basis of the above description.Here
Without also cannot all of embodiment be given exhaustive.And thus amplified out obvious
Change or change among still in protection scope of the present invention.
Claims (10)
1. the response system preparing ethylene of differing heights input gas, comprising: slurry bed system is anti-
Answer device, condenser, condensation separator, condensate tank, solvent pump, tower base solvent storage tank, filtration
Equipment, green oil removing system, high-temperature heating equipment and catalyst reduction device；
Wherein said paste state bed reactor includes housing, heater and sieve plate,
The bottom of described housing side and the middle part of housing side are provided with reaction gas inlet；Described housing
Bottom be provided with liquid flux entrance and liquid outlet；The top of described housing is provided with gas outlet and liquid
Body entrance；
Described heater is arranged on the bottom in described housing；
Described sieve plate is positioned at described housing, is fixed in described inner walls, is positioned at described liquid and enters
Under Kou, on described reaction gas inlet, described liquid flux entrance；
Described green oil removing system is connected with described paste state bed reactor by described liquid flux entrance,
Described tower base solvent storage tank is connected with described paste state bed reactor by described liquid outlet, described condensation
Device is connected with described paste state bed reactor by described gas outlet, and described solvent pump passes through described liquid
Entrance connects with described paste state bed reactor；
Described condenser, described condensation separator, described condensate tank and described solvent pump connect successively
Logical；Described tower base solvent storage tank, described filter plant, described high-temperature heating equipment, described catalyst
Reduction apparatus and described condensate tank are sequentially communicated；Described filter plant removes system with described green oil
Connection.
System the most according to claim 1, it is characterised in that be provided with in described condensate tank
Agitating device.
System the most according to claim 1, it is characterised in that described condensation separator connection second
Alkene collection device.
System the most according to claim 1, it is characterised in that inside described paste state bed reactor
It is dispersed with the sieve plate that multilamellar is parallel to each other, spaced between the sieve plate of adjacent layer, the interval of each layer sieve plate
Equal.
System the most according to claim 1, it is characterised in that every layer of described sieve plate includes by liquid
Dish, bubbling area, downflow weir and downspout；Wherein, in the part edge of described sieve plate and described housing
Wall is fixed；
The part that described fixing part edge and described downflow weir fence up is seal pot, is used for holding
The liquid flowed down from downspout described in upper strata；
The centre of described seal pot is distributed sieve aperture, forms bubbling area, and described bubbling area is gas-liquid
The main region of reaction；Described downflow weir is located at revocable edge of described sieve plate, described downflow weir
Higher than the seal pot of place layer, for keeping the height of liquid on every layer of described sieve plate；
Described downspout is for making liquid flow to sieve plate described in lower floor from the downflow weir of sieve plate described in upper strata
Seal pot, is positioned at the side of described downflow weir.
System the most according to claim 5, it is characterised in that described sieve aperture is equally distributed
Circular aperture, the centre-to-centre spacing of described aperture is 1-5 times of aperture, a diameter of 5-20mm of described aperture.
System the most according to claim 5, it is characterised in that the sieve aperture of described sieve plate is provided with floating
Valve or bubble-cap.
System the most according to claim 5, it is characterised in that the downspout of sieve plate described in upper strata
Bottom be not higher than the height of sieve plate downflow weir described in lower floor.
9. utilize the method that system described in any one of claim 1 to 8 prepares ethylene, described side
Method includes:
The gaseous mixture of acetylene and hydrogen is sent in described paste state bed reactor；
Utilize described solvent pump that the liquid flux in described condensate tank and catalyst are sent into described slurry
In state bed reactor；
Described liquid flux and catalyst is made to flow to through described sieve plate in described paste state bed reactor described
The bottom of paste state bed reactor；
Utilize the described heater bottom described paste state bed reactor that described liquid flux is evaporated to solvent
Steam；
The gaseous mixture making described acetylene and hydrogen is reacted by catalyst；
Described acetylene and the reacted gas of hydrogen is made to circulate into described condensation from described paste state bed reactor
Device, then by described condensation separator, the solvent in described reacted gas is condensed out；Make
The solvent condensed out enters into described condensate tank, separates the most cooled for condensed gas
To ethylene；
The partially liq solvent bottom described paste state bed reactor and catalyst is made to enter described tower base solvent
Storage tank, then by described filter plant；The described partially liq solvent being filtrated to get is sent into described green
The bottom of described paste state bed reactor is returned again to after oil removing system；The described part being filtrated to get is urged
Agent is sequentially sent to described high-temperature heating equipment, catalyst reduction device and condensate tank.
Method the most according to claim 9, it is characterised in that by described condensate tank
In agitating device by after catalyst and liquid flux mix homogeneously, then by described solvent pump by described
Mixed described catalyst and described liquid flux are sent in described paste state bed reactor.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104826558A (en) * | 2015-05-15 | 2015-08-12 | 北京神雾环境能源科技集团股份有限公司 | Slurry bed reactor and reaction system for producing ethylene by using acetylene selective hydrogenation |
| CN105152836A (en) * | 2015-08-28 | 2015-12-16 | 北京神雾环境能源科技集团股份有限公司 | Method using acetylene hydrogenation to produce ethylene |
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2016
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104826558A (en) * | 2015-05-15 | 2015-08-12 | 北京神雾环境能源科技集团股份有限公司 | Slurry bed reactor and reaction system for producing ethylene by using acetylene selective hydrogenation |
| CN105152836A (en) * | 2015-08-28 | 2015-12-16 | 北京神雾环境能源科技集团股份有限公司 | Method using acetylene hydrogenation to produce ethylene |
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