CN102649553A - CO gas oxydehydrogenation method - Google Patents

CO gas oxydehydrogenation method Download PDF

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CN102649553A
CN102649553A CN2011100450705A CN201110045070A CN102649553A CN 102649553 A CN102649553 A CN 102649553A CN 2011100450705 A CN2011100450705 A CN 2011100450705A CN 201110045070 A CN201110045070 A CN 201110045070A CN 102649553 A CN102649553 A CN 102649553A
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gas
fluidized
bed reactor
reaction
dehydrogenation
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CN102649553B (en
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刘俊涛
刘国强
李蕾
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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Abstract

The invention relates to a CO gas oxydehydrogenation method, which mainly solves the technical problems of low hydrogenation rate and high CO loss rate in the CO gas raw material oxydehydrogenation process in the prior art. According to the method, mixed gas containing CO and hydrogen gas is adopted as raw materials, and water is selected as terminating agents. The method comprises the following steps that: (a) the raw materials firstly enter a fluidized bed reactor from the bottom of the fluidized bed reactor and are in contact with catalysts in a dense phase region and a transition region of the fluidized bed reactor to take reaction, and first effluent containing the CO and the catalysts is formed; and (b) the first effluent is in contact with the terminating agents at the bottom of a gas-solid fast separation region at the upper part of the transition region of the fluidized bed reactor, formed second effluent enters the gas-solid fast reaction region arranged at the upper part of the fluidized bed reactor to be subjected to primary gas-solid separation, then, the gas enters an external spiral cyclone separator to be continuously separated, and the separated gas enters the subsequent station to be separated. Through the technical scheme, the problem is perfectly solved, and the method can be used in CO gas oxydehydrogenation industrial production.

Description

Method by the dehydrogenation of CO gas cyaniding
Technical field
The present invention relates to a kind of method, particularly, divide device soon, be useful in the CO gas raw material oxidative dehydrogenation process about adopting the fluidized-bed reactor coupling riser reactor of outward turning cyclonic separator by the dehydrogenation of CO gas cyaniding.
Background technology
Barkite is important Organic Chemicals, is used for fine chemistry industry in a large number and produces various dyestuffs, medicine, important solvent, extraction agent and various midbody.Get into 21 century, barkite receives international extensively attention as degradable environment-friendly engineering plastics monomer.In addition, the barkite ordinary-pressure hydrolysis can get oxalic acid, and normal pressure ammonia is separated and can be got high-quality slow chemical fertilizer oxamyl.Barkite can also be used as solvent, produces medicine and dyestuff intermediate etc., for example carries out various condensation reactions with fatty ester, hexamethylene phenyl methyl ketone, amido alcohol and many heterogeneous ring compounds.It can also synthesize at the chest acyl alkali that pharmaceutically is used as hormone.In addition, the barkite low-voltage hydrogenation can prepare crucial industrial chemicals terepthaloyl moietie, and terepthaloyl moietie mainly relies on petroleum path to prepare at present, and cost is higher, and China needs a large amount of import terepthaloyl moietie every year, and import volume was nearly 4,800,000 tons in 2007.
The production route of tradition barkite utilizes oxalic acid to prepare with alcohol generation esterification, and the production technique cost is high, and energy consumption is big, and is seriously polluted, and prepared using is unreasonable.And adopt the carbon monoxide coupling technology to produce the focus that barkite has become domestic and international research.
As everyone knows; Carbon monoxide can be from the various gas mixtures that contain carbon monoxide separation and Extraction, the virgin gas that can be used for separating carbon monoxide in the industry comprises: the tail gas of synthetic gas, water-gas, semi-water gas and Iron And Steel Plant, calcium carbide factory and yellow phosphorus factory that Sweet natural gas and oil transform etc.It is pressure swing adsorption process that existing CO separates the main method of purifying; China has many companies to develop transformation fractionation by adsorption carbon monoxide new technology; Especially the high-efficiency adsorbent of developing; Carbon monoxide there are high loading capacity and selectivity, can solve a difficult problem of from the high virgin gas of nitrogen or methane content, isolating high-purity carbon monooxide, can design and build up large-scale carbon monoxide tripping device.However, by this technology isolated carbon monoxide from synthetic gas, under the prerequisite of taking into account the carbon monoxide yield, generally the content of its hydrogen can reach more than 1%.And research shows that the existence of hydrogen can cause the active reduction of follow-up CO coupling reaction catalyst, can't carry out until reaction, and therefore, the exploitation carbon monoxide selects the dehydrogenation technical meaning great.
At present, the dehydrogenation catalyst of report mainly contains Pd/Al both at home and abroad 2O 3, CoMo/Al 2O 3Deng, the dehydrogenating agent based on the manganese series metal oxide is also arranged, purify but these catalyzer or dehydrogenating agent generally are used for the dehydrogenation of non-reducing gas such as high purity nitrogen, high purity oxygen and carbonic acid gas, and reaction process is generally fixed-bed process.And exist down for the CO reducing gas, existing catalyzer and technology are low to the decreasing ratio of hydrogen, and the rate of loss of CO is high.As adopt the method and the catalyzer of the disclosed catalytic oxidative dehydrogenation of document CN97191805.8, and be raw material at the CO mixed gas that is used for hydrogen content 10%, 220 ℃ of temperature of reaction, volume space velocity 3000 hours -1, oxygen/hydrogen mol ratio is 0.6: 1, and reaction pressure is under the condition of 0.5MPa, and the rate of loss of CO is up to 1.5%, and the content of hydrogen is up to 1000ppm in the reaction effluent.
The subject matter that the related technology of above-mentioned document exists is the difficult control of temperature, and catalyst selectivity is poor, and causes the CO rate of loss high.
Summary of the invention
Technical problem to be solved by this invention is to exist in the technical literature to be used for existing the hydrogen decreasing ratio low by CO gas cyaniding dehydrogenation reaction process in the past, and the technical problem that the CO rate of loss is high provides a kind of new method by the dehydrogenation of CO gas cyaniding.This method is used for CO gas raw material oxidative dehydrogenation process, has hydrogen decreasing ratio height, the advantage that the CO rate of loss is low.
In order to solve the problems of the technologies described above, the technical scheme that the present invention adopts is following: a kind of method by the dehydrogenation of CO gas cyaniding is a raw material with the gas mixture that contains CO and hydrogen, is terminator to be selected from water, may further comprise the steps:
(a) raw material at first gets into from the fluidized-bed reactor bottom, in fluidized-bed reactor emulsion zone and zone of transition and catalyzer contact reacts, forms the elute I that contains CO and catalyzer;
(b) the elute I from (a) step contacts with terminator in the bottom, gas-solid sharp separation district on fluidized-bed reactor zone of transition top; Form elute II; Elute II gets into the gas-solid sharp separation district on fluidized-bed reactor top after the gas-solid initial gross separation; Gas gets into the outward turning cyclonic separator again to be continued to separate, and the gas after the separation gets into follow-up workshop section to be separated, and solid catalyst gets into revivifier regeneration;
(c) return the fluidized-bed reactor bottom dense from the regenerated catalyst of revivifier and proceed reaction.
In the technique scheme in the fluidized-bed reactor zone of transition of emulsion zone through the undergauge structure link to each other with gas-solid sharp separation district, top, gas-solid sharp separation district is provided with the outward turning cyclonic separator.The reaction conditions of fluidized-bed reactor is preferably: temperature of reaction is 80～260 ℃, and volume space velocity is 100～10000 hours -1, oxygen/hydrogen mol ratio is 0.5～10: 1, reaction pressure is-0.08～5.0MPa.The reaction conditions of fluidized-bed reactor is more preferably: 130～240 ℃ of temperature of reaction, volume space velocity are 1000～8000 hours -1, oxygen/hydrogen mol ratio is 0.6～8: 1, reaction pressure is 0～3.0MPa.The catalyzer preferred version is selected from least a for active ingredient in the platinum metals, is 0.003～1% of catalyst weight in the simple substance consumption; Being selected from least a for auxiliary agent in basic metal, earth alkali metal or the transition metal element compound, is 0.005～15% of catalyst weight in the simple substance consumption; The ball-aluminium oxide carrier that 84～99.5% particle diameter average out to is 20～300 microns.Catalyzer more preferably scheme active ingredient is selected from platinum or palladium in the platinum metals, is 0.02～0.8% of catalyst weight in the simple substance consumption; Auxiliary agent is selected from least a in K, Mg, Ba, V, Mn, Fe, Cu, Ce, La or the Sn compound, is 0.01～10% of catalyst weight in the simple substance consumption.The fluidized-bed reactor preferred version is selected from bubbling fluidized bed, turbulent fluidized bed, fast fluidized bed or riser reactor.Fluidized-bed reactor more preferably scheme is selected from fast fluidized bed.The weight ratio of raw material and terminator is 5～1000: 1, and the terminator feeding temperature is 10～200 ℃.
As everyone knows, carbon monoxide and hydrogen are the stronger gas of reductibility, and under the condition of the two and oxygen coexistence, normal conditions are when hydrogen is removed in selective oxidation, and CO equally also can react and lose bigger.Be strong exothermal reaction for the reaction of CO and oxygen and the reaction of hydrogen and oxygen, reaction temperature rising can be far up to more than 100 ℃ under to a certain degree.Research is also found; In the selective oxidation dehydrogenation process, the decreasing ratio of hydrogen and the rate of loss of CO and temperature of reaction were closely related under carbon monoxide existed, and the decreasing ratio of the high more hydrogen of temperature is high more; But the rate of loss of CO is also high more; And temperature is low more, and the rate of loss of CO can be low more, but the decreasing ratio of hydrogen possibly cannot say for sure to demonstrate,prove.Therefore, in selective oxidation dehydrogenation process under the carbon monoxide existence, temperature controlling is extremely important.The present invention by the characteristic that fluidized-bed temperature is evenly distributed, can realize higher hydrogen decreasing ratio and lower CO rate of loss through adopting fluid catalyst.In addition; Consider and adopt the CO gas raw material by in the catalytic oxidation dehydrogenation reaction process; Under raw material and the catalyzer Long contact time situation, still can continue to transform, especially at the settling zone of CO gas raw material oxydehydrogenation fluidized-bed reactor; A large amount of unsegregated catalyzer can continue to react with CO under the condition of high temperature, cause the CO rate of loss high.The present invention also injects terminator through the zone, outlet position of leaving catalytic bed in catalyzer and reaction product; On the one hand; The terminator that temperature is lower contacts with pyroreaction mixture and catalyzer, can significantly reduce the temperature of reaction mixture and catalyzer, and this can further quicken the rapid temperature-fall period of pyroreaction mixture and catalyzer; After reaction mixture that temperature sharply reduces and catalyzer leave reaction zone; Side reaction is few, and it is little to continue the reaction odds, has reduced the rate of loss of raw material.
Method by the dehydrogenation of CO gas cyaniding of the present invention is used device shown in Figure 1, and adopting precious metal palladium or platinum load aluminum oxide is catalyzer, and water is terminator, is 80～260 ℃ in temperature of reaction, and volume space velocity is 100～10000 hours -1, oxygen/hydrogen mol ratio is 0.5～10: 1, reaction pressure is under the condition of-0.08～5.0MPa; Raw material contacts with the precious metal fluid catalyst, and the hydrogen in the raw material is oxidized to water, in containing the gas raw material of CO; The volumn concentration of hydrogen is greater than under 0～15% the condition; The decreasing ratio of hydrogen can reach 100%, and the rate of loss of CO can obtain better technical effect less than 0.5%.
Description of drawings
The fluidized-bed reactor synoptic diagram of Fig. 1 for adopting in the method for the present invention by the dehydrogenation of CO gas cyaniding.
A is that emulsion zone, B are that zone of transition, C are negative areas, the 1st among Fig. 1, material inlet, the 2nd, sparger or grid distributor, the 3rd, interchanger, the 4th, riser tube; The 5th, settling vessel, the 6th, divide device soon, the 7th, gas tube, the 8th, outward turning cyclonic separator; The 9th, collection chamber, the outlet of 10 product gas, the 11st, stripper, the 12nd, regenerator sloped tube; The 13rd, inclined tube to be generated, the 14th, stripped vapor inlet, the 15th, terminator inlet.
Raw material is introduced by material inlet 1 among Fig. 1, and through gas distributor or grid distributor 2 laggard emulsion zone A and the catalyzer contact reacts of going into fluidized-bed that distribute, catalyzer and reaction mixture are through zone of transition B entering riser tube 4; Behind vortex quick separation device 6 sharp separation of riser tube 4 upper ends (end); Most of catalyzer gets into the lower region of settling vessel C; The part catalyzer that reaction mixture is carried secretly gets into settling vessel 5 top dilute phase spaces and carries out secondary separation through outward turning cyclonic separator 8; Product gas after the separation gets into collection chamber 9 through the outlet of outward turning cyclonic separator 8, is drawn by product gas outlet 10.Return the lower region of settling vessel 5 through the dipleg of outward turning cyclonic separator 8 from the catalyzer after 8 separation of outward turning cyclonic separator.The reclaimable catalyst of the C bottom, negative area in the settling vessel 5 gets into stripper 11; Behind stripped vapor stripping from stripped vapor inlet 14; Get into revivifier (revivifier omits among the figure) through inclined tube 12 to be generated, regenerator gets into fluidized-bed reactor emulsion zone A through regenerator sloped tube 12.In addition, the part catalyzer in the settling vessel 5 continues reaction through the laggard fluidized-bed reactor emulsion zone A of going into of interchanger 3 heat exchange bottom with catalyst mix, and whole process circulation is carried out.
Through embodiment the present invention is done further elaboration below, but be not limited only to present embodiment.
Embodiment
[embodiment 1]
Ironic oxalate is dissolved in the water, is heated to 70 ℃, the vacuum rotary dipping is 50 microns Al at average particulate diameter 2O 3On the bead, then in 120 ℃ of dryings 6 hours.With SnCl 2, magnesium nitrate and Palladous nitrate be dissolved in the water respectively, using the HCl regulator solution to make its pH value is about 4, then this solution is heated to 80 ℃; Be immersed on the carrier once more; Then in 140 ℃ of dryings 8 hours, then roasting 4 hours in 450 ℃ of air atmospheres, reductase 12 hour in 400 ℃ of hydrogen atmospheres; Obtain catalyst A, it consists of like table 1:
The catalyst A that takes by weighing above-mentioned preparation is packed in the reactor drum of accompanying drawing 1 shown device, uses the CO mixed gas of hydrogen content 10% to be raw material, 220 ℃ of temperature of reaction, and volume space velocity 3000 hours -1, oxygen/hydrogen mol ratio is 0.6: 1, and reaction pressure is under the condition of 0.5MPa, and reaction result is: the rate of loss of CO is 0.31%, and the content of hydrogen is 2ppm in the reaction effluent.
[embodiment 2]
Iron nitrate is dissolved in the water, is heated to 80 ℃, the vacuum rotary dipping is 60 microns Al at average particulate diameter 2O 3On the bead, then in 120 ℃ of dryings 4 hours.Repone K and ammonium palladic chloride are dissolved in the water respectively, and using the HCl regulator solution to make its pH value is about 4, then this solution is heated to 80 ℃; Be immersed on the carrier once more; Then in 140 ℃ of dryings 4 hours, then roasting 4 hours in 450 ℃ of air atmospheres, reductase 12 hour in 400 ℃ of hydrogen atmospheres; Obtain catalyst B, it consists of like table 1.
The catalyst B that takes by weighing above-mentioned preparation is packed in the reactor drum of accompanying drawing 1 shown device, uses the CO mixed gas of hydrogen content 8% to be raw material, 180 ℃ of temperature of reaction, and volume space velocity 1000 hours -1, oxygen/hydrogen mol ratio is 0.7: 1, and reaction pressure is under the condition of 0.2MPa, and reaction result is: the rate of loss of CO is 0.21%, and the content of hydrogen is 5ppm in the reaction effluent.
[embodiment 3]
Nitric acid niobium, rubidium nitrate are dissolved in the water respectively, and vacuum impregnation is 100 microns Al at average particulate diameter 2O 3On the bead, 140 ℃ of dryings 4 hours.Ammonium chloroplatinate is dissolved in the ethanolic soln, is immersed in once more on the carrier, 140 ℃ of dryings 4 hours; Then roasting 4 hours in 450 ℃ of air atmospheres, reduction is 4 hours in 300 ℃ of hydrogen atmospheres, then in nitrogen atmosphere, is cooled to room temperature; Obtain catalyzer C, form and see table 1.
The catalyzer C that takes by weighing above-mentioned preparation packs in the reactor drum of accompanying drawing 1 shown device, uses the CO mixed gas of hydrogen content 0.5% to be raw material, 200 ℃ of temperature of reaction, and volume space velocity 3000 hours -1, oxygen/hydrogen mol ratio is 1: 1, reaction pressure is-condition of 0.05MPa under, reaction result is: the rate of loss of CO is 0.33%, the content of hydrogen is 0 in the reaction effluent.
[embodiment 4]
Manganous nitrate, saltpetre are dissolved in the water respectively, and the vacuum rotary dipping is 80 microns Al at average particulate diameter 2O 3On the bead, 140 ℃ of dryings 4 hours.The inferior palladium acid of chlorine is dissolved in the ethanolic soln, is immersed in once more on the carrier, 140 ℃ of dryings 4 hours; Then roasting 4 hours in 450 ℃ of air atmospheres, reduction is 4 hours in 450 ℃ of hydrogen atmospheres, then in nitrogen atmosphere, is cooled to room temperature; Obtain catalyzer D, form and see table 1.
The catalyzer D that takes by weighing above-mentioned preparation packs in the reactor drum of accompanying drawing 1 shown device, 350 ℃ of reduction 4 hours, uses the CO mixed gas of hydrogen content 1% to be raw material with hydrogen then, 130 ℃ of temperature of reaction, and volume space velocity 800 hours -1, oxygen/hydrogen mol ratio is 8: 1, and reaction pressure is under the condition of 5.0MPa, and reaction result is: the rate of loss of CO is 0.15%, and the content of hydrogen is 0 in the reaction effluent.
[embodiment 5]
Iron nitrate, nitrate of baryta are dissolved in the water respectively, and the vacuum rotary dipping is 100 microns Al at average particulate diameter 2O 3On the bead, 140 ℃ of dryings 4 hours.Ammonium palladic chloride is dissolved in the ethanolic soln, is immersed in once more on the carrier, 140 ℃ of dryings 4 hours, then 450 ℃ of roastings 4 hours, reduction is 4 hours in 350 ℃ of hydrogen atmospheres, then in nitrogen atmosphere, is cooled to room temperature, obtains catalyzer E, forms and sees table 1.
The catalyzer E that takes by weighing above-mentioned preparation packs in the reactor drum of accompanying drawing 1 shown device, 350 ℃ of reduction 4 hours, uses the CO mixed gas of hydrogen content 0.5% to be raw material with hydrogen then, 100 ℃ of temperature of reaction, and volume space velocity 500 hours -1, oxygen/hydrogen mol ratio is 5: 1, and reaction pressure is under the condition of 4.0MPa, and reaction result is: the rate of loss of CO is 0.12%, and the content of hydrogen is 0 in the reaction effluent.
[embodiment 6]
Getting 200 gram average particulate diameters is 120 microns Al 2O 3On the bead; Be immersed in the 200 ml water solution that contain 8.0 gram Platinic chlorides, 14 gram magnesium nitrates, 15 milliliters of hydrochloric acid, take out the back, then roasting 2 hours in 450 ℃ of air atmospheres 140 ℃ of oven dry 4 hours; Reduction is 4 hours in 350 ℃ of hydrogen atmospheres; Then in nitrogen atmosphere, be cooled to room temperature, obtain catalyzer F, form and see table 1.
The catalyzer F that takes by weighing above-mentioned preparation packs in the reactor drum of accompanying drawing 1 shown device, 350 ℃ of reduction 4 hours, uses the CO mixed gas of hydrogen content 0.5% to be raw material with hydrogen then, 250 ℃ of temperature of reaction, and volume space velocity 8000 hours -1, oxygen/hydrogen mol ratio is 0.7: 1, and reaction pressure is under the condition of 0.2MPa, and reaction result is: the rate of loss of CO is 0.20%, and the content of hydrogen is 0 in the reaction effluent.
[embodiment 7]
Cerous nitrate, zirconium nitrate, iron nitrate are dissolved in the water respectively, and vacuum impregnation is 150 microns Al at average particulate diameter 2O 3On the bead, 140 ℃ of dryings 4 hours.Ammonium palladic chloride is dissolved in the ethanolic soln, is immersed in once more on the carrier, 140 ℃ of dryings 4 hours; Then roasting 2 hours in 450 ℃ of air atmospheres, reduction is 4 hours in 300 ℃ of hydrogen atmospheres, then in nitrogen atmosphere, is cooled to room temperature; Obtain catalyzer G, form and see table 1.
The catalyzer G that takes by weighing above-mentioned preparation packs in the reactor drum of accompanying drawing 1 shown device, 350 ℃ of reduction 4 hours, uses the CO mixed gas of hydrogen content 5% to be raw material with hydrogen then, 190 ℃ of temperature of reaction, and volume space velocity 5000 hours -1, oxygen/hydrogen mol ratio is 2: 1, and reaction pressure is under the condition of 2.0MPa, and reaction result is: the rate of loss of CO is 0.38%, and the content of hydrogen is 0 in the reaction effluent.
[embodiment 8]
Cupric nitrate, Lanthanum trinitrate, nickelous nitrate are dissolved in the water respectively, and vacuum impregnation is 200 microns Al at average particulate diameter 2O 3On the bead, 140 ℃ of dryings 4 hours.Ammonium palladic chloride is dissolved in the ethanolic soln, is immersed in once more on the carrier, 140 ℃ of dryings 4 hours; Then roasting 4 hours in 450 ℃ of air atmospheres, reduction is 4 hours in 300 ℃ of hydrogen atmospheres, then in nitrogen atmosphere, is cooled to room temperature; Obtain catalyzer H, form and see table 1.
The catalyzer H that takes by weighing above-mentioned preparation packs in the reactor drum of accompanying drawing 1 shown device, 350 ℃ of reduction 4 hours, uses the CO mixed gas of hydrogen content 1% to be raw material with hydrogen then, 90 ℃ of temperature of reaction, and volume space velocity 200 hours -1, oxygen/hydrogen mol ratio is 1: 1, and reaction pressure is under the condition of 1.0MPa, and reaction result is: the rate of loss of CO is 0.58%, and the content of hydrogen is 0 in the reaction effluent.
[comparative example 1]
The preparation of this oxide catalyst is according to shown in the embodiment 2 of 4812597 li of U.S. Pat.Ultimate analysis shows with regard to whole catalyzer and contains Pt 0.20% according to the mass percent meter, and Sn 0.23%, and Li 0.20%.
Identical raw material and condition according to embodiment 1 just adopt fixed-bed reactor, and reaction result is: the rate of loss of CO is 2.5%, and the content of hydrogen is 150ppm in the reaction effluent.
[comparative example 2]
The preparation of this oxide catalyst is according to shown in the embodiment 3 of 6858769 li of U.S. Pat.Ultimate analysis shows with regard to whole catalyzer and contains Pt 0.14% according to the mass percent meter, and Sn 0.16%, and Li 0.72%.
Identical raw material and condition according to embodiment 2 just adopt fixed-bed reactor, and reaction result is: the rate of loss of CO is 3.1%, and the content of hydrogen is 180ppm in the reaction effluent.
Obviously the inventive method is used for the selective oxidation of CO mixed gas except that H-H reaction, has higher hydrogen decreasing ratio and lower CO rate of loss.
The composition of table 1 catalyzer
The catalyzer numbering Catalyst weight is formed (in metal)
A 0.17％Pd+0.28％Sn+0.23％Mg+0.12％Fe/Al 2O 3
B 0.45％Pd+0.40％K+0.22％Fe/Al 2O 3
C 0.01％Pt+1％Nb+0.2％Rb/Al 2O 3
D 0.34％Pd+1.0％K+0.46％Mn/Al 2O 3
E 0.11％Pd+0.6％Ba+0.2％Fe/Al 2O 3
F 0.6％Pt+1.1％Mg/Al 2O 3
G 0.8％Pd+10％Ce+0.003％Zr+0.0507％Fe/Al 2O 3
H 0.005％Pd+0.015％La+5％Cu+0.2％Ni/Al 2O 3

Claims (9)

1. the method by the dehydrogenation of CO gas cyaniding is a raw material with the gas mixture that contains CO and hydrogen, is terminator to be selected from water, may further comprise the steps:
(a) raw material at first gets into from the fluidized-bed reactor bottom, in fluidized-bed reactor emulsion zone and zone of transition and catalyzer contact reacts, forms the elute I that contains CO and catalyzer;
(b) the elute I from (a) step contacts with terminator in the bottom, gas-solid sharp separation district on fluidized-bed reactor zone of transition top; Form elute II; Elute II gets into the gas-solid sharp separation district on fluidized-bed reactor top after the gas-solid initial gross separation; Gas gets into the outward turning cyclonic separator again to be continued to separate, and the gas after the separation gets into follow-up workshop section to be separated, and solid catalyst gets into revivifier regeneration;
(c) return the fluidized-bed reactor bottom dense from the regenerated catalyst of revivifier and proceed reaction.
2. according to the said method of claim 1 by the dehydrogenation of CO gas cyaniding, it is characterized in that emulsion zone in the fluidized-bed reactor links to each other with gas-solid sharp separation district through the zone of transition of undergauge structure, top, gas-solid sharp separation district is provided with the outward turning cyclonic separator.
3. according to the said method by the dehydrogenation of CO gas cyaniding of claim 1, the temperature of reaction that it is characterized in that fluidized-bed reactor is 80～260 ℃, and volume space velocity is 100～10000 hours -1, oxygen/hydrogen mol ratio is 0.5～10: 1, reaction pressure is-0.08～5.0MPa.
4. according to the said method of claim 3 by the dehydrogenation of CO gas cyaniding, it is characterized in that 130～240 ℃ of the temperature of reaction of fluidized-bed reactor, volume space velocity is 1000～8000 hours -1, oxygen/hydrogen mol ratio is 0.6～8: 1, reaction pressure is 0～3.0MPa.
5. according to the said method of claim 1 by the dehydrogenation of CO gas cyaniding, it is characterized in that catalyzer is selected from least a in the platinum metals and is active ingredient, be 0.003～1% of catalyst weight in the simple substance consumption; Being selected from least a for auxiliary agent in basic metal, earth alkali metal or the transition metal element compound, is 0.005～15% of catalyst weight in the simple substance consumption; The ball-aluminium oxide carrier that 84～99.5% particle diameter average out to is 20～300 microns.
6. according to the said method by the dehydrogenation of CO gas cyaniding of claim 5, it is characterized in that catalyzer is selected from active ingredient and is selected from platinum or palladium in the platinum metals, is 0.02～0.8% of catalyst weight in the simple substance consumption; Auxiliary agent is selected from least a in K, Mg, Ba, V, Mn, Fe, Cu, Ce, La or the Sn compound, is 0.01～10% of catalyst weight in the simple substance consumption.
7. according to the said method of claim 1, it is characterized in that fluidized-bed reactor is selected from bubbling fluidized bed, turbulent fluidized bed, fast fluidized bed or riser reactor by the dehydrogenation of CO gas cyaniding.
8. according to the said method of claim 7, it is characterized in that fluidized-bed reactor is selected from fast fluidized bed by the dehydrogenation of CO gas cyaniding.
9. according to the said method by the dehydrogenation of CO gas cyaniding of claim 1, the weight ratio that it is characterized in that raw material and terminator is 5～1000: 1, and the terminator feeding temperature is 10～100 ℃.
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