CN205774196U - A kind of response system of pressure-variable adsorption ethylene - Google Patents
A kind of response system of pressure-variable adsorption ethylene Download PDFInfo
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- CN205774196U CN205774196U CN201620557149.4U CN201620557149U CN205774196U CN 205774196 U CN205774196 U CN 205774196U CN 201620557149 U CN201620557149 U CN 201620557149U CN 205774196 U CN205774196 U CN 205774196U
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- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 239000005977 Ethylene Substances 0.000 title claims abstract description 39
- 238000001179 sorption measurement Methods 0.000 title claims abstract description 27
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- 239000002002 slurry Substances 0.000 claims abstract description 62
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- 239000007789 gas Substances 0.000 claims abstract description 40
- 239000003054 catalyst Substances 0.000 claims abstract description 38
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 29
- 230000008676 import Effects 0.000 claims abstract description 29
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- 238000011069 regeneration method Methods 0.000 claims abstract description 26
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- 238000000034 method Methods 0.000 description 19
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- 239000002245 particle Substances 0.000 description 10
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- HNJBEVLQSNELDL-UHFFFAOYSA-N pyrrolidin-2-one Chemical compound O=C1CCCN1 HNJBEVLQSNELDL-UHFFFAOYSA-N 0.000 description 9
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- 238000006243 chemical reaction Methods 0.000 description 7
- 239000003085 diluting agent Substances 0.000 description 7
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- 239000000470 constituent Substances 0.000 description 6
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- 238000005516 engineering process Methods 0.000 description 6
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- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 239000003463 adsorbent Substances 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 4
- 239000003208 petroleum Substances 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 238000009825 accumulation Methods 0.000 description 3
- 150000001336 alkenes Chemical class 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
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- 229910052814 silicon oxide Inorganic materials 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 239000008234 soft water Substances 0.000 description 2
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- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 1
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- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
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- CDQSJQSWAWPGKG-UHFFFAOYSA-N butane-1,1-diol Chemical compound CCCC(O)O CDQSJQSWAWPGKG-UHFFFAOYSA-N 0.000 description 1
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- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
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- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 229920002451 polyvinyl alcohol Polymers 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
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- 229910002027 silica gel Inorganic materials 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
This utility model relates to the response system of a kind of pressure-variable adsorption ethylene.Described system includes hydrogen alkynes mixing pressure unit, hydrogenation reaction unit, psa unit, vacuum filter element, high-temperature steam and fluidized bed regeneration unit and vacuum low-pressure distillation unit；Hydrogenation reaction unit includes slurry bed system, slurry bed system attemperating unit, gas-liquid condensation separating unit, the gas products import of gas-liquid condensation separating unit connects the gas products outlet of described slurry bed system, the condensate outlet of described gas-liquid condensation separating unit connects the lime set import of described slurry bed system, and the gas outlet of described gas-liquid condensation separating unit connects the gas feed of described psa unit；The liquid phase material outlet of described vacuum filter element connects described vacuum low-pressure distillation unit, and the solid-phase material outlet of described vacuum filter element connects described high-temperature steam and fluidized bed regeneration unit.It is big that this utility model has operating flexibility, the advantage adaptable to catalyst.
Description
Technical field
This utility model generally relates to the response system of a kind of ethylene processed, is specifically related to the anti-of a kind of pressure-variable adsorption ethylene
Answer system.
Background technology
Ethylene is a kind of primary raw material of petro chemical industry, and current process of preparing is mainly splitting by Petroleum
Solve alkene processed and olefin hydrocarbon making by coal.Within 2015, domestic ethylene aggregated capacity reaches about 22,000,000 t/a, and the year two thousand twenty domestic ethylene production capacity is entered
One step will be added to 32,500,000 t/a, and expecting the year two thousand twenty domestic ethylene consumption figure is 48,000,000 tons/year, then will appear from demand
Phenomenon more than production capacity.Serious strategy threat is constituted for this China that oil reserve is not enriched.Therefore, seek separately
A kind of new source and process, thus can be at field of industrial production petroleum replacings to prepare ethylene, it is possible to largely
Alleviate China's dependency for petroleum.
In coal chemical technology, pass through carbide technique or with natural gas for raw material by Non-catalytic partial oxygen with coal for raw material
Metallization processes produces acetylene, has been widely used.With acetylene as raw material, under selective hydrocatalyst effect, standby by Hydrogenation
Ethylene product, can expand Development of Coal Chemical Industry approach further.And the downstream product polrvinyl chloride (PVC) that acetylene is main in the last few years
Supply exceed demand, and PVC industrial profit is the highest, is badly in need of expanding acetylene downstream product industrial chain；And polyethylene price is with oil valency
Lattice wave is dynamic very big, and other downstream product such as ethylene glycol, and butanediol, acrylic acid, polyvinyl alcohol etc. also have good economic worth.
Therefore, the novel technique of exploitation producing ethylene with acetylene hydrogenation can be that ethylene industry provides a kind of new raw material source, and reduces second
The alkene degree of dependence to petroleum resources 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, but its research contents master
Concentrate on and remove cracking petroleum hydrocarbon and prepare the acetylene (0.01 5 volume %) of trace during ethylene process.Acetylene hydrogenation is
Strong exothermal reaction, high concentration acetylene hydrogenation is released a large amount of reaction heat, bed shifting heat difficulty, is easily caused catalysqt deactivation, side reaction
Increase, yield of ethene declines, so the method for the special catalysis selective hydrogenation ethylene with high concentration acetylene as raw material is few
Exploration, corresponding industrialization large-scale application is had to have no report especially.
Therefore, in order to avoid the fixed bed temperature runaway phenomenon of high purity acetylene Hydrogenation ethylene, reaction heat shifting heat in traditional method
Difficulty and bed pressure drop is big, slurry reactor pressure is low, production capacity is little problem and green oil gather, affect catalyst activity
Problem, it is necessary to propose the response system of a kind of new pressure-variable adsorption ethylene.
Utility model content
The purpose of this utility model is to provide the response system of a kind of pressure-variable adsorption ethylene, to solve in traditional method
The fixed bed temperature runaway phenomenon of high purity acetylene Hydrogenation ethylene, reaction heat move heat difficulty and bed pressure drop is big, slurry reactor pressure
Problem that low, production capacity is little and green oil accumulation, the problem affecting catalyst activity.
This utility model provides the response system of a kind of pressure-variable adsorption ethylene, and described system includes that the mixing of hydrogen alkynes is all pressed
Unit, hydrogenation reaction unit, psa unit, vacuum filter element, high-temperature steam and fluidized bed regeneration unit and vacuum are low
Pressure distillation unit；Described hydrogenation reaction unit includes slurry bed system, slurry bed system attemperating unit, gas-liquid condensation separating unit, wherein, institute
State slurry bed system and be provided with combi inlet port, gas products outlet, lime set import, serum outlet and heat transferring medium import, heat exchange Jie
Matter exports；Described combi inlet port connects described hydrogen alkynes mixing pressure unit；The described vacuum that connects described serum outlet filters single
Unit；Described slurry bed system attemperating unit is exported by described heat transferring medium, heat transferring medium import connects with described slurry bed system；Described gas
The gas products import of liquid condensing separating device connects the gas products outlet of described slurry bed system, described gas-liquid condensation separating unit
Condensate outlet connect the lime set import of described slurry bed system, the gas outlet of described gas-liquid condensation separating unit connects described transformation
The gas feed of absorbing unit；The liquid phase material outlet of described vacuum filter element connects described vacuum low-pressure distillation unit, institute
The solid-phase material outlet stating vacuum filter element connects described high-temperature steam and fluidized bed regeneration unit.
Above-mentioned system, described hydrogen alkynes mixing pressure unit is venturi mixer.
Above-mentioned system, the hydrogen inlet of the hydrogen outlet of described psa unit and described hydrogen alkynes mixing pressure unit
It is connected.
Above-mentioned system, described slurry bed system attemperating unit includes electric heater, condenser and automatic temperature control system.
Above-mentioned system, the solvent outlet of described vacuum low-pressure distillation unit connects the colvent inlet of described slurry bed system；Institute
State high-temperature steam and fluidized bed regeneration unit includes the most connected high-temperature steam washing device and fluid bed, described fluid bed
Discharging opening is connected with the catalyst inlet of described slurry bed system.
The method and system of pressure-variable adsorption ethylene that this utility model provides, it is to avoid high purity acetylene Hydrogenation ethylene is consolidated
Fixed bed temperature runaway, reaction heat move the problem that heat is difficult and bed pressure drop is big, slurry reactor pressure is low, production capacity is little, and this reality
There is operating flexibility greatly with novel, the advantage adaptable to catalyst.
This utility model uses venturi mixer to realize the mixing of high pressure hydrogen and low pressure acetylene, it is to avoid mixed pressure
The use of contracting machine, and then reduce the potential safety hazard of compression acetylene, reduce the investment of equipment simultaneously.
This utility model uses pressure swing adsorption, and cycle period is short, it is easy to accomplish automatization, separates maximization gas
Production process is especially suitable.
This utility model uses continuous vacuum to filter and low-pressure distillation technology, it is to avoid green oil accumulation, affect catalyst work
The defect of property, and achieve solvent reclamation.
This utility model uses high-temperature steam and fluidized bed regeneration catalyst technology, it is achieved that catalyst on-line regeneration, fall
The low technique requirement to catalyst life so that in slurry bed system, catalyst activity is high, in stable condition.
Accompanying drawing explanation
Fig. 1 is the system schematic of the pressure-variable adsorption ethylene of a kind of embodiment of this utility model；
Fig. 2 is the workflow diagram of the pressure-variable adsorption ethylene of a kind of embodiment of this utility model.
In figure: 1-slurry bed system；2-condenser；3-gas-liquid condensation separating unit；4-psa unit；The mixing of 5-hydrogen alkynes is all
Pressure unit；6-fluid bed；7-vacuum filter element；8-vacuum low-pressure distillation unit；9-slurry bed system attemperating unit；10-gas produces
Product export；11-lime set import；12-heat transferring medium import；13-heat transferring medium exports；14-slurry inlet；15-serum outlet；
16-combi inlet port；17-heavy constituent exports；18-ethylene exports；19-high-temperature steam washing device；20-high-temperature steam entrance；
21-high-temperature steam outlet.
Detailed description of the invention
Below in conjunction with drawings and Examples, detailed description of the invention of the present utility model is described in more details, with
Just the advantage that better understood when scheme of the present utility model and its various aspects.But, specific implementations described below
Mode and embodiment are only descriptive purposes rather than to restriction of the present utility model.
As it is shown in figure 1, the system of a kind of pressure-variable adsorption ethylene, including hydrogen alkynes mixing pressure unit, hydrogenation reaction unit,
Psa unit, vacuum filter element, high-temperature steam and fluidized bed regeneration unit and hypergravity rectification cell.Wherein, high temperature
Steam and fluidized bed regeneration unit include high-temperature steam washing device and the fluid bed being sequentially connected.
Hydrogen alkynes mixing pressure unit can use venturi mixer to replace gaseous mixture compressor, reduces the peace of compression acetylene
Full hidden danger, reduces the investment of equipment simultaneously.When venturi mixer is for application static mixer, two strands or more than two strands
Fluid, before entering static mixer, designs for each fluid streams smooth delivery of power.Fluid in course of conveying, often due to
Each fluid streams discharge pressure imbalance affects mixing ratio, selects venturi shaped allotter, venturi shaped to distribute in this case
Utensil has injection boosting pump performance, under conditions of ensureing time stream flow, makes the outlet pressure of material reach required pressure
Power.
Described hydrogenation reaction unit includes slurry bed system, slurry bed system attemperating unit, gas-liquid condensation separating unit, described slurry bed system
Being provided with combi inlet port, gas products outlet, lime set import, serum outlet and heat transferring medium to import and export, described gaseous mixture enters
Mouth connects hydrogen alkynes mixing pressure unit mixed gas outlet, and described serum outlet connects vacuum filter element, described slurry bed system temperature control
Device is provided with heat transferring medium and imports and exports, and is connected with slurry bed system heat transferring medium exit port respectively.Described gas-liquid condensation separating unit sets
Having gas products import, condensate outlet and gas outlet, condensate outlet connects slurry bed system lime set import, and described gas outlet is even
Connect psa unit gas feed.
The principle of psa unit is the characteristic that the equilibrium adsorption capacity utilizing adsorbent increases with partial component pressure rising,
Carry out pressurized adsorbent, decompression desorption.Pressure-variable adsorption is usually normal-temperature operation, is not necessary to heat supply, therefore cycle period is short, it is easy to accomplish from
Dynamicization, especially suitable to maximization gas separation production process.The adsorbent primarily now used has pressure-variable adsorption silica gel, activity
Aluminium oxide, efficient Cu system adsorbent (PU-1), lithio oxygen absorbent (PU-8) etc..
Further, described slurry bed system attemperating unit can include conduction oil attemperating unit, high pressure soft water attemperating unit, steam
Attemperating unit and flue gas attemperating unit.
Described vacuum filter element includes continuous vacuum defecator, is provided with slurry inlet, liquid phase material and solid-phase material
Outlet, the outlet of described liquid phase material connects vacuum low-pressure distillation unit, and solid-phase material outlet is steamed with high temperature through belt conveyer
The charging aperture of vapour and fluidized bed regeneration unit connects.
Further, described vacuum low-pressure distilling apparatus includes low-pressure distillation column, is provided with liquid phase material import, solvent outlet
And heavy constituent outlet.
Further, described vacuum apparatus can include rotary drum vacuum filter, belt vacuum filter or tipping bucket
Formula vacuum filter.
This utility model uses continuous vacuum to filter and low-pressure distillation technology, it is to avoid green oil accumulation, affect catalyst work
The defect of property, and achieve solvent reclamation.
Further, the high-temperature steam washing device of described high-temperature steam and fluidized bed regeneration unit is provided with high-temperature steam and enters
Mouth, high-temperature steam outlet and feed inlet and outlet, the charging aperture of high-temperature steam washing device is connected with the discharging opening of vacuum filter element,
Its discharging opening is connected with the charging aperture of fluid bed.Vapor (steam) temperature in high-temperature steam and fluidized bed regeneration unit is 150 DEG C-230
℃.Described fluid bed is provided with feed inlet and outlet and gas inlet and outlet.Arranging high-temperature steam washing device before fluid bed is to use
High-temperature steam eluting catalyst surface attachment.Further, the steam (vapor) outlet of described high-temperature steam washing device is soft with high pressure
Water attemperating unit steam inlet or steam attemperating unit steam inlet are connected, and are used for reclaiming high-temperature steam heat.
This utility model uses high-temperature steam and fluidized bed regeneration regeneration unit catalyst technology, it is achieved that catalyst is online
Regeneration, reduces the technique requirement to catalyst life so that in slurry bed system, catalyst activity is high, in stable condition.
The method of pressure-variable adsorption ethylene of the present utility model, comprises the steps:
1) mixing of hydrogen alkynes is all pressed
Low pressure acetylene and high pressure hydrogen are mixed by venturi mixer, realize hydrogen alkynes simultaneously and all press.
2) hydrogenation reaction
By step 1) gained gaseous mixture is passed through the slurry bed system in hydrogenation reaction operation, carries out acetylene selective hydrogenation reaction.
3) pressure-variable adsorption
The gas-phase product of acetylene hydrogenation reaction being carried out pressure-variable adsorption, obtains product ethylene, hydrogen more than needed is sent into hydrogen alkynes and is mixed
Close pressure process.
4) vacuum filters
Serosity in slurry bed system is drawn continuously, by vacuum filter isolated solid-phase material and liquid phase material.
5) high-temperature steam and fluidized bed regeneration
Described solid-phase material is first through high-temperature steam eluting, then through fluidized bed processing, obtains regenerated catalyst.
6) vacuum low-pressure distillation
Described liquid phase material is distilled by vacuum low-pressure, recycling design.
Wherein, low pressure acetylene pressure is 5KPa-40KPa, and temperature is 5-80 DEG C.Described high pressure hydrogen pressure is
0.1MPa-2.2MPa MPa, temperature is 5-40 DEG C.Acetylene is 1:3-15 with the mol ratio of hydrogen.
Wherein, described solid-phase material includes catalyst and catalyst diluent.
Wherein, catalyst diluent includes that perlite particle, alumina particle, silicon oxide particle, molecular sieve (are crystalline states
Silicate or aluminosilicate, silicon-oxy tetrahedron or aluminum-oxygen tetrahedron be connected by oxygen bridged bond and formed.) and ceramic particle in
One or more；Catalyst diluent particle diameter is the 80%-120% of catalyst mean diameter；Catalyst diluent and catalysis
The mass ratio of agent is 0.1-10:1.
Wherein, the atmosphere of the fluid bed of high-temperature steam and fluidized bed regeneration unit is hydrogen and nitrogen, and its mol ratio is 1:
3-9, the temperature in described fluid bed is 150-350 DEG C；Vapor (steam) temperature in described high-temperature steam and fluidized bed regeneration unit is
150℃-230℃。
The system of pressure-variable adsorption ethylene that this utility model provides, it is to avoid high purity acetylene Hydrogenation second in traditional method
Alkene fixed bed temperature runaway, reaction heat move the problem that heat is difficult and bed pressure drop is big, slurry reactor pressure is low, production capacity is little, and
It is big that this utility model has operating flexibility, the advantage adaptable to catalyst.
Now with following most preferred embodiment, this utility model is described.Technique numerical value in following example is exemplary saying
Bright, concrete scope is as the criterion with the value in description.
Embodiment 1
As in figure 2 it is shown, the system of a kind of high-purity pressure-variable adsorption ethylene, it is characterised in that this system includes that hydrogen alkynes mixes
Pressure unit 5, hydrogenation reaction unit, psa unit 4, vacuum filter element 7, high-temperature steam and fluidized bed regeneration unit and
Hypergravity rectification cell 8.Wherein high-temperature steam and fluidized bed regeneration unit include again fluid bed 6 and high-temperature steam washing device
19.High-temperature steam washing device 19 is provided with high-temperature steam entrance 20 and high-temperature steam outlet 21, and high-temperature steam entrance 20 is for defeated
Enter high-temperature steam, high-temperature steam outlet 21 and high pressure soft water attemperating unit steam inlet or steam attemperating unit steam inlet phase
Even.
Described hydrogenation reaction unit includes slurry bed system 1, slurry bed system attemperating unit 9, gas-liquid condensation separating unit 3, described slurry
State bed is provided with combi inlet port 16, gas products outlet 10, lime set import 11, serum outlet 15 and heat transferring medium import and export
12,13, described combi inlet port 16 connects hydrogen alkynes mixing pressure unit mixed gas outlet, and described serum outlet 15 connects vacuum mistake
Filter unit 7, described attemperating unit 9 is provided with heat transferring medium import and export, go out with slurry bed system heat transferring medium respectively, import 13,12 even
Connecing, described gas-liquid condensation separating unit 3 is provided with gas products import, condensate outlet and gas outlet, and condensate outlet connects slurry
State bed 1 lime set import, described gas outlet connects psa unit 4 gas feed.Psa unit 4 is provided with ethylene and goes out
Mouth 18.
Described vacuum filter element 7 includes continuous vacuum defecator, is provided with slurry inlet 14, liquid phase material and solid formation
Material outlet, the outlet of described liquid phase material connects vacuum low-pressure distillation unit, and solid-phase material exports through belt conveyer and rotation
Bed charging aperture connects.
Described high-temperature steam and fluidized bed regeneration unit, be provided with feed inlet and outlet and gas inlet and outlet.Wherein high-temperature steam is washed
The charging aperture that off loading is put exports with the solid-phase material of vacuum filter element 7 and is connected.The gas feed of fluid bed is used for inputting atmosphere
Hydrogen and nitrogen.The discharging opening of fluid bed is for being connected with the catalyst inlet of hydrogenation reaction unit.The gas outlet of fluid bed
For the atmosphere recirculation of output being exported the atmosphere entrance of self.
Described vacuum low-pressure distillation unit includes low-pressure distillation column, is provided with liquid phase material import, solvent outlet and heavy constituent
Outlet 17.Liquid phase material import is for connecting the liquid phase material outlet of vacuum filter element 7.Solvent outlet can be with hydrogenation reaction list
The lime set import of unit connects, and can realize recycling of solvent.Heavy constituent outlet 17 is used for exporting side-product green oil.The present embodiment
In, slurry bed system attemperating unit 9 is heat-conducting oil system, is provided with electric heater, condenser 2 and automatic temperature control system.
Embodiment 2
Using the system of embodiment 1, the technique of pressure-variable adsorption ethylene is:
By catalyst diluent aluminium oxide that particle diameter is 50 mesh-80 mesh and acetylene hydrogenation catalyst according to the mass ratio of 2:1
After example mix homogeneously forms solid-phase material, add slurry bed system inside and be mixed to form serosity with solvent N-first class ketopyrrolidine.Will
20KPa, the acetylene of 40 DEG C are mixed by venturi mixer by the mol ratio of 1:6 with the hydrogen of 0.1MPa, 5 DEG C, form mixing
Gas.Gaseous mixture enters serosity by slurry bed system internal gas distributor, reacts under the conditions of 130 DEG C.Reacted gaseous phase materials
Obtaining target product ethylene through pressure-variable adsorption, the hydrogen of recovery mixes with raw hydrogen.Liquid phase material is through rotating drum vacuum filtration
Machine obtains solid-phase material and liquid phase material.Solid-phase material is first through 150 DEG C of eluting of high-temperature steam, then delivers to fluid bed through belt, stream
Changing bed atmosphere is hydrogen and nitrogen, and its mol ratio is 1:3, and solid-phase material obtains the catalyst of regeneration, catalyst through 150 DEG C of reduction
Return slurry bed system is continuing with.Liquid phase material pumps into vacuum low-pressure distillation column, pressure 5KPa (A), and collecting boiling range is 130 DEG C-150
DEG C fraction (N-first class ketopyrrolidine), the N-first class ketopyrrolidine of recovery returns slurry bed system, and heavy constituent is green oil.
Embodiment 3
Using the system of embodiment 1, the technique of pressure-variable adsorption ethylene is:
By catalyst diluent perlite particle that particle diameter is 100 mesh-150 mesh with acetylene hydrogenation catalyst according to 10:1's
After ratio mix homogeneously forms solid-phase material, add slurry bed system inside and be mixed to form serosity with solvent N-first class ketopyrrolidine.Will
40KPa, the acetylene of 80 DEG C are mixed by venturi mixer by the mol ratio of 1:15 with the hydrogen of 2.2MPa, 10 DEG C, are formed mixed
Close gas.Gaseous mixture enters serosity by slurry bed system internal gas distributor, reacts under the conditions of 170 DEG C.Reacted gas gas-phase objects
Material obtains target product ethylene through pressure-variable adsorption, and the hydrogen of recovery mixes with raw hydrogen.Liquid phase material is through belt vacuum mistake
Filter obtains solid-phase material and liquid phase material.Solid-phase material is first through 230 DEG C of eluting of high-temperature steam, then delivers to fluid bed through belt,
Fluid bed atmosphere is hydrogen and nitrogen, and its mol ratio is 1:6, obtains the catalyst of regeneration through 350 DEG C of reduction, and catalyst returns slurry
State bed is continuing with.Liquid phase material pumps into vacuum low-pressure distillation column, pressure 5KPa (A), and collecting boiling range is 130 DEG C-150 DEG C evaporate
Dividing (N-first class ketopyrrolidine), the N-first class ketopyrrolidine of recovery returns slurry bed system, and heavy constituent is green oil.
Embodiment 4
Using the system of embodiment 1, the technique of pressure-variable adsorption ethylene is:
It is the catalyst diluent silicon oxide particle of 100 mesh-150 mesh, molecular sieve and ceramic mixture and second by particle diameter
After alkynes hydrogenation catalyst forms solid-phase material according to the ratio mix homogeneously of 0.1:1, add slurry bed system inside and solvent N-first class
Ketopyrrolidine is mixed to form serosity.The acetylene of 5KPa, 5 DEG C is pressed the mol ratio of 1:3 by literary composition mound with 1.1MPa, the hydrogen of 40 DEG C
In blender mixing, formed gaseous mixture.Gaseous mixture enters serosity by slurry bed system internal gas distributor, under the conditions of 170 DEG C
Reaction.Reacted gaseous phase materials obtains target product ethylene through pressure-variable adsorption, and the hydrogen of recovery mixes with raw hydrogen.Liquid
Phase materials obtains solid-phase material and liquid phase material through belt vacuum filter.Solid-phase material is first through 190 DEG C of eluting of high-temperature steam, Gu
Phase materials delivers to fluid bed through belt, and fluid bed atmosphere is hydrogen and nitrogen, and its mol ratio is 1:9, obtains through 250 DEG C of reduction again
Raw catalyst, catalyst returns slurry bed system and is continuing with.Liquid phase material pumps into vacuum low-pressure distillation column, pressure 5KPa (A), receives
Collection boiling range is the fraction (N-first class ketopyrrolidine) of 130 DEG C-150 DEG C, and the N-first class ketopyrrolidine of recovery returns slurry bed system, restructuring
Divide and be green oil.
It is last that it is noted that obviously above-described embodiment is only for clearly demonstrating this utility model example,
And not restriction to embodiment.For those of ordinary skill in the field, the most also may be used
To make other changes in different forms.Here without also cannot all of embodiment be given exhaustive.And thus
That is amplified out obviously changes or changes among still in protection domain of the present utility model.
Claims (5)
1. a response system for pressure-variable adsorption ethylene, described system include hydrogen alkynes mixing pressure unit, hydrogenation reaction unit,
Psa unit, vacuum filter element, high-temperature steam and fluidized bed regeneration unit and vacuum low-pressure distillation unit；
Described hydrogenation reaction unit includes slurry bed system, slurry bed system attemperating unit, gas-liquid condensation separating unit, wherein, described slurry
Bed is provided with combi inlet port, gas products outlet, lime set import, serum outlet and heat transferring medium import, heat transferring medium goes out
Mouthful；Described combi inlet port connects described hydrogen alkynes mixing pressure unit；Described serum outlet connects described vacuum filter element；
Described slurry bed system attemperating unit is exported by described heat transferring medium, heat transferring medium import connects with described slurry bed system；
The gas products import of described gas-liquid condensation separating unit connects the gas products outlet of described slurry bed system, and described gas-liquid is cold
The condensate outlet of solidifying segregation apparatus connects the lime set import of described slurry bed system, and the gas outlet of described gas-liquid condensation separating unit is even
Connect the gas feed of described psa unit；
The liquid phase material outlet of described vacuum filter element connects described vacuum low-pressure distillation unit, described vacuum filter element
Solid-phase material outlet connects described high-temperature steam and fluidized bed regeneration unit.
System the most according to claim 1, it is characterised in that described hydrogen alkynes mixing pressure unit is venturi mixer.
System the most according to claim 1, it is characterised in that the hydrogen outlet of described psa unit and described hydrogen alkynes
The hydrogen inlet of mixing pressure unit is connected.
System the most according to claim 1, it is characterised in that described slurry bed system attemperating unit includes electric heater, condensation
Device and automatic temperature control system.
System the most according to claim 1, it is characterised in that the solvent outlet of described vacuum low-pressure distillation unit connects institute
State the colvent inlet of slurry bed system；Described high-temperature steam and fluidized bed regeneration unit include the high-temperature steam washing device that order is connected
And fluid bed, the discharging opening of described fluid bed is connected with the catalyst inlet of described slurry bed system.
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