CN103044179A - Method for preparing ethylene through liquid-phase selective hydrogenation of acetylene in slurry reactor - Google Patents
Method for preparing ethylene through liquid-phase selective hydrogenation of acetylene in slurry reactor Download PDFInfo
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Abstract
The invention belongs to the technical field of chemical material preparing methods, and particularly relates to a method for preparing ethylene through liquid-phase selective hydrogenation of acetylene in a slurry reactor. A liquid-phase solvent with high selective solubility for acetylene and low selective solubility for ethylene is introduced into a gas-solid catalytic system, and the relative solubility coefficient of the solvent is larger than 8; a catalyst is dispersed evenly in the liquid-phase solvent, and process coupling is achieved through the high selective solubility of the liquid-phase solvent for acetylene, so that the selectivity of ethylene is improved; and ethylene is prepared and separated through an hydrogenation reaction of acetylene. According to the method, the concentration of ethylene on the surface of the catalyst is reduced through the process coupling, therefore a path of ethane generation through deep hydrogenation is blocked to a certain extent, and the selectivity of ethylene can be improved remarkably. Simultaneously, the liquid-phase dilution thermal effect can accelerate heat transfer in the slurry reactor, and temperature runaway is avoided. The method is not only used for preparing ethylene from acetylene obtained from natural gas pyrolysis, but also is an efficient method in a process for removing acetylene in ethylene.
Description
Technical field
The invention belongs to chemical materials preparation method technical field, particularly a kind of acetylene liquid phase selective hydrogenation in slurry attitude bed prepares the method for ethene.
Background technology
Ethene is a kind of important basic material in the modern industry, also is one of chemical of world wide production maximum, and the output of domestic ethene in 2010 is above 1,400 ten thousand tons.Ethene mainly is that the method by cracking petroleum hydrocarbon makes, and oil is a kind of Nonrenewable resources in short supply, and its price with impact fluctuations such as international environment variations very greatly; Current China annual petroleum consumption rank the second in the world, dependence on foreign countries for oil had reached 56.5% in 2011, and this has formed serious strategy and has threatened for China that oil reserve is not enriched.Therefore, seek another kind of new source and processing method and prepare large basic organic chemical raw material---ethene, as raw material, can alleviate to a great extent China for the dependency of oil at the field of industrial production petroleum replacing.
Since 2005, the carrying out of U.S.'s shale gas revolution makes world energy sources market that deep variation occur.Along with the quick progress of shale gas production technique, the energy center of gravity of the U.S. moves westwards gradually, and externally interdependency significantly descends.Data presentation, in the time of 2005, only 196 cubic metres of U.S.'s shale gas annual production, and by 2010,1378 billion cubic meters have been reached, if add compact sandstone gas and coal bed methane gas, the unconventional Sweet natural gas that the U.S. produces now accounts for about half of its Sweet natural gas ultimate production, estimates can reach 65% before the year two thousand thirty.U.S.'s Gas Prices also drops to 2 dollars/BTU in 2012 from 9 dollars/BTU in 2005, significantly changing the energy consumption structure of U.S. domestic.
The China's natural gas aboundresources, in the last few years, gas production increased gradually, and the proportion that Sweet natural gas accounts for national energy expenditure increases year by year, reached 5% of national total energy consumption to 2011, " the West-east Gas engineering increases considerably western gas utilization factor.
On the other hand, because the extensive employing of domestic Sweet natural gas acetylene technology processed and calcium carbide legal system acetylene technology, supply exceed demand for the main derived product polyvinyl chloride (PVC) of acetylene in the last few years, and the PVC industrial profit is not high, is badly in need of expanding acetylene derived product industrial chain; And polyethylene (PE) price is very large with oil price fluctuation, and other derived product such as ethylene glycol, butyleneglycol, vinylformic acid, polyvinyl alcohol (PVA) etc. also have good economic worth.Therefore, by selecting acetylene as the raw material of ethene, provide a kind of novel ethene preparation technology, can provide a kind of new raw material sources for ethylene industry, and reduce ethene to the dependency degree of petroleum resources, reduce the ethene cost.
Contain trace acetylene in naphtha cracking stove ethene out, therefore this part acetylene need to be down to acetylene content below 10 ppm the toxic effect of follow-up ethylene polymerization.Industrially react away acetylene in the ethene by acetylene selective hydrogenation, the reactor that uses is fixed-bed reactor, and the filling solid-phase catalyst carries out gas-solid phase reaction in reactor.Select to control the deep hydrogenation of acetylene in the hydrogenation process in gas phase, improve the selectivity of ethene, can further improve the economic benefit of process.Industrial acetylene hydrogenation reactor is controlled in the lower temperature range, and hydrogenation reaction is strong exothermal reaction, is easy to occur " temperature runaway " phenomenon.
Mention a kind of method of acetylene liquid-phase hydrogenatin in the US2005/0049445 patent, the flow process of this patent is: at first acetylene is dissolved in the liquid phase solvent, will be dissolved with liquid phase solvent and other gas phases (H of acetylene again
2, CO) together the beds by fixed bed react, at last liquid phase is separated the liquid phase solvent obtain respectively gas-phase product and recovery.This process is complicated, and it is higher to consume energy, and uneconomical.At this, we propose a kind of method that need not to carry out the acetylene liquid-phase hydrogenatin of gas-liquid separation operation.
Summary of the invention
Not enough for prior art, the invention provides the method that a kind of acetylene liquid phase selective hydrogenation in slurry attitude bed prepares ethene.
A kind of acetylene liquid phase selective hydrogenation in slurry attitude bed prepares the method for ethene, it is characterized in that: add liquid phase in reactor, described liquid phase solvent has the high solvability of selecting to acetylene, and ethene is had the low solvability of selecting, and its relative solubility coefficient is greater than 1; Catalyzer is dispersed in formation slurry phase in the liquid phase solvent; Acetylene and hydrogen mixture hydrogenation reaction are occured by the slurry that gas distributor is passed in the reactor in mutually, and by selective dissolution and the reaction process of gas phase in liquid phase carried out PROCESS COUPLING, ethene is isolated in preparation.
A kind of acetylene liquid phase selective hydrogenation in slurry attitude bed prepares the method for ethene, and its concrete steps are as follows:
(1) load liquid phase solvent in reactor, it has the high solvability of selecting to acetylene, and ethene is had the low solvability of selecting, and solubility coefficient is greater than 1 relatively; Granules of catalyst is dispersed in the liquid phase solvent of reactor;
(2) acetylene gas is mixed with hydrogen, gas mixture is passed into selected reactor again, high concentration ethylene gas flows out from slurry attitude bed top, by the condenser in exit, volatile liquid phase solvent is back in the reactor, does not pollute exit gas; The operation air speed scope of described reactor is 1000 ~ 30000 ml/ (gcath), and operating temperature range is 30 ~ 200 ℃, and the working pressure scope is 0.1 ~ 2 MPa, and hydrogen and acetylene volume ratio scope are 1 ~ 12;
(3) reactor exit high concentration ethylene gas separates being met the high-purity ethylene gas that polyreaction requires by tripping device.
Described catalyzer is a kind of in the group VIII metal, or two kinds of formed binary metal catalyzer in the group VIII metal, or group VIII metal and silver, copper, gold, gallium, zinc, tin, lead, the formed binary metal catalyzer of indium, wherein the charge capacity of VIII family reactive metal is 0.01 wt% ~ 0.1 wt%.
Described support of the catalyst is SiO
2, α-Al
2O
3, γ-Al
2O
3, TiO
2, ZnO, Zr
2O
3, the one or more combination in gac, carbon nanotube and the molecular sieve.
Described reactor is by being segmented into the multistage paste state bed reactor, with residence time distribution and regulation and control conversion of alkyne and the ethylene selectivity of control reactant gases in reactor.
Described liquid phase solvent is the one or more combination in N-Methyl pyrrolidone (NMP), dimethyl formamide (DMF), tetrahydrofuran (THF) (THF), dimethyl sulfoxide (DMSO) (DMSO), Monomethylamine (MMA) and the ionic liquid.
Described ionic liquid is [DMIM] [MeHPO
3], [DMIM] [Me
2PO
4], [BMIM] [MeHPO
3], [BMIM] [Me
2PO
4], [BMIM] [OAc] and [BMPyrr] [BuHPO
3] in one or more combination.
Described exit gas is C2 and C4.
Described C2 is one or more in ethane, ethene and the acetylene, and C4 is one or more in butane, butylene and the divinyl.
In the described reactor, pass into coiled pipe and carry out heat exchange with the control temperature of reaction.
Beneficial effect of the present invention is:
The present invention introduces the liquid phase solvent high, low to ethene solubleness to acetylene solubleness in the acetylene hydrogenation reaction system, pass through PROCESS COUPLING, reduce the ethylene concentration of catalyst surface, block to a certain extent the approach that deep hydrogenation generates ethane, can increase substantially the selectivity of ethene.Simultaneously, in paste state bed reactor, liquid phase heat of dilution effect can accelerate to move heat, avoids " temperature runaway ".Paste state bed reactor is carried out classification, can obtain higher conversion of alkyne and the yield of ethene of Geng Gao.
The producing ethylene with acetylene hydrogenation that the present invention not only obtains for natural gas pyrolysis, also the process for acetylene removal of impurities in the ethene provides a kind of efficient method.
Description of drawings
Fig. 1 is process flow sheet of the present invention;
Fig. 2 is a kind of process flow sheet that adopts the two-stage slurry reactor to carry out the liquid phase acetylene selective hydrogenation;
Number in the figure: 1-unstripped gas opening for feed; The 2-gas distributor; 3-first paragraph slurry filler; 4-first step conversion zone; The liquid level position of 5-first step conversion zone; 6-inter-stage gas phase flow passage; 7-inter-stage panels; 8-second stage conversion zone; 9-selects the hydrogenation loaded catalyst; 10-second segment slurry filler; The 11-gaseous phase outlet.
Embodiment
The invention provides the method that a kind of acetylene liquid phase selective hydrogenation in multistage slurry attitude bed prepares ethene, the present invention will be further described below in conjunction with the drawings and specific embodiments.
Fig. 1 is the operational flowchart of selective hydrogenation reaction in liquid phase, and concrete operations flow process of the present invention is:
(1) a certain amount of liquid phase solvent of filling in reactor, it has the high solvability of selecting to acetylene, and ethene is had the low solvability of selecting; Granules of catalyst is dispersed in the liquid phase solvent of reactor;
(2) acetylene gas is mixed with hydrogen, gas mixture is passed into selected reactor again, high concentration ethylene gas flows out from slurry attitude bed top, by the condenser in exit, volatile liquid phase solvent is back in the reactor, does not pollute exit gas; The operation air speed scope of described reactor is 1000 ml/ (gcath) ~ 30000 ml/ (gcath), and operating temperature range is 30 ℃ ~ 200 ℃, and the working pressure scope is 0.1 MPa ~ 2 MPa, and hydrogen and acetylene volume ratio scope are 1 ~ 12;
(3) reactor exit high concentration ethylene gas separates being met the high-purity ethylene gas that polyreaction requires by tripping device.
Fig. 2 is a kind of synoptic diagram that adopts the two-stage paste state bed reactor to carry out selective hydrogenation reaction in liquid phase.According to one embodiment of the present invention, by be divided into first step conversion zone 4 and second stage conversion zone 8 by the inter-stage member, the inter-stage member comprises inter-stage gas phase flow passage 6 and inter-stage panels 7 with reactor; To be packed into reactor by first paragraph slurry filler 3 and second segment slurry filler 10 after liquid phase solvent and the catalyst mix, the raw material gas phase feeding mouth 1 of unstripped gas from reactor bottom passed into, be dispersed into bubble through gas distributor 2 and enter in the reactor; Gas phase enters second stage conversion zone by inter-stage gas phase flow passage 6, and liquid phase (slurry phase) only flows in level, flows by the inter-stage member hardly; Gas phase flows out from being positioned at reactor top gaseous phase outlet 11.The angry phased soln process of gas-liquid-solid three-phase hybrid concurrency in reactor and selective hydrogenation reaction process, reactor liquid-phase outlet place obtains the ethylene product of high density.
In all embodiments of the present invention, selected preferred processing condition is: reactor preferred operations air speed scope is 1000 ml/ (gcath) ~ 1000 ml/ (gcath), more preferably 3000 ml/ (gcath) ~ 6000 ml/ (gcath); The preferred operations temperature is 60 ℃ ~ 150 ℃, more preferably 80 ℃ ~ 120 ℃; The preferred operations pressure range is 0.1 MPa ~ 0.2 MPa; The preferred volume ratio of hydrogen and acetylene is 2 ~ 12, more preferably 3 ~ 6.
Adopt one section paste state bed reactor, wherein load 100 ml N-Methyl pyrrolidone, 0.5 g catalyzer, catalyzer are the Pd/SiO that pickling process prepares
2, wherein the charge capacity of Pd is 0.01 wt%.In the reaction process, rotating speed is 700 rpm.Wherein C4 is butane, 1-butylene, cis-2-butene, Trans-2-butene, 1,3-butadiene.
Service temperature: 80 ℃,
Working pressure: 0.1 MPa,
Operation air speed: 3600 ml/ (gcath),
Hydrogen and acetylene volume ratio: 6,
Detection mode: GC7900, fid detector, capillary column.
Table 1 embodiment 1 experimental data table
100 h are carried out in experiment, without obvious deactivation phenomenom.
Adopt one section paste state bed reactor, wherein load 100 ml N-Methyl pyrrolidone, 0.5 g catalyzer, catalyzer are the Pd/SiO that pickling process prepares
2, wherein the charge capacity of Pd is 0.01 wt%.In the reaction process, rotating speed is 700 rpm.Wherein C4 is butane, 1-butylene, cis-2-butene, Trans-2-butene, 1,3-butadiene.
Service temperature: 100 ℃,
Working pressure: 0.1 MPa,
Operation air speed: 3600 ml/ (gcath),
Hydrogen and acetylene volume ratio: 10,
Detection mode: GC7900, fid detector, capillary column.
Table 2 embodiment 2 experimental data tables
100 h are carried out in experiment, without obvious deactivation phenomenom.
Adopt one section paste state bed reactor, wherein load 100 ml N-Methyl pyrrolidone, 0.5 g catalyzer, catalyzer are the Pd/SiO that pickling process prepares
2, wherein the charge capacity of Pd is 0.01 wt%.In the reaction process, rotating speed is 700 rpm.Wherein C4 is butane, 1-butylene, cis-2-butene, Trans-2-butene, 1,3-butadiene.
Service temperature: 100 ℃,
Working pressure: 0.1 MPa,
Operation air speed: 8000 ml/ (gcath),
Hydrogen and acetylene volume ratio: 10,
Detection mode: GC7900, fid detector, capillary column.
Table 3 embodiment 3 experimental data tables
100 h are carried out in experiment, without obvious deactivation phenomenom.
Embodiment 4
Adopt one section paste state bed reactor, wherein load 100 ml N-Methyl pyrrolidone, 0.5 g catalyzer, catalyzer are the Pd/SiO that pickling process prepares
2, wherein the charge capacity of Pd is 0.01 wt%.In the reaction process, rotating speed is 700 rpm.Wherein C4 is butane, 1-butylene, cis-2-butene, Trans-2-butene, 1,3-butadiene.
Service temperature: 80 ℃,
Working pressure: 0.1 MPa,
Operation air speed: 3600 ml/ (gcath),
Hydrogen and acetylene volume ratio: 6,
Detection mode: GC7900, fid detector, capillary column.
Table 4 embodiment 4 experimental data tables
100 h are carried out in experiment, without obvious deactivation phenomenom.
Claims (10)
1. acetylene liquid phase selective hydrogenation in slurry attitude bed prepares the method for ethene, and it is characterized in that: add liquid phase in reactor, described liquid phase solvent has the high solvability of selecting to acetylene, and ethene is had the low solvability of selecting, and its relative solubility coefficient is greater than 1; Catalyzer is dispersed in formation slurry phase in the liquid phase solvent; Acetylene and hydrogen mixture hydrogenation reaction are occured by the slurry that gas distributor is passed in the reactor in mutually, and by selective dissolution and the reaction process of gas phase in liquid phase carried out PROCESS COUPLING, ethene is isolated in preparation.
2. a kind of acetylene according to claim 1 liquid phase selective hydrogenation in slurry attitude bed prepares the method for ethene, it is characterized in that concrete steps are as follows:
(1) load liquid phase solvent in reactor, it has the high solvability of selecting to acetylene, and ethene is had the low solvability of selecting, and solubility coefficient is greater than 1 relatively; Granules of catalyst is dispersed in the liquid phase solvent of reactor;
(2) acetylene gas is mixed with hydrogen, gas mixture is passed into selected reactor again, high concentration ethylene gas flows out from slurry attitude bed top, by the condenser in exit, volatile liquid phase solvent is back in the reactor, does not pollute exit gas; The operation air speed scope of described reactor is 1000 ~ 30000 ml/ (gcath), and operating temperature range is 30 ~ 200 ℃, and the working pressure scope is 0.1 ~ 2 MPa, and hydrogen and acetylene volume ratio scope are 1 ~ 12;
(3) reactor exit high concentration ethylene gas separates being met the high-purity ethylene gas that polyreaction requires by tripping device.
3. a kind of acetylene according to claim 1 and 2 liquid phase selective hydrogenation in slurry attitude bed prepares the method for ethene, it is characterized in that: described catalyzer is a kind of in the group VIII metal, or two kinds of formed binary metal catalyzer in the group VIII metal, or group VIII metal and silver, copper, gold, gallium, zinc, tin, lead, the formed binary metal catalyzer of indium, wherein the charge capacity of VIII family reactive metal is 0.01 wt% ~ 0.1 wt%.
4. a kind of acetylene according to claim 3 liquid phase selective hydrogenation in slurry attitude bed prepares the method for ethene, and it is characterized in that: described support of the catalyst is SiO
2, α-Al
2O
3, γ-Al
2O
3, TiO
2, ZnO, Zr
2O
3, the one or more combination in gac, carbon nanotube and the molecular sieve.
5. a kind of acetylene according to claim 1 and 2 liquid phase selective hydrogenation in slurry attitude bed prepares the method for ethene, it is characterized in that: described reactor is by being segmented into the multistage paste state bed reactor, with residence time distribution and regulation and control conversion of alkyne and the ethylene selectivity of control reactant gases in reactor.
6. a kind of acetylene according to claim 1 and 2 liquid phase selective hydrogenation in slurry attitude bed prepares the method for ethene, and it is characterized in that: described liquid phase solvent is the one or more combination in N-Methyl pyrrolidone, dimethyl formamide, tetrahydrofuran (THF), dimethyl sulfoxide (DMSO), Monomethylamine and the ionic liquid.
7. a kind of acetylene according to claim 6 liquid phase selective hydrogenation in slurry attitude bed prepares the method for ethene, and it is characterized in that: described ionic liquid is [DMIM] [MeHPO
3], [DMIM] [Me
2PO
4], [BMIM] [MeHPO
3], [BMIM] [Me
2PO
4], [BMIM] [OAc] and [BMPyrr] [BuHPO
3] in one or more combination.
8. a kind of acetylene according to claim 2 liquid phase selective hydrogenation in slurry attitude bed prepares the method for ethene, and it is characterized in that: described exit gas is C2 and C4.
9. a kind of acetylene according to claim 8 liquid phase selective hydrogenation in slurry attitude bed prepares the method for ethene, and it is characterized in that: described C2 is one or more in ethane, ethene and the acetylene, and C4 is one or more in butane, butylene and the divinyl.
10. a kind of acetylene according to claim 1 and 2 liquid phase selective hydrogenation in slurry attitude bed prepares the method for ethene, it is characterized in that: in the described reactor, pass into coiled pipe and carry out heat exchange with the control temperature of reaction.
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| CN104829406A (en) * | 2015-05-15 | 2015-08-12 | 北京神雾环境能源科技集团股份有限公司 | Method for preparing ethylene by heterogeneous reaction |
| CN105057002A (en) * | 2015-08-07 | 2015-11-18 | 北京神雾环境能源科技集团股份有限公司 | Acetylene to ethylene liquid catalyst and preparation method therefor |
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