CN106345374A - Reaction system and method for producing ethylene from acetylene - Google Patents
Reaction system and method for producing ethylene from acetylene Download PDFInfo
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- CN106345374A CN106345374A CN201610853243.9A CN201610853243A CN106345374A CN 106345374 A CN106345374 A CN 106345374A CN 201610853243 A CN201610853243 A CN 201610853243A CN 106345374 A CN106345374 A CN 106345374A
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- 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
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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
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/082—Controlling processes
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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
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/10—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by stirrers or by rotary drums or rotary receptacles or endless belts
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- 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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Abstract
The invention relates to a reaction system and method for producing ethylene from acetylene. The system comprises two hydrogenation reactors, a heat exchanger, a gas-liquid separator, a hydrogen extracting device and a regeneration tower, wherein the two hydrogenation reactors are of alternate use, and the other one is used for regenerating a catalyst when one is applied to a hydrogenation reaction; catalyst linings are arranged in the hydrogenation reactors, and the hydrogen extracting device comprises a gas inlet, a hydrogen gas outlet and an ethylene outlet; the regeneration tower comprises a material inlet, a solvent outlet and a green oil outlet; a reactant outlet of the hydrogenation reactor for the hydrogenation reaction is sequentially connected with the heat exchanger and the gas-liquid separator, a gas outlet of the gas-liquid separator is connected with the gas inlet of the hydrogen extracting device, and a liquid outlet of the gas-liquid separator is connected with the material inlet of the regeneration tower; a reactant outlet of the hydrogenation reactor for catalyst regeneration is connected with an inlet of the heat exchanger. According to the reaction system and method for producing the ethylene from the acetylene, provided by the invention, hydrogenation and catalyst regeneration can be achieved simultaneously, and the problem of high energy consumption in a high-temperature roasting regeneration process can be avoided.
Description
Technical field
Present invention relates generally to the preparation field of ethylene is and in particular to a kind of response system of acetylene ethylene and method.
Background technology
With petroleum resources increasingly depleted, developing the chemical process that Coal Chemical Industry is raw material becomes petroleum replacing chemical industry route
Significant process, this technology gets the attention, and achieves fast development.
In coal chemical technology, acetylene is produced for raw material by carbide technique with coal, has been widely used.It is former with acetylene again
Material, under selective hydrocatalyst effect, by Hydrogenation for ethylene product, can expand Coal Chemical Industry Route further.And it is near
Over a little years, supply exceed demand for the main downstream product polrvinyl chloride (pvc) of acetylene, and pvc industrial profit is not high, is badly in need of expanding second
Alkynes downstream product industrial chain；Ethylene is most important basic material in petrochemical industry, is referred to as " mother of petrochemical industry ".Extensively use
In plastics, lubricating oil, polymer and some intermediate, mainly pass through cracking by oil or low-carbon alkanes at present.Ethylene
Downstream product such as ethylene glycol, butanediol, acrylic acid, polyvinyl alcohol etc. also have good economic worth.Therefore, develop acetylene hydrogenation
The novel technique of ethylene processed can provide a kind of new raw material source for ethylene industry, and reduces the dependence to petroleum resources for the ethylene
Degree and the production cost of ethylene, have broad application prospects.
Although acetylene selective hydrogenation is the current focus of attention, report both domestic and external also compares many, its research contents master
Be applied to remove cracking petroleum hydrocarbon and prepare micro acetylene (0.01-5 volume %) during ethylene process, and for special with
High concentration acetylene is the catalysis selective hydrogenation technique for producing ethylene then rare exploration of raw material, and corresponding industrialization large-scale application is even more
Have no report.
A kind of existing technique using traditional fixed-bed catalytic hydrogenation.Solid catalyst used by this technology is typically using dipping
Prepared by method, active metal is uniformly distributed in catalyst surface.This technology dominant response is reacted for gas-solid contact, but acetylene hydrogenation
For strong exothermal reaction, fixed bed device and used catalyst move heat difficult it is impossible to control the depth of acetylene hydrogenation reaction.Substantial amounts of
Reaction heat can make palladium catalyst carbon distribution inactivate.Again because its activity is very high, in reaction, acetylene polymerization generates green oil, and covers
Catalyst surface leads to rapid catalyst deactivation.And due to the uncontrollable reaction depth of this technology, acetylene therefore can be caused
Deep hydrogenation generates ethane, thus reducing the yield of reaction target product ethylene.
Also have a kind of technique carrying out hydrogenation reaction using slurry bed system, reaction liberated heat can be removed, but due to
The blasting of gas, catalysts and solvents are constantly in flow regime under its drive, easily cause the abrasion of catalyst, and catalyst grinds
Easily carried by gas-liquid and cause damage again after damage, and there is difficult life of difficult recovery of solid catalyst used by slurry bed system etc. and ask
Topic.
Therefore, in order to avoid catalyst surface temperature rise is excessive, cause bed temperature runaway, it is to avoid acetylene autohemagglutination, ethylene are further
The generation of the side reactions such as hydrogenation, and the problem that catalyst activity inactivation, green oil waste is it is necessary to invent a kind of new acetylene second
The response system of alkene and method.
Content of the invention
It is an object of the invention to provide a kind of response system of acetylene ethylene and method, to solve prior art preparation
Ethylene makes the problem that internal heat is difficult to spread out of, reaction depth is uncontrollable, catalyst inactivation, green oil waste.
The present invention provides a kind of response system of acetylene ethylene, comprising: hydrogenation reactor, heat exchanger, gas-liquid separation
Device, carry hydrogen production device, regenerator, the quantity of described hydrogenation reactor is two, and this two hydrogenation reactors are used alternatingly, when wherein
One be used for hydrogenation reaction when, another be used for catalyst regeneration；Wherein, it is provided with catalyst layer in described hydrogenation reactor,
It includes reactant entrance and reactant outlet；The described hydrogen production device that carries includes gas access, hydrogen outlet and ethylene outlet；Described
Regenerator includes material inlet, solvent outlet and green oil outlet；Reactant for the described hydrogenation reactor of hydrogenation reaction goes out
Mouth connects the entrance of described heat exchanger, and the outlet of described heat exchanger connects the entrance of described gas-liquid separator；Described gas-liquid separation
The gas access of hydrogen production device is carried, the liquid outlet of described gas-liquid separator connects described regenerator described in gas outlet's connection of device
Material inlet；Reactant outlet for the described hydrogenation reactor of catalyst regeneration connects the entrance of described heat exchanger.
Further, the solvent outlet of regenerator described in above-mentioned system can connect the reactant of described hydrogenation reactor
Entrance.
Further, the hydrogen outlet carrying hydrogen production device described in above-mentioned system can connect the reaction of described hydrogenation reactor
Thing entrance.
Above-mentioned system, the reactant entrance of described hydrogenation reactor is provided with atomizer.
Above-mentioned system, the catalyst layer of described hydrogenation reactor is rotatable.
Above-mentioned system, can be provided with solvent pump and solution reservoir before described hydrogenation reactor.
The present invention provides a kind of method preparing ethylene using said system, and methods described includes step: by hydrogen, acetylene
The described hydrogenation reactor sent into for hydrogenation reaction with liquid phase solvent is reacted；Reactant after hydrogenation reaction is sent into institute
It is re-fed into described gas-liquid separator after stating heat exchanger to carry out separating, obtain gas and liquid；Send separating the described gas obtaining
Carry hydrogen production device described in entering to carry out proposing hydrogen process, obtain ethylene product；Enter separating the described liquid described regenerator of feeding obtaining
Row solvent reclamation；The hydrogenation reactor that reactant has been reacted and eliminated to liquid phase solvent feeding carries out catalyst regeneration；To urge
After product after agent regeneration sends into described heat exchanger heat exchange, enter gas-liquid separator separates, obtain separating solution；Will be described
Separate the solution described regenerator of feeding and carry out solvent reclamation, and obtain green oil product.
Above-mentioned method, methods described may further comprise the step of: and processes, by carrying hydrogen, the hydrogen described hydrogenation reaction of return extracted
Device is reacted；The solvent that regeneration is obtained returns described hydrogenation reactor and is circulated utilization；Solvent after regeneration is sent into
Carry out heat exchange process in reactant after hydrogenation reaction, make described temperature of charge cooling.
Further, solvent described in above-mentioned method includes n- N-methyl-2-2-pyrrolidone N (nmp), pyridine, imidazoles, quinoline
One or more of quinoline.
The beneficial effects of the present invention is, the present invention proposes a kind of new response system of acetylene ethylene and method,
This response system and method are simple to operation, and the main process temperature of this producing ethylene with acetylene hydrogenation technique can control 250
Operated below DEG C, thus catalyst regeneration process is low-temp recovery, thus avoiding the high energy of high-temperature roasting regenerative process
Consumption and the fume emission that brings of burn off Organic substance, it is to avoid the bed temperature runaway of catalyst high temperature initiation, acetylene autohemagglutination, ethylene occur
The generation of the side reaction such as hydrogenation further.
The hydrogenation plant of the present invention can realize hydrogenation simultaneously and catalyst regenerates two kinds of functions, and this technical process can be
Big degree reclaims the by-product green oil in acetylene hydrogenation course of reaction, it is to avoid green oil loss and wasting, and reduces catalysis
The energy consumption of agent regeneration, simplifies regenerative process.
Brief description
Fig. 1 is the flowage structure schematic diagram of acetylene ethylene process process of the present invention.
Specific embodiment
Below in conjunction with drawings and Examples, the specific embodiment of the present invention is described in more details, so that energy
The advantage enough more fully understanding the solution of the present invention and its various aspects.However, specific embodiments described below and reality
Applying example is only descriptive purpose, rather than limitation of the present invention.
If Fig. 1 is the flowage structure schematic diagram of acetylene ethylene process process in present embodiment.
The present invention mainly includes following device: two acetylene hydrogenations using the technique of high concentration producing ethylene with acetylene hydrogenation
Reactor i, ii, wherein hydrogenation reactor i is in running order, and another hydrogenation reactor ii is in catalyst reproduced state,
Vice versa；Heat exchanger, carries out heat exchange between the solution after reaction and regeneration；Gas-liquid separator, anti-for being hydrogenated with
Reacted gas-liquid mixture in device is answered to carry out the separation of gas-liquid；Regenerator, for the solvent of regeneration dissolving green oil, after regeneration
To solvent can be circulated utilization, the green oil obtaining after regeneration is reclaimed；Carry hydrogen production device, the gas after gas-liquid separation is carried out
Carry hydrogen to process, hydrogen can recycle as reaction gas, and ethylene is gas products to be obtained.
It is provided with catalyst layer, it includes reactant entrance and reactant outlet in described hydrogenation reactor.
The described hydrogen production device that carries includes gas access, hydrogen outlet and ethylene outlet.
Described regenerator includes material inlet, solvent outlet and green oil outlet.
Divide in the described hydrogenation reactor for hydrogenation reaction and for the hydrogenation reactor of catalytic regeneration with described gas-liquid
It is provided with heat exchanger between device, carry out heat exchange between the solution after reaction and regeneration.After heat exchange, solution is cooled to 100
DEG C about, after gas-liquid separation, liquid enters solvent regeneration tower.Solvent regeneration tower column bottom temperature controls at 140-240 DEG C.
Reactant outlet for the described hydrogenation reactor of hydrogenation reaction connects reconnection gas-liquid separator after heat exchanger
Entrance, the gas outlet of described gas-liquid separator connect described in carry the gas access of hydrogen production device, the liquid of described gas-liquid separator
Body outlet connects the material inlet of described regenerator.
Also described gas-liquid is connected after reactant outlet connection heat exchanger for the described hydrogenation reactor of catalyst regeneration
The entrance of separator.
For recycling of solvent, the solvent outlet of described regenerator can be connected the reactant of described hydrogenation reactor
Entrance.
Equally, for the recycling of hydrogen, the described hydrogen outlet carrying hydrogen production device can be connected described hydrogenation reactor
Reactant entrance.
Specifically, two hydrogenation reactors in the present invention, one of them is hydrogenated with another and is in regeneration stage.Regenerate
The reactor becoming is in resting state, and after reactor catalyst inactivates, then this reactor is regenerated, and another is carried out instead
Should.
When hydrogenation reactor is in hydrogenated state, the charging of this device is divided into biphase, three strands of raw materials, and liquid phase is organic molten
Agent, gas phase is the mixed gas of hydrogen and acetylene.Gas-liquid separator is entered back into after reacted gas-liquid mixture heat exchange.
Acetylene hydrogenation device reaction pressure is 0.1-0.4mpa, and reaction temperature controls between 100-200 DEG C.
Can enter through atomizer after the reactant entrance that hydrogen enters acetylene hydrogenation device together with liquid phase solvent and urge
Agent bed is reacted.
The volume ratio of hydrogen, acetylene and solvent is 30-900:7-250:1.
Acetylene hydrogenation device is the beds being in rotation status, and rotating speed is 50-1000rpm.
The catalyst of acetylene hydrogenation device is with molecular sieve, aluminium oxide, silicon dioxide, Kaolin and montmorillonite etc. as carrier
Load pd active metal and ag auxiliary agent, the mass ratio of pd and ag is 1:1-5.
When hydrogenation reactor is in reproduced state, the charging of this device then individually feeds for liquid phase.Liquid phase organic solvent is molten
De-covering is in the green oil of catalyst surface, and takes reactor out of, enters gas-liquid separator afterwards after heat exchange, and liquid enters back into regeneration
Tower carries out Regeneration Treatment, generates green oil product.Organic solvent after regeneration can be circulated use.Now, this device catalyst
Bed is still within rotation status, and rotating speed is 50-1000rpm.During regeneration extraction, reaction bed temperature controls at 40-100 DEG C
Between.
, after proposing hydrogen production device process, ethylene gas are as product, the hydrogen conduct of recovery for gas after gas-liquid separation
Hydrogenating materials return the hydrogenation plant being in hydrogenation working condition.
Renovation process of the present invention is solvent regeneration process, it is, extractant will be urged after flowing through reaction bed
The green oil that agent surface covers dissolves and takes reactor out of.
Catalyst extraction actified solution of the present invention can share a set of organic solvent with hydrogenation reaction organic solution
Regenerative system.
Organic solvent of the present invention specifically includes that n- N-methyl-2-2-pyrrolidone N (nmp), pyridine, imidazoles, quinoline etc.,
It can be the mixture of one or more of they.
The method of present invention ethylene, mainly comprises the steps that
Hydrogen, acetylene and liquid phase solvent are sent into and is used for the described hydrogenation reactor of hydrogenation reaction and is reacted.After reaction
Generate gas and liquid mixture.
Carry out separating by sending into described gas-liquid separator after the reactant heat exchange after hydrogenation reaction, obtain gas and liquid.
Carry hydrogen production device described in the described gas feeding that separation is obtained to carry out proposing hydrogen process, obtain ethylene product and hydrogen.
Carry out solvent reclamation by separating the liquid that obtains and sending into solvent regeneration tower, so that the recycling of solvent.
The hydrogenation reactor that reactant has been reacted and eliminated to liquid phase organic solvent feeding carries out catalyst regeneration.
Send into gas-liquid separator after product heat exchange after catalyst is regenerated to carry out separating, obtain separating solution.
Carry out solvent reclamation by separating solution feeding regenerator, and obtain green oil product.
Certainly, said method also can comprise the steps of
The hydrogen proposing hydrogen process extraction is returned described hydrogenation reactor reacted, formation recycles.
The solvent that regeneration is obtained returns described hydrogenation reactor and is circulated utilization, can serve as catalytic extraction agent and also may be used
As hydrogenation reaction solvent.
Also the solvent after regeneration can be sent in the reactant after hydrogenation reaction and carry out heat exchange process, make described reactant temperature
Degree cooling.
The response system of the present invention be different from fixed bed traditional gas-solid contact reaction, dominant response be solid catalyst and
Gas-liquid film haptoreaction.Non-polar organic solvent, acetylene and hydrogen enter the beds of rotation status through sprayer unit
In, carry out selective hydrogenation.The heat discharging in hydrogenation process so that the liquid of dissolved acetylene undergoes phase transition and changes, part
Gaseous state is changed into from liquid, removing reaction heat, thus avoiding catalyst surface temperature rise excessive, causing bed temperature runaway, it can be avoided that second
Alkynes autohemagglutination, ethylene such as are hydrogenated with further at a large amount of generations of side reaction.
Catalyst life-time service in acetylene hydrogenation reactor bed can cause green oil to cover in catalyst surface, thus making
Become catalyst active center cannot contact with reactant and lead to inactivate.The renovation process of catalyst and conventional catalyst in this technique
Agent renovation process is different, can not only fully recycle the green oil on catalyst surface, and reduce catalyst regeneration
Energy consumption, simplifies regenerative process.
Embodiment 1
Using as shown in Figure 1 for the system of acetylene ethylene in embodiment.
The pressure of hydrogenation plant acetylene unstripped gas is 0.3mpa, and the flow of acetylene is 6nm3/h；The raw gas pressure of hydrogen
For 0.3mpa, hydrogen flowing quantity is 30nm3/h.Organic solvent is squeezed in acetylene hydrogenation reactor by pump, and the outlet pressure of pump is
0.3mpa, flow is 0.8m3/h.
Reaction bed temperature controls at 150 DEG C, by the velocity of rotation that rotary electric machine controls beds is
500rpm.
The catalyst that beds adopt is а-al2o3 bead, and particle size distribution range is 2-5mm, supported active metals
Pd and ag.The load capacity of pd is 0.03% (wt), and the load capacity of ag is 0.07% (wt).
When the catalyst of hydrogenation plant is in reproduced state, regeneration pressure is normal pressure, and organic solvent flow is 0.4m3/ h,
Reaction bed temperature controls at 60 DEG C.
Product heat exchange is cooled to so as to enter into gas-liquid separator after 25 DEG C, the gas after separating enters and carries hydrogen
Device extracts circulating hydrogen, and liquid product then enters into solvent regeneration tower and carries out Regeneration Treatment.
Regenerator treating capacity is 1.2m3/ h, controls regenerator column bottom temperature to be 220 DEG C, the organic solvent after regeneration is from tower
Overhead stream goes out, and is circulated utilization, and green oil is then flowed out as product by bottom of towe.
The gas that gas-liquid separator separates go out enters and carries out after carrying hydrogen production device proposing hydrogen process, and hydrogen makes as unstripped gas circulation
With ethylene gas are as output of products.
After in hydrogenation plant, catalyst covers inactivation due to green oil, system switches into reproduced state operation, regeneration
Carry out hydroprocessing again after good catalyst.
Organic solvent is n- N-methyl-2-2-pyrrolidone N (nmp), pyridine, imidazoles, the mixture of quinoline.
Embodiment 2
The system of the producing ethylene with acetylene hydrogenation of the present embodiment and operating procedure such as embodiment 1, difference is used organic molten
Agent is different, and it is the mixture of n- N-methyl-2-2-pyrrolidone N (nmp) and pyridine.
Embodiment 3
The system of the producing ethylene with acetylene hydrogenation of the present embodiment and operating procedure such as embodiment 1, difference is used organic molten
Agent is different, and it is the mixture of n- N-methyl-2-2-pyrrolidone N (nmp) and imidazoles.
Embodiment 4
The system of the producing ethylene with acetylene hydrogenation of the present embodiment and operating procedure such as embodiment 1, difference is used organic molten
Agent is different, and it is the mixture of n- N-methyl-2-2-pyrrolidone N (nmp) and quinoline.
Embodiment 5
The system of the producing ethylene with acetylene hydrogenation of the present embodiment and operating procedure such as embodiment 1, difference is used organic molten
Agent is different, and it is n- N-methyl-2-2-pyrrolidone N (nmp).
Because the combination of organic solvent in the present invention is more, can be either of which kind or multiple mixture, thus
Here will not enumerate, and all should be understood that all of compound mode is all feasible for those of ordinary skill.
It is last that it is noted that obvious, above-described embodiment is only intended to clearly illustrate example of the present invention, and simultaneously
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-forms.There is no need to be exhaustive to all of embodiment.And thus drawn
Obvious change that Shen goes out or change among still in protection scope of the present invention.
Claims (9)
1. a kind of response system of acetylene ethylene, comprising: hydrogenation reactor, heat exchanger, gas-liquid separator, carry hydrogen production device,
Regenerator, the quantity of described hydrogenation reactor is two, and this two hydrogenation reactors are used alternatingly, when one of them is used for being hydrogenated with
During reaction, another is used for the regeneration of catalyst；Wherein,
It is provided with catalyst layer, it includes reactant entrance and reactant outlet in described hydrogenation reactor；
The described hydrogen production device that carries includes gas access, hydrogen outlet and ethylene outlet；
Described regenerator includes material inlet, solvent outlet and green oil outlet；
Reactant outlet for the described hydrogenation reactor of hydrogenation reaction connects the entrance of described heat exchanger, described heat exchanger
Outlet connects the entrance of described gas-liquid separator；The gas carrying hydrogen production device described in gas outlet's connection of described gas-liquid separator enters
Mouthful, the liquid outlet of described gas-liquid separator connects the material inlet of described regenerator；
Reactant outlet for the described hydrogenation reactor of catalyst regeneration connects the entrance of described heat exchanger.
2. system according to claim 1 is it is characterised in that the solvent outlet of described regenerator connects described hydrogenation reaction
The reactant entrance of device.
3. system according to claim 1 is it is characterised in that the described hydrogen outlet carrying hydrogen production device connects described hydrogenation instead
Answer the reactant entrance of device.
4. system according to claim 1 is it is characterised in that the reactant entrance of described hydrogenation reactor is provided with atomization spray
Mouth.
5. system according to claim 1 is it is characterised in that the catalyst layer of described hydrogenation reactor is rotatable.
6. system according to claim 1 is stored up it is characterised in that being provided with solvent pump before described hydrogenation reactor with solution
Tank.
7. the method for system ethylene described in a kind of utilization any one of claim 1 to 6, methods described includes step:
Hydrogen, acetylene and liquid phase solvent are sent into and is used for the described hydrogenation reactor of hydrogenation reaction and is reacted；
Carry out separating by being re-fed into described gas-liquid separator after the reactant described heat exchanger of feeding after hydrogenation reaction, obtain gas
With liquid；
Carry hydrogen production device described in the described gas feeding that separation is obtained to carry out proposing hydrogen process, obtain ethylene product；
Carry out solvent reclamation by separating the described liquid described regenerator of feeding obtaining；
The hydrogenation reactor that reactant has been reacted and eliminated to liquid phase solvent feeding carries out catalyst regeneration；
After product after catalyst is regenerated sends into described heat exchanger heat exchange, enter gas-liquid separator separates, obtain separation molten
Liquid；
The described solution described regenerator of feeding that separates is carried out solvent reclamation, and obtains green oil product.
8. method according to claim 7 is it is characterised in that methods described further comprises the steps of:
The hydrogen proposing hydrogen process extraction is returned described hydrogenation reactor reacted；
The solvent that regeneration is obtained returns described hydrogenation reactor and is circulated utilization；
Solvent after regeneration is sent in the reactant after hydrogenation reaction and carries out heat exchange process, make described temperature of charge cooling.
9. method according to claim 7 it is characterised in that described solvent include n- N-methyl-2-2-pyrrolidone N (nmp),
One or more of pyridine, imidazoles, quinoline.
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| CN201610853243.9A CN106345374A (en) | 2016-09-26 | 2016-09-26 | Reaction system and method for producing ethylene from acetylene |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111013501A (en) * | 2019-10-25 | 2020-04-17 | 河北美邦工程科技股份有限公司 | Slurry bed continuous hydrogenation reaction device and method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111013501A (en) * | 2019-10-25 | 2020-04-17 | 河北美邦工程科技股份有限公司 | Slurry bed continuous hydrogenation reaction device and method |
| CN111013501B (en) * | 2019-10-25 | 2021-09-14 | 河北美邦工程科技股份有限公司 | Slurry bed continuous hydrogenation reaction device and method |
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