CN106147899B - A kind of method and device producing substitute natural gas - Google Patents
A kind of method and device producing substitute natural gas Download PDFInfo
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Abstract
The present invention provides a kind of method and device for producing substitute natural gas.The present invention is that the continuous processing process for the methane-rich gas that molar percentage containing methane is 94% or more is produced using coal or gasification of biomass product as raw material.Production technology provided by the invention can not only preferably control the operation temperature of methanator, the problems such as catalyst temperature runaway is sintered caused by avoiding because of the larger or accident of raw material fluctuation, and methanation reaction heat release is provided using system, improves total energy approach efficiency.
Description
Technical field
The present invention relates to a kind of method and devices for producing substitute natural gas, more particularly to coal or gasification of biomass production
Object is the method and device that raw material produces substitute natural gas, belongs to substitute natural gas technical field.
Background technique
Since last century the seventies, along with oil crisis, preparing methane from coal (also known as synthetic natural gas (Synthetic
Natural Gas, abbreviation SNG) or substitute natural gas) comparatively fast developed.The main method of preparing methane from coal includes: coal hydrogenation gas
Change and directly produce methane, and produces methane indirectly through synthesis gas.
Coal hydrogenation gasification directly produces methanol method and is primarily present following problems: efficiency of carbon con version is low, methane yield is low, gas
Complicated composition, methane concentration are low and cannot get the synthetic natural gas etc. of high quality.Comparatively, coal produces indirectly through synthesis gas
The technique of methane has the significant advantage that technical maturity is high, carbon utilisation rate is high and methane concentration is high.
The methanation catalyst at the beginning of the eighties in last century, German Lucci corporation combination BASF AG completes methane chemical industry
The exploitation of skill, and it is successfully applied to the natural gas from coal factory of 389 cubic meters per day of big plain in U.S.A factory；Centrica is public
Department develops HICOM technique and corresponding catalyst for the synthesis gas feature of BGL gasification furnace, and establishes 2832m3In/d
Trial assembly is set；Rope company, Top, Denmark successfully has developed the wide temperature range type catalyst that highest is resistant to 700 DEG C of high temperature, and develops TREMP
Full methanation technique.
More mature coal gas portion of methane has been established in last century for the purpose of using coal production city coal gas in China
Change technology: as Dalian Chemiclophysics Inst., Chinese Academy of Sciences has developed " Partial-methanation of Water-coal Gas At Atmospheric Pressure methanation production city coal gas technology "
(project year number 0100050009, announce 2001 times)；Chemical fertilizer research institute, the Ministry of Chemical Industry develops with normal pressure semiwater gas
For the RHM-266 type nickel system's methanation catalyst and technique of unstripped gas；Coal Mining Research Institute develops two stage furnace water gas first
Alkylation process (meet into etc., the exploitation of normal pressure two stage furnace water gas methanation process, clean coal technology, the 1st phase of volume 4 in 1998,
Page 36~39).
However, energy-saving, raising efficiency of energy utilization becomes the side of each technology development with the needs of sustainable development
To and trend.For methanation, high temperature, operation with high pressure, wide temperature range type catalyst are conducive to equipment and process intensification, in turn
Energy consumption is reduced, and improves the hot grade of methanation reaction by-product and recovery utilization rate.In consideration of it, wide temperature range type methanation catalyst, high
Temperature, high pressure full methanation technology have become the development trend of current methanation technology.Only has big plain in U.S.A in the world at present
One methanation commercial plants, and in being, low temperature methanation technology, it is complete for the high temperature of methanation development trend, high pressure
Methanation technology, the still not no precedent of industrial applications.Domestic methanation technology only stays in portion of methane at present, and is catalyzed
Agent adaptive temperature narrow range, strongly limits the comprehensive utilization ratio of energy；In addition the portion of methane technology carried out under normal pressure
It is unfavorable for reaction and equipment intensification, lacks reactor design and substance-energy integrated optimization.Therefore, there are still provide the energy
The demand of the method and device of the high production synthetic natural gas of utilization efficiency.
Summary of the invention
Therefore, the purpose of the present invention is to provide the methods and dress of a kind of generation substitute natural gas that efficiency of energy utilization is high
It sets.
What the present invention adopts the following technical solutions to realize.
The present invention provides a kind of method for producing substitute natural gas, and referring to Fig.1, the method includes following steps:
A) unstripped gas (1) 1:(0.1~5 by volume after the first heat exchange equipment (2) is warming up to 150~400 DEG C) it is divided into
First burst of unstripped gas (4) and second burst of unstripped gas (5)；
B) first burst of unstripped gas (4) in step a), the circulating air (19) after heating are mixed with the first steam (51)
The first gaseous mixture (6) for being 250~400 DEG C to temperature, the first gaseous mixture (6) is passed through in first segment methanator (7)
It reacts, obtains the first segment product gas (8) that temperature is 450~750 DEG C, which sets through the second heat exchange
Standby (9) and third heat exchange equipment (11) be cooled to 250~400 DEG C cooled down after first segment product gas (12)；
C) by 1:(0.1~5 by volume of the first segment product gas (12) after cooling that step b) is obtained) it is divided into circulating air
(14) and second burst of first segment product gas (13), circulation of the circulating air (14) after the 4th heat exchange equipment (15) is cooled down
Gas (16), the circulating air (16) after cooling obtain pressurized circulating air (18), the pressurization through recycle compressor (17) pressurization
Circulating air (18) afterwards through the 4th heat exchange equipment (15) be warming up to 150~380 DEG C heated up after circulating air (19)；
D) second burst of first segment product gas (13), second burst of unstripped gas (5) and the second steam (52) obtained step c)
It is mixed to get the second gaseous mixture (20) that temperature is 250~400 DEG C, the second gaseous mixture (20) is passed through second segment methanation reaction
Device reacts in (21), obtains the second segment product gas (22) that temperature is 400~650 DEG C, the second segment product gas (22) warp
5th heat exchange equipment (23), the first heat exchange equipment (2) and the 6th heat exchange equipment (26) are cooled to 120~400 DEG C of obtained coolings
Second segment product gas (27) afterwards；
E) by after cooling that step d) is obtained second segment product gas (27) and third steam (53) to be mixed to get third mixed
Close gas (28), third gaseous mixture (28) is passed through in third methanator (29) and is reacted, obtain temperature be 300~
450 DEG C of third section product gas (30)；
F) the third section product gas (30) that step e) is obtained is passed through gas-liquid separation after the cooling of the 6th heat exchange equipment (26)
Device (32) obtains product gas (33) and the process condensate (34) that temperature is 20~80 DEG C.
Preferably, the molar percentage composition of the unstripped gas (1) is as follows: carbon monoxide 5~50%, and carbon dioxide 0~
30%, hydrogen 20~80%, methane 0~20%.
Preferably, first burst of unstripped gas (4) for being divided into the unstripped gas (1) in the step a) and second burst of original
The volume ratio for expecting gas (5) can be 1:(0.1~1).
Preferably, in the step d), circulating air (14) that the first segment product gas (12) after the cooling is divided into
It can be 1:(0.1~1 with second burst of first segment product gas (13) volume ratio).
In a kind of preferred embodiment of the invention, the method also includes utilizing methanation anti-in the following manner
Answer heat release: make the boiler feedwater (35) from battery limit (BL) it is preheated after enter drum (36), make from (36) first boiler of drum to
Water (37) enters the first saturated vapor (38) that third heat exchange equipment (11) generate 3~10MPa, comes from second pot of drum (36)
Furnace water supply (39) enters the second saturated vapor (40) that the 5th heat exchange equipment (23) generates 3~10MPa, makes from drum (36)
Third saturated vapor (41) heats up through the second heat exchange equipment (9), obtains the superheated steam (42) that temperature is 300~550 DEG C.
The method of the production substitute natural gas provided according to the present invention, this method are original with coal or gasification of biomass product
Material produces substitute natural gas, and the molar percentage containing methane is 94% or more in resulting substitute natural gas product.
On the other hand, the present invention also provides the device for above-mentioned production substitute natural gas method provided by the invention,
The device includes:
Methanator, including first segment methanator (7), the second segment methane for carrying out methanation reaction
Change reactor (21) and third section methanator (29)；
Heat exchange equipment, including for heating and/or cooling gas the first heat exchange equipment (2), the second heat exchange equipment (9),
Third heat exchange equipment (11), the 4th heat exchange equipment (15), the 5th heat exchange equipment (23) and the 6th heat exchange equipment (26)；
Recycle compressor, including the recycle compressor (17) for circulating air to be pressurized.
In the preferred embodiment of present device, the first segment methanator (7), second segment methanation are anti-
Answering device (21) and third section methanator (29) is insulation fix bed methanator.
Preferably, described device further includes drum (36), is set for providing boiler feedwater for heat exchange equipment and receiving heat exchange
The standby saturated vapor generated, while saturated vapor is delivered to heat exchange equipment.Specifically, the drum (36) for third for changing
Hot equipment (11) provides the first boiler feedwater (37), provides the second boiler feedwater (39) for the 5th heat exchange equipment (23), and receive
The second saturated vapor that the first saturated vapor (38) and the 5th heat exchange equipment (23) that third heat exchange equipment (11) generates generate
(40), the second heat exchange equipment (9) while by third saturated vapor (41) are delivered to.
Preferably, the heat exchange equipment is selected from useless pot and steam superheater.
Preferably, described device further includes desulfurization reactor, for carrying out deep desulfuration to unstripped gas.
Preferably, described device further includes deoxidation reactor, for carrying out depth deoxidation to unstripped gas.
Preferably, described device further includes gas-liquid separator, for the condensed water in separating technology gas.
The alternative of 94mol% containing methane or more is produced using coal or gasification of biomass product as raw material the present invention provides a kind of
The continuous processing process and device of natural gas.Process flow provided by the invention is as follows: it is divided into two strands after unstripped gas is preheated,
In first strand of unstripped gas mixed with circulating air after enter first segment methanator react to obtain first segment product gas；It should
First segment product gas is divided into two strands, enters back into first segment methanator after the pressurization of the first stock-traders' know-how recycle compressor；Second strand
Unstripped gas enters second segment methanator after mixing with second burst of first segment product gas and reacts to obtain second segment product
Gas, the second segment product gas enter third section methanator and react；Third section product gas obtains after gas-liquid separation
Product gas.
If still containing a small amount of carbon monoxide and carbon dioxide in product gas of the invention, gas can further be reacted
Obtain final products.
Compared with prior art, the present invention realizes the synthesis gas of coal or gasification of biomass product after purified is complete
Methanation produces substitute natural gas, has process flow reasonable, has an operability；Capacity usage ratio is high, energy saving, ring
The advantages that border is friendly.
Detailed description of the invention
Hereinafter, carrying out the embodiment that the present invention will be described in detail in conjunction with attached drawing, in which:
Fig. 1 is a kind of process flow chart of embodiment of present invention production substitute natural gas method；
Fig. 2 is low temperature methanation process flow chart in tradition, is used for and production substitute natural gas method provided by the invention
It compares.
Specific embodiment
The present invention is further described in detail With reference to embodiment, and the embodiment provided is only for explaining
The bright present invention, the range being not intended to be limiting of the invention.
Methanator used in the examples can load a large amount of commercialized methanation catalysts, such as Davy company
CRG catalyst series, the MCR-2X catalyst of Topsoe company, south chemistry G1-85 and G1-86 catalyst etc..
Embodiment 1
The present embodiment is a kind of preferred embodiment of the production method of substitute natural gas provided by the invention, the present embodiment
Process flow chart it is as shown in Figure 1.
A) coal or biomass pass through the unstripped gas that gasification unit, converter unit and clean unit are met the requirements, raw material
Gas 1 is divided into first strand of unstripped gas, 4, second strands of unstripped gas 5 after the first heat exchange equipment 2 is warming up to 190~210 DEG C；
B) first strand of unstripped gas 4 in step a), the circulating air 19 after heating and the first steam 51 are mixed to get temperature
For 280~300 DEG C of the first gaseous mixture 6, the first gaseous mixture 6 is passed through in first segment methanator 7 and is reacted, is obtained
The first segment product gas 8 that temperature is 600~620 DEG C, the first segment product gas 8 is through the second heat exchange equipment 9 and third heat exchange equipment
11 be cooled to 300~320 DEG C cooled down after first segment product gas 12；
C) the first segment product gas 12 after cooling that step b) is obtained is divided into circulating air 14 and second strand of first segment product
Gas 13, circulating air 16 of the circulating air 14 after the 4th heat exchange equipment 15 is cooled down, the circulating air 16 after cooling is through recycling
The pressurization of compressor 17 obtains pressurized circulating air 18, and the pressurized circulating air 18 is warming up to through the 4th heat exchange equipment 15
250~270 DEG C heated up after circulating air 19；
D) second burst of first segment product gas, 13, second strands of unstripped gas 5 that step c) is obtained and the second steam 52 are mixed
The second gaseous mixture 20 for being 290~300 DEG C to temperature, the second gaseous mixture 20 is passed through in second segment methanator 21 and is occurred
Reaction, obtaining temperature is 500~520 DEG C of second segment product gas 22, and the second segment product gas 22 is through the 5th heat exchange equipment 23, the
One heat exchange equipment 2, the 6th heat exchange equipment 26 are cooled to the second segment product gas 27 after the cooling that 220~240 DEG C obtain；
E) by after cooling that step d) is obtained second segment product gas 27 and third steam 53 to be mixed to get temperature be 220-
Third gaseous mixture 28 is passed through third methanator 29 and reacted by 240 DEG C of third gaseous mixture 28, and obtaining temperature is
370~390 DEG C of third product gas 30；
F) the third product gas 30 that step e) is obtained is passed through gas-liquid separator 32 after the cooling of the 6th heat exchange equipment 26, obtained
Product gas 33 and process condensate 34 to temperature for 30~50 DEG C.Wherein, methanation reaction it is exothermic using technique include: come
Boiler feedwater 35 from battery limit (BL) is preheated rear into drum 36, makes to set from 36 first boiler feedwater 37 of drum into third heat exchange
Standby 11 generate the first saturated vapor 38 of 4.5~5.5MPa, and the second boiler feedwater 39 from drum 36 enters the 5th heat exchange and sets
Standby 23 generate the second saturated vapor 40 of 4.5~5.5MPa, set the third saturated vapor 41 from drum 36 through the second heat exchange
Standby 9 heating, obtains the superheated steam 42 that temperature is 440~460 DEG C.
Wherein, the volume ratio 1:0.12 of first strand of unstripped gas 4 and second strand of unstripped gas 5, circulating air 14 and second strand second
The volume ratio of section product gas 12 is 1:0.33.
Below by way of the gas composition parameter of each logistics in table 1, intuitively describe each in process flow shown in FIG. 1
A workshop section's methanation reaction actually occurs situation.
Table 1
The explanation of logistics number: 1 is unstripped gas；6 be the first gaseous mixture；8 be first segment product gas；20 be the second mixing
Gas；22 be second segment product gas；28 be third gaseous mixture；30 be third section product gas；14 be circulating air；33 be product gas SNG；
42 be superheated steam.
Embodiment 2
The present embodiment is a kind of preferred embodiment of the production method of substitute natural gas provided by the invention, the present embodiment
Process flow chart it is as shown in Figure 1.
A) coal or biomass pass through the unstripped gas that gasification unit, converter unit and clean unit are met the requirements, raw material
Gas 1 is divided into first strand of unstripped gas, 4, second strands of unstripped gas 5 after the first heat exchange equipment 2 is warming up to 220~240 DEG C；
B) first strand of unstripped gas 4 in step a), the circulating air 19 after heating and the first steam 51 are mixed to get temperature
For 290~310 DEG C of the first gaseous mixture 6, the first gaseous mixture 6 is passed through in first segment methanator 7 and is reacted, is obtained
The first segment product gas 8 that temperature is 590~610 DEG C, the first segment product gas 8 is through the second heat exchange equipment 9 and third heat exchange equipment
11 be cooled to 340~360 DEG C cooled down after first segment product gas 12；
C) the first segment product gas 12 after cooling that step b) is obtained is divided into circulating air 14 and second strand of first segment product
Gas 13, circulating air 16 of the circulating air 14 after the 4th heat exchange equipment 15 is cooled down, the circulating air 16 after cooling is through recycling
The pressurization of compressor 17 obtains pressurized circulating air 18, and the pressurized circulating air 18 is warming up to through the 4th heat exchange equipment 15
290~310 DEG C heated up after circulating air 19；
D) second burst of first segment product gas, 13, second strands of unstripped gas 5 that step c) is obtained and the second steam 52 are mixed
The second gaseous mixture 20 for being 320~340 DEG C to temperature, the second gaseous mixture 20 is passed through in second segment methanator 21 and is occurred
Reaction, obtaining temperature is 560~580 DEG C of second segment product gas 22, and the second segment product gas 22 is through the 5th heat exchange equipment 23, the
One heat exchange equipment 2, the 6th heat exchange equipment 26 are cooled to the second segment product gas 27 after the cooling that 230~250 DEG C obtain；
E) by after cooling that step d) is obtained second segment product gas 27 and third steam 53 to be mixed to get temperature be 230-
Third gaseous mixture 28 is passed through third methanator 29 and reacted by 250 DEG C of third gaseous mixture 28, and obtaining temperature is
390~410 DEG C of third product gas 30；
F) the third product gas 30 that step e) is obtained is passed through gas-liquid separator 32 after the cooling of the 6th heat exchange equipment 26, obtained
Product gas 33 and process condensate 34 to temperature for 30~50 DEG C.Wherein, methanation reaction it is exothermic using technique include: come
Boiler feedwater 35 from battery limit (BL) is preheated rear into drum 36, makes to set from 36 first boiler feedwater 37 of drum into third heat exchange
Standby 11 generate the first saturated vapor 38 of 5.5~6.5MPa, and the second boiler feedwater 39 from drum 36 enters the 5th heat exchange and sets
Standby 23 generate the second saturated vapor 40 of 5.5~6.5MPa, set the third saturated vapor 41 from drum 36 through the second heat exchange
Standby 9 heating, obtains the superheated steam 42 that temperature is 490~510 DEG C.
Wherein, the volume ratio 1:0.15 of first strand of unstripped gas 4 and second strand of unstripped gas 5, circulating air 14 and second strand second
The volume ratio of section product gas 12 is 1:0.15.
Below by way of the gas composition parameter of each logistics in table 2, intuitively describe each in process flow shown in FIG. 1
A workshop section's methanation reaction actually occurs situation.
Table 2
The explanation of logistics number is the same as table 1.
Embodiment 3
The present embodiment is a kind of preferred embodiment of the production method of substitute natural gas provided by the invention, the present embodiment
Process flow chart it is as shown in Figure 1.
A) coal or biomass pass through the unstripped gas that gasification unit, converter unit and clean unit are met the requirements, raw material
Gas 1 is divided into first strand of unstripped gas, 4, second strands of unstripped gas 5 after the first heat exchange equipment 2 is warming up to 220~220 DEG C；
B) first strand of unstripped gas 4 in step a), the circulating air 19 after heating and the first steam 51 are mixed to get temperature
For 290~310 DEG C of the first gaseous mixture 6, the first gaseous mixture 6 is passed through in first segment methanator 7 and is reacted, is obtained
The first segment product gas 8 that temperature is 600~620 DEG C, the first segment product gas 8 is through the second heat exchange equipment 9 and third heat exchange equipment
11 be cooled to 300~320 DEG C cooled down after first segment product gas 12；
C) the first segment product gas 12 after cooling that step b) is obtained is divided into circulating air 14 and second strand of first segment product
Gas 13, circulating air 16 of the circulating air 14 after the 4th heat exchange equipment 15 is cooled down, the circulating air 16 after cooling is through recycling
The pressurization of compressor 17 obtains pressurized circulating air 18, and the pressurized circulating air 18 is warming up to through the 4th heat exchange equipment 15
250~370 DEG C heated up after circulating air 19；
D) second burst of first segment product gas, 13, second strands of unstripped gas 5 that step c) is obtained and the second steam 52 are mixed
The second gaseous mixture 20 for being 290~310 DEG C to temperature, the second gaseous mixture 20 is passed through in second segment methanator 21 and is occurred
Reaction, obtaining temperature is 500~520 DEG C of second segment product gas 22, and the second segment product gas 22 is through the 5th heat exchange equipment 23, the
One heat exchange equipment 2, the 6th heat exchange equipment 26 are cooled to the second segment product gas 27 after the cooling that 240~260 DEG C obtain；
E) by after cooling that step d) is obtained second segment product gas 27 and third steam 53 to be mixed to get temperature be 240-
Third gaseous mixture 28 is passed through third methanator 29 and reacted by 260 DEG C of third gaseous mixture 28, and obtaining temperature is
360~380 DEG C of third product gas 30；
F) the third product gas 30 that step e) is obtained is passed through gas-liquid separator 32 after the cooling of the 6th heat exchange equipment 26, obtained
Product gas 33 and process condensate 34 to temperature for 30~50 DEG C.Wherein, methanation reaction it is exothermic using technique include: come
Boiler feedwater 35 from battery limit (BL) is preheated rear into drum 36, makes to set from 36 first boiler feedwater 37 of drum into third heat exchange
Standby 11 generate the first saturated vapor 38 of 5.5~6.5MPa, and the second boiler feedwater 39 from drum 36 enters the 5th heat exchange and sets
Standby 23 generate the second saturated vapor 40 of 5.5~6.5MPa, set the third saturated vapor 41 from drum 36 through the second heat exchange
Standby 9 heating, obtains the superheated steam 42 that temperature is 470~490 DEG C.
Wherein, the volume ratio 1:0.11 of first strand of unstripped gas 4 and second strand of unstripped gas 5, circulating air 14 and second strand second
The volume ratio of section product gas 12 is 1:0.30.
Below by way of the gas composition parameter of each logistics in table 3, intuitively describe each in process flow shown in FIG. 1
A workshop section's methanation reaction actually occurs situation.
Table 3
The explanation of logistics number is the same as table 1.
Comparative example 1
It is raw using low temperature methanation technology in tradition under the conditions of identical design basis to be compared with embodiment 1
Substitute natural gas is produced, concrete technology flow process figure is as shown in Figure 2.
A) coal or biomass pass through the unstripped gas that gasification unit, converter unit and clean unit are met the requirements, raw material
Gas 501 heated up after the first heat exchange equipment 502 is warming up to 140~160 DEG C after unstripped gas 503.Raw material after heating
Gas 503 is divided into two streams, it may be assumed that first strand of unstripped gas 504 and second strand of unstripped gas 505.
B) first strand of unstripped gas 504 is mixed with the circulating air 524 after heating, obtains first that temperature is 270~290 DEG C
Gaseous mixture 506 is passed into first segment methanator 507 and carries out methanation reaction, and obtaining temperature is 490~510 DEG C
First segment product gas 508.First segment product gas 508 cools down by the second heat exchange equipment 509 and third heat exchange equipment 511, obtains
The first segment product gas 512 after cooling for being 300~320 DEG C to temperature, while by-product saturated vapor and superheated steam.
C) the first segment product gas 512 after cooling is mixed with second strand of unstripped gas 505, obtaining temperature is 270~290 DEG C
The second gaseous mixture 513, be passed into second segment methanator 514 and carry out methanation reaction, obtain temperature be 490~
510 DEG C of second segment product gas 515.Second segment product gas 515 obtains after the 4th heat exchange equipment 516 is cooled to 230~250 DEG C
Second segment product gas 517 after cooling.
D) the second segment product gas 517 after cooling is divided to for two strands: first bursts of second segment product gas 518 and second strand second
Section product gas 519.After first burst of second segment product gas 518 obtains cooling after the 5th heat exchange equipment 520 is cooled to 30~50 DEG C
First burst of second segment product gas 521.First burst of second segment product gas 521 after cooling enters recycle compressor 522 and is pressurized, and obtains
To circulating air 523, circulating air 523 heats up through the 5th heat exchange equipment 520, the circulation after obtaining the heating that temperature is 190~210 DEG C
Gas 524.
E) second burst of second segment product gas 519 for obtaining step d), which is passed through in third section methanator 525, carries out
Methanation reaction obtains the third section product gas 526 that temperature is 290~310 DEG C.Third section product gas 526 is set through the first heat exchange
Standby 502 cool down and pass through gas-liquid separator 528, obtain product gas 529 (SNG) and the process condensate that temperature is 30~50 DEG C
530。
Wherein, it using technique includes: that vapour is sent into after the boiler feedwater 531 from battery limit (BL) is preheated that methanation reaction is exothermic
Packet 532, the first boiler feedwater 533 and the second boiler feedwater 534 in drum 532 respectively enter third by downspout and change
Hot equipment 511 and the 4th heat exchange equipment 517 produce the first saturated vapor 534 and the second saturated vapor 536, the first saturated vapor
534 and second saturated vapor 536 by riser enter drum 532, the third saturated vapor 537 that drum 532 generates is through second
Heat exchange equipment 509 heats up, and obtains the superheated steam 538 that temperature is 440~460 DEG C and sends out battery limit (BL).
Wherein, the volume ratio of first strand of unstripped gas, 504, second strands of unstripped gas 505 is 1:1.30, first strand of second segment product
The volume ratio of gas 518 and second burst of second segment product gas 519 is 1:0.25.
Below by way of the gas composition parameter of each logistics in table 4, intuitively describe each in process flow shown in Fig. 2
A workshop section's methanation reaction actually occurs situation.
Table 4
The explanation of logistics number: 501 be unstripped gas；506 be the first gaseous mixture；508 be first segment product gas；513 be
Two gaseous mixtures；515 be second segment product gas；519 be second burst of second segment product gas；526 be third section product gas；521 be to follow
Ring gas；529 be product gas SNG；538 be superheated steam.
Compared with comparative example 1, under identical design basis, embodiment 1 is higher than heat utilization ratio, consumption is low: embodiment 1
The by-product superheated steam amount of by-product superheated steam 184.7t/h, 1 by-product superheated steam 158.6t/h of comparative example, embodiment 1 compare
Ratio 1 high 16.5%.
Claims (10)
1. a kind of method for producing substitute natural gas, the described method comprises the following steps:
A) unstripped gas (1) 1:(0.1~5 by volume after the first heat exchange equipment (2) is warming up to 150~400 DEG C) it is divided into first
Stock unstripped gas (4) and second burst of unstripped gas (5)；
B) first burst of unstripped gas (4) in step a), the circulating air (19) after heating and the first steam (51) are mixed to get temperature
First gaseous mixture (6) is passed through in first segment methanator (7) and occurs by the first gaseous mixture (6) that degree is 250~400 DEG C
Reaction obtains the first segment product gas (8) that temperature is 450~750 DEG C, and the first segment product gas (8) is through the second heat exchange equipment (9)
With third heat exchange equipment (11) be cooled to 250~400 DEG C cooled down after first segment product gas (12)；
C) by 1:(0.1~5 by volume of the first segment product gas (12) after cooling that step b) is obtained) it is divided into circulating air (14)
With second burst of first segment product gas (13), circulating air of the circulating air (14) after the 4th heat exchange equipment (15) is cooled down
(16), the circulating air after cooling (16) obtains pressurized circulating air (18) through recycle compressor (17) pressurization, after the pressurization
Circulating air (18) through the 4th heat exchange equipment (15) be warming up to 150~380 DEG C heated up after circulating air (19)；
D) second burst of first segment product gas (13), second burst of unstripped gas (5) and the second steam (52) mixing obtained step c)
The second gaseous mixture (20) that temperature is 250~400 DEG C is obtained, the second gaseous mixture (20) is passed through second segment methanator
(21) it reacts in, obtaining temperature is 450~650 DEG C of second segment product gas (22), and the second segment product gas (22) is through the
After five heat exchange equipments (23), the first heat exchange equipment (2), the 6th heat exchange equipment (26) are cooled to the cooling that 120~400 DEG C obtain
Second segment product gas (27)；
E) by after cooling that step d) is obtained second segment product gas (27) and third steam (53) be mixed to get temperature be 120~
400 DEG C of third gaseous mixture (28), third gaseous mixture (28) is passed through in third methanator (29) and is reacted, is obtained
The third product gas (30) that temperature is 300~450 DEG C；
F) the third product gas (30) that step e) is obtained is passed through gas-liquid separator (32) after the cooling of the 6th heat exchange equipment (26),
Obtain product gas (33) and the process condensate (34) that temperature is 20~80 DEG C；
Wherein, the method also includes utilizing methanation reaction heat release in the following manner: making the boiler feedwater from battery limit (BL)
(35) preheated rear into drum (36), so that the first boiler feedwater (37) from drum (36) is entered third heat exchange equipment
(11), the first saturated vapor (38) for generating 3~10MPa makes the second boiler feedwater (39) from drum (36) enter the 5th
Heat exchange equipment (23) generates the second saturated vapor (40) of 3~10MPa, makes the third saturated vapor (41) from drum (36)
It heats up through the second heat exchange equipment (9), obtains the superheated steam (42) that temperature is 300~550 DEG C.
2. according to the method described in claim 1, wherein, the molar percentage composition of the unstripped gas is as follows: carbon monoxide 5~
50%, carbon dioxide 0~30%, hydrogen 20~80%, methane 0~20%.
3. method according to claim 1 or 2, in the step a), first burst of original that the unstripped gas (1) is divided into
The volume ratio for expecting gas (4) and second burst of unstripped gas (5) is 1:(0.1~1).
4. the first segment product gas (12) after the cooling is divided into circulating air (14) by method according to claim 1 or 2
Volume ratio with second burst of first segment product gas (13) is 1:(0.1~1).
5. being used for the device of any one of claims 1 to 4 the method comprising:
Methanator, it is anti-including the first segment methanator (7) for carrying out methanation reaction, second segment methanation
Answer device (21), third section methanator (29)；
Heat exchange equipment, including the first heat exchange equipment (2), the second heat exchange equipment (9), third for heating and/or cooling gas
Heat exchange equipment (11), the 4th heat exchange equipment (15), the 5th heat exchange equipment (23) and the 6th heat exchange equipment (26)；
Recycle compressor, including the recycle compressor (17) for circulating air to be pressurized；With
Drum (36) while will satisfy for providing boiler feedwater for heat exchange equipment and receiving the saturated vapor of heat exchange equipment generation
Heat exchange equipment is delivered to steam.
6. device according to claim 5, wherein the first segment methanator (7), second segment methanation reaction
Device (21) and third section methanator (29) are insulation fix bed methanator.
7. device according to claim 5 or 6, wherein the heat exchange equipment is selected from useless pot and steam superheater.
8. device according to claim 5 or 6, wherein described device further includes desulfurization reactor, for unstripped gas into
Row deep desulfuration.
9. device according to claim 5 or 6, wherein described device further includes deoxidation reactor, for unstripped gas into
Row depth deoxidation.
10. device according to claim 5 or 6, wherein described device further includes gas-liquid separator, is used for separating technology
Condensed water in gas.
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