CN106045809A - Reaction system and method for preparing ethylene by using slurry bed reactor - Google Patents
Reaction system and method for preparing ethylene by using slurry bed reactor Download PDFInfo
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- CN106045809A CN106045809A CN201610581539.XA CN201610581539A CN106045809A CN 106045809 A CN106045809 A CN 106045809A CN 201610581539 A CN201610581539 A CN 201610581539A CN 106045809 A CN106045809 A CN 106045809A
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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
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
- B01J8/0085—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction promoting uninterrupted fluid flow, e.g. by filtering out particles in front of the catalyst layer
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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
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
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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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00026—Controlling or regulating the heat exchange system
- B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
- B01J2208/00088—Flow rate measurement
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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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00548—Flow
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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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00628—Controlling the composition of the reactive mixture
- B01J2208/00637—Means for stopping or slowing down the reaction
Abstract
The invention relates to a reaction system and method for preparing ethylene by using a slurry bed reactor. The system comprises the slurry bed reactor, a condenser, a condensation separator, a solvent pump, a solvent mixing tank, a solvent temperature control system, filter equipment, a green oil removing system, a high-temperature heating device and a catalyst reduction device, wherein the solvent temperature control system comprises a heater, a solvent bypass and a cooler; the solvent mixing tank communicates with the slurry bed reactor; the filter equipment communicates with the slurry bed reactor; the condenser communicates with the slurry bed reactor; the solvent temperature control system communicates with the slurry bed reactor; the condenser, the condensation separator and the solvent mixing tank communicate with one another successively; the solvent mixing tank, the solvent pump and the solvent temperature control system communicate with one another successively; the filter equipment, the high-temperature heating device, the catalyst reducing device and the solvent mixing tank communicate with one another successively; and the filter equipment, the green oil removing system and the solvent mixing tank communicate with one another successively. By the reaction system and method, the problems that heat inside prepared ethylene cannot be transferred out easily, and the utilization rate of a catalyst is low can be solved effectively.
Description
Technical field
Present invention relates generally to the preparation field of ethylene, be specifically related to a kind of utilize prepared in slurry bed reactor for ethylene anti-
Answer system and method.
Background technology
Ethylene is a kind of important basic material in modern industry, is also one of maximum chemicals of world wide production, and it produces
Product are widely used in the fields such as national economy, people's lives, national defence, are " mothers of organic synthesis ".Shortage in the face of petroleum resources
Soaring with international oil price, raw material sources become the bottleneck of development ethylene industry, are also asking of must solving in face of people of pendulum
Topic.Therefore, a kind of new Technology is researched and developed to prepare ethylene, to be allowed to petroleum replacing as industrial raw materials, it is possible to
Alleviate the modern industry dependency to oil.
In coal chemical technology, with coal for raw material by carbide technique, or pass through Non-catalytic partial with natural gas for raw material
Oxidation technology produces acetylene, it has also become maturation process.Again with acetylene as raw material, under the effect of selective hydrocatalyst, logical
Cross hydrogenation process and obtain ethylene product, Coal Chemical Industry Route can be expanded further.Therefore, the new technology of producing ethylene with acetylene hydrogenation is developed
Technology, has broad application prospects.
Low concentration acetylene gas solid catalysis hydrogen addition technology is the most highly developed, is mainly used in ethylene removing
Acetylene impurities, the reactor of use is fixed bed reactors, and filling solid-phase catalyst carries out gas-solid phase reaction in the reactor.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 is solid phase fixed bed
Hydrogenation reactor there are still 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 comprises the following steps:
Catalyst and diluent is added in fluidized-bed reactor；Catalyst is carried out heating reduction；Acetylene and hydrogen mixture are led to
Fluidized bed reactor；Selective hydrogenation of acetylene generates ethylene；Cooling medium is passed through reactor heat exchange component to remove reaction
Heat；Isolated ethylene product.This Technology has the disadvantage in that
Preparing ethylene by selective hydrogenation of acetylene is strong exothermal reaction, although when cooling medium is in order to remove reaction in the process
The substantial amounts of heat released, but still it is difficult to hidden danger that when reacting local gas temperature too high is completely eliminated；
The fluid bed used because of this technique, is just difficult to avoid that the mutual sharp impacts of catalyst particles intergranular, and this can bring catalysis
The problems such as the abrasion of the loss of agent, the difficulty of increase dedusting, increase heat exchange component and reactor.
Prior art two is continuously separated production line for a kind of ethylene, including oxygen hydrogenation reactor, cracking gas the second exsiccator,
Removal of mercaptans/cos reactor, dearsenization reactor, acetylene hydrogenation reactor.Its acetylene hydrogenation reactor used is used
Reactor is fixed bed reactors.It is merely able to process the acetylene of low concentration, and treating capacity is smaller；If acetylene content increases,
A large amount of green oil, the problem causing catalyst cycle period to shorten, even there will be reactor " temperature runaway " can be generated.
Therefore, so that reactor adapts to larger amount of reaction acetylene gas, do not result in catalyst utilization low,
The problem of reactor " temperature runaway ", fundamentally improves gas-liquid flow field distribution, the quality fluidized in improving 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 a kind of utilize prepared in slurry bed reactor for the response system of ethylene and method, to solve
Certainly prior art prepares the problem that ethylene makes internal heat be difficult to spread out of, catalyst utilization is low.
The present invention provide a kind of utilize prepared in slurry bed reactor for the response system of ethylene, comprising: paste state bed reactor,
Condenser, condensation separator, solvent pump, solvent blending tank, solvent temperature control system, filter plant, green oil removing system, high temperature add
Thermal and catalyst reduction device；Wherein, described paste state bed reactor includes that housing and sieve plate, the bottom of described housing are provided with
Reaction gas inlet, liquid outlet；The top of described housing is provided with gas outlet and liquid inlet；Described sieve plate is positioned at described shell
Internal, it is fixed in described inner walls, is positioned under described liquid inlet, on described reaction gas inlet；Described solvent
Temperature control system includes that the bypass of heater, solvent and cooler, described heater and described cooler are set up in parallel, by described solvent
Road is connected with described cooler with described heater respectively by heat exchange pipeline；Described solvent blending tank passes through described liquid outlet
Connecting with described paste state bed reactor, described filter plant is connected with described paste state bed reactor by described liquid outlet, institute
Stating condenser to be connected with described paste state bed reactor by described gas outlet, described solvent temperature control system is entered by described liquid
Mouth connects with described paste state bed reactor；Described condenser, described condensation separator and described solvent blending tank are sequentially communicated；Institute
State solvent blending tank, described solvent pump and described solvent temperature control system to be sequentially communicated；Described filter plant, described high-temperature heating fill
Put, described catalyst reduction device and described solvent blending tank are sequentially communicated；Described filter plant, described green oil removing system and
Described solvent blending tank is sequentially communicated.
Above-mentioned system, is provided with agitating device in described solvent blending 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 inside described paste state bed reactor, the sieve plate of adjacent layer
Between spaced, the interval of each layer sieve plate is equal.
The described sieve plate of above-mentioned system every layer includes seal pot, bubbling area, downflow weir and downspout；Wherein, described sieve plate
Part edge fix with described inner walls；Revocable edge is provided with downflow weir, and described downflow weir is used for keeping every layer of institute
State the liquid having certain altitude on sieve plate；Downspout described in upper strata is seal pot in the view field of sieve plate described in lower floor, is used for
Hold the liquid flowed down from downspout described in upper strata；Described downspout is by the inwall of the downflow weir of described sieve plate and described housing
Gap is formed, and is located at the side of described downflow weir, for making liquid flow to described in lower floor at the downflow weir of sieve plate described in upper strata
The seal pot of sieve plate, keeps the seriality of liquid phase；The centre of described sieve plate is described bubbling area, and it is evenly distributed with sieve
Hole.
Above-mentioned system, described sieve aperture is equally distributed circular aperture, and the centre-to-centre spacing of described aperture is the 1-5 in aperture
Times, a diameter of 3-20mm 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 the height of sieve plate downflow weir described in lower floor.
The present invention provides a kind of method utilizing said system to prepare ethylene, and described method includes: by acetylene and hydrogen
Gaseous mixture is sent in described paste state bed reactor；Utilize described solvent pump by the liquid flux in described solvent blending tank and catalysis
Agent is sent in described solvent temperature control system, is sent to described slurry after regulating the temperature of described liquid flux and catalyst again
In bed reactor；Described liquid flux and catalyst is made to flow to described slurry bed system through described sieve plate in described paste state bed reactor
The bottom of reactor；The gaseous mixture making described acetylene and hydrogen is reacted by catalyst；Make described acetylene and hydrogen reaction
After gas circulate into described condenser from described paste state bed reactor, then by described condensation separator, after described reaction
Gas in solvent condense out；The solvent condensed out is made to enter into described solvent blending tank, by condensed gas again
Cooled isolated ethylene；Make the partially liq solvent bottom described paste state bed reactor and catalyst enter described solvent to mix
Close tank, another part liquid flux and catalyst by described filter plant；By molten for described another part liquid of being filtrated to get
Agent returns again to described solvent blending tank after sending into described green oil removing system；The described another part catalyst being filtrated to get is depended on
The described high-temperature heating equipment of secondary feeding, catalyst reduction device and solvent blending tank.
Above-mentioned method, described method further comprises the steps of: by opening described heater and making described heater with described
Solvent bypass, the flow controlling heat exchange power and described bypass solvent controls the intensification speed of liquid flux and catalyst
Rate；By opening described cooler and making described cooler and described solvent bypass, control cooling power, solvent bypass
Flow controls the rate of temperature fall of described liquid flux and catalyst；Bypass with described solvent by alternately opening described heater
Connection and heating or the connection of described cooler and described solvent bypass and cooling, to maintain described liquid flux and catalyst
Stablizing of temperature.
The beneficial effects of the present invention is, the present invention propose a kind of new utilize prepared in slurry bed reactor for ethylene anti-
Answering system and method, this response system and method are simple to operation, and course of reaction is easily achieved shifting heat, catalyst profit capable of circulation
With, it is possible to remove green oil in time so that utilizing paste state bed reactor to carry out high concentration selective hydrogenation of acetylene becomes a kind of important
The production ways of alkene processed.
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 described in more details, in order to energy
The advantage being enough more fully understood that the solution of the present invention and its various aspects.But, specific embodiments described below and reality
Executing example is only descriptive purpose rather than limitation of the present invention.
If Fig. 1 is the structure chart of the paste state bed reactor in the present invention.Wherein: 1, reaction gas inlet；2, liquid outlet；
3, gas outlet；4, liquid inlet；5, sieve plate；6, downspout；7, seal pot；8, bubbling area.
The principle of paste state bed reactor be gas with bubbling form by being suspended with liquid (serosity) layer of solid fine grain, with
Realize the reactor of gas-liquid-solid phase reaction process.This kind is for the paste state bed reactor of preparing ethylene by selective hydrogenation of acetylene, described
Paste state bed reactor includes reactor shell and sieve plate 5.
Reactor shell bottom is provided with reaction gas inlet 1 and liquid outlet 2, and gas outlet is arranged at reactor shell top
3 and liquid inlet 4.
Described sieve plate 5 is positioned at described housing, is fixed in described inner walls, is positioned under described liquid inlet 4, institute
State on reaction gas inlet 1.
Middle part in reactor enclosure body, is evenly distributed sieve plate 5.Every layer of sieve plate 5 has seal pot 7, downflow weir,
Downspout 6 and bubbling area 8.The part edge of sieve plate 5 is fixed with inner walls, and revocable edge is provided with downflow weir.
Upper strata downspout is called seal pot in the view field of lower floor's sieve plate, for holding the liquid flowed down from upper strata downspout
Body.
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 maintain on every layer of sieve plate to be had
The liquid of certain altitude.It is next to downspout 6 at downflow weir.Specifically, downspout 6 can by the downflow weir of described sieve plate 5 with
The gap of described reactor wall is formed.Certainly downspout 6 may also be other structure is such as pipeline configuration.The work of downspout 6
With being the seal pot 7 allowing liquid flow to lower floor's sieve plate at the downflow weir of upper strata sieve plate.The bottom of the downspout 6 of upper strata sieve plate 5
The not higher than height of lower floor's sieve plate 5 downflow weir.So design is to realize fluid-tight, i.e. prevents gas from rising at downspout 6
Each layer gas is caused to connect and short-circuit.Central region on sieve plate 5 is bubbling area 8, and it is uniform-distribution with sieve aperture, and it is circle
Shape aperture.Aperture is the main thoroughfare that gas rises, it is possible to make gas and liquid uniform contact.
The described downspout 6 of reactor adjacent layer is projected on circumferential angle on the direction being perpendicular to described seal pot 7
On be staggeredly arranged.The most conveniently realize the liquid that upper strata sieve plate 5 flows down and be stored in adjacent lower sieve plate 5 upper certain time, until
Liquid exceeds the downflow weir of this lower floor and flows out to the sieve plate 5 of lower floor again.
Aperture can keep pitching row's state with the flow direction of liquid, and the arrangement mode of aperture can be positive trigonometric expression.Small hole center away from
For 1-5 times of aperture, the centre-to-centre spacing between preferred hole is 1.5 times；A diameter of 3-20mm in hole, preferred hole a diameter of
10mm。
The sieve aperture of sieve plate also can be provided with float valve or bubble-cap.Float valve can float, along with gas flow on sieve plate
Change and change its open degree.There is riser in bubble-cap, between bubble-cap and riser, form rotary space.Riser is fixed on
On sieve plate, gas phase enters rotary space by riser, sprays by slot with certain spouting velocity, with the liquid shape on sieve plate
Become bubbling contact.
Being illustrated in figure 3 the response system utilizing prepared in slurry bed reactor for ethylene, it includes mentioning in described above
Paste state bed reactor 10, condenser 20, condensation separator 30, solvent blending tank 40, solvent pump 50, heater 60, cooler 70,
Filter plant 80, green oil removing system 90, high-temperature heating equipment 100 and catalyst reduction device 110.
The bypass of heater 60, solvent and cooler 70 constitute described solvent temperature control system, described heater 60 and described cold
But device 70 is set up in parallel, described solvent bypass (figure does not marks sequence number) by heat exchange pipeline respectively with described heater 60 and institute
State cooler 70 to connect.Described solvent blending tank 40 is connected with described paste state bed reactor 10 by described liquid outlet 2, described
Filter plant 80 connects with described paste state bed reactor 10 also by described liquid outlet 2.Described condenser 20 is by described gas
Body outlet 3 connects with described paste state bed reactor 10.Described solvent temperature control system is by described liquid inlet 4 and described slurry bed system
Reactor 10 connects.Described condenser 20, described condensation separator 30 and described solvent blending tank 40 are sequentially communicated.Described solvent
Blending tank 40, described solvent pump 50 and described solvent temperature control system are sequentially communicated.Described filter plant 80, described high-temperature heating fill
Put 100, described catalyst reduction device 110 and described solvent blending tank 40 to be also sequentially communicated.Described filter plant 80, described green
Oil removing system 90 and described solvent blending tank 40 are sequentially communicated.
Above-mentioned system, is provided with agitating device in described solvent blending tank 40, in solvent blending tank 40 solvent with urge
The stirring of agent.
Above-mentioned system, described condensation separator 30 connects ethylene collection device.When preparing ethylene, acetylene and hydrogen mixed
Close gas to be entered in reactor by the reaction gas inlet 1 bottom paste state bed reactor 10.Reacting gas is by reactor
Aperture on the sieve plate in portion enters among liquid phase.The liquid inlet 4 on catalyst and carrier solvent autoreactor top flows into.
Because aperture is equally distributed on sieve plate 5, 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 departs from this layer of sieve plate 5, then
Entered in the middle of supernatant liquid by the aperture of upper strata sieve plate 5.The most repeatedly until passing through reactor sieve plate 5 topmost, from
The gas outlet 3 of reactor top goes out.
In the reactor, gas be to lower and on the flow direction, liquid is the flow direction from top to down, gas phase and liquid phase overall in
Reveal the direction of adverse current, increase the effect of mass transfer and heat transfer.Owing to reactor having multiple sieve plate, namely mean reaction
Device also exists multiple little paste state bed reactor, increases the contact area that gas-liquid-solid three-phase is fully contacted, improve gas-liquid
Flow Field Distribution, it is to avoid short circuit, 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 20, gas temperature is cooled down.Subsequently,
By condensation separator 30, the solvent in gas is condensed out again.The solvent condensed out enters into solvent blending tank 40, gas
Body i.e. can get product ethylene through degree of depth refrigerated separation again.
Solvent at reactor bottom is entered in filter plant 80 by liquid outlet 2 rear portion, and a part is then entered
Enter to solvent blending tank 40.Enter into the solvent in filter plant 80, catalyst is filtered out from solvent.Molten after filtration
Agent enters in green oil removing system 90, is separated with solvent by green oil by green oil removing system 90, and solvent enters back into solvent
In blending tank 40, green oil then enters green oil storage tank and preserves.The catalyst filtered out from filter plant 80 is again through high temperature
After the calcining of heater 100, it is possible to the impurity such as the green oil of effective Removal of catalyst surface attachment and solvent, it is achieved catalyst
Regeneration.But the catalyst after calcination is oxidation state, therefore to realize the reduction of catalyst again through catalyst reduction device 110.
Catalyst after reducing/regenerating adds to solvent blending tank 40 again.
In solvent blending tank 40, it is provided with agitating device, by the catalysts and solvents of reactor bottom, carrys out autocondensation and divide
Solvent in device 30, from the solvent of filter plant 80, catalyst mix homogeneously after reduction.Pass through solvent pump again
50, solvent is driven in temperature control system.Temperature control system is made up of heater 60, solvent bypass and cooler 70 three-line,
Can regulate and control according to the different operating modes needed for reactor.When solvent needs to heat up when, it is switched on heater 60 and molten
Agent bypasses, and controls heating rate by the flow of regulation heat exchange power and solvent bypass.When reactor is in reaction, reactor
Need to move heat, it is possible to the cooling power simultaneously controlling the heating power of heater 60, bypass flow and cooler 70 controls
Solvent temperature keeps stable.When system need cooling time, be switched on cooler 70 and solvent bypass, by regulation heat exchange power and
The flow of solvent bypass controls rate of temperature fall.Temperature control system disclosure satisfy that the control for system temperature of the slurry bed system each operating mode.
It should be noted that owing to the solvent of slurry bed system containing rigid granules, heater 60 and the heat exchange of cooler 70
Pipeline can not be too thin, and has prevented dead angle, prevents catalyst deposit from blocking pipeline.
Solvent is by, after temperature control system temperature control, by the colvent inlet of reactor head, entering in reactor.In reaction
Solvent in device, more step by step by every layer of sieve plate, flow to reactor bottom.
It is real that high-temperature heating equipment 100 in the present invention can use the heaters such as electrical heating, revolving bed, fluid bed
Existing.
Compared with the technology of acetylene hydrogenation a small amount of with current ethylene, this technology can realize being added by high concentration selective acetylene
Hydrogen ethylene, has expanded the technology path of Coal Chemical Industry further.
Further, in technical solution of the present invention, gas be to lower and on the flow direction, liquid is stream from top to down
To, gas phase and liquid phase entirety present the direction of adverse current, increase the effect of mass transfer and heat transfer.
Further, the reactor of technical scheme there is multiple sieve plate, namely mean reactor is deposited
At multiple little paste state bed reactors, increase the area that gas-liquid-solid three-phase is fully contacted, improve gas-liquid flow field distribution, can
Avoid short circuit, but also turbulence and gas-liquid mass transfer can be strengthened, the quality fluidized in improving reactor.
Further, system is provided with green oil removing system and catalyst regeneration system, significantly reduce green oil and
Catalyst activity reduces the impact on reaction, it is achieved that the smooth long term running of device；The system and method for the present invention makes simultaneously
Obtain catalyst can recycle, improve the utilization ratio of catalyst.
Technical scheme utilizes the sensible heat of liquid phase solvent, and (sensible heat refers to, when this heat adds or after removing, can lead
Cause the change of mass temperature, and do not undergo phase transition), heat-sinking capability significantly improves, and can be quickly moved out because of selective hydrogenation of acetylene
The heat generating ethylene and produce, reduces the temperature of reaction bed, improves conversion ratio and the selectivity of ethylene of acetylene.
It addition, the system of the technical program is provided with temperature control system (bypass of heater, solvent and cooler), it is possible to real
The now accurate control to system solvent temperature, the temperature keeping solvent is the most stable, thus ensure that the steady fortune of whole system
OK.And, the solvent that reactor top condenses out re-starts heating so that solvent temperature is more homogeneous, so that reactor
Interior temperature is more uniform.
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
There is " temperature runaway " phenomenon, the catalyst bed that can cause during preferably suppressing preparation of ethylene through selective hydrogenation of acetylene because of exothermic reaction
The appearance of focus in Ceng, it is possible to remove green oil in time, it is to avoid catalysqt deactivation, improves the stability of catalyst.The present invention proposes
Equipment use catalyst recycling mode solve 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.Native system reacts
The operation pressure of device is 0.15-0.3MPa, and temperature is 100-180 DEG C.First with nitrogen as in source of the gas, with paste state bed reactor 10
The solvent containing catalyst set up gas-liquid flow to.Subsequently, more gradually open the heater 60 of temperature control system gradually to heat up solvent
System.After the solvent temperature in reactor reaches target temperature and system even running, then acetylene and hydrogen are passed into
In reactor.In the reactor, acetylene and hydrogen generate ethylene under the catalytic action of catalyst.Reacted gas passes through again
Condenser 20 and condensation separator 30, after being condensed out by the solvent in gas, then send reaction battery limit (BL).Condense from reactor top
The solvent condensed out in separator 30 enters in solvent blending tank 40.After solvent is mixed homogeneously with catalyst, with solvent pump
50 enter in temperature control system, enter back in reactor.
When finding that catalyst activity reduces when, a part is contained the solvent of catalyst by filter plant 80, mistake
Leach catalysts and solvents.The solvent filtered out is again by green oil removing system 90.Will by green oil removing system 90
Green oil separates with solvent, after removing green oil, then is transferred to by solvent in solvent blending tank 40.The catalyst filtered out leads to the most again
Cross high-temperature heating equipment 100 and catalyst reduction device 110, it is achieved the regeneration of catalyst.The most again by the catalyst after regeneration
It is transferred in the middle of solvent blending tank 40.After solvent is mixed homogeneously in solvent blending tank 40 with catalyst, use solvent pump 50 will
It is transported to temperature control system, then enters reactor from the liquid inlet 4 of reactor head.
In the present embodiment, the solvent of use is N-Methyl pyrrolidone.The temperature that temperature control system maintains solvent is relative
Stable, thus maintain stablizing of system temperature.When starting selective hydrogenation of acetylene reaction, the substantial amounts of heat of releasing is permissible
Realized by temperature control system heat exchange, it is to avoid internal system local temperature is too high.The particle diameter of the catalyst used is 40-150 μ
m。
It is last that it is noted that obviously above-described embodiment is only for clearly demonstrating example of the present invention, and also
The non-restriction to embodiment.For those of ordinary skill in the field, can also do on the basis of the above description
Go out change or the variation of other multi-form.Here without also cannot all of embodiment be given exhaustive.And thus drawn
What Shen went out obviously changes or changes among still in protection scope of the present invention.
Claims (10)
1. utilize prepared in slurry bed reactor for a response system for ethylene, comprising: paste state bed reactor, condenser, condensation
Separator, solvent pump, solvent blending tank, solvent temperature control system, filter plant, green oil remove system, high-temperature heating equipment and urge
Agent reduction apparatus；
Wherein, described paste state bed reactor includes housing and sieve plate,
The bottom of described housing is provided with reaction gas inlet, liquid outlet；The top of described housing is provided with gas outlet and liquid
Entrance；
Described sieve plate is positioned at described housing, is fixed in described inner walls, is positioned under described liquid inlet, described reaction
On gas access；
Described solvent temperature control system includes that the bypass of heater, solvent and cooler, described heater and described cooler set side by side
Putting, described solvent by-passes around heat exchange pipeline and is connected with described cooler with described heater respectively；
Described solvent blending tank is connected with described paste state bed reactor by described liquid outlet, and described filter plant is by described
Liquid outlet connects with described paste state bed reactor, and described condenser is by described gas outlet with described paste state bed reactor even
Logical, described solvent temperature control system is connected with described paste state bed reactor by described liquid inlet；Described condenser, described condensation
Separator and described solvent blending tank are sequentially communicated；Described solvent blending tank, described solvent pump and described solvent temperature control system depend on
Secondary connection；Described filter plant, described high-temperature heating equipment, described catalyst reduction device and described solvent blending tank connect successively
Logical；Described filter plant, described green oil removing system and described solvent blending tank are sequentially communicated.
System the most according to claim 1, it is characterised in that be provided with agitating device in described solvent blending tank.
System the most according to claim 1, it is characterised in that described condensation separator connection ethylene collection device.
System the most according to claim 1, it is characterised in that be dispersed with multilamellar inside described paste state bed reactor the most flat
The sieve plate of row, spaced between the sieve plate of adjacent layer, the interval of each layer sieve plate is equal.
System the most according to claim 1, it is characterised in that 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；Revocable edge is provided with downflow weir, institute
State downflow weir for keeping the liquid having certain altitude on every layer of described sieve plate；Downspout described in upper strata is at sieve plate described in lower floor
View field is seal pot, for holding the liquid flowed down from downspout described in upper strata；
Described downspout is formed by the gap of the downflow weir of described sieve plate Yu the inwall of described housing, is located at the side of described downflow weir
Limit, for making liquid flow to the seal pot of sieve plate described in lower floor at the downflow weir of sieve plate described in upper strata, keeps the continuous of liquid phase
Property；The centre of described sieve plate is described bubbling area, and it is evenly distributed with sieve aperture.
System the most according to claim 5, it is characterised in that described sieve aperture is equally distributed circular aperture, described little
The centre-to-centre spacing in hole is 1-5 times of aperture, a diameter of 3-20mm 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 float valve or bubble-cap.
System the most according to claim 5, it is characterised in that the bottom of the downspout of sieve plate described in upper strata is not higher than lower floor
The height of described sieve plate downflow weir.
9. utilize the method that system described in any one of claim 1 to 8 prepares ethylene, described method to include:
The gaseous mixture of acetylene and hydrogen is sent in described paste state bed reactor；
Described solvent pump is utilized to send in described solvent temperature control system by the liquid flux in described solvent blending tank and catalyst,
It is sent to again in described paste state bed reactor after regulating the temperature of described liquid flux and catalyst；Make described liquid flux
With the bottom that catalyst flow to described paste state bed reactor in described paste state bed reactor through described sieve plate；
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 condenser from described paste state bed reactor, then by described
Condensation separator, condenses out the solvent in described reacted gas；The solvent condensed out is made to enter into described solvent
Blending tank, by the most cooled for condensed gas isolated ethylene；
The partially liq solvent bottom described paste state bed reactor and catalyst is made to enter described solvent blending tank, another part liquid
Body solvent and catalyst are by described filter plant；The described another part liquid flux the being filtrated to get described green oil of feeding is taken off
Except returning again to described solvent blending tank after system；The described another part catalyst being filtrated to get is sequentially sent to described high temperature add
Thermal, catalyst reduction device and solvent blending tank.
Method the most according to claim 9, it is characterised in that described method further comprises the steps of:
By opening described heater and making described heater and described solvent bypass, control heat exchange power and described bypass
The flow of solvent controls the heating rate of liquid flux and catalyst；
By opening described cooler and making described cooler and described solvent bypass, control cooling power, solvent bypass
Flow control the rate of temperature fall of described liquid flux and catalyst；
By alternately opening by described heater and the connection of described solvent bypass and heating or described cooler and described solvent
The connection on road and cooling, to maintain stablizing of described liquid flux and catalyst temperature.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108069428A (en) * | 2016-11-18 | 2018-05-25 | 江苏中能硅业科技发展有限公司 | For handling the device and technique of polysilicon by-product slurry |
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| 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 |
| CN105175208A (en) * | 2015-08-07 | 2015-12-23 | 北京神雾环境能源科技集团股份有限公司 | Method for preparation of ethylene from hydrogenation of acetylene and reaction tower for the method |
| CN205893121U (en) * | 2016-07-21 | 2017-01-18 | 北京华福工程有限公司 | Utilize reaction system of thick liquid attitude bed reactor preparation ethylene |
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| 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 |
| CN105175208A (en) * | 2015-08-07 | 2015-12-23 | 北京神雾环境能源科技集团股份有限公司 | Method for preparation of ethylene from hydrogenation of acetylene and reaction tower for the method |
| CN205893121U (en) * | 2016-07-21 | 2017-01-18 | 北京华福工程有限公司 | Utilize reaction system of thick liquid attitude bed reactor preparation ethylene |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108069428A (en) * | 2016-11-18 | 2018-05-25 | 江苏中能硅业科技发展有限公司 | For handling the device and technique of polysilicon by-product slurry |
| CN108069428B (en) * | 2016-11-18 | 2023-10-10 | 江苏中能硅业科技发展有限公司 | Device and process for treating polysilicon byproduct slag slurry |
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Effective date of registration: 20200527 Address after: 100121 1105, floor 1, building 1, yard 18, Shuangqiao East Road, Chaoyang District, Beijing Patentee after: Beijing Jintai Chengrui Technology Development Co., Ltd Address before: 102200 No. 18 Fukang Road, Changping District science and Technology Park, Beijing Patentee before: BEIJING HUAFU ENGINEERING Co.,Ltd. |