CN204841618U - Methanization reactor - Google Patents
Methanization reactor Download PDFInfo
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- CN204841618U CN204841618U CN201520580925.8U CN201520580925U CN204841618U CN 204841618 U CN204841618 U CN 204841618U CN 201520580925 U CN201520580925 U CN 201520580925U CN 204841618 U CN204841618 U CN 204841618U
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Abstract
The utility model discloses a methanization reactor, this reactor include that casing, intake pipe, a center section of thick bamboo, center tube, sleeve, outlet duct and setting, can load catalytic activity components in this declines the reaction channel at a center section of thick bamboo and the telescopic reaction channel that declines. Compared with the prior art, the utility model discloses a not only the catalyst use amount is few for methanization reactor, and the bed pressure drop is low in addition, and gaseous dwell time is short, reaction bed space utilization height, no gaseous bias flow and short circuit phenomenon.
Description
Technical field
The utility model relates to a kind of methanator.
Background technology
Methanator is one of nucleus equipment of coal preparing natural gas project.Methanation reaction is strong exothermic reaction, in synthesis gas methanation reaction process, there is CO and CO
2competition methanation reaction and high temperature under reverse water-gas-shift reaction, efficient heat and mass transfer is control CO and CO
2the key of competition methanation and high temperature Reversed Water-gas Shift.Research shows, often transforms CO or CO of 1%
2producible adiabatic temperature rise reaches 70 DEG C or 60 DEG C respectively.In order to control methanation reaction temperature, reclaim a large amount of heat energy produced in reaction, industrialization methanation process adopts multiple fixed bed methanator to contact, and carries out methanation reaction step by step.There are Davy company of Britain, Denmark in the company having realized the application of methanation patented technology business
the Lugri company of company and Germany.
Current methanator mainly contains two types, and one is axial restraint bed bioreactor, and another kind is radial fixed-bed reactor.Axial methanator design, process are relatively easy, simple to operate, but exist reactor apparatus bulky dimensions, bed pressure drop greatly, easily there is local run aways, move heat slowly, low conversion rate, enlarge-effect obviously and reactor need the problems such as material grade is high.Radial bed reactor ratio of height to diameter compared with large, bed pressure drop is little, reactant is short in the beds time of staying, but be difficult to realization response thing being uniformly distributed diametrically, unit catalyst bed production intensity lower.
In order to overcome the problem that in traditional chemical industry, existence is conducted heat, mass-transfer efficiency is low, rise micro-Chemical Engineering Technology twentieth century the 80s and 90s.Microreactor as the core component of micro-Chemical Engineering Technology, the chemical reaction system that it is is magnitude with millimeter, micron.The features such as microreactor has minute yardstick, larger specific surface, diffusion length is short, the time of staying is short, resistance is little on the one hand, its mass transfer, heat transfer and the reaction effect comparatively common response device height 1-3 order of magnitude; On the other hand, according to the industrial capacity requirement of reality, can be reached by the increase and decrease of the microreactor module integration and quantity with functionalization and control and regulate to produce, be conducive to the maximum utilization ratio of the equipment that realizes, shorten the process time of equipment simultaneously.
Micro passage reaction, as the class in microreactor, is used methanation reaction also to rarely have report.CN201320593757.7 discloses a kind of micro passage reaction for methanation process, and this micro-reaction channel is fixed in the gripper shoe in the middle part of reactor, is difficult to eliminate the stress expanding with heat and contract with cold and produce; CN201110030881.8 discloses a kind of method of micro passage reaction and synthesis gas full methanation thereof, and this microreactor is by some reaction channels and move the arrangement of passage of heat alternating parallel, and the pressure drop of reactor is comparatively large, is difficult to bear high pressure simultaneously.
Therefore, improve per volume of catalyst production intensity, reduce the equipment size of reactor, shorten gas in the catalyst surface time of staying, the loss of reduction reactor pressure decrease, improve the transformation efficiency of reactant, in the service life of abundant extending catalyst, the demand meeting reactor maximization is technical problem urgently to be resolved hurrily at present.
Utility model content
The purpose of this utility model is to provide a kind of methanator, this methanator adopts micro-reaction channel as reaction channel, and not only catalyst use amount is few, and bed pressure drop is low, gas residence time is short, and reaction bed space availability ratio is high, without gas bias current and short circuit phenomenon.
To achieve these goals, the utility model provides a kind of methanator, it is characterized in that, the catalytic reaction unit that this reactor comprises circular radial shaped seals pressure-bearing shell, extend into the air inlet pipe of enclosure interior, extend into the escape pipe of enclosure interior and be arranged in described housing below described air inlet pipe above described escape pipe from described housing bottom from described case top; Described catalytic reaction unit comprises central tube and is set at least one sleeve outside central tube; Central tube has central tube, and between central tube with escape pipe, fluid is communicated with; Mass flow pathway and runner is isolated between central tube and the barrel of sleeve and between the barrel of adjacent two sleeves by baffle plate fluid isolation; Annular space is formed between the outer wall of outermost sleeve and the inwall of housing; Central tube and sleeve all have micro-reaction channel that multiple radial direction is arranged, and the cylindrical shell of central tube is inside and outside and the cylindrical shell of sleeve is inside and outside by means of only this micro-reaction channel fluid connection; Air inlet pipe is communicated with the microchannel reaction gas inlet of micro-reaction channel by runner or annular space, and the microchannel reacting product outlet of micro-reaction channel is by mass flow pathway or central tube and fluid communication of giving vent to anger.
Preferably, the quantity of described sleeve is 2-500.
Preferably, the inner surface load of described micro-reaction channel has catalytic active component.
Preferably, the diameter of described micro-reaction channel reduces gradually from described microchannel reaction gas inlet to the direction of microchannel reacting product outlet.
Preferably, the diameter of described micro-reaction channel is between 2-50 millimeter.
Preferably, the ratio of the diameter of described microchannel reaction gas inlet and the diameter of described microchannel reacting product outlet is (1.1-25): 1.
Preferably, the cumulative volume of the inner space of micro-reaction channel of described multiple radial direction setting is the 30%-90% of the volume of described catalytic reaction unit.
Preferably, described micro-reaction channel is the wherein one be selected from conical pipe, flaring pipe and Y tube.
Preferably, the bottom of described air inlet pipe is provided with at least one gas distributor for the reaction gas sending into described reactor that distributes.
Preferably, the upper end of described annular space be opening and with air inlet fluid communication, the bottom end closure of annular space.
Preferably, heat-barrier material district is provided with between the bottom of described catalytic reaction unit and the bottom of described housing.
The methanator that the utility model provides is compared with existing methanator, and tool has the following advantages:
1, methanation reaction is the quick strong exothermal reaction of volume-diminished, adopt the methanator of the micro-reaction channel containing load methanation reaction catalytic active component, along with reactant flows from micro-reaction channel larger diameter end to smaller diameter end, reaction channel is more and more less, increase the motive force that methanation reaction transforms to product direction, because gas flow rate is increasing, make the time of staying of product gas in micro-reaction channel shorter;
2, by the inner surface of active constituent loading at micro-reaction channel, active component use amount is the 5%-25% of the conventional fixed bed reactors amount used of equal disposal ability, significantly reduces Catalyst Production cost;
3, due to reacting gas in the reactor the time of staying shorter, extend the service life (life-span can improve 15%-20%) of catalyst, the radial reactor of bed pressure drop comparatively with treating capacity low (50%-85%);
4, this methanator forms conversion zone by micro-reaction channel that some sizes are identical, the Biased flow phenomenon of reactionless dead band and gas, and the temperature of bed is comparatively even, there will not be focus, fully ensure that the even running in the whole service cycle;
5, the feed stock conversion of this methanator is high, target product CH
4selective more than 97%, the more conventional fixed bed of unit reactor production intensity, the fluidisation height of bed;
6, can according to the industrial capacity requirement of reality, reached by the increase and decrease of micro-reaction channel module integration and quantity with functionalization and control and regulate to produce, be conducive to the maximum utilization ratio of the equipment that realizes, without obvious enlarge-effect, shorten the process time of equipment simultaneously, reduce reactor production cost further;
7, not only can apply to coal system and substitute natural gas and gas employing methanation of coke oven technique, also can be used for the fixed-bed catalytic exothermic reactions such as methanol-fueled CLC, CO conversion and F-T synthesis.
Other feature and advantage of the present utility model are described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide further understanding of the present utility model, and forms a part for description, is used from explanation the utility model, but does not form restriction of the present utility model with detailed description of the invention one below.In the accompanying drawings:
Fig. 1 is the structural representation of a kind of detailed description of the invention of the methanator that the utility model provides;
Fig. 2 is the sectional view sectional view of A-A face (namely in Fig. 1) of a kind of detailed description of the invention of the methanator that the utility model provides;
Fig. 3 is the structural representation of the another kind of detailed description of the invention of the methanator that the utility model provides;
Fig. 4 is the sectional view sectional view of A-A face (namely in Fig. 3) of the another kind of detailed description of the invention of the methanator that the utility model provides;
Fig. 5 is the schematic diagram of a kind of detailed description of the invention (conical pipe) of micro-reaction channel that methanator that the utility model provides adopts;
Fig. 6 is the schematic diagram of a kind of detailed description of the invention (flaring pipe) of micro-reaction channel that methanator that the utility model provides adopts;
Fig. 7 is the schematic diagram of a kind of detailed description of the invention (Y tube) of micro-reaction channel that methanator that the utility model provides adopts.
Description of reference numerals
1 reacting product outlet 14 heat-barrier material district 15 first, reaction gas inlet 13 microchannel, housing 2 air inlet pipe 3 escape pipe 4 central tube 5 sleeve 6 central tube 7 baffle plate 8 mass flow pathway 9 runner 10 annular space 11 micro-reaction channel 12 microchannel gas distributor 16 second gas distributor
Detailed description of the invention
Below in conjunction with accompanying drawing, detailed description of the invention of the present utility model is described in detail.Should be understood that, detailed description of the invention described herein, only for instruction and explanation of the utility model, is not limited to the utility model.
The utility model provides a kind of methanator, it is characterized in that, this reactor comprises circular radial shaped seals pressure-bearing shell 1, the air inlet pipe 2 extending into enclosure interior from described housing 1 top, the escape pipe 3 extending into enclosure interior bottom described housing 1 and the catalytic reaction unit be arranged in described housing 1 below described air inlet pipe 2 above described escape pipe 3; At least one sleeve 5 that described catalytic reaction unit comprises central tube 4 and is set in outside central tube 4; Central tube 4 has central tube 6, and between central tube 6 with escape pipe 3, fluid is communicated with; Mass flow pathway 8 and runner 9 is isolated between the barrel of central tube 4 and sleeve 5 and between the barrel of adjacent two sleeves 5 by baffle plate 7 fluid isolation; Annular space 10 is formed between the outer wall of outermost sleeve 5 and the inwall of housing 1; Central tube 4 and sleeve 5 all have micro-reaction channel 11 that multiple radial direction is arranged, and the cylindrical shell of central tube 4 is inside and outside and the cylindrical shell of sleeve 5 is inside and outside by means of only this micro-reaction channel 11 fluid connection; Air inlet pipe 2 is communicated with the microchannel reaction gas inlet 12 of micro-reaction channel 11 by runner 9 or annular space 10, and the microchannel reacting product outlet 13 of micro-reaction channel 11 is communicated with escape pipe 3 fluid by mass flow pathway 8 or central tube 6.
According to a kind of detailed description of the invention of the present utility model, described central tube 4 and described sleeve 5 all can be made up of the top sealing plate be tightly connected, sealed bottom plate and sidewall, can be hollow in it, can be solid, as long as micro-reaction channel 11 can be held.The diameter of the diameter of described central tube 4 and the diameter ratio of central tube 5 and described central tube 4 and the diameter ratio of described sleeve 5 all can for any ratios be applicable to.
According to the utility model, under identical reaction condition and reactor diameter, the quantity increasing sleeve 5 can increase the time of contact of reacting gas and catalyst, reduces reacting gas flow velocity, thus reaches reduction pressure drop, improves the effect of conversion ratio.Can adjust the quantity of sleeve 5 according to real reaction situation, the quantity of described sleeve 5 can be 2-500, is preferably 2-15.
According to the utility model, in order to make described methanator can be used in producing methane, the inner surface of described micro-reaction channel 11 load can have catalytic active component.Described catalytic active component can adopt catalytic active component well-known to those skilled in the art, such as, can be nickel, the metal such as ruthenium and rhodium with methanation reaction activity; Described load refer to can pass through the methods such as dipping, ion sputtering, coating or filling by the catalyst containing active component or directly by active constituent loading in micro-reaction channel.Wherein, active metal component coating loading process can adopt the pretreatment and the painting method in two stages of catalyst deposit that comprise metallic matrix well-known to those skilled in the art.
According to the utility model, in order to ensure the efficiency of methanation reaction, the diameter of described micro-reaction channel 11 can between 2-50 millimeter.Because methanation reaction is the reaction that cumulative volume reduces, therefore the diameter of described micro-reaction channel 11 can reduce from described microchannel reaction gas inlet 12 to the direction of microchannel reacting product outlet 13 (ensure that the diameter of microchannel reaction gas inlet 12 is greater than the diameter of microchannel reacting product outlet 13, also comprise channel diameter and first reduce rear constant situation) gradually.The ratio of the diameter of described microchannel reaction gas inlet 12 and the diameter of described microchannel reacting product outlet 13 can be (1.1-25): 1, is preferably (2-10): 1.It should be noted that, if reactor of the present utility model to be used for other reaction, the diameter of micro-reaction channel 11 can be set according to the concrete condition of this reaction.
According to the utility model, because methanation reaction is exothermic reaction, in order to the temperature taking into account reaction efficiency and methanator controls, the cumulative volume of the inner space of micro-reaction channel 11 that described multiple radial direction is arranged can be the 30%-90% of the volume of described catalytic reaction unit.Be preferably 50%-85%.
According to a kind of detailed description of the invention of the present utility model, described micro-reaction channel 11 can for being selected from wherein a kind of (respectively as shown in Fig. 5, Fig. 6 and Fig. 7) in conical pipe, flaring pipe and Y tube; It should be understood that the diameter of described microchannel reaction gas inlet 12 is greater than the diameter of described microchannel reacting product outlet 13.Described conical pipe, flaring pipe and Y tube can adopt metal material pipe, ceramic material pipe, preferably adopt the metal tube do not reacted with the gas in methanation reaction system.It should be noted that, the conical pipe that those skilled in the art's routine uses refers to the truncated cone-shaped hollow material of both ends open, but not axial cross section is the section bar of taper.
According to the utility model, the bottom of described air inlet pipe 2 can be provided with at least one gas distributor for the reaction gas sending into described reactor that distributes.Described gas distributor can adopt those skilled in the art conventional to use, the utility model repeats no more, and described gas distributor is preferably provided with two.
According to the utility model, the upper end of described annular space 10 can be opening and be communicated with air inlet pipe 2 fluid, and the bottom of annular space 10 can be closed.
According to the utility model, excessively be heated to prevent the bottom of housing 1 and stop central tube 4 and sleeve 5 to move down, between the bottom of described catalytic reaction unit (i.e. central tube 4 and sleeve 5) and the bottom surface of described housing 1, heat-barrier material district 14 can be provided with.The heat-barrier materials such as the heat insulating ball of single material well-known to those skilled in the art or multiple composite, heat insulation felt rug or heat insulating belt can be placed with in described heat-barrier material district 14.
Further illustrate the utility model below in conjunction with accompanying drawing by embodiment, but therefore the utility model is not subject to any restriction.
Embodiment 1
As shown in Figure 1, the methanator that the present embodiment adopts comprises the pressure-bearing shell 1 that upper end is provided with air inlet pipe 2, lower end is provided with escape pipe 3, the top of described air inlet pipe 2 is provided with air inlet, the below that bottom is provided with the first gas distributor 15, first gas distributor 15 is provided with the second gas distributor 16.What be arranged on the below of described air inlet pipe 2 in described housing 1 is the catalytic reaction unit with 1 central tube 4 and 1 sleeve 5, and described central tube has central tube 6.Described central tube 4 and sleeve 5 are the container that hold micro-reaction channel 11 coaxial with cylindrical shell 1, comprise sealed bottom plate, top sealing plate and sidewall, this sleeve 5 is set in the outside of central tube 4, completely cuts off into mass flow pathway 8 (sleeve side) and runner 9 (central tube side) between sleeve 5 with central tube 4 by baffle plate 7.The sidewall of this sleeve 5 and the madial wall of described housing 1 are formed with annular space 10.The sealed bottom plate of described central tube 4 and sleeve 5 can stop central tube 4 and sleeve 5 to move down, and prevent reacting gas enter bottom sealed bottom plate and housing 1 between heat-barrier material district 14.In described housing 1, reaction zone is radial flow reaction zone, and as shown in Figure 2, described central tube 4 and sleeve 5 comprise the radial flow reaction zone that micro-reaction channel 11 of being coated with methanation activity catalyst by some inner surfaces is formed.As shown in Figure 5, micro-reaction channel 11 of described tapered tube configuration, tube wall is coated with methanation catalyst active component, and two ends are respectively with the sidewall of central tube 4 with central tube 6 is tightly connected and be tightly connected respectively at outboard tube wall in sleeve 5.
Methanator diameter of the housing is 910mm, the height of central tube and sleeve is 1200mm, central tube diameter is 150mm, central tube diameter is 450mm, sleeve diameter is 855mm, and the micro-reaction channel length of the conical pipe adopted is 150mm, conical pipe porch diameter 10mm, exit diameter 4mm, the ratio that the cumulative volume of all conical pipes accounts for catalytic reaction unit volume is 50.2%.
Provide in table 1 be the utility model adopt micro passage reaction and radial reactor contrast situation.Two kinds of reactor catalysis reaction members have same size, and as can be seen from consumption four indexs of selective, service life of target product, bed pressure drop and active metal Ni, micro passage reaction all shows comparatively excellent performance.
Table 1 micro passage reaction and radial reactor contrast table
| Type of reactor | CH 4Selective/(%) | Service life/(year) | Pressure drop/(bar) | Ni consumption/(kg) |
| Radial reactor | ≥90 | 2 | 0.175 | 240 |
| Micro passage reaction | ≥97 | 2.35 | 0.04 | 20.42 |
Embodiment 2
As shown in Figure 3, embodiment 2 is, when diameter of the housing does not become, the quantity of sleeve 5 is 3 with the difference of embodiment 1.
As shown in Figure 4, due to the increase of sleeve 5 quantity, the thickness of whole catalytic reaction unit reduces, the contraction in length of micro-reaction channel 11, adds the time of contact of reacting gas and catalyst, reduces reacting gas flow velocity, reach reduction pressure drop, improve the effect of conversion ratio.
Methanator diameter of the housing is 910mm, the height of central tube and sleeve is 1200mm, central tube diameter is 100mm, central tube diameter is 250mm, outer layer sleeve diameter is 880mm, and the micro-reaction channel length of the conical pipe adopted is 75mm, conical pipe porch diameter 8mm, exit diameter 4mm, the ratio that the cumulative volume of all conical pipes accounts for catalytic reaction unit volume is 50.4%.
The operation principle of the methanator that the utility model embodiment provides is as follows:
With reference to Fig. 1, coal based synthetic gas enters in housing 1 by reactor air inlet, successively by the first gas distributor 15 and the second gas distributor 16, after reactor cross-section is uniformly distributed, unstripped gas enters annular space 10 and runner 9, then to enter and radially across the central tube 4 of the micro-reaction channel 11 be made up of conical pipe and sleeve 5, the conical pipe inner surface that synthesis gas is being coated with methanation activity catalyst component carries out methanation reaction from microchannel reaction gas inlet 12.Reacted gas collects along the microchannel reacting product outlet 13 of micro-reaction channel 11 at central tube 5 and mass flow pathway 8.Gas product centrally pipe 5 and mass flow pathway 8 flows downward, and through heat-barrier material district 14, bottom housing 1, leaves methanator by the gas outlet of escape pipe 3.
The methanator compact conformation that the utility model provides, active metal consumption is few, bed pressure drop is little, without obvious enlarge-effect, per volume of catalyst production intensity is large, product is short in the catalyst surface time of staying, reaction heat can be removed in time, avoid catalyst to occur superheat region, extend the service life of catalytic active component.
Claims (11)
1. a methanator, it is characterized in that, this reactor comprises circular radial shaped seals pressure-bearing shell (1), extend into the air inlet pipe (2) of enclosure interior from described housing (1) top, extend into the escape pipe (3) of enclosure interior and be arranged on the catalytic reaction unit of described air inlet pipe (2) the described escape pipe in below (3) top in described housing (1) from described housing (1) bottom;
Described catalytic reaction unit comprises central tube (4) and is set in central tube (4) at least one sleeve (5) outward; Central tube (4) has central tube (6), and between central tube (6) with escape pipe (3), fluid is communicated with; Pass through baffle plate (7) fluid isolation between the barrel of central tube (4) and sleeve (5) and between the barrel of adjacent two sleeves (5) and isolate mass flow pathway (8) and runner (9); Annular space (10) is formed between the outer wall of outermost sleeve (5) and the inwall of housing (1); Central tube (4) and sleeve (5) all have micro-reaction channel (11) that multiple radial direction is arranged, and the cylindrical shell of central tube (4) is inside and outside and be communicated with by means of only this micro-reaction channel (11) fluid inside and outside the cylindrical shell of sleeve (5); Air inlet pipe (2) is communicated with the microchannel reaction gas inlet (12) of micro-reaction channel (11) by runner (9) or annular space (10), and the microchannel reacting product outlet (13) of micro-reaction channel (11) is communicated with escape pipe (3) fluid by mass flow pathway (8) or central tube (6).
2. methanator according to claim 1, is characterized in that, the quantity of described sleeve (5) is 2-500.
3. methanator according to claim 1, is characterized in that, the inner surface load of described micro-reaction channel (11) has catalytic active component.
4. methanator according to claim 1, it is characterized in that, the diameter of described micro-reaction channel (11) reduces gradually from described microchannel reaction gas inlet (12) to the direction of microchannel reacting product outlet (13).
5. methanator according to claim 1, is characterized in that, the diameter of described micro-reaction channel (11) is between 2-50 millimeter.
6. methanator according to claim 1, is characterized in that, the ratio of the diameter of described microchannel reaction gas inlet (12) and the diameter of described microchannel reacting product outlet (13) is (1.1-25): 1.
7. methanator according to claim 1, is characterized in that, the cumulative volume of the inner space of micro-reaction channel (11) that described multiple radial direction is arranged is the 30%-90% of the volume of described catalytic reaction unit.
8. methanator according to claim 1, is characterized in that, described micro-reaction channel (11) is for being selected from the wherein one in conical pipe, flaring pipe and Y tube.
9. methanator according to claim 1, is characterized in that, the bottom of described air inlet pipe (2) is provided with at least one gas distributor for the reaction gas sending into described reactor that distributes.
10. methanator according to claim 1, is characterized in that, the upper end of described annular space (10) is opening and is communicated with air inlet pipe (2) fluid, the bottom end closure of annular space (10).
11. methanators according to claim 1, is characterized in that, are provided with heat-barrier material district (14) between the bottom of described catalytic reaction unit and the bottom of described housing (1).
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| CN201520580925.8U CN204841618U (en) | 2015-08-04 | 2015-08-04 | Methanization reactor |
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| CN201520580925.8U CN204841618U (en) | 2015-08-04 | 2015-08-04 | Methanization reactor |
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| CN107224940A (en) * | 2016-03-23 | 2017-10-03 | 中国石化工程建设有限公司 | A kind of methanator and methanation process |
| CN107224938A (en) * | 2016-03-23 | 2017-10-03 | 中国石化工程建设有限公司 | A kind of radial reactor |
| CN107227184A (en) * | 2016-03-23 | 2017-10-03 | 中国石化工程建设有限公司 | It is a kind of to produce the system and technique for substituting natural gas |
| CN107224939A (en) * | 2016-03-23 | 2017-10-03 | 中国石化工程建设有限公司 | A kind of axial flow reactor |
| CN107398237A (en) * | 2016-05-20 | 2017-11-28 | 中国石化工程建设有限公司 | A kind of cold shock formula reactor |
| WO2018098547A1 (en) * | 2016-11-29 | 2018-06-07 | Adecoagro Vale Ivinhema S.A. | Biological filter for methanization reactors and reactor for methanization of industrial effluents |
| CN109694042A (en) * | 2017-10-20 | 2019-04-30 | 中国石化工程建设有限公司 | A kind of reforming hydrogen-preparation reactor and its method of reburner and reformation hydrogen production reaction |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107224940A (en) * | 2016-03-23 | 2017-10-03 | 中国石化工程建设有限公司 | A kind of methanator and methanation process |
| CN107224938A (en) * | 2016-03-23 | 2017-10-03 | 中国石化工程建设有限公司 | A kind of radial reactor |
| CN107227184A (en) * | 2016-03-23 | 2017-10-03 | 中国石化工程建设有限公司 | It is a kind of to produce the system and technique for substituting natural gas |
| CN107224939A (en) * | 2016-03-23 | 2017-10-03 | 中国石化工程建设有限公司 | A kind of axial flow reactor |
| CN107227184B (en) * | 2016-03-23 | 2019-10-08 | 中国石化工程建设有限公司 | A kind of system and technique producing substitution natural gas |
| CN107224940B (en) * | 2016-03-23 | 2019-10-15 | 中国石化工程建设有限公司 | A kind of methanator and methanation process |
| CN107224938B (en) * | 2016-03-23 | 2019-10-15 | 中国石化工程建设有限公司 | A kind of radial reactor |
| CN107398237A (en) * | 2016-05-20 | 2017-11-28 | 中国石化工程建设有限公司 | A kind of cold shock formula reactor |
| CN107398237B (en) * | 2016-05-20 | 2020-02-14 | 中国石化工程建设有限公司 | Cold quenching type reactor |
| WO2018098547A1 (en) * | 2016-11-29 | 2018-06-07 | Adecoagro Vale Ivinhema S.A. | Biological filter for methanization reactors and reactor for methanization of industrial effluents |
| CN109694042A (en) * | 2017-10-20 | 2019-04-30 | 中国石化工程建设有限公司 | A kind of reforming hydrogen-preparation reactor and its method of reburner and reformation hydrogen production reaction |
| CN109694042B (en) * | 2017-10-20 | 2021-03-05 | 中国石化工程建设有限公司 | Reforming hydrogen production reactor, reforming furnace thereof and reforming hydrogen production reaction method |
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