CN202337769U - Partially methanated water gas shift system - Google Patents
Partially methanated water gas shift system Download PDFInfo
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- CN202337769U CN202337769U CN2011204244613U CN201120424461U CN202337769U CN 202337769 U CN202337769 U CN 202337769U CN 2011204244613 U CN2011204244613 U CN 2011204244613U CN 201120424461 U CN201120424461 U CN 201120424461U CN 202337769 U CN202337769 U CN 202337769U
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 78
- 239000007789 gas Substances 0.000 claims abstract description 167
- 239000012495 reaction gas Substances 0.000 claims abstract description 39
- 238000006243 chemical reaction Methods 0.000 claims description 177
- 229910052799 carbon Inorganic materials 0.000 claims description 99
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 93
- 238000000034 method Methods 0.000 claims description 42
- 239000012530 fluid Substances 0.000 claims description 12
- 238000004891 communication Methods 0.000 claims description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 5
- 229910002091 carbon monoxide Inorganic materials 0.000 abstract description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 29
- 230000001105 regulatory effect Effects 0.000 description 8
- 238000011144 upstream manufacturing Methods 0.000 description 8
- 238000010237 hybrid technique Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 239000003345 natural gas Substances 0.000 description 5
- 239000003245 coal Substances 0.000 description 4
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 238000002309 gasification Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 2
- 230000002860 competitive effect Effects 0.000 description 2
- 235000009508 confectionery Nutrition 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 210000000952 spleen Anatomy 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 238000005987 sulfurization reaction Methods 0.000 description 1
- 230000003407 synthetizing effect Effects 0.000 description 1
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Abstract
The utility model relates to a partially methanated water gas shift system. The system comprises (A) a general water gas inlet (110), (B) a carbon monoxide shift section (100) which comprises (B1) a carbon monoxide shift reactor (101), (B2) first water gas inlet pipelines (120, 140) and (B3) shift reaction gas outlet pipelines (160, 180), (C) a methanation section (200) which comprises (C1) a methanation reactor (201), (C2) second water gas inlet pipelines (130, 150) and (C3) methanation reaction gas outlet pipelines (170, 190), wherein the carbon monoxide shift section (100) and the methanation section (200) are connected in parallel. According to the system, the general investment and operation cost of the coal-to-synthetic natural gas can be reduced.
Description
Technical field
The utility model relates to a kind of part methanation water-gas shift system.
Background technology
Synthetic natural gas (SNG) is a kind of clean fuel, can utilize existing pipeline and facility to supply with, widely instead of natural gas.Substitute natural gas prepares project and just starts in big area, but the anti-sulphur part changing device that supporting carbon monoxide conversion device still adopts in the methanol synthetizing technology to be adopted.Though this flow process can satisfy the demand of present technology, this utility model can better be suitable for the substitute natural gas project.
The method of anti-sulphur part conversion is usually directed to the transformationreation of carbon monoxide and water vapour.Through transformationreation, hydrogen-carbon ratio is adjusted to 2.05-2.15.
Basically, the transformationreation process comprises following reaction, is the equal-volume reaction:
CO+H
2O→CO
2+H
2
The methanation reaction process comprises following reaction,
CO+3H
2→CH
4+H
2O。
A common focus of existing technology is exactly that anti-sulfuration conversion is merely able to regulate hydrogen-carbon ratio, can not have the methanation function concurrently.Because through behind the methanation reaction, gas volume reduces.Do not have the carbon monodixe conversion technology of methanation, the gas volume of seeing off is huge, and is bigger for the dimensional requirement of follow-up pipeline and equipment, increased construction cost.Compressor power consumption for methanation workshop section also is bigger simultaneously, has increased running cost.
Above defective will influence the cost of methanation device, and therefore influenced SNG with the competitive power of petrochemical industry Sweet natural gas.
The utility model content
The utility model technical problem to be solved is overall investment of coal system synthetic natural gas and the high problem of running cost.
The utility model relates to a kind of part methanation water-gas shift system, comprising:
(A) total water-gas inlet;
(D) hybrid reaction gas outlet;
(B) carbon monodixe conversion section comprises:
(B1) carbon monodixe conversion reactor drum;
(B2) the first water-gas inlet duct is with total water-gas inlet and carbon monodixe conversion reactor fluid UNICOM;
With
(B3) transformationreation gas outlet conduit is with carbon monodixe conversion reactor drum and hybrid reaction gas outlet fluid communication;
(C) methanation section comprises:
(C1) methanator,
(C2) the second water-gas inlet duct is with total water-gas inlet and methanator fluid communication; With
(C3) methanation reaction gas outlet conduit is with methanator and hybrid reaction gas outlet fluid communication;
Wherein, carbon monodixe conversion section and methanation section are parallel connection.
Preferably, carbon monodixe conversion reactor drum and/or methanator are adiabatic reactor.
Preferably, carbon monodixe conversion reactor drum and/or methanator are axial-flow reactor or diameter of axle formula reactor drum.
Preferably, the carbon monodixe conversion section further comprises:
Conversion road first interchanger is arranged between total water-gas inlet and the carbon monodixe conversion reactor drum; With
Conversion road the 3rd interchanger is arranged between the outlet of carbon monodixe conversion reactor drum and hybrid reaction gas.
Preferably, the carbon monodixe conversion section further comprises:
Conversion road first water separator is arranged between conversion road first interchanger and the carbon monodixe conversion reactor drum; With
Conversion road second water separator is arranged between the outlet of conversion road the 3rd interchanger and hybrid reaction gas.
Preferably, the carbon monodixe conversion section further comprises:
Conversion road second interchanger; Be arranged on the downstream line of conversion road first water separator and the outlet conduit intersection of carbon monodixe conversion reactor drum, make said first water-gas and the outlet process gas heat exchange of said carbon monodixe conversion reactor drum in the downstream line of said conversion road first water separator.
Preferably, the methanation section further comprises:
Methanation road first interchanger is arranged between total water-gas inlet and the methanator; With
Methanation road the 3rd interchanger is arranged between the outlet of methanator and hybrid reaction gas.
Preferably, the methanation section further comprises:
Methanation road first water separator is arranged between methanation road first interchanger and the methanator; With
Methanation road second water separator is arranged between the outlet of methanation road the 3rd interchanger and hybrid reaction gas.
Methanation road second interchanger; Be arranged on the downstream line of methanation road first water separator and the outlet conduit intersection of methanator, make second water-gas and the outlet process gas heat exchange of said methanator in the downstream line of said methanation road first water separator.
Preferably, said system further comprises:
Regulator is arranged on the transformationreation gas outlet conduit and/or on the methanation reaction gas outlet conduit.
Adopt this system, overall investment of coal system synthetic natural gas and running cost are reduced.
Description of drawings
Fig. 1 is the artwork of a kind of preferred implementation of the utility model.
Embodiment
In the utility model, under the situation of not contradiction or conflict, all embodiment, embodiment and the characteristic of the utility model can make up each other.
In the utility model, all units, parts etc. both can be purchased, also can be according to the disclosed content self-control of the utility model.
In the utility model, for the emphasis of outstanding the utility model, the omission that some conventional operations and unit, parts are carried out, or only do simple description.
In the utility model; Term " carbon monodixe conversion section ", " carbon monodixe conversion workshop section " and " carbon monodixe conversion road " can exchange use; Be meant the workshop section that carries out carbon monodixe conversion, and can abbreviate " conversion section ", " conversion section " or " conversion road " as.
In the utility model, term " methanation section ", " methanation workshop section " and " methanation road " can exchange use, are meant the workshop section that carries out methanation.
And being advanced to conversion section with the part methanation reaction, the utility model carries out; Because gas volume obviously reduces behind the methanation reaction; So can effectively reduce the volume of variation workshop section process gas, can reduce the size of follow-up workshop section pipeline and equipment, reducing the construction costs.Simultaneously owing to the process gas volume that has reduced to get into methanation workshop section, so can reduce the watt consumption of methanation workshop section compressor.So, also reduced the production run cost.
The root problem that the utility model will solve provides a kind of method of more cost-effective and competition, and this method can either can also be dwindled the volume of delivering gas through methanation in presence of sulfur through conversion adjusting hydrogen-carbon ratio.More specifically, the utility model is intended to methanation reaction is carried out in advance, reduces the volume of the conversion gas that changing device, reduces the size of follow-up pipeline, equipment, reduces overall investment.
The basic thought of the utility model is that methanation reaction is advanced to conversion section and realizes regulating the hydrogen-carbon ratio function.Thereby; Address the above problem through a kind of part methanation water-gas shift method; Said method comprises the steps: that the water-gas that gasification installation comes is divided into two-way to be passed into respectively in two adiabatic reactors arranged side by side and to react, so that carbon monodixe conversion and methanation are separately carried out, is characterized in that; Described process can the better controlled methanation and the carrying out of carbon monodixe conversion reaction, can realize effective adjusting of hydrogen-carbon ratio again.
In preferred embodiment, water-gas is divided into two strands of water-gas streams, and per share described water-gas flow point is not input in conversion road and the methanation road.More preferably, per share water-gas stream accounts for the 20%-80% of the whole water-gas of available.
The typical arrangement be, in two reactor drums arranged side by side, tells 73% water-gas to the conversion road, and 27% water-gas is to the methanation road.The allocation proportion of water-gas depends on the quality (methane content and hydrogen-carbon ratio) of gas of type and the requirement of catalyzer.
Another aspect according to the utility model; The distribution of gas is to carry out according to following mode: install a flowrate control valve additional at carbon monodixe conversion gas and methane gasification meet; This valve both can be installed in the conversion road also can be installed in the methanation road, and this valve main purpose is the distribution of control two-way gas.
Because the utility model reduces through can effectively conversion gas being amassed after the methanation, can reduce the size of follow-up workshop section transport pipe and equipment, effectively reduces cost of investment.
Another advantage is because the utility model is advanced to conversion section with the part methanation and carries out, can the heat properly distributed be reduced the load of methanation workshop section recovery of heat.Can also improve simultaneously the quality and the grade of conversion section byproduct steam.
Be noted that recovery of heat can not receive the influence of the utility model, i.e. the production of byproduct steam is identical with art methods.
All above-mentioned advantages make the project overall investment of coal system synthetic natural gas (SNG) and running cost reduce, and are more obvious with the competitive edge of petrochemical industry Sweet natural gas.The utility model is specially adapted to prepare SNG through biomass or gasification.
The feature and advantage of the utility model will be more obvious through the description of following preferred exemplary and non-limiting specific embodiment and according to accompanying drawing.
An aspect of the utility model relates to a kind of part methanation water-gas shift system, comprising:
(A) total water-gas inlet;
(D) hybrid reaction gas outlet;
(B) carbon monodixe conversion section comprises:
(B1) carbon monodixe conversion reactor drum;
(B2) the first water-gas inlet duct, with total water-gas inlet and carbon monodixe conversion reactor fluid UNICOM,
(B3) transformationreation gas outlet conduit is with carbon monodixe conversion reactor drum and hybrid reaction gas outlet fluid communication;
(C) methanation section comprises:
(C1) methanator,
(C2) the second water-gas inlet duct, with total water-gas inlet and methanator fluid communication,
(C3) methanation reaction gas outlet conduit is with methanator and hybrid reaction gas outlet fluid communication;
Wherein, carbon monodixe conversion section and methanation section are parallel connection.
Preferably, (B1) the carbon monodixe conversion reactor drum and/or (C1) methanator be adiabatic reactor.
Preferably, (B1) the carbon monodixe conversion reactor drum and/or (C1) methanator be axial-flow reactor or diameter of axle formula reactor drum.
Preferably, the carbon monodixe conversion section further comprises:
Conversion road first interchanger is arranged between total water-gas inlet and the carbon monodixe conversion reactor drum; And/or
Conversion road the 3rd interchanger is arranged between the outlet of carbon monodixe conversion reactor drum and hybrid reaction gas.
Preferably, the carbon monodixe conversion section further comprises:
Conversion road first water separator is arranged between conversion road first interchanger and the carbon monodixe conversion reactor drum; And/or
Conversion road second water separator is arranged between the outlet of conversion road the 3rd interchanger and hybrid reaction gas.
Preferably, the carbon monodixe conversion section further comprises:
Conversion road second interchanger is arranged on the downstream line of conversion road first water separator and the outlet conduit intersection of carbon monodixe conversion reactor drum, makes the outlet process gas heat exchange of first water-gas and carbon monodixe conversion reactor drum.
Preferably, the methanation section further comprises:
Methanation road first interchanger is arranged between total water-gas inlet and the methanator; And/or
Methanation road the 3rd interchanger is arranged between the outlet of methanator and hybrid reaction gas.
Preferably, the methanation section further comprises:
Methanation road first water separator is arranged between methanation road first interchanger and the methanator; And/or
Methanation road second water separator is arranged between the outlet of methanation road the 3rd interchanger and hybrid reaction gas.
Preferably, the methanation section further comprises:
Methanation road second interchanger is arranged on the downstream line of methanation road first water separator and the outlet conduit intersection of methanator, makes the outlet process gas heat exchange of second water-gas and the methanator in the first water separator downstream, methanation road.
Preferably, total water-gas inlet is connected to coal gasification apparatus.
The utility model relate to a kind of part methanation water-gas shift method on the other hand, may further comprise the steps:
Total water-gas is split into first water-gas and second water-gas;
First water-gas feeds the carbon monodixe conversion reactor drum, carries out the carbon monodixe conversion reaction;
Second water-gas feeds methanator, carries out methanation reaction;
Wherein, carbon monodixe conversion reactor drum and methanator are parallel connection.
The utility model relate to a kind of part methanation water-gas shift method on the other hand, may further comprise the steps:
Total water-gas is split into first water-gas and second water-gas;
First water-gas feeds the carbon monodixe conversion section, and the carbon monodixe conversion section comprises the carbon monodixe conversion reactor drum, carries out the carbon monodixe conversion reaction therein;
Second water-gas feeds the methanation section, and the methanation section comprises methanator, carries out methanation reaction therein;
Wherein, carbon monodixe conversion section and methanation section are parallel connection.
Preferably, second process gas behind reacted first process gas of carbon monodixe conversion and the methanation reaction is mixed, obtain hybrid technique gas.
Preferably, first water-gas account for total water-gas total volumetric flow rate 60%～80%, preferred 60%～80%.
Preferably, first water-gas is adjusted to the by volume water to steam ratio and is (1～2): 1, preferred (1.1～1.2): 1.
Preferably, second water-gas is adjusted to the by volume water to steam ratio and is (0.4～0.6): 1, and preferred 0.5: 1.
Preferably, carbon monodixe conversion reactor drum and/or methanator are adiabatic reactor.
Preferably, carbon monodixe conversion reactor drum and/or methanator are axial-flow reactor or diameter of axle formula reactor drum.
Preferably, hybrid technique gas is passed into another methanation device.
Methanation comprises following reaction:
CO+3H2→CH4+H2O。
The system of 1 pair of the utility model is described in detail with reference to the accompanying drawings.
As shown in Figure 1, the part methanation water-gas shift system of the utility model comprises the carbon monodixe conversion section 100 and methanation section 200 of parallel connection.As shown in Figure 1, part methanation water-gas shift system comprises total water-gas inlet 110, carbon monodixe conversion section 100, methanation section 200 and hybrid reaction gas outlet 202.Carbon monodixe conversion section 100 is parallel connection with methanation section 200.
As shown in Figure 1, carbon monodixe conversion section 100 comprises carbon monodixe conversion reactor drum 101, the first water-gas inlet duct 120,140 and transformationreation gas outlet conduit 160,180.
Carbon monodixe conversion reactor drum 101 can be an adiabatic reactor.Carbon monodixe conversion reactor drum 101 itself is known, for example, can be axial-flow reactor or diameter of axle formula reactor drum.Have suitable catalyzer in the carbon monodixe conversion reactor drum 101, be used for catalysis carbon monodixe conversion reaction.
Provided upstream at carbon monodixe conversion reactor drum 101 is equipped with conversion road first water separator (condensate separator) 121.Comprise the upstream line 120 of (or being divided into) conversion road first water separator 121 and the downstream line 140 of conversion road first water separator 121 with respect to conversion road first water separator, 121, the first water-gas inlet ducts 120,140.Thereby correspondingly, accommodate first water-gas 14 that has separated water of condensation in the downstream line 140 of conversion road first water separator 121.On the upstream line 120 of conversion road first water separator 121, be provided with conversion road first interchanger (heat exchanger of hot water/steam-pipe) 111.In other words, conversion road first interchanger 111 is arranged between total water-gas inlet 110 and conversion road first water separator 121.
Carbon monodixe conversion section 100 also comprises conversion road second interchanger 112; Be arranged on the downstream line 140 of conversion road first water separator 121 and outlet conduit 160 intersections of carbon monodixe conversion reactor drum 101, make outlet process gas 16 heat exchange of first water-gas 14 that separated water of condensation and carbon monodixe conversion reactor drum 101.First water-gas 14 with outlet process gas 16 heat exchange of carbon monodixe conversion reactor drum 101, obtains heat in second interchanger 112 of conversion road before getting into carbon monodixe conversion reactor drum 101, can guarantee certain superheating temperature.
Carbon monodixe conversion section 100 also comprises conversion road second water separator (condensate separator) 122, is arranged on the downstream of carbon monodixe conversion reactor drum 101.Similarly; With respect to conversion road second water separator 122, transformationreation gas outlet conduit 160,180 comprises the upstream line 160 (being the outlet conduit 160 of carbon monodixe conversion reactor drum 101) of (or being divided into) conversion road second water separator 122 and the downstream line 180 of conversion road second water separator 122.Carbon monodixe conversion section 100 also comprises conversion road, conversion road the 3rd interchanger 113, is arranged between conversion road second interchanger 112 and conversion road second water separator 122.
As shown in Figure 1, methanation section 200 is similar with being provided with of carbon monodixe conversion section 100.Methanation section 200 comprises methanator 201, the second water-gas inlet duct 130,150 and methanation reaction gas outlet conduit 170,190.
The provided upstream of methanator 201 is equipped with methanation road first water separator (condensate separator) 221.Comprise the upstream line 130 of (or being divided into) methanation road first water separator 221 and the downstream line 150 of methanation road first water separator 221 with respect to methanation road first water separator, 221, the second water-gas inlet ducts 130,150.Thereby correspondingly, accommodate second water-gas 15 that has separated water of condensation in the downstream line 150 of methanation road first water separator 221.On the upstream line 130 of methanation road first water separator 221, be provided with methanation road first interchanger (heat exchanger of hot water/steam-pipe) 211.In other words, methanation road first interchanger 211 is arranged between total water-gas inlet 110 and methanation road first water separator 221.
The system of the utility model can also be provided with regulator (like regulating valve) 302, the allocation proportion that is used to regulate water-gas.For example, regulator 302 can be arranged on transformationreation gas outlet conduit and the methanation reaction gas outlet conduit meet upper reaches transformationreation gas outlet conduit 180 and/or on the methanation reaction gas outlet conduit 190.As shown in the figure, regulator (like regulating valve) 302 is arranged on the methanation reaction gas outlet conduit 190, on the downstream line 190 of namely for methane road second water separator 222.Certainly, shown in Figure 1 is exemplary, and regulator (like regulating valve) 302 also can be arranged on the transformationreation gas outlet conduit 180, promptly on the downstream line 180 of conversion road second water separator 122.Perhaps, be provided with regulator (like regulating valve) 302 on the transformationreation gas outlet conduit 180 He on the methanation reaction gas outlet conduit 190.
The method of 1 pair of the utility model is described in detail with reference to the accompanying drawings.
As shown in Figure 1, total water-gas 11 feeds through total water-gas inlet 110, splits into first water-gas 12 and second water-gas 13.First water-gas 12 gets into carbon monodixe conversion section 100; Second water-gas 13 gets into methanation section 200.
Preferably, first water-gas 12 accounts for the 20%-80% of the total volumetric flow rate of total water-gas 11, preferred 60%～80%.
First water-gas 12 and second water-gas 13 obtain second process gas 19 behind reacted first process gas 18 of carbon monodixe conversion and the methanation reaction respectively after carbon monodixe conversion section 100 and methanation section 200 react.First process gas 18 and second process gas 19 are converged (mixing) and are obtained hybrid technique gas 20.Hybrid technique gas 20 is passed into another methanation device (not shown) of downstream through hybrid reaction gas outlet 202.
For the carrying out that reacts in the better controlling reactor, first water-gas 12 is regulated the water to steam ratio rears through conversion road first interchanger (waste heat boiler) 111 and conversion road first water separator 121 and is got into carbon monodixe conversion reactor drums 101.Preferably, first water-gas is adjusted to water to steam ratio and is (1～2): 1, most preferably (1.1～1.2): 1.
In order to guarantee certain superheating temperature, first water-gas 14 with outlet process gas 16 heat exchange of carbon monodixe conversion reactor drum 101, obtains heat in second interchanger 112 of conversion road before getting into carbon monodixe conversion reactor drum 101.Preferably, the temperature of the inlet gas of carbon monodixe conversion reactor drum 101 (first water-gas) 14 is 240-300 ℃.Preferably, the temperature of the exit gas of carbon monodixe conversion reactor drum 101 (first process gas or transformationreation gas) 16 is about 400-600 ℃.
Through first process gas (transformationreation gas) 16 after the transformationreation; Temperature very high (for example being 420 ℃); Cooling in conversion road second interchanger 112, conversion road the 3rd interchanger 113; And, obtain the first cold process gas (transformationreation gas) 18 through behind conversion road second water separator (condensate separator) the 122 separating and condensing liquid.
For the carrying out that reacts in the better controlling reactor, second water-gas 13 is regulated the water to steam ratio rears through methanation road first interchanger (waste heat boiler) 211 and methanation road first water separator 221 and is got into methanators 201.Preferably, second water-gas is adjusted to water to steam ratio (volume ratio) and is (0.4～0.6): 1, and most preferably 0.5: 1.
In order to guarantee certain superheating temperature, second water-gas 15 with outlet process gas 17 heat exchange of methanator 201, obtains heat in second interchanger 212 of methanation road before getting into methanator 201.
Through second process gas (methanation reaction gas) 17 behind the methanation reaction; For example be 600 ℃; Cooling in methanation road second interchanger 212, methanation road the 3rd interchanger 213, and, obtain the second cold process gas (methanation reaction gas) 19 through behind second water separator, the 222 separating and condensing liquid of methanation road.
Refrigerative first process gas 18 is mixed with refrigerative second process gas 19, obtains hybrid technique gas 20.Hybrid technique gas 20 can be passed into another methanation device of downstream (another methanation workshop section), carries out further methanation reaction.
Reactor drum 101,201 itself is known, and for example, the axial or diameter of axle that has suitable catalyzer is to flow reactor, and gas is at about 56 crust normal atmosphere, and the inlet gas temperature is moved down for 240-300 ℃ and the about 400-600 of temperature out ℃.Heat exchanger 112 and 212 receives hot gas respectively from reactor drum 101 and 201, and can be used as the high pressure steam boiler use, or as required, water preheat or steam superheating function is provided.The heat exchanger 111,112,113,211,212,213 of hot water/steam-pipe is as shown in Figure 1.
As shown in Figure 1, water-gas flows 11 dispensed in parallel in reactor drum 101 and 201.In order better to control the carrying out that reacts in two reactor drums, before the entering reactor drum 101 and 201, water-gas need be regulated the water to steam ratio rear through waste heat boiler and separator and get into reactor drum.The molar flow of preferred each air- flow 12,13 is 40-60% of total water-gas 11.
The utility model can be explained by following embodiment, but the utility model is not limited to these embodiment.
Embodiment
Embodiment 1
Adopt the flow process of the utility model Fig. 1.
Total water-gas inlet wet basis flow 789436Nm
3, butt flow 332098Nm
3 First process gas 18 account for total water-gas total volumetric flow rate 83%.It is 1.1: 1 (volume ratio) that first water-gas is adjusted to water to steam ratio.It is 0.5: 1 (volume ratio) that second water-gas is adjusted to water to steam ratio.
Hybrid reaction gas butt volumetric flow rate is 395329Nm
3
Comparative example 1
Adopt conventional flow process, do not carry out the part methanation, only carry out carbon monodixe conversion.Total water-gas inlet flow rate is identical with embodiment 1.The butt volumetric flow rate that the tradition conversion is seen off is 442394Nm
3
Can find out that by above data adopt the mode of the utility model, the butt volumetric flow rate of working off one's feeling vent one's spleen after the reaction is 395329Nm
3, the volumetric flow rate of seeing off is traditional 89%.
Certainly, the utility model also can have other embodiments, and the preferred implementation that the above is merely the utility model is not the protection domain that is used for limiting the utility model; Under the situation that does not deviate from the utility model spirit, those of ordinary skills are every to make various corresponding variations and modification according to the utility model content, all belongs to the protection domain of the claim of the utility model.
Claims (10)
1. a part methanation water-gas shift system is characterized in that, comprising:
(A) total water-gas inlet (110);
(D) hybrid reaction gas outlet (202);
(B) carbon monodixe conversion section (100) comprising:
(B1) carbon monodixe conversion reactor drum (101);
(B2) the first water-gas inlet duct (120,140) is with said total water-gas inlet (110) and said carbon monodixe conversion reactor drum (101) fluid communication; With
(B3) transformationreation gas outlet conduit (160,180) is with said carbon monodixe conversion reactor drum (101) and said hybrid reaction gas outlet (202) fluid communication;
(C) methanation section (200) comprising:
(C1) methanator (201),
(C2) the second water-gas inlet duct (130,150) is with said total water-gas inlet (110) and said methanator (201) fluid communication; With
(C3) methanation reaction gas outlet conduit (170,190) is with said methanator (201) and said hybrid reaction gas outlet (202) fluid communication;
Wherein, said carbon monodixe conversion section (100) and said methanation section (200) are parallel connection.
2. system according to claim 1, wherein, said carbon monodixe conversion reactor drum (101) and/or said methanator (201) are adiabatic reactor.
3. system according to claim 1, wherein, said carbon monodixe conversion reactor drum (101) and/or said methanator (201) are axial-flow reactor or diameter of axle formula reactor drum.
4. system according to claim 1, wherein, said carbon monodixe conversion section (100) further comprises:
Conversion road first interchanger (111) is arranged between said total water-gas inlet (110) and the said carbon monodixe conversion reactor drum (101); With
Conversion road the 3rd interchanger (113) is arranged between said carbon monodixe conversion reactor drum (101) and the said hybrid reaction gas outlet (202).
5. system according to claim 4, wherein, said carbon monodixe conversion section (100) further comprises:
Conversion road first water separator (121) is arranged between said conversion road first interchanger (111) and the said carbon monodixe conversion reactor drum (101); With
Conversion road second water separator (122) is arranged between said conversion road the 3rd interchanger (113) and the said hybrid reaction gas outlet (202).
6. system according to claim 5, wherein, carbon monodixe conversion section (100) further comprises:
Conversion road second interchanger (112); Be arranged on the downstream line (140) of said conversion road first water separator (121) and outlet conduit (160) intersection of said carbon monodixe conversion reactor drum (101), make outlet process gas (16) heat exchange of said first water-gas (14) and said carbon monodixe conversion reactor drum (101) in the downstream line (140) of said conversion road first water separator (121).
7. system according to claim 1, wherein, said methanation section (200) further comprises:
Methanation road first interchanger (211) is arranged between said total water-gas inlet (110) and the said methanator (201); With
Methanation road the 3rd interchanger (213) is arranged between said methanator (201) and the said hybrid reaction gas outlet (202).
8. system according to claim 7, wherein, said methanation section (200) further comprises:
Methanation road first water separator (221) is arranged between said methanation road first interchanger (211) and the said methanator (201); With
Methanation road second water separator (222) is arranged between said methanation road the 3rd interchanger (213) and the said hybrid reaction gas outlet (202).
9. system according to claim 8, wherein, said methanation section (200) further comprises:
Methanation road second interchanger (212); Be arranged on the downstream line (150) of said methanation road first water separator (121) and outlet conduit (170) intersection of said methanator (201), make outlet process gas (17) heat exchange of second water-gas (15) and said methanator (201) in the downstream line (150) of said methanation road first water separator (121).
10. system according to claim 1, wherein, said system further comprises:
Regulator (302) is arranged on the said transformationreation gas outlet conduit and/or on the said methanation reaction gas outlet conduit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011204244613U CN202337769U (en) | 2011-10-31 | 2011-10-31 | Partially methanated water gas shift system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011204244613U CN202337769U (en) | 2011-10-31 | 2011-10-31 | Partially methanated water gas shift system |
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| Publication Number | Publication Date |
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| CN202337769U true CN202337769U (en) | 2012-07-18 |
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| CN2011204244613U Expired - Lifetime CN202337769U (en) | 2011-10-31 | 2011-10-31 | Partially methanated water gas shift system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102433180A (en) * | 2011-10-31 | 2012-05-02 | 神华集团有限责任公司 | Partial methanation water gas conversion system and method |
| CN104591084A (en) * | 2014-12-29 | 2015-05-06 | 南京敦先化工科技有限公司 | Shallow carbon monoxide conversion method and system |
-
2011
- 2011-10-31 CN CN2011204244613U patent/CN202337769U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102433180A (en) * | 2011-10-31 | 2012-05-02 | 神华集团有限责任公司 | Partial methanation water gas conversion system and method |
| CN104591084A (en) * | 2014-12-29 | 2015-05-06 | 南京敦先化工科技有限公司 | Shallow carbon monoxide conversion method and system |
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