CN107224940A - A kind of methanator and methanation process - Google Patents
A kind of methanator and methanation process Download PDFInfo
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- CN107224940A CN107224940A CN201610170361.XA CN201610170361A CN107224940A CN 107224940 A CN107224940 A CN 107224940A CN 201610170361 A CN201610170361 A CN 201610170361A CN 107224940 A CN107224940 A CN 107224940A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
- B01J8/0257—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical annular shaped bed
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0278—Feeding reactive fluids
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00893—Feeding means for the reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00893—Feeding means for the reactants
- B01J2208/00911—Sparger-type feeding elements
Abstract
The invention discloses a kind of methanator and methanation process, the reactor includes cylindrical shape seal and pressure bearing housing (1), extend into the air inlet pipe of enclosure interior (2) at the top of the housing (1), the escape pipe of enclosure interior (3) is extend into from the housing (1) bottom, being arranged on the interior heat collecting device of radial direction catalytic reaction zone and the radial direction catalytic reaction zone in the housing (1) below the air inlet pipe (2) above the escape pipe (3).Compared with prior art, not only active metal usage amount is few, equipment size is smaller for the methanator of the present invention, and using the methanation process of the methanator, bed pressure drop is low, feed stock conversion is high, without gas bias current and short circuit phenomenon, with high financial profit, the low feature of comprehensive energy consumption.
Description
Technical field
The present invention relates to a kind of methanator and methanation process.
Background technology
The energy resource structure of China is rich coal, oil-poor, few gas, and current domestic natural gas yield is far from satisfaction
The fast-developing demand of national economy.It is both to the cleaning of coal resources, high that Development of Coal system, which substitutes natural gas,
Effect is utilized, and is the strategy supplement not enough to China's conventional gas again.For optimizing the structure of production, ensure
The normal operation of national economy, serves vital effect.
Coal system substitutes natural gas mainly by works such as coal gasification, conversion, sour gas removing, methanations
Skill finally gives the methane product for meeting quality requirement.Methanation reaction is CO, CO2With H2In methane
Change under catalyst action, generate CH4And H2O reaction, is that the strong of molecularity of reaction reduction is put
Thermal response.Research shows, often converts 1% CO or CO2Producible adiabatic temperature rise is respectively reached
70 DEG C or 60 DEG C.In order to control methanation reaction temperature, a large amount of heat energy produced in reaction, industry are reclaimed
Change methanation process to contact using multiple fixed bed adiabatic methanators, methanation is carried out step by step anti-
Should, heat reclaim unit is set between reactor.
Methanator is one of nucleus equipment of natural gas from coal project.Current methanator master
Fixed bed adiabatic reactor is used, there is reactor apparatus bulky dimensions, bed pressure drop and go out greatly, easily
Existing local run aways, shifting heat are slow, the low deficiency of conversion ratio.In order to overcome in traditional chemical industry exist heat transfer,
The problem of mass-transfer efficiency is low, twentieth century the 80s and 90s has risen micro- Chemical Engineering Technology.Microreactor conduct
The core component of micro- Chemical Engineering Technology, it be using millimeter, micron as magnitude chemical reaction system.One
Aspect microreactor has minute yardstick, larger ratio surface, diffusion length is short, the residence time is short, resistance
The features such as power is small, its mass transfer, heat transfer and reaction effect the 1-3 orders of magnitude high compared with common response device；The opposing party
Face, can pass through the microreactor module collection with functionalization according to actual industrial capacity requirement
Into and quantity increase and decrease reach control and regulation production, be advantageously implemented the maximum utilization ratio of equipment,
Shorten the process time of equipment simultaneously.
In recent years, micro passage reaction gas-solid catalysis, solid super acid reaction in by more next
More concerns.Notification number discloses a kind of microchannel plate for CN202893334U Chinese patent should
Device, the micro passage reaction uses titanium alloy plank frame, is provided with each titanium alloy cooling cover plate cold
But storehouse and reaction warehouse, the micro passage reaction can bear high pressure and corrosion stability, be disadvantageous in that reaction
Thing residence time in reaction warehouse is short, and production efficiency is relatively low.Notification number is CN203540513U China
Patent discloses a kind of micro passage reaction for methanation process, and the reactor consolidates micro- reaction channel
It is scheduled in the supporting plate in the middle part of reactor, it is difficult to eliminate the stress for generation of expanding with heat and contract with cold.Notification number is
CN102151531A Chinese patent discloses a kind of methanator and its synthesis gas full methanation
Method, the microreactor is by some reaction channels and moves passage of heat alternating parallel and arranges, the pressure of reactor
Drop is larger, while being difficult to bear high pressure.Notification number is CN204841617U, CN204816459U
Chinese patent, coal to SNG methanation process is applied to by methanator, target product have compared with
High selectivity, is disadvantageous in that unstripped gas is shorter in the residence time of such reactor, causes raw material
Conversion ratio is relatively low.
Therefore, equipment size, the reduction droop loss of reactor are reduced, it is to avoid raw material is in beds
The channel and short circuit phenomenon of middle appearance, improve the transformation efficiency of reactant, the use of abundant extension reactor
Life-span, the demand for meeting reactor maximization is technical problem urgently to be resolved hurrily at present.
The content of the invention
It is an object of the invention to provide a kind of methanator and methanation process, the methanator
Not only active metal usage amount is few, equipment size is smaller, and using the methanation of the methanator
Technique, bed pressure drop is low, feed stock conversion is high, without gas bias current and short circuit phenomenon, and reactor lifetime is more
It is long, with high financial profit, the low feature of comprehensive energy consumption.
To achieve these goals, first aspect present invention：A kind of methanator is provided, the reaction
Device includes cylindrical shape seal and pressure bearing housing, the air inlet pipe for extending into from case top enclosure interior, from housing
Bottom extend into the escape pipe of enclosure interior, is arranged on the radial direction below air inlet pipe above escape pipe in housing
Catalytic reaction zone and the interior heat collecting device of radial direction catalytic reaction zone；Radial direction catalytic reaction zone includes central tube
And including or do not include being set at least one sleeve outside central tube；Central tube has central tube, in
Heart pipe and outlet fluid communication；Between the barrel of the sleeve of central tube and innermost layer and adjacent sleeve
Mass flow pathway is formed between barrel；The outer wall of outermost sleeve or central tube during in the absence of sleeve
Annular space is formed between outer wall and the inwall of housing；Central tube and sleeve are respectively provided with multiple footpaths being radially arranged
To micro- reaction channel, and central tube cylinder is inside and outside and the cylinder of sleeve inside and outside it is only radially micro- by this
Reaction channel is in fluid communication；Air inlet pipe passes through the footpath in annular space below and central tube or outermost layer sleeve
It is in fluid communication to the radial direction microchannel reaction gas inlet of micro- reaction channel, the micro- reaction of radial direction in central tube
The radial direction microchannel reacting product outlet of passage passes through central tube and outlet fluid communication；Radially micro- reaction
The guiding subassembly of increase Hydrodynamic turbulence effect is provided with passage.
Preferably, the top of housing has at least one cooling medium entrance, and the bottom of housing has at least
One cooling medium outlet, interior heat collecting device includes cooling medium pipeline；Central tube and each sleeve each have
There is the closing space for accommodating micro- reaction channel that the inner and outer wall by respective cylinder is formed, each closing is empty
Between top be in fluid communication by cooling medium pipeline and cooling medium entrance, under each closing space
Portion is by cooling medium pipeline and cooling medium communication, and each closing space and air inlet
Pipe, central tube are that fluid is not connected with escape pipe.
Preferably, the top of housing has at least one cooling medium entrance, and the bottom of housing has at least
One cooling medium outlet, interior heat collecting device includes cooling medium pipeline；Cooling medium entrance and cooling medium
By being arranged in mass flow pathway and around central tube and/or the cooling medium pipeline fluid of sleeve between outlet
Connection.
Preferably, guiding subassembly includes fixing axle and the string being fixedly connected with the inwall of radially micro- reaction channel
It is associated in the diversion member in fixing axle, one end for being radially oriented micro- reaction channel airintake direction of diversion member
For convex.
Preferably, diversion member is selected from cone, circular conical surface, hemisphere, hemisphere face, spheroid and ball
At least one of face；Cone, the basal diameter of circular conical surface are between radial direction microchannel reacting product outlet
Diameter and radial direction microchannel reaction gas inlet diameter between；Hemisphere, hemisphere face, sphere, ball
Diameter and radial direction microchannel reacting gas of the spherical diameter of body between radial direction microchannel reacting product outlet
Between the diameter of entrance；The spacing of two neighboring diversion member is not less than the height of diversion member.
Preferably, each guiding subassembly includes 3-100 diversion member.
Preferably, radially the inner surface of micro- reaction channel and/or the outer surface of diversion member are loaded with respectively
Catalytic active component；Radially the diameter of micro- reaction channel is between 2-50 millimeters；Radially micro- reaction channel
Diameter from radial direction microchannel reaction gas inlet to the direction of radial direction microchannel reacting product outlet gradually
Reduce；The diameter of radial direction microchannel reaction gas inlet and the diameter of radial direction microchannel reacting product outlet
Ratio is (1.1-20)：1；Radially micro- reaction channel be selected from conical pipe, flaring pipe, Y tube and
One of which in laddertron；The cumulative volume of the inner space of micro- reaction channel is radial direction catalytic reaction zone
The 30%-80% of volume.
Second aspect of the present invention：A kind of methanation process is provided, the technique includes：A, coal gasification obtained
To the purified processing of synthesis gas and preheating after be divided into two strands, first burst of synthesis gas feeding main methanation of 1# is anti-
Device is answered to carry out the main methanation reactions of 1#, after reacted material is mixed after cooling with second strand of synthesis gas
The main methanators of feeding 2# carry out the main methanation reactions of 2# together, obtain the first product；B, will step
The first product of gained sends at least one supplement methanator after cooling and carries out supplement first in rapid a
Alkylation reaction, obtains the second product；C, by step b gained the second product divided after cooling
From processing, methanation product is obtained；Wherein, the main methanators of 1#, the main methanators of 2# and
At least one in the methanator methanator provided by first aspect present invention is provided.
Preferably, the boiler feedwater of the process boiler water-suppling heater preheating from drum is situated between by cooling down
Matter entrance, which is added in reactor, to carry out taking heat, takes the steam obtained after heat to send into drum.
Preferably, synthesis gas includes hydrogen and carbon monoxide and/or carbon dioxide, and the M values of synthesis gas are
2.85-3.5；M values for synthesis gas institute hydrogen volume and carbon dioxide volume the same carbon monoxide of difference
With the ratio of carbon dioxide volume sum.
Preferably, the condition of the main methanation reactions of 1# is：Reaction temperature is 300-700 DEG C, reaction pressure
For 1.0-8.5 MPas, volume space velocity is 2000-50000h-1；The condition of the main methanation reactions of 2# is：Instead
It is 300-700 DEG C to answer temperature, and reaction pressure is 1.0-8.5 MPas, and volume space velocity is 2000-50000h-1；
Supplement methanation reaction condition be：Reaction temperature is 300-550 DEG C, and reaction pressure is 1.0-4.5 MPas,
Volume space velocity is 2000-50000h-1；The volume ratio of first strand of synthesis gas and second strand of synthesis gas is 1:
(1-3.5)。
Compared with prior art, the methanator and methanation process that the present invention is provided have following excellent
Point：
1st, be provided with micro- reaction channel increase Hydrodynamic turbulence effect guiding subassembly, and guiding subassembly with
Radially micro- reaction channel is coaxial, adds turbulent extent of the reaction raw materials in microchannel, improves raw material
The probability acted on catalyst activity position, so as to improve feed stock conversion；
2nd, the conversion zone that the reactor is made up of some micro- reaction channels of size identical, it is reactionless dead
Area and the Biased flow phenomenon of gas, interior heat collecting device can effectively remove liberated heat in course of reaction, bed
Temperature it is more uniform, be not in focus, fully ensured that the even running in whole service cycle, prolonged
The service life (life-span can improve 15%-50%) of reactor is grown, bed pressure drop is relatively with treating capacity
The low 50%-85% of radial reactor；
3rd, using micro- reaction channel and/or water conservancy diversion member of the coating containing methanation reaction catalytic active component
Part, active metal usage amount is the 5%-35% of the conventional fixed bed reactors amount used of equal disposal ability,
The usage amount of active metal has been saved, has been particular enable to reduce the production cost of noble metal catalyst；
4th, the feed stock conversion of the methanation process is high, CO conversion ratio nearly 100%, target product
CH4Selectivity more than 95%, disclosure satisfy that existing coal system substitutes the production process of natural gas；
5th, micro- reaction channel with functionalization can be passed through according to actual industrial capacity requirement
Module is integrated and increase and decrease of quantity reaches control and regulation production, is advantageously implemented the maximum utilization of equipment
Efficiency, without obvious enlarge-effect, while shorten the process time of equipment, further reduction reactor production
Cost；
6th, it can not only apply to coal system and substitute natural gas and gas employing methanation of coke oven technique, it may also be used for
The fixed-bed catalytic exothermic reactions such as methanol-fueled CLC, CO conversion, F- T synthesis.
Other features and advantages of the present invention will be described in detail in subsequent embodiment part.
Brief description of the drawings
Accompanying drawing is, for providing a further understanding of the present invention, and to constitute a part for specification, with
Following embodiment is used to explain the present invention together, but is not construed as limiting the invention.
In accompanying drawing：
Fig. 1 is a kind of structural representation of the embodiment for the methanator that the present invention is provided
(there are two sleeves and micro- reaction channel is the conical pipe with hemisphere diversion member)；
Fig. 2 is that a kind of sectional view of the embodiment for the methanator that the present invention is provided (is schemed
The sectional view in A-A faces in 1)；
Fig. 3 is that a kind of schematic flow sheet of the embodiment for the methanation process that the present invention is provided (is adopted
With the methanator shown in Fig. 1, methanator is supplemented with 1#)；
Fig. 4 is the structural representation of another embodiment for the methanator that the present invention is provided
(not having sleeve, micro- reaction channel is the conical pipe with cone diversion member)；
Fig. 5 be the sectional view for another embodiment of methanator that the present invention is provided (i.e.
The sectional view in A-A faces in Fig. 4)；
Fig. 6 is the schematic flow sheet of another embodiment for the methanation process that the present invention is provided
(using the methanator shown in Fig. 4, methanator is supplemented with 1#, 2#)；
Fig. 7 is the structural representation of the third embodiment of the methanator that the present invention is provided
(there are two sleeves and micro- reaction channel is the conical pipe with hemisphere diversion member, cooling medium pipe
Line is arranged in mass flow pathway)；
Fig. 8 be the sectional view for the third embodiment of methanator that the present invention is provided (i.e.
The sectional view in A-A faces in Fig. 7)；
Fig. 9 is the schematic flow sheet of the third embodiment of the methanation process that the present invention is provided
(using the methanator shown in Fig. 7, methanator is supplemented with 1#)；
Figure 10 is a kind of having of being used of embodiment of methanator that the present invention is provided
Micro- reaction channel schematic diagram of guiding subassembly；
Figure 11 is sectional view (the i.e. A-A faces in Figure 10 for the micro- reaction channel of conical pipe that the present invention is provided
Sectional view)；
Figure 12 is sectional view (the i.e. B-B faces in Figure 10 for the micro- reaction channel of conical pipe that the present invention is provided
Sectional view)；
Figure 13 is a kind of specific reality for micro- reaction channel that the methanator that the present invention is provided is used
Apply the schematic diagram of mode (conical pipe)；
Figure 14 is a kind of specific reality for micro- reaction channel that the methanator that the present invention is provided is used
Apply the schematic diagram of mode (flaring pipe)；
Figure 15 is a kind of specific reality for micro- reaction channel that the methanator that the present invention is provided is used
Apply the schematic diagram of mode (Y tube)；
Figure 16 is a kind of specific reality for micro- reaction channel that the methanator that the present invention is provided is used
Apply the schematic diagram of mode (laddertron)；
Figure 17 is a kind of specific embodiment party for the guiding subassembly that the methanator that invention is provided is used
The schematic diagram of formula (hemisphere)；
A kind of specific embodiment party for the guiding subassembly that the methanator that Figure 18 present invention is provided is used
The schematic diagram of formula (hemisphere face)；
A kind of specific embodiment party for the guiding subassembly that the methanator that Figure 19 present invention is provided is used
The schematic diagram of formula (sphere)；
A kind of specific embodiment party for the guiding subassembly that the methanator that Figure 20 present invention is provided is used
The schematic diagram of formula (spheroid)；
A kind of specific embodiment party for the guiding subassembly that the methanator that Figure 21 present invention is provided is used
The schematic diagram of formula (cone)；
A kind of specific embodiment party for the guiding subassembly that the methanator that Figure 22 present invention is provided is used
The schematic diagram of formula (circular conical surface).
Description of reference numerals
The central tube of 1 housing, 2 air inlet pipe, 3 escape pipe 4
The microchannel reacting product outlet of 5 central tube, 6 microchannel reaction gas inlet 7
The second gas distributor of 8 annular space, 9 sleeve, 10 first gas distributor 11
The micro- guiding subassembly of reaction channel 14 of the radial direction of 12 heat-barrier material area 13
The diversion member of 15 mass flow pathway, 16 closing space, 17 fixing axle 18
The main main methanators of the 2# of methanator 20 of 19 1#
The 2# coolers of 21 1# supplement methanators, 22 1# coolers 23
The drum of 24 boiler water-suppling heater, 25 product separator 26
The 2# of 27 steam superheater, 28 1# waste heat boilers 29 supplements methanator
30 2# waste heat boilers
Embodiment
The embodiment of the present invention is described in detail below in conjunction with accompanying drawing.It should be appreciated that
Embodiment described herein is merely to illustrate and explain the present invention, and is not limited to this hair
It is bright.
First aspect present invention：A kind of methanator is provided, the reactor includes cylindrical shape sealing and held
Pressure shell body 1, from the top of housing 1 it extend into the air inlet pipe 2 of enclosure interior, is extend into from the bottom of housing 1
The escape pipe 3 of enclosure interior, the radial direction being arranged in housing 1 above 2 lower section escape pipe of air inlet pipe 3 are urged
Change reaction zone and the interior heat collecting device of radial direction catalytic reaction zone；Radial direction catalytic reaction zone includes central tube 4
And including or do not include being set at least one sleeve 9 outside central tube 4；Central tube 4 has center
Pipe 5, central tube 5 is in fluid communication with escape pipe 3；The barrel of the sleeve 9 of central tube 4 and innermost layer it
Between and the barrel of adjacent sleeve 9 between be formed with mass flow pathway 15；The outer wall of outermost sleeve 9 or
Annular space 8 is formed between the outer wall of central tube 4 during in the absence of sleeve 9 and the inwall of housing 1；Center
Cylinder 4 and sleeve 9 are respectively provided with the micro- reaction channel 13 of multiple radial directions being radially arranged, and the cylinder of central tube 4
Only it is in fluid communication inside and outside the cylinder of inside and outside and sleeve 9 by the micro- reaction channel 13 of the radial direction；Air inlet
Pipe 2 passes through the micro- reaction channel 13 of radial direction in annular space 8 below and central tube 4 or outermost layer sleeve 9
Microchannel reaction gas inlet 6 be in fluid communication, the micro- reaction channel 13 of the radial direction in central tube 4 it is micro-
Pathway reaction product exit 7 is in fluid communication by central tube 5 with escape pipe 3；Radially micro- reaction channel 13
Inside it is provided with the guiding subassembly 14 of increase Hydrodynamic turbulence effect.
According to the first aspect of the invention, central tube 4 and sleeve 9 can be by the tops that are tightly connected
Sealing plate, sealed bottom plate and side wall are constituted, can be with hollow in it, can be with solid, as long as can accommodate
Micro- reaction channel 13.The diameter of central tube 4 and the diameter ratio of central tube 5 and central tube 4
The diameter ratio of diameter and sleeve 9 can be suitable any ratio.
According to the first aspect of the invention, under identical reaction condition and reactor diameter, sleeve is increased
9 quantity can increase the time of contact of reacting gas and catalyst, reduce reacting gas flow velocity, so that
Reduction pressure drop is reached, the effect of conversion ratio is improved, therefore sleeve can be adjusted according to real reaction situation
9 quantity, the quantity of the sleeve 9 preferred 1-500, more preferably 2-50.
Because methanation reaction is exothermic reaction, it is therefore desirable to reduce the temperature of methanator, this hair
The bright interior heat collecting device by radial direction catalytic reaction zone cools to methanator, and interior heat collecting device includes
Cooling medium pipeline.A kind of embodiment according to the first aspect of the invention, the top of housing 1
1# cooling mediums entrance and 2# cooling medium entrances can be oppositely disposed, the bottom of housing 1 also may be used
To be symmetrically provided with the outlet of 1# cooling mediums and the outlet of 2# cooling mediums；Central tube 4 and each sleeve 9
Each there is the closing space 16 of the micro- reaction channel 13 of receiving formed by the inner and outer wall of respective cylinder,
The top of each closing space 16 is in fluid communication by cooling medium pipeline and cooling medium entrance, often
The bottom of one closing space 16 by cooling medium pipeline and cooling medium communication, and
Each closing space 16 is that fluid is not connected with air inlet pipe 2, central tube 5 and escape pipe 3.
Another embodiment according to a first aspect of the present invention, cooling medium entrance and cooling medium
By being arranged in mass flow pathway 15 and around central tube 4 and/or the cooling medium pipe of sleeve 9 between outlet
Line is in fluid communication.It should be noted that with can be between a pair of cooling medium entrances and cooling medium outlet
It is in fluid communication by many cooling medium pipelines.
According to the first aspect of the invention, in order to improve the conversion ratio of unstripped gas, in radially micro- reaction channel
The guiding subassembly 14 of increase Hydrodynamic turbulence effect is provided with 13, guiding subassembly 14 includes fixing axle 17
With diversion member 18.Guiding subassembly 14 and radially micro- reaction channel 13 are coaxial, the two ends of guiding subassembly 14
Microchannel reaction gas inlet 6, microchannel reacting product outlet 7 are individually fixed in, diversion member 18 is gone here and there
Connection is fixed in fixing axle 17, as shown in Figure 10, Figure 11, Figure 12.Make in same guiding subassembly 14
The size of diversion member 18 can be gone out from microchannel reaction gas inlet 6 to microchannel reaction product
Mouth 7 is gradually reduced, and can also gradually be increased, can also be constant, and same guiding subassembly 14 preferably makes
The size of diversion member 18 is identical.The micro- reaction channel 13 of the direction radial direction of diversion member 18 enters
The one end in gas direction is convex, for example, can be selected from hemisphere, hemisphere face, sphere, spheroid, circular cone
One kind in body, circular conical surface (respectively such as Figure 17, Figure 18, Figure 19, Figure 20, Figure 21 and Figure 22).
A kind of embodiment according to a first aspect of the present invention, further, when diversion member 18
During for cone or circular conical surface, its basal diameter leads between the diameter of microchannel reacting product outlet 7 with micro-
Between the diameter of road reaction gas inlet 6, it is preferred that its basal diameter is microchannel reacting product outlet
7 diameter and 4th/1 to five/5ths of the diameter sum of microchannel reaction gas inlet 6, length
No more than radially 0.9 times of the micro- length of reaction channel 13, further, length is logical for radially micro- reaction
0.1-0.5 times of the length of road 13；When diversion member 18 is hemisphere, hemisphere face, sphere or spheroid,
Its spherical diameter is straight between diameter and the microchannel reaction gas inlet 6 of microchannel reacting product outlet 7
Between footpath, it is preferred that spherical diameter is the diameter and microchannel reaction gas of microchannel reacting product outlet 7
4th/to five/5ths of the diameter sum of body entrance 6.The spacing of two neighboring diversion member 18
Not less than the height of the diversion member 18.
According to the first aspect of the invention, diversion member 18 and fixing axle 17 can using metal material pipe,
Ceramic material pipe, it is preferred to use the metal tube not reacted with the gas in reaction system；Each water conservancy diversion
The quantity of diversion member 18 included by component 14 can be according to the size and reality of radially micro- reaction channel 13
Border response situation is adjusted, for example, can be 3-100.
According to the first aspect of the invention, in order that the methanator can be used in producing methane,
Radially the inner surface of micro- reaction channel 13, the outer surface of diversion member 18 can be loaded with catalytic activity group
Point.The catalytic active component can use catalytic active component well-known to those skilled in the art, example
Such as can be nickel, ruthenium and rhodium metal with methanation reaction activity；Described load refers to lead to
Crossing the methods such as dipping, ion sputtering, coating or filling will be living by the catalyst containing active component or directly
Property component is loaded in micro- reaction channel.Wherein, active metal component coating loading process can be using this
The painting in two stages of pretreatment and catalyst deposit including metallic matrix known to art personnel
Coating method.
According to the first aspect of the invention, in order to ensure the efficiency of methanation reaction, the micro- reaction of the radial direction
The diameter of passage 13 can be between 2-50 millimeters.Because methanation reaction is the reaction that cumulative volume reduces,
Therefore the diameter of the micro- reaction channel 13 of radial direction can be from the microchannel reaction gas inlet 6 to micro-
The direction of pathway reaction product exit 7, which is gradually reduced, (ensures that the diameter of microchannel reaction gas inlet 6 is big
In the diameter of microchannel reacting product outlet 7, constant feelings after also first reducing including channel diameter
Condition).The diameter of the microchannel reaction gas inlet 6 is straight with the microchannel reacting product outlet 7
The ratio in footpath can be (1.1-20)：1, be preferably (2-10)：1.If it should be noted that will
The reactor of invention is used for other reactions, can set micro- reaction channel 13 according to the concrete condition of the reaction
Diameter.
According to a first aspect of the present invention, radially micro- reaction channel 13 can be selected from conical pipe, tubaeform
One of which in pipe, Y tube and laddertron is (respectively such as Figure 13, Figure 14, Figure 15 and Figure 16 institute
Show)；It should be understood that the diameter of microchannel reaction gas inlet 6 goes out more than microchannel reaction product
The diameter of mouth 7.Conical pipe, flaring pipe, Y tube and laddertron can be using metal material pipe, potteries
Porcelain material pipe, it is preferred to use the metal tube not reacted with the gas in methanation reaction system.Need
Illustrate, the conventional use of conical pipe of those skilled in the art refers to the truncated cone-shaped hollow type of both ends open
Material, rather than the section bar that axial cross section is taper.
According to the first aspect of the invention, because methanation reaction is exothermic reaction, in order to take into account reaction effect
The temperature control of rate and methanator, radially the cumulative volume of the inner space of micro- reaction channel 13 can
Think the 30%-80% of the volume of catalytic reaction zone, preferably 35%-65%.
According to the first aspect of the invention, the bottom of air inlet pipe 2 can be provided with least one and be used to be distributed
Send into the gas distributor of the reaction gas of reactor.Gas distributor can be normal using those skilled in the art
Used in rule, the present invention is repeated no more, and gas distributor is preferably provided with two.
According to the first aspect of the invention, the upper end of annular space 8 can connect for opening and with the fluid of air inlet pipe 2
Logical, the bottom of annular space 8 can be closed.
According to the first aspect of the invention, in order to prevent the bottom of housing 1 excessively heated and prevention center
Cylinder 4 and sleeve 9 are moved down, and can be set between the bottom of radial direction catalytic reaction zone and the bottom of housing 1
It is equipped with heat-barrier material area 12.Those skilled in the art institute can be placed with the heat-barrier material area 12 ripe
The heat-barrier materials such as single material or the heat insulating ball of a variety of composites, heat-insulated felt rug or the heat insulating belt known.
Second aspect of the present invention：A kind of methanation process is provided, the technique includes：A, coal gasification obtained
To the purified processing of synthesis gas and preheating after be divided into two strands, first burst of synthesis gas feeding main methanation of 1# is anti-
Device 19 is answered to carry out the main methanation reactions of 1#, reacted material is mixed with second strand of synthesis gas after cooling
The main methanators 20 of 2# are sent into after conjunction together and carry out the main methanation reactions of 2#, the first product is obtained；
B, by step a gained the first product sent into after cooling at least one supplement methanator enter
Row supplement methanation reaction, obtains the second product；C, by step b gained the second product through cooling
After carry out separating treatment, obtain methanation product；Wherein, the main methanators 19 of 1#, the main methane of 2#
Change what reactor 20 was provided with least one in supplement methanator by first aspect present invention
Methanator.Preferably, the quantity of the supplement methanator is 1-3 platforms.
According to the second aspect of the invention, can be by pot in order to control the reaction temperature of methanator
The main methanators 19 of stove feedwater (i.e. cooling medium) feeding 1#, the main and of methanator 20 of 2#
Carry out taking in heat, produced steam feeding drum in supplement methanator, the steam of generation passes through
Steam superheater 27 obtains super-pressure superheated steam, and the present invention preferably multiple methanators share one
Individual drum.
According to the second aspect of the invention, synthesis gas be it is well-known to those skilled in the art containing hydrogen,
The mixed gas of carbon monoxide and/or carbon dioxide, preferably M values are 2.85-3.5 synthesis gas；Institute
State M values for methanation synthesis gas institute hydrogen volume and carbon dioxide volume difference with contain one
The ratio of carbonoxide and carbon dioxide volume sum, i.e. M=(V (H2)-V(CO2))/(V(CO+CO2)), because
If carrying out complete, V (H for methanation reaction2)：V(CO2)=4:1, V (H2)：V (CO)=3:1, and
M values are 3 or so, it is meant that almost just react complete containing hydrocarbon and hydrogen.
According to the second aspect of the invention, the purified treatment can include those skilled in the art institute successively
Well known hydrolysis, desulfurization, deoxidation and denitration process.
According to the second aspect of the invention, the condition of the main methanation reactions of the 1# is：Reaction temperature is
300-700 DEG C, reaction pressure is 1.0-8.5 MPas, and volume space velocity is 2000-50000h-1；The 2# master
The condition of methanation reaction is：Reaction temperature is 300-700 DEG C, and reaction pressure is 1.0-8.5 MPas, body
Product air speed is 2000-50000h-1；It is described supplement methanation reaction condition be：Reaction temperature is
300-550 DEG C, reaction pressure is 1.0-4.5 MPas, and volume space velocity is 2000-50000h-1；First burst of conjunction
Volume ratio into gas and second strand of synthesis gas is 1:(1-3.5).
The present invention is further illustrated by embodiment below in conjunction with accompanying drawing, not therefore but the present invention
And it is any way limited.
Embodiment 1
As shown in figure 3, the reaction unit of the present embodiment is by the main methanators 19 of 1#, the main methane of 2#
Change reactor 20,1# supplements methanator 21,1# coolers 22,2# coolers 23, boiler to give
Water heater 24, product separator 25, drum 26, steam superheater 27 and the phase of 1# waste heat boilers 28
Even.The main methanators 19 of 1# are connected with the main methanators of 2# 20 using series-parallel mode.
Operating procedure is as follows：
1st, by H2/ CO volume ratios are 3.0 (M=3.0), and pressure is that 3.5MPa, temperature are 280 DEG C
Synthesis gas, is divided into two strands, and first strand enters the main methanators 19 of 1# and carry out the main methanation reactions of 1#,
Reaction temperature is 650 DEG C, and pressure is 3.48MPa, and volume space velocity is 9000h-1, reacted gas warp
Cross 1# waste heat boilers 28 to remove after partial heat, the main methanations of 2# are entered together with second strand of synthesis gas anti-
Device 20 is answered to carry out the main methanation reactions of 2#, reaction temperature is 645 DEG C, and pressure is 3.43MPa, volume
Air speed is 15000h-1, the volume ratio of first strand of synthesis gas and second strand of synthesis gas is 1:1.5, two main first
The structural parameters of alkylation reactors are identical；
2nd, the first product of the main methanators 19 of 1# and the main gained of methanator 20 of 2# passes through
After steam superheater 27 exchanges heat, temperature is reduced to 410 DEG C, and methanator 21 is supplemented subsequently into 1#,
Further convert unreacted synthesis gas in the first product；1# supplements the reaction temperature of methanator 21
Spend for 435 DEG C, pressure is 3.38MPa；
3rd, after 1# supplement methanators, the second product is cold through boiler water-suppling heater 24,2#
But after device 23 and 1# coolers 22 cool, the isolated methanation product after product separator 25；
4th, boiler feedwater is after the preheating of boiler water-suppling heater 24, into drum 26, divides seven strands, its
In with two bursts of forms from top respectively enter the main methanators 19 of 1#, the main methanators 20 of 2#,
1# supplements methanator 21, and remaining one enters 1# waste heat boilers 28, produces steam and all enters
Enter drum 26, three methanators share a drum 26；Water vapour in drum is through steam mistake
Reaction battery limit (BL) is sent out after hot device overheat.
The conversion ratio of carbon monoxide is 100% in the present embodiment, and the selectivity of methane is 97.5%, simultaneously
By-product 10.4MPa, 530 DEG C of super-pressure superheated steam.
As depicted in figs. 1 and 2, structure is as follows for 3 methanators that the present embodiment is used：
As depicted in figs. 1 and 2, methanator includes housing 1, air inlet pipe 2, the and of escape pipe 3
Radial direction catalytic reaction zone.The lower end of air inlet pipe 2 is provided with first gas distributor 10 and second gas point
Be provided between the bottom surface of cloth device 11, radial direction catalytic reaction zone and housing 1 by heat-insulated felt rug constitute it is heat-insulated
Material sections 12.Radial direction catalytic reaction zone is included in coaxial central tube 4 and 2 sleeves 9, central tube 4
The heart has central tube 5, and mass flow pathway 15, sleeve are formed between central tube 4 and sleeve 9, between sleeve 9
9 and the side wall formation annular space 8 of housing 1.Central tube 4 and sleeve 9 are coated active by some inner surfaces
The micro- reaction channel 13 of radial direction of catalyst is constituted.The micro- reaction channel 13 of radial direction that the present embodiment is used for
Conical pipe as shown in fig. 13 that, taper pipe internal surface supported active metals NiO amount is 20g/m2, it is whole
It (is clear that individual radial direction catalytic reaction zone inner conical caliber is 62800 to the quantity of micro- reaction channel 13
It has been shown that, is not entirely shown).
The height of central tube is 1500mm, and housing inner diameter is 1000mm, a diameter of 200mm of central tube,
Annular space spacing is 35mm, and two sleeves are identical with the thickness of central tube (radial distance is identical), at this
Embodiment mass flow pathway width is 25mm, and the micro- reaction channel length of conical pipe used is micro- for 105mm
Diameter 4mm at diameter 12mm at pathway reaction gas access, microchannel reacting product outlet, water conservancy diversion member
Part uses hemisphere (as shown in figure 17), and sphere is towards microchannel reaction gas inlet, its basal diameter
For 3mm, adjacent guide element spacing is 5mm, and each guiding subassembly is (real comprising 7 diversion members
Apply in example for the ease of observation, do not provide all), diversion member outer surface not load active component is led
Fluid element is fixed in reaction channel by fixing axle, and the cumulative volume of all conical pipes accounts for catalytic reaction unit
Volume ratio be 42.8%.
There are six interior heat collecting devices in the methanator that the present embodiment is used, wherein, two are arranged on
In central tube 4, four are arranged in sleeve 9.Two strands of cooling mediums are respectively from the 1# in the outside of housing 1
Cooling medium entrance and 2# cooling mediums entrance enter in housing 1, the 1# cooling mediums entrance and institute
2# cooling mediums entrance is stated respectively by three cooling medium pipelines with the central tube 4, the inwall of sleeve 9
The closing space 16 formed with the outer wall of the micro- reaction channel of the radial direction 13 is in fluid communication, and the closing is empty
Between pass through the cooling medium pipeline through heat-barrier material area 12 and 1# cooling mediums and export and 2# cooling mediums
Communication, methanator is sent out by cooling medium.
Embodiment 2
As shown in fig. 6, the difference for the flow and embodiment 1 that the present embodiment is used is the present embodiment
Supplemented in 1# and be provided with the He of 2# waste heat boilers 30 between methanator and boiler water-suppling heater 24
2# supplements methanator 29, while main methanation reaction and supplement methanator inner radial are urged
Change reaction zone also different from embodiment 1.
Reaction mass after 1# supplements methanator 21 passes through the removal portion of 2# waste heat boilers 30
Feeding 2# supplement methanators 29 proceed to supplement methanation reaction after point heat, and the of gained
After two products cool through boiler water-suppling heater 24,2# coolers 23 and 1# coolers 22 again, through production
Isolated methanation product after product separator 25；The conversion ratio of carbon monoxide is in the present embodiment
99.99%, the selectivity of methane is 98%, while by-product 10.4MPa, 530 DEG C of super-pressure overheat is steamed
Vapour.
The methanator used in the present embodiment only has central tube, without sleeve, such as Fig. 4, Fig. 5
It is shown.The height of central tube 8 is 1500mm, and housing inner diameter is 1000mm, and central tube is a diameter of
200mm, annular space spacing is 35mm, and the micro- reaction channel length of conical pipe used is micro- for 365mm
Diameter 4mm at diameter 10mm at pathway reaction gas access, microchannel reacting product outlet, water conservancy diversion member
Part uses cone (as shown in figure 21), and its basal diameter is 3mm, and length is 4mm, adjacent to lead
Fluid element spacing is 5mm, each guiding subassembly comprising 35 diversion members (in embodiment for the ease of
Observation, is not provided all), diversion member is fixed in reaction channel by fixing axle；Entirely radially urge
The quantity for changing the micro- reaction channel 10 of reaction zone inner conical pipe is 41800 (inwhole to clearly show that
Show), the ratio that the cumulative volume of all conical pipes accounts for the volume of catalytic reaction unit is 65.1%.
Have in the methanator that the present embodiment is used in two interior heat collecting devices, centrally disposed cylinder.
Two strands of cooling mediums enter from the 1# cooling mediums entrance and 2# cooling mediums entrance in the outside of housing 1 respectively
In housing 1,1# cooling mediums entrance is with 2# cooling mediums entrance respectively by a cooling medium pipeline with
The closing space 16 that the outer wall of the heart 4 inwalls of cylinder and micro- reaction channel 13 is formed is in fluid communication, the closing
Space 16 is exported by the cooling medium pipeline through heat-barrier material area 12 and 1# cooling mediums and 2# is cold
But media outlet is in fluid communication, and cooling medium is sent out into methanator.
Embodiment 3
As shown in figure 9, the flow of the use of the present embodiment is same as Example 1.Difference is this
The main methanator of use of embodiment is different with the interior heat collecting device inside supplement methanator, such as
Shown in Fig. 7, Fig. 8.
The conversion ratio of carbon monoxide is 100% in the present embodiment, and the selectivity of methane is 97%, while secondary
Produce 10.4MPa, 530 DEG C of super-pressure superheated steam.
The methanator that the methanator that the present embodiment is used is used with embodiment 1 is not
It is that the interior heat collecting device in the methanator that the present embodiment is used is arranged on two affluxs with part
It is in the mass flow pathway 15 and circular by being arranged between cooling medium entrance and media outlet in road 15
The cooling medium pipeline of central tube 4 and sleeve 9 is in fluid communication.Cooling of the cooling medium from the outside of housing 1
Medium inlet enters inside housing 1, is then divided into two strands, and one is configured circular in internal layer mass flow pathway
The cooling medium pipeline of central tube 4 cools to methanator, and another stock-traders' know-how is arranged on outer layer collection
The pipeline cylinder by a cooling medium pipeline coiling in runner cools to methanator.
Methanator compact conformation that the present invention is provided, active metal consumption are few；The methanation is anti-
When answering device progress methanation reaction, bed pressure drop is small, per volume of catalyst production intensity is big, reactant
Diffusion path is shorter, feed stock conversion is high, no gas bias current and short circuit phenomenon, and can remove reaction in time
Heat, it is to avoid superheat region occurs in catalyst, extends the service life of reactor, disclosure satisfy that existing coal
System substitutes the production process of natural gas.
The preferred embodiment of the present invention is described in detail above in association with accompanying drawing, still, the present invention is not limited
Detail in above-mentioned embodiment, can be to the present invention in the range of the technology design of the present invention
Technical scheme carry out a variety of simple variants, these simple variants belong to protection scope of the present invention.
In addition, various embodiments of the present invention can be combined randomly, as long as its
Without prejudice to the thought of the present invention, it should equally be considered as content disclosed in this invention.
Claims (10)
1. a kind of methanator, it is characterised in that the reactor includes cylindrical shape seal and pressure bearing shell
Body (1), the air inlet pipe (2) that enclosure interior is extend at the top of the housing (1), from the housing
(1) bottom extend into the escape pipe of enclosure interior (3), is arranged on the air inlet in the housing (1)
Manage the radial direction catalytic reaction zone below (2) above the escape pipe (3) and the radial direction is catalyzed instead
Answer the interior heat collecting device in area；
The radial direction catalytic reaction zone include central tube (4) and including or include be set in central tube
(4) at least one sleeve (9) outside；Central tube (4) has central tube (5), central tube (5)
It is in fluid communication with escape pipe (3)；Between the barrel of the sleeve (9) of central tube (4) and innermost layer with
And mass flow pathway (15) is formed between the barrel of adjacent sleeve (9)；Outside outermost sleeve (9)
Shape between wall or the outer wall of central tube (4) and the inwall of housing (1) during in the absence of sleeve (9)
Into there is annular space (8)；Central tube (4) and sleeve (9) are respectively provided with the micro- reaction of multiple radial directions being radially arranged
Only pass through inside and outside passage (13), and the cylinder of central tube (4) and inside and outside the cylinder of sleeve (9)
The micro- reaction channel (13) of radial direction is in fluid communication；Air inlet pipe (2) by annular space (8) below with
The microchannel reaction gas of the micro- reaction channel of radial direction (13) in central tube (4) or outermost layer sleeve (9)
Body entrance (6) is in fluid communication, the microchannel plate of the micro- reaction channel of radial direction (13) in central tube (4)
Product exit (7) is answered to be in fluid communication by central tube (5) and escape pipe (3)；
The guiding subassembly (14) of increase Hydrodynamic turbulence effect is provided with the micro- reaction channel of radial direction (13).
2. methanator according to claim 1, wherein, the top of the housing (1) has
At least one cooling medium entrance, the bottom of the housing (1) is exported with least one cooling medium,
The interior heat collecting device includes cooling medium pipeline；The central tube (4) and each sleeve (9) each have
The closing space (16) for the receiving micro- reaction channel (13) for thering is the inner and outer wall by respective cylinder to be formed,
The top of each closing space (16) passes through the cooling medium pipeline and the cooling medium entrance stream
Body is connected, and the bottom of each closing space (16) is situated between by the cooling medium pipeline with the cooling
Matter communication, and each closing space (16) and the air inlet pipe (2), central tube (5)
It is that fluid is not connected with escape pipe (3).
3. methanator according to claim 1, wherein, the top of the housing (1) has
At least one cooling medium entrance, the bottom of the housing (1) is exported with least one cooling medium,
The interior heat collecting device includes cooling medium pipeline；Lead between cooling medium entrance and the cooling medium outlet
Cross and be arranged in the mass flow pathway (15) and around the central tube (4) and/or the sleeve (9)
Cooling medium pipeline is in fluid communication.
4. methanator according to claim 1, wherein, the guiding subassembly (14) includes
The fixing axle (17) that is fixedly connected with the inwall of the micro- reaction channel of the radial direction (13) and it is connected on described
Diversion member (18) in fixing axle (17), the direction radial direction of the diversion member (18) is micro-
One end of reaction channel (13) airintake direction is convex.
5. methanator according to claim 4, wherein, the diversion member (18) is choosing
From at least one of cone, circular conical surface, hemisphere, hemisphere face, spheroid and sphere；
The cone, circular conical surface basal diameter between microchannel reacting product outlet (7) diameter
Between the diameter of microchannel reaction gas inlet (6)；The hemisphere, hemisphere face, sphere, ball
Diameter and microchannel reaction gas inlet of the spherical diameter of body between microchannel reacting product outlet (7)
(6) between diameter；The spacing of the two neighboring diversion member (18) is not less than water conservancy diversion member
The height of part (18).
6. methanator according to claim 4, wherein, each guiding subassembly (14)
Including the 3-100 diversion members (18).
7. methanator according to claim 4, wherein, the micro- reaction channel of radial direction (13)
Inner surface and/or the outer surface of diversion member (18) be loaded with catalytic active component respectively；
The diameter of the micro- reaction channel of radial direction (13) is between 2-50 millimeters；The micro- reaction of the radial direction
The diameter of passage (13) is from microchannel reaction gas inlet (6) to microchannel reacting product outlet (7)
Direction be gradually reduced；The diameter of the microchannel reaction gas inlet (6) should with the microchannel plate
The ratio of the diameter of product exit (7) is (1.1-20)：1；The micro- reaction channel of radial direction (13) is
One of which in conical pipe, flaring pipe, Y tube and laddertron；The micro- reaction of radial direction is logical
The cumulative volume of the inner space in road (13) is the 30%-80% of the volume of the radial direction catalytic reaction zone.
8. a kind of methanation process, the technique includes：
It is divided into two strands, first burst of synthesis after the purified processing of a, the synthesis gas for obtaining coal gasification and preheating
Pneumatic transmission enters the main methanators of 1# (19) and carries out the main methanation reactions of 1#, and reacted material passes through
The main methanators of 2# (20) are sent into together with after second burst of synthesis gas mixing carry out 2# master after cooling
Methanation reaction, obtains the first product；
B, by step a gained the first product sent into after cooling at least one supplement methanation reaction
Device carries out supplement methanation reaction, obtains the second product；
C, by step b gained the second product separating treatment is carried out after cooling, obtain methanation production
Thing；
Wherein, the main methanators of the 1# (19), the main methanators of 2# (20) and supplement
At least one in methanator is anti-for the methanation in claim 1-7 described in any one
Answer device.
9. methanation process according to claim 8, wherein, the warp of drum (26) will be come from
The boiler feedwater for crossing boiler water-suppling heater (24) preheating is added to reaction by the cooling medium entrance
Carry out taking heat in device, take the steam obtained after heat to send into drum (26).
10. methanation process according to claim 8, wherein, the synthesis gas include hydrogen and
Carbon monoxide and/or carbon dioxide, the M values of the synthesis gas are 2.85-3.5；The M values are described
The difference of the volume of synthesis gas institute hydrogen and the volume of carbon dioxide is with carbon monoxide and carbon dioxide volume
The ratio of sum；
The condition of the main methanation reactions of 1# is：Reaction temperature is 300-700 DEG C, and reaction pressure is
1.0-8.5 MPa, volume space velocity is 2000-50000h-1；The condition of the main methanation reactions of 2# is：
Reaction temperature is 300-700 DEG C, and reaction pressure is 1.0-8.5 MPas, and volume space velocity is 2000-50000h-1；
It is described supplement methanation reaction condition be：Reaction temperature is 300-550 DEG C, and reaction pressure is 1.0-4.5
MPa, volume space velocity is 2000-50000h-1；The volume ratio of first strand of synthesis gas and second strand of synthesis gas is
1:(1-3.5)。
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| CN108722321A (en) * | 2018-08-23 | 2018-11-02 | 浙江工业大学上虞研究院有限公司 | A kind of micro passage reaction |
| CN109045947A (en) * | 2018-09-03 | 2018-12-21 | 青岛科技大学 | A kind of fluidized bed cluster reactor |
| CN109499262A (en) * | 2018-12-14 | 2019-03-22 | 青岛科技大学 | A kind of novel longitudinal parallel bed adsorption device |
| CN110170281A (en) * | 2019-05-06 | 2019-08-27 | 新奥科技发展有限公司 | A kind of reactor |
| CN110802228A (en) * | 2019-10-24 | 2020-02-18 | 中国科学院力学研究所 | 3D printing micro-channel reactor for preparing natural gas from coal gas and printing process thereof |
| CN110803677A (en) * | 2019-10-24 | 2020-02-18 | 中石化宁波工程有限公司 | Double-steam-drum isothermal transformation hydrogen production method and isothermal transformation furnace |
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| CN108722321A (en) * | 2018-08-23 | 2018-11-02 | 浙江工业大学上虞研究院有限公司 | A kind of micro passage reaction |
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| CN110802228A (en) * | 2019-10-24 | 2020-02-18 | 中国科学院力学研究所 | 3D printing micro-channel reactor for preparing natural gas from coal gas and printing process thereof |
| CN110803677A (en) * | 2019-10-24 | 2020-02-18 | 中石化宁波工程有限公司 | Double-steam-drum isothermal transformation hydrogen production method and isothermal transformation furnace |
| CN110803677B (en) * | 2019-10-24 | 2023-03-14 | 中石化宁波工程有限公司 | Double-steam-drum isothermal transformation hydrogen production method and isothermal transformation furnace |
| CN114685234A (en) * | 2020-12-31 | 2022-07-01 | 上海昶法新材料有限公司 | System and method for producing internal olefin |
| CN113967448A (en) * | 2021-10-28 | 2022-01-25 | 中国石油化工股份有限公司 | Internal circulation catalytic wet oxidation reactor and water treatment system |
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