CN107090320A - Based on the synthesis gas fluid bed preparing natural gas by methanation device being dehydrated between level - Google Patents
Based on the synthesis gas fluid bed preparing natural gas by methanation device being dehydrated between level Download PDFInfo
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- CN107090320A CN107090320A CN201710455221.1A CN201710455221A CN107090320A CN 107090320 A CN107090320 A CN 107090320A CN 201710455221 A CN201710455221 A CN 201710455221A CN 107090320 A CN107090320 A CN 107090320A
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- 239000007789 gas Substances 0.000 title claims abstract description 89
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 59
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 24
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 24
- 239000012530 fluid Substances 0.000 title claims abstract description 22
- 239000003345 natural gas Substances 0.000 title claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000007788 liquid Substances 0.000 claims abstract description 23
- 239000007787 solid Substances 0.000 claims abstract description 21
- 239000002826 coolant Substances 0.000 claims abstract description 4
- 238000006243 chemical reaction Methods 0.000 claims description 53
- 239000003054 catalyst Substances 0.000 claims description 18
- 239000000498 cooling water Substances 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 3
- 238000000034 method Methods 0.000 description 18
- 239000000047 product Substances 0.000 description 15
- 239000003245 coal Substances 0.000 description 5
- 230000018044 dehydration Effects 0.000 description 5
- 238000006297 dehydration reaction Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 238000005804 alkylation reaction Methods 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 238000009413 insulation Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000002194 synthesizing effect Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 1
- 240000002853 Nelumbo nucifera Species 0.000 description 1
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000013341 scale-up Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- 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
-
- 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
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/106—Removal of contaminants of water
-
- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/08—Drying or removing water
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention is provided based on the synthesis gas fluid bed preparing natural gas by methanation device being dehydrated between level, the gas-solid separator gas vent of fluidized-bed reactor of the one-level with heat removing tube is connected by water cooler with gas-liquid eddy flow dehydrator entrance, and the gas vent of gas-liquid eddy flow dehydrator is connected with the gas distributor of two grades of fluidized-bed reactors with heat removing tube；The gas-solid separator gas vent of two grades of fluidized-bed reactors with heat removing tube is connected by water cooler with gas-liquid eddy flow dehydrator entrance, and the gas vent of gas-liquid eddy flow dehydrator is connected with the gas distributor of fluidized-bed reactor of the three-level with heat removing tube；Water cooler and fixed bed methanator entrance UNICOM of the gas-solid separator gas vent of fluidized-bed reactor of the three-level with heat removing tube by temperature adjustment, the outlet of fixed bed methanator is product gas outlet；The coolant outlet of water cooler is connected with the entrance of heat removing tube.
Description
1. technical field
The present invention is provided based on the synthesis gas fluid bed preparing natural gas by methanation device being dehydrated between level, belongs to coal chemical industry neck
Domain.
2. background technology
Coal obtains synthesis gas by gasification, and a kind of important way that natural gas is coal clean conversion is produced in synthesis gas methanation
Footpath is China's Optimization of Energy Structure and ensures a kind of important means of energy security, is that the one kind for alleviating local atmosphere pollution has
Effect means, and natural gas from coal has certain competitiveness, and this has all promoted flourishing for natural gas from coal industry.
Mainly include H in the unstripped gas of synthesis gas methanation reaction2、CO、CO2、CH4、H2O、N2With the gas such as Ar, in methane
The chemical reaction that may occur during change has 11 kinds, and wherein key reaction is CO methanation reactions, CO2Methanation reaction and CO
Transformationreation etc..
CO methanation reactions are CO+3H2=CH4+H2O, CO2Methanation reaction is CO2+4H2=CH4+2H2O, CO conversion are anti-
Answer position CO+H2O=H2+CO2, CO methanation reactions, CO2Methanation reaction is the positive reaction for promoting methane generation, CO transformationreations
Position CO+H2O=H2+CO2It is to suppress the negative reaction that methane is generated, removing generation water is conducive to during synthesis gas methanation reaction
Improve methanation conversion ratio and selectivity.Other CO methanation reactions and CO2Methanation reaction is strong exothermal reaction, usual feelings
Under condition, 74 DEG C of temperature rise can be produced by often converting 1% CO, often convert 1% CO260 DEG C of temperature rise can be produced, and reacts temperature
Degree is higher, and CO conversion ratios are lower, and the requirement to methanation catalyst is also higher.
Since being found from CO methanation reactions, methanation reaction is widely used in ammonia synthesizing industry, trace amounts of CO removing, fuel
Battery, part gas methanation and in terms of producing synthetic natural gas.Since 1940s, people successively develop a variety of
Methanation process, can be divided into insulation fix bed, isothermal fixed bed, fluid bed and liquid phase methanation several according to type of reactor
Technique.
In insulation fix bed methanation, the adiabatic temperature rise that methanation reaction directly occurs for synthesis gas is high, reactor
Outlet temperature is more than 900 DEG C, this heat-resisting quantity to reactor, waste heat boiler, steam superheater, the selection of pipeline and catalyst
Very high requirement can be proposed, and cracking reaction analysis carbon easily occurs for methane under high temperature, increases bed pressure drop and reduces catalyst
Life-span.For effectively control reactor temperature rise, realized typically by dilution unstripped gas, optional mode there are some processes
Gas is circulated at high proportion, some processes gas is circulated and increases a small amount of steam, addition some vapor etc., realizes the methane under decreasing temperature
Change reaction balance, synthetic natural gas is obtained eventually through multistage methanation reaction.Process gas circulates add compression energy at high proportion
Consumption and investment.
Fixed bed indirect heat exchange isothermal methanation reactor, is moved during hot cold pipe is embedded beds, and with these
Isothermal fixed bed methanation process is have developed based on warm methanator.Isothermal fixed bed methanator is by first
Alkylation reaction liberated heat can byproduct steam.But due to structure limitation, equipment enlarging is limited.
Compared with fixed bed reactors, mass transfer and heat transfer have greater advantage in fluidized-bed reactor, more
Be adapted to extensive strongly exothermic process, particularly fluid catalyst easily to remove, add and recycle, with reaction effect it is good,
The advantages of simple to operate and relatively low operating cost, be the optimum response device of synthesis gas full methanation.But some are also faced with to ask
Topic, is particularly engineered scale-up problem, and such as catalyst entrainment and loss are serious, reaction temperature is whard to control, device operating pressure
Low, reaction conversion ratio is relatively low, and catalyst change amount is larger to result in the need for cheap catalyst etc..
Slurry bed system methanation process is that the mixed gas entrained catalyst that generates in paste state bed reactor and liquid phase component are logical
Cross gas-liquid separator separates, gas-phase product produces synthetic natural gas by condensation, separation, liquid product with it is fresh in storage tank
Catalyst is mixed to join in slurry bed system methanator, and pre- heat effect is played to fresh catalyst.Slurry bed system methane chemical industry
Skill has good heat transfer property, easily realizes low-temperature operation, with higher CH4Selective and preferable flexibility, but due to
Process liquid is isolated, and CO conversion ratios are relatively low, and catalyst loss is larger.
Select suitable reactor and device, how controlling reaction temperature in the reasonable scope and makes full use of methanation anti-
It is to improve synthesis gas methanation process process competitiveness to answer heat, improve methanation conversion ratio and selectivity and reduce process energy consumption
Key point.
3. the content of the invention
The purpose of the present invention is exactly to provide and be based between level to overcome the shortcomings of existing synthesis gas methanation technology to exist
The synthesis gas fluid bed preparing natural gas by methanation device of dehydration, reduces taking for fluid bed heat removing tube hot negative by fractional order reaction
Lotus, improves the effecting reaction sectional area of fluid bed；Dehydration inhibits the negative reaction of methanation reaction between level, greatly improves methane
Change conversion ratio and selectivity；Remnants CO and H are solved finally by fixed bed methanator2Highly effective reaction, regulate and control product
Quality.
Technical scheme：
The purpose of the present invention is by taking by the methanation of synthesis gas fluid bed, fractional order reaction regulation and control and being dehydrated between heat, level
Conversion ratio and selectivity, heat removing tube the Integration ofTechnology such as independently disconnect to reduce energy consumption and the investment of preparing methane by synthetic gas device, really
The stable of neighbourhood administrative system alkylation unit covers with excellent operation.It is characterized in that the gas-solid separator of fluidized-bed reactor of the one-level with heat removing tube
Gas vent is connected by water cooler with gas-liquid eddy flow dehydrator entrance, and the gas vent of gas-liquid eddy flow dehydrator is carried with two grades
The gas distributor connection of the fluidized-bed reactor of heat removing tube；The gas-solid separator of two grades of fluidized-bed reactors with heat removing tube
Gas vent is connected by water cooler with gas-liquid eddy flow dehydrator entrance, and the gas vent of gas-liquid eddy flow dehydrator is carried with three-level
The gas distributor connection of the fluidized-bed reactor of heat removing tube；The gas-solid separator of fluidized-bed reactor of the three-level with heat removing tube
Water cooler and fixed bed methanator entrance UNICOM of the gas vent by temperature adjustment, the outlet of fixed bed methanator is
Product gas outlet；The coolant outlet of water cooler is connected with the entrance of heat removing tube.
Fluidized-bed reactor inner bottom part with heat removing tube is provided with gas distributor；Top is separated provided with gas solid separation
Device, the solid dipleg with flutter valve is extend into the middle part of the catalyst bed of material, and gas vent stretches out fluidized-bed reactor；Fluidized-bed reaction
Circumferentially be provided with equally distributed heat removing tube at the top of device, the cooling water inlet of every heat removing tube and high temperature saturation water out respectively with
Cold intake pipe is independently connected with drum by valve.
Heat removing tube is to enter to go out at the top of cooling water, endless tube at the top of the connection of interior bottom of the tube, the sleeve structure of top seal, central tube
High temperature saturation water.
The lower part outlet of gas-liquid eddy flow dehydrator carries two-stage lock hopper, and lock hopper lower end is respectively mounted lock hopper valve.
The reaction condition of fluidized-bed reactor with heat removing tube is 240-500 DEG C and 0.3-6.0Mpa, synthesis gas CO/H2
For 1:3.
The temperature of product gas is 30-150 DEG C, the water cooling that the third level passes through temperature adjustment cross-line valve after first and second grades of water coolers
The temperature of product gas is 250-400 DEG C after device.
Embodiment is described the features of the present invention by the present invention in detail.
4. brief description of the drawings
Accompanying drawing is process schematic representation of the invention.
The drawing of accompanying drawing sets bright as follows：
1st, one-level with the fluidized-bed reactor 2 of heat removing tube, gas distributor 3, gas-solid separator 4, water cooler 5,
Gas-liquid eddy flow dehydrator 6, lock hopper 7, lock hopper valve 8, heat removing tube 9, two grades of fluidized-bed reactors with heat removing tube, 10, three
Level with the fluidized-bed reactor 11 of heat removing tube, fixed bed reactors 12, stop valve 13, saturated vapor water bag 14, temperature adjustment across
The product gas outlet of line valve 15.
With reference to the accompanying drawings and examples come be described in detail the present invention process characteristic.
5. embodiment
Embodiment, gas-solid separator (3) gas vent of fluidized-bed reactor (1) of the one-level with heat removing tube passes through water cooling
Device (4) is connected with gas-liquid eddy flow dehydrator (5) entrance, and the gas vent of gas-liquid eddy flow dehydrator (5) and two grades carry heat removing tube
Fluidized-bed reactor (9) gas distributor (2) connection；The gas-solid point of two grades of fluidized-bed reactors (9) with heat removing tube
It is connected from device (3) gas vent by water cooler (4) with gas-liquid eddy flow dehydrator (5) entrance, the gas of gas-liquid eddy flow dehydrator (5)
Body is exported to be connected with the gas distributor (2) of fluidized-bed reactor (10) of the three-level with heat removing tube；Three-level carries heat removing tube
Water cooler (4) and fixed bed methanation reaction that gas-solid separator (3) gas vent of fluidized-bed reactor (10) passes through temperature adjustment
Device (11) entrance UNICOM, fixed bed methanator (11) outlet is product gas outlet；The coolant outlet of water cooler (4) with
The entrance connection of heat removing tube (8).
Fluidized-bed reactor inner bottom part with heat removing tube is provided with gas distributor (2)；Top is provided with gas solid separation point
From device (3), the solid dipleg with flutter valve is extend into the middle part of the catalyst bed of material, and gas vent stretches out fluidized-bed reactor；Fluidisation
Bed reactor head is circumferentially provided with equally distributed heat removing tube (8), the cooling water inlet of every heat removing tube (8) and high temperature saturation
Water out is independently connected with cold intake pipe and drum by valve respectively.
Heat removing tube (8) is to enter cooling water, endless tube top at the top of the connection of interior bottom of the tube, the sleeve structure of top seal, central tube
Portion goes out high temperature saturation water.
The lower part outlet of gas-liquid eddy flow dehydrator (5) carries two-stage lock hopper (6), and lock hopper lower end is respectively mounted lock hopper valve (7).
The reaction condition of fluidized-bed reactor with heat removing tube is 240-500 DEG C and 0.3-6.0Mpa, synthesis gas CO/H2
For 1:3.
First and second grades of water coolers (4) afterwards product gas temperature be 30-150 DEG C, the third level passes through temperature adjustment cross-line valve
(14) water cooler (4) afterwards product gas temperature be 250-400 DEG C.
Concrete operations are：CO/H after converting2For 1:3 decontaminating syngas sends into one-level band by gas distributor (2)
There are the fluidized-bed reactor (1) of heat removing tube, part CO and/H2With micro mist catalyst under 240-500 DEG C and 0.3-6.0Mpa, lead to
Cross heat removing tube (8) heat exchange and occur samming methanation reaction, generation methane and vapor, product gas is de- by gas-solid separator (3)
After catalyst, cooled down by water cooler (4), into gas-liquid eddy flow dehydrator (5)；Product gas is carried into two grades and taken after dehydration
The fluidized-bed reactor (9) of heat pipe, repeats said process；Product gas after second dehydration is again introduced into three-level and carries heat removing tube
After fluidized-bed reactor (10), CO and/H2With micro mist catalyst under 240-500 DEG C and 0.3-6.0Mpa, pass through heat removing tube (8)
Samming methanation reaction occurs for heat exchange, after product gas is by gas-solid separator (3) Removal of catalyst, passes through the tune of water cooler (4)
Warm cross-line valve (14) regulating and controlling temperature；In every grade of fluid bed methanation, cooling water is being entered after first passing through water cooler (4) heat exchange
Enter heat removing tube (8) heat exchange and produce mesohigh saturated vapor；Third-order reaction gas is directly entered methanation fixed bed reactors (11), adjusts
The product quality of synthetic natural gas is controlled, generation product gas sends into pipe network after being dehydrated by product gas outlet (15).
In addition, the technique can also be by increasing or decreasing the series that reaction is classified, the series being mainly dehydrated, to adapt to not
With the change for synthesizing its raw material composition.
It is provided by the present invention based on the synthesis gas fluid bed preparing natural gas by methanation device being dehydrated between level, it is anti-by classification
The thermic load that takes of fluid bed heat removing tube should be reduced, heat removing tube total sectional area is less than fluid bed sectional area 13%, it is ensured that fluidisation
Quality, improves fluid bed effecting reaction region；Dehydration inhibits the negative reaction of methanation reaction between level, and CO conversion ratios are more than
99%th, methanation is selectively more than 99%；Remnants CO and H are solved finally by fixed bed methanator2Highly effective reaction,
Natural gas methane content is more than 99.6%；Relatively existing fixed bed part circulation methanation industrialization process, energy-conservation 35% is saved
Investment 30%；Compared with fluid bed methanation experiment or pilot process, conversion ratio improves 15%, and selectivity improves 10%, classification
Reaction puies forward the design and processing that control takes calorific intensity to simplify fluidized-bed reactor, and single branch heat removing tube breaks down, and only need to cut off top
Portion's stop valve, does not influence production is stable to cover with excellent operation.
Claims (6)
1. based on the synthesis gas fluid bed preparing natural gas by methanation device being dehydrated between level, its technical characteristic is that one-level carries heat removing tube
The gas-solid separator gas vent of fluidized-bed reactor be connected by water cooler with gas-liquid eddy flow dehydrator entrance, gas-liquid eddy flow
The gas vent of dehydrator is connected with the gas distributor of two grades of fluidized-bed reactors with heat removing tube；Two grades carry heat removing tube
The gas-solid separator gas vent of fluidized-bed reactor be connected by water cooler with gas-liquid eddy flow dehydrator entrance, gas-liquid eddy flow
The gas vent of dehydrator is connected with the gas distributor of fluidized-bed reactor of the three-level with heat removing tube；Three-level carries heat removing tube
The gas-solid separator gas vent of fluidized-bed reactor joined by the water cooler of temperature adjustment with fixed bed methanator entrance
Logical, the outlet of fixed bed methanator is product gas outlet；The coolant outlet of water cooler is connected with the entrance of heat removing tube.
2. it is according to claim 1 based on the synthesis gas fluid bed preparing natural gas by methanation device being dehydrated between level, its feature
It is that the fluidized-bed reactor inner bottom part with heat removing tube is provided with gas distributor；Top is provided with gas solid separation separator, band
The solid dipleg for having flutter valve is extend into the middle part of the catalyst bed of material, and gas vent stretches out fluidized-bed reactor；Fluidized-bed reactor top
Portion is circumferentially provided with equally distributed heat removing tube, and the cooling water inlet of every heat removing tube and high temperature saturation water out take with cold respectively
Water pipe is independently connected with drum by valve.
3. it is according to claim 1 based on the synthesis gas fluid bed preparing natural gas by methanation device being dehydrated between level, its feature
It is to enter at the top of cooling water, endless tube to go out high temperature at the top of the connection of interior bottom of the tube, the sleeve structure of top seal, central tube to be heat removing tube
Saturation water.
4. it is according to claim 1 based on the synthesis gas fluid bed preparing natural gas by methanation device being dehydrated between level, its feature
It is that the lower part outlet of gas-liquid eddy flow dehydrator carries two-stage lock hopper, lock hopper lower end is respectively mounted lock hopper valve.
5. it is according to claim 1 based on the synthesis gas fluid bed preparing natural gas by methanation device being dehydrated between level, its feature
The reaction condition for being the fluidized-bed reactor with heat removing tube is 240-500 DEG C and 0.3-6.0Mpa, synthesis gas CO/H2For 1:
3。
6. it is according to claim 1 based on the synthesis gas fluid bed preparing natural gas by methanation device being dehydrated between level, its feature
The temperature for being product gas after first and second grades of water coolers is 30-150 DEG C, after water cooler of the third level by temperature adjustment cross-line valve
The temperature of product gas is 250-400 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710455221.1A CN107090320B (en) | 2017-06-16 | 2017-06-16 | Device for preparing natural gas by methanation of synthetic gas fluidized bed based on interstage dehydration |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710455221.1A CN107090320B (en) | 2017-06-16 | 2017-06-16 | Device for preparing natural gas by methanation of synthetic gas fluidized bed based on interstage dehydration |
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2017
- 2017-06-16 CN CN201710455221.1A patent/CN107090320B/en active Active
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| CN104357117A (en) * | 2014-10-31 | 2015-02-18 | 西南化工研究设计院有限公司 | Non-circulating methanation process of coal-based synthetic natural gas and liquefied natural gas |
| CN207672007U (en) * | 2017-06-16 | 2018-07-31 | 中国石油大学(华东) | Based on the synthesis gas fluid bed preparing natural gas by methanation device being dehydrated between grade |
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