CN108865307A - Raw gas combined type full methanation technique and system without circulation loop - Google Patents
Raw gas combined type full methanation technique and system without circulation loop Download PDFInfo
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- CN108865307A CN108865307A CN201810896052.XA CN201810896052A CN108865307A CN 108865307 A CN108865307 A CN 108865307A CN 201810896052 A CN201810896052 A CN 201810896052A CN 108865307 A CN108865307 A CN 108865307A
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- 238000000034 method Methods 0.000 title claims abstract description 32
- 238000006243 chemical reaction Methods 0.000 claims abstract description 129
- 239000007789 gas Substances 0.000 claims abstract description 129
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000012495 reaction gas Substances 0.000 claims abstract description 26
- 238000000746 purification Methods 0.000 claims abstract description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 36
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 35
- 229910052739 hydrogen Inorganic materials 0.000 claims description 34
- 239000001257 hydrogen Substances 0.000 claims description 34
- 230000009466 transformation Effects 0.000 claims description 23
- 238000000844 transformation Methods 0.000 claims description 13
- 239000003245 coal Substances 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 8
- 238000002309 gasification Methods 0.000 claims description 6
- 238000011049 filling Methods 0.000 claims description 5
- 230000003247 decreasing effect Effects 0.000 claims description 4
- 239000003345 natural gas Substances 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 3
- 239000000843 powder Substances 0.000 claims description 3
- 239000002002 slurry Substances 0.000 claims description 3
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 5
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 206010054949 Metaplasia Diseases 0.000 abstract 1
- 230000015689 metaplastic ossification Effects 0.000 abstract 1
- 150000002431 hydrogen Chemical class 0.000 description 23
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 6
- 230000015572 biosynthetic process Effects 0.000 description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 6
- 238000003786 synthesis reaction Methods 0.000 description 6
- 238000010348 incorporation Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 238000005804 alkylation reaction Methods 0.000 description 2
- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 125000001741 organic sulfur group Chemical group 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000002829 reductive effect Effects 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000003113 dilution method Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
- 238000009423 ventilation Methods 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
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)
Abstract
The invention discloses the raw gas combined type full methanation technique and system of a kind of no circulation loop, technical solution is to include the following steps：Raw gas after oil removing, dedusting is divided into two strands, it is directly entered high-temperature methanation reaction member after one raw gas is transformed and purification, is subsequently sent to concatenated multistage methanation reaction unit and carries out methanation reaction to obtain the synthetic natural gas that methane contents on dry basis is greater than 95mol%；Gas is purified after another strand of raw gas is purified, the purified gas is further divided into multiply and is mixed in all or part of entrance reaction gas of concatenated multistage methanation reaction unit respectively, participates in subsequent methanation reaction.Present invention process is simple, it is easily operated, without product gas circulation, production cost is low, methane concentration is high, present system structure is simple, easily controllable, and operating cost is low, is suitable for large-scale methane metaplasia produces.
Description
Technical field
The present invention relates to a kind of methanation process and systems.
Background technique
The energy resource structure feature in China is " rich coal, oil-poor, few gas ", and as coal production and consumption big country, urgently
Need to find a kind of clean, efficient, acceptable trans-utilization mode of cost.Domestic and foreign experience is explored and used for reference by many years,
Develop the clean coal utilizations modes such as coal gas, can both realize the clean utilization of coal resources, reduce environmental pollution, can also subtract
Light natural gas is to external interdependency, guarantee Chinese energy safety.
In traditional natural gas from coal technique, raw gas first passes around conversion reaction adjustment H:Cmoleratio in 3.0-
Between 3.05, subsequently enters methanation unit and methanation reaction occurs.Reaction principle is as follows：
The characteristics of methanation reaction be it is strongly exothermic, high-concentration carbon monoxide reacts the insulation of generation in adiabatic reactor
Temperature rise is big, if not adopting an effective measure, it will equipment overtemperature and sintering of catalyst is caused to inactivate.Traditional process route uses
Portioned product gas circulation, and enter high-temperature methanation reactor after mixing with unstripped gas, by diluting an oxidation in raw material indirectly
Concentration of carbon controls reactor outlet temperature.The Datang gram flag of commercialized running at present, Xinjiang celebrating China, Inner Mongol remittance can be adopted
Reactor outlet temperature is controlled with setting circulation loop method.But it is anti-to will lead to primary high-temperature methanation after setting circulation loop
Device gas inlet amount is answered to increase, loaded catalyst and equipment investment increase, and further limit the enlargement of unit scale.
Meanwhile the process also needs to increase recycle compressor, plant maintenance and operating cost increase.Domestic natural gas from coal technique
Related patents are mostly also using the outlet temperature of the method control high-temperature methanation reactor of circulation loop
(CN201210029444, CN201110268668, CN201510161040.9) also has using the side such as vapor charge dilution
Method designs the report (CN201410598644, CN201410631615.4) without circulation loop methanation process.But it is steamed using water
It needs additionally to add steam in the scheme of gas charge dilution, needs steam control system, there are a large amount of inertia vapor anti-
It answers in device and reacts, increase system investments.Therefore so far, none more perfect technological means solves above-mentioned technology
Problem.
Summary of the invention
The purpose of the present invention is to solve above-mentioned technical problem, provide a kind of simple process, it is easily operated, without product
Gas circulation, production cost is low, methane concentration is high, suitable for large-scale production the raw gas combined type without circulation loop it is complete
Methanation process.
The present invention also provides a kind of structures simply, the raw gas combined type of operation no circulation loop low with cost of investment
Full methanation system.
The present invention includes the following steps：Raw gas after oil removing, dedusting is divided into two strands, one raw gas is transformed and net
High-temperature methanation reaction member is directly entered after change, it is anti-to be subsequently sent to concatenated multistage methanation reaction unit progress methanation
It should obtain the synthetic natural gas that methane contents on dry basis is greater than 95mol%；It is purified gas after another strand of raw gas is purified, institute
It states purified gas and is further divided into multiply and mixed in all or part of entrance reaction gas of multistage methanation reaction unit respectively, after participation
Continuous methanation reaction.
The method for being mixed into purified gas by share split, control enter the hydrogen of first order methanation reaction unit entrance reaction gas
Carbon modulus ratio is in 20-28, and the hydrogen carbon modulus ratio of concatenated multistage methanation reaction unit entrance reaction gas is successively decreased step by step, directly
Hydrogen carbon modulus ratio to afterbody methanation reaction unit entrance reaction gas is 2.6-3.2.
The hydrogen carbon modulus of the next stage methanation reaction unit entrance reaction gas compares upper level methanation reaction unit
The hydrogen carbon modulus ratio of entrance reaction gas reduces 1-4.
The tolerance of one raw gas accounts for the 60-90mol% of raw gas total amount, and the tolerance of another strand of raw gas accounts for slightly
The 10-40mol% of coal gas total amount.
It is characterized in that, product gas of the raw gas in dry coal powder gasification and coal-water slurry gasification.
The shift step includes three-level conversion reaction, controls conversion reaction unit entrances at different levels by filling into water vapour
Liquid to steam ratio is between 0.1-0.6；The one-stage transfor-mation reacts 200-230 DEG C of inlet temperature, 420-470 DEG C of outlet temperature；Two
200-230 DEG C of inlet temperature of conversion reaction, 320-400 DEG C of outlet temperature of grade；200-230 DEG C of inlet temperature of three-level conversion reaction,
240-300 DEG C of outlet temperature.
The multistage methanation reaction unit includes concatenated multistage high-temperature methanation reaction member and multistage low temperature methane
Change reaction member；The purified gas is divided into multiply, mix respectively the second level to afterbody high-temperature methanation reaction member and
In the entrance reaction gas of all or part of multistage low temperature methanation reaction unit.
The outlet temperature of the high-temperature methanation reaction member is controlled at 550-700 DEG C；The low temperature methanation unit
Outlet temperature controls between 300-460 DEG C.
Present system includes sequentially connected converter unit, the first clean unit and multistage methanation reaction unit, is gone back
It include the second clean unit, the gas access of second clean unit is connect with the gas access of the converter unit, institute
The gas vent for stating the second clean unit connects each gas access of multistage methanation reaction unit through valve respectively.
The multistage methanation reaction unit includes concatenated multistage high-temperature methanation reaction member and multistage low temperature methane
Change reaction member, the second level of the gas vent of second clean unit respectively through valve connection to afterbody high temperature first
The gas access of alkylation reaction unit and all or part of gas access of low temperature methanation reaction unit.
The converter unit includes one-stage transfor-mation reaction member, two-dimensional transform reaction member and three-level conversion reaction unit.
The inlet of the one-stage transfor-mation reaction member and two-dimensional transform reaction member is additionally provided with steam and fills into mouth.
The problem of for background technique, inventor carry out further investigation discovery, exist for high-concentration carbon monoxide
The big problem of the adiabatic temperature rise of generation, the hydrogen carbon modulus ratio of the inlet gas of methanation reaction unit are reacted in adiabatic reactor
Control it is particularly important, can not only have the heating problem for inhibiting methanation reaction by the control of hydrogen carbon modulus ratio, control is anti-
Device outlet temperature is answered, without circulation loop is arranged, plant investment is reduced, simplifies operating process.And make high temperature first
Alkylation reaction carries out under hydrogen-rich atmosphere, and catalyst is not easy carbon deposit, extends catalyst service life；To realize methanation reaction
The control of the hydrogen carbon modulus ratio of the inlet gas of unit is designed as follows under the premise of not using product gas to recycle：(1)
Raw gas is divided into two strands, one carries out transformation and purification process, and another stock is multistage as carbon raw material incorporation after then purifying
In methanation reaction unit, so as to simply adjust the hydrogen carbon modulus ratio into methanation reaction unitary gas；It is preferred that
, the tolerance of one raw gas typically constitutes from the 60-90mol% of raw gas total amount, and another burst of tolerance accounts for the 10- of raw gas total amount
40mol%, another burst of raw gas tolerance excessively will affect the hydrogen-carbon ratio of system, very few to be unfavorable for making full use of in synthesis gas
Effective gas.(2) since methanation reaction unit is usually plural serial stage, inventor limits second burst of tolerance and is divided into multiply
The gas access for mixing multistage methanation reaction unit respectively, further, with the progress of methanation reaction, every grade of methanation
Methanation content gradually increases in the synthesis gas of reaction member outlet, thus the reaction depth of methanation reaction unit at different levels
Not identical, second strand of raw gas is according to methanations at different levels to the incorporation of every grade of methanation reaction unit inlet gas
The hydrogen carbon modulus ratio of reaction member inlet gas requires to control, and in the present invention, limits and enters first order methanation reaction list
The hydrogen carbon modulus ratio of first inlet gas is in 20-28, and the hydrogen carbon modulus ratio of concatenated multistage methanation reaction unit inlet gas
Successively decrease step by step, until the hydrogen carbon modulus ratio of afterbody methanation reaction unit inlet gas is 2.6-3.2, every grade of methanation
After reaction, methanation content is gradually risen in synthesis gas, by the realization reaction of successively decreasing step by step for making hydrogen carbon modulus ratio in gas
The complete conversion of effective gas in gas.Preferably, total hydrogen carbon modulus in conversion gas and second strand of raw gas after first burst of transformation
Than between 2.99-3.05.
First strand of raw gas is first converted, and the purpose of transformation is in order to obtain rich in the methanation for having hydrogen
Unstripped gas, transformation can using one or more levels transformation, such as using three-level transformation when, according to need can be by filling into water vapour
The control of one-stage transfor-mation reactor inlet liquid to steam ratio is controlled between 0.2-0.8, two-dimensional transform device is reacted into mouthful liquid to steam ratio control and exists
Between 0.2-0.8；200-230 DEG C of inlet temperature of the one-stage transfor-mation reactor, 420-450 DEG C of outlet temperature；Second level becomes
200-230 DEG C of the inlet temperature of parallel operation reactor, 350-400 DEG C of outlet temperature.
The present invention controls reactor outlet temperature by adjusting carbon monoxide content in methanation reaction unit inlet gas
Degree, by the way that purified gas share split is mixed the control realized in synthesis gas to methanation reaction unit entrance carbon monoxide content, no
It needs that circulation loop is arranged, does not need recycle compressor, reduce plant investment, simplify operating process；Methanation reaction is in hydrogen-rich
It is carried out under atmosphere, catalyst is not easy carbon deposit, extends catalyst service life；For transformation, methanation in presence of sulfur, high/low temperature methane
Changing unit can be according to unstripped gas composition and each reactor outlet temperature requirement, the quantity and entrance object of each reactor of flexible configuration
Parameter is flowed, gas product can reach index request, and present invention process is suitable for a variety of raw gas, is applicable to processing and comes from
One of the product gas or oven gas of dry coal powder gasification or coal-water slurry gasification, pyrolysis gas.
Detailed description of the invention
Fig. 1 is process flow chart of the invention；
Fig. 2 is present system figure.
Wherein, R101- one-stage transfor-mation reaction member；R102- two-dimensional transform reaction member；S101- converts gas-liquid separation
Tank；S102- methanation knockout drum；S103- product knockout drum；The first clean unit of A101-；A102- second is purified
Unit；R201- high-temperature methanation reaction member；R202- high-temperature methanation reaction member；The reaction of R203- high-temperature methanation is single
Member；R204- high-temperature methanation reaction member；R205- low temperature methanation reaction unit；R206- low temperature methanation reaction unit；
R207- low temperature methanation reaction unit；R208- low temperature methanator；R209- low temperature methanator；R210- is low
Warm methanator.
Specific embodiment
Explanation is further explained to present system with reference to the accompanying drawing：
The loop-free full methanation integrated system of the present invention include sequentially connected one-stage transfor-mation reaction member R101,
Convert knockout drum S101, two-dimensional transform reaction member R102, three-level conversion reaction unit R 103, the first clean unit
A101 and multistage methanation reaction unit, the multistage methanation reaction unit include concatenated multistage high-temperature methanation reaction
Unit R 201, R202, R203, R204 and multistage low temperature methanation reaction unit R 205, R206, R207, R208, R209,
R210.Wherein, in the present embodiment, 210 front and back of afterbody low temperature methanation reaction unit R is also in series with methanation gas respectively
Liquid knockout drum S102 and product knockout drum S103, to realize gas-liquid separation；
It further include thering is the gas access of the second clean unit A102, the second clean unit A102 and the level-one to become
The gas access connection of reaction member R101 is changed, the gas vent of the second clean unit A102 connects through valve more respectively
The gas access of grade methanation reaction unit.In the present embodiment, the gas vent of the second clean unit A102 is respectively through valve
Door be connected to multistage high-temperature methanation reaction member R202, R203, R304 and multistage low temperature methanation reaction unit R 205,
R206, R207, the gas access of R208.
Steam benefit is additionally provided at the one-stage transfor-mation reaction member R101, the gas access two-dimensional transform reaction member R102
Entrance, for filling into middle pressure steam.
Process flow is as shown in Figure 1, the raw gas after dedusting, oil removing (forms H2- 17.98mol%, CO-
52.47mol%, CO2- 7.45mol%, CH4- 0, N2- 0.8mol%, H2O-20.8mol%, C2H6- 0, H2S-0.43mol%,
COS-0.01mol%, Ar-0.06mol%, O2-0；168 DEG C of temperature, pressure 3.9MPa, flow 30776.7kmol/h) it is divided into
Two strands, first strand of raw gas enters one-stage transfor-mation reaction member R101, two-dimensional transform reaction member R102 and three-level transformation is anti-
Unit R 103 is answered, tolerance accounts for the 60-90mol% of raw gas total amount, enters by filling into water vapour control conversion reaction units at different levels
The liquid to steam ratio of mouth is between 0.2-0.8,420-470 DEG C of outlet temperature of one-stage transfor-mation reaction member R101, two-dimensional transform reaction
320-400 DEG C of 102 outlet temperature of unit R, 240-300 DEG C of 103 outlet temperature of three-level conversion reaction unit R.Transformed change
Ventilation is directly entered the hydrogen sulfide of the first clean unit A101 removing, carbonyl sulfur, after the sulfur impurities such as organic sulfur, hydrogen in conversion gas
Gas contents on dry basis is 80-95%.Another strand of raw gas first removes hydrogen sulfide, carbonyl sulfur, organic sulfur through the second clean unit A102
It is purified gas after equal impurity, is separated into multiply as carbon source and mixes respectively the reaction gas of methanation reaction unit entrances at different levels
In, it participates in subsequent methanation reaction and generates methane.
The reaction gas that per share purified gas is drawn with upper level methanation reaction unit in proportion mixes, and mainly passes through control
Carbon monoxide content in mixed reaction gas controls high-temperature methanation reaction member outlet temperature between 600-700 DEG C,
The high-temperature methanation reaction member quantity is 4-10, and particular number is made of raw gas and high-temperature methanation reactor goes out
Mouth temperature determines, if hydrogen content is more in raw gas, while the setting of high-temperature methanation reaction member outlet temperature is higher, then
The quantity of high-temperature methanation reactor can be reduced accordingly.It is connected in the present embodiment using seven high-temperature methanation reaction members,
The control of carbon monoxide contents on dry basis is in 2-15mol% in entrance reaction gas；Control enters first order high-temperature methanation reaction member
The hydrogen carbon modulus ratio of R201 entrance reaction gas is in 20-28, and concatenated multistage high-temperature methanation reaction member and multistage low temperature
The hydrogen carbon modulus ratio of methanation reaction unit entrance reaction gas is successively decreased step by step, until afterbody methanation reaction unit entrance
The hydrogen carbon modulus ratio of reaction gas is 2.6-3.2.Preferably, the hydrogen carbon of the next stage methanation reaction unit entrance reaction gas
The hydrogen carbon modulus ratio that modulus compares upper level methanation reaction unit entrance reaction gas reduces 1-4.In the present embodiment, consider into
Hydrogen carbon modulus ratio has met control and has required in mouth reaction gas, and last two-stage low temperature methanation reaction unit R 209, R210 are practical
And it is not incorporated into purified gas (another strand of raw gas), when actual motion, those skilled in the art can be according to measuring and calculating
Hydrogen carbon modulus ratio select in the entrance reaction gas of each grade low-temp methanation reaction unit whether all or part of incorporation purified gas with
And specific mixed ratio, it can specifically be required according to the hydrogen carbon modulus ratio of design to control.
The moisture that transformation and methanation generate can be set as needed knockout drum and be removed water.In order to guarantee an oxygen
Change carbon completion and be converted into methane, the present invention connected simultaneously 5 low temperature methanation reaction unit Rs 205, R206, R207,
R208, R209, R210, outlet temperature control between 300-460 DEG C, and are entering afterbody low temperature methanation reaction
Before unit R 210, synthesis gas removes partial moisture through supercooling, separation, and it is anti-then to enter back into afterbody low temperature methanation
Unit R 210 is answered, guarantees that CO conversion is greater than 99.9%.Synthesis gas and second strand after first burst of transformation of the present invention
Total hydrogen carbon modulus ratio is between 2.99-3.05 in raw gas.After above-mentioned reaction process, the group of produced synthetic natural gas becomes
H2- 0.6mol%, CO-0, CO2- 0.5mol%, CH4- 97.6mol%, N2- 0.8mol%, H2O-0.4mol%；40 DEG C of temperature,
Pressure 2.17MPa, flow 5472.9kmol/h.
It is recycled in present invention process without product gas, low energy consumption, equipment investment and operating cost are low, is suitable for extensive first
Alkanisation production.
Claims (12)
1. a kind of raw gas combined type full methanation technique of no circulation loop, which is characterized in that include the following steps：It removes
Oil, the raw gas after dedusting are divided into two strands, are directly entered high-temperature methanation reaction member after one raw gas is transformed and purification,
It is subsequently sent to concatenated multistage methanation reaction unit and carries out the conjunction that methanation reaction obtains methane contents on dry basis greater than 95mol%
At natural gas；Gas is purified after another strand of raw gas is purified, the purified gas is further divided into multiply and mixes multistage methane respectively
In all or part of entrance reaction gas for changing reaction member, subsequent methanation reaction is participated in.
2. the raw gas combined type full methanation technique without circulation loop as described in claim 1, which is characterized in that pass through
The method that share split is mixed into purified gas, control enter the hydrogen carbon modulus ratio of first order methanation reaction unit entrance reaction gas in 20-
28, and the hydrogen carbon modulus ratio of concatenated multistage methanation reaction unit entrance reaction gas is successively decreased step by step, until afterbody methane
The hydrogen carbon modulus ratio for changing reaction member entrance reaction gas is 2.6-3.2.
3. the raw gas combined type full methanation technique without circulation loop as claimed in claim 2, which is characterized in that described
The hydrogen carbon modulus of next stage methanation reaction unit entrance reaction gas compares upper level methanation reaction unit entrance reaction gas
Hydrogen carbon modulus ratio reduces 1-4.
4. the raw gas combined type full methanation technique without circulation loop as described in claim 1, which is characterized in that described
The tolerance of one raw gas accounts for the 60-90mol% of raw gas total amount, and the tolerance of another strand of raw gas accounts for the 10- of raw gas total amount
40mol%.
5. the raw gas combined type full methanation technique without circulation loop as described in claim 1, which is characterized in that described
Product gas of the raw gas in dry coal powder gasification and coal-water slurry gasification.
6. such as the raw gas combined type full methanation technique without circulation loop that any one of claim 1-4 is stated, feature exists
In the shift step includes three-level conversion reaction, controls conversion reaction unit entrance liquid to steam ratio at different levels by filling into water vapour
Between 0.1-0.6；The one-stage transfor-mation reacts 200-230 DEG C of inlet temperature, 420-470 DEG C of outlet temperature；Two-dimensional transform
200-230 DEG C of inlet temperature, 320-400 DEG C of outlet temperature of reaction；200-230 DEG C of inlet temperature of three-level conversion reaction, outlet temperature
240-300 DEG C of degree.
7. the raw gas combined type full methanation technique of no circulation loop according to any one of claims 1-4, feature
It is, the multistage methanation reaction unit includes that concatenated multistage high-temperature methanation reaction member and multistage low temperature methanation are anti-
Answer unit；The purified gas is divided into multiply, respectively mix the second level to afterbody high-temperature methanation reaction member and all or
In the entrance reaction gas of the multistage low temperature methanation reaction unit in part.
8. the raw gas combined type full methanation technique of no circulation loop as claimed in claim 7, which is characterized in that the height
The outlet temperature of warm methanation reaction unit is controlled at 600-700 DEG C；The outlet temperature control of the low temperature methanation unit exists
Between 300-460 DEG C.
9. a kind of raw gas combined type full methanation system of no circulation loop, including sequentially connected converter unit, first
Clean unit and multistage methanation reaction unit, which is characterized in that it further include having the second clean unit, second clean unit
Gas access connect with the gas access of the converter unit, the gas vent of second clean unit connects through valve respectively
Connect each gas access of multistage methanation reaction unit.
10. the raw gas combined type full methanation system without circulation loop as claimed in claim 9, which is characterized in that institute
Stating multistage methanation reaction unit includes concatenated multistage high-temperature methanation reaction member and multistage low temperature methanation reaction unit,
The second level of the gas vent of second clean unit respectively through valve connection is to afterbody high-temperature methanation reaction member
Gas access and low temperature methanation reaction unit all or part of gas access.
11. the raw gas combined type full methanation system without circulation loop as described in claim 9 or 10, feature exist
In the converter unit includes one-stage transfor-mation reaction member, two-dimensional transform reaction member and three-level conversion reaction unit.
12. the raw gas combined type full methanation system without circulation loop as claimed in claim 11, which is characterized in that institute
The inlet for stating one-stage transfor-mation reaction member and two-dimensional transform reaction member is additionally provided with steam and fills into mouth.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810896052.XA CN108865307B (en) | 2018-08-08 | 2018-08-08 | Combined complete methanation process and system for raw gas without circulation loop |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810896052.XA CN108865307B (en) | 2018-08-08 | 2018-08-08 | Combined complete methanation process and system for raw gas without circulation loop |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108865307A true CN108865307A (en) | 2018-11-23 |
| CN108865307B CN108865307B (en) | 2023-10-24 |
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| CN208803039U (en) * | 2018-08-08 | 2019-04-30 | 中国五环工程有限公司 | Raw gas combined type full methanation system without circulation loop |
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| US4354960A (en) * | 1979-03-01 | 1982-10-19 | Hans Hammer | Process for the production of boron-containing nickel-aluminum oxide catalysts |
| CN102229827A (en) * | 2011-05-14 | 2011-11-02 | 大连瑞克科技有限公司 | Method for producing synthetic natural gas |
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