CN102757830B - Reversed flow cycle operation reaction device for methanation of synthesis gas and application thereof - Google Patents
Reversed flow cycle operation reaction device for methanation of synthesis gas and application thereof Download PDFInfo
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Abstract
The invention discloses a reversed flow cycle operation reaction device for methanation of synthesis gas and an application thereof and belongs to the field of coal chemical industry. The reaction device comprises a reactor unit and a heat exchange device, wherein the reactor unit consists of a packed bed catalytic reactor divided into three layers, two two-station three-way valves and a connecting pipeline of the two two-way stop valves; the heat exchange device comprises a raw material preheating heat exchanger and a recovered heat exchanger; and three reactor units can be connected in three combined modes during practice. According to the device, the two two-station three-way valves are alternately controlled to open and close in the process of carrying out a methanation reaction of the synthesis gas, and the flow direction of the gas is periodically changed in the packed bed catalytic reactor; and moreover, when the three reactor units are combined, the two two-way stop valves are closed, so that the whole system does not stop, and the catalysts in a certain reactor unit can be replaced, and the continuity of the production process is guaranteed. According to the device and the method, the service life of the catalyst is prolonged, and the conversion efficiency of feed gas is high.
Description
Technical field
The invention belongs to coal chemical technology, particularly a kind of flow-reversal cycleoperation reaction unit of synthesis gas methanation.
Background technology
Natural gas is a kind of clean, convenient, safe high-grade energy, and its main component is methane.Expect 2020, the consumption demand of China's natural gas year will reach 3000 billion cubic meters, have approximately 1500 billion cubic meter breach, and externally interdependency will reach 50%.The price of international energy is upheaval sharply, will bring and have a strong impact on Chinese energy safety.The energy resource structure characteristics of oil-poor, the weak breath of China, rich coal, determined that coal will occupy the main status of Chinese primary energy consumption for a long time.Utilize the relatively abundant coal resources of China or biomass resource to prepare synthetic natural gas and have more transport economic specific property and utilize usefulness, be conducive to focus on pollutant, environmental contamination reduction, for the town dweller provides efficient, clean gaseous fuel with industry.
With other coal chemical technology routes such as generating, coal liquefaction, coal methyl alcohol processed, coal derived DMEs, compare, coal or biomass-making synthetic natural gas have that energy conversion efficiency is high, the water consumption less, invest the advantages such as low, good in economic efficiency, be the optimization approach of coal conversion.Synthesis gas full methanation technology is the core technology of coal preparing natural gas.
Coal or living beings obtain synthesis gas through vaporizing system and are converted into synthetic natural gas through the full methanation process again, and main the generation reacted as follows:
2CO?+?2H
2?→?CH
4?+?H
2O
CO
2?+?4H
2?→?CH
4?+?2H
2O
CO?+?H
2O?→?CO
2?+H
2
The catalyzing methanation of synthesis gas reaction is a strong heat release reversible reaction, and existing synthesis gas methanator mainly contains following three major types.
The first kind is the plural serial stage insulation fix bed reactor, and the mode by external heat exchanger realizes that heat pipettes.Representational technology has the multistage insulation fix bed reaction process technology of German Lurgi company and South Africa SASOL company joint development, and this technology has realized many cover industrial production devices.U.S. Fuelcell Energy, Inc. discloses a kind of multistage fixed bed reaction process (CN1957076) of improved series and parallel connections combination, further reduces the load of each reactor, and product is used as to the unstripped gas of fuel cell.This class technique usually needs a plurality of reactors, and adopts the CO up to the circulating air diluting reactor import more than 5 times, to control the temperature rise in reactor, has both increased equipment investment, has increased again the power consumption of circulating air, has reduced its economy.
Equations of The Second Kind is to adopt fluidized-bed reactor.The unstripped gas of usining not only can promote unstripped gas and the effective of catalyst to contact as the fluidized-bed reaction technique of catalyst fluidization medium, can also significantly improve the heat transfer efficiency of built-in heat exchanger, be conducive to shifting out with reaction bed temperature of heat of reaction even, can under high reaction velocity, move continuously, improve the production capacity of device.Patent CN1960954 discloses a kind of methanation reaction process based on fluidized-bed reactor, but this technology depends on aromatic hydrocarbon additional in the unstripped gas heat absorption of synchronously reforming, carrys out balance.The price of aromatic hydrocarbon own is higher, and the benzene in claim, toluene or naphthalene etc. are all the end products of market demand, and the material heat-obtaining that consumes these high values does not have economy and universality.Patent CN10817716A discloses the technique of fluid bed and fixed bed coupling; Patent CN102180756A discloses gas-solid-gas-solids reactors, but all have in reactor the serious and serious problem of catalyst abrasion of back-mixing.
The 3rd class reaction process is to adopt paste state bed reactor.Patent CN101979476A discloses the technology that adopts paste state bed reactor, solved shifting out of reaction heat, but the diabatic process step is many, and during large-scale industrial application, whole efficiency remains further to be improved.
Based on the prior art feature, the present invention proposes a kind of packed bed catalytic reactor and method of the cycleoperation of the flow-reversal for methanation.By the periodically-varied feed flow direction, methanation catalytic reactor and heat exchanger are integrated, increased the integrated level of process and improved efficiency, reached the conversion ratio and selective that is beyond one's reach under traditional stationary state operating condition, having reduced the speed of catalysqt deactivation.
Summary of the invention
The purpose of this invention is to provide a kind of flow-reversal cycleoperation reaction unit of synthesis gas methanation, described reaction unit structure is as follows:
(1) reactor unit 13 comprises a packed bed catalytic reactor 5, two two-position three-way valves, two two-way stop valves and connecting pipe:
Described packed bed catalytic reactor 5 is divided into three layers: upper strata is for loading inert filler or having the heat transfer zone 8 of the solid catalyst of reactivity; Intermediate layer is the reaction zone 7 that filling has the solid catalyst of reactivity; Lower floor is for loading inert filler or having the heat transfer zone 6 of the solid catalyst of reactivity; Packed bed catalytic reactor 5 upper/lower terminals respectively have the opening of a supplied gas turnover;
The c port of first two-position three-way valve 11 is connected by pipeline with second two-way stop valve 18, and a port is connected with pipeline respectively with the b port; The f port of second two-position three-way valve 12 is connected by pipeline with first two-way stop valve 17, and the d port is connected with pipeline respectively with the e port; The other end of first two-way stop valve 17 and second two-way stop valve 18 is respectively by pipeline be positioned at the opening of supplied gas turnover of described packed bed catalytic reactor 5 lower ends and the opening of the supplied gas turnover of upper end directly is connected;
(2) heat-exchanger rig comprises a raw material preheating heat exchanger 9 and a recovery heat heat exchanger 10:
Described raw material preheating heat exchanger 9 is arranged on unstripped gas and enters on reactor unit pipeline before; Described recovery heat heat exchanger 10 is arranged on gas product from reactor unit on the pipeline out, and is connected on raw material preheating heat exchanger 9 by pipeline, thereby utilizes waste heat that gas product is with preheating to unstripped gas.
Described inert filler refers to the high temperature resistant fillers of inert inorganic such as silica, carborundum or alundum (Al2O3).
In practice, also can as required three reactor units be connected, with the content that improves methane in gas product and the stability of improving whole technical process, the mode of connection has following three kinds:
The first connected mode: an end of first reactor unit 14 has raw material gas inlet, and the outlet of its other end is connected by pipeline with the import of second reactor unit 15; The outlet of second reactor unit 15 is connected by pipeline with the import of the 3rd reactor unit 16, or directly by pipeline output products gas; The outlet of the 3rd reactor unit 16 is connected with the import of second reactor unit 15 by pipeline;
The second connected mode: an end of the 3rd reactor unit 16 has raw material gas inlet, and the outlet of its other end is connected by pipeline with the import of second reactor unit 15 and the import of first reactor unit 14; The outlet of the outlet of first reactor unit 14 and second reactor unit 15 converges rear output products gas by pipeline;
The third connected mode: an end of second reactor unit 15 has raw material gas inlet, and the outlet of its other end is connected by pipeline with the import of the 3rd reactor unit 16; The outlet of the 3rd reactor unit 16 is connected by pipeline with the import of first reactor unit 14, or directly by pipeline output products gas; The outlet of first reactor unit 14 is connected with the import of the 3rd reactor unit 16 by pipeline;
The flow-reversal cycleoperation reaction unit that has respectively the synthesis gas methanation with three reactor units of above-mentioned three kinds of connected modes all contains a raw material preheating heat exchanger 9 and a recovery heat heat exchanger 10 separately; Described raw material preheating heat exchanger 9 is installed in unstripped gas and enters first on reactor unit pipeline before; Described recovery heat heat exchanger 10 is installed in gas product and finally goes out on reactor unit pipeline afterwards, and is connected on raw material preheating heat exchanger 9 by pipeline, thereby utilizes waste heat that gas product is with preheating to unstripped gas.
Another object of the present invention is to provide a kind of method of using above-mentioned reaction unit to carry out the synthesis gas methanation, and described method is as follows:
Unstripped gas enters reactor unit after raw material preheating heat exchanger 9 is preheating to 80 ~ 250 ℃; Keep first two-way stop valve 17 and second two-way stop valve 18 always in opening; The a-c port of first two-position three-way valve 11 is communicated, and the e-f port of second two-position three-way valve 12 communicates, and unstripped gas flows from top to bottom in packed bed catalytic reactor 5; Reach time half period t
1/2the time, by computer control, the b-c port of first two-position three-way valve 11 is communicated, the d-f port of second two-position three-way valve 12 communicates, and at this moment unstripped gas flows from bottom to top in packed bed catalytic reactor 5; By setting time half period t
1/2the a-c port of regularly alternately automatically controlling first two-position three-way valve 11 communicates and the communicating of the e-f port of second two-position three-way valve 12, or the b-c port of first two-position three-way valve 11 communicates and the communicating of the d-f port of second two-position three-way valve 12, and realizes the periodicity conversion of gas flow direction in packed bed catalytic reactor 5; From reactor unit, gas product out first reclaims heat by-product superheated steams through reclaiming heat heat exchanger 10, and then through raw material preheating heat exchanger 9 by the unstripped gas preheating;
Described time half period t
1/2value be 5 minutes ~ 5 hours; Reaction temperature in packed bed catalytic reactor 5 is 250 ~ 700 ℃, and pressure is 0.1 ~ 6.0MPa, and the air speed of unstripped gas is 2000 ~ 50000 h
-1; Methanation catalyst used is the industrialization nickel catalyst of nickel content at 5 ~ 20wt%.Use these apparatus and method can make the conversion ratio of unstripped gas reach 70 ~ 98%, in gas product, the volume fraction of methane reaches more than 97%.
When using three reactor units to be connected to carry out the synthesis gas methanation, technological process is as follows:
The first connected mode: unstripped gas enters first reactor unit 14 after raw material preheating heat exchanger 9 is preheating to 80 ~ 250 ℃, enters second reactor unit 15 from first reactor unit 14 gas out and further reacts; Second reactor unit 15 gas part out enters next technical process as gas product, and another part enters reactor unit 16 and further reacts; Entering second reactor unit 15 from the 3rd reactor unit 16 gas out further reacts again.Use these apparatus and method can make the conversion ratio of unstripped gas reach 75 ~ 98%, in gas product, the volume fraction of methane reaches more than 98%;
The second connected mode: unstripped gas enters the 3rd reactor unit 16 after raw material preheating heat exchanger 9 is preheating to 80 ~ 250 ℃; Enter first reactor unit 14 from the 3rd reactor unit 16 a gas part out, another part enters second reactor unit 15 and further reacts; Enter next technical process as gas product from first reactor unit 14 and second reactor unit 15 gas mixing out.Use these apparatus and method can make the conversion ratio of unstripped gas reach 75 ~ 98%, in gas product, the volume fraction of methane reaches more than 96%;
The third connected mode: unstripped gas enters second reactor unit 15 after raw material preheating heat exchanger 9 is preheating to 80 ~ 250 ℃; Entering the 3rd reactor unit 16 from second reactor unit 15 gas out further reacts, the gas part of the 3rd reactor unit 16 outlets enters next technical process as gas product, and another part enters first reactor unit 14 and further reacts; Entering the 3rd reactor unit 16 from first reactor unit 14 gas out further reacts again.Use these apparatus and method can make the conversion ratio of unstripped gas reach 75 ~ 98%, in gas product, the volume fraction of methane reaches more than 98%;
Under normal operation, first two-way stop valve 17 and second two-way stop valve 18 of three reactor units all are held open state; When needs are changed the catalyst of some reactor units, first two-way stop valve 17 and second two-way stop valve 18 are all closed, the d-e port of second two-position three-way valve 12 of a-b port connected sum of first two-position three-way valve 11 is communicated with simultaneously; Thereby realizing that whole system is not stopped changes the catalyst of a certain reactor unit, guarantee the continuity of production process.
Beneficial effect of the present invention is:
1, in multistage packed bed catalytic reactor, the solid catalyst bed has " sandwich " formula structure, at beds two inert filler that end regions filling thermal capacity is large, intensity is high, allow inert filler serve as the heat exchanger of bed two end regions, and bear the impact to beds of the air-flow that causes due to the periodicity flow-reversal, reduce the efflorescence of catalyst, extended catalyst service life;
2, the operating characteristic of optimizing
For the synthesis gas methanation reaction, its thermodynamical equilibrium curve is as shown in the curve I in Fig. 5.What now extensively adopt due to the restriction that is subject to thermodynamical equilibrium and fuel factor is the technological process of the multistage insulation fixed bed series connection of steady state operation, and its thermodynamical equilibrium curve is as shown in the broken line IV in Fig. 5; With the optimum thermodynamical equilibrium curve shown in curve III in Fig. 5, differ greatly; And adopt flow-reversal cycleoperation technology of the present invention, its thermodynamical equilibrium curve is as shown in the curve II in Fig. 5, approach very much desirable optimum thermodynamical equilibrium curve, thereby reduced the consumption of catalyst, and reaction bed temperature is reduced on the whole, improve the final conversion ratio of raw material;
3, by the method for flow-reversal cycleoperation, by the packed bed catalytic reactor by simple function reaction zone commonly used, expand to that two ends can be recovered, three functional areas of reaction zone of the heat transfer zone of reproducibility and middle part, gas-solid catalysis heat exchange alternate with gas-solid organically integrated, reach the purpose of process intensification;
4, the heat transfer zone at packed bed catalytic reactor two ends, both can load inert filler, also can load the solid catalyst with reactivity;
5, just can replace existing multistage insulation fixed bed reactor and heat exchanger with the packed bed catalytic reactor of single hop flow-reversal cycleoperation, greatly simplified the technological process of whole synthesis gas methanation, the utilization rate of reaction heat is high, increase substantially the thermal efficiency of process, reduced equipment investment and operating cost;
6, be suitable for processing the low-temperature and low-concentration unstripped gas: even unstripped gas temperature and concentration are lower, reaction also can self-heating be carried out;
7, insensitive to the fluctuation of input parameter: the antijamming capability of flow-reversal cycleoperation is stronger, have than the larger operating flexibility of stationary state operation, reduce the sensitivity of reactor output to some conditional fluctuation of charging, even unstripped gas concentration and flow velocity be frequent fluctuation within the specific limits, system also can maintain normal operating;
8, such reversible strong exothermal reaction for the synthesis gas methanation, can reach very high conversion rate at tube exit.
The accompanying drawing explanation
Fig. 1 is synthesis gas methanation flow-reversal cycleoperation reaction unit structure of the present invention, schematic flow sheet;
Fig. 2 is the first connected mode schematic diagram that three reactor units are connected;
Fig. 3 is the second connected mode schematic diagram that three reactor units are connected;
Fig. 4 is the third connected mode schematic diagram that three reactor units are connected;
Fig. 5 is synthesis gas methanator thermodynamical equilibrium curve synoptic diagram;
Curve I is the thermodynamical equilibrium curve of synthesis gas methanation reaction; Curve II utilizes the multilayer packed bed catalytic reactor of flow-reversal cycleoperation of the present invention to carry out the thermodynamical equilibrium curve of methanation reaction; Curve III is the optimal heat mechanical balance curve of methanation reaction; Curve IV is the thermodynamical equilibrium curve of methanation reaction in existing multistage insulation fixed bed reactor;
The comparison diagram of conversion ratio when Fig. 6 is flow-reversal cycleoperation of the present invention and stationary state operation;
Curve V is feed gas methane conversion ratio situation curve over time under steady state operation condition; Curve VI is feed gas methane conversion ratio situation over time under flow-reversal cycleoperation condition of the present invention;
The comparison diagram of average bed temperature when Fig. 7 is flow-reversal cycleoperation of the present invention and steady state operation;
Curve VII is temperature situation curve over time under steady state operation condition; Curve VIII is temperature situation curve over time under flow-reversal cycleoperation condition of the present invention.
The specific embodiment
Below in conjunction with the drawings and specific embodiments, the present invention will be further described in detail:
Fig. 1 is shown in embodiment 1(technological process)
Unstripped gas enters reactor unit after raw material preheating heat exchanger 9 is preheating to 120 ℃, keep the a-c port of first two-position three-way valve 11 to communicate, the e-f port of second two-position three-way valve 12 communicates, and unstripped gas flows from top to bottom in packed bed catalytic reactor 5; Reach time half period t
1/2the time, by computer control, the b-c port of first two-position three-way valve 11 is communicated, the d-f port of second two-position three-way valve 12 communicates, and at this moment unstripped gas flows from bottom to top in packed bed catalytic reactor 5; By setting time half period t
1/2the a-c port of regularly alternately automatically controlling first two-position three-way valve 11 communicates and the communicating of the e-f port of second two-position three-way valve 12, or the b-c port of first two-position three-way valve 11 communicates and the communicating of the d-f port of second two-position three-way valve 12, and realizes the periodicity conversion of gas flow direction in packed bed catalytic reactor 5;
The time half period t adopted
1/2value be 10 minutes; Methanation catalyst used is the industrialization nickel catalyst of nickel content at 15wt%, and reaction temperature is 300 ℃, and pressure is 0.6MPa, and the air speed of unstripped gas is 5000 h
-1.In order to take full advantage of the heat of methanation reaction, from reactor, gas product out first reclaims the superheated steam of heats by-product 4.0 MPa through reclaiming heat heat exchanger 10, and then through raw material preheating heat exchanger 9 by the unstripped gas preheating.Use these apparatus and method can make the conversion ratio of unstripped gas reach 93%, in gas product, the volume fraction of methane reaches more than 94%.
Fig. 2 is shown in embodiment 2(technological process)
Unstripped gas enters first reactor unit 14 after raw material preheating heat exchanger 9 is preheating to 200 ℃, enters second reactor unit 15 from first reactor unit 14 gas out and further reacts; 50% of second reactor unit 15 gas out enters next technical process as gas product, and remaining 50% enters reactor unit 16 and further react; Entering second reactor unit 15 from the 3rd reactor unit 16 gas out further reacts again.
Three time half period t that reactor unit adopts
1/2be 15 minutes, methanation catalyst used is the industrialization nickel catalyst of nickel content at 10wt%, and reaction temperature is 400 ℃, and pressure is 0.6MPa, and the air speed of unstripped gas is 5000 h
-1.Use these apparatus and method can make the conversion ratio of unstripped gas reach 95%, in gas product, the volume fraction of methane reaches more than 97%.
The reactor network that the present embodiment adopts three reactor units to form " product " word configuration replaces the single-reactor unit, has further reduced the disturbance to downstream process and equipment, has improved the content of methane in conversion ratio and gas product; And easily realize the needs that any one reactor unit stops separately, as long as first two-way stop valve 17 and second two-way stop valve 18 are all closed, the d-e port of second two-position three-way valve 12 of a-b port connected sum of first two-position three-way valve 11 is communicated with simultaneously and just can realizes that whole system is not stopped and change the catalyst of a certain reactor unit, the continuity of assurance production process.
Fig. 3 is shown in embodiment 3(technological process)
Unstripped gas enters the 3rd reactor unit 16 after raw material preheating heat exchanger 9 is preheating to 250 ℃; Enter first reactor unit 14 from 50% of the 3rd reactor unit 16 gas out, remaining 50% enters second reactor unit 15 and further reacts; Enter next technical process as gas product from first reactor unit 14 and second reactor unit 15 gas mixing out.
Three time half period t that reactor unit adopts
1/2be 20 minutes, methanation catalyst used is the industrialization nickel catalyst of nickel content at 10wt%, and reaction temperature is 350 ℃, and pressure is 0.6MPa, and the air speed of unstripped gas is 5000h
-1.Use these apparatus and method can make the conversion ratio of unstripped gas reach 94%, in gas product, the volume fraction of methane reaches more than 96%.
The reactor network that the present embodiment adopts three reactor units to form " product " word configuration replaces the single-reactor unit, has further reduced the disturbance to downstream process and equipment, has improved the content of methane in conversion ratio and gas product; And easily realize the needs that any one reactor unit stops separately, as long as first two-way stop valve 17 and second two-way stop valve 18 are all closed, the d-e port of second two-position three-way valve 12 of a-b port connected sum of first two-position three-way valve 11 is communicated with simultaneously and just can realizes that whole system is not stopped and change the catalyst of a certain reactor unit, the continuity of assurance production process.
Fig. 4 is shown in embodiment 4(technological process)
Unstripped gas enters second reactor unit 15 after raw material preheating heat exchanger 9 is preheating to 200 ℃; Entering the 3rd reactor unit 16 from second reactor unit 15 gas out further reacts, 60% of the gas of the 3rd reactor unit 16 outlets enters next technical process as gas product, 40% entering first reactor unit 14 and further react in addition; Entering the 3rd reactor unit 16 from first reactor unit 14 gas out further reacts again.
Three time half period t that reactor unit adopts
1/2be 25 minutes, methanation catalyst used is the industrialization nickel catalyst of nickel content at 10wt%, and reaction temperature is 500 ℃, and pressure is 0.6MPa, and the air speed of unstripped gas is 4000 h
-1.Use these apparatus and method can make the conversion ratio of unstripped gas reach 98%, in gas product, the volume fraction of methane reaches more than 98%.
The reactor network that the present embodiment adopts three reactor units to form " product " word configuration replaces the single-reactor unit, has further reduced the disturbance to downstream process and equipment, has improved the content of methane in conversion ratio and gas product; And easily realize the needs that any one reactor unit stops separately, as long as first two-way stop valve 17 and second two-way stop valve 18 are all closed, the d-e port of second two-position three-way valve 12 of a-b port connected sum of first two-position three-way valve 11 is communicated with simultaneously and just can realizes that whole system is not stopped and change the catalyst of a certain reactor unit, the continuity of assurance production process.
Claims (4)
1. the flow-reversal cycleoperation reaction unit of a synthesis gas methanation, it is characterized in that, contain three reactor units, the structure of described single reactor unit, comprise a packed bed catalytic reactor (5), two two-position three-way valves, two two-way stop valves and connecting pipe: described packed bed catalytic reactor (5) is divided into three layers: upper strata is for loading inert filler or having the heat transfer zone (8) of the solid catalyst of reactivity; Intermediate layer is the reaction zone (7) that filling has the solid catalyst of reactivity; Lower floor is for loading inert filler or having the heat transfer zone (6) of the solid catalyst of reactivity; Packed bed catalytic reactor (5) upper/lower terminal respectively has the opening of a supplied gas turnover; The c port of first two-position three-way valve (11) is connected by pipeline with second two-way stop valve (18), and a port is connected with pipeline respectively with the b port; The f port of second two-position three-way valve (12) is connected by pipeline with first two-way stop valve (17), and the d port is connected with pipeline respectively with the e port; The other end of first two-way stop valve (17) and second two-way stop valve (18) is respectively by pipeline be positioned at the opening of supplied gas turnover of described packed bed catalytic reactor (5) lower end and the opening of the supplied gas turnover of upper end directly is connected;
The structure of the flow-reversal cycleoperation reaction unit of described synthesis gas methanation is as follows:
(1) three reactor unit, their connected mode is as follows:
One end of first reactor unit (14) has raw material gas inlet, and the outlet of its other end is connected by pipeline with the import of second reactor unit (15); The outlet of second reactor unit (15) is connected by pipeline with the import of the 3rd reactor unit (16), or directly by pipeline output products gas; The outlet of the 3rd reactor unit (16) is connected with the import of second reactor unit (15) by pipeline;
(2) heat-exchanger rig comprises a raw material preheating heat exchanger (9) and a recovery heat heat exchanger (10):
Described raw material preheating heat exchanger (9) is arranged on unstripped gas and enters on first reactor unit (14) pipeline before; Described recovery heat heat exchanger (10) is arranged on gas product from second reactor unit (15) on the pipeline out, and it is upper to be connected to raw material preheating heat exchanger (9) by pipeline, thereby utilizes waste heat that gas product is with preheating to unstripped gas.
2. the method that right to use requires 1 described device to carry out the synthesis gas methanation, is characterized in that, described method is as follows:
Unstripped gas enters first reactor unit (14) after raw material preheating heat exchanger (9) is preheating to 80～250 ℃, enters second reactor unit (15) from first reactor unit (14) gas out and further reacts; Second reactor unit (15) gas part out enters next technical process as gas product, and another part enters reactor unit (16) and further reacts; Entering second reactor unit (15) from the 3rd reactor unit (16) gas out further reacts again;
Under normal operation, first two-way stop valve (17) and second two-way stop valve (18) of three reactor units all are held open state; When needs are changed the catalyst of some reactor units, first two-way stop valve (17) and second two-way stop valve (18) are all closed, the d-e port of second two-position three-way valve of a-b port connected sum (12) of first two-position three-way valve (11) is communicated with simultaneously; Thereby realizing that whole system is not stopped changes the catalyst of a certain reactor unit, guarantee the continuity of production process.
3. the flow-reversal cycleoperation reaction unit of a synthesis gas methanation, it is characterized in that, contain three reactor units, the structure of described single reactor unit, comprise a packed bed catalytic reactor (5), two two-position three-way valves, two two-way stop valves and connecting pipe: described packed bed catalytic reactor (5) is divided into three layers: upper strata is for loading inert filler or having the heat transfer zone (8) of the solid catalyst of reactivity; Intermediate layer is the reaction zone (7) that filling has the solid catalyst of reactivity; Lower floor is for loading inert filler or having the heat transfer zone (6) of the solid catalyst of reactivity; Packed bed catalytic reactor (5) upper/lower terminal respectively has the opening of a supplied gas turnover; The c port of first two-position three-way valve (11) is connected by pipeline with second two-way stop valve (18), and a port is connected with pipeline respectively with the b port; The f port of second two-position three-way valve (12) is connected by pipeline with first two-way stop valve (17), and the d port is connected with pipeline respectively with the e port; The other end of first two-way stop valve (17) and second two-way stop valve (18) is respectively by pipeline be positioned at the opening of supplied gas turnover of described packed bed catalytic reactor (5) lower end and the opening of the supplied gas turnover of upper end directly is connected;
The structure of the flow-reversal cycleoperation reaction unit of described synthesis gas methanation is as follows:
(1) three reactor unit, their connected mode is as follows:
One end of the 3rd reactor unit (16) has raw material gas inlet, and the outlet of its other end is connected by pipeline with the import of second reactor unit (15) and the import of first reactor unit (14); The outlet of the outlet of first reactor unit (14) and second reactor unit (15) converges rear output products gas by pipeline;
(2) heat-exchanger rig comprises a raw material preheating heat exchanger (9) and a recovery heat heat exchanger (10):
Described raw material preheating heat exchanger (9) is arranged on unstripped gas and enters on the 3rd reactor unit (16) pipeline before; Described recovery heat heat exchanger (10) is arranged on the pipeline of gas product from first reactor unit (14) and second reactor unit (15) out converge, and it is upper to be connected to raw material preheating heat exchanger (9) by pipeline, thereby utilize waste heat that gas product is with preheating to unstripped gas.
4. the method that right to use requires 3 described devices to carry out the synthesis gas methanation, is characterized in that, described method is as follows:
Unstripped gas enters the 3rd reactor unit (16) after raw material preheating heat exchanger (9) is preheating to 80～250 ℃; From the 3rd reactor unit (16), a gas part out enters first reactor unit (14), and another part enters second reactor unit (15) and further reacts; Enter next technical process as gas product from first reactor unit (14) and second reactor unit (15) gas mixing out;
Under normal operation, first two-way stop valve (17) and second two-way stop valve (18) of three reactor units all are held open state; When needs are changed the catalyst of some reactor units, first two-way stop valve (17) and second two-way stop valve (18) are all closed, the d-e port of second two-position three-way valve of a-b port connected sum (12) of first two-position three-way valve (11) is communicated with simultaneously; Thereby realizing that whole system is not stopped changes the catalyst of a certain reactor unit, guarantee the continuity of production process.
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| CN201210260783.8A CN102757830B (en) | 2012-07-25 | 2012-07-25 | Reversed flow cycle operation reaction device for methanation of synthesis gas and application thereof |
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| CN102757830B true CN102757830B (en) | 2014-01-08 |
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