CN106147899A - 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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- CN106147899A CN106147899A CN201510137677.4A CN201510137677A CN106147899A CN 106147899 A CN106147899 A CN 106147899A CN 201510137677 A CN201510137677 A CN 201510137677A CN 106147899 A CN106147899 A CN 106147899A
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Abstract
The present invention provides a kind of method and device producing substitute natural gas.The present invention is to contain the continuous processing flow process of the methane-rich gas that methane molar percentage is more than 94% with coal or gasification of biomass product for raw material production.The production technology that the present invention provides can not only preferably control the operation temperature of methanator, avoid because of problems such as raw material fluctuation is relatively big or accident causes catalyst temperature runaway sintering, and provide methanation reaction heat release and utilize system, improve total energy approach efficiency.
Description
Technical field
The present invention relates to a kind of method and device producing substitute natural gas, more particularly to coal or life
Gasification substance product is the method and device of raw material production substitute natural gas, belongs to substitute natural gas technology
Field.
Background technology
Since last century the seventies, along with oil crisis, preparing methane from coal (is also called synthesis of natural
Gas (Synthetic Natural Gas is called for short SNG) or substitute natural gas) comparatively fast developed.Coal
The main method of methane processed includes: coal hydrogenation gasification is directly produced methane, and delivers a child through between synthesis gas
Methane phase.
Coal hydrogenation gasification is directly produced methanol method and is primarily present problems with: efficiency of carbon con version is low, methane
Yield is low, gas composition is complicated, methane concentration is low and can not get high-quality synthetic natural gas etc..
Comparatively speaking, coal is indirectly given birth to methanogenic technique through synthesis gas and is had that technology maturity is high, carbon utilisation rate
High and that methane concentration is high significant advantage.
At the beginning of the eighties in last century, the methanation catalyst that LURGI of Germany combines BASF AG is complete
Become the exploitation of methanation process, and be successfully applied to big plain in U.S.A factory 389 cubic meters per day
Natural gas from coal factory；Company of Centrica develops for the synthesis gas feature of BGL gasification furnace
HICOM technique and corresponding catalyst, and establish 2832m3The pilot-plant of/d；Top of Denmark
Suo company successfully have developed can the wide temperature range type catalyst of resistance to 700 DEG C of high temperature, and develop TREMP
Full methanation technique.
In China, for the purpose of utilizing coal production city coal gas, set up more ripe coal in last century
Gas portion of methane technology: as Dalian Chemiclophysics Inst., Chinese Academy of Sciences have developed " water at atmospheric pressure coal gas portion
Point methanation production city coal gas technology " (project year numbering 0100050009, announcement time 2001
Year)；The Ministry of Chemical Industry's chemical fertilizer institute develops the RHM-266 type nickel with normal pressure semiwater gas as unstripped gas
It is methanation catalyst and technique；Coal Mining Research Institute develops two stage furnace water gas methanation process
(meet into etc., the exploitation of normal pressure two stage furnace water gas methanation process, clean coal technology, 1998 years
Volume 4 the 1st phase, page 36～39).
But, along with the needs of sustainable development, energy-saving and cost-reducing, raising efficiency of energy utilization becomes each
The direction of technology development and trend.For methanation, high temperature, operation with high pressure, wide temperature range type are urged
Agent is conducive to equipment and process intensification, and then reduces energy consumption, and improves the hot product of methanation reaction by-product
Position and recovery utilization rate.In consideration of it, wide temperature range type methanation catalyst, high temperature, high pressure full methanation
Technology has become the development trend of current methanation technology.Only have big plain in U.S.A one the most in the world
Methanation commercial plants, and in being, low temperature methanation technology, for the height of methanation development trend
Temperature, high pressure full methanation technology, still do not have the precedent of industrial applications.Domestic methanation technology mesh
Before only stay in portion of methane, and catalyst adaptive temperature narrow range, strongly limit energy combine
Close utilization ratio；The portion of methane technology additionally carried out under normal pressure is unfavorable for reaction and equipment intensification,
Lack reactor design and the integrated optimization of material-energy.Therefore, still suffer from providing efficiency of energy utilization
The demand of the method and device of high production synthetic natural gas.
Summary of the invention
Therefore, it is an object of the invention to provide the generation substitute natural gas that a kind of efficiency of energy utilization is high
Method and device.
The present invention realizes by the following technical solutions.
The present invention provides a kind of method producing substitute natural gas, with reference to Fig. 1, described method include with
Under step:
A) unstripped gas (1) after the first heat transmission equipment (2) is warming up to 150～400 DEG C by volume
1:(0.1～5) it is divided into first burst of unstripped gas (4) and second burst of unstripped gas (5)；
B) by the circulating air (19) and first after first burst of unstripped gas (4) in step a), intensification
Steam (51) is mixed to get the first gaseous mixture (6) that temperature is 250～400 DEG C, by the first gaseous mixture
(6) being passed through in first paragraph methanator (7) and react, obtaining temperature is 450～750 DEG C
First paragraph product gas (8), this first paragraph product gas (8) is through the second heat transmission equipment (9) and the 3rd
Heat transmission equipment (11) be cooled to 250～400 DEG C lowered the temperature after first paragraph product gas (12)；
C) first paragraph product gas (12) 1:(0.1 by volume～5 after the cooling that step b) is obtained)
Being divided into circulating air (14) and second burst of first paragraph product gas (13), described circulating air (14) is through
Four heat transmission equipments (15) lowered the temperature after circulating air (16), circulating air (16) warp after cooling
Recycle compressor (17) supercharging obtains the circulating air (18) after supercharging, the circulating air after described supercharging
(18) through the 4th heat transmission equipment (15) be warming up to 150～380 DEG C heated up after circulating air (19)；
D) second burst of first paragraph product gas (13) step c) obtained, second burst of unstripped gas (5)
It is mixed to get the second gaseous mixture (20) that temperature is 250～400 DEG C, by second with the second steam (52)
Gaseous mixture (20) is passed through in second segment methanator (21) and reacts, and obtains temperature and is
Second segment product gas (22) of 400～650 DEG C, this second segment product gas (22) is through the 5th heat transmission equipment
(23), the first heat transmission equipment (2) and the 6th heat transmission equipment (26) are cooled to 120～400 DEG C and obtain
Cooling after second segment product gas (27)；
E) second segment product gas (27) after the cooling that step d) is obtained and the 3rd steam (53)
It is mixed to get the 3rd gaseous mixture (28), the 3rd gaseous mixture (28) is passed through front three alkylation reactors
(29) react in, obtain the 3rd section of product gas (30) that temperature is 300～450 DEG C；
F) the 3rd section of product gas (30) obtained by step e) is lowered the temperature through the 6th heat transmission equipment (26)
After be passed through gas-liquid separator (32), obtain product gas (33) and process condensate that temperature is 20～80 DEG C
Liquid (34).
Preferably, the molar percentage composition of described unstripped gas (1) is as follows: carbon monoxide 5～50%,
Carbon dioxide 0～30%, hydrogen 20～80%, methane 0～20%.
Preferably, in described step a), first strand of unstripped gas that described unstripped gas (1) is divided into
(4) volume ratio of and the second burst of unstripped gas (5) can be 1:(0.1～1).
Preferably, in described step d), by first paragraph product gas (12) after described cooling point
The circulating air (14) and second burst of first paragraph product gas (13) volume ratio that become can be 1:(0.1～1).
In a kind of preferred embodiment of the present invention, described method also includes profit in the following manner
Use methanation reaction heat release: after making the boiler feedwater from battery limit (BL) (35) preheated, enter drum (36),
Make to enter the 3rd heat transmission equipment (11) from drum (36) first boiler feedwater (37) and produce 3～10
First saturated vapor (38) of MPa, the second boiler feedwater (39) from drum (36) enters
5th heat transmission equipment (23) produces second saturated vapor (40) of 3～10MPa, makes from drum (36)
The 3rd saturated vapor (41) through the second heat transmission equipment (9) heat up, obtaining temperature is 300～550
DEG C superheated steam (42).
According to the method for the production substitute natural gas that the present invention provides, the method is with coal or gasification of biomass
Product is raw material, produce substitute natural gas, in the substitute natural gas product of gained containing methane mole
Percentage ratio is more than 94%.
On the other hand, the above-mentioned production substitute natural gas side provided for the present invention is provided
The device of method, this device includes:
Methanator, including the first paragraph methanator (7) for carrying out methanation reaction,
Second segment methanator (21) and the 3rd section of methanator (29)；
Heat transmission equipment, including for heating and/or cool down first heat transmission equipment (2) of gas, second changing
Hot equipment (9), the 3rd heat transmission equipment (11), the 4th heat transmission equipment (15), the 5th heat transmission equipment (23)
With the 6th heat transmission equipment (26)；
Recycle compressor, including for by the recycle compressor (17) of circulating air supercharging.
In the preferred embodiment of present device, described first paragraph methanator (7),
Two-stage nitration methanator (21) and the 3rd section of methanator (29) are insulation fix bed first
Alkylation reactors.
Preferably, described device also includes drum (36), for providing boiler feedwater for heat transmission equipment
And accept the saturated vapor that heat transmission equipment produces, saturated vapor is delivered to heat transmission equipment simultaneously.Specifically
Ground, described drum (36) is used for being that the 3rd heat transmission equipment (11) provides the first boiler feedwater (37),
It is that the 5th heat transmission equipment (23) provides the second boiler feedwater (39), and accepts the 3rd heat transmission equipment (11)
The second saturated vapor that the first saturated vapor (38) produced and the 5th heat transmission equipment (23) produce
(40), the 3rd saturated vapor (41) is delivered to the second heat transmission equipment (9) simultaneously.
Preferably, described heat transmission equipment is selected from useless pot and steam superheater.
Preferably, described device also includes desulfurization reactor, for unstripped gas is carried out deep desulfuration.
Preferably, described device also includes deoxidation reactor, for unstripped gas is carried out degree of depth deoxidation.
Preferably, described device also includes gas-liquid separator, the condensed water in separating technology gas.
The invention provides a kind of with coal or gasification of biomass product for raw material production 94mol% in methane
The continuous processing flow process of above substitute natural gas and device.The technological process that the present invention provides is as follows:
It is divided into two strands after unstripped gas is preheated, after wherein first strand of unstripped gas mixes with circulating air, enters first paragraph
Methanator reacts and obtains first paragraph product gas；This first paragraph product edema caused by disorder of QI becomes two strands, the
First paragraph methanator is entered back into after one stock-traders' know-how recycle compressor supercharging；Second strand of unstripped gas and
After two bursts of first paragraph product gas mixing, entrance second segment methanator reacts and obtains second segment
Product gas, this second segment product gas enters the 3rd section of methanator and reacts；3rd section of product
Gas obtains product gas after gas-liquid separation.
If the product gas of the present invention still contains a small amount of carbon monoxide and carbon dioxide, can be by gas
Reaction obtains final products further.
Compared with prior art, present invention achieves after purified to coal or gasification of biomass product
Synthesis gas full methanation produces substitute natural gas, has technological process reasonable, possesses operability；
Capacity usage ratio is high, saves the energy, advantages of environment protection.
Accompanying drawing explanation
Hereinafter, describe embodiment of the present invention in detail in conjunction with accompanying drawing, wherein:
Fig. 1 is the process chart that the present invention produces a kind of embodiment of substitute natural gas method；
Fig. 2 is low temperature methanation process flow chart in tradition, for alternative with the production that the present invention provides
Natural gas method contrasts.
Detailed description of the invention
Below in conjunction with detailed description of the invention, the present invention is further described in detail, the enforcement be given
Example is only for illustrating the present invention rather than in order to limit the scope of the present invention.
The methanator used in embodiment can load a large amount of business-like methanation catalyst,
Such as the CRG catalyst series of Davy company, the MCR-2X catalyst of Topsoe company, south
G1-85 and the G1-86 catalyst etc. of chemistry.
Embodiment 1
The one side of being preferable to carry out of the production method of the substitute natural gas that the present embodiment provides for the present invention
Formula, the process chart of the present embodiment is as shown in Figure 1.
A) coal or biomass are met requirement through gasification unit, converter unit and clean unit
Unstripped gas, unstripped gas 1 is divided into first strand of raw material after the first heat transmission equipment 2 is warming up to 190～210 DEG C
4, second strand of unstripped gas 5 of gas；
B) by the circulating air 19 after first strand of unstripped gas 4 in step a), intensification and the first steam
51 are mixed to get the first gaseous mixture 6 that temperature is 280～300 DEG C, and the first gaseous mixture 6 is passed through first
Section methanator 7 reacts, obtains the first paragraph product gas 8 that temperature is 600～620 DEG C,
This first paragraph product gas 8 is cooled to 300～320 through the second heat transmission equipment 9 and the 3rd heat transmission equipment 11
First paragraph product gas 12 after DEG C being lowered the temperature；
C) the first paragraph product gas 12 after the cooling obtained by step b) is divided into circulating air 14 and second
Stock first paragraph product gas 13, the circulation after the 4th heat transmission equipment 15 is lowered the temperature of the described circulating air 14
Gas 16, the circulating air 18 after recycle compressor 17 supercharging obtains supercharging of the circulating air 16 after cooling,
Circulating air 18 after described supercharging through the 4th heat transmission equipment 15 be warming up to 250～270 DEG C heated up after
Circulating air 19；
D) 13, second strand of unstripped gas 5 of second strand of first paragraph product gas step c) obtained and
Two steam 52 are mixed to get the second gaseous mixture 20 that temperature is 290～300 DEG C, by the second gaseous mixture 20
It is passed through in second segment methanator 21 and reacts, obtain the second segment that temperature is 500～520 DEG C
Product gas 22, this second segment product gas 22 through the 5th heat transmission equipment the 23, first heat transmission equipment 2,
Six heat transmission equipments 26 are cooled to the second segment product gas 27 after 220～240 DEG C of coolings obtained；
E) second segment product gas 27 and the 3rd steam 53 after the cooling obtained by step d) mix
To the 3rd gaseous mixture 28 that temperature is 220-240 DEG C, the 3rd gaseous mixture 28 is passed through front three alkanisation anti-
Answer device 29 to react, obtain the three products gas 30 that temperature is 370～390 DEG C；
F) the three products gas 30 obtained by step e) is passed through gas after the 6th heat transmission equipment 26 cooling
Liquid/gas separator 32, obtains product gas 33 and process condensate 34 that temperature is 30～50 DEG C.Wherein,
The technique that utilizes of methanation reaction heat release includes: the preheated rear entrance of boiler feedwater 35 from battery limit (BL)
Drum 36, makes to enter the 3rd heat transmission equipment 11 from drum 36 first boiler feedwater 37 and produces
First saturated vapor 38 of 4.5～5.5MPa, the second boiler feedwater 39 from drum 36 enters
Five heat transmission equipments 23 produce second saturated vapor 40 of 4.5～5.5MPa, make from drum 36
Three saturated vapors 41 heat up through the second heat transmission equipment 9, obtain the superheated steam that temperature is 440～460 DEG C
42。
Wherein, first strand of unstripped gas 4 and volume ratio 1:0.12 of second strand of unstripped gas 5, circulating air
14 and the volume ratio of second strand of second segment product gas 12 be 1:0.33.
Below by way of the gas composition parameter of each logistics in table 1, intuitively describe shown in Fig. 1
In technological process, each workshop section's methanation reaction actually occurs situation.
Table 1
The explanation of logistics numbering: 1 is unstripped gas；6 is the first gaseous mixture；8 is first paragraph product gas；20 is the second gaseous mixture；
22 is second segment product gas；28 is the 3rd gaseous mixture；30 is the 3rd section of product gas；14 is circulating air；33 is product
Gas SNG；42 is superheated steam.
Embodiment 2
The one side of being preferable to carry out of the production method of the substitute natural gas that the present embodiment provides for the present invention
Formula, the process chart of the present embodiment is as shown in Figure 1.
A) coal or biomass are met requirement through gasification unit, converter unit and clean unit
Unstripped gas, unstripped gas 1 is divided into first strand of raw material after the first heat transmission equipment 2 is warming up to 220～240 DEG C
4, second strand of unstripped gas 5 of gas；
B) by the circulating air 19 after first strand of unstripped gas 4 in step a), intensification and the first steam
51 are mixed to get the first gaseous mixture 6 that temperature is 290～310 DEG C, and the first gaseous mixture 6 is passed through first
Section methanator 7 reacts, obtains the first paragraph product gas 8 that temperature is 590～610 DEG C,
This first paragraph product gas 8 is cooled to 340～360 through the second heat transmission equipment 9 and the 3rd heat transmission equipment 11
First paragraph product gas 12 after DEG C being lowered the temperature；
C) the first paragraph product gas 12 after the cooling obtained by step b) is divided into circulating air 14 and second
Stock first paragraph product gas 13, the circulation after the 4th heat transmission equipment 15 is lowered the temperature of the described circulating air 14
Gas 16, the circulating air 18 after recycle compressor 17 supercharging obtains supercharging of the circulating air 16 after cooling,
Circulating air 18 after described supercharging through the 4th heat transmission equipment 15 be warming up to 290～310 DEG C heated up after
Circulating air 19；
D) 13, second strand of unstripped gas 5 of second strand of first paragraph product gas step c) obtained and
Two steam 52 are mixed to get the second gaseous mixture 20 that temperature is 320～340 DEG C, by the second gaseous mixture 20
It is passed through in second segment methanator 21 and reacts, obtain the second segment that temperature is 560～580 DEG C
Product gas 22, this second segment product gas 22 through the 5th heat transmission equipment the 23, first heat transmission equipment 2,
Six heat transmission equipments 26 are cooled to the second segment product gas 27 after 230～250 DEG C of coolings obtained；
E) second segment product gas 27 and the 3rd steam 53 after the cooling obtained by step d) mix
To the 3rd gaseous mixture 28 that temperature is 230-250 DEG C, the 3rd gaseous mixture 28 is passed through front three alkanisation anti-
Answer device 29 to react, obtain the three products gas 30 that temperature is 390～410 DEG C；
F) the three products gas 30 obtained by step e) is passed through gas after the 6th heat transmission equipment 26 cooling
Liquid/gas separator 32, obtains product gas 33 and process condensate 34 that temperature is 30～50 DEG C.Wherein,
The technique that utilizes of methanation reaction heat release includes: the preheated rear entrance of boiler feedwater 35 from battery limit (BL)
Drum 36, makes to enter the 3rd heat transmission equipment 11 from drum 36 first boiler feedwater 37 and produces
First saturated vapor 38 of 5.5～6.5MPa, the second boiler feedwater 39 from drum 36 enters
Five heat transmission equipments 23 produce second saturated vapor 40 of 5.5～6.5MPa, make from drum 36
Three saturated vapors 41 heat up through the second heat transmission equipment 9, obtain the superheated steam that temperature is 490～510 DEG C
42。
Wherein, first strand of unstripped gas 4 and volume ratio 1:0.15 of second strand of unstripped gas 5, circulating air
14 and the volume ratio of second strand of second segment product gas 12 be 1:0.15.
Below by way of the gas composition parameter of each logistics in table 2, intuitively describe shown in Fig. 1
In technological process, each workshop section's methanation reaction actually occurs situation.
Table 2
The explanation of logistics numbering is with table 1.
Embodiment 3
The one side of being preferable to carry out of the production method of the substitute natural gas that the present embodiment provides for the present invention
Formula, the process chart of the present embodiment is as shown in Figure 1.
A) coal or biomass are met requirement through gasification unit, converter unit and clean unit
Unstripped gas, unstripped gas 1 is divided into first strand of raw material after the first heat transmission equipment 2 is warming up to 220～220 DEG C
4, second strand of unstripped gas 5 of gas；
B) by the circulating air 19 after first strand of unstripped gas 4 in step a), intensification and the first steam
51 are mixed to get the first gaseous mixture 6 that temperature is 290～310 DEG C, and the first gaseous mixture 6 is passed through first
Section methanator 7 reacts, obtains the first paragraph product gas 8 that temperature is 600～620 DEG C,
This first paragraph product gas 8 is cooled to 300～320 through the second heat transmission equipment 9 and the 3rd heat transmission equipment 11
First paragraph product gas 12 after DEG C being lowered the temperature；
C) the first paragraph product gas 12 after the cooling obtained by step b) is divided into circulating air 14 and second
Stock first paragraph product gas 13, the circulation after the 4th heat transmission equipment 15 is lowered the temperature of the described circulating air 14
Gas 16, the circulating air 18 after recycle compressor 17 supercharging obtains supercharging of the circulating air 16 after cooling,
Circulating air 18 after described supercharging through the 4th heat transmission equipment 15 be warming up to 250～370 DEG C heated up after
Circulating air 19；
D) 13, second strand of unstripped gas 5 of second strand of first paragraph product gas step c) obtained and
Two steam 52 are mixed to get the second gaseous mixture 20 that temperature is 290～310 DEG C, by the second gaseous mixture 20
It is passed through in second segment methanator 21 and reacts, obtain the second segment that temperature is 500～520 DEG C
Product gas 22, this second segment product gas 22 through the 5th heat transmission equipment the 23, first heat transmission equipment 2,
Six heat transmission equipments 26 are cooled to the second segment product gas 27 after 240～260 DEG C of coolings obtained；
E) second segment product gas 27 and the 3rd steam 53 after the cooling obtained by step d) mix
To the 3rd gaseous mixture 28 that temperature is 240-260 DEG C, the 3rd gaseous mixture 28 is passed through front three alkanisation anti-
Answer device 29 to react, obtain the three products gas 30 that temperature is 360～380 DEG C；
F) the three products gas 30 obtained by step e) is passed through gas after the 6th heat transmission equipment 26 cooling
Liquid/gas separator 32, obtains product gas 33 and process condensate 34 that temperature is 30～50 DEG C.Wherein,
The technique that utilizes of methanation reaction heat release includes: the preheated rear entrance of boiler feedwater 35 from battery limit (BL)
Drum 36, makes to enter the 3rd heat transmission equipment 11 from drum 36 first boiler feedwater 37 and produces
First saturated vapor 38 of 5.5～6.5MPa, the second boiler feedwater 39 from drum 36 enters
Five heat transmission equipments 23 produce second saturated vapor 40 of 5.5～6.5MPa, make from drum 36
Three saturated vapors 41 heat up through the second heat transmission equipment 9, obtain the superheated steam that temperature is 470～490 DEG C
42。
Wherein, first strand of unstripped gas 4 and volume ratio 1:0.11 of second strand of unstripped gas 5, circulating air
14 and the volume ratio of second strand of second segment product gas 12 be 1:0.30.
Below by way of the gas composition parameter of each logistics in table 3, intuitively describe shown in Fig. 1
In technological process, each workshop section's methanation reaction actually occurs situation.
Table 3
The explanation of logistics numbering is with table 1.
Comparative example 1
For contrasting with embodiment 1, under the conditions of identical design basis, use low temperature in tradition
Methanation technology produces substitute natural gas, and concrete technology flow chart is as shown in Figure 2.
A) coal or biomass are met requirement through gasification unit, converter unit and clean unit
Unstripped gas, unstripped gas 501 is heated up after the first heat transmission equipment 502 is warming up to 140～160 DEG C
After unstripped gas 503.Unstripped gas 503 after intensification is divided into two streams, it may be assumed that first strand of raw material
Gas 504 and second strand of unstripped gas 505.
B) being mixed with the circulating air 524 after intensification by first strand of unstripped gas 504, obtaining temperature is
First gaseous mixture 506 of 270～290 DEG C, is passed in first paragraph methanator 507 carrying out first
Alkylation reaction, obtains the first paragraph product gas 508 that temperature is 490～510 DEG C.First paragraph product gas 508
Lowering the temperature through the second heat transmission equipment 509 and the 3rd heat transmission equipment 511, obtaining temperature is 300～320 DEG C
Cooling after first paragraph product gas 512, by-product saturated vapor and superheated steam simultaneously.
C) the first paragraph product gas 512 after cooling is mixed with second strand of unstripped gas 505, obtain temperature
Degree is second gaseous mixture 513 of 270～290 DEG C, is passed in second segment methanator 514
Carry out methanation reaction, obtain the second segment product gas 515 that temperature is 490～510 DEG C.Second segment produces
Second segment after product gas 515 is lowered the temperature after the 4th heat transmission equipment 516 is cooled to 230～250 DEG C produces
Product gas 517.
D) the second segment product gas 517 after cooling is divided into two strands: first strand of second segment product gas 518
With second strand of second segment product gas 519.First strand of second segment product gas 518 is through the 5th heat transmission equipment 520
First strand of second segment product gas 521 after being lowered the temperature after being cooled to 30～50 DEG C.After cooling first
Stock second segment product gas 521 enters recycle compressor 522 supercharging, obtains circulating air 523, circulating air
523 heat up through the 5th heat transmission equipment 520, obtain the circulating air after the intensification that temperature is 190～210 DEG C
524。
E) the second strand of second segment product gas 519 obtained by step d) is passed through the 3rd section of methanation reaction
Device 525 carries out methanation reaction, obtains the 3rd section of product gas 526 that temperature is 290～310 DEG C.
3rd section of product gas 526 is lowered the temperature through the first heat transmission equipment 502 and passes through gas-liquid separator 528, obtains
Temperature is product gas 529 (SNG) and the process condensate 530 of 30～50 DEG C.
Wherein, the technique that utilizes of methanation reaction heat release includes: from boiler feedwater 531 warp of battery limit (BL)
Send into drum 532 after preheating, give from the first boiler feedwater 533 in drum 532 and the second boiler
Water 534 respectively enters the 3rd heat transmission equipment 511 by downspout and the 4th heat transmission equipment 517 produces
One saturated vapor 534 and the second saturated vapor 536, the first saturated vapor 534 and the second saturated vapor
536 enter drum 532 through riser, and the 3rd saturated vapor 537 that drum 532 produces is through second
Heat transmission equipment 509 heats up, and obtains the superheated steam 538 that temperature is 440～460 DEG C and sends battery limit (BL).
Wherein, the volume ratio of 504, second strand of unstripped gas 505 of first strand of unstripped gas is 1:1.30, the
The volume ratio of one second segment product gas 518 and second strand 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 shown in Fig. 3
In technological process, each workshop section's methanation reaction actually occurs situation.
Table 4
The explanation of logistics numbering: 501 is unstripped gas；506 is the first gaseous mixture；508 is first paragraph product gas；513 is
Two gaseous mixtures；515 is second segment product gas；519 is second strand of second segment product gas；526 is the 3rd section of product gas；
521 is circulating air；529 is product gas SNG；538 is superheated steam.
Compared with comparative example 1, under identical design basis, embodiment 1 is higher than heat utilization ratio,
Consume low: embodiment 1 by-product superheated steam 184.7t/h, comparative example 1 by-product superheated steam 158.6t/h,
The by-product superheated steam amount of embodiment 1 is higher than comparative example 1 by 16.5%.
Claims (9)
1. the method producing substitute natural gas, said method comprising the steps of:
A) unstripped gas (1) after the first heat transmission equipment (2) is warming up to 150～400 DEG C by volume
1:(0.1～5) it is divided into first burst of unstripped gas (4) and second burst of unstripped gas (5)；
B) by the circulating air (19) and first after first burst of unstripped gas (4) in step a), intensification
Steam (51) is mixed to get the first gaseous mixture (6) that temperature is 250～400 DEG C, by the first gaseous mixture
(6) being passed through in first paragraph methanator (7) and react, obtaining temperature is 450～750 DEG C
First paragraph product gas (8), this first paragraph product gas (8) is through the second heat transmission equipment (9) and the 3rd
Heat transmission equipment (11) be cooled to 250～400 DEG C lowered the temperature after first paragraph product gas (12)；
C) first paragraph product gas (12) 1:(0.1 by volume～5 after the cooling that step b) is obtained)
Being divided into circulating air (14) and second burst of first paragraph product gas (13), described circulating air (14) is through
Four heat transmission equipments (15) lowered the temperature after circulating air (16), circulating air (16) warp after cooling
Recycle compressor (17) supercharging obtains the circulating air (18) after supercharging, the circulating air after described supercharging
(18) through the 4th heat transmission equipment (15) be warming up to 150～380 DEG C heated up after circulating air (19)；
D) second burst of first paragraph product gas (13) step c) obtained, second burst of unstripped gas (5)
It is mixed to get the second gaseous mixture (20) that temperature is 250～400 DEG C, by second with the second steam (52)
Gaseous mixture (20) is passed through in second segment methanator (21) and reacts, and obtains temperature and is
Second segment product gas (22) of 450～650 DEG C, this second segment product gas (22) is through the 5th heat transmission equipment
(23), the first heat transmission equipment (2), the 6th heat transmission equipment (26) are cooled to 120～400 DEG C and obtain
Second segment product gas (27) after cooling；
E) second segment product gas (27) after the cooling that step d) is obtained and the 3rd steam (53)
It is mixed to get the 3rd gaseous mixture (28) that temperature is 120～400 DEG C, the 3rd gaseous mixture (28) is passed through
Front three alkylation reactors reacts in (29), obtains the three products that temperature is 300～450 DEG C
Gas (30)；
F) the three products gas (30) obtained by step e) is after the 6th heat transmission equipment (26) cooling
It is passed through gas-liquid separator (32), obtains product gas (33) and process condensate that temperature is 20～80 DEG C
(34)。
Method the most according to claim 1, wherein, the molar percentage composition of described unstripped gas
As follows: carbon monoxide 5～50%, carbon dioxide 0～30%, hydrogen 20～80%, methane 0～20%.
Method the most according to claim 1 and 2, in described step a), by described raw material
First burst of unstripped gas (4) and the volume ratio of second burst of unstripped gas (5) that gas (1) is divided into are 1:(0.1～1).
The most according to the method in any one of claims 1 to 3, by the first paragraph after described cooling
Product gas (12) is divided into the volume ratio of circulating air (14) and second burst of first paragraph product gas (13)
1:(0.1～1).
Method the most according to any one of claim 1 to 4, described method also include by with
Under type utilizes methanation reaction heat release: enter after making the boiler feedwater (35) from battery limit (BL) preheated
Drum (36), makes to enter the 3rd heat transmission equipment (11) from drum (36) first boiler feedwater (37)
Produce first saturated vapor (38) of 3～10MPa, from second boiler feedwater (39) of drum (36)
Enter the 5th heat transmission equipment (23) and produce second saturated vapor (40) of 3～10MPa, make from vapour
3rd saturated vapor (41) of bag (36) heats up through the second heat transmission equipment (9), and obtaining temperature is
The superheated steam (42) of 300～550 DEG C.
6. for the device of method according to any one of claim 1 to 5, comprising:
Methanator, including the first paragraph methanator (7) for carrying out methanation reaction,
Second segment methanator (21), the 3rd section of methanator (29)；
Heat transmission equipment, including for heating and/or cool down first heat transmission equipment (2) of gas, second changing
Hot equipment (9), the 3rd heat transmission equipment (11), the 4th heat transmission equipment (15), the 5th heat transmission equipment (23)
With the 6th heat transmission equipment (26)；
Recycle compressor, including for by the recycle compressor (17) of circulating air supercharging.
Device the most according to claim 6, wherein, described first paragraph methanator (7),
Second segment methanator (21) and the 3rd section of methanator (29) are insulation fix bed
Methanator.
8., according to the device described in claim 6 or 7, described device also includes drum (36),
For providing boiler feedwater for heat transmission equipment and accepting the saturated vapor that heat transmission equipment produces, simultaneously will be full
It is delivered to heat transmission equipment with steam.
9. according to the device according to any one of claim 6 to 8, wherein, described heat transmission equipment choosing
From useless pot and steam superheater；
Preferably, described device also includes desulfurization reactor, for unstripped gas is carried out deep desulfuration；
Preferably, described device also includes deoxidation reactor, for unstripped gas is carried out degree of depth deoxidation；
Preferably, described device also includes gas-liquid separator, the condensed water in separating technology gas.
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| CN101880559A (en) * | 2010-06-18 | 2010-11-10 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
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| CN101880559A (en) * | 2010-06-18 | 2010-11-10 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
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