CN103897758A - Equipment and method for producing synthesized gas with low H2/CO ratio - Google Patents

Equipment and method for producing synthesized gas with low H2/CO ratio Download PDF

Info

Publication number
CN103897758A
CN103897758A CN201310726935.3A CN201310726935A CN103897758A CN 103897758 A CN103897758 A CN 103897758A CN 201310726935 A CN201310726935 A CN 201310726935A CN 103897758 A CN103897758 A CN 103897758A
Authority
CN
China
Prior art keywords
sng
methane
building
gas
synthesizer
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN201310726935.3A
Other languages
Chinese (zh)
Inventor
白俊铉
刘永敦
姜锡焕
高东准
金晋号
金秀贤
柳在洪
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Research Portfolio Institute Of Advanced Technology
Research Institute of Industrial Science and Technology RIST
Original Assignee
Research Portfolio Institute Of Advanced Technology
Research Institute of Industrial Science and Technology RIST
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Research Portfolio Institute Of Advanced Technology, Research Institute of Industrial Science and Technology RIST filed Critical Research Portfolio Institute Of Advanced Technology
Publication of CN103897758A publication Critical patent/CN103897758A/en
Pending legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/08—Production of synthetic natural gas
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/323—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/04—Gasification
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/06—Heat exchange, direct or indirect
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/14—Injection, e.g. in a reactor or a fuel stream during fuel production
    • C10L2290/148—Injection, e.g. in a reactor or a fuel stream during fuel production of steam

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The present invention discloses a piece of equipment and method for producing synthesized gas with low H2/CO ratio. The invention provides the production of SNG equipment, including: the first synthesis of SNG device and the second SNG synthesis device, the H2 / CO concentration ratio of 0.60.95 synthesis gas. There is also provided a method for the production of SNG, including: the first SNG synthesis and SNG synthesis of second, H2 / CO concentration which is supplied to the first SNG synthesis gas in the synthetic process is 0.60.95. Synthesis gas supply will have low H2 / CO concentration ratio to the first SNG synthesis process, at the same time caused by water soluble phenoxy resin and methane synthesis reaction. Therefore, without water gas shift process additional. In addition, the first in the synthesis process of SNG supply steam, without processfor recirculation control reaction temperature, whichcan produce SNG with low cost.

Description

Use low H 2equipment and the method for the synthetic gas production synthetic natural gas of/CO ratio
CROSS-REFERENCE TO RELATED APPLICATIONS
The application requires the right of priority of No. 10-2012-0153905th, the korean patent application of submitting to Koran Office on December 26th, 2012, and it is incorporated by reference herein in full.
Background
The present invention relates to use low H 2equipment and the method for the synthetic gas production synthetic natural gas (SNG) of/CO concentration ratio.
Due within the scope of All Around The World, coal facies are enriched for other fuel source, and therefore, large quantity research has been carried out so that coal is changed into SNG in the whole world, a kind of cleaner fuel.
Can pass through gasification, control of dust process, scavenging process or CO 2removal process, from mainly being contained the synthetic gas of carbon monoxide and hydrogen such as coal or the biomass that contain a large amount of carbon.Then, can, by this type of synthetic gas is carried out to methane building-up process, obtain SNG.
The method of producing SNG from coal comprises direct method and indirect method, in direct method, by hydrogen or high-temperature steam are reacted and directly change into methane with coal, and in indirect method, produce synthetic gas by reacting between coal and oxygen, and change into SNG by methane building-up process.
It shown in Fig. 1, is the schematic diagram of a kind of typical indirect method in correlation technique.Can be by following process from coal 1(starting material) produce SNG12: by coal 1 being processed such as the process of gasification 4, control of dust process 6, water-gas conversion process 7, sour gas (sulfocompound) and co 2 removal process and methane building-up process, in described water-gas conversion process 7, control the concentration ratio of hydrogen and carbon monoxide.
[background technology file]
(patent document 1) korean patent application discloses No. 10-2004-0015790
(patent document 2) United States Patent (USP) discloses No. 2009/0173081
(patent document 3) United States Patent (USP) discloses No. 2009/0264542
Referring to Fig. 1, in gasification 4, coal 1 to be supplied with together with oxygen 2, organic substance contained in coal is converted to synthetic gas, removes constantly for example dust of inorganic substance and slag 3 simultaneously.After processing synthetic gas by thermal-arrest process 5 and control of dust process 6, in water-gas conversion process 7 by H in synthetic gas 2: the concentration ratio of CO is adjusted to 3:1, and removes sulfocompound and carbonic acid gas 10 from synthetic gas in sour gas and co 2 removal process 8.In methane building-up process 9, the concentration of hydrogen and carbon monoxide is more than or equal to 99% synthetic gas and changes into methane, and by dry and compression process 11, methane is processed to obtain SNG12.
In most of SNG processes of correlation technique, by water-gas conversion process by H 2the concentration ratio of/CO is adjusted to and is more than or equal to 3.0, and passes through Sour gas disposal process by most CO 2remove together with sulfocompound.Afterwards, synthetic gas is supplied to each methane synthesis reactor, to control the temperature of reaction of methane synthesis reactor, or a certain amount of gas of discharging from the first or second methane synthesis reactor is compressed and recirculation, to control the temperature of reaction of the first or second methane synthesis reactor.By this way, suppressed the inactivation of catalyzer.
But, if not to H 2the concentration ratio of/CO is controlled or the temperature of reactor is maintained at the temperature that is more than or equal to approximately 650 DEG C-700 DEG C, be generally in the SNG process of 20atm at tonnage, and nickel-containing catalyst meeting inactivation, thus possibly cannot produce the SNG of high density.
In addition,, because the cost of the compressor for recirculation using has accounted for tens of per-cents of the equipment total cost of SNG synthesis technique, need a kind of improved SNG synthetic method that does not adopt compressor in much technique.
General introduction
Aspects more of the present invention provide equipment and the method for the production of synthetic natural gas (SNG), and it will be by having low H 2the synthetic gas of/CO concentration ratio is supplied to reactor together with steam, to control the internal temperature of reactor, and increases the concentration of SNG without process recycling owing to there is water gas shift reaction and methane building-up reactions in reactor simultaneously.
According to an aspect of the present invention, comprise for the production of the equipment of SNG: a SNG synthesizer that contains methane synthesizing catalyst and the 2nd SNG synthesizer, a described SNG synthesizer is configured to receive steam and contains H 2, CO and CO 2synthetic gas, and discharge the methane-containing gas produced by methane building-up reactions; Described the 2nd SNG synthesizer is configured to receive methane-containing gas, and discharges the SNG producing by methane building-up reactions, wherein, and the H of synthetic gas 2/ CO concentration ratio is 0.6-0.95.
The one SNG synthesizer can comprise 2-4 reactor.
Can be by each reactor of steam supply to a SNG synthesizer.
Described equipment also can comprise heat exchanger, and it is configured to carry out heat exchange with the methane-containing gas of discharging from a SNG synthesizer, thereby produces steam.
According to another aspect of the present invention, comprise for the production of the method for SNG: carry out a SNG building-up process, wherein will be containing H 2, CO and CO 2synthetic gas supply with together with steam, to cause water gas shift reaction and methane building-up reactions simultaneously, and discharge methane-containing gas; And carry out the 2nd SNG building-up process, wherein supply with described methane-containing gas, for producing SNG and discharge SNG, the H of the synthetic gas of wherein supplying with in a SNG building-up process by methane building-up reactions 2/ CO concentration ratio is 0.6-0.95.
The one SNG building-up process can be carried out 2-4 time.
The steam of supplying with in a SNG building-up process and the volume ratio of carbon monoxide can be 2-5.
Can produce described steam by the heat exchanging process that utilizes the methane-containing gas of discharging in a SNG building-up process.
Can under the temperature of reaction of 300 DEG C-680 DEG C, carry out a SNG building-up process.
Can under the temperature of reaction of 250 DEG C-350 DEG C, carry out the 2nd SNG building-up process.
Brief description of the drawings
By reference to the accompanying drawings, can more clearly understand above and other of the present invention aspect, characteristic and other advantages by following detailed description, wherein:
It shown in Fig. 1, is the schematic flow sheet of a kind of typical indirect method in correlation technique;
It shown in Fig. 2, is the equipment schematic diagram for the production of synthetic natural gas (SNG) according to an exemplary embodiment of the present invention.
Fig. 3 is the schematic flow sheet of producing the method for SNG according to an exemplary embodiment of the present invention for explaining;
Shown in Fig. 4, be according to the volume ratio of steam and carbon monoxide, the temperature variation schematic diagram in a SNG synthesizer;
It shown in Fig. 5, is the schematic diagram of the conversion percentages of carbon monoxide in the SNG synthesizer in embodiment 3; And
It shown in Fig. 6, is the schematic diagram of the conversion percentages of carbon monoxide in the SNG synthesizer in embodiment 4.
Detailed Description Of The Invention
Below further describe illustrative embodiments of the present invention with reference to accompanying drawing.But the present invention can implement in many different modes, should not be interpreted to the embodiment being defined in this proposition.On the contrary, provide these embodiments to make to illustrate thorough and complete, can fully show scope of the present invention to those skilled in the art.
It shown in Fig. 2, is the equipment schematic diagram for the production of synthetic natural gas (SNG) according to an exemplary embodiment of the present invention; It shown in Fig. 3, is the method schematic diagram for the production of SNG according to an exemplary embodiment of the present invention.Below with reference to Fig. 2 and 3, embodiments of the present invention are described.
Provide the equipment of illustrative embodiments of the present invention to there is low H to adopt 2the synthetic gas 10 of/CO concentration ratio is produced SNG.Specifically, described equipment comprises: a SNG synthesizer that contains methane synthesizing catalyst and the 2nd SNG synthesizer 180, a described SNG synthesizer is configured to receive together steam 20 and contains H 2, CO and CO 2 synthetic gas 10, and discharge the methane-containing gas produced by methane building-up reactions; Described the 2nd SNG synthesizer 180 is configured to receive methane-containing gas, and discharges the SNG80 producing by methane building-up reactions, wherein, and the H of synthetic gas 10 2/ CO concentration ratio is 0.6-0.95.
Provide the method for illustrative embodiments of the present invention to there is low H to adopt 2the synthetic gas 10 of/CO concentration ratio is produced SNG.Specifically, described method comprises: carry out a SNG building-up process, and wherein will be containing H 2, CO and CO 2 synthetic gas 10 supply with together with steam 20, to cause water gas shift reaction and methane building-up reactions simultaneously, and discharge methane-containing gas; And carry out the 2nd SNG building-up process, wherein supply with described methane-containing gas, for producing SNG80 and discharge SNG80, the H of the synthetic gas 10 of wherein supplying with in a SNG building-up process by methane building-up reactions 2/ CO concentration ratio is 0.6-0.95.
Described equipment can comprise that a SNG synthesizer is to receive synthetic gas 10 synthesizing methane.Can produce synthetic gas 10 by coal vaporescence, described synthetic gas 10 is not owing to passing through water-gas conversion process, so it can have low H 2/ CO concentration ratio.For example, the H of synthetic gas 10 2/ CO concentration ratio can be in the scope of 0.6-0.95.But embodiments of the present invention are not limited to this.Therefore, if will there is low H 2the synthetic gas 10 of/CO concentration ratio is supplied to a SNG synthesizer, water gas shift reaction and methane building-up reactions can occur simultaneously as a SNG building-up process.Due to described water gas shift reaction and methane building-up reactions, can discharge methane-containing gas from a SNG synthesizer.
In addition, in a SNG building-up process, be supplied to the steam 20 of a SNG synthesizer and the volume ratio of carbon monoxide can the scope at 2-5 in.If steam 20 is less than 2 with the volume ratio of carbon monoxide,, along with coking can occur for water gas shift reaction and methane building-up reactions, this may cause methane synthesizing catalyst inactivation, and increases the pressure of reactor, thereby reduces the synthetic productive rate of methane.If steam 20 is greater than 5 with the volume ratio of carbon monoxide, excessive steam 20 can cause the competitive power of a SNG building-up process aspect economy to decline.
The one SNG synthesizer can comprise multiple SNG synthesis reactor that are connected in series.The quantity of reactor does not limit.For example, the quantity of reactor can be 2-4.Can connect extraly adiabatic reactor to increase selectivity and the productive rate of final methane production.
Steam 20 can be supplied to together with synthetic gas 10 to a SNG synthesizer.In the case, steam 20 can be supplied to each reactor of a SNG synthesizer.In correlation technique, the methane-containing gas of discharging from reactor is carried out to recirculation, to increase the synthetic productive rate of methane and to control temperature of reaction.But recirculation device is comparatively expensive.According to the embodiment of the present invention, control the temperature of reactor by supplying with steam 20 to each reactor, thereby can save for the required cost of recirculation device so that economy aspect is improved.Can produce described steam 20 by the heat exchanging process that utilizes the methane-containing gas of discharging from the reactor of a SNG synthesizer.For this reason, in the present embodiment, SNG production unit also can comprise heat exchanger 140, and its methane-containing gas that is configured to discharge with the reactor from a SNG synthesizer carries out heat exchange.
Can be by supplying with steam 20, by the temperature of reaction of a SNG synthesizer, the temperature of reaction of a SNG building-up process is adjusted in the scope of 300 DEG C-680 DEG C.But present embodiment is not limited to this.As shown in Figure 2, if a SNG synthesizer of SNG production unit comprises the first to the 3rd reactor 110,120 and 130(3 reactor), the first temperature of reaction to the 3rd reactor can be adjusted to respectively in the scope of 300 DEG C-680 DEG C, 300 DEG C-510 DEG C and 300 DEG C-365 DEG C.But present embodiment is not limited to this.If the temperature of reaction of the reactor of a SNG synthesizer drops on outside above-mentioned scope, methane synthesizing catalyst can stand coking or sintering, the inactivation and the reverse water gas shift reaction that cause catalyzer, as a result of, the conversion percentages that methane is synthetic and productive rate can decline.
Can process therefrom to remove water 90 and carbonic acid gas 100 to the methane-containing gas of discharging from a SNG synthesizer, afterwards methane-containing gas is supplied to the 2nd SNG synthesizer 180, thereby increase the synthetic productive rate of methane.Then, methane-containing gas can be compressed to the applicable pressure of supplying with via natural gas line.For this reason, the SNG production unit of present embodiment also can comprise condenser 150, co 2 removal device 160 and compressor 170.Described compressor 170 can be compressed to methane-containing gas the pressure of 50-70atm, then methane-containing gas can be supplied to the 2nd SNG synthesizer 180.But present embodiment is not limited to this.
Methane-containing gas can be supplied to the 2nd SNG synthesizer 180 to carry out the 2nd SNG building-up process, thereby produce SNG80 by methane building-up reactions.The methane concentration of SNG80 can be to be more than or equal to 95%.But present embodiment is not limited to this.In addition, condenser 150 can be removed the moisture the SNG80 discharging from the 2nd SNG synthesizer.
Embodiments of the invention will be described below.But, the invention is not restricted to these embodiment.
Embodiment 1
Use the SNG production unit of embodiments of the present invention to produce SNG.With 4,905Nm 3/ hour speed by H 2/ CO concentration ratio is the first reactor that 0.93 synthetic gas is supplied to a SNG synthesizer.Amount of substance and concentration in each device and reactor are shown in Table 1, and represent that with the Reference numeral of Fig. 2 material flows.
[table 1]
Figure BDA0000446459550000071
As shown in table 1, the methane concentration of the methane-containing gas of discharging from the reactor of a SNG synthesizer is respectively 14.00 % by mole, 27.54 % by mole and 34.1 % by mole, after removing water and carbonic acid gas and described methane-containing gas is compressed from methane-containing gas, the methane concentration of methane-containing gas is increased to 90.47 % by mole.Produce and the methane concentration of the final SNG that dewaters is 97.50 % by mole by the 2nd SNG synthesizer.That is to say, can use the SNG production unit production methane concentration of embodiments of the present invention to be more than or equal to 95% SNG.
Embodiment 2
At 20atm and 360 DEG C, use and comprise the synthetic gas (H that 2g nickel-containing catalyst (purchased from S-C company (Sud-Chemie)) and gas concentration lwevel are 22% 2/ CO concentration ratio=0.93) produce SNG.Synthetic gas is supplied to reactor, simultaneously reduces successively the volume ratio of steam and carbon monoxide in synthetic gas with 4.0,2.5 and 2.0, and measure the internal temperature of reactor.The temperature value recording as shown in Figure 4.
As shown in Figure 4, in the time that the steam of synthetic gas and the volume ratio of carbon monoxide are 2.0, the internal temperature of reactor maintains 360 DEG C.Under this condition, there is water gas shift reaction and methane building-up reactions, and because the internal temperature of reactor is maintained 360 DEG C by reaction heat.But because the volume ratio of steam and carbon monoxide is 2.0,, during water gas shift reaction and methane building-up reactions, catalyzer, due to coking inactivation, as a result of, has increased the internal pressure of reactor.Therefore, preferably the volume ratio of steam and carbon monoxide is greater than 2.0.In addition, if the H of synthetic gas 2/ CO concentration ratio is greater than 0.93, and steam declines with the ratio regular meeting of carbon monoxide.In Fig. 4, TC-1 to TC-5 refers to the temperature that the upper catalyst layer from reactor records to lower catalyst layer, measures and is spaced apart 20mm.
Embodiment 3
Under the condition identical with embodiment 2, produce SNG, difference is that the volume ratio of steam and carbon monoxide is 2.5, and air speed is maintained to 7,000ml/g catalyzer hour.Measure in a SNG synthesizer carbon monoxide to the conversion percentages of carbonic acid gas and methane, as shown in Figure 5.
As shown in Figure 5, continual and steady 42 hours of water gas shift reaction and methane building-up reactions.The conversion percentages of carbon monoxide is that the carbon monoxide of 100%:48.7% changes into carbonic acid gas, and 51.3% carbon monoxide changes into methane.
Embodiment 4
Under the condition identical with embodiment 2, produce SNG, difference is following condition: use 1g nickel-containing catalyst (purchased from S-C company); The volume ratio of steam and carbon monoxide is 2.5; And air speed is maintained to 32,500ml/g catalyzer hour.Measure in a SNG synthesizer carbon monoxide to the conversion percentages of carbonic acid gas and methane, as shown in Figure 6.
As shown in Figure 6, continual and steady 620 hours of water gas shift reaction and methane building-up reactions.The conversion percentages of carbon monoxide is that the carbon monoxide of 96.59%:48.24% changes into carbonic acid gas, and 48.35% carbon monoxide changes into methane.
As mentioned above, according to an illustrative embodiment of the invention, in the equipment and method for the production of SNG, will there is low H 2the synthetic gas of/CO concentration ratio is supplied in a SNG building-up process, to cause water-soluble phenoxy resin and methane building-up reactions simultaneously.Therefore, can be without carrying out extra water-gas conversion process.In addition, owing to having supplied with steam in a SNG building-up process, can be without the process recycling carrying out for controlling temperature of reaction, thus can be with low cost production SNG.
Although shown and described illustrative embodiments of the present invention, having it will be apparent for a person skilled in the art that the spirit and scope of the present invention in the case of not deviating from claims restriction and can carry out various amendments and change.

Claims (10)

1. for the production of an equipment of synthetic natural gas (SNG), this equipment comprises:
A SNG synthesizer that contains methane synthesizing catalyst, a described SNG synthesizer is configured to receive steam and contains H 2, CO and CO 2synthetic gas, and discharge the methane-containing gas produced by methane building-up reactions; And
The 2nd SNG synthesizer, described the 2nd SNG synthesizer is configured to receive methane-containing gas, and discharges the SNG producing by methane building-up reactions,
Wherein, the H of described synthetic gas 2/ CO concentration ratio is 0.6-0.95.
2. equipment as claimed in claim 1, is characterized in that, a described SNG synthesizer comprises 2-4 reactor.
3. equipment as claimed in claim 2, is characterized in that, by each reactor of steam supply to a SNG synthesizer.
4. equipment as claimed in claim 1, described equipment also comprises heat exchanger, it is configured to carry out heat exchange with the methane-containing gas of discharging from a SNG synthesizer, thereby produces steam.
5. a method of producing SNG, the method comprises:
Carry out a SNG building-up process, wherein will be containing H 2, CO and CO 2synthetic gas supply with together with steam, to cause water gas shift reaction and methane building-up reactions simultaneously, and discharge methane-containing gas; And
Carry out the 2nd SNG building-up process, wherein supply with described methane-containing gas, to produce SNG and to discharge SNG by methane building-up reactions,
The H of the synthetic gas of wherein supplying with in a SNG building-up process 2/ CO concentration ratio is 0.6-0.95.
6. method as claimed in claim 5, is characterized in that, a described SNG building-up process is carried out 2-4 time.
7. method as claimed in claim 5, is characterized in that, the steam of supplying with in a SNG building-up process and the volume ratio of carbon monoxide are 2-5.
8. method as claimed in claim 5, is characterized in that, produces described steam by the heat exchanging process that utilizes the methane-containing gas of discharging in a SNG building-up process.
9. method as claimed in claim 5, is characterized in that, carries out a described SNG building-up process under the temperature of reaction of 300 DEG C-680 DEG C.
10. method as claimed in claim 5, is characterized in that, carries out described the 2nd SNG building-up process under the temperature of reaction of 250 DEG C-350 DEG C.
CN201310726935.3A 2012-12-26 2013-12-25 Equipment and method for producing synthesized gas with low H2/CO ratio Pending CN103897758A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
KR10-2012-0153905 2012-12-26
KR1020120153905A KR101429973B1 (en) 2012-12-26 2012-12-26 Apparatus and method for producing synthetic natural gas using synthesis gas of low H2/CO ratio

Publications (1)

Publication Number Publication Date
CN103897758A true CN103897758A (en) 2014-07-02

Family

ID=50989341

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201310726935.3A Pending CN103897758A (en) 2012-12-26 2013-12-25 Equipment and method for producing synthesized gas with low H2/CO ratio

Country Status (3)

Country Link
KR (1) KR101429973B1 (en)
CN (1) CN103897758A (en)
AU (1) AU2013270551B2 (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105112111A (en) * 2015-09-24 2015-12-02 中国石化工程建设有限公司 Integration process and equipment for loop-free methanation of coal-based syngas to prepare natural gas
CN105385478A (en) * 2015-12-08 2016-03-09 大唐国际化工技术研究院有限公司 Method and apparatus for producing synthetic natural gas
CN107445785A (en) * 2016-11-29 2017-12-08 中国神华能源股份有限公司 The synthetic method and synthesis system of methane

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104357117A (en) * 2014-10-31 2015-02-18 西南化工研究设计院有限公司 Non-circulating methanation process of coal-based synthetic natural gas and liquefied natural gas
KR101628661B1 (en) * 2014-12-10 2016-06-10 재단법인 포항산업과학연구원 Apparatus and method for producing synthetic natural gas
KR101660472B1 (en) * 2015-05-11 2016-09-27 고려대학교 산학협력단 Method of Synthetic Natural Gas Production Using Sorption-enhanced Methanation
KR20170029274A (en) 2015-09-07 2017-03-15 고등기술연구원연구조합 Method for producing synthetic natural gas using the dump power and carbon dioxide
US20220127538A1 (en) * 2019-01-31 2022-04-28 Korea Research Institute Of Chemical Technology Carbon dioxide conversion process and system therefor
KR102230155B1 (en) * 2019-01-31 2021-03-22 한국화학연구원 Process for Carbon Dioxide Conversion and System Thereof
KR102397182B1 (en) * 2020-05-26 2022-05-12 고등기술연구원연구조합 Apparatus for producing higher calorific synthetic natural gas using synthetic gas of low hydrogen concentration

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3904386A (en) * 1973-10-26 1975-09-09 Us Interior Combined shift and methanation reaction process for the gasification of carbonaceous materials
US3938968A (en) * 1972-09-08 1976-02-17 The Ralph M. Parsons Company Process for the production of substitute natural gas
US4017274A (en) * 1974-07-30 1977-04-12 Bechtel Associates Professional Corporation Process for the methanation of gases containing high concentration of carbon monoxide
GB2060686A (en) * 1979-10-22 1981-05-07 Conoco Inc Concurrent shift-methanation process
CN1957076A (en) * 2004-04-06 2007-05-02 燃料电池能有限公司 Methanation device using multiple reactors
CN101560423A (en) * 2008-04-16 2009-10-21 卡萨尔甲醇公司 Process and plant for substitute natural gas
CN101851537A (en) * 2010-06-21 2010-10-06 上海浦景化工技术有限公司 Method and device for preparing synthetic natural gas
KR20120075312A (en) * 2010-12-28 2012-07-06 주식회사 포스코 Synthetic natural gas production process

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8182771B2 (en) * 2009-04-22 2012-05-22 General Electric Company Method and apparatus for substitute natural gas generation

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3938968A (en) * 1972-09-08 1976-02-17 The Ralph M. Parsons Company Process for the production of substitute natural gas
US3904386A (en) * 1973-10-26 1975-09-09 Us Interior Combined shift and methanation reaction process for the gasification of carbonaceous materials
US4017274A (en) * 1974-07-30 1977-04-12 Bechtel Associates Professional Corporation Process for the methanation of gases containing high concentration of carbon monoxide
GB2060686A (en) * 1979-10-22 1981-05-07 Conoco Inc Concurrent shift-methanation process
CN1957076A (en) * 2004-04-06 2007-05-02 燃料电池能有限公司 Methanation device using multiple reactors
CN101560423A (en) * 2008-04-16 2009-10-21 卡萨尔甲醇公司 Process and plant for substitute natural gas
CN101851537A (en) * 2010-06-21 2010-10-06 上海浦景化工技术有限公司 Method and device for preparing synthetic natural gas
KR20120075312A (en) * 2010-12-28 2012-07-06 주식회사 포스코 Synthetic natural gas production process

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105112111A (en) * 2015-09-24 2015-12-02 中国石化工程建设有限公司 Integration process and equipment for loop-free methanation of coal-based syngas to prepare natural gas
CN105385478A (en) * 2015-12-08 2016-03-09 大唐国际化工技术研究院有限公司 Method and apparatus for producing synthetic natural gas
CN107445785A (en) * 2016-11-29 2017-12-08 中国神华能源股份有限公司 The synthetic method and synthesis system of methane

Also Published As

Publication number Publication date
AU2013270551A1 (en) 2014-07-10
AU2013270551B2 (en) 2015-12-17
KR101429973B1 (en) 2014-08-18
KR20140085671A (en) 2014-07-08

Similar Documents

Publication Publication Date Title
CN103897758A (en) Equipment and method for producing synthesized gas with low H2/CO ratio
US8470059B2 (en) Process for producing a methane-rich gas
CN105308154B (en) Sour gas disposal in liquid fuel production method
CN101830775B (en) Co-production of methanol and ammonia
JP5052703B2 (en) Ethanol production method
CN100526273C (en) Method for integral production of liquid ammonia and methanol and/or dimethyl ether by using coke oven gas as raw material
CN102782161A (en) Blast furnace operation method, iron mill operation method, and method for utilizing a gas containing carbon oxides
WO2014000503A1 (en) Method for preparing liquid hydrocarbon product from biomass-produced synthetic gas
CN102585951A (en) Novel process for co-production of liquefied synthesis gas, pure hydrogen and methanol from coke-oven gas
CN104937078A (en) Hybrid plant for liquid fuel production and method for operating it where a gasification unit in the hybrid plant is operating at less than its design capacity or is not operational
GB2039518A (en) A process and a plant for preparing a gas rich in methane
JP4030846B2 (en) Methanol production method and apparatus
CN102746870B (en) FT synthesis technology
CN102732317A (en) Technological process for preparing synthetic gas by using biomass
CN100404409C (en) Process for preparing synthetic gas by reforming carbon dioxide-methane
CN100596293C (en) Stage associating process for producing methanol and ammonia using coal and coke oven gas as material
CN110015939B (en) Method and device for producing hydrogen and co-producing methane by coal
CN110002954A (en) A kind of coal gasification couples the process and device of coking of coal methanol with joint production acid or ester
KR101628661B1 (en) Apparatus and method for producing synthetic natural gas
CN109810739B (en) Sulfur-tolerant methane synthesis process and device
CN215667848U (en) Device and system for preparing fuel and chemicals through coal gasification
EP4332200A1 (en) Synthetic fuel production method
CN105347302A (en) Method for producing synthesis gas by converting natural gas
CN104087348A (en) Gas supply method for supplying gases for formic acid, methanol and synthetic ammonia production techniques by utilizing coal water slurry gasification furnace
JPS5857473B2 (en) Method for producing methane-rich gas that can be substituted for natural gas

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
RJ01 Rejection of invention patent application after publication
RJ01 Rejection of invention patent application after publication

Application publication date: 20140702