CN205443125U - Device of high concentration acetylene hydrogenation system ethylene - Google Patents
Device of high concentration acetylene hydrogenation system ethylene Download PDFInfo
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- CN205443125U CN205443125U CN201521127361.9U CN201521127361U CN205443125U CN 205443125 U CN205443125 U CN 205443125U CN 201521127361 U CN201521127361 U CN 201521127361U CN 205443125 U CN205443125 U CN 205443125U
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Abstract
The utility model provides a device of high concentration acetylene hydrogenation system ethylene. The utility model discloses device of high concentration acetylene hydrogenation system ethylene includes acetylene hydrogenation reactor, solvent absorption tower and ethylene concentration unit. The utility model discloses device of high concentration acetylene hydrogenation system ethylene simple structure, acetylene feeding pipe pass through acetylene solvent jar and link to each other with the acetylene hydrogenation reactor, dissolve acetylene to let in the acetylene hydrogenation reactor again in the solvent, through the liquid phase pressurization, overcome the restriction of acetylene pressure, can make acetylene hydrogenation operate with the upward pressure at 1.5MPaG, the acetylene hydrogenation reactor links to each other with the solvent absorption tower, and acetylene hydrogenation reaction back gained gaseous phase is passed through the solvent and is absorbed, has avoided multitower rectification separation in the traditional handicraft, and the energy consumption is low. The utility model discloses find the outlet not only for the surplus carbide productivity of china, has greatly alleviated china's ethylene demand moreover, to promote the green sustainable development of china's acetylene chemical industry, energy saving and emission reduction has important meaning.
Description
Technical field
This utility model relates to technical field of petrochemical industry, in particular to the device of a kind of high concentration producing ethylene with acetylene hydrogenation.
Background technology
Ethylene is a kind of important basic material in modern industry, is also one of maximum chemicals of world wide production.Ethylene yield has become the mark weighing a national oil development of chemical industry level, and its production capacity is counted as the embodiment of a national economic strength.
Ethylene is mainly prepared by the method for cracking petroleum hydrocarbon, and oil is a kind of non-renewable resources in short supply, and its price is with impact fluctuations such as international environment changes the most greatly.Current China annual petroleum consumption ranking the second in the world, within 2011, dependence on foreign countries for oil has reached 56.5%, defines serious strategy threat for this China not enriched oil reserve.Therefore, find another kind of new source and process prepares large basic organic chemical raw material ethylene, at field of industrial production petroleum replacing as raw material, it is possible to largely alleviate China's dependency for oil.
The most not yet carry out the direct technique for producing ethylene of acetylene to explore.The low concentration acetylene gas solid catalysis hydrogen addition technology being widely used at present and high purity acetylene ethylene have the biggest difference.
Low concentration acetylene gas solid catalysis hydrogen addition technology is the most highly developed, is mainly used in ethylene removing acetylene impurities.The existence of acetylene, can reduce the activity of ethylene rolymerization catalyst, makes polymerization be deteriorated, and therefore should control acetylene content at below 1ppm.For the production of the course of processing of some particular/special requirement, such as low-pressure polyethylene, in essence ethylene, acetylene content requires less than 0.1ppm.Industry removes a small amount of (about 1%) acetylene in ethylene and uses fixed-bed process, with Pd or Ni as catalyst, react under the conditions of 30～100 DEG C.But owing to ethyne reactive high hydrogenation reaction heat effect is big, even there is a small amount of acetylene in cracking gas, traditional fixed bed hydrogenation reactor still suffers from the serious problems such as green oil generating amount is big, catalyst cycle period is short, reactor easily " temperature runaway ".Therefore, when removing acetylene in petroleum industry, while generally using millisecond pyrolysis furnace, original one-stage hydrogenation technique changing three series connection, the multi-stek hydrogenation technique of intersegmental cooling into, reaction process is complex.
In view of this, special proposition this utility model.
Utility model content
First purpose of the present utility model is to provide the device of a kind of high concentration producing ethylene with acetylene hydrogenation, the device of described high concentration producing ethylene with acetylene hydrogenation has simple in construction, pressurizeed by liquid phase, acetylene pressure is overcome to limit, acetylene hydrogenation can be made to operate in 1.5MPaG pressure above, low power consumption and other advantages.
Second purpose of the present utility model is to provide a kind of method carrying out producing ethylene with acetylene hydrogenation of device using above-mentioned high concentration producing ethylene with acetylene hydrogenation, the method technique is simple, overcome acetylene pressure to limit, acetylene hydrogenation can be made to operate in 1.5MPaG pressure above；Meanwhile, after hydrogenation reaction, tail gas passes through solvent absorption, it is to avoid in traditional handicraft, multitower rectification separates, and reduces energy consumption, and technique is advanced.
In order to realize above-mentioned purpose of the present utility model, spy by the following technical solutions:
The device of a kind of high concentration producing ethylene with acetylene hydrogenation, the device of described high concentration producing ethylene with acetylene hydrogenation includes acetylene hydrogenation reactor, solvent absorption tower and ethylene concentration unit；Wherein, acetylene hydrogenation reactor, solvent absorption tower and ethylene concentration unit are sequentially connected；Described acetylene hydrogenation reactor is connected with acetylene feeding pipe and hydrogen feed tube road respectively；On described acetylene feeding pipe, solvents for ethyne tank is set；Described ethylene concentration unit is connected with ethylene discharging pipeline.
The apparatus structure of this utility model high concentration producing ethylene with acetylene hydrogenation is simple, acetylene feeding pipe is connected with acetylene hydrogenation reactor by solvents for ethyne tank, acetylene is dissolved and is passed through acetylene hydrogenation reactor the most again, pressurizeed by liquid phase, overcome acetylene pressure to limit, acetylene hydrogenation can be made to operate in 1.5MPaG pressure above；Acetylene hydrogenation reactor is connected with solvent absorption tower, and after acetylene hydrogenation reaction, gained gas phase passes through solvent absorption, it is to avoid in traditional handicraft, multitower rectification separates, and energy consumption is low.
Described acetylene feeding pipe is connected with bottom acetylene hydrogenation reactor by venturi-type eductors the most respectively with hydrogen feed tube road.Solvent and hydrogen dissolved with acetylene preferably mix in venturi-type eductors.
It is preferably provided with heat exchanger on acetylene feeding pipe between described solvents for ethyne tank and acetylene hydrogenation reactor.
Described acetylene hydrogenation reactor preferably employs paste state bed reactor, built-in solvent.
Preferably it is connected with catalyst filtration device bottom described acetylene hydrogenation reactor, in order to reclaim dead catalyst.Described catalyst filtration device preferably employs one or more of plate and frame type filter-press, chamber-type press filter, pressure leaf filter, Rotary Filter Press or belt filter press.
Described solvent absorption tower bottom preferably sequentially passes through pump and is connected with solvent absorption top of tower with heat exchanger.
Described solvent absorption tower is connected with solvent refining tower；Described solvent refining tower is connected with acetylene hydrogenation reactor, and the solvent recovery after refining uses.
Described solvent refining top of tower is connected with light component discharging pipeline；Described solvent refining tower bottom is connected with heavy constituent discharging pipeline.
Described solvent refining top of tower sequentially passes through heat exchanger and is connected with light component discharging pipeline with return tank.
Described solvent refining tower bottom is preferably connected with heat exchanger, constitutes closed circuit.
Each pipeline as required, is preferably respectively provided with the valve of correspondence, in order to control the opening and closing of each pipeline；Each pipeline is connected in parallel with one or more in corresponding piezometer, effusion meter, controller the most respectively, in order to monitor each pipeline actual condition.
The method using the device of above-mentioned a kind of high concentration producing ethylene with acetylene hydrogenation to carry out producing ethylene with acetylene hydrogenation, comprises the steps:
Raw material acetylene mixes with solvent, and the solvent having dissolved acetylene enters acetylene hydrogenation reactor；Hydrogen is directly entered acetylene hydrogenation reactor；Both generate ethylene at reaction in acetylene hydrogenation reactor；Reaction gained gas phase is after solvent absorption, and in gas phase, ethylene and hydrogen are isolated to product ethylene.
The method technique of this utility model producing ethylene with acetylene hydrogenation is simple, and raw material acetylene uses the mode that solvent dissolves, it is possible to overcome acetylene pressure to limit, and acetylene hydrogenation can be made to operate in 1.5MPaG pressure above；Meanwhile, after hydrogenation reaction, tail gas passes through solvent absorption, it is to avoid in traditional handicraft, multitower rectification separates, and reduces energy consumption, and technique is advanced.
The method of described a kind of producing ethylene with acetylene hydrogenation, comprises the steps:
(1) acetylene hydrogenation:
Acetylene enters solvents for ethyne tank, mixes with solvents for ethyne tank internal solvent and is dissolved completely in solvent, and solvent carries acetylene and sends into acetylene hydrogenation reactor after pump boosts after heat exchanger heats；Hydrogen mixes with acetylene at reactor inlet together sends into hydrogenation reactor；Unstrpped gas is passed through bottom acetylene hydrogenation reactor, by the bubbling of gas so that catalyst suspends with slurry form in a solvent, reacts；Preferably remove heat of reaction by built-in heat exchanger；After reaction, gained gas phase sends into solvent absorption tower；
Dominant response equation is as follows:
C2H2+H2→C2H4(1)
C2H2+2H2→C2H6(2)
2C2H2+2H2→C4H8(3)
(2) solvent absorption:
After acetylene hydrogenation reaction, gained gas phase enters bottom solvent absorption tower, and solvent enters heat exchanger after solvent pump boosts, and the solvent after heat exchanger cools down enters top, absorption tower；Solvent react with acetylene hydrogenation after gained gas phase counter current contacting, absorb the byproduct of reaction in gas phase；
(3) ethylene concentration:
From top, solvent absorption tower gas phase out after ethylene concentration unit ethylene concentration is refined, obtain product ethylene；Hydrogen (may contain trace by-product) returns acetylene hydrogenation reactor and recycles；
(4) solvent refining:
The by-product that acetylene hydrogenation produces, delivers to solvent refining tower through solvent absorption tower bottom；Solvent refining tower carries out rectification cutting to solvent；According to the difference with solvent boiling point, it is referred to as light component and heavy constituent；Light component, the heavy constituent impurity contained in solvent is removed by rectification cutting；Solvent after solvent refining tower lateral line withdrawal function is refined, is pumped to acetylene hydrogenation reactor recycling；
(5) catalyst reclaims:
Through longtime running, acetylene hydrogenation catalyst inactivates；Inactivation rear catalyst delivers to catalyst filtration device after stopping, and reclaims dead catalyst.
It is 0.02～0.2MPaG that acetylene enters the pressure of acetylene cylinder, preferably 0.02-0.15MPaG, and temperature is-20～40 DEG C, is preferably-10 DEG C.
Solvent and acetylene flow-rate ratio are 2～20:1 (mass ratioes), preferably 5～10:1.
Acetylene solution mixes with hydrogen through venturi mixer, and hydrogen and acetylene flow-rate ratio are 2～10:1 (mol ratios), preferably 4～6:1.
Hydrogen feeding temperature is 20～200 DEG C, preferably 40 DEG C, and feed pressure is 0.2～2.0MPaG, preferably 0.45～1.5MPaG.
Described solvent is one or more in N-Methyl pyrrolidone, dimethylformamide, dimethyl sulfoxide, monomethyl amine and acetone.
Used catalyst be palladium be main active component, silver and ruthenium be auxiliary agent, aluminium sesquioxide be the catalyst of carrier.Reaction pressure is 0.1～3.0MPaG, preferably 0.45～1.5MPaG, more preferably 0.8MPaG, and reaction temperature is 120～250 DEG C, preferably 150 DEG C.
Described solvent absorption tower operation temperature is-40 DEG C～60 DEG C, is preferably-5～40 DEG C, and operation pressure is 0.2～1.0MPaG, preferably 0.2～0.8MPaG.
Described solvent preferably employs fresh solvent, sealing and circulating.The cold medium that heat exchanger uses is preferably one or more in recirculated water, chilled water, liquefied ammonia, propylene.
Used ethylene concentrating method is preferably one or both that membrance separation separates with PSA.
Solvent refining tower is preferably rectifying column, and operation temperature is-60 DEG C～150 DEG C, is preferably-20～30 DEG C, more preferably 20 DEG C, and operation pressure is-0.2MPaA～1.5MPaG, preferably 0.5～1.5MPaG, more preferably 1.0PaG.
Described catalyst filtration device preferably employs continuous operation or intermittently operated, and operation pressure is-0.2MPaA～1.5MPaG, preferably 0.5MPaA, and operation pressure reduction is 0.02MPa～0.6MPa, preferably 0.2MPaA, and operation temperature is 20～150 DEG C, preferably 50 DEG C.
Compared with prior art, the beneficial effects of the utility model are:
The apparatus structure of this utility model high concentration producing ethylene with acetylene hydrogenation is simple, acetylene feeding pipe is connected with acetylene hydrogenation reactor by solvents for ethyne tank, acetylene is dissolved and is passed through acetylene hydrogenation reactor the most again, pressurizeed by liquid phase, overcome acetylene pressure to limit, acetylene hydrogenation can be made to operate in 1.5MPaG pressure above；Acetylene hydrogenation reactor is connected with solvent absorption tower, and after acetylene hydrogenation reaction, gained gas phase passes through solvent absorption, it is to avoid in traditional handicraft, multitower rectification separates, and energy consumption is low.The method technique of this utility model producing ethylene with acetylene hydrogenation is simple, and raw material acetylene uses the mode that solvent dissolves, and uses acetylene liquid phase pressurized delivered, safer compared with tradition acetylene in gas phase pressurization；Acetylene pressure is high pressure acetylene higher than 0.15MPaG, and risk of explosion easily occurs, and therefore traditional handicraft seldom has acetylene high pressure operating mode；The method of this utility model producing ethylene with acetylene hydrogenation can overcome acetylene pressure to limit, and acetylene hydrogenation can be made to operate in 1.5MPaG pressure above；Meanwhile, after hydrogenation reaction, tail gas passes through solvent absorption, it is to avoid in traditional handicraft, multitower rectification separates, and reduces energy consumption, and technique is advanced.The carbide production capacity that this utility model not only gives China superfluous finds a way out, and greatly alleviates China's ethylene requirements, has great importance to promoting China's acetylene chemical industry Green Sustainable, energy-saving and emission-reduction.
Accompanying drawing explanation
In order to be illustrated more clearly that this utility model detailed description of the invention or technical scheme of the prior art, the accompanying drawing used required in detailed description of the invention or description of the prior art will be briefly described below, apparently, accompanying drawing in describing below is embodiments more of the present utility model, for those of ordinary skill in the art, on the premise of not paying creative work, it is also possible to obtain other accompanying drawing according to these accompanying drawings.
Fig. 1 is the apparatus structure schematic diagram of this utility model high concentration producing ethylene with acetylene hydrogenation；
Reference:
1-acetylene hydrogenation reactor；2-solvent absorption tower；3-solvent refining tower；
4-ethylene concentration unit；5-acetylene cylinder；6-return tank；
7-catalyst filtration device；8-heat exchanger；9-pump；
10-venturi-type eductors；LC, FC, TC-controller.
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, the technical solution of the utility model is clearly and completely described, but it will be understood to those of skill in the art that, following described embodiment is a part of embodiment of this utility model, rather than whole embodiments, it is merely to illustrate this utility model, and is not construed as limiting scope of the present utility model.Based on the embodiment in this utility model, the every other embodiment that those of ordinary skill in the art are obtained under not making creative work premise, broadly fall into the scope of this utility model protection.Unreceipted actual conditions person in embodiment, the condition advised according to normal condition or manufacturer is carried out.Agents useful for same or instrument unreceipted production firm person, being can be by the commercially available conventional products bought and obtain.
In description of the present utility model, it should be noted that, orientation or the position relationship of the instruction such as term " " center ", " on ", D score, "left", "right", " vertically ", " level ", " interior ", " outward " they be based on orientation shown in the drawings or position relationship; be for only for ease of description this utility model and simplifying and describe; rather than instruction or imply the device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore it is not intended that to restriction of the present utility model.Additionally, term " first ", " second ", " the 3rd " are only used for describing purpose, and it is not intended that instruction or hint relative importance.
In description of the present utility model, it should be noted that unless otherwise clearly defined and limited, term " is installed ", " being connected ", " connection " should be interpreted broadly, and connects for example, it may be fixing, it is also possible to be to removably connect, or be integrally connected；Can be to be mechanically connected, it is also possible to be electrical connection；Can be to be joined directly together, it is also possible to be indirectly connected to by intermediary, can be the connection of two element internals.For the ordinary skill in the art, above-mentioned term concrete meaning in this utility model can be understood with concrete condition.
Embodiment 1
Entering acetylene cylinder from out-of-bounds acetylene, it is 0.02～0.2MPaG that acetylene enters acetylene cylinder pressure, and this example is preferably 0.15MPaG, and temperature is-20～40 DEG C, and this example is preferably 10 DEG C.Mixing with acetylene cylinder internal solvent and be dissolved completely in solvent, solvent is the one or more combination of N-Methyl pyrrolidone, dimethylformamide, dimethyl sulfoxide, monomethyl amine and acetone, and this example is preferably N-Methyl pyrrolidone.Solvent and acetylene flow-rate ratio 2～20:1 (mass ratio), this example is preferably 10:1.Solvent carries acetylene and sends into acetylene hydrogenation reactor after pump boosts after heat exchanger heats.Hydrogen mixes with acetylene at acetylene hydrogenation reactor entrance together sends into hydrogenation reactor.Hydrogen feeding temperature is 20～200 DEG C, and this example is preferably 40 DEG C.Feed pressure is 0.2～2.0MPaG, and this example is preferably 1.5MPaG.Acetylene solution mixes with hydrogen through venturi mixer, and hydrogen and acetylene flow-rate ratio are 2～10:1 (mol ratios), and this example is preferably 4:1.
Dominant response equation is as follows:
C2H2+H2→C2H4(1)
C2H2+2H2→C2H6(2)
2C2H2+2H2→C4H8(3)
Described acetylene hydrogenation reactor uses paste state bed reactor, built-in solvent.Solvent is one or more of N-Methyl pyrrolidone, dimethylformamide, dimethyl sulfoxide, monomethyl amine and acetone.This example is preferably N-Methyl pyrrolidone.Used catalyst be palladium be main active component, silver and ruthenium be auxiliary agent, aluminium sesquioxide be the catalyst of carrier.Reaction pressure is 0.1～3.0MPaG, and reaction temperature is 120～250 DEG C.This example preferably reaction pressure is 1.5MPaG, and reaction temperature is 150 DEG C.Gas is passed through bottom acetylene hydrogenation reactor, by the bubbling of gas so that catalyst suspends with slurry form in a solvent, reacts.Heat of reaction is removed by built-in heat exchanger.After reaction, gained gas phase sends into solvent absorption tower.
After reaction, gained gas phase enters bottom solvent absorption tower, and solvent enters heat exchanger after solvent pump boosts, and the solvent after heat exchanger cools down enters solvent absorption top of tower.Solvent and reaction gas counter current contacting, absorb the byproduct of reaction in gas.Solvent is one or more of N-Methyl pyrrolidone, dimethylformamide, dimethyl sulfoxide, monomethyl amine and acetone.This example is preferably N-Methyl pyrrolidone.Absorption tower operation temperature is-40 DEG C～60 DEG C, and operation pressure is 0.2～1.0MPaG.It is 40 DEG C that this example is preferably operation temperature, and operation pressure is 0.2MPaG.Solvent uses fresh solvent, sealing and circulating.Heat exchanger uses cold medium to be one or more in recirculated water, chilled water, liquefied ammonia, propylene, and this example is preferably recirculated water.
In the gas out of top, solvent absorption tower, mainly contain hydrogen and mixture of ethylene, after ethylene concentration is refined, obtain product ethylene.Hydrogen and trace by-product return acetylene hydrogenation reactor and recycle.The preferred PSA of used concentrating method separates.
The by-product that acetylene hydrogenation produces, delivers to solvent refining tower through solvent absorption tower bottom, solvent is carried out rectification cutting.According to the difference with solvent boiling point, it is referred to as light component and heavy constituent.The light component and heavy constituent impurity contained in solvent is removed by rectification cutting.Solvent after solvent refining tower lateral line withdrawal function is refined, is pumped to acetylene hydrogenation reactor recycling.Solvent refining tower operation temperature is-60 DEG C～150 DEG C, and operation pressure is-0.2MPaA～1.5MPaG.This example is preferably operation temperature 20 DEG C, operates pressure 1.0MPaG.
Through longtime running, acetylene hydrogenation catalyst inactivates.Inactivation rear catalyst delivers to catalyst filtration device after stopping, and reclaims dead catalyst.Dead catalyst producer reclaims.The preferred pressure leaf filter of catalyst filtration device.Operation pressure is preferably 0.5MPaG, and operation pressure reduction is preferably 0.2MPa, and operation temperature is preferably 50 DEG C.
Embodiment 2
Entering acetylene cylinder from out-of-bounds acetylene, it is 0.02～0.2MPaG that acetylene enters acetylene cylinder pressure, and this example is preferably 0.15MPaG, and temperature is-20～40 DEG C, and this example is preferably-10 DEG C.Mixing with acetylene cylinder internal solvent and be dissolved completely in solvent, solvent is the one or more combination of N-Methyl pyrrolidone, dimethylformamide, dimethyl sulfoxide, monomethyl amine and acetone, and this example is preferably acetone.Solvent and acetylene flow-rate ratio 2～20:1 (mass ratio), this example is preferably 5:1.Solvent carries acetylene and sends into acetylene hydrogenation reactor after pump boosts after heat exchanger heats.Hydrogen mixes with acetylene at acetylene hydrogenation reactor entrance together sends into hydrogenation reactor.Hydrogen feeding temperature is 20～200 DEG C, and this example is preferably 40 DEG C.Feed pressure is 0.2～2.0MPaG, and this example is preferably 0.45MPaG.Acetylene solution mixes with hydrogen through venturi mixer, and hydrogen and acetylene flow-rate ratio are 2～10:1 (mol ratios), and this example is preferably 6:1.
Described acetylene hydrogenation reactor uses paste state bed reactor, built-in solvent.Solvent is one or more of N-Methyl pyrrolidone, dimethylformamide, dimethyl sulfoxide, monomethyl amine and acetone.This example is preferably acetone.Used catalyst be palladium be main active component, silver and ruthenium be auxiliary agent, aluminium sesquioxide be the catalyst of carrier.Reaction pressure is 0.1～3.0MPaG, and reaction temperature is 120～250 DEG C.This example preferably reaction pressure is 0.45MPaG, and reaction temperature is 150 DEG C.Gas is passed through bottom acetylene hydrogenation reactor, by the bubbling of gas so that catalyst suspends with slurry form in a solvent, reacts.Heat of reaction is removed by built-in heat exchanger.After reaction, gained gas phase sends into solvent absorption tower.
After reaction, gained gas phase enters bottom solvent absorption tower, and solvent enters heat exchanger after solvent pump boosts, and the solvent after heat exchanger cools down enters solvent absorption top of tower.Solvent and reaction gas counter current contacting, absorb the byproduct of reaction in gas.Solvent is one or more of N-Methyl pyrrolidone, dimethylformamide, dimethyl sulfoxide, monomethyl amine and acetone.This example is preferably acetone.Absorption tower operation temperature is-40 DEG C～60 DEG C, and operation pressure is 0.2～1.0MPaG.This example is preferably operation temperature and is-5 DEG C, and operation pressure is 0.2MPaG.Solvent uses fresh solvent, sealing and circulating.Heat exchanger uses cold medium to be one or more in recirculated water, chilled water, liquefied ammonia, propylene, and this example is preferably liquefied ammonia.
In the gas out of top, solvent absorption tower, mainly contain hydrogen and mixture of ethylene, after ethylene concentration is refined, obtain product ethylene.Hydrogen and trace by-product return acetylene hydrogenation reactor and recycle.The preferred PSA of used concentrating method separates.
The by-product that acetylene hydrogenation produces, delivers to solvent refining tower through solvent absorption tower bottom, solvent is carried out rectification cutting.According to the difference with solvent boiling point, it is referred to as light component and heavy constituent.The light component and heavy constituent impurity contained in solvent is removed by rectification cutting.Solvent after solvent refining tower lateral line withdrawal function is refined, is pumped to acetylene hydrogenation reactor recycling.Solvent refining tower operation temperature is-60 DEG C～150 DEG C, and operation pressure is-0.2MPaA～1.5MPaG.This example is preferably operation temperature 20 DEG C, operates pressure 1.0MPaG.
Through longtime running, acetylene hydrogenation catalyst inactivates.Inactivation rear catalyst delivers to catalyst filtration device after stopping, and reclaims dead catalyst.Dead catalyst producer reclaims.The preferred pressure leaf filter of catalyst filtration device.Operation pressure is preferably 0.5MPaG, and operation pressure reduction is preferably 0.2MPa, and operation temperature is preferably 50 DEG C.
Embodiment 3
Entering acetylene cylinder from out-of-bounds acetylene, it is 0.02～0.2MPaG that acetylene enters acetylene cylinder pressure, and this example is preferably 0.15MPaG, and temperature is-20～40 DEG C, and this example is preferably-10 DEG C.Mixing with acetylene cylinder internal solvent and be dissolved completely in solvent, solvent is the one or more combination of N-Methyl pyrrolidone, dimethylformamide, dimethyl sulfoxide, monomethyl amine and acetone, and this example is preferably acetone.Solvent and acetylene flow-rate ratio 2～20:1 (mass ratio), this example is preferably 5:1.Solvent carries acetylene and sends into acetylene hydrogenation reactor after pump boosts after heat exchanger heats.Hydrogen mixes with acetylene at acetylene hydrogenation reactor entrance together sends into hydrogenation reactor.Hydrogen feeding temperature is 20～200 DEG C, and this example is preferably 40 DEG C.Feed pressure is 0.2～2.0MPaG, and this example is preferably 0.45MPaG.Acetylene solution mixes with hydrogen through venturi mixer, and hydrogen and acetylene flow-rate ratio are 2～10:1 (mol ratios), and this example is preferably 6:1.
Described acetylene hydrogenation reactor uses paste state bed reactor, built-in solvent.Solvent is one or more of N-Methyl pyrrolidone, dimethylformamide, dimethyl sulfoxide, monomethyl amine and acetone.This example is preferably acetone.Used catalyst be palladium be main active component, silver and ruthenium be auxiliary agent, aluminium sesquioxide be the catalyst of carrier.Reaction pressure is 0.1～3.0MPaG, and reaction temperature is 120～250 DEG C.This example preferably reaction pressure is 0.45MPaG, and reaction temperature is 150 DEG C.Gas is passed through bottom acetylene hydrogenation reactor, by the bubbling of gas so that catalyst suspends with slurry form in a solvent, reacts.Heat of reaction is removed by built-in heat exchanger.After reaction, gained gas phase sends into solvent absorption tower.
After reaction, gained gas phase enters bottom solvent absorption tower, and solvent enters heat exchanger after solvent pump boosts, and the solvent after heat exchanger cools down enters solvent absorption top of tower.Solvent and reaction gas counter current contacting, absorb the byproduct of reaction in gas.Solvent is one or more of N-Methyl pyrrolidone, dimethylformamide, dimethyl sulfoxide, monomethyl amine and acetone.This example is preferably acetone.Absorption tower operation temperature is-40 DEG C～60 DEG C, and operation pressure is 0.2～1.0MPaG.This example is preferably operation temperature and is-5 DEG C, and operation pressure is 0.2MPaG.Solvent uses fresh solvent, sealing and circulating.Heat exchanger uses cold medium to be one or more in recirculated water, chilled water, liquefied ammonia, propylene, and this example is preferably liquefied ammonia.
In the gas out of top, solvent absorption tower, mainly contain hydrogen and mixture of ethylene, after ethylene concentration is refined, obtain product ethylene.Hydrogen and trace by-product return acetylene hydrogenation reactor and recycle.The preferred PSA of used concentrating method separates.
The by-product that acetylene hydrogenation produces, delivers to solvent refining tower through solvent absorption tower bottom, solvent is carried out rectification cutting.According to the difference with solvent boiling point, it is referred to as light component and heavy constituent.The light component and heavy constituent impurity contained in solvent is removed by rectification cutting.Solvent after solvent refining tower lateral line withdrawal function is refined, is pumped to acetylene hydrogenation reactor recycling.Solvent refining tower operation temperature is-60 DEG C～150 DEG C, and operation pressure is-0.2MPaA～1.5MPaG.This example is preferably operation temperature 30 DEG C, operates pressure 1.5MPaG.
Through longtime running, acetylene hydrogenation catalyst inactivates.Inactivation rear catalyst delivers to catalyst filtration device after stopping, and reclaims dead catalyst.Dead catalyst producer reclaims.The preferred pressure leaf filter of catalyst filtration device.Operation pressure is preferably 0.5MPaG, and operation pressure reduction is preferably 0.2MPa, and operation temperature is preferably 50 DEG C.
Embodiment 4
Entering acetylene cylinder from out-of-bounds acetylene, it is 0.02～0.2MPaG that acetylene enters acetylene cylinder pressure, and this example is preferably 0.15MPaG, and temperature is-20～40 DEG C, and this example is preferably-10 DEG C.Mixing with acetylene cylinder internal solvent and be dissolved completely in solvent, solvent is the one or more combination of N-Methyl pyrrolidone, dimethylformamide, dimethyl sulfoxide, monomethyl amine and acetone, and this example is preferably acetone.Solvent and acetylene flow-rate ratio 2～20:1 (mass ratio), this example is preferably 5:1.Solvent carries acetylene and sends into acetylene hydrogenation reactor after pump boosts after heat exchanger heats.Hydrogen mixes with acetylene at acetylene hydrogenation reactor entrance together sends into hydrogenation reactor.Hydrogen feeding temperature is 20～200 DEG C, and this example is preferably 40 DEG C.Feed pressure is 0.2～2.0MPaG, and this example is preferably 0.45MPaG.Acetylene solution mixes with hydrogen through venturi mixer, and hydrogen and acetylene flow-rate ratio are 2～10:1 (mol ratios), and this example is preferably 6:1.
Described acetylene hydrogenation reactor uses paste state bed reactor, built-in solvent.Solvent is one or more of N-Methyl pyrrolidone, dimethylformamide, dimethyl sulfoxide, monomethyl amine and acetone.This example is preferably acetone.Used catalyst be palladium be main active component, silver and ruthenium be auxiliary agent, aluminium sesquioxide be the catalyst of carrier.Reaction pressure is 0.1～3.0MPaG, and reaction temperature is 120～250 DEG C.This example preferably reaction pressure is 0.8MPaG, and reaction temperature is 150 DEG C.Gas is passed through bottom acetylene hydrogenation reactor, by the bubbling of gas so that catalyst suspends with slurry form in a solvent, reacts.Heat of reaction is removed by built-in heat exchanger.After reaction, gained gas phase sends into solvent absorption tower.
After reaction, gained gas phase enters bottom solvent absorption tower, and solvent enters heat exchanger after solvent pump boosts, and the solvent after heat exchanger cools down enters solvent absorption top of tower.Solvent and reaction gas counter current contacting, absorb the byproduct of reaction in gas.Solvent is one or more of N-Methyl pyrrolidone, dimethylformamide, dimethyl sulfoxide, monomethyl amine and acetone.This example is preferably acetone.Absorption tower operation temperature is-40 DEG C～60 DEG C, and operation pressure is 0.2～1.0MPaG.This example is preferably operation temperature and is-5 DEG C, and operation pressure is 0.8MPaG.Solvent uses fresh solvent, sealing and circulating.Heat exchanger uses cold medium to be one or more in recirculated water, chilled water, liquefied ammonia, propylene, and this example is preferably liquefied ammonia.
In the gas out of top, solvent absorption tower, mainly contain hydrogen and mixture of ethylene, after ethylene concentration is refined, obtain product ethylene.Hydrogen and trace by-product return acetylene hydrogenation reactor and recycle.The preferred PSA of used concentrating method separates.
The by-product that acetylene hydrogenation produces, delivers to solvent refining tower through solvent absorption tower bottom, solvent is carried out rectification cutting.According to the difference with solvent boiling point, it is referred to as light component and heavy constituent.The light component and heavy constituent impurity contained in solvent is removed by rectification cutting.Solvent after solvent refining tower lateral line withdrawal function is refined, is pumped to acetylene hydrogenation reactor recycling.Solvent refining tower operation temperature is-60 DEG C～150 DEG C, and operation pressure is-0.2MPaA～1.5MPaG.This example preferably operates temperature-20 DEG C, operates pressure 0.5MPaG.
Through longtime running, acetylene hydrogenation catalyst inactivates.Inactivation rear catalyst delivers to catalyst filtration device after stopping, and reclaims dead catalyst.Dead catalyst producer reclaims.The preferred pressure leaf filter of catalyst filtration device.Operation pressure is preferably 0.5MPaG, and operation pressure reduction is preferably 0.2MPa, and operation temperature is preferably 50 DEG C.
The apparatus structure of this utility model high concentration producing ethylene with acetylene hydrogenation is simple, acetylene feeding pipe is connected with acetylene hydrogenation reactor by solvents for ethyne tank, acetylene is dissolved and is passed through acetylene hydrogenation reactor the most again, pressurizeed by liquid phase, overcome acetylene pressure to limit, acetylene hydrogenation can be made to operate in 1.5MPaG pressure above；Acetylene hydrogenation reactor is connected with solvent absorption tower, and after acetylene hydrogenation reaction, gained gas phase passes through solvent absorption, it is to avoid in traditional handicraft, multitower rectification separates, and energy consumption is low.The method technique of this utility model producing ethylene with acetylene hydrogenation is simple, and raw material acetylene uses the mode that solvent dissolves, and uses acetylene liquid phase pressurized delivered, safer compared with tradition acetylene in gas phase pressurization；Acetylene pressure is high pressure acetylene higher than 0.15MPaG, and risk of explosion easily occurs, and therefore traditional handicraft seldom has acetylene high pressure operating mode；The method of this utility model producing ethylene with acetylene hydrogenation can overcome acetylene pressure to limit, and acetylene hydrogenation can be made to operate in 1.5MPaG pressure above；Meanwhile, after hydrogenation reaction, tail gas passes through solvent absorption, it is to avoid in traditional handicraft, multitower rectification separates, and reduces energy consumption, and technique is advanced.The carbide production capacity that this utility model not only gives China superfluous finds a way out, and greatly alleviates China's ethylene requirements, has great importance to promoting China's acetylene chemical industry Green Sustainable, energy-saving and emission-reduction.
Although illustrate and describing this utility model with specific embodiment, however it will be appreciated that may be made that in the case of without departing substantially from spirit and scope of the present utility model many other change and amendment.It is, therefore, intended that all such changes and modifications in the range of including belonging to this utility model in the following claims.
Claims (10)
1. the device of a high concentration producing ethylene with acetylene hydrogenation, it is characterised in that the device of described high concentration producing ethylene with acetylene hydrogenation includes acetylene hydrogenation reactor, solvent absorption tower and ethylene concentration unit；Wherein, acetylene hydrogenation reactor, solvent absorption tower and ethylene concentration unit are sequentially connected；Described acetylene hydrogenation reactor is connected with acetylene feeding pipe and hydrogen feed tube road respectively；On described acetylene feeding pipe, solvents for ethyne tank is set；Described ethylene concentration unit is connected with ethylene discharging pipeline.
The device of a kind of high concentration producing ethylene with acetylene hydrogenation the most according to claim 1, it is characterised in that described acetylene feeding pipe is connected with bottom acetylene hydrogenation reactor by venturi-type eductors respectively with hydrogen feed tube road.
The device of a kind of high concentration producing ethylene with acetylene hydrogenation the most according to claim 1, it is characterised in that on the acetylene feeding pipe between described solvents for ethyne tank and acetylene hydrogenation reactor, heat exchanger is set.
The device of a kind of high concentration producing ethylene with acetylene hydrogenation the most according to claim 1, it is characterised in that described acetylene hydrogenation reactor is connected with catalyst filtration device.
The device of a kind of high concentration producing ethylene with acetylene hydrogenation the most according to claim 1, it is characterised in that described solvent absorption tower bottom sequentially passes through pump and is connected with solvent absorption top of tower with heat exchanger.
The device of a kind of high concentration producing ethylene with acetylene hydrogenation the most according to claim 1, it is characterised in that described solvent absorption tower is connected with solvent refining tower.
The device of a kind of high concentration producing ethylene with acetylene hydrogenation the most according to claim 6, it is characterised in that described solvent refining tower is connected with acetylene hydrogenation reactor.
8. according to the device of a kind of high concentration producing ethylene with acetylene hydrogenation described in claim 6 or 7, it is characterised in that described solvent refining top of tower is connected with light component discharging pipeline.
The device of a kind of high concentration producing ethylene with acetylene hydrogenation the most according to claim 8, it is characterised in that described solvent refining top of tower sequentially passes through heat exchanger and is connected with light component discharging pipeline with return tank.
10. according to the device of a kind of high concentration producing ethylene with acetylene hydrogenation described in claim 6 or 7, it is characterised in that described solvent refining tower bottom is connected with heavy constituent discharging pipeline.
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| CN107676627A (en) * | 2017-10-26 | 2018-02-09 | 北京华福工程有限公司 | The method of controlling security of producing ethylene with acetylene hydrogenation device |
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